NYCDEPCostAnalys isReport-0607 .pdf - New York-New Jersey ...

Executive Summary 

At the request of the New York City Department of Environmental Protection (NYCDEP) the 

Advanced Wastewater Treatment Programmatic Assistance Team (AWT Team) has developed 

conceptual designs, cost estimates and treatment projections for ten levels of treatment at four of 

the City’s Water Pollution Control Plants (WPCPs): Port Richmond, Red Hook, North River, and 

Owls Head. This work was prepared in response to the Nutrient Workgroup of the New York- 

New Jersey Harbor Estuary Plan (HEP), which has expressed an intent to promulgate a Total 

Maximum Daily Load (TMDL) for nitrogen and carbon by December 31, 2008 for sections of 

New York Harbor. Detailed water quality modeling is underway that will specify the limiting 

nutrient – carbon, nitrogen, or a combination of the two – and the key zones of the harbor in need 

of load reduction. The nutrient workgroup has stated that it will consider the associated costs of 

advanced treatment alternatives in combination with their projected water quality benefit. 

The year 2045 was selected as the design horizon for this project, and a set of projected flows 

and loads were developed and agreed upon for this effort. Conceptual design reports and 

drawing sets were prepared at each of the facilities selected for in-depth analysis. Projected 

annual average effluent concentrations were developed from BioWin process modeling and fullscale 

experience. Capital cost estimates were prepared from these conceptual design reports, 

drawing sets, and a set of contingencies and escalation factors were applied appropriate for the 

New York City marketplace. 

The Team’s conceptual capital cost curves are presented in this executive summary. These cost 

curves include conceptual costs developed on behalf of HEP. Where available, these conceptual 

cost curves were supplemented with known construction costs (escalated to 2007 dollars) for 

Advanced Basic BNR and Full Step BNR technologies currently under construction at Upper 

East River WPCPs. These conceptual capital cost estimates do not include the cost of land 

acquisition, which are unknown at this time. Land acquisition is likely to be a major cost driver 

for advanced technologies at space-constrained plants such as North River, Owls Head, and to a 

lesser extend Red Hook. 

This submittal intends to fulfill the HEP Nutrient Workgroup’s request for draft cost information. 

Objectives for the final submittal in November 2007 include providing operation and 

maintenance (O&M) cost curves as well as capital costs, and refining this report based on the 

feedback provided by NYCDEP and HEP. 

Background 

Low levels of dissolved oxygen (DO) have been observed in various locations throughout the 

New York-New Jersey Harbor Estuary in numerous water quality sampling studies. Water 

quality modeling shows that low levels of dissolved oxygen will continue to persist in future 

conditions. This water quality modeling work has shown that both nitrogen and carbon 

discharges have an impact on harborwide water quality issues. The degree to which these two 

constituents influence DO levels under varying conditions is an additional variable at play. HEP 

is developing management zones for locations throughout the Harbor, similar in nature to the 

Long Island Sound Study (LISS) management zones, of which, the Upper and Lower East River 

are a part. In the long term, these management zones may be used to establish Total Maximum 

___________________________________________________________________________________________________________ 

EX-1

Daily Loads (TMDLs) for New York Harbor, which would impact Water Pollution Control 

Plants (WPCPs) in New York and New Jersey as well as nonpoint sources of discharge. 

HydroQual has been tasked with the System Wide Eutrophication Modeling (SWEM) to 

determine critical management zones that impact Harbor water quality, and within those key 

management zones, determining which nutrient is the critical resource. This focusing of HEP on 

key WPCPs and nutrients is anticipated to be completed in the next 6-8 months. 

Key unknowns at this time are: 

• HEP has not clarified which New York City WPCPs (if any) will be targeted for nutrient 

removal enhancements. If water quality modeling has progressed to the point where HEP 

could narrow NYCDEP’s efforts, this would allow the Team to focus its limited resources on 

the plants most likely targeted for upgrades. 

• What set of water quality standards will be used to assess compliance scenarios? 

• Does HEP intend to promulgate an annual average TMDL, such as the Total Nitrogen TMDL 

under the Long Island Sound Study? Or does HEP intend to promulgate a limit based on a 

different timeperiod, such as a maximum monthly average or an instantaneous maximum? 

Approach 

Upon project approval, the Team acquired the necessary documentation and materials for the 

development of the project. Information included design drawings, site plans, historical data, 

and information about future upgrades. The Team also visited plant sites in order to discuss 

process control and operation to gain a better understanding of potential plant limitations to 

achieve higher levels of treatment. 

The Team utilized the most recent projections for wastewater flows for WPCPs in the calculation 

of projected influent loadings to each plant for the year 2045, which is the design and modeling 

milestone for project work. These flow projections are based on historical wastewater data in 

conjunction with available population and employment projections for each WPCP service area. 

The Team evaluated potential industrial contributions in drainage areas that have a significant 

industrial component. 

A set of project-wide global assumptions was established for this effort. In addition to project 

flows and loads, an N+1 level of redundancy was chosen for process infrastructure (tanks, 

filtration units, etc) and an N+1+1 level of redundancy was chosen for process equipment 

(pumps, blowers, etc). From a hydraulic standpoint, all unit processes were designed for 1.5 

times the WPCP’s design dry weather flow (DDWF) capacity; the preservation of the secondary 

bypass channel is assumed within this work. 

The conceptual design reports for Port Richmond, Red Hook, North River, and Owls Head 

follow this executive summary. 

Selection of Technologies 

The following ten levels of treatment were chosen for this project. The first two levels of 

treatment are presented to provide context for a potential ‘knee-of-the-curve’ analysis, followed 

by eight levels of technology that remove nitrogen and/or carbon to varying degrees. The first 

___________________________________________________________________________________________________________ 

EX-2

two options are defined for process modeling purposes, as New York City WPCPs currently 

exceed base secondary treatment standards. These levels do enter our costing analysis. 

• Base Case – The base case is developed using the design dry weather flow rate (DDWF) and 

the projected 2045 wastewater characteristics. A TN removal of 35 percent and an effluent 

CBOD of 25 mg/L and TSS of 30 mg/L are assumed. Removals of 85 percent for CBOD 

and TSS were applied when this condition proven to be stricter. These characteristics are 

consistent with SPDES permit requirements. 

• Existing Conditions – Based on the plant flow and effluent quality for Fiscal Years 2003 to 

2005, this level assumes the current plant performance observed will continue. 

• Existing Conditions with Solids Filtration – Equivalent to the previous level of technology 

plus filtration. The Filtration design level utilizes deep bed filters provided at the end of the 

secondary process train to reduce the particulate fraction of the secondary effluent discharged 

under the existing conditions. This technology preserves the existing secondary treatment 

infrastructure, but designs the additional unit process based on the plant-specific 2045 flows 

and loads. (carbon only) 

• Existing Conditions with Microfiltration/Ultrafiltration – The 

Microfiltration/Ultrafiltration design level further reduces the particulate fraction of the 

secondary effluent from the existing conditions through the implementation of membrane 

technology. This technology preserves the existing secondary treatment infrastructure, but 

designs the additional unit process based on the plant-specific 2045 flows and loads. (carbon 

only) 

• Advanced Basic BNR – Based on the original AWT design guidance, the Advanced Basic 

BNR design will provide enhancements to the current step feed operation for increased BNR 

performance at the facilities. This level of treatment is currently under construction at the 

Bowery Bay, Wards Island, and Tallman Island WPCPs to meet Long Island Sound Total 

Nitrogen goals. (nitrogen only) 

• Full Step BNR – This treatment level provides the Advanced Basic BNR level with 

additional flexibility, and incorporates supplemental carbon addition to enhance 

denitrification. This level of treatment is currently under construction at the Hunts Point 

WPCP to meet Long Island Sound Total Nitrogen goals. (nitrogen only) 

• Full Step BNR with Solids Filtration – Equivalent to the previous level of technology, the 

Filtration design level would utilize deep bed filters at the end of the process train to reduce 

the particulate fraction of the secondary effluent discharge. (carbon and nitrogen) 

• Full Step BNR with Microfiltration/Ultrafiltration – The Microfiltration/Ultrafiltration 

design level further reduces the particulate fraction of the secondary effluent through the 

implementation of membrane technology. (carbon and nitrogen) 

___________________________________________________________________________________________________________ 

EX-3

• Full Step BNR with Denitrification Filters – Denitrification filters provided at the end of 

secondary process train will remove additional particulates and nutrients from the secondary 

effluent. (carbon and nitrogen) 

• Membrane Bioreactor Tanks – Provides the greatest improvement in effluent quality, but 

will require different technology than the standard step-feed BNR configurations with the 

installation of Membrane Bioreactors. (carbon and nitrogen) 

Effluent Projections 

Table EX-1 provides the estimated annual average effluent quality for each level of treatment 

for all 14 New York City WPCPs. Table EX-1 pulls from several analyses, including this 

conceptual design conducted at Port Richmond, Red Hook, North River, and Owls Head, BioWin 

analysis conducted at the Jamaica Bay WPCPs (26 th Ward, Coney Island, Jamaica, and 

Rockaway), and a BioWin analysis conducted at the Upper East River WPCPs (Bowery Bay, 

Hunts Point, Tallman Island, and Wards Island). 

Cost Estimation 

Conceptual cost estimates were developed for each of the eight new technologies at the four 

WPCPs included in this study. Table EX-2 highlights key costing assumptions and 

contingencies. Each of these assumptions is based on best available information culled from 

recent competitive bids on major NYCDEP capital construction projects. The detailed 

conceptual cost estimates provided in this report include major unit process improvements and 

the ancillary equipment needed to support them. Detailed plant-specific designs are beyond the 

scope of this conceptual study, and the project design contingency was selected to account for 

these costs. A higher design contingency was selected for the membrane bioreactor level of 

technology, as this technology has not yet been implemented at plants as big as the North River 

WPCP. This higher contingency reflects greater uncertainty as well as unanticipated scale-up 

issues for this limit of technology alternative. 

___________________________________________________________________________________________________________ 

EX-4

WPCP 

26th 

Ward 

Bowery 

Bay 

Coney 

Island 

Hunts 

Point 

Jamaica 

Newtown 

Creek 

North 

River 

Oakwood 

Beach 

Nutrient 

Base 

Case* 

Flow (mgd) 85 

Carbon (mg/L)

WPCP 

Owls 

Head 

Port 

Richmond 

Red Hook 

Rockaway 

Tallman 

Island 

Nutrient 

Base 

Case* 

Flow (mgd) 120 

Carbon (mg/L)

Table EX-2: Key Cost Assumptions 

Annual Cost Escalation 8.5% 

Assumed Construction Start Date 2020 

Cost Basis 

June 2007 Dollars 

Land Acquisition Costs 

Not included 

4 Years for ABBNR 

Construction Duration 

5 Years for FSBNR 

8 Years for all other technologies 

Contractor Overhead and Profit 21% 

Design Contingency 

60% for MBR 

40% for all other technologies 

Bond and Insurance 6% 

Construction Allowances and Unit Price Items 6% 

Table EX-3 provides capital construction cost estimates for each technology at each WPCP in 

this study. These figures exclude the cost of land acquisition at space constrained facilities, 

which would be major cost drivers at the North River and Owls Head WPCPs. Detailed cost 

estimates follow the conceptual design reports in this deliverable. 

Table EX-3: Estimated Capital Construction Costs (Escalated to the Midpoint of 

Construction) 

North River Owls Head Red Hook Port Richmond 

Solids Filtration $587 $485 $307 $274 

Microfiltration/ 

Ultrafiltration 

$813 $650 $379 $374 

Advanced Basic 

BNR 

$434 $257 $225 $216 

Full Step BNR $499 $319 $296 $270 

Full Step BNR with 

Solids Filtration 

$1,334 $931 $632 $501 


Denitrification 

$1,501 $1,051 $682 $578 


Microfiltration/ $1,568 $1,096 $704 $601 


Membrane 

Bioreactor 

$3,210 $2,345 $1,572 $1,398 

Technology Cost Curves 

Figures EX-1 through EX-8 provide cost curves for capital construction costs for each level of 

technology included in this study. Previous work conducted at several New York City WPCPs 

that yielded costs for various treatment and technology levels were included in some of the cost 

curves, including an analysis examining the impact of BNR upgrades at the four Upper East 

River WPCPs (Bowery Bay, Hunts Point, Tallman Island, and Wards Island). 

___________________________________________________________________________________________________________ 

EX-7

Plant sizes are in millions of gallons per day and costs are in millions of 2007 dollars with the 

impact of escalation excluded. Actual construction costs for Advanced Basic BNR and Full Step 

BNR from the New York City Nitrogen program are also included. 

Figure EX-1: Solids Filtration 

$160 

$140 

y = 4.283x 0.6919 

R 2 = 0.9801 

North River 

$120 

Owl's Head 

Cost (Millions 2007 Dollars) 

$100 

$80 

$60 

Red Hook 

Port Richmond 

$40 

$20 

$0 

0 20 40 60 80 100 120 140 160 180 

Plant Size (MGD) 

The best fit cost curve is y= $4.283x 0.6919 ; this has an R 2 correlation of 0.9801. Note this 

equation estimates the capital construction cost (in millions of 2007 dollars) excluding the 

impact of escalation. Escalated cost is a more accurate representation of future project costs. 

This curve is statistically valid over a range of 60-170 mgd. 

___________________________________________________________________________________________________________ 

EX-8

Figure EX-2: Microfiltration/Ultrafiltration 

$250 

Capital Construction Cost (Millions 2007 Dollars) 

$200 

$150 

$100 

$50 

Red Hook 

Port Richmond 

Owl's Head 

y = 4.3975x 0.7491 

R 2 = 0.9981 

North River 

$0 

0 20 40 60 80 100 120 140 160 180 






___________________________________________________________________________________________________________ 

EX-9

Figure EX-3: Advanced Basic BNR 

$250 

Capital Construction Cost (Millions 2007 dollars) 

$200 

$150 

$100 

$50 

Red Hook 

Port Richmond 

Tallman Island 

Owl's Head 

Bowery Bay 

North River 

y = 4.9287x 0.6463 

R 2 = 0.6947 

Wards Island 

$0 

0 50 100 150 200 250 300 






___________________________________________________________________________________________________________ 

EX-10

Figure EX-4: Full Step BNR 

$350 


$300 

$250 

$200 

$150 

$100 

$50 

Red Hook 

Port Richmond 

Owl's Head 

y = 1.9455x 0.8731 

R 2 = 0.7014 

North River 

Hunts Point 

$0 

0 50 100 150 200 250 






___________________________________________________________________________________________________________ 

EX-11

Figure EX-5: Full Step BNR with Solids Filtration 

$400 


$350 

$300 

$250 

$200 

$150 

$100 

$50 

Red Hook 

Port Richmond 

Owl's Head 

y = 5.1246x 0.8068 

R 2 = 0.9454 

North River 

$0 

0 20 40 60 80 100 120 140 160 180 






___________________________________________________________________________________________________________ 

EX-12

Figure EX-6: Full Step BNR with Denitrification Filtration 

$400 


$350 

$300 

$250 

$200 

$150 

$100 

$50 

Red Hook 

Port Richmond 

Owl's Head 

y = 5.4967x 0.8166 

R 2 = 0.9704 

North River 

$0 

0 20 40 60 80 100 120 140 160 180 






___________________________________________________________________________________________________________ 

EX-13

Figure EX-7: Full Step BNR with Microfiltration/Ultrafiltration 

$450 


$400 

$350 

$300 

$250 

$200 

$150 

$100 

$50 

Red Hook 

Port Richmond 

y = 5.5231x 0.8243 

Owl's Head 

R 2 = 0.9731 

North River 

$0 

0 20 40 60 80 100 120 140 160 180 






___________________________________________________________________________________________________________ 

EX-14

Figure EX-8: Membrane Bioreactor 

$900 

North River 

$800 

y = 19.027x 0.7236 


$700 

$600 

$500 

$400 

$300 

$200 

Red Hook 

Port Richmond 

R 2 = 0.9794 

Owl's Head 

$100 

$0 

0 20 40 60 80 100 120 140 160 180 






Next Steps 

The Team will augment this deliverable for the HEP Nutrient Workgroup’s final deliverable 

deadline of November 2007. Goals for the Team’s work include: 

• Developing O&M cost estimates in addition to capital cost estimates 

• Verifying the adequacy of the various conceptual capital construction cost curves, 

particularly for carbon technologies where only four New York City data points are 

available. 

• Expanding the predictive range of each cost curve. 

• Conducting an independent review of cost estimates. 

• Incorporating NYCDEP and HEP feedback, and revising and resubmitting this work Fall 

2007. 

___________________________________________________________________________________________________________ 

EX-15

1 INTRODUCTION 

At times the water quality of the New York-New Jersey Harbor estuary falls below water quality 

standards. Since the estuary was accepted into the National Estuary Program in 1988, water 

quality issues have been a major focus for improvement. The Harbor Estuary Program (HEP), a 

joint effort between New York, New Jersey and the United States Environmental Protection 

Agency (USEPA), evaluated these water quality concerns and prepared a Comprehensive 

Conservation and Management Plan (CCMP). Within the CCMP, significant problems have 

been identified and include: 

• Habitat loss and degradation (such as loss of wetlands) 

• Toxic contamination (including metals and pesticides) 

• Pathogen contamination 

• Floatable debris (originating from improper trash disposal and decay of shoreline structures) 

• Nutrient and organic enrichment (including increased carbon loadings and increased nitrogen 

loadings resulting in reduced dissolved oxygen levels) 

The goals of the New York/New Jersey Harbor Estuary Program are to bring the Harbor waters 

into compliance with the Clean Water Act. The various areas focused on in this conceptual 

design include: 

• Meeting the Fishable/Swimable goal of the Clean Water Act 

• Meeting the Fishable/Swimable goal for Toxics 

• Attaining a Fishable/Swimable status in terms of nutrients and Oxygen levels 

• Making Harbor waters free from floatable debris 

• Preserving, managing, and enhancing the Estuary’s vital habitat, ecological function, and 

biodiversity so that the Harbor is a system of diverse natural communities 

• Ensuring that all residents in the core area of the Harbor have a public waterfront access site 

within thirty minutes of their home for boating, fishing, swimming and/or waterfront leisure 

(e.g. walking, bird watching, and picnicking), without harming important habitat areas 

• Reducing sediment hot spots, and point and non-point sources of contaminants entering the 

Harbor, such that levels of toxics in newly deposited sediments do not inhibit a healthy 

thriving ecosystem and can be dredged and beneficially reused 

HEP is developing a plan to improve water quality and is evaluating the impact of wastewater 

treatment improvements on receiving waters. The cost for different levels of treatment will be 

considered during the development of the plan. The New York City Department of 

Environmental Protection (NYCDEP) is independently developing conceptual designs and cost 

estimates for nitrogen and carbon removal technologies at several Water Pollution Control Plants 

(WPCPs) that discharge to the Harbor. The conceptual designs will cover several levels of 

technology, including Existing Conditions with Solids Filtration, Existing Conditions with 

Microfiltration/Ultrafiltration, Advanced Basic BNR Treatment, Full Step BNR Treatment, Full 

Step BNR Treatment with Solids Filtration, Full Step BNR Treatment with 

Microfiltration/Ultrafiltration, Full Step BNR Treatment with Denitrification Filters, and 

Membrane Bioreactors. This report describes the existing conditions at the Port Richmond 

WPCP and the potential upgrades that can be implemented for each level of technology.

This report includes four conceptual design reports prepared by the NYCDEP as requested by the 

HEP nutrient workgroup. To date, the NYCDEP has prepared conceptual design reports for the 

Red Hook, Port Richmond, North River, and Owls Head WPCPs in support of the HEP analysis. 

1.1 Treatment Technologies 

As part of the Harbor Estuary Program, the Advanced Wastewater Treatment Program 

Assistance (AWTPA) Team will develop conceptual designs for nitrogen and carbon removal 

technologies at the four WPCPs. Ten levels of treatment were identified as well as 

corresponding sets of secondary effluent characteristics that should be achieved at each level. 

The ten levels identified are described in detail below and are listed here: 

• Base Case 

• Existing Conditions 

• Existing Conditions with Solids Filtration 

• Existing Conditions with Microfiltration/Ultrafiltration 

• Advanced Basic BNR 

• Full Step BNR 

• Full Step BNR with Solids Filtration 

• Full Step BNR with Microfiltration/Ultrafiltration 

• Full Step BNR with Denitrification Filters 

• Membrane Bioreactor Tanks 

It should be emphasized that possible changes in wastewater quality and quantity between now 

and 2045 could heavily influence technology selection and may result in additional technologies 

being considered in the future. In addition, this analysis is based on evaluating current “state-ofthe-art” 

treatment technologies. The evolution of current technologies in addition to any new 

treatment processes may provide additional options to be assessed in the future. 

1.1.1 Base Case 

The Base Case scenario is based on the treatment level permitted for the WPCP. The principal 

design considerations include: 

• 25 mg/L CBOD 5 and 30 mg/L TSS or 85% removal, whichever is stricter 

• Assume 35% removal of TN, based on the projected nitrogen loading for 2045. The same 

TN removal efficiency is assumed for all WPCPs considered in this project 

• Design dry weather flow rate 

• Assumed treatment levels are shown for each plant in Table EX-1 in the Executive Summary 

The base case scenario is defined as the treatment level that meets the current permit levels for 

wastewater discharge. The treatment process evaluated for the base case is the existing 

condition.

The treatment levels to be examined for the base case are the levels upon which each WPCP is 

permitted to operate. The permit levels described in the State Pollutant Discharge Elimination 

System (SPDES) are summarized in Table 1-1. 

Flow 

Table 1-1: Permit Limits, Levels and Monitoring Requirements for the HEP WPCPs 

Permit Sample 

Parameter Unit Type 

Remarks 

level frequency 

mgd 

12 months avg 

CBOD 5 mg/L 

Monthly avg 

7-day avg 

TSS 

Nitrogen 

Total 

Ammonia 

TKN 

Nitrite 

Nitrate 

Phosphorus 

Total 

Soluble (ortho) 

mg/L 

mg-N/L 

mg-P/L 

1.1.2 Existing Conditions 

Monthly avg 

7-day avg 

1-day maximum 

N/A 

N/A 

60 – PR 

60 – RH 

170 – NR 

120 – OH 

25 

40 

30 

45 

50 

To be 

monitored 

To be 

monitored 

Continuous 

1/day 

1/day 

1/day 

1/day 

1/day 

1/week 

2/month 

At least 85% 

removal 

At least 85% 

removal 

The Existing Conditions scenario maintains the treatment levels currently achieved at each 

WPCP. The design considerations include: 

 

 

 

Existing plant effluent quality for CBOD and TSS (using average of FY2003-05, see 

Table EX-1 and Table 1-2 below) 

Existing plant removal percentage for TN 

Existing plant flow 

Existing wastewater flow, influent concentrations, and effluent concentrations were calculated by 

taking averages of the operational data during fiscal years of 2003 through 2005. A summary of 

the existing plant influent and effluent characteristics from 2003 to 2005 is presented in Table 1- 

2.

Table 1-2: 2003-2005 Influent and Effluent Water Quality 

Plant 

Flow 

Waste 

CBOD CBOD TSS TSS TN TN 

rate 

Stream 

mgd mg/L lb/d mg/L lb/d mg/L lb/d 

26th Ward 

Influent 60 136 66,600 133 66,300 22 10,400 

Effluent - 7.9 3,900 14.1 7,000 14.6 7,300 

Bowery Bay 

Influent 116 138 131,500 122 117,100 30 28,800 

Effluent - 9.9 9,600 11.3 10,900 19.3 18,700 

Coney Island 

Influent 92 112 84,700 157 119,500 28 20,900 

Effluent - 8.0 6,100 13.9 10,600 17.1 13,100 

Hunts Point 

Influent 120 95 92,900 104 102,900 22 21,100 

Effluent - 10.2 10,200 12.3 12,300 20.1 20,100 

Jamaica 

Influent 82 147 98,700 142 96,200 30 19,500 

Effluent - 10.0 6,900 14.1 9,700 21.3 14,600 

Newtown Influent 231 136 259,500 160 309,100 24 45,900 

Creek Effluent - 37.8 72,800 30.0 57,800 18.2 35,100 

North River 

Influent 130 167 180,400 200 215,800 29 31,400 

Effluent - 11.4 12,300 15 16,200 18.4 19,900 

Oakwood Influent 31 120 30,400 183 46,800 30 7,500 

Beach Effluent - 6.6 1,700 13.0 3,400 20.0 5,200 

Owls Head 

Influent 102 167 141,600 185 157,300 30 25,700 

Effluent - 11.6 9,900 17.3 14,700 19.1 16,200 

Port Influent 36 175 49,900 182 53,700 26 7,300 

Richmond Effluent - 7.1 2,100 11.4 3,400 13.4 4,000 

Red Hook 

Influent 31 147 36,800 180 46,200 30 7,500 

Effluent - 6.8 1,800 7.8 2,000 16.1 4,200 

Rockaway 

Influent 20 72 12,000 103 17,100 19 3,100 

Effluent - 4.7 800 8.4 1,400 12.8 2,100 

Tallman Influent 58 117 55,800 126 60,300 27 12,700 

Island Effluent - 10.7 5,200 5.4 2,600 18.1 8,800 

Wards Island 

Influent 203 109 184,100 109 183,800 19 32,600 

Effluent - 5.6 9,500 9.3 15,700 16.8 28,400 

The Existing Conditions scenario is defined as the treatment level currently in place at each of 

the WPCPs. The treatment process and the treatment levels evaluated for the Existing 

Conditions scenario are the existing conditions. 

1.1.3 Existing Conditions with Solids Filtration 

The Existing Conditions with Solids Filtration (EC-SF) process will maintain all the existing 

infrastructure and processes currently in place at each WPCP, in addition to a solids filtration

process installed downstream of the secondary treatment process to enhance the removal of 

particulates in the wastewater, including solids, particulate BOD, and particulate TKN. 

Secondary effluent is applied to a filter bed and the filter media within the bed physically remove 

and store particulates from the waste stream. Sand or anthracite is typically used for the media. 

Secondary effluent is evenly applied to the filters at a constant flowrate per surface area, until 

accumulated solids within the filter reduce the filtration rate (or rate of application). To restore 

the filter, a backwash operation is performed with air and/or water to purge the media. 

A schematic of the process is shown in Figure 1-1. 

Figure 1-1: EC-SF Process Configuration 

1.1.4 Existing Conditions with Microfiltration/Ultrafiltration 

The Existing Conditions with Microfiltration/Ultrafiltration (EC-MF) process will maintain all 

the existing infrastructure and processes currently in place at each WPCP, in addition to a 

membrane filter process installed downstream of the secondary treatment process to further 

enhance the removal of particulates in the wastewater. Filtered secondary effluent would be

extracted through the membranes as a permeate. Compared to filtration, the removals are greater 

due to typical pore sizes between 0.1 to 0.2 m. 

The mechanism of membrane filtration is to use hydrostatic pressure to force liquid against a 

semipermeable membrane. Only the liquid and particles smaller than the membrane's pore size 

can pass through. Pore size refers to the diameter of the spherical particle that the filter would 

retain. A filter is rated with two pore sizes corresponding to two tiers of retention efficiency: 

• Absolute pore size - the particle size retained with 100% efficiency 

• Nominal pore size - the particle size retained with a selected majority efficiency 

Membrane filters are designated by pore sizes as shown in Table 1-3. 

Filtration 

Type 

Membrane 

filtration 


Nanofiltration 

Pore 

Size 

(µm) 

0.1-10 

0.01 

0.001 

Reverse 

Osmosis 0.0001 

Table 1-3: Membrane Filter Designations 

Pressure 

low-pressure 

cross-flow 

up to 145 psi 

(10 bar) 

mid-range 

pressure 

30–250 psi 

(2–17 bar) 

high-pressure 

Removal 

Turbidity. Colloidal and suspended particles including 

fats 

Microorganisms/pathogens, viruses, high molecularweight 

substances, organic and inorganic polymeric 

molecules including proteins, silicates 

Color. Demineralization, desalination (divalent salts), 

softening (polyvalent cation removal), sugars, pesticides, 

herbicides 

All suspended and dissolved solids. Low-molecularweight 

substances such as monovalent salts 

Membrane filtration is not commonly used on the scale of full tertiary treatment. It achieves 

removals far in excess of current regulation, and does so at significantly greater cost than 

conventional filtration. 

A schematic of the process is shown in Figure 1-2.

1.1.5 Advanced Basic BNR 

Figure 1-2: EC-MF Process Configuration 

Advanced Basic Biological Nitrogen Removal (ABBNR) is a process that maximizes the use of 

existing facilities to removal nitrogen from the process stream. The process was developed by 

the NYCDEP in the 1990s at the Tallman Island WPCP and has been further developed through 

continued research and testing. It is currently being implemented at five of the 14 NYCDEP 

WPCPs. 

The process involves modification of the existing step aeration process to include the cycling of 

oxic and anoxic zones that are necessary to remove nitrogen. ABBNR calls for maximized use 

of existing infrastructure and footprints (i.e. not changing location of gates, replacing air headers, 

or modify other major equipment, if possible). The process will require baffle walls to separate 

the oxic and anoxic portions of the tank and pre-anoxic zones to minimize the DO carryover 

from oxic to anoxic switch zones. Mixers will be required in the anoxic zones to keep solids in 

suspension and prevent the formation of stagnant zones. The anoxic zones will be fitted with 

membrane diffusers and isolated air droplegs to allow the zone to operate in an aerobic mode to 

meet the winter nitrification requirements. The blower and aeration system will be expanded to 

meet the needs of nitrogen removal. The RAS system will also be expanded to maximize the

capacity within the constraints of the existing facility. Automated flow control to Pass D will be 

provided to further enhance clarifier operation along with the capability to add polymer. The 

production of biological foam or froth is associated with the longer SRTs needed for 

nitrification. ABBNR includes three methods to control froth: RAS chlorination, froth hoods, 

and froth wasting. A moderate level of instrumentation will also be provided. A schematic of 

the process is shown in Figure 1-3. 

Figure 1-3: ABBNR Process Configuration 

In addition, this technology typically includes the capability to direct sludge dewatering centrate 

to a dedicated aeration tank for separate nitrification. A portion of mainstream RAS would be 

added to seed the process and alkalinity would be provided to satisfy the centrate nitrification 

requirement. Nitrified centrate would be returned to the head of the A Pass of the remaining 

tanks to be further treated. At Port Richmond, sludge is shipped to another facility for 

dewatering and therefore this capability will not be provided. 

1.1.6 Full Step BNR

The Full Step BNR (FSBNR) process is similar to the ABBNR, but provides additional control 

and flexibility. All of the components of ABBNR will be provided, in addition to the following: 

• Flow distribution and control will be provided on all 4 passes of the aeration tanks. 

• Alkalinity and Methanol facilities will be provided and sized to meet the load to the aeration 

tanks. 

• The RAS capacity will be expanded to 100% of the DDWF. 

• The process blowers and aeration system will be upgraded to meet the needs of the nitrogen 

removal process. 


1.1.7 Full Step BNR with Solids Filtration 

Figure 1-4: FSBNR Process Configuration 

The FSBNR with Solids Filtration (FSBNR-SF) process will provide all of the components of 

FSBNR, in addition to a solids filtration process installed downstream of the secondary treatment 

process to enhance the removal of particulates in the wastewater, including solids, particulate 

BOD, and particulate TKN. Secondary effluent is applied to a filter bed and the filter media

within the bed physically remove and store particulates from the waste stream. Sand or 

anthracite is typically used for the media. 

Secondary effluent is evenly applied to the filters at a constant flowrate per surface area, until 

accumulated solids within the filter reduce the filtration rate (or rate of application). To restore 

the filter, a backwash operation is performed with air and/or water to purge the media. 


Figure 1-5: FSBNR-SF Process Configuration 

1.1.8 Full Step BNR with Microfiltration/Ultrafiltration 

The FSBNR with Microfiltration/Ultrafiltration (FSBNR-MF) process will provide all of the 

components of FSBNR, in addition to a membrane filter process installed downstream of the 

secondary treatment process to further enhance the removal of particulates in the wastewater. 

Filtered secondary effluent would be extracted through the membranes as a permeate. Compared 

to filtration, the removals are greater due to typical pore sizes between 0.1 to 0.2 m. 


Figure 1-6: FSBNR-MF Process Configuration 

1.1.9 Full Step BNR with Denitrification Filters 

The FSBNR with denitrification filters (FSBNR-DF) process will provide all of the components 

of FSBNR, in addition to a denitrification filter process installed downstream of the secondary 

clarifiers and upstream of the disinfection system to both enhance the removal of particulates in 

the wastewater and remove Nitrogen through denitrification. 

This process will include all of the equipment listed for FSBNR plus the installation of 

denitrification filters and all supporting equipment. Supplemental carbon, such as methanol, will 

be added downstream of the FSBNR process rather than directly to the activated sludge process 

tanks. Denitrification filters are similar to conventional filters, however in addition to filtering 

out particulates, the media are used to grow fixed film denitrifying bacteria. These bacteria 

utilize methanol to convert nitrites and nitrates to free nitrogen gas and allows the overall process 

to achieve very low nitrogen levels. 


1.1.10 Membrane Bioreactors 

Figure 1-7: FSBNR-DF Process Configuration 

Membrane Bioreactors (MBR) are a combination of activated sludge reactors and membrane 

filtration facilities. Membrane facilities replace the clarification process by a physical barrier 

that separates solids from the liquid phase within the wastewater. Because the MBRs replace the 

clarifiers and provide a physical barrier, the aeration tanks can be operated at higher mixed liquor 

concentrations (approximately 8,500 mg/L) than conventional activated sludge systems. This 

allows for reduced tank sizes when compared to other activated sludge processes. The 

membranes used for this process are similar to the membrane filtration process, but they are 

operated at much lower flux rates (flow per unit) to handle the significantly higher solids loading 

rates. 

The process involves modification of the existing step aeration process to allow the entire flow 

stream to the head of the first pass. Zones will be created to allow the cycling of oxic and anoxic 

zones that are necessary to remove nitrogen. The process will require baffle walls to separate the 

oxic and anoxic portions of the tank. Mixers will be required in the anoxic zones to keep solids 

in suspension and prevent the formation of stagnant zones. The process will include the 

installation of fine screening, recirculation pumping, RAS pumping, and the construction of new

Membrane Bioreactors. The blower and aeration system will be expanded to meet the needs of 

nitrogen removal. Alkalinity feed systems will be provided to enhance nitrogen removal. The 

production of biological foam or froth is associated with the longer SRTs needed for 

nitrification. This technology includes three methods to control froth: RAS chlorination, froth 

hoods, and froth wasting. New instrumentation and controls will be provided. 

The process configuration consists of a series of four activated sludge process zones that cycle 

between nitrification and denitrification. The first and third zones are anoxic (un-aerated) and 

the second and fourth zones are aerobic (aerated). The MBR tanks are aerated to provide oxygen 

for the biomass and to provide scouring of the membrane surfaces. Return pumps remove excess 

solids from the MBR tanks and return them to the process tanks. Internal recycle pumping is 

provided between the third and first passes to maximize the nitrate concentration in the anoxic 

zones for denitrification. The effluent will be pumped to the disinfection tank and discharged. A 

schematic of the process is shown in Figure 1-8. 

Figure 1-8: Membrane Bioreactor Process Configuration 

A summary of each technology and the projected effluent concentrations is shown below in 

Table 1-4.

Table 1-4: Carbon and Nitrogen Removal Technologies Summary 

Level of Treatment 

Characteristics 

Base Case 

Effluent Characteristics: 

• Current permitted effluent quality, according to 

SPDES permit 

CBOD ≤ 25mg/L 

TSS ≤ 30mg/L 

• TSS = 30mg/L, CBOD = 25mg/L or 85% removal 

from influent conditions, whichever is stricter 

TN = 18-21mg/L 

• TN removal of 35% 

Existing Conditions 


CBOD = 8-15mg/L 

TSS = 8-18mg/L 

TN = 13-19mg/L 

Existing Conditions with Solids Filtration 



TSS = 4-5mg/L 

TN = 13-19mg/L 

Existing Conditions with 

Microfiltration/Ultrafiltration 



TSS = ~1mg/L 

TN = 13-19mg/L 

Advanced Basic BNR 



TSS = 12-15mg/L 

TN = 10-12mg/L 

Full-Step BNR 



TSS = 12-15mg/L 

TN = 6-10mg/L 

• Plant flow and effluent quality for Fiscal Years 2003 to 

2005 

• Assumes current performance observed will continue 

Same characteristics from Existing Conditions option, but 

with the following additions: 

• 1,500 mg/L AEMLSS 

• Deep-bed sand filters added after secondary treatment 

to provide additional solids and carbon removal 

• Water backwash and air scour system for filter 

cleaning 

Same characteristics from Existing Conditions option, but 

with the following additions: 


• Zenon Microfilters/Ultrafilters added after secondary 

treatment to provide additional solids and carbon 

removal 

• Air scour system for filter cleaning 

• 2 mm screens upstream of Microfilters/Ultrafilters 

Biological Nitrogen Removal Enhancements to Secondary 

treatment to include: 


• 0-33-33-33 flow split 

• Baffles to create switch zones 

• Anoxic and Pre-anoxic zones with mixers 

• Froth control hoods 

• Alkalinity addition 

• Return sludge capability at 50% 

Biological Nitrogen Removal Enhancements to Secondary 



• 10-40-30-20 flow split 

• Baffles to create switch zones 

• Anoxic and Pre-anoxic zones with mixers 

• Froth control hoods 



• Methanol Addition


Full-Step BNR with Solids Filtration 



TSS = 4-5mg/L 

TN = 6-10mg/L 

Full-Step BNR with 




TSS = ~1mg/L 

TN = 6-10mg/L 

Full-Step BNR with Denitrification 

Filters 



TSS = 4-5mg/L 

TN = 4-5mg/L 

Membrane Bioreactors 



TSS = ~1mg/L 

TN = 3-4mg/L 


Same characteristics from Full-Step BNR option, but with 

the following additions: 

• Deep-bed sand filters added after secondary treatment 

to provide additional solids and carbon removal 


cleaning 



• Zenon Microfilters/Ultrafilters added after secondary 

treatment to provide additional solids and carbon 

removal 


• 2 mm screens upstream of Microfilters/Ultrafilters 



• Denitrification filters added after secondary treatment 

to provide additional solids, carbon, and nitrogen 

removal 


cleaning 

Zenon Membrane Bioreactor inclusion in Secondary 


• 8,500 mg/L AEMLSS (10,000 mg/L at OH) 

• Internal recycle from Pass C to Pass A 

• Anoxic zones 



• Methanol Addition 


• 6 mm and 2 mm screens upstream of MBRs 

1.2 Design Standards 

Basic design standards employed for the conceptual design are consistent for the four WPCPs 

considered in the HEP as summarized below: 

• Design standard is 1.5 times design dry weather flow for secondary treatment components 

sized on the basis of flow. Secondary bypass channel to be preserved 

• Design standard is 2.0 times dry weather flow for components before/after secondary bypass 

• Design standard is projected 2045 load for components sized on the basis of load 

• Degree of redundancy is N+1 for process infrastructure, N+1+1 for process equipment 

1.3 Influent Flows and Loads 

The flows and loads used for the basis of design for this evaluation are based on the NYCDEP 

Interim Water Demand and Wastewater Flow Projections developed by the Bureau of 

Environmental Planning and Assessment (BEPA) in July 2006, with the exception of the North 

River WPCP, which is explained in detail in Section 1.3.3. The projections utilized the

population projections prepared by the Department of City Planning, which in turn used the 2000 

Census. A summary table for the 2045 projected flows and loads at each WPCP in New York 

City is presented in Table 1-5 below. 

Table 1-5: 2045 Influent Flow and Load Assumptions 

Plant Flow Inf BOD Inf TSS Inf TN 

mgd lb/d lb/d lb/d 

26th Ward 57 88,762 95,466 13,525 

Bowery Bay 131 147,284 133,903 32,526 

Coney Island 96 116,792 130,600 23,578 

Hunts Point 124 112,302 124,608 25,591 

Jamaica 89 122,050 109,987 23,844 

Newtown Creek 240 359,882 466,617 69,476 

North River 137 198,141 188,400 36,637 

Oakwood Beach 37 58,380 59,504 8,431 

Owls Head 105 161,275 149,979 27,119 

Port Richmond 38 78,322 71,578 9,145 

Red Hook 33 46,696 54,741 8,734 

Rockaway 24 18,006 19,401 4,279 

Tallman Island 62 68,909 65,273 14,511 

Wards Island 213 225,672 226,323 45,402 

1.3.1 Port Richmond 

Future flows and loads were evaluated and used as a basis of design for the Port Richmond 

WPCP. Table 1-6 shows the projections for the year 2045 for Port Richmond, which served as 

the design year and the peak loads. 

Table 1-6: Projected Flows and Loads for 2045 

Flow (mgd) CBOD TSS TN 

Concentration, mg/L 205 225 28.6 

38.1 

Loading, lb/d 

65,200 71,600 9,100 

Flow and load peaking factors were based on representative plant-specific work at the East River 

WPCPs during the development of the LISS BNR program. Table 1-7 shows the peaking 

factors used in this analysis.

Table 1-7: Flow and Load Peaking Factors 

Loading 

Condition 

Flow Peaking 

Factors 

TSS Load 

Peaking Factors 

CBOD Load 


TKN Load 


Minimum Week 0.81 0.72 0.72 0.72 

Minimum Month 0.83 0.79 0.83 0.83 

Annual Average 1.00 1.00 1.00 1.00 

Maximum Month 1.22 1.23 1.28 1.28 

Maximum Week 1.50 1.53 1.53 1.53 

Maximum Day 2.00 1.78 1.78 1.78 

Peak Hour 2.00 2.00 2.00 2.00 

These peaking factors were applied to the 2045 projected loads to determine peak loading 

conditions. The peaking factors were applied to the projected 2045 flows and loads to create the 

influent flows and loads assumptions shown in Table 1-8 and are as follows: 

1.3.2 Red Hook 

Table 1-8: Basis of Design Influent Flow and Load 

Average 

Peak Daily 

Flow (mgd) 38.1 76.2 

TSS (lb/d) 71,600 143,156 

CBOD (lb/d) 65,200 130,400 

TKN (lb/d) 9,100 18,290 

Future flows and loads were evaluated and used as a basis of design for the Red Hook WPCP. 

Table 1-9 shows the projections for the year 2045 for Red Hook, which served as the design year 

and the peak loads. 


Flow (mgd) CBOD TSS TN 


32.9 

Loading, lb/d 

39,000 54,700 8,700 

Flow and load peaking factors were based on representative plant-specific work at the East River 

WPCPs during the development of the LISS BNR program. Table 1-10 shows the peaking 

factors used in this analysis.

Table 1-10: Flow and Load Peaking Factors 

Loading 

Condition 

Flow Peaking 

Factors 

TSS Load 


CBOD Load 


TKN Load 


Minimum Week 0.81 0.72 0.72 0.72 

Minimum Month 0.83 0.79 0.83 0.83 

Annual Average 1.00 1.00 1.00 1.00 

Maximum Month 1.22 1.23 1.28 1.28 

Maximum Week 1.50 1.53 1.53 1.53 

Maximum Day 2.00 1.78 1.78 1.78 

Peak Hour 2.00 2.00 2.00 2.00 

These peaking factors were applied to the 2045 projected loads to determine peak loading 

conditions. The peaking factors were applied to the projected 2045 flows and loads to create the 

influent flows and loads assumptions shown in Table 1-11 and are as follows: 


Average 

Peak Hour 

Flow (mgd) 39.2 78.4 

TSS (lb/d) 54,700 109,400 

CBOD (lb/d) 39,900 79,800 

TKN (lb/d) 8,700 17,400 

Of concern is that the current CBOD load at the Red Hook WPCP (39,800 pounds per day on an 

annual average basis) is slightly greater than the BEPA CBOD projected load for 2045 (39,000 

pounds) despite this service area being a likely area of population and employment growth. 

1.3.3 North River 

Existing and future flows and loads were evaluated and used as a basis of design for the North 

River WPCP. 

1.3.3.1 Existing Flows and Loads 

An evaluation of existing flows and loads was performed to develop peaking factors that may be 

used for future flow and load projections. Plant Data from 2003 to 2005 was evaluated to 

determine average and peak (monthly, weekly and daily) loadings to the facilities. Peaking 

factors (monthly, weekly and daily) were developed for flows and loads and were determined 

based on 2 times the standard deviation plus the average to ensure designs are not based on 

anomalies that would result in excessive costs. Plant data is shown in Appendix A of the North 

River Report. Table 1-12 shows the flow and load conditions at the plant and Table 1-13 shows 

the peaking factors that will be used to evaluate future conditions.

Table 1-12: Influent Flow and Load (2003-2005) 

Average Max Month Max Week Peak Daily 

Flow (mgd) 129.6 143.3 155.0 181.0 

TSS (lb/d) 215,800 302,400 324,200 391,700 

CBOD (lb/d) 180,400 227,600 238,000 274,200 

TKN (lb/d) 31,400 38,100 41,800 41,800 

Table 1-13: Peaking Factors 


Flow 1.00 1.11 1.20 1.40 

TSS 1.00 1.40 1.50 1.82 

CBOD 1.00 1.26 1.32 1.52 

TKN 1.00 1.21 1.33 1.33 

1.3.3.2 Future Flows and Loads 

The flows and loads used for the basis of design for this evaluation are based on plant data and 

the NYCDEP Interim Water Demand and Wastewater Flow Projections developed by the Bureau 

of Environmental Planning and Assessment (BEPA) in July 2006. The flow ad load projections 

utilized the population projections prepared by the Department of City Planning (projections use 

2000 Census as a basis). Table 1-14 shows the projections for the year 2045 for North River, 

which served as the design year and the peak loads. 

Table 1-14: 2045 Projected Influent Flow and Load 

(MGD) (mg/L) (lbs/day) 

Flow 136.7 --- --- 

TSS --- 165 188,400 

CBOD --- 145 165,400 

TKN --- 32.1 36,600 

The above projections were based on the year 2000 census data and corresponding wastewater 

characteristics and projecting to the year 2045 based on population change data presented by 

BEPA. However, more recent plant data (2003 to 2005) shows that the above projections 

underestimate current TSS and CBOD loads and may underestimate the future TSS and CBOD 

loading to the plant. Figures 1-9 and 1-10 show the disparity of the projections to the more 

recent existing data.

300,000 

250,000 

TSS Load (lbs/day) 

200,000 

150,000 

100,000 

50,000 

0 

Projected TSS Loading 

Actual TSS Loading 

1989 

1991 

1993 

1995 

1997 

1999 

2001 

2003 

2005 

2007 

2009 

2011 

2013 

2015 

2017 

2019 

2021 

2023 

2025 

2027 

2029 

2031 

2033 

2035 

2037 

2039 

2041 

2043 

2045 

Figure 1-9: Comparison of Actual and Projected TSS Loads 

250,000 

200,000 

BOD Load (lbs/day) 

150,000 

100,000 

50,000 

Projected BOD Loading 

0 

Actual BOD Loading 

1989 

1991 

1993 

1995 

1997 

1999 

2001 

2003 

2005 

2007 

2009 

2011 

2013 

2015 

2017 

2019 

2021 

2023 

2025 

2027 

2029 

2031 

2033 

2035 

2037 

2039 

2041 

2043 

2045 

Figure 1-10: Comparison of Actual and Projected CBOD Loads 

Due to the disparity of projections and actual data, an increase of 20% for TSS and CBOD loads 

will be assumed. Further research is recommended to resolve the differences in the projected 

loads and existing plant data at the North River WPCP. 

The data for nitrogen are generally consistent with the BEPA projections (Figure 1-11.) and will 

be used for this evaluation. A summary of the flows and loads that will be used as a basis of 

design are shown in Table 1-15.

Temperature data was also reviewed as part of the evaluation. A peak temperature of 26.4 

degrees Celsius and a minimum temperature of 12 degrees Celsius were used as the basis of 

design. 

40,000 

35,000 

TKN Load (lbs/day) 

30,000 

25,000 

20,000 

15,000 

10,000 

5,000 

0 

Projected TKN Loading 

Actual TKN Loading 

1989 

1991 

1993 

1995 

1997 

1999 

2001 

2003 

2005 

2007 

2009 

2011 

2013 

2015 

2017 

2019 

2021 

2023 

2025 

2027 

2029 

2031 

2033 

2035 

2037 

2039 

2041 

2043 

2045 

Figure 1-11: Comparison of Actual and Projected TKN Loads 



Flow (mgd) 136.7 151.1 163.5 190.9 

TSS (lb/d) 258,900 362,900 389,100 470,000 

CBOD (lb/d) 216,500 273,100 285,600 329,100 

TKN (lb/d) 36,600 44,400 48,700 48,700 

1.3.4 Owls Head 

The projected values for the Owls Head WPCP are shown in Table 1-16. The conceptual design 

for each treatment alternative is developed as a design year of 2045. 


Flow rate 

CBOD TSS TN 

MGD 


104.6 

Loading, lb/d 

134,400 150,000 27,100 

Three years of operating data (fiscal year 2003 through fiscal year 2005) for Owls Head WPCP 

were analyzed and maximum week peaking factors were developed for BOD, TSS, and 

ammonia. These peaking factors were applied to the 2045 projected loads to determine peak

loading conditions. The peaking factors were applied to the projected 2045 flows and loads to 

create the influent flows and loads assumptions shown in Table 1-17 and are as follows: 

• BOD: 1.31 

• TSS: 1.65 

• TKN: 1.52 

Table 1-17: Influent Flow and Load Assumptions 

Conditions 

Flow BOD TSS TKN 

(MGD) (mg/L) (lbs/d) (mg/L) (lbs/d) (mg/L) (lbs/d) 

Design Average 120 134.3 134,400 150 150,000 27 27,100 

Design Maximum 120 176 176,064 247 247,500 41.2 41,192 

Per the mass balances presented in Section 2 of the Owls Head report, the Primary Settling 

Tanks remove a substantial portion of influent TSS, as well as BOD and TKN. The percent 

removals across the Primary Settling Tanks are as follows: 

• 53% reduction of TSS loading 

• 17.2% reduction of BOD loading 

• 11.2% reduction of TKN loading 

Applying these removals to the influent characteristics estimates the characteristics of the 

primary effluent to be used in the model. The estimated primary effluent characteristics are 

presented below in Table 1-18. 

Table 1-18: Primary Effluent Flow and Load Assumptions 

Conditions 

Flow BOD TSS TKN 

(MGD) (mg/L) (lbs/d) (mg/L) (lbs/d) (mg/L) (lbs/d) 

Design Average 120 111 111,283 70 70,500 24 24,065 

Design Maximum 120 146 145,781 116 116,325 37 36,578 

1.4 Plant Specific Analysis 

The following four reports detail the conceptual designs developed to implement the various 

levels of technology listed in Section 1.1. The reports are presented as follows: 

• Port Richmond 

• Red Hook 

• North River 

• Owls Head 

The reports provide an introduction to the existing plants and step through each level of 

technology, addressing the impacts on each treatment step and providing conceptual designs to 

incorporate each technology into the plant’s infrastructure and operations.

Harbor Estuary Program 

Port Richmond 

Water Pollution Control Plant 

Conceptual Design Report 

June 2007 

DRAFT

Harbor Estuary Program June 2007 

Port Richmond Water Pollution Control Plant 

DRAFT 

TABLE OF CONTENTS 

Section Description Page 

1 PORT RICHMOND WATER POLLUTION CONTROL PLANT 1-1 

1.1 BACKGROUND 1-1 

1.2 EXISTING CONDITIONS 1-1 

1.2.1 Plant Hydraulics 1-2 

1.2.2 Influent Screening and Main Sewage Pumping 1-5 

1.2.3 Primary Settling 1-6 

1.2.4 Primary Sludge Pumping and Degritting 1-8 

1.2.5 Aeration 1-9 

1.2.6 Final Settling Tanks 1-12 

1.2.7 Disinfection and Outfall 1-13 

1.2.8 Return Activated Sludge 1-16 

1.2.9 Waste Activated Sludge/Mixed Liquor 1-16 

1.2.10 Sludge Thickening and Elutriation 1-16 

1.2.11 Anaerobic Digestion 1-20 

1.2.12 Sludge Storage and Transfer 1-23 

1.2.13 Summary of Plant Operations 1-23 

1.3 ONGOING AND PLANNED UPGRADES 1-29 

2 MASS BALANCE DIAGRAMS 2-1 

3 BASIS OF DESIGN 3-1 

4 EXISTING CONDITIONS WITH SOLIDS FILTRATION 4-1 

4.1 PRIMARY SETTLING TANKS 4-1 

4.2 FINE SCREENS 4-1 

4.3 AERATION TANKS 4-1 

4.3.1 Flow Distribution and Control 4-1 

4.3.2 Baffles and Zone Sizing 4-1 

4.3.3 Anoxic Zone Mixers 4-1 

4.3.4 Air Distribution and Control 4-1 

4.3.5 Diffusers 4-2 

4.4 PROCESS AERATION SYSTEM 4-2 

4.5 FINAL SETTLING TANKS 4-2 

4.6 RETURN ACTIVATED SLUDGE SYSTEM 4-2 

4.7 WASTE ACTIVATED SLUDGE SYSTEM 4-2 

4.8 FROTH CONTROL 4-2 

4.8.1 Froth Control Hoods 4-2 

4.8.2 RAS Chlorination 4-2 

4.8.3 Surface Wasting 4-3 

4.9 CHEMICAL FACILITIES 4-3 

4.9.1 Alkalinity 4-3 

4.9.2 Carbon 4-3 

TOC-1



DRAFT 

4.10 INTERMEDIATE PUMPING STATION 4-3 

4.11 TERTIARY TREATMENT 4-3 

4.11.1 Solids Filtration 4-3 

4.11.2 Microfiltration/Ultrafiltration 4-4 

4.11.3 Denitrification Filters 4-4 

4.12 MEMBRANE BIOREACTORS 4-4 

4.13 ODOR CONTROL 4-5 

5 EXISTING CONDITIONS WITH MICROFILTRATION/ULTRAFILTRATION 5-1 



















5.9.2 Carbon 5-3 








6 ADVANCED BASIC BNR 6-1 










TOC-2



DRAFT 










6.9.2 Carbon 6-11 








7 FULL STEP BNR 7-1 



















7.9.2 Carbon 7-6 








8 FULL STEP BNR WITH SOLIDS FILTRATION 8-1 

TOC-3



DRAFT 



















8.9.2 Carbon 8-2 








9 FULL STEP BNR WITH MICROFILTRATION/ULTRAFILTRATION 9-1 



















TOC-4



DRAFT 

9.9.2 Carbon 9-3 








10 FULL STEP BNR WITH DENITRIFICATION FILTERS 10-1 



















10.9.2 Carbon 10-2 








11 MEMBRANE BIOREACTORS 11-1 









TOC-5



DRAFT 



11.6 RETURN ACTIVATED SLUDGE SYSTEM/INTERNAL RECYCLE 11-6 








11.9.2 Carbon 11-7 








12 SUMMARY OF COST AND PERFORMANCE 12-1 

APPENDIX A 

APPENDIX B 

I 

XXIX 

TOC-6



DRAFT 

TABLE OF FIGURES 

Figure Description Page 

Figure 1-1: Overall Plant Flow Schematic................................................................................... 1-2 

Figure 1-2: Plant Hydraulic Profile.............................................................................................. 1-3 

Figure 1-3: MSP and Influent Screening Process Overview ....................................................... 1-6 

Figure 1-4: Primary Settling Tank Schematic Overview............................................................. 1-8 

Figure 1-5: Aeration Tank Flow Schematic............................................................................... 1-10 

Figure 1-6: Average Aerator MLSS Concentrations ................................................................. 1-11 

Figure 1-7: Schematic Overview of Chlorination Facilities...................................................... 1-14 

Figure 1-8: Arrangement of the Sludge Thickening Facilities .................................................. 1-17 

Figure 1-9: Mass Balance on Elutriators ................................................................................... 1-19 

Figure 1-10: Mass Balance on Sludge Thickening.................................................................... 1-20 

Figure 1-11: Schematic of the Digestion Process ...................................................................... 1-21 

Figure 11-1: MBR Setup............................................................................................................ 11-9 

TOC-7



DRAFT 

TABLE OF TABLES 

Table Description Page 

Table 1-1: Port Richmond Design Flows..................................................................................... 1-2 

Table 1-2: Summary of Wet Weather Flows and Bypasses ........................................................ 1-4 

Table 1-3: Unit Process Maximum Treatment Capacities........................................................... 1-5 

Table 1-4: MSP and Influent Screening Design Criteria ............................................................. 1-6 

Table 1-5: Primary Settling Tank Design Criteria....................................................................... 1-8 

Table 1-6: Primary Sludge Pumping and Degritting Design Criteria.......................................... 1-9 

Table 1-7: Aeration System Design Criteria.............................................................................. 1-11 

Table 1-8: Aeration System Operating Parameters ................................................................... 1-12 

Table 1-9: Final Settling Tank Design Criteria.......................................................................... 1-13 

Table 1-10: Disinfection System Design Criteria...................................................................... 1-15 

Table 1-11: RAS Pump Design Criteria .................................................................................... 1-16 

Table 1-12: Sludge Thickening System Design Criteria ........................................................... 1-18 

Table 1-13: Digester System Design Criteria ............................................................................ 1-22 

Table 1-14: Anaerobic Digester Performance ........................................................................... 1-23 

Table 1-15: Port Richmond WPCP Existing Facility Description............................................. 1-23 

Table 6-1: Operating Flow Distribution Assumptions for ABBNR ............................................ 6-1 

Table 6-2: Anticipated Inter-Zone Baffle Wall Locations for ABBNR ...................................... 6-2 

Table 6-3: Anticipated Mixed Liquor Concentrations for ABBNR ............................................ 6-4 

Table 6-4: Anticipated Mixing Zone Sizing (per tank) for ABBNR ........................................... 6-4 

Table 6-5: Anticipated Number of Anoxic Zone Mixers for ABBNR ........................................ 6-4 

Table 6-6: Diffuser Requirements for ABBNR ........................................................................... 6-6 

Table 6-7: Future 2045 Air Requirements for ABBNR............................................................... 6-6 

Table 7-1: Operating Flow Distribution Assumptions for FSBNR ............................................. 7-1 

Table 7-2: Anticipated Inter-Zone Baffle Wall Locations for FSBNR ....................................... 7-2 

Table 7-3: Anticipated Mixed Liquor Concentrations for FSBNR ............................................. 7-2 

Table 7-4: Anticipated Mixing Zone Sizing (per tank) for FSBNR ............................................ 7-2 

Table 7-5: Anticipated Number of Anoxic Zone Mixers for FSBNR ......................................... 7-3 

Table 7-6: Diffuser Requirements for FSBNR ............................................................................ 7-4 

Table 7-7: Future 2045 Air Requirements for FSBNR................................................................ 7-4 

TOC-8



DRAFT 

Table 11-1: Operating Flow Distribution Assumptions for MBR ............................................. 11-3 

Table 11-2: Anticipated Inter-Zone Baffle Wall Locations for MBR ....................................... 11-3 

Table 11-3: Anticipated Mixed Liquor Concentrations for MBR ............................................. 11-3 

Table 11-4: Anticipated Mixing Zone Sizing (per tank) for MBR............................................ 11-4 

Table 11-5: Anticipated Number of Anoxic Zone Mixers for MBR ......................................... 11-4 

Table 11-6: Diffuser Requirements for MBR............................................................................ 11-5 

Table 11-7: Future 2045 Air Requirements for MBR ............................................................... 11-5 

Table 12-1: Secondary Effluent for Each Level of Technology................................................ 12-1 

Table 12-2: Capital Construction Costs for Levels of Treatment.............................................. 12-1 

TOC-9



DRAFT 

1 PORT RICHMOND WATER POLLUTION CONTROL PLANT 

1.1 Background 

The Port Richmond Water Pollution Control Plant (WPCP) is a 60 million gallon per day (mgd) 

design dry weather flow, 120 mgd peak wet weather flow, facility located on the northern side of 

Staten Island. It was built in 1953 and services 9,665 acres in the Northern section of Staten 

Island, including the communities of Howland Hock, Arlington, Old Place, Marnier's Harbor, 

Port Ivory, Graniteville, Port Richmond, Westerleigh, Livingston, Elm Park, West New 

Brighton, Silver Lake, St. George, Ward Hill, Stapleton, Grymes Hill, Clifton, Fox Hills, 

Rosebank, Shore Acres, Bloomfield, Chelsea, Travis, Bulls Head, Emerson Hill, Concord, 

Grasmere, and Arrochar. It is located at 1801 Richmond Terrace, Staten Island, NY, 10310 in 

Staten Island, New York. The site is adjacent to the Kill Van Kull, leading into the Upper New 

York Bay, located between Clove Road and Taylor Street. 

The Port Richmond WPCP has been providing full secondary treatment since 1979. Processes 

include primary screening, raw sewage pumping, grit removal and primary settling, air activated 

sludge capable of operating in the step aeration mode, final settling, and chlorine disinfection. 

The Port Richmond WPCP has a design dry weather flow (DDWF) capacity of 60 mgd, and is 

designed to receive a maximum flow of 120 mgd (2 times DDWF) with 90 mgd (1.5 times 

DDWF) receiving secondary treatment. Flows over 90 mgd receive primary treatment and 

disinfection. The daily average flow during 2004 was 35 mgd, with a dry weather flow average 

of 32 mgd. During severe wet weather events in 2004 the plant treated 97 to 109 mgd 

1.2 Existing Conditions 

The Port Richmond WPCP is a secondary treatment plant that provides preliminary screening, 

primary settling, biological treatment through a step-feed activated sludge process, secondary 

settling and disinfection. The combined primary and waste activated sludge flow is gravity 

thickened, anaerobically digested, elutriated, and transferred offsite for dewatering and centrate 

treatment. Figure 1-1 includes an overall plant layout and general flow pattern. 

1-1



DRAFT 

1.2.1 Plant Hydraulics 

Figure 1-1: Overall Plant Flow Schematic 

A plant hydraulic profile is included as Figure 1-2. Port Richmond is sized for a maximum 

influent flow of 160 mgd with one primary settling tank (PST), one aeration tank (AT), and one 

final settling tank (FST) out of service. Table 1-1 shows the dry and wet weather design flows 

for Port Richmond. 

Table 1-1: Port Richmond Design Flows 

Port Richmond Plant Capacity 

Design Dry Weather Flow 

60 mgd 

Design Wet Weather Flow 

120 mgd 

1-2



DRAFT 

Figure 1-2: Plant Hydraulic Profile 

Raw sewage flow from the influent sewer separates intro three channels, each equipped with a 5- 

foot wide stop gate and a dedicated, mechanically-cleaned bar screen. Screened sewage then 

splits into two channels. Flow in each channel passes through two 72-inch diameter sluice gates 

in separate 72-inch main sewage pumps (MSP) suction headers. Three vertical centrifugal 

pumps are connected to each of the two headers and lift the sewage to the primary settling tank 

influent channel which allows flow by gravity through the remainder of the plant. 

The four primary settling tanks each have two bays, and each bay is fed by the influent conduit 

via three 42-inch sluice gates. Primary settling tanks effluent flows into a 9-foot wide primary 

effluent channel before discharging into a 96-inch diameter pipe that transports flow to the 

aeration tank influent channel. 

Stop logs and a manually-operated electromechanical butterfly gate is used to direct primary 

effluent flow greater than 90 mgd to the bypass channel. Operations staff estimate that 10 

percent of wet weather events require use of the bypass channel. The bypass channel splits into 

two 60-inch pipes prior to entering the final settling tank effluent channel upstream of the 

Parshall flume. 

Primary effluent enters the aeration tank influent chamber where it mixes with thickener and 

elutriator overflow before being distributed between two aeration tank influent channels located 

at the East and West ends of the aeration tanks. One influent channel feeds passes A and C of 

each tank, while the other channel feeds passes B and D. Each pass can receive primary effluent 

1-3



DRAFT 

through two 48 by 72 inch motor operated sluice gates. The tanks are operated in step-feed 

mode. 

RAS is pumped to a trapezoidal return sludge channel from which it enters sludge sight wells 

located at the upstream end of pass A of each aeration tank through two 24-inch square sluice 

gates. Flow exits the aeration tanks through two 36 by 60 inch sluice gates located at the effluent 

end of Pass D. Aeration tank connections to the final settling tank influent distribution channels 

are somewhat asymmetric. 

Aeration tank mixed liquor is fed to the final settling tanks from two 8-foot wide final settling 

tank influent channels through six 3 by 3 foot slide gates per tank. Sludge in each tank is 

collected via a flight-and-chain mechanism to a center channel, and is then moved by a cross 

collector to two hoppers. RAS is drained by each hopper through variable elevation bell weirs 

and fed into one of two 30-inch diameter RAS pipes. These pipes discharge by gravity into a 

RAS wet well. 

The secondary effluent discharges through a Parshall flume into a 6-foot wide chlorine contact 

tank influent channel. The influent channel discharges into two separate chlorine contact tanks 

through four 48 by 60 inch sluice gates (two gates per tank). 

After traveling over the chlorine contact tank weirs, flow leaves the plant through the 96-inch 

plant outfall. The outfall is 524 feet long and terminates in a large headwall. 

The 24-inch diameter plant drain receives recycle streams from throughout the plant and 

discharges just downstream of the bar screens. Recycle flows include tank overflows, unit 

process tank drains, and final settling tank skimmings. Skimmings pit underflow and degritted 

primary sludge wet well overflow are also returned downstream of the bar screens via a 10-inch 

diameter pipe. 

The plant is permitted to accept up to 120 mgd, or two times the 60 mgd Design Dry Weather 

Flow capacity. Wet weather flows in excess of 90 mgd, as measured by the MSP meters, 

receives primary settling and disinfection. Table 1-2 summarizes wet weather flows and bypass 

during the two-year study period of November 1999 through October 2001. 

Table 1-2: Summary of Wet Weather Flows and Bypasses 

Description 

Value 

Design Dry Weather Flow (mgd) 60 

Maximum Hourly Flow (mgd) 130 

Maximum Daily Flow (mgd) 104 

Percent of Days Bypass was Required 9.7 

Average Flow to Bypass Channel When Required (mgd) 3.0 

While the plant is permitted to handle up to 120 mgd, many of the process units were designed 

for higher flow rates, as presented in Table 1-3. 

1-4



DRAFT 

Table 1-3: Unit Process Maximum Treatment Capacities 

Unit Process 

Maximum Capacity (mgd) 

Headworks 160 

MSPs 180 

Primary Settling Tanks 122 

Chlorine Contact Tanks 156 

Plant Outfall At Least 160 

Secondary Bypass 40 

1.2.2 Influent Screening and Main Sewage Pumping 

Raw sewage flow from the influent sewer separates into three channels, each equipped with a 5- 

foot wide isolation sluice gate. The influent channels are flushed daily to minimize grit 

accumulation. Each influent channel has a dedicated, mechanically-cleaned bar screen. Each 

bar screen cleaner is powered by a submersible motor enclosure. The current units replaced the 

bar-and-rack units in 1994. The bar screens empty into nearby satellite containers, which are 

periodically transferred to a common 20 or 26 cubic yard disposal container using a forklift. 

Under normal conditions, one bar screen and channel are used. A second channel and screen are 

used during wet weather events. After screening, the three channels combine into a common 

channel. 

Screened sewage then enters into two 72-inch main sewage pump (MSP) suction headers 

through two 72-inch sluice gates. Three pumps are connected to each of the two headers to lift 

the sewage to the raw sewage plenum. The MSPs are of the vertical, non-clogging, centrifugal, 

mixed flow type and are manually controlled to maintain a constant water surface elevation. 

Pumps operate at speeds varying between 70 to 97 percent of the maximum speed, resulting in 

pumping rates between 17 and 30 mgd. Under normal conditions, one pump is operated at night, 

two are operated during the day, and four are operated during rain events. The MSPs have 

pumped over 120 mgd during rain events. MSP seal water (city water) is provided by a system 

including a 300-gallon seal water tank and two 60-gpm pumps. 

The screenings removal rate is calculated based on the number of 20 and 26 cubic yard 

containers removed. However, both screenings and grit accumulate in these containers, and it is 

assumed that each of these sources occupy 50 percent of the total container volume. 

Raw influent samples are collected from the primary influent channel on an hourly basis by an 

automatic sampler, which composites them once daily. Primary influent flow is measured by 

strap-on Doppler flow meters located on the discharge of each MSP. These flow measurements 

were utilized for plant reporting prior to installation of the Parshall flume at the final settling tank 

effluent in 1988. 

Table 1-4 lists design criteria for these unit processes and Figure 1-3 provides a schematic 

overview of these processes. 

1-5



DRAFT 

Table 1-4: MSP and Influent Screening Design Criteria 

Parameter 

Value 

Number of Bar Screens 3 

• Width (ft) 5 

• Clear Opening (in) 7/8 

• Inclination from Horizontal (degrees) 84 

Number of MSPs 6 

• Type Mixed Flow, Centrifugal 

• Pump Speed (rpm) 500 – 585 

• Capacity (mgd) 17 – 30 

• TDH (ft) 34 -38.5 

• Motor Horsepower (hp) 250 

Number of Ring Flush Pumps 2 

• Type Mixed Flow, Centrifugal 

• Pump Speed (rpm) 900 

• Capacity (gpm) 470 

• TDH (ft) 43 

• Motor Horsepower (hp) 15 

1.2.3 Primary Settling 

Figure 1-3: MSP and Influent Screening Process Overview 

1-6



DRAFT 

The Port Richmond WPCP has four rectangular primary settling tanks with two bays each. The 

primary settling tanks are not symmetric about the MSP discharge plenum, which is located 

along the influent end of primary settling tanks 1 and 2. Both bays of each primary settling tank 

are fed from the influent conduit through three 42-inch square sluice gates. Primary settling 

tanks are taken out of service on an as-needed basis for cleaning and maintenance. 

The primary settling tanks are equipped with influent channel aeration, conventional chain and 

flight sludge collectors/surface skimmers, inlet baffles and adjustable overflow weirs. The 

influent channel is aerated to prevent deposition of raw sewage and grit and to prevent a buildup 

of floatables on the surface. Each primary settling tank has two longitudinal chain and flight 

sludge collectors/surface skimmers (one per bay) and one screw-type cross collector. 

The chain and flight collectors skim the surface to convey skimmings to a dipping weir at the 

downstream end of the primary settling tanks. Skimmings removal is initiated manually by 

visual inspection. The skimmings dipper discharges to an open channel that discharges to two 

pits located next to the primary settling tanks. The two skimmings pits both discharge to a 

common decanting pit. Several hours after a skimmings pit is filled, a telescoping subnatant 

valve is lowered slowly to transfer excess skimmings carrier liquid to the decanting pit. An 

overhead crane then lowers a 7 cubic foot clamshell bucket into the skimmings pit to lift 

concentrated skimmings to 6 cubic foot disposal containers, which are disposed of offsite. The 

skimmings pit underflow is continuously drained and returned to the head of the plant. 

Primary influent flow is measured by strap-on Doppler flow meters. Raw influent samples are 

taken from the primary influent channel. Samples are also taken from the primary effluent 

channel six times a day, five days per week and composited at the end of each day. Flow 

bypassing in the secondary system is measured using a Parshall flume, equipped with an 

ultrasonic level sensor. The sensor records measurements in a data logger that needs to be 

regularly downloaded. 

Current surface overflow rates are within typical design standards. The plant’s design surface 

overflow rate of 1,970 gpd/ft 2 is consistent with the New York City design criteria of 2,000 

gpd/ft 2 . Current weir overflow rates of 28,400 gpd/ft exceed typical design standards (such as 

15,000 gpd/ft for the Ten States Standard), but are within the plant’s design value of 50,500 

gpd/ft. New York City design criteria for surface overflow and weir overflow are significantly 

higher than industry design standards. 

Table 1-5 includes primary settling tank design criteria. Figure 1-4 is a schematic overview of 

the primary settling tank unit process. 

1-7



DRAFT 

Table 1-5: Primary Settling Tank Design Criteria 

Parameter 

Value 

Number of primary settling tanks 4 

• Number of Bays per Tank 2 

• Length (ft) 186 

• Width per Tank (ft) 41 

• Average Side Water Depth (ft) 12 

• Total Surface Area - All Tanks ( ft 2 ) 30,504 

• Weir Length – All Tanks (ft) 1,188 

Number of Skimmings Pits 2 

• Maximum Length (ft) 6 

• Maximum Width (ft) 6 

• Maximum Depth (ft) 14 

• Volume Per Well (ft 3 ) 480 

Figure 1-4: Primary Settling Tank Schematic Overview 

1.2.4 Primary Sludge Pumping and Degritting 

Primary sludge is conveyed by chain and flight mechanisms in each primary settling tank bay 

into a collector channel and then by a cross collector into a common sludge sump pit for each 

tank. Six primary sludge pumps, located in the primary tank gallery, are operated continuously 

to prevent sludge blanket buildup in the primary settling tanks. The pumps are organized in 

series of three, with pumps 1-3 dedicated to primary settling tanks 1 and 2 and pumps 4-6 

1-8



DRAFT 

dedicated to primary settling tanks 3 and 4. Generally, two pumps per set are in service while 

the other two are in standby. Occasionally, one pump per set is operated. The primary sludge 

pumps were replaced in 1988; each pump generally operates at 600 gpm. 

Primary sludge is pumped to five cyclone/classifier units. Normally, one unit is dedicated to 

each operating sludge pump, with an extra unit in standby. Each cyclone discharges to one 

washer/classifier. The cyclone degritters are sized to remove grit of 150 mesh and larger. The 

washer/classifiers currently do not use wash water. Each washer/classifier discharges into 1.5 

cubic yard satellite containers, which are transferred into nominal 20 and 26 cubic yard 

containers, where they are combined with screenings and hauled off site. 

Degritted primary sludge passes through a secondary screen and flows by gravity into a wet well, 

where it is pumped by three centrifugal pumps (one duty and two standby) to the gravity 

thickener distribution box. The overflow pipe from this wet well drains to the headworks just 

downstream of the bar screens. 

Primary sludge flow is neither metered nor sampled. Grit is measured by the number of 20 and 

26 cubic yard boxes that are filled. 

Table 1-6 provides primary sludge pumping and degritting design criteria. 

Table 1-6: Primary Sludge Pumping and Degritting Design Criteria 

Parameter 

Value 

Number of Primary Sludge Pumps 

6 (4 duty, 2 standby) 

• Type Torque-Flow 

• Capacity (gpm) 300 @ 76 ft, 600 @ 65 ft 

• TDH (ft) 65 - 76 

• Unit HP (hp) 30 

Number of Classifiers 


• Classifier Type Rake 

• Number of Cyclones per Classifier 1 

• Cyclone Capacity, Each (gpm) 550 

• Design Grit Removal Mesh Size 150 

Number of Degritted Primary Sludge Pumps 


• Type Centrifugal – Mixed Flow 

• Capacity (gpm) 1,300 

• TDH (ft) 44 


1.2.5 Aeration 

The aeration system consists of four aeration tanks, each comprised of four passes arranged in a 

serpentine manner. Primary effluent enters the aeration tank influent chamber where it mixes 

with gravity thickener and elutriator overflow and is distributed to one of the two influent 

channels. The tanks operate via the step-feed aeration process; primary effluent can enter any of 

1-9



DRAFT 

the four passes through two 72 by 48 inch motor operated sluice gates, located at the head end of 

each pass. Primary effluent is designed to be evenly distributed to passes B, C, and D. Return 

Activated Sludge (RAS) is pumped to a return sludge channel, from which it enters pass A of the 

aeration tanks. Aerator effluent is discharged from pass D through two 36 by 68 inch motor 

operated sluice gates per tank and flows to the final settling tank influent channel. An aeration 

tank flow schematic is presented in Figure 1-5. 

Figure 1-5: Aeration Tank Flow Schematic 

Spray water is used to control frothing problems; it is only used approximately six times a year 

for a maximum of a week at a time. Process air is compressed by air blowers and discharged to a 

54-inch diameter common header. Port Richmond uses fine-pore ceramic tube diffusers which 

are currently being replaced in each aeration tank. Process air is also withdrawn from the main 

header to aerate the primary influent and effluent channels and the final settling tank influent 

channel. Dissolved oxygen levels are manually controlled by adjusting blower inlet guide vanes. 

Typically, one blower is operational and the remaining two are on standby. The fourth blower is 

not operational. 

Mixed liquor suspended solids (MLSS) concentrations are sampled at the midpoint of each pass 

once a day, four days a week. The four samples are composited, and reported as average aerator 

MLSS for each aeration tank. The aerator effluent MLSS is sampled from the end of Pass D of 

each aeration tank six times a day, four days a week, and composited at the end of each day. 

Dissolved oxygen concentrations at the end of Pass D of each aeration tank is monitored four 

times daily. Reported air flow rates are based on blower vane setting charts. 

1-10



DRAFT 

Table 1-7 details design criteria for the aeration system. 

Table 1-7: Aeration System Design Criteria 

Parameter 

Value 

Number of Aeration Tanks 4 

• Number of Passes per Tank 4 

• Length (ft) 263 

• Width per Pass (ft) 26 

• Average Side Water Depth (ft) 17.4 

• Total Volume, All Tanks (MG) 14.2 

Number of Blowers 4 

• Rated Capacity (cfm) 24,000 

• Discharge Pressure (psig) 9 

• Unit HP (hp) 1,250 

• Diameter of Diffuser Tubes (in) 1.75 

• Number of Manifolds per Tank 296 

• Number of Diffuser Tubes per Tank 12,108 

• Average Height Above Bottom (ft) 2 

Figure 1-6 shows the average aerator MLSS concentration. 

Figure 1-6: Average Aerator MLSS Concentrations 

The plant typically operated with a mixed liquor concentration between 1,500 and 2,000 mg/L 

(with periods as high as 3,000 mg/L). The introduction of the Visy Paper load forced a reduction 

in operating MLSS concentrations, which decreased Nitrogen removal rates. Since March 1998, 

AEMLSS concentrations have been fairly constant. 

Port Richmond has a longer design HRT (5.7 hours) than most NYC plants (3-3.5 hours). The 

Solids Retention Time: 

1-11



DRAFT 

V 

AT 

 

X 

AvgAer 

 

Q 

X 

 

Q Q 

WAS 

WAS 

Inf 

WAS 

X 

eff 

 

and Gould Sludge Age: 

V 

 

X 

 

 

Q 

AT 

AerInf 

X 

MLSS 

AerInf 

 

are within normal industry standards. The design Gould Sludge Age at Port Richmond is 3-6 

days, and the typical design for New York City plants is 3-5 days. The Visy Paper load forced a 

reduction in Gould Sludge Age from 10 to 15 days to only 4.2 days on average. Plant operations 

personnel target a minimum Dissolved Oxygen (DO) concentration of 5.0 mg/L in order to 

handle peak organic loads from Visy Paper. Table 1-8 details the aeration system operating 

parameters between November 1999 and October 2001. 

Table 1-8: Aeration System Operating Parameters 

Parameter Port Richmond 

Current 

Port Richmond 

Design 

NYCDEP Typical 

Design Standards 

Operations 

AEMLSS (mg/L) 890 3,900 1,500-2,500 

BOD 5 Loading 

(lb BOD 5 / 1000 ft 3 ) 

21.9 45.2 50 

HRT, average (hr) 8.0 5.7 3-3.5 

HRT, min flow (hr) 10.1 - - 

HRT, max flow (hr) 3.4 - - 

SRT (days) 5 5-7 - 

Gould Sludge Age (days) 4.2 3-6 3-5 

F/M Ratio 0.48 0.25-0.5 0.25-0.33 

SVI (mL/g) 121 100 100 

Effluent DO (mg/L) 5.6 2.0-3.0 - 

Air Flow (mcf) 74.7 78.1 - 

1.2.6 Final Settling Tanks 

There are six final settling tanks, each of which is divided into three bays. Final settling tanks 

are equipped with sludge collectors, surface skimming mechanisms, inlet sluice gates, inlet 

baffles, and overflow weirs. Aeration tank effluent is fed to the final settling tanks by two sideby-side 

aerated final settling tank influent channels through two 3-foot square slide gates per 

bay. Flow is controlled by varying the inlet gate openings. Final settling tank effluent 

discharges over weirs into the final settling tank effluent channel. 

The plant currently takes waste sludge from the aerator effluent channel. The plant also has the 

capability to withdraw RAS from the final settling tanks using hydrostatic lifts. Sludge is 

collected by means of a chain and flight collector to a center channel, and is then moved by a 

cross collector to two hoppers. Each hopper has a hydrostatic lift pipe that collects RAS from a 

1-12



DRAFT 

set of three final settling tanks and discharges into the RAS wet well. Skimmings are collected 

once per shift using the manually operated dipping weirs. 

Final settling tank effluent flow is measured by a Parshall flume, which has been used to report 

plant flows since January 1999. The secondary bypass enters the final settling tank effluent 

channel upstream of the Parshall flume. 

The Staten Island Infrastructure Study concluded that the Port Richmond final settling tanks are 

underloaded. The final settling tanks were operated at higher solids loading rates prior to the 

introduction of the Visy Paper load in 1997. The average solids loading rate on the final settling 

tanks during the infrastructure investigation was 3.8 pounds per square foot per day; plants are 

usually designed for a loading between 20 and 30 pounds per square foot per day. Table 1-9 

details final settling tank design criteria. 

Table 1-9: Final Settling Tank Design Criteria 

Parameter 

Value 

Number of Tanks 6 

Number of Bays Per Tank 3 

Length (ft) 298 

Width Per Tank (ft) 45 

Average Side Water Depth (ft) 10.8 

Total Volume, All Tanks (ft 3 ) 869,000 

Surface Area, All Tanks (ft 2 ) 80,460 

Weir Length, All Tanks (ft) 1,980 

1.2.7 Disinfection and Outfall 

A schematic of the chlorination facilities is shown in Figure 1-7 

1-13



DRAFT 

Figure 1-7: Schematic Overview of Chlorination Facilities 

Disinfection is provided through chlorination of the final settling tank effluent. Each of two 

chlorine contact tanks is comprised of three passes. Two sluice gates control the influent to each 

tank. Chlorine tank effluent exits over weirs at the end of the third pass and enters the plant 

outfall that discharges to Kill Van Kull. 

The sodium hypochlorite (hypo) feed system is located in the sludge pumping and chlorination 

building and consists of three 12,000-gallon FRP storage tanks, three transfer pumps, three 

volumetric liquid feeders, and a dilution water system. Hypo solution is delivered at 15 percent 

concentration by truck. Hypo consumption increased considerably in 1997 with the introduction 

of the Visy paper load. There are two peristaltic hypo metering pumps and one centrifugal-type 

backup pump, which draw from a common header that serves all three storage tanks. One of the 

pumps constantly feeds chlorine to the RAS well to help control the growth of filamentous 

organisms. The other metering pump delivers chlorine to the three (two duty, one standby) 

volumetric feeders. The feeders are manually adjusted to achieve the target chlorine residual of 

1.3 mg/L. Any overflow from the return header of excess hypo solution is returned to the 

1-14



DRAFT 

suction side of the hypo feed pumps. Two centrifugal pumps provide plant effluent water into 

which hypo is fed. There is also a 1,000-gallon emergency hypo tank adjacent to the final 

settling tank effluent channel which can be used in the event of a disinfection system 

interruption. This system, which is connected to emergency power, can dose final settling tank 

effluent for 8 to 12 hours. 

Plant data indicates average retention time in the chlorine contact tanks at 71.2 minutes, well 

beyond typical design standards. Table 1-10 details disinfection system design criteria. 

Table 1-10: Disinfection System Design Criteria 

Parameter 

Value 

Number of Chlorine Contact Tanks 2 

• Passes Per Tank 3 

• Length Per Pass (ft) 233.4 

• Width Per Pass (ft) 14 

• Average Side Water Depth (ft) 11.13 

• Total Volume, All Tanks (MG) 1.63 

• Weir Length, Per Tank (ft) 260 

Number of Hypo Tanks 3 

• Material FRP 

• Nominal Capacity, Each (gallons) 12,000 

• Diameter (ft) 12 

• Height (ft) 13.38 

Number of Hypo Transfer Pumps 2,1 

• Type Peristaltic, Centrifugal 

• Capacity, Each (gpm) 2.5 


• Unit HP (hp) 0.75 

Number of Volumetric Feeders 3 



Number of Dilution Water Pumps 2 

• Type Centrifugal 


• TDH (ft) 35 


Plant Outfall Length (ft) 524 

• Diameter (in) 96 

Samples from the chlorine contact tank influent and effluent channels are collected hourly via 

sample pumps to monitor the influent and effluent chlorine residuals. Fecal Coliform samples 

are collected once per day from the effluent sample pump. A small amount of plant effluent is 

pumped from the chlorine contact tank effluent channel to the chlorination building, where it is 

collected by an auto-sampler. 

1-15



DRAFT 

1.2.8 Return Activated Sludge 

Return Activated Sludge (RAS) is withdrawn from the final settling tanks. RAS is pumped from 

the wet well to a return sludge distribution channel by five centrifugal pumps, 3 constant speed 

and 2 variable speed. One constant speed pump and one variable speed pump are typically 

operated. From the distribution channel, return sludge enters eight sight wells located at the head 

of pass A of each aeration tank through two 24 X 24 inch sluice gates per sight well. 

RAS flow has been chlorinated for filamentous organism control since 1998. The RAS wet well 

overflow pipe discharges into the waste sludge wet well through a Kennison nozzle. The plant is 

not provided with a RAS flow meter. RAS is sampled six times per day, four days a week. 

Samples are typically taken from one of the RAS sight wells. The samples are composited at the 

end of the day. 

The maximum total RAS pump capacity is 32.8 mgd, which represents 55 percent of the design 

plant flow. This is not an operational problem given the plant receives approximately 50 percent 

of its design flow, but it should be noted that the RAS pump capacity is below current design 

standards. 

The RAS typically averages a 2,470 mg/L solids concentration. Table 1-11 details RAS pump 

design criteria. 

Table 1-11: RAS Pump Design Criteria 

Type Constant Speed Variable Speed 

Number 3 2 

• Capacity, Each (gpm) 5,700 3,750 to 5,700 

• TDH (ft) 13 13 

• Motor HP (hp) 30 30 

1.2.9 Waste Activated Sludge/Mixed Liquor 

The activated sludge process at Port Richmond is controlled by maintaining a target MLSS 

concentration and Gould sludge age. The waste sludge wet well receives waste mixed liquor, 

final settling tank underflow, and final settling tank effluent for thickener balance water. 

Currently, sludge is only wasted from the mixed liquor channel. The waste sludge and balance 

water mixture are pumped to the thickeners by three (one duty, two standby) horizontal, nonclog, 

variable speed, centrifugal waste sludge pumps. Only one pump is operating under normal 

conditions. The capacity of each pump is between 2,000 and 6,000 gallons per minute. Each 

pump is powered by a 50 horsepower motor, creating a total dynamic head of 20-39 feet. 

The waste mixed liquor line has a magnetic flow meter. The plant has no means of controlling 

or metering the balance water flow rate. The lack of flow metering makes process control and 

the development of accurate mass balances difficult. 

1.2.10 Sludge Thickening and Elutriation 

1-16



DRAFT 

The plant has four tanks dedicated to gravity thickening and two smaller tanks for elutriation. 

Typically, two gravity thickeners are in operation and two are used for stand-by. All tanks are 

circular, conical-bottom tanks. The general arrangement of the sludge thickening facilities is 

shown in Figure 1-8. 

Figure 1-8: Arrangement of the Sludge Thickening Facilities 

Gravity thickener feed flows to the thickener splitter box, from which sludge is distributed 

amongst the operating thickeners. Within the thickeners, most of the solids settle to the bottom 

by gravity while the released liquor flows radially outward. Thickener overflow passes through 

V-notch weirs and flows by gravity to the primary effluent channel. Rake mechanisms move 

settled sludge to a pit at the bottom of each tank. One duty and one standby plunger pump are 

installed per thickener to pump thickened sludge to one of two digester heating loops. The 

thickened sludge pumps are cycled on and off manually to maintain a consistent sludge blanket 

depth between two and three feet. 

Elutriation washes Nitrogen from the digested sludge and decreases the sludge Nitrogen load on 

the WPCP that accepts Port Richmond visitor sludge. The elutriation feed consists of digested 

1-17



DRAFT 

sludge and plant effluent for balance water. Sludge is pumped from the secondary digester to the 

sludge distribution box, which is equipped with stop logs to keep the digested sludge separate 

from the waste sludge that is sent to the thickeners. Overflow from the elutriators is returned by 

gravity to the primary effluent channel, while the elutriated sludge is pumped back to the 

anaerobic digesters. Settled elutriated sludge is also pumped to one of two digester heating 

loops. A sludge blanket depth of 2.5 to 3.5 feet is generally maintained in the elutriators. 

Both thickener and elutriator overflow are sampled six times a day, four days a week from the 

overflow weirs. The samples are composited and reported as separate values for each overflow 

stream. Neither overflow stream is metered. Thickened and elutriated sludge flows are sampled 

six times a day from the pump discharge. Reported flow is calculated based on pump capacity 

and run time. 

Table 1-12 illustrates sludge thickening system design criteria 

Table 1-12: Sludge Thickening System Design Criteria 

Parameter 

Value 

Number of Gravity Thickeners 


• Diameter (ft) 70 

• Center Cone Depth (ft) 8 

• Surface Area per Tank (ft 2 ) 3,850 

Number of Elutriation Tanks 2 

• Elutriator Diameter (ft) 56 

• Center Cone Depth (ft) 6.4 

• Surface Area Per Tank (ft 2 ) 2,460 

Number of Thickened and Elutriated Sludge Pumps 12 

• Type Triplex Plunger 

• Capacity of Each (gpm) 150 

• TDH (ft) 231 


Number of Elutriator Feed Pumps 2 

• Type Duplex Plunger 


• TDH (ft) 231 


Number of Elutriator Balance Water Pumps 1 


• Capacity (gpm) 680 

• TDH (ft) 61 

• Unit HP (hp) 1,150 

The current thickener solids loading rate is 5.2ppd/ft 2 , which is within the design value of 

7.8ppd/ft 2 . However, the surface overflow rate is 1,250gpd/ft 2 , which is higher than the design 

surface overflow rate of 600gpd/ft 2 . The thickener solids loading rate decreased substantially 

after the introduction of the elutriation process as a result of the decreased primary influent 

1-18



DRAFT 

concentration and a decrease in primary sludge removal. The thickeners generally produce 

sludge with a solids content between 2.0 and 3.7 percent, with an average of 2.7 percent. This 

poor thickener performance has increased the hydraulic loading on the digesters, and thus 

impacted the plant’s ability to consistently meet PSRP. 

Figure 1-9 is a mass balance on the elutriators based on data collected from November 2000 to 

October 2001. This was the first year of plant operation inclusive of the Visy Paper wastewater 

load and the digested sludge elutriation process. Note, the elutriated sludge flow seems very 

low. 

Port Richmond- 

Elutriation Process 

Thickened 

Sludge 

Primary 

Digesters (2) 

Secondary 

Digester (1) 

To Storage 

Digested Sludge 

Elutriated Sludge 

Balance Water 

M 

Elutriators 

(2) 

Elutriator Overflow 

To Aeration Tanks 

Summary 

## DEP Data 

## Mass Balance Assumption 

Field Program Data: 10/28/02 thru 12/5/02 

M 

Temporary Flow Meter 

Figure 1-9: Mass Balance on Elutriators 

Figure 1-10 is a mass balance on the sludge thickening process based on data collected from 

November 2000 to October 2001. 

1-19



DRAFT 

Port Richmond- 

Sludge Thickening Process 

WAS 

Waste 

ML 

M 

Degritted 

Primary Sludge 

Wet Well 

M 

M 

WAS 

Wetwell 

M 

Balance Water 

Thickener Splitter 

Box 

Thickener Overflow 

Gravity 

Thickeners (2) 

Summary 

Thickened Sludge 

## DEP Data 

M Temporary Flow Meter ## Mass Balance Assumption 

1.2.11 Anaerobic Digestion 

Primary 

Digesters (2) 

Figure 1-10: Mass Balance on Sludge Thickening 

Field Program Data: 10/28/02 thru 12/5/02 

The plant has three fixed-cover circular anaerobic digesters. Digesters 1 and 2 accept thickened 

sludge from gravity thickeners, while digester 3 is operated as a secondary digester and accepts 

overflow from digesters 1 and 2. Digesters 1 and 2 are mixed and heated, digester 3 is not. 

Sludge can be transferred by gravity between any of the digesters. A plunger-type pump is used 

to transfer sludge from the secondary digester back to the elutriators. A schematic of the digester 

process is provided in Figure 1-11. 

1-20



DRAFT 

Figure 1-11: Schematic of the Digestion Process 

Sludge from the primary digesters overflows by gravity to the secondary digester. The sludge 

level in the secondary digester is carefully maintained; if it rises too high, the primary digesters 

overflow to the plant drain. Operators report this is a rare occurrence at the plant. 

Thickened and elutriated sludge is mixed with recirculating heated digester sludge downstream 

of the heat exchangers and transferred to the primary digesters via two sludge heating loops. 

Any of the digesters can be connected to either heating loop. The digesters were originally 

equipped with a gas mixing system, but this system is no longer in use. The only mixing 

achieved is via the sludge heating loops. Digester gas is withdrawn from each digester and sent 

1-21



DRAFT 

either to the gas boosters or the waste gas burner. The plant’s Wiggins-type gas holder is in poor 

condition and has not been in operation since 1994. A small amount of plant effluent water is 

pumped to the waste heat exchangers through two centrifugal 400 gpm pumps, one duty and one 

standby. 

Table 1-13 details the digestion system design criteria 

Table 1-13: Digester System Design Criteria 

Parameter 

Value 

Number of Primary Digesters 2 

• Volume of Each Primary Digester (MG) 1.51 

Number of Secondary Digesters 1 

• Volume of Secondary Digester (MG) 1.44 

Number of Sludge Heat Exchangers 2 

• Type of Sludge Heat Exchangers Tube-in-tube 

• Capacity of Each (BTU/hr) 3,500,000 

Number of Sludge Heating Pumps 


• Type Torque Flow, Centrifugal 


• TDH (ft) 33 


Number of Gas Boosters 4 

• Type Rotary 

• Capacity of Each (cfm) 167 



Number of Hot Water Pumps 2 


• Capacity of each (gpm) 350 

• TDH (ft) 55 


Number of Waste Heat Pumps 




• TDH (ft) 35 


Number of waste heat exchangers 3 

• Type Tube-in-tube 

Number of waste gas burners 1 

Digested sludge is sampled once per day from the discharge of the sludge transfer pump. 

Digested sludge flow rate is reported based on the operation of the digested sludge pumps. The 

flow rate of the digested sludge to elutriation is determined from run time records of the plunger 

pumps used to transfer sludge. The majority of anaerobic digester performance characteristics 

falls within typical design standards. A review of plant data shows that prior to the introduction 

1-22



DRAFT 

of the elutriation process, hydraulic residence time in the digesters frequently fell below the 15 

days required to meet PSRP. The inability to provide adequate detention time could become an 

issue if the plant discontinued the elutriation process. In the absence of a functioning gas mixing 

system, digester mixing is provided only by the heating system and is not adequate. Also, gas 

piping that transfers digester gas from the gas boosters to the boilers is leaking. 

Table 1-14 shows the anaerobic digester performance compared to the design information for 

Port Richmond’s digesters. 

Table 1-14: Anaerobic Digester Performance 

Average Value 

Design 

Plant Flow (mgd) 37.5 60 

Temperature (ºF) 98.5 90-95 

TS Loading (lb/d) 48,600 93,000 

Volatile Solids loading rate (lb VSS/1,000ft 3 ) 95 160 

Volatile Solids destruction (%) 70 50 

HRT (days) 26.7 19.9 

Digested Sludge to Storage (mgd) 0.13 .22 

Gas Production (mcf) 272 535 

1.2.12 Sludge Storage and Transfer 

There are two sludge storage tanks at Port Richmond. The older tank is in poor structural 

condition and is not used. Four pumps are available to transfer sludge from the digesters to the 

operable storage tank, which has a maximum capacity of 121,060 cubic feet of sludge. Port 

Richmond sludge is barged to other WPCPs for dewatering and centrate treatment. 

1.2.13 Summary of Plant Operations 

Table 1-15 shows a summary of the existing facilities and equipment at the Port Richmond 

WPCP. 

Opening 

Upgrade 

Tributary Area 

Table 1-15: Port Richmond WPCP Existing Facility Description 

Description Units Value 

General 

1953 – Primary Treatment 

1979 – Secondary Treatment 

9,665 acres on northern half of Staten Island 

Flows 

Actual Daily Average (FY 2002-2005) mgd 33 

Design Dry Weather Flow mgd 60 

Design Secondary Treatment Flow mgd 90 

Design Wet Weather Flow mgd 120 

1-23



DRAFT 


Maximum Daily Flow mgd 104 

Maximum Hourly Flow mgd 130 

Screening 

Number of Bar Screens 3 

Width ft 5 

Clear Opening in 7/8 

Inclination from Horizontal degrees 84 

Main Sewage Pumps 

Number of MSPs 6 

Type 

Mixed Flow, Centrifugal 

Pump Speed rpm 500 – 585 

Capacity mgd 17 – 30 

TDH ft 34 -38.5 

Motor Horsepower hp 250 

Ring Flush Pumps 

Number 2 

Type 

Mixed Flow, Centrifugal 

Pump Speed rpm 900 

Capacity gpm 470 

TDH ft 43 


Primary Settling Tanks 

Number 4 

Number of Bays per Tank 2 

Length ft 186 

Width per Tank ft 41 

Average Side Water Depth ft 12 

Total Surface Area - All Tanks ft 2 30,504 

Weir Length – All Tanks ft 1,188 

Skimmings Pits 

Number 2 

Maximum Length ft 6 

Maximum Width ft 6 

Maximum Depth ft 14 

Volume Per Well ft 3 480 

Number 

Primary Sludge Pumps 

1-24 

6 (4 duty, 2 standby)



DRAFT 


Type 

Torque-Flow 

Capacity gpm 300 @ 76 ft, 600 @ 65 ft 

TDH ft 65 - 76 

Unit HP hp 30 

Classifiers 

Number 


Type 

Rake 

Number of Cyclones per Classifier 1 

Cyclone Capacity, Each 550 

Design Grit Removal Mesh Size 150 

Degritted Primary Sludge Pumps 

Number 


Type 

Centrifugal – Mixed Flow 

Capacity gpm 1,300 

TDH ft 44 

Unit HP hp 50 

Aeration Tanks 

Number 4 

Number of Passes per Tank 4 

Length ft 263 

Width per Pass ft 26 

Average Side Water Depth ft 17.4 

Total Volume, All Tanks MG 14.2 

Blowers 

Number 4 

Rated Capacity scfm 24,000 

Discharge Pressure psig 9 

Unit HP hp 1,250 

Diameter of Diffuser Tubes in 1.75 

Number of Manifolds per Tank 296 

Number of Diffuser Tubes per Tank 12,108 

Average Height Above Bottom ft 2 

Final Settling Tanks 

Number 6 


Length ft 298 

Width Per Tank ft 45 

1-25



DRAFT 



Total Volume, All Tanks ft 3 869,000 

Surface Area, All Tanks ft 2 80,460 

Weir Length, All Tanks ft 1,980 

RAS Pumps 

Type 

Constant and Variable Speed 

Number 

5 (3 constant speed, 2 variable speed) 

Capacity, each mgd 8.2 

WAS Pumps 

Type 

Horizontal, non-clog 

Number 


Capacity mgd 8.6 

Chlorine Contact Tanks 

Number 2 

Passes Per Tank 3 

Length Per Pass ft 233 

Width Per Pass ft 14 



Weir Length, Per Tank ft 260 

Hypo Tanks 

Number 3 

Material 

FRP 

Nominal Capacity, Each gal 12,000 

Diameter ft 12 

Height ft 13.38 

Hypo Transfer Pumps 

Number 2,1 

Type 

Peristaltic, Centrifugal 

Capacity, Each gpm 2.5 


Unit HP hp 0.75 

Volumetric Feeders 

Number 3 



Dilution Water Pumps 

1-26



DRAFT 


Number 2 

Type 

Centrifugal 


TDH ft 35 


Plant Outfall 

Location 

Kill Van Kull 

Length ft 524 

Diameter in 96 

Gravity Thickeners 

Number 



Center Cone Depth ft 8 

Surface Area per Tank ft 2 3,850 

Elutriation Tanks 

Number 2 

Elutriator Diameter ft 56 

Center Cone Depth ft 6.4 

Surface Area Per Tank ft 2 2,460 

Thickened and Elutriated Sludge Pumps 

Number 12 

Type 

Triplex Plunger 

Capacity of Each gpm 150 

TDH ft 231 

Unit HP hp 30 

Elutriator Feed Pumps 

Number 2 

Type 

Duplex Plunger 

Capacity of Each (gpm) gpm 150 

TDH (ft) ft 231 

Unit HP (hp) hp 8.5 

Elutriator Balance Water Pumps 

Number 1 

Type 

Centrifugal 


TDH ft 61 

Unit HP hp 1,150 

1-27



DRAFT 


Digesters 


Volume (each) MG 1.51 


Volume (each) MG 1.44 

Sludge Heat Exchangers 

Number 2 

Type 

Tube-in-tube 

Capacity of Each BTU/hr 3,500,000 

Sludge Heating Pumps 

Number 


Type 

Torque Flow, Centrifugal 

Capacity (each) gpm 700 

TDH ft 33 

Unit HP hp 25 

Gas Boosters 

Number 4 

Type 

Rotary 

Capacity (each) cfm 167 


Unit HP hp 15 

Hot Water Pumps 

Number 2 

Type 

Centrifugal 


TDH ft 55 

Unit HP hp 10 

Waste Heat Pumps 

Number 


Type 

Centrifugal 


TDH ft 35 

Unit HP hp 900 

Waste Heat Exchangers 

Number 3 

Type 

Tube-in-tube 

1-28



DRAFT 

1.3 Ongoing and Planned Upgrades 

There is no ongoing work or planned upgrades at the Port Richmond WPCP. 

1-29



DRAFT 

2 MASS BALANCE DIAGRAMS 

Plant wide process flow diagrams and mass balances for each level of treatment described in 

Section 2.0 are included in the attached drawing packet in Appendix B. The nodes identified 

along the top of each drawing correspond to those shown in the process flow diagram. 

2-1



DRAFT 

3 BASIS OF DESIGN 

The basis of design presented in the following sections is broken down by process technology, 

beginning with Existing Conditions with Solids Filtration and moving through each level of 

technology. For both the Base Case and Existing Conditions levels of technology, it is assumed 

that no modifications to the plant’s infrastructure or processes will be made. 

An analysis of each treatment step or component will be presented for the different process 

technologies, including: 

• Primary Settling Tanks 

• Screening 

• Aeration Tanks 

Flow Distribution and Control 

Baffles and Zone Sizing 

Anoxic Zone Mixers 

Air Distribution and Control 

Diffusers 

• Process Aeration System 

• Final Settling Tanks 

• Return Activated Sludge System 

• Waste Activated Sludge System 

• Froth Control 

Froth Control Hoods 

RAS Chlorination 

Surface Wasting 

• Chemical Facilities 

Alkalinity 

Carbon 

• Intermediate Pumping Station 

• Tertiary Treatment 



Denitrification Filters 

• Membrane Bioreactors 

• Odor Control 

Any new facilities to be constructed in the following conceptual designs are assumed to be 

constructed to the latest New York State building codes. A placeholder cost is included for 

foundation work assuming average subsurface conditions, however, detailed pile/caisson design 

is not realistic for a conceptual design report that lacks boring logs and a detailed subsurface 

analysis. 

In addition, any new construction is assumed to be in accordance with all requirements and 

conditions regarding wetlands encroachment: remaining 150 feet horizontal or 10 feet vertical 

from the nearest wetlands. 

3-1



DRAFT 

4 EXISTING CONDITIONS WITH SOLIDS FILTRATION 

4.1 Primary Settling Tanks 

A description of Port Richmond’s PSTs was provided in Section 1. The principal function of the 

primary settling tanks is to removal particulate material to reduce the load on the secondary 

system. In addition, the PSTs contribute to the overall hydraulic profile of the facility. In order 

to implement improvements in downstream facilities such as increased screening and aeration 

tank flow distribution, minor modifications may be needed that may have limited impacts on 

plant hydraulics. For the Existing Conditions with Solids Filtration level of technology, there are 

no modifications necessary. 

4.2 Fine Screens 

There are currently no fine screening units installed at the Port Richmond WPCP. No fine 

screens are needed for the Existing Conditions with Solids Filtration level of technology. 

4.3 Aeration Tanks 

A description of Port Richmond’s Aeration Tanks was provided in Section 1. The principal 

function of the aeration tanks is to provide a reactor volume for the activated sludge to take up 

nutrients, thereby removing them from the wastewater. Several operational components of the 

aeration tanks are discussed below. 

4.3.1 Flow Distribution and Control 

Flow distribution and control is an important factor that can affect treatment performance. The 

constraints for flow distribution at Port Richmond WPCP include the existing hydraulic profile, 

tank size, channel internal structure, and flow requirements. There are no modifications for the 

flow distribution and control necessary for the Existing Conditions with Solids Filtration level of 

treatment. 

4.3.2 Baffles and Zone Sizing 

No baffle walls are necessary for the Existing Conditions with Solids Filtration level of 

treatment. 

4.3.3 Anoxic Zone Mixers 

No anoxic zone mixers will be installed for the Existing Conditions with Solids Filtration level 

of treatment. 

4.3.4 Air Distribution and Control 

Air distribution and control is an important factor that can affect treatment performance. There 

are no modifications for the air distribution and control necessary for the Existing Conditions 

with Solids Filtration level of treatment. 

4-1



DRAFT 

4.3.5 Diffusers 

Diffusers deliver process air to the aeration tanks and also provide a means to keep solids in 

suspension in aerated sections of the aeration tank. There are no modifications for the diffuser 

system necessary for the Existing Conditions with Solids Filtration level of treatment. 

4.4 Process Aeration System 

A description of Port Richmond’s Process Aeration System was provided in Section 1. The 

objective of the process aeration system is to ensure sufficient air is provided to the biomass. 

There are no modifications to the process aeration system necessary for the Existing Conditions 


4.5 Final Settling Tanks 

A description of Port Richmond’s Final Settling Tanks (FSTs) was provided in Section 1. The 

function of the FSTs is the removal of particulate material to provide high quality treated effluent 

and to return biomass to the aeration tanks to maintain the overall treatment process. No 

modifications to the Final Settling Tanks are needed for the Existing Conditions with Solids 

Filtration level of technology. 

4.6 Return Activated Sludge System 

A description of Port Richmond’s RAS system was provided in Section 1. The principal 

function of the RAS system is to maintain the solids inventory in the aeration tanks and return 

acclimated biomass to treatment. No modifications to the Return Activated Sludge System are 

needed for the Existing Conditions with Solids Filtration level of technology. 

4.7 Waste Activated Sludge System 

A description of Port Richmond’s WAS system was provided in Section 1. No modifications to 

the Waste Activated Sludge System are needed for the Existing Conditions with Solids Filtration 

level of technology. 

4.8 Froth Control 

4.8.1 Froth Control Hoods 

Currently, spray water is used to control frothing problems; it is only used approximately six 

times a year for a maximum of a week at a time. Froth Control Hoods are not recommended for 

the Existing Conditions with Solids Filtration level of technology. 

4.8.2 RAS Chlorination 

The Port Richmond WPCP has an existing sodium hypochlorite storage and feed system, which 

provides chlorine for effluent disinfection. The system houses 15% sodium hypochlorite in three 

12,000-gallon fiberglass reinforced plastic storage tanks. There are two peristaltic hypo 

4-2



DRAFT 

metering pumps and one centrifugal-type backup pump, which draw from a common header that 

serves all three storage tanks. One of the pumps constantly feeds chlorine to the RAS well to 

help control the growth of filamentous organisms. The other metering pump delivers chlorine to 

the three (two duty, one standby) volumetric feeders. The feeders are manually adjusted to 

achieve the target chlorine residual of 1.3 mg/L. No additional RAS chlorination measures are 

recommended for the Existing Conditions with Solids Filtration level of technology. 

4.8.3 Surface Wasting 

There is currently no surface wasting capabilities at the Port Richmond WPCP. Surface wasting 

is not recommended for the Existing Conditions with Solids Filtration level of technology. 

4.9 Chemical Facilities 

4.9.1 Alkalinity 

Alkalinity addition is not recommended for the Existing Conditions with Solids Filtration level 

of technology. 

4.9.2 Carbon 

Carbon addition is not recommended for the Existing Conditions with Solids Filtration level of 

technology. 

4.10 Intermediate Pumping Station 

An intermediate pump station will be provided for the Existing Conditions with Solids Filtration 

level of technology. It will be located in the North section of the WPCP near the filters and will 

provide eight feet of additional head to account for headlosses from this new add-on process 

technology. A sufficient number of pumps will be provided to pump 1.5 times the plant’s design 

dry weather flow capacity with an N+1+1 level of redundancy. These pumps will be placed 

inside a small headed building in parallel to each other. Best efforts were made to place this 

pumphouse in an accessible location to account for equipment maintenance and replacement. 

Emergency power will not be provided for this facility; in the event of a blackout, current 

NYCDEP policy calls for main sewage pumping, settling via PSTs, and chlorination along with 

the powering of vital EH&S assets. 

4.11 Tertiary Treatment 

4.11.1 Solids Filtration 

Solids filtration is a process that is installed down stream of a secondary treatment process to 

enhance removal of particulates within the wastewater, including solids, particulate BOD and 

TKN. The addition of conventional solids filtration after the final settling tanks will achieve 

lower levels of particulates in the waste stream. The objectives include: 

• Achieve low levels of solids (TSS = 4 mg/L to 5 mg/L) 

• Achieve low levels of carbonaceous matter (CBOD = 3 mg/L to 5 mg/L) 

4-3



DRAFT 

• Provide sufficient filter area to meet treatment goals 

Solids filters were designed for a maximum annual average flux rate of four gallons per minute 

per square foot and a max week flux rate of six gallons per minute per square foot. The solids 

filters will be placed downstream of the FSTs and upstream of disinfection at Port Richmond. 

This physical location of the new solids filtration tanks will be on the north side of the plant. A 

new structure will be constructed to house the associated equipment (pumps, blowers, etc.). 

Secondary effluent will be directed through a new conduit constructed from the Final Settling 

Tank Effluent channel to the solids filtration tanks and flow North by gravity to the newly 

constructed filters. The secondary effluent will be evenly applied to the filters at a constant flow 

rate per surface area and will be allowed to flow downward through the media. As the secondary 

effluent flows through the media, larger particulates will be physically filtered by the media. 

Filtered effluent will flow back to the existing disinfection system. 

To maintain the efficiency of the filters, periodic backwashing must be performed to remove the 

accumulated solids. Backwash will be discharged to the head of primary settling tanks and 

returned to the treatment process. Equipment will be provided that will flush the media by 

recycling the treated effluent to serve as wash water. A blower system will also be provided for 

air scouring of the media when the filter units are not operating in a downward flow mode. The 

reused effluent and released solids will then be pumped to the gravity thickeners. 

The Team assumes twenty percent of the filters will be offline at any given time for backwash 

and O&M requirements. This translates to a design surface area of 7,276 square feet. The team 

assumes rectangular solids filters, with each filter providing 610 square feet of contact surface 

area. A total of 12 of these filters will be provided. Sand will be the medium of choice. The 

team assumes a grain size of 2 mm and a filter depth of 6 feet. 

The Team assumes a dual water/air backwash system. The team assumes a water backwash rate 

of 6 gallons per square foot per minute and an air backwash rate of 5 cubic feet per square foot of 

filter per minute. To provide for backwash needs, three water backwash pumps will be provided, 

each with a capacity of 4,400 gallons per minute. These pumps will provide 35 feet of total 

dynamic head. 50 horsepower motors will be provided. A total of three scour air blowers will 

be provided, each with a capacity of 3,650 scfm. 

4.11.2 Microfiltration/Ultrafiltration 

No Microfilters/Ultrafilters are needed for the Existing Conditions with Solids Filtration level of 

technology. 

4.11.3 Denitrification Filters 

No Denitrification Filters are needed for the Existing Conditions with Solids Filtration level of 

technology. 

4.12 Membrane Bioreactors 

4-4



DRAFT 

No Membrane Bioreactors are needed for the Existing Conditions with Solids Filtration level of 

technology. 

4.13 Odor Control 

Odor control regulations are becoming increasingly restrictive for New York City WPCPs. The 

City’s Bureau of Environmental Planning and Design (BEPA) is in charge of providing an 

internal environmental evaluation of NYCDEP projects. The four aeration basins at the Port 

Richmond WPCP are located indoors as an odor control provision. No additional odor control 

measures are needed for the Existing Conditions with Solids Filtration level of technology. 

4-5



DRAFT 

5 EXISTING CONDITIONS WITH 

MICROFILTRATION/ULTRAFILTRATION 


No modifications to the Primary Settling Tanks are needed for the Existing Conditions with 

Microfiltration/Ultrafiltration level of technology. 


Microfiltration/Ultrafiltration technologies require more-advanced removal of secondary effluent 

solids than is typically achieved in the final settling tanks. Fine screens can be used to remove 

solids from secondary effluent that may cause clogging of the membranes reducing their 

treatment efficiency and increasing maintenance requirements. 

The design objectives of the fine screening process for Microfilters/Ultrafilters include: 

• Remove particles larger than 2 mm from secondary effluent 

• Collect screened solids and remove them from the plant 

• Account for typical variations in wastewater flows 

The proposed design for the fine screening process at the Port Richmond WPCP consists of an 

installation of secondary effluent screens in the secondary effluent channel, immediately 

upstream of the intermediate pump station prior to the Microfiltration/Ultrafiltration tanks. 

The Team assumes Jones and Atwood band screens will be selected for the 2 mm screens. Each 

screen has a design capacity of 15 mgd and assumes discharge velocity of 0.87 feet per second. 

The Team assumes a channel depth of 11 feet and a width (per screen) of 12 feet. Provisions 

will be made for a bypass around the screens in case of fouling, however the number of screens 

was designed conservatively in order to minimize fouling and required plant Operations and 

Maintenance (O&M) activities. Through information supplied by the manufacturer, the 

anticipated solids removal rate is 15 cubic feet per screen per hour. This volume was used to 

calculate the additional screenings processing infrastructure needed as well as the impact on the 

O&M disposal costs for grit. 

A total of 12 secondary screens will be installed: two in-service screens will be provided for each 

secondary settling tank, and one spare screen for each tank will be stored in the event a screen 

must be replaced. Screen reject will be sent to solids handling through the waste sludge line. 

Each screening unit will be connected to a spray water system to remove the collected screenings 

from the screen panels. The spray water system will be connected to the plant’s existing effluent 

water system or will utilize the screening effluent to wash the screen panels. The screenings 

residuals and washwater will be discharged to a collection trough and will flow by gravity to a 

wet well from where it will be pumped to the sludge thickeners. The screens are of sufficient 

capacity that two would be sufficient under a max flow condition, with one screen per tank 

offline for O&M. 

5-1



DRAFT 



There are no modifications for the flow distribution and control necessary for the Existing 

Conditions with Microfiltration/Ultrafiltration level of treatment. 


No baffle walls are necessary for the Existing Conditions with Microfiltration/Ultrafiltration 

level of treatment. 


No anoxic zone mixers will be installed for the Existing Conditions with 

Microfiltration/Ultrafiltration level of treatment. 


There are no modifications for the air distribution and control necessary for the Existing 



There are no modifications for the diffuser system necessary for the Existing Conditions with 




with Microfiltration/Ultrafiltration level of treatment. 


No modifications to the Final Settling Tanks are needed for the Existing Conditions with 



No modifications to the Return Activated Sludge System are needed for the Existing Conditions 

with Microfiltration/Ultrafiltration level of technology. 


No modifications to the Waste Activated Sludge System are needed for the Existing Conditions 



5-2



DRAFT 


Froth Control Hoods are not recommended for the Existing Conditions with 



No additional RAS chlorination measures are recommended for the Existing Conditions with 



Surface wasting is not recommended for the Existing Conditions with 




Alkalinity addition is not recommended for the Existing Conditions with 


5.9.2 Carbon 

Carbon addition is not recommended for the Existing Conditions with 



An intermediate pump station will be provided for the Existing Conditions with 

Microfiltration/Ultrafiltration level of technology. It will be located in the East section of the 

WPCP near the filters and will provide ten feet of additional head to account for headlosses from 

this new add-on process technology. A sufficient number of pumps will be provided to pump 1.5 

times the plant’s design dry weather flow capacity with an N+1+1 level of redundancy. These 

pumps will be placed inside a small headed building in parallel to each other. Best efforts were 

made to place this pumphouse in an accessible location to account for equipment maintenance 

and replacement. Emergency power will not be provided for this facility; in the event of a 

blackout, current NYCDEP policy calls for main sewage pumping, settling via PSTs, and 

chlorination along with the powering of vital EH&S assets. 



No Solids Filters are needed for the Existing Conditions with Microfiltration/Ultrafiltration level 


5-3



DRAFT 


Microfiltration/Ultrafiltration is a process that is installed downstream of a secondary treatment 

process to enhance removal of particulates within the wastewater. Removals are anticipated to 

be beyond those capable with conventional filtration. The addition of 

Microfiltration/Ultrafiltration after the final settling tanks will achieve lower levels of 

particulates in the waste stream. The objectives include: 

• Achieve low levels of solids (TSS = ~ 1 mg/L) 



Microfilters/Ultrafilters were designed for a maximum annual average flux rate of 18 gallons per 

square foot per day and an instantaneous peak flux rate of 28 gallons per square foot per day. 

Similar to the conventional filtration design, Microfilters/Ultrafilters will be placed downstream 

of the FSTs and upstream of disinfection at Port Richmond. This physical location of the new 

Microfiltration/Ultrafiltration tanks will be on the North side of the plant. A new structure will 

be constructed to house the associated equipment (pumps, blowers, etc.). 

Secondary effluent will be directed through a new conduit to the filtration tanks by gravity. 

Within the tanks, membrane filters will extract the treated effluent from the wastewater, thereby 

leaving the particulate matter in the tanks. Due to the small pore size of the membranes, 

virtually all of the particulate matter will remain within the tanks. Permeate pumps will generate 

a vacuum within the membranes to draw the effluent through the membrane. Treated effluent 

will be directed to the existing disinfection system. 

To maintain the efficiency or a high flux across the membrane, periodic back pulsing must be 

performed to remove the accumulated solids from the surface of the membranes. The permeate 

flow is reversed through the membrane, forcing the solids off the membrane surface and 

dislodging any particulates in the pore spaces. Backwash will be discharged to the head of 

primary settling tanks and returned to the treatment process. 

This conceptual design will be based on the Zenon membrane system, but other vendors should 

be considered during subsequent design phases. The membrane system consists of membrane 

units and an air scour system. Each membrane unit is 68 ft. long, 18.5 ft. wide, and 12 deep. 

Three membrane units will be installed in each tank. The membrane unit consists of a cassette, 

support frames and support beams. The Zenon process connects ZeeWeed membrane cassettes 

to the support frame. Permeate will be pulled from the top of each ZeeWeed cassette into a 

common permeate header. Connected to the header is a back pulse header that provides 

intermittent cleaning of the membranes. Permeate will be pulled by the permeate pump system 

provided by the vendor and discharged to either the back pulse storage tank or the disinfection 

tanks. Below each membrane cassette are air scour diffusers that draw air from an air header that 

extends along the top of the tank. The air supply originates at new process scour air blowers 

The nominal pore size of membrane cassettes is 0.04 microns. 340 square feet of contact surface 

area will be provided per cassette, and a total of 48 cassettes will be provided per module. 

5-4



DRAFT 

Twenty modules will be provided per Microfiltration/Ultrafiltration tank. Each 

Microfiltration/Ultrafiltration tank will be 100 feet long and 21 feet wide. A total of 11 

Microfiltration/Ultrafiltration tanks will be provided. This allows for annual average and 

maximum flux rates in line with the manufacturer’s recommendation with one 

Microfiltration/Ultrafiltration tank offline. 

Six 12,000 scfm scour air blowers will be provided. The basis of design was providing 1.4 cfm 

of air per 100 square feet of contact surface area, as per the manufacturer’s recommendation. 

This translates to an anticipated scour air demand of 50,600 scfm. 


No Denitrification Filters are needed for the Existing Conditions with 



No Membrane Bioreactors are needed for the Existing Conditions with 



No additional odor control measures are needed for the Existing Conditions with 


5-5



DRAFT 

6 ADVANCED BASIC BNR 


No modifications to the Primary Settling Tanks are needed for the Advanced Basic BNR level of 

technology. 


No fine screens are needed for the Advanced Basic BNR level of technology. 



Flow distribution and control is an important factor that can affect the nitrogen removal 

performance of any BNR process. The constraints for flow distribution at Port Richmond WPCP 

include the existing hydraulic profile, tank size, channel internal structure, and flow 

requirements. The following are the major design objectives and parameters for Advanced Basic 

BNR treatment. 

Objectives: 

• Maintain existing gate locations 

• Provide relatively uniform distribution of PE flow to each Aeration Tank and Aeration Tank 

pass 

• Provide automation of Pass D gate to receive excess wet weather flows 

• Coordinate operation of flow splitting with secondary bypass 

Parameters: 

• Design Flow Range: 30.7 mgd to 90 mgd (minimum week to 1.5 x DDWF) 

• Design Operating Flow Ranges: 

• Pass A: 0 - 30 mgd (0 to 30 %) 

• Pass B: 6 - 45 mgd (20 to 50%) 

• Pass C: 6 - 45 mgd (20 to 50%) 

• Pass D: 0 - 32 mgd (0 to 35%) 

To achieve the desired flow distribution scheme, a hydraulic analysis was carried out to 

determine if the Aeration Tank inlet gates are sufficiently sized and located. The operating flow 

distribution assumptions can be seen below in Table 6-1. Gate positioning will be optimized to 

ensure that the flow distribution to each pass meets the requirements shown below. 

Table 6-1: Operating Flow Distribution Assumptions for ABBNR 

Percent of Total Design Flow 

Level of Treatment Pass A Pass B Pass C Pass D 

Advanced Basic BNR 0% 33% 33% 33% 

6-1



DRAFT 

Gate positioning will be optimized to meet a 0:33:33:33 flow split to Passes A, B, C, and D. The 

gate to Pass D will require the installation of a motorized gate control containing an automated 

actuator to provide rapid response during storm events. This automated gate control actuator 

will open the gate fully to allow all Aeration Tank flow to enter into the head of Pass D. A gate 

controller will be tied into the plant SCADA control system to allow for either flow paced or 

manual control. 


The objectives of the baffle walls include: 

• Provide physical barrier between oxic and anoxic zones 

• Minimize back mixing between successive zones by providing sufficient velocity across 

baffle wall 

• Prevent entrapment of floatable scum (froth) at any point/area in Aeration Tank 

• Ensure capability to drain tank without wall failure through bottom openings in baffles 

• Minimize head losses between successive process zones. 

• Promote reactor conditions approaching plug flow 

Parameters include: 

• Flow assumptions from Table 6-1: Operating Flow Distribution Assumptions for 

ABBNR 

The baffle wall locations were determined based on the required volume of each pre-anoxic, 

anoxic, and oxic zone within each Pass. The anticipated baffle wall locations for Advanced 

Basic BNR are seen below in Table 6-2 and a sketch of these locations is seen in the drawings in 

Appendix B. 

Pass 

A 

B 

C 

D 

Table 6-2: Anticipated Inter-Zone Baffle Wall Locations for ABBNR 

Baffle 1 Baffle 2 Baffle 3 Baffle 4 Baffle 5 

(between Preanoxic 

zones 

(between (between (between 

(between Oxic 

successive successive Anoxic/ 

and Pre-anoxic and 

Anoxic/Switch Anoxic/Switch Switch and 

zones) subsequent 

zones) 

zones) Oxic zone) 

Pass) 

1/6 length of 

5% from end 

1/3 length of pass N/A 

N/A 

pass 

of pass 

1/6 length of 

5% from end 


N/A 

pass 

1/6 length of 

pass 

1/6 length of 

pass 


of pass 

10% from end 

of pass 

N/A 

1/3 length of pass N/A N/A N/A 

6-2



DRAFT 

The design of the Advanced Basic BNR baffle walls will include the construction of eleven (11) 

new baffle walls in each tank to separate the different pre-anoxic, anoxic and oxic zones. These 

baffle walls will be installed across the entire width of each pass (26 feet) and will be modular in 

nature but sufficiently stable to withstand the applied forces and the corrosive nature of the 

wastewater. The walls will have removable sections to allow changes in the process and pass 

specific variations in the baffle height requirements. The height of the baffle walls will be 

determined and adjusted in the field based on the flow through each pass to achieve a minimum 

velocity of 1 foot per second across the wall. 

The walls will be permanent from tank bottom to approximately 8 feet. On each end, the 

existing Y shaped walls will be squared off from the top of the Y down vertically to the new 

permanent wall section. Concrete columns with channels will be installed parallel to the squared 

off portion and extend from the top of the permanent wall to the full height of the aeration tanks 

(approximately 8 feet above the permanent wall). The channels will allow baffle sections to 

slide into place in order to achieve desired baffle wall height. These sections will be made of 

wood or FRP. The permanent wall section will include three 1-foot by 1-foot openings at the 

floor of the tank to allow filling and draining of the tank. 


The design objectives and parameters of the anoxic zone mixers for Advanced Basic BNR are 

given below: 

Objectives: 

• Provide sufficient mixing energy to keep the mixed liquor solids in suspension 

• Prevent the formation of dead or stagnant pockets 

• Minimize the level of surface turbulence 

Parameters: 

• Minimum 1 mixer per anoxic zone 

• Anoxic Zone Target DO: 0 mg/L 

• Mixed Liquor Suspended Solids (MLSS) concentration 

• Pass A: 4,000 to 8,000 mg/L 

• Pass B: 2,000 to 6,000 mg/L 

• Pass C: 1,500 to 4,000 mg/L 

• Pass D: 1,000 to 3,000 mg/L 

• Target AEMLSS Concentration: 2,000 mg/L 

Mechanical mixers are proposed for installation in the Aeration Tanks to keep the mixed liquor 

in suspension in the anoxic and pre-anoxic zones. Submersible stainless steel mixers are 

proposed for this conceptual design. Each mixer will have 7 hp and a propeller speed of 180 

rpm. It is estimated that two mixers will be required in each anoxic zone, and that 2 spare mixers 

per anoxic zones will be kept as replacements, resulting in a total of 44 mixers per tank for the 

ABBNR technology. Each mixer will be mounted from the top of the reactor with a supporting 

structure as suggested by the vendor. 

6-3



DRAFT 

Mixer design is a function of zone size and mixed liquor concentration. Due to the step-feed 

configuration, varied flow distributions, and zone sizing, a range of mixing energies will be 

required. The anticipated mixed liquor concentrations will be based on the design level of 

treatment operating conditions, including aerated effluent mixed liquor and flow distribution. 

The anticipated mixed liquor concentrations are shown in Table 6-3. 

Table 6-3: Anticipated Mixed Liquor Concentrations for ABBNR 

Mixed Liquor Concentration (mg/L) 


Pass A Pass B Pass C Pass D 

Advanced Basic BNR 8,000 4,000 2,667 2,000 

The anticipated zone sizing is shown below in Table 6-4. In subsequent design phases, zone 

sizing should be refined using BioWin or other modeling with plant-specific coefficients and 

varying process temperatures; thereby possibly changing mixer requirements. 

Pass 

Table 6-4: Anticipated Mixing Zone Sizing (per tank) for ABBNR 

Zone Volume (ft 3 ) 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 19,400 19,400 71,600 5,800 

Pass B 19,400 19,400 71,600 5,800 

Pass C 19,400 19,400 65,800 11,600 

Pass D 19,400 19,400 77,400 

In order to determine the number and variety of required shelf spares, one consistent sized mixer 

is proposed. The number of anoxic zone mixers depends on the required horsepower, which is a 

function of the mixed liquor concentration and zone sizing. Based on the above operating 

conditions, 7.0 hp mixers are anticipated to best suit mixing energy requirements. The number 

of anoxic zone mixers necessary is shown below in Table 6-5. 

Pass 

Table 6-5: Anticipated Number of Anoxic Zone Mixers for ABBNR 

Number of Mixers Per Zone Per Tank – (88 Mixers Total) 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 2 2 N/A 2 

Pass B 2 2 N/A 2 

Pass C 2 2 N/A 2 

Pass D 2 2 N/A 


6-4



DRAFT 

With the new Advanced Basic BNR technology design levels, air requirements are anticipated to 

increase. The air distribution system will need enhancements to supply the increased air volume 

that will be directed into the aeration tanks. The objectives of the process aeration upgrades are 

to ensure sufficient air is provided for nitrification and to optimize the control of DO levels. 

These objectives include: 

• Provide sufficient oxygen to satisfy all process requirements 

• Provide flexibility for different process operating conditions 

• Allow control and measurement of aeration input along the length of individual passes to 

minimize under-aeration and over-aeration 

Under the Advanced Basic BNR design level, the 54 inch main air header will continue to run 

along the East Aeration Tank influent channel and distribute air to eight smaller pass header 

lines, located in the Y-walls separating the A/B and C/D passes in each tank. The smaller header 

lines will feed droplegs that will provide process air to the diffusers covering the floor of each 

aeration tank. The main header decreases in diameter from 54 inches to 24 inches as it feeds the 

smaller headers. The smaller headers decrease in diameter from 24 inches to 8 inches as they 

feed the aeration tank. Motorized butterfly valves will provide the aeration tank headers with 

increased flow control and allow for an aeration tank to be taken offline. 

Six droplegs will branch off of the pass headers into each pass. In the ABBNR design, for 

Passes A, B, C, and D, both switch zones at the head of the pass will have a dropleg and 

connected diffuser grid and the remaining four droplegs will service the oxic zone. Each dropleg 

will be provided with a butterfly valve. 


With the increase in the aeration capacity under the new Advanced Basic BNR design upgrades, 

the diffuser grids will be redesigned to provide a distribution of air throughout the aeration tank 

oxic zones and switch zones. The objectives of the process aeration upgrades are to ensure 

sufficient air is provided for nitrification and to optimize the control of DO levels. These 

objectives include: 


• Provide flexibility for different process operating conditions, including the implementation of 

switch zones 

• Provide a tapered diffuser design to match the needs of the process 

The quantity of diffusers required for each design level was based on the air requirements that 

will be shown in the next section. The selected diffuser type was the 9” diameter fine bubble 

membrane disc diffuser with a manufacturer recommended air flow range of 1 to 3 scfm per 

diffuser. An average flow of 1.5 scfm per diffuser was initially assumed under average loading 

conditions. Anticipated variations in loads were evaluated to ensure sufficient capacity was 

available and that the diffusers operated within their appropriate manufacturer-suggested typical 

range. Table 6-6 shows the required diffusers. 

6-5



DRAFT 


Table 6-6: Diffuser Requirements for ABBNR 

Peak Day Required 

(scfm) 

Total Diffusers 

Required (1) 

Advanced Basic BNR 40,000 26,600 

Notes: (1) - Diffuser quantity based on 1.5 scfm/diffuser airflow rate 

Further refinement of the tapered diffuser design should be pursued to ensure proper design of 

the diffuser grid. 


With the implementation of Advanced Basic BNR at the facility, the amount of air required and 

the demand placed on the current aeration system are both expected to increase. To meet the 

new air requirements and allow the facility to fully utilize the new technologies, the process air 

blower system will need to be enhanced. 

The objectives of the process aeration upgrades are to ensure sufficient air is provided for 

nitrification and to optimize the control of DO levels. These objectives include: 





• Provide turndown and shutoff features to accommodate different process operating 

conditions 

An evaluation was performed to determine the future air requirements for the various design 

levels based on the projected flows and loads from the Introduction and the projected mass 

balance for 2045 in Section 2.0. The calculated air requirements can then be compared against 

the existing process aeration system to determine the necessary increase in aeration capacity that 

must be provided. Table 6-7 presents the calculated air requirements. 

Level of 

Treatment 

Table 6-7: Future 2045 Air Requirements for ABBNR 

Aeration 

Current Blower 

Tank BioWin Predicted Capacity 

Loading Air Demand (scfm) (2 offline) 

Condition 

(scfm) 

Additional 

Blowers 

Needed 

Advanced Average 23,507 48,000 0 

Basic BNR Peak Hourly 39,962 48,000 0 

The air requirements were determined at both the average and peak daily loading conditions, 

using a peaking factor of 1.7 to determine the peak hourly air requirement. 

The existing system was evaluated to determine of the proposed technologies can be satisfied 

using the existing blowers. The peak hourly loading conditions can be met for the Advanced 

6-6



DRAFT 

Basic BNR technology, while still providing the spare and standby requirements identified in the 

BNR design guidance documents (N+1+1). 


No modifications to the Final Settling Tanks are needed for the Advanced Basic BNR level of 

technology. 


The RAS system is important in maintaining the solids inventory in the aeration tanks and can 

affect the nitrogen removal performance of a BNR process. The following are the major design 

objectives and parameters for Advanced Basic BNR treatment. 

Objectives: 

• Increase pumping capacity within existing infrastructure and footprint (i.e. electrical, 

distribution piping, etc.) 

• Maximize pipe/channel capacity within existing structures 

• Provide capability to pump over entire range of flows 

• Provide flow monitoring 

Parameters 

• RAS underflow concentration: not to exceed 8,000 mg/L 

• RAS capacity: 30 mgd 

• Design Load: 4,000 to 8,000 mg/L 

To achieve desired flow capacity with three units in operation and two units in standby, larger 

pumps are required. There is no room in the existing sludge pumping station to install addition 

RAS pumps, so it is recommended that the current RAS pumps be replaced with five 10 mgd 

pumps. The installation of magnetic flow meters for accurate flow control is recommended. 

Respective suction and discharge piping for each pump must also be replaced. Furthermore, the 

existing suction and discharge headers may be insufficient to handle the proposed flow and may 

need to be replaced by larger piping and valves. 


The design objectives and parameters for the WAS system for Advanced Basic BNR include: 

Objectives: 

• Provide monitoring of WAS rate (flow and solids) to enable MCRT calculation; at minimum, 

provide local flow meter and totalizer 

• Provide metering of WAS draw from RAS box and Aeration Tank effluent from each 

Aeration Tank 

• Provide separate metering of primary and WAS sludge 

• Provide (or maintain) capability to waste sludge from RAS and Aerator Effluent 

• Maintain equal solids inventories among Aeration Tanks in the same battery 

6-7



DRAFT 

Parameters: 

• Design concentration: 2,000 to 6,000 mg/L 

• System MCRT: 5 to 20 days 

• Design flow operating range: 

WAS: 0.6 – 2.4 mgd 

Aeration Tank Effluent: 3.0 – 12 mgd 

For the Advanced Basic BNR alternative, sludge will be wasted from the final settling tank 

underflow, as opposed to the aerator effluent mixed liquor line. This will result in a higher solids 

concentration in the waste flow, reducing the overall waste flow volume. The BNR treatment 

alternative includes increasing the solids inventory of the aeration tanks to provide more biomass 

for nutrient removal. Thus, there is a reduced wasting rate from current conditions. For this 

level of treatment, the existing WAS pumps are sufficient to handle the new operating 

conditions. New flow meters will be installed in order to accurately measure the wasting rate to 

enable better process control. 


Biologically induced frothing is relatively common at high sludge-age BNR Plants and presents 

problems with respect to MCRT control, housekeeping, and anaerobic digester operation. 

Frothing occurs because of the proliferation of filamentous organisms such as Nocardia spp, M. 

parvicella, and others. These organisms are hydrophobic in nature and when present in 

sufficient numbers they attach to air bubbles and rise to the surface in aeration tanks as froth. 

Once at the surface, the froth tends to stay there causing the operational problems. 


In order to mitigate froth problems, several control measures are recommended, which include 

enclosed Froth Control Systems such as Froth Control Hoods (FCH). These systems provide a 

chlorinated spray on the surface of the aeration tanks, which selectively destroys the surface 

bacteria causing the froth issues. 

The objective of froth control hoods is to allow for a chlorinated spray at the surface of the 

Aeration Tanks, while ensuring the health and safety of the operators. The chlorine 

concentration must be sufficient to kill the froth forming bacteria, but the dosage must be 

mitigated to prevent killing the entire treatment process. The design objectives of the FCH are as 

follows: 

• Provision of two hoods in both Passes A and B; located at approximately 1/6 and 2/3 of the 

pass length 

• Provide emergency dosage equivalent to 4 to 8 mg/L in the wastewater stream using all froth 

control entry points 

• Provide maintenance dosage equivalent 0.5 to 2 mg/L in the wastewater stream using two 

froth control entry points 

• Provide dilution water to achieve nozzle Cl 2 concentration between 1,000 to 3,000 mg/L 

6-8



DRAFT 

• Provide 4-5 days of chemical storage for average flow conditions; coordinate with RAS 

chlorination storage 

A typical froth control hood includes chemical storage and feed, dilution water pumping, 

distribution system, nozzles to spray the chlorine solution onto the water surface and protective 

enclosures to avoid personnel contact with the chlorinated spray. The chemical storage and feed 

facility will be described in the RAS Chlorination section. 

As indicated above, a total of four froth control hoods will be required per tank. The spray 

headers installed will have connectors, nozzle pipe leads, nozzle fittings and nozzles to apply the 

chlorinated spray. The distance between nozzle connections will be determined by the nozzle 

type and dose requirements. It can be assumed that approximately six nozzle connections will be 

installed per hood. The spray nozzles will be installed at approximately 3 feet above the water 

surface to provide enough elevation for sufficient spray coverage. Each individual spray nozzle 

pipe lead will be provided with individual quick disconnects or unions to facilitate removal for 

maintenance. Valves will be installed at each header for on/off switching of chlorine spray. The 

chlorine solution to be applied will be provided by means of a chlorine solution distribution 

main. There will be distribution piping extended from the main to the side of each of the hoods. 

From there it will be divided into each of the nozzle pipes. 

Hatches will provide personnel access to the sliding retractable baffle segments. These segments 

will be lifted in unison by an actuated mechanism located atop the hood structure. These 

adjacent flaps will span the width of the pass and extend below the water surface to trap the foam 

within the enclosed hood area. The flaps will facilitate the trapping of the froth to ensure 

effective chlorination. They shall be retractable by mechanically sliding them up to allow any 

trapped material to flow freely on the surface of the water when the hood is not in use. A 

mechanism will be included to lock the flaps into place when raised by personnel. 

Chlorine storage, feed and distribution throughout the plant is included in another section. 

Piping will be used to bring the chlorine solution from the distribution main to each hood. A 

dual strainer will be installed for each aeration tank with an interconnection that will allow it to 

serve two tanks, providing sufficient redundancy. 


The chlorination of RAS can be used to kill nuisance organisms that contribute to froth 

formation and poor settling secondary solids. It is assumed that the existing disinfection system 

will not be sufficient for froth control at the increased RAS flow rates. Instead, a dedicated 

chemical storage and feed facility will be constructed on the Northwest side of the facility. This 

facility will include alkalinity, chlorine for froth control, and supplemental carbon for 

appropriate alternatives. 

The design objectives and features for RAS Chlorination include: 

• Control proliferation of filamentous bacteria that results in bulking and/or biological froth 

formation on the aeration tank surface through chlorination 

6-9



DRAFT 

• Add chlorine to the RAS line or at the RAS pump volute 

• Allow for a dose of 3 to 5 lbs of chlorine per 1000 lbs of MLSS inventory per day 

Assuming a target chlorine dose of 2.0 mg/L in the aeration basins, an assumed sodium 

hypochlorite storage concentration of 15 percent, and a 5-day chemical storage requirement, the 

Team calculates a design storage volume of 12,576 gallons. This will be provided via four 

4,000-gallon aboveground storage tanks (ASTs). All tanks will comply with New York State 

Chemical Bulk Storage regulations, such as secondary containment, spill protection, and leak 

detection systems. 

The Team assumes two hypochlorite metering pumps, each with a capacity of 189 gallons per 

minute. Each pump will be powered by a 1 hp motor equipped with a VFD. 


Surface wasting has been identified as an effective long-term solution to control aeration tank 

froth formation and provide SRT control. Implementation of surface wasting to control the 

secondary treatment process reduces the potential for froth formation. The design objectives as 

described in the BNR design guidance document include: 

• Remove MLSS and biological froth from aeration surfaces to solids handling facilities 

• Control froth formation by preferentially wasting froth and filamentous bacteria 

• Avoid returning the waste stream to the primary and secondary treatment systems 

• Provide the capability to chlorinate the waste stream to avoid solids handling issues 

• Account for typical variations in the surface water level 

• Allow for the wasted solids to be accounted for within the SRT calculations 

Adjustable downward opening gates are recommended for surface wasting for the Port 

Richmond WPCP. The downward opening gates will be mounted on two new surface wasting 

pump sumps built at the end of each Pass A. Lowering a gate(s) will allow the froth and/or 

MLSS to overflow the weir into the surface wasting pump station(s). The surface waste will be 

pumped to the existing waste activated sludge wet well near the Final Settling Tanks for further 

delivery to sludge processing. The flow and TSS concentration of the surface waste will be 

measured and totalized. The flow and TSS data will dictate time based operation of the pumps to 

preventing overwasting. The elevation of the downward opening gates will be operated either 

automatically or manually based on the aeration tank wastewater elevation. 



New York wastewaters are low in alkalinity and nitrification can consume significant amounts of 

alkalinity. Consumption of alkalinity can decrease pH, which can, in turn, decrease the rate of 

nitrification. Therefore, alkalinity addition is an important component of BNR strategies. 

The design objectives for Advanced Basic BNR include the following: 

6-10



DRAFT 

• Maintain constant and optimum pH plus provide sufficient alkalinity for nitrification 

• Maintain 50 to 100 mg/L CaCO 3 in all passes 

• Control based on pH feedback 

• Provide mixing at dosage point 

• Provide 4 to 5 days of chemical storage under average conditions 

The proposed conceptual design provides a liquid chemical system based on caustic soda. The 

system includes six (6) 25,000 gallon FRP liquid chemical storage tanks (total storage 150,000 

gallons). The storage tanks will be insulated and heat traced to avoid crystallization of the 

caustic. The storage tanks will be located inside a new chemical handling and storage building, 

the location of which is shown on drawings in Appendix B. 

Four alkalinity metering pumps will be provided. Each pump will have a design flowrate of 833 

gallons per minute with a design backpressure of 75 psi. Each pump will be powered by a 1 

horsepower motor. Two alkalinity transfer pumps will be provided. These pumps will have a 

150 gallon per minute flowrate. Each pump will have a 3 horsepower motor and be able to 

provide a total dynamic head of 75 psi. 

The Team conservatively assumes no credit for denitrification. The Team assumes an alkalinity 

consumption of 7.1 mg CaCO 3 per mg of TKN. The Team assumes a Sodium Hydroxide 

concentration of 25 percent and a target residual alkalinity concentration of 75 mg/L as CaCO 3 . 

Based on a 5-day storage requirement, the Team calculates a need for 125,960 gallons of storage. 

This will be provided by 6 25,000-gallon storage tanks. Each tank will have a diameter of 13 

feet and an effective height of 25 feet. 

6.9.2 Carbon 

Carbon addition is not recommended for the Advanced Basic BNR level of technology. 


Construction of an Intermediate Pumping Station is not needed for the Advanced Basic BNR 




No Solids Filters are needed for the Advanced Basic BNR level of technology. 


No Microfilters/Ultrafilters are needed for the Advanced Basic BNR level of technology. 


6-11



DRAFT 

No Denitrification Filters are needed for the Advanced Basic BNR level of technology. 


No Membrane Bioreactors are needed for the Advanced Basic BNR level of technology. 


The four aeration basins at the Port Richmond WPCP are located indoors as an odor control 

provision, however, given the dynamic nature of this field, a placeholder cost was included for 

additional odor control provisions, with the understanding that appropriate technologies will be 

implemented at the time of detailed design after consultation with BEPA. 

6-12



DRAFT 

7 FULL STEP BNR 


No modifications to the Primary Settling Tanks are needed for the Full Step BNR level of 

technology. 


No fine screens are needed for the Full Step BNR level of technology. 



The operating flow distribution assumptions for the Full Step BNR technology can be seen 

below in Table 7-1. Gate positioning will be optimized to ensure that the flow distribution to 

each pass meets the requirements shown below. 

Table 7-1: Operating Flow Distribution Assumptions for FSBNR 



Full Step BNR 10% 40% 30% 20% 

This level of treatment is higher than that of Advanced Basic and requires improved flow 

distribution and gate setting. Gate positioning will be optimized to meet a 10:40:30:20 flow split 

to Passes A, B, C, and D. The gate to Pass D will require the installation of a motorized gate 

control containing an automated actuator to provide rapid response during storm events. This 

automated gate control actuator will open the gate fully to allow all Aeration Tank flow to enter 

into the head of Pass D. A gate controller will be tied into the plant SCADA control system to 

allow for either flow paced or manual control. 



anoxic, and oxic zone within each Pass. The anticipated baffle wall locations for Full Step BNR 

are seen below in Table 7-2 and a sketch of these locations is seen in the drawings in Appendix 

B. The only difference between the baffle wall design from the Advanced Basic BNR to the Full 

Step BNR technology is the number of walls installed in Pass D. 

7-1



DRAFT 

Pass 

A 

B 

C 

D 

Table 7-2: Anticipated Inter-Zone Baffle Wall Locations for FSBNR 



zones 


(between Oxic 





zones) 


Pass) 

1/6 length of 

1/2 length of 5% from end 

1/3 length of pass 

N/A 

pass 

pass of pass 

1/6 length of 

5% from end 


N/A 

pass 

1/6 length of 

pass 

1/6 length of 

pass 



1/2 length of 

pass 

of pass 

10% from end 

of pass 

N/A 

N/A 

N/A 







Table 7-3: Anticipated Mixed Liquor Concentrations for FSBNR 




Full Step BNR 6,558 3,810 2,899 2,500 




Pass 

Table 7-4: Anticipated Mixing Zone Sizing (per tank) for FSBNR 


Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 19,400 19,400 19,400 52,200 5,800 

Pass B 19,400 19,400 71,600 5,800 

Pass C 19,400 19,400 65,800 11,600 

Pass D 19,400 19,400 19,400 58,000 

7-2



DRAFT 





of mixers necessary is shown below in Table 7-5. 

Pass 

Table 7-5: Anticipated Number of Anoxic Zone Mixers for FSBNR 

Number of Mixers Per Zone Per Tank (104 Mixers Total) 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 2 2 2 N/A 2 



Pass D 2 2 2 N/A 


With the Full Step BNR technology design levels, air requirements are anticipated to increase 

slightly from those needed at Advanced Basic BNR. The air distribution system will need 

enhancements to supply the increased air volume that will be directed into the aeration tanks. 

Under the Full Step BNR design level, the 54 inch main air header will continue to run along the 

East Aeration Tank influent channel and distribute air to eight smaller pass header lines, located 

in the Y-walls separating the A/B and C/D passes in each tank. The smaller header lines will 

feed droplegs that will provide process air to the diffusers covering the floor of each aeration 

tank. The main header decreases in diameter from 54 inches to 24 inches as it feeds the smaller 

headers. The smaller headers decrease in diameter from 24 inches to 8 inches as they feed the 

aeration tank. Motorized butterfly valves will provide the aeration tank headers with increased 

flow control and allow for an aeration tank to be taken offline. 

Six droplegs will branch off of the pass headers into each pass. In the FSBNR design, for Passes 

B and C, both switch zones at the head of the pass will have a dropleg and connected diffuser 

grid and the remaining four droplegs will service the oxic zone. For Passes A and D, the third 

switch zone will also have a dedicated dropleg and connected diffuser grid and the remaining 

three droplegs will service the oxic zone. Each dropleg will be provided with a butterfly valve. 


With the increase in the aeration capacity under the Full Step BNR, additional diffusers will be 

required. The quantity of diffusers required for each design level was based on the air 

requirements that will be shown in the next section. The selected diffuser type was the 9” 

diameter fine bubble membrane disc diffuser with a manufacturer recommended air flow range 

of 1 to 3 scfm per diffuser. An average flow of 1.5 scfm per diffuser was initially assumed under 

average loading conditions. Anticipated variations in loads were evaluated to ensure sufficient 

7-3



DRAFT 

capacity was available and that the diffusers operated within their appropriate manufacturersuggested 

typical range. Table 7-6 shows the required diffusers. 


Table 7-6: Diffuser Requirements for FSBNR 


(scfm) 


Required (1) 

Full Step BNR 43,300 28,900 





With the implementation of Full Step BNR at the facility, the amount of air required and the 

demand placed on the current aeration system are both expected to increase. To meet the new air 

requirements and allow the facility to fully utilize the new technologies, the process air blower 

system will need to be enhanced. 






Level of 

Treatment 

Full Step BNR 

Table 7-7: Future 2045 Air Requirements for FSBNR 

Current 

Aeration Tank BioWin Predicted Blower 

Loading Air Demand Capacity 

Condition 

(scfm) (2 offline) 

(scfm) 

Additional 

Blowers Needed 

Average 25,495 48,000 0 

Peak Hourly 43,342 48,000 0 




using the existing blowers. The peak hourly loading conditions can be met for the Full Step 

BNR technology, while still providing the spare and standby requirements identified in the BNR 

design guidance documents (N+1+1). 


7-4



DRAFT 

No modifications to the Final Settling Tanks are needed for the Full Step BNR level of 

technology. 




objectives and parameters for Full Step BNR treatment. 

Objectives 

• Increase pump capacity to 100% DDWF 

• Increase pipe/channel capacity 



Parameters 




• Air lift pumps prohibited 

To achieve desired flow capacity with three units in operation and two units in standby, larger 

pumps are required. There is no room in the existing sludge pumping station to install addition 

RAS pumps, so it is recommended that the current RAS pumps be replaced with five 20 mgd 

pumps. Respective suction and discharge piping for each pump must also be replaced. 

Furthermore, the existing suction and discharge headers may be insufficient to handle the 

proposed flow and may need to be replaced by larger piping and valves. 


No modifications to the Waste Activated Sludge System are needed for the Full Step BNR level 

of technology, as per the Advanced Basic BNR Design in Section 6.7. 



A description of the Froth Control Hoods design needed for the Full Step BNR level of 

technology was provided in Section 6.8.1 for the Advanced Basic BNR treatment option. 


A description of the RAS Chlorination design needed for the Full Step BNR level of technology 

was provided in Section 6.8.2 for the Advanced Basic BNR treatment option. 


7-5



DRAFT 

A description of the Surface Wasting design needed for the Full Step BNR level of technology 




A description of the Alkalinity addition design needed for the Full Step BNR level of technology 


7.9.2 Carbon 

New York wastewater has a relatively low readily biodegradable carbon content and the carbon 

available in the wastewater may be insufficient to promote sufficient denitrification to meet low 

levels of nitrogen. Supplemental carbon addition will be required the Full Step BNR design 

alternative. 

The design objectives and features as described in the BNR design guidance include the 

following: 

• Provide supplemental carbon to enhance denitrification 

• Provide capability to feed to the head of all anoxic zones 

• Provide manual dosage control and the ability to feed on a diurnal pattern based on the flow, 

BOD, and TKN with a feedback bias based on residual nitrate measurement 

• Provide mixing at dosage points 


The proposed conceptual design is based on the use of methanol as the supplemental carbon 

source and follows the requirements given in the BNR guidance documentation. Methanol has 

flammable properties that impose restrictions on its unloading, storage and feeding systems. The 

systems are subject to: the regulations of several entities including the Department of 

Transportation, the Occupational Safety and Health Act, and local and state safety and fire codes; 

to guidelines provided by independent associations such as the National Fire Protection 

Association and the Manufacturing Chemists Association; and to precautions and requirements 

imposed by insurance providers. It is important to recognize that, in addition to basic system 

requirements identified by the conceptual design needs, a methanol system will have ancillary 

requirements, such as the need for explosion proof equipment and lighting, which will contribute 

significantly to the cost of the installation. 

The carbon addition system will consist of storage tanks with appropriate unloading and spill 

containment provisions, metering pumps, and chemical piping. The chemical will be introduced 

into the anoxic zone in a manner that uses the existing zone mixing device to introduce the 

chemical in the process stream. A separate chemical mixing device will not be provided. 

The Team assumes a design methanol storage concentration of 100% and a methanol dosing 

concentration of 15%. Based on a 5-day storage requirement under maximum loading 

7-6



DRAFT 

conditions, the Team calculates a design storage volume of 8,360 gallons for the Full Step BNR 

alternative. A single 12,000 gallon underground storage tank will be provided. 


Construction of an Intermediate Pumping Station is not needed for the Full Step BNR level of 

technology. 



No Solids Filters are needed for the Full Step BNR level of technology. 


No Microfilters/Ultrafilters are needed for the Full Step BNR level of technology. 


No Denitrification Filters are needed for the Full Step BNR level of technology. 


No Membrane Bioreactors are needed for the Full Step BNR level of technology. 






7-7



DRAFT 

8 FULL STEP BNR WITH SOLIDS FILTRATION 


No modifications to the Primary Settling Tanks are needed for the Full Step BNR with Solids 



No fine screens are needed for the Full Step BNR with Solids Filtration level of technology. 



A description of the modifications to flow distribution and control needed for the Full Step BNR 

with Solids Filtration level of technology was provided in Section 7.3.1 for the Full Step BNR 

treatment option. 


A description of the baffle walls needed for the Full Step BNR with Solids Filtration level of 

technology was provided in Section 7.3.2 for the Full Step BNR treatment option. 


A description of the anoxic zone mixers needed for the Full Step BNR with Solids Filtration 

level of technology was provided in Section 7.3.3 for the Full Step BNR treatment option. 


A description of the modifications to the air distribution and control needed for the Full Step 

BNR with Solids Filtration level of technology was provided in Section 7.3.4 for the Full Step 

BNR treatment option. 


A description of the modifications to the diffuser system needed for the Full Step BNR with 

Solids Filtration level of technology was provided in Section 7.3.5 for the Full Step BNR 



A description of the modifications to the Process Air system needed for the Full Step BNR with 

Solids Filtration level of technology was provided in Section 7.4 for the Full Step BNR 


8-1



DRAFT 


No modifications to the Final Settling Tanks are needed for the Full Step BNR with Solids 



A description of the Return Activated Sludge System design needed for the Full Step BNR with 




No modifications to the Waste Activated Sludge System are needed for the Full Step BNR with 

Solids Filtration level of technology, as per the Advanced Basic BNR Design in Section 6.7. 



A description of the Froth Control Hoods design needed for the Full Step BNR with Solids 

Filtration level of technology was provided in Section 6.8.1 for the Advanced Basic BNR 



A description of the RAS Chlorination design needed for the Full Step BNR with Solids 




A description of the Surface Wasting design needed for the Full Step BNR with Solids Filtration 

level of technology was provided in Section 6.8.3 for the Advanced Basic BNR treatment 

option. 



A description of the Alkalinity addition design needed for the Full Step BNR with Solids 



8.9.2 Carbon 

A description of the Carbon addition design needed for the Full Step BNR with Solids Filtration 


8-2



DRAFT 


An intermediate pump station will be provided for the Full Step BNR with Solids Filtration level 

of technology. It will be located in the North section of the WPCP near the filters and will 











A description of the Solids Filtration design needed for the Full Step BNR with Solids Filtration 

level of technology was provided in Section 4.11.1 for the Existing Conditions with Solids 

Filtration treatment option. 


No Microfilters/Ultrafilters are needed for the Full Step BNR with Solids Filtration level of 

technology. 


No Denitrification Filters are needed for the Full Step BNR with Solids Filtration level of 

technology. 


No Membrane Bioreactors are needed for the Full Step BNR with Solids Filtration level of 

technology. 






8-3



DRAFT 

9 FULL STEP BNR WITH MICROFILTRATION/ULTRAFILTRATION 


No modifications to the Primary Settling Tanks are needed for the Full Step BNR with 



A description of the fine screens needed for the Full Step BNR with 

Microfiltration/Ultrafiltration level of technology was provided in Section 5.2 for the Existing 

Conditions – Microfiltration/Ultrafiltration treatment option. 




with Microfiltration/Ultrafiltration level of technology was provided in Section 7.3.1 for the Full 

Step BNR treatment option. 


A description of the baffle walls needed for the Full Step BNR with 

Microfiltration/Ultrafiltration level of technology was provided in Section 7.3.2 for the Full Step 

BNR treatment option 


A description of the anoxic zone mixers needed for the Full Step BNR with 





BNR with Microfiltration/Ultrafiltration level of technology was provided in Section 7.3.4 for 

the Full Step BNR treatment option. 






9-1



DRAFT 


Microfiltration/Ultrafiltration level of technology was provided in Section 7.4 for the Full Step 



No modifications to the Final Settling Tanks are needed for the Full Step BNR with 








Microfiltration/Ultrafiltration level of technology, as per the Advanced Basic BNR Design in 

Section 10.7. 



A description of the Froth Control Hoods design needed for the Full Step BNR with 

Microfiltration/Ultrafiltration level of technology was provided in Section 6.8.1 for the 

Advanced Basic BNR treatment option. 


A description of the RAS Chlorination design needed for the Full Step BNR with 




A description of the Surface Wasting design needed for the Full Step BNR with 





A description of the Alkalinity addition design needed for the Full Step BNR with 



9-2



DRAFT 

9.9.2 Carbon 

A description of the Carbon addition design needed for the Full Step BNR with 




An intermediate pump station will be provided for the Full Step BNR with 

Microfiltration/Ultrafiltration level of technology. It will be located in the East section of the 

WPCP near the filters and will provide ten feet of additional head to account for headlosses from 

this new add-on process technology. A sufficient number of pumps will be provided to pump 1.5 

times the plant’s design dry weather flow capacity with an N+1+1 level of redundancy. These 

pumps will be placed inside a small headed building in parallel to each other. Best efforts were 

made to place this pumphouse in an accessible location to account for equipment maintenance 

and replacement. Emergency power will not be provided for this facility; in the event of a 

blackout, current NYCDEP policy calls for main sewage pumping, settling via PSTs, and 

chlorination along with the powering of vital EH&S assets. 



No Solids Filters are needed for the Full Step BNR with Microfiltration/Ultrafiltration level of 

technology. 


A description of the Microfiltration/Ultrafiltration design needed for the Full Step BNR with 

Microfiltration/Ultrafiltration level of technology was provided in Section 5.11.2 for the Existing 



No Denitrification Filters are needed for the Full Step BNR with Microfiltration/Ultrafiltration 



No Membrane Bioreactors are needed for the Full Step BNR with Microfiltration/Ultrafiltration 





9-3



DRAFT 



9-4



DRAFT 

10 FULL STEP BNR WITH DENITRIFICATION FILTERS 



Denitrification Filters level of technology. 


No fine screens are needed for the Full Step BNR with Denitrification Filters level of 

technology. 




with Denitrification Filters level of technology was provided in Section 7.3.1 for the Full Step 



A description of the baffle walls needed for the Full Step BNR with Denitrification Filters level 

of technology was provided in Section 7.3.2 for the Full Step BNR treatment option 


A description of the anoxic zone mixers needed for the Full Step BNR with Denitrification 

Filters level of technology was provided in Section 7.3.3 for the Full Step BNR treatment option. 



BNR with Denitrification Filters level of technology was provided in Section 7.3.4 for the Full 




Denitrification Filters level of technology was provided in Section 7.3.5 for the Full Step BNR 




Denitrification Filters level of technology was provided in Section 7.4 for the Full Step BNR 


10-1



DRAFT 










Denitrification Filters level of technology, as per the Advanced Basic BNR Design in Section 

6.7. 




Denitrification Filters level of technology was provided in Section 6.8.1 for the Advanced Basic 



A description of the RAS Chlorination design needed for the Full Step BNR with Denitrification 

Filters level of technology was provided in Section 6.8.2 for the Advanced Basic BNR treatment 

option. 


A description of the Surface Wasting design needed for the Full Step BNR with Denitrification 


option. 



A description of the Alkalinity addition design needed for the Full Step BNR with Denitrification 


option. 

10.9.2 Carbon 

10-2



DRAFT 

A description of the Carbon addition design needed for the Full Step BNR with Denitrification 


Under the BNR with Denitrification Filters level of technology, carbon is also added to the 

Denitrification Filters. 


An intermediate pump station will be provided for the Full Step BNR with Denitrification Filters 

level of technology. It will be located in the East section of the WPCP near the filters and will 










10.11.1Solids Filtration 

No Solids Filters are needed for the Full Step BNR with Denitrification Filters s level of 

technology. 

10.11.2Microfiltration/Ultrafiltration 

No Microfilters/Ultrafilters are needed for the Full Step BNR with Denitrification Filters level of 

technology. 

10.11.3Denitrification Filters 

Serving as an enhancement to the Full Step BNR design, Denitrification Filters can be added 

downstream of the final settling tanks to treat nitrified secondary effluent. The addition of 

Denitrification Filters to the Full Step BNR design level will achieve lower levels of nitrogen 

and provide filtration to remove additional particulate matter from the waste stream. The 

addition of denitrification filters allows the step feed process tanks to operate with additional 

aerated zone volume to enhance the nitrification process. Enhanced levels of denitrification can 

be achieved in the denitrification filters. The objectives include: 

• Achieve low nitrogen discharge levels (TN = 4 mg/L to 5 mg/L) 




Denitrification filters were designed for a maximum annual average flux rate of two gallons per 

minute per square foot and a max day flux rate of four gallons per minute per square foot. The 

10-3



DRAFT 

Denitrification Filters will be located downstream of the FSTs and upstream of disinfection at 

Port Richmond. A new structure will be constructed on the North end of the plant to house the 

new equipment. The design of the Full Step Feed BNR upgrades includes switch zones that 

allow the activated sludge process to operate with additional oxic volume to enhance the 

nitrification capability. No additional facilities will be required for the aeration tanks. 

The size and porosity of the media will allow biomass to attach and grow. As the nitrified 

secondary effluent flows through the biomass-enriched media, denitrification will occur, as well 

as removals of particulate matter. The denitrification process will be supported by maintaining 

an anoxic state within the filters and by having a supplemental carbon addition point upstream of 

the filters. The biomass responsible for denitrification will utilize the supplemental carbon and 

any inherent carbon in the secondary effluent. 

To maintain the efficiency of the Denitrification filters, periodic backwashing must be performed 

to remove the accumulated solids from between the media particles. Equipment will be provided 

that will flush the media by recycling the treated effluent to serve as washwater. A blower 

system will also be provided for air scouring of the media when the filter units are not operating 

in a denitrification mode. The reused effluent and released solids will then be directed to the 

gravity thickeners. 

The design condition of the denitrification filters is a flux rate of 4 gallons per square foot per 

minute on a maximum day condition. The Team assumes ten percent of the filters will be offline 

at any given time for backwash and O&M requirements. This translates to a design surface area 

of 14,552 square feet. The team assumes rectangular denitrification filters, with each filter 

providing 665 square feet of contact surface area. A total of 22 of these filters will be provided. 

Sand will be the medium of choice. The team assumes a grain size of 2 mm and a filter depth of 

6 feet. Methanol will be provided to enhance denitrification. Methanol design specifications are 

listed in Section 10.9.2. 






be provided, each with a capacity of 3,325 scfm 


No Membrane Bioreactors are needed for the Full Step BNR with Denitrification Filters level of 

technology. 




10-4



DRAFT 



10-5



DRAFT 

11 MEMBRANE BIOREACTORS 


Modification of the primary settling tanks is required for the Membrane Bioreactor alternative. 

A major source of head loss will be the new fine screenings described later in this section. To 

gain a portion of that head loss, it is proposed to demolish the existing primary settling tanks and 

rebuild them 6 feet higher to account for increased headloss. Detailed hydraulic design 

evaluating the hydraulic gradient between influent and effluent levels will refine and confirm the 

necessary elevation change. 


MBR technologies require more-advanced removal of influent solids than is typically achieved 

by conventional settling. Fine screens can be used to remove solids from process effluent that 

may cause clogging of the membranes reducing their treatment efficiency and increasing 

maintenance requirements. 

The design objectives of the fine screening process for Membrane Bioreactor Tanks and include: 

• Remove particles larger than 6 mm from primary influent 

• Remove particles larger than 2 mm from primary effluent 



The proposed design for the fine screening process at the Port Richmond WPCP consists of an 

installation of primary influent screens in the primary influent channel, and the primary effluent 

screens in the primary effluent channel. 

The Team assumes Jones and Atwood band screens will be selected for the 6 mm screens. These 

screens will be placed at the upstream end of the primary settling tanks. Each screen has a 

design capacity of 20 mgd and assumes discharge velocity of 1.65 feet per second under annual 

average conditions. The projected headloss for a screen of this size is three to six inches, 

depending on the overall flowrate to the plant. The Team assumes a channel depth of 12 feet and 

a width (per screen) of 9 feet. Through information supplied by the manufacturer, the 

anticipated solids removal rate is 13 cubic feet per screen per hour. This volume is used to 



A total of 8 primary influent screens will be installed: one in-service screen will be provided for 

each primary settling tank, and one spare screen for each tank will be stored in the event a screen 

must be replaced.. The screens are of sufficient capacity that one per PST would be sufficient 

under a max flow condition, with one screen per tank offline for O&M. Screen reject will be 

sent to solids handling through the primary sludge line. Each screening unit will be connected 

to a spray water system to remove the collected screenings from the screen panels. The spray 

water system will be connected to the plant’s existing effluent water system or will utilize the 

11-1



DRAFT 

screening effluent to wash the screen panels. The screenings residuals and washwater will be 

discharged to a collection trough and will flow by gravity to a wet well from where it will be 

pumped to the sludge thickeners. 


screen has a design capacity of 15 mgd and assumes discharge velocity of 0.87 feet per second. 



was designed conservatively in order to minimize fouling and required plant Operations and 

Maintenance (O&M) activities. Through information supplied by the manufacturer, the 

anticipated solids removal rate is 15 cubic feet per screen per hour. This volume was used to 



A total of 12 primary effluent screens will be installed: two in-service screens will be provided 

for each primary settling tank, and one spare screen for each tank will be stored in the event a 

screen must be replaced. Screen reject will be sent to solids handling through the waste sludge 

line. Each screening unit will be connected to a spray water system to remove the collected 

screenings from the screen panels. The spray water system will be connected to the plant’s 

existing effluent water system or will utilize the screening effluent to wash the screen panels. 

The screenings residuals and washwater will be discharged to a collection trough and will flow 

by gravity to a wet well from where it will be pumped to the sludge thickeners. The screens are 

of sufficient capacity that two would be sufficient under a max flow condition, with one screen 

per tank offline for O&M. 




performance of the MBR process. The constraints for flow distribution at Port Richmond WPCP 


requirements. The following are the major design objectives and parameters for MBR treatment. 

Objectives: 

• Provide capability to direct 100% of influent flow into Aeration Tank influent channel 

Parameters: 

• Design flow: 90 mgd (1.5 x DDWF) 



distribution assumptions for each technology can be seen below in Table 11-1. Gate positioning 

will be optimized to ensure that the flow distribution to each pass meets the requirements shown 

below. 

11-2



DRAFT 

Table 11-1: Operating Flow Distribution Assumptions for MBR 



Membrane Bioreactor 100% NA NA NA 

The entire flow distribution of the aeration tanks will change under the MBR treatment 

alternative. To implement the MBR process, all primary effluent flow will be directed to a point 

20% down the length of Pass A. In addition, an internal recycle will return four times the 

influent flow from the end of Pass C to the primary effluent input point. Two new motor 

operated sluice gates will be installed approximately 40 feet down the length of Pass A to allow 

both primary effluent and internal recycle into Pass A. All existing sluice gates at the head of 

Passes B, C, and D will be closed to allow plug flow through the aeration tanks. The RAS gates 

at the head of Pass A will remain open to allow RAS to flow into the aeration tank. 


The baffle wall locations for the Membrane Bioreactor level of technology were determined 

based on the required volume of each pre-anoxic, anoxic, and oxic zone within each Pass. The 

anticipated baffle wall locations for MBR are seen below in Table 11-2 and a sketch of these 

locations is seen in the drawings in Appendix B. 

Pass 

D 

Table 11-2: Anticipated Inter-Zone Baffle Wall Locations for MBR 

Baffle 1 

(between successive Anoxic/Oxic zones) 

50% from end of pass 







Table 11-3: Anticipated Mixed Liquor Concentrations for MBR 




Membrane Bioreactor 8,500 8,500 8,500 8,500 




11-3



DRAFT 

Table 11-4: Anticipated Mixing Zone Sizing (per tank) for MBR 


Pass Oxic Anoxic 

Pass A 0 89,200 

Pass D 44,600 44,600 






Table 11-5: Anticipated Number of Anoxic Zone Mixers for MBR 

Number of Mixers Per Zone Per Tank 


Pass A N/A 6 

Pass D N/A 3 


The air distribution system (including the main air header, aeration tank headers, pass headers 

and droplegs) under the Membrane Bioreactor design will be very similar to that of the Step Feed 

BNR designs. One difference is that with Pass A and the first half of Pass D being converted to 

totally anoxic zones, there will be no droplegs servicing those two areas. Passes B and C will 

have six droplegs, which will be evenly spaced along the pass length. The last half of Pass D 

will have three droplegs, evenly spaced along the remainder of the pass length. Another 

difference will be an increase in the pipe diameters of the air headers, as more air must be 

directed towards the aeration tanks due the increased operating mixed liquor concentrations and 

the consequential reduction in the oxygen transfer efficiency. 


The quantity of diffusers required for the Membrane Bioreactor design level was based on the air 







11-4



DRAFT 


Table 11-6: Diffuser Requirements for MBR 


(scfm) 


Required (1) 

Membrane Bioreactor 50,200 33,500 





An evaluation was performed to determine the future air requirements for the Membrane 

Bioreactor design level based on the projected flows and loads from the Introduction and the 

projected mass balance for 2045 in Section 2.0. The calculated air requirements can then be 

compared against the existing process aeration system to determine the necessary increase in 

aeration capacity that must be provided. Table 11-7 presents the calculated air requirements. 

Level of 

Treatment 

Table 11-7: Future 2045 Air Requirements for MBR 

Current 



Condition 


(scfm) 

Additional 


Membrane Average 29,558 48,000 0 

Bioreactor Peak Hourly 50,249 48,000 1 




using the existing blowers. A new process air blower will be required as part of the MBR 

alternative. 

The new blower for the MBR alternative was chosen to be the same size as the existing process 

air blowers (24,000 scfm) to provide redundancy and flexibility. As the current blower building 

is not large enough to install an additional blower, a new blower building, housing both the 

additional process air blower and scour air blowers, will be built in the location of the existing 

final settling tanks. As final settling tanks are not needed in MBR operation, the tanks can be 

demolished and a new blower building constructed in its footprint. 

As the new blower will not be housed in the existing process air blower building, an air header 

will be constructed from the new blower to the exiting 54 inch air header that runs along the east 

Aeration Tank Influent Channel. 


11-5



DRAFT 

For the Membrane Bioreactor process, final settling tanks are not required for settling. The tanks 

will be demolished or permanently removed from service to provide room for the additional RAS 

pumps, process air blowers, and scour air blowers needed to operate an MBR treatment train. 

11.6 Return Activated Sludge System/Internal Recycle 



objectives and parameters for MBR treatment. 

Objectives 

• RAS: Remove solids from the membrane tanks and return to the process 

• Internal Recycle: Recycle nitrified effluent to the anoxic zones to facilitate denitrification 

Parameters 

• RAS concentration 8,000 – 10,000 mg/L 

• RAS capacity: 3 times DDWF (180 mgd) 

• Internal Recycle concentration 8,000 – 10,000 mg/L 

• Internal Recycle capacity: 4 times DDWF (240 mgd) 

The MBR process requires significant RAS and internal recycle pumping capacity. The existing 

RAS facilities cannot be used to meet the RAS and internal recycling flow requirements. New 

facilities must be constructed to house additional RAS and recycle pumps. 

RAS will be collected from the MBR process tanks and must be returned to the aeration tanks. 

Flow will be directed to the expanded sludge pumping building. Ten 22.5 mgd RAS pumps will 

be needed to meet the design standard of 180 mgd, with two pumps offline. New suction and 

discharge piping for each pump must be installed. The installation of magnetic flow meters for 

accurate flow control is recommended. 

Internal recycle flow will be collected from the end of Pass C and be directed to the expanded 

sludge pumping building. Ten 30 mgd RAS pumps will be needed to meet the design standard 

of 240 mgd, with two pumps offline. New suction and discharge piping for each pump must be 

installed. The installation of magnetic flow meters for accurate flow control is recommended. 


No modifications to the Waste Activated Sludge System are needed for the Membrane 

Bioreactor level of technology, as per the Advanced Basic BNR Design in Section 6.7. 



A description of the Froth Control Hoods design needed for the Membrane Bioreactor level of 


11-6



DRAFT 


A description of the RAS Chlorination design needed for the Membrane Bioreactor level of 



A description of the Surface Wasting design needed for the Membrane Bioreactor level of 

technology was provided in Section 6.8.3 for the Advanced Basic BNR treatment option. The 

only difference between the Advanced Basic BNR design and the MBR design is that the 

adjustable downward opening gates recommended for surface wasting will be located at the end 

of aerated Pass B instead of mounted on two new surface wasting pump sumps built at the end of 

each Pass A. 



A description of the Alkalinity addition design needed for the Membrane Bioreactor level of 


11.9.2 Carbon 

A description of the Carbon addition design needed for the Membrane Bioreactor level of 

technology was provided in Section 7.9.2 for the Full Step BNR treatment option. However, 

based on a 5-day storage requirement under maximum loading conditions, the Team calculates a 

design storage volume of 10,560 gallons for the MBR alternative. Two 12,000 gallon 

underground storage tanks will be provided for the MBR alternative. 


Construction of an Intermediate Pumping Station is not needed for the Membrane Bioreactor 




No Solids Filters are needed for the Membrane Bioreactor level of technology. 


No Microfilters/Ultrafilters are needed for the Membrane Bioreactor level of technology. 


No Denitrification Filters are needed for the Membrane Bioreactor level of technology. 

11-7



DRAFT 


The Membrane Bioreactor process is used to achieve low levels of nitrogen, solids and 

carbonaceous matter. The overall process will utilize the activated sludge process for treatment, 

but will replace the secondary clarifiers with a membrane filtration process. Because this will be 

a filtration process that doesn’t depend on the capability of solids to settle, the membrane process 

allows significantly higher operating biomass concentrations in the process tanks and therefore a 

comparatively higher treatment capacity for a given tank volume. The objectives include: 


• Achieve low levels of solids (TSS 1 mg/L) 


• Provide sufficient tank volume to meet treatment goals 

• Operation of process tanks at elevated mixed liquor concentration (8,500 mg/L) 

The Membrane Bioreactor (MBR) process will require new fine screening facilities, a new 

Intermittent Pump Station, modification of the existing aeration tanks, new Membrane 

Bioreactor facilities and other supporting equipment. The facilities will be constructed in the 

existing aeration tank volume. Modification of the aeration tanks, including addition of 

Membrane Bioreactors, will be discussed in this section. 

The existing aeration tanks will be retrofitted to provide anoxic/oxic treatment as well as MBR 

modules within the current volume. The aeration treatment at Port Richmond currently consists 

of four aeration tanks, each comprised of four passes arranged in a serpentine manner. The tanks 

are 263 feet long with a width of 104 feet (26 feet per pass) and a side water depth of 17.4 feet. 

For the MBR option, the lengths of each pass will be shortened to allow for installation of the 

MBRs in the western section of the tanks. The MBRs will fit into the last 63 feet of the 

aeration tank, and, taking into account the 3-foot wide MBR influent channel, the new aeration 

tank length will be 197 feet. 

The aeration tank zones will be configured to operate Pass A completely anoxic, Passes B and C 

completely aerobic, and Pass D with the first half anoxic and the second half aerobic. 

Supplemental carbon will be introduced into the first half of Pass D to enhance denitrification. 

Flow will exit Pass D and flow into a 3 foot wide, 416 foot long MBR influent channel, running 

the width of all four aeration tanks. This will enable all MBR tanks to be utilized, even if the 

aeration tank they are installed in is taken offline for service. 

This conceptual design will be based on the Zenon MBR Reactor system, but other vendors 

should be considered during subsequent design phases. The MBR system consists of MBR 

tanks, permeate pumping system, and air scour system. Each MBR tank is 100 feet long and 21 

feet wide. Three MBR tanks will be installed at the western end of each aeration tank, with a 

total of 12 MBR tanks provided. This allows for annual average and maximum flux rates in line 

with the manufacturer’s recommendation with one MBR tank offline. MBRs were designed for 

an annual average flux rate of 10-12 gallons per square foot per day, a max week flux rate of 17 

gallons per square foot per day, and an instantaneous peak of 28 gallons per square foot per day. 

11-8



DRAFT 

The membrane tanks consist of modules containing membrane cassettes, support frames and 

support beams. The Zenon process connects ZeeWeed membrane cassettes to the support frame. 

Permeate will be pulled from the top of each ZeeWeed cassette into a common permeate header. 

Connected to the header is a back pulse header that provides intermittent cleaning of the 

membranes. Permeate will be pulled by the permeate pump system provided by the vendor and 

discharged to either the back pulse storage tank or the disinfection tanks. Below each membrane 

cassette are air scour diffusers that draw air from an air header that extends along the top of the 

tank. The air supply originates at new process scour air blowers 

The nominal pore size of the MBR membranes is 0.04 microns. Each cassette will provided 340 

square feet of contact surface area. A total of 48 cassettes will be provided per module, and 20 

modules will be provided per MBR tank. As mentioned previously, a total of 12 MBR tanks will 

be provided. A diagram showing the MBR set up is shown in Figure 11-1. The target MLSS 

for entry to the MBR tank is 8,500 mg/L. 

Figure 11-1: MBR Setup 

Port Richmond 

Aeration Tank 1, 

Western end 

(not to scale) 

Pass 

A 

Pass 

B 

Pass 

C 

Pass 

D 

MBR Module, 20 

modules per tank 

MBR Tank 1-A 

MBR Tank 1-B 

MBR Tank 1-C 

MBR Cassettes, 48 

cassettes per 

module 

Six 12,000 scfm scour air blowers will be provided. The basis of design was providing 1.4 cfm 

of air per 100 square feet of contact surface area, as per the manufacturer’s recommendation. 

This translates to an anticipated scour air demand of 55,000 scfm. 






11-9



DRAFT 

12 SUMMARY OF COST AND PERFORMANCE 

A summary of the performance of each of the technologies is given below in Table 12-1. 

Table 12-1: Secondary Effluent for Each Level of Technology 

Flow CBOD TSS 

Level of Technology 

(mgd) (mg/L) (mg/L) 

TN 

(mg/L) 

Base Case 60 30 25 13.1 

Existing Conditions 32.8 7.8 11.9 13.1 

Existing Conditions with Filtration 32.8 3 – 5 4 – 5 13.1 

Existing Conditions with Microfiltration/Ultrafiltration 32.8 1 – 2 ~ 1 13.1 

Advanced Basic BNR 38.1 10 – 15 12 – 15 10 – 12 

Full Step BNR 38.1 10 – 15 12 – 15 6 – 10 

Full Step BNR with Filtration 38.1 3 – 5 4 – 5 6 – 10 

Full Step BNR with Microfiltration/Ultrafiltration 38.1 1 – 2 ~ 1 6 – 10 

Full Step BNR with Denitrification Filters 38.1 3 – 5 4 – 5 4 – 5 

Membrane Bioreactors Tanks 38.1 1 – 2 ~ 1 3 - 4 

A capital cost estimate for each level of technology was developed based on the conceptual 

designs presented in this document and the drawings attached in Appendix B. Table 12-2 

provides a summary of anticipated capital construction costs for each level of technology at the 

Port Richmond WPCP. The project executive summary provides details into the contingencies 

used, key cost assumptions, and overall approach to cost estimation. The detailed cost estimates 

for eight technologies at each of the four WPCPs in question can be found in their entirety after 

the four plant-specific conceptual design reports and drawing sets. 

Table 12-2: Capital Construction Costs for Levels of Treatment 

(in Millions of Dollars) 


Capital Construction Cost 

Existing Conditions with Solids Filtration $274 

Existing Conditions with Microfiltration/Ultrafiltration $374 

Advanced Basic BNR $216 

Full Step BNR $270 

Full Step BNR with Solids Filtration $501 

Full Step BNR with Denitrification Filtration $578 

Full Step BNR with Microfiltration/Ultrafiltration $601 

Membrane Bioreactors $1,398 

12-1



DRAFT 

APPENDIX A 

Basis of Design Spreadsheets 

I



DRAFT 

Port Richmond WPCP 

HEP Conceptual Design 

Process Design Criteria for New Facilities – Existing Conditions w Solids Filters 

Parameter Units Minimum Week 

Minimum 

Month 

Annual Average 

Maximum 

Month 

Maximum Week DDWF Maximum Day Peak Hour 

FLOW AND LOAD CONDITIONS (2045) 

influent flow (mgd) 30.7 31.8 38.1 46.5 57.2 60.0 76.2 90.0 

flow peaking factors (%) 81% 83% 100% 122% 150% 200% 200% 

TSS concentrations (mg/L) 199 211 225 227 229 200 190 

TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 

load peaking factors (%) 72% 79% 100% 123% 153% 178% 200% 

CBOD concentrations (mg/L) 183 204 205 214 209 182 173 

CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 


TKN concentrations (mg/L) 25.7 28.7 28.6 29.9 29.1 25.5 24.2 

TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 


SOLID FILTERS 

Filtration Rate (GPM/SF) 3.2 3.3 4.0 4.9 6.0 8.0 9.4 

Required Surface Area (SF) 5,292 5,292 6,615 5,292 5,292 5,292 5,292 

Design Surface Area (+10%) (SF) 5,821 5,821 7,276 5,821 5,821 5,821 5,821 

Surface Area per Filter (SF) 610 610 610 610 610 610 610 

Number of Filters (#) 12 12 12 12 12 12 12 

Medium sand sand sand sand sand sand sand 

Grain Size (mm) 2 2 2 2 2 2 2 

Filter Depth (ft) 6 6 6 6 6 6 6 

Type of Backwash System 

Water Backwash with Auxiliary Air Scour 

Percent of filters being backwashed (%) 17% 17% 17% 17% 17% 17% 17% 

Water backwash rate gal/sf/min 6 6 6 6 6 6 6 

Needed water for backwash gpm 8,800 8,800 8,800 8,800 8,800 8,800 8,800 

Air backwash rate ft3/ft2/min 5 5 5 5 5 5 5 

Needed air for backwash CFM 4,851 4,851 6,063 4,851 4,851 4,851 4,851 

WATER BACKWASH PUMPS FOR FILTERS 

Quantity (#) 3 3 3 3 3 3 3 

Capacity (GPM) 4400 4400 4400 4400 4400 4400 4400 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 50 50 50 50 50 50 50 

Motor Specs (Voltage/Hertz/phase) 480/60/3 480/60/3 480/60/3 480/60/3 480/60/3 480/60/3 480/60/3 

SCOURGE AIR BLOWER FOR FILTERS 

Quantity (#) 3 3 3 3 3 3 3 

Unit Capacity CFM 3,650 3,650 3,650 3,650 3,650 3,650 3,650 

II



DRAFT 



Process Design Criteria for New Facilities – Existing Conditions w Microfiltration/Ultrafiltration 

Parameter Units Minimum Week Minimum Month Annual Average Maximum Month Maximum Week DDWF Maximum Day Peak Hour 





TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 


MICROFILTRATION 

Design Flux Rate gal/sf/d 18 28 

Nominal Pore Size, Microfilter (microns) 0.04 0.04 0.04 0.04 0.04 0.04 0.04 

Filter Surface Area Per Casette (ft2) 340 340 340 340 340 340 340 

Casettes per Module (#) 48 48 48 48 48 48 48 

Modules per Tank (#) 20 20 20 20 20 20 20 

Microfiltration/Ultrafiltration tank length (ft) 100 100 100 100 100 100 100 

Microfiltration/Ultrafiltration tank width (ft) 21 21 21 21 21 21 21 

Contact Surface Area per Microfiltration/Ultrafiltration tank (ft2) 326,400 326,400 326,400 326,400 326,400 326,400 326,400 

Number of Microfiltration/Ultrafiltration Tanks in Operation (#) 10 10 10 10 10 10 10 

Calculated Flux gal/sf/d 9 10 12 14 18 23 28 

Design Number of Microfiltration/Ultrafiltration Tanks (N+1) (#) 11 11 11 11 11 11 11 

Microfiltration/Ultrafiltration Tank Footprint (ft2) 2,100 2,100 2,100 2,100 2,100 2,100 2,100 

Total footprint occupied by Microfiltration/Ultrafiltration (ft2) 23,100 23,100 23,100 23,100 23,100 23,100 23,100 

MEMBRANE AIR 

Microfilter Air Requirement (Method 1) 

cfm/100 sf Surface 

Area 1.4 1.4 1.4 1.4 1.4 1.4 1.4 

Required Scourge Air Demand (Method 1) cfm 50,266 50,266 50,266 50,266 50,266 50,266 50,266 

Microfilter Air Requirement (Method 2) cfm per module 230 230 230 230 230 230 230 


Assumed Blower Size cfm 12,000 12,000 12,000 12,000 12,000 12,000 12,000 

Number of New Blowers Required # 6 6 6 6 6 6 6 

III



DRAFT 



Process Design Criteria for New Facilities - Advanced Basic BNR 

Parameter Units Minimum Week Minimum Month Annual Average 

Maximum 

Month 






TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 


AERATION BASIN MODIFICATION: BAFFLE WALLS 

Number of Aeration tanks (#) 4 4 4 4 4 4 4 

Passes per tank (#) 4 4 4 4 4 4 4 

Tank Length (ft) 263 263 263 263 263 263 263 

Pass Width (ft) 26 26 26 26 26 26 26 

Tank Depth (ft) 17.4 17.4 17.4 17.4 17.4 17.4 17.4 

Number of New Baffle Walls Required per tank (#) 11 11 11 11 11 11 11 

Total Number of Baffle Walls required (#) 44 44 44 44 44 44 44 

AERATION BASIN MODIFICATION: ANOXIC ZONE MIXERS 

Number of Mixers per Anoxic Zone (#) 2 2 2 2 2 2 2 

Mixing Type - Submersible Submersible Submersible Submersible Submersible Submersible Submersible 

Mixer Material - Stainless Steel Stainless Steel Stainless Steel Stainless Steel Stainless Steel Stainless Steel Stainless Steel 

Horsepower hp 7 7 7 7 7 7 7 

Propeller Speed rpm 180 180 180 180 180 180 180 

Electrical Service - 

460 V, 60 Hz, 3 

phase 

461 V, 60 Hz, 3 

phase 

462 V, 60 Hz, 3 

phase 

463 V, 60 Hz, 3 

phase 

464 V, 60 Hz, 3 

phase 

465 V, 60 Hz, 3 

phase 

466 V, 60 Hz, 3 

phase 


Number of anoxic/switch zones per aeration tank (#) 8 8 8 8 8 8 8 

Number of pre-anoxic zones per aeration tank (#) 3 3 3 3 3 3 3 

Total Number of Zones (#) 44 44 44 44 44 44 44 

Total Number of Mixers (#) 88 88 88 88 88 88 88 

AERATION TANK MODIFICATION: SPRAY WATER SYSTEM 

Spray Water discharge flow (gpm/nozzle) 3 3 3 3 3 3 3 

Spray Water discharge pressure (psi) 10 10 10 10 10 10 10 

Nozzle Spacing (ft) 5 5 5 5 5 5 5 

Fan Spread per Nozzle (in) 72 72 72 72 72 72 72 

Nozzles per Tank (#) 172 172 172 172 172 172 172 

Total Nozzles (#) 688 688 688 688 688 688 688 

AERATION TANK MODIFICATION: FLOW DISTRIBUTION 

IV



DRAFT 





Maximum 

Month 


Assumed Flow Split 0-33-33-33 0-33-33-33 0-33-33-33 0-33-33-33 0-33-33-33 0-33-33-33 0-33-33-33 

Necessary Upgrades 

Current infrastructure sufficient 

PROCESS AIR BLOWERS 

Number of Existing Process Air Blowers (#) 4 4 4 4 4 4 4 

Capacity of an Individual Blower (SCFM) 24000 24000 24000 24000 24000 24000 24000 

Total Capacity (Assuming 1 Blower Offline for O&M) (SCFM) 72000 72000 72000 72000 72000 72000 72000 

Biowin predicted air demand (SCFM) 23,507 

Max Day peaking Factor For Design 1.7 

Max Day peaking Factor For Design 39,962 

Design Number of blowers (N+1+1) (# 24,000 SCFM blowers) 4 

RAS PUMPING SYSTEM 

Number of RAS Pumps (#) 5 5 5 5 5 5 5 5 

Number of RAS Pumps assuming 2 offline for O&M (#) 3 3 3 3 3 3 3 3 

Design Standard 

50% of design flow 

Design Condition (mgd) 15.4 15.9 19.1 23.2 28.6 30.0 38.1 45.0 

Capacity of an individual pump (mgd) 5.1 5.3 6.4 7.7 9.5 10.0 12.7 15.0 

WAS PUMPING SYSTEM 

Number of WAS Pumps (#) 3 3 3 3 3 3 3 

Capacity of an individual pump (mgd) 8.6 8.6 8.6 8.6 8.6 8.6 8.6 

Total Capacity (Assuming 1 pump offline for O&M) (mgd) 17.2 17.2 17.2 17.2 17.2 17.2 17.2 


No upgrades to WAS needed 

FROTH HOODS 

Number of Froth Hoods per Aeration Tank (#) 4 4 4 4 4 4 4 

Total Number of Froth Hoods (#) 16 16 16 16 16 16 16 

Maintenance Dose Equivalent (mg/L) 0.5-2.0 0.5-2.0 0.5-2.0 0.5-2.0 0.5-2.0 0.5-2.0 0.5-2.0 

Emergency Dose Equivalent (mg/L) 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 

HYPOCHLORITE STORAGE TANKS 

Average Chlorine Dose in Aeration Basins (mg/L) 2.0 2.0 2.0 2.0 2.0 2.0 2.0 

Required Mass of chlorine (lb/d) 512 529 635 774 952 1,269 1,499 

Required Mass of Sodium Hypochlorite (lb/d) 1,075 1,110 1,332 1,626 1,999 2,665 3,147 

Storage Standard (days) 5 5 5 5 5 5 5 

Assumed Sodium Hypochlorite Concentration (%) 15% 15% 15% 15% 15% 15% 15% 

Volume of Storage Needed (gallons) 4,295 4,437 5,324 6,495 7,986 10,648 12,576 

Assumed AST Capacity (gallons) 4,000 4,000 4,000 4,000 4,000 4,000 4,000 

Number of ASTs Required (#) 4 4 4 4 4 4 4 

Note that tanks will comply with NYSCBS rules (secondary containment, spill protection, etc) 

HYPOCHLORITE METERING PUMPS 

Number of Pumps (#) 2 2 2 2 2 2 2 

Flow (GPM) 189 189 189 189 189 189 189 

Back Pressure (PSI) 75 75 75 75 75 75 75 

Motor Enclosure Type TEFC TEFC TEFC TEFC TEFC TEFC TEFC 

Motor Size (HP) 1 1 1 1 1 1 1 

V



DRAFT 





VI 

Maximum 

Month 


Motor Speed Control VFD VFD VFD VFD VFD VFD VFD 


CENTRATE TREATMENT 

Digested sludge sent via forcemain to Oakwood Beach for dewatering and centrate treatment. 

ALKALINITY STORAGE AND FEED SYSTEM 

Alkalinity Consumption mg CaCO3/mg TKN 7.1 7.1 7.1 7.1 7.1 7.1 7.1 

Design Assumption 

No credit assumed for denitrification 

Assumed Sodium Hydroxide Concentration (%) 25 25 25 25 25 25 25 

Desired Target Residual Alkalinity mg/L as CaCO3 75 75 75 75 75 75 75 

Sodium Hydroxide Consumption (gal/d) 8,603 8,887 10,665 13,011 15,997 21,329 25,192 

Alkalinity Storage design criteria (days) 5 5 5 5 5 5 5 

Sodium Hydroxide storage requirement (gallons) 43,014 44,436 53,323 65,054 79,985 106,646 125,960 

Volume per Storage Tank (gallons) 25,000 25,000 25,000 25,000 25,000 25,000 25,000 

Tank Diameter (ft) 13 13 13 13 13 13 13 

Approximate Working Height (ft) 25 25 25 25 25 25 25 

Number of Tanks Needed (#) 6 6 6 6 6 6 6 

ALKALINITY METERING PUMPS 

Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 

Nominal Back Pressure (PSI) 75 75 75 75 75 75 75 


Motor Size (HP) 1 1 1 1 1 1 1 



ALKALINITY TRANSFER PUMPS 

Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 


SUPPLEMENTAL CARBON 

No supplemental carbon in ABBNR 

FINAL SETTLING TANKS 

Number of Tanks (#) 6 6 6 6 6 6 6 

Tank Length (FT) 298 298 298 298 298 298 298 

Tank Width (FT) 45 45 45 45 45 45 45 

Tank Depth (FT) 10.8 10.8 10.8 10.8 10.8 10.8 10.8 

Total Volume (CF) 868,968 868,968 868,968 868,968 868,968 868,968 868,968 

Total Surface Area (SF) 80,460 80,460 80,460 80,460 80,460 80,460 80,460 

Surface Overflow Rate (GAL/SF/D) 382 395 474 578 710 947 1,119 

Planned Upgrades 

No Upgrades to FSTs planned in ABBNR 

PROCESS CONTROL



DRAFT 





Upgrades to Raw Sewage Pump Station 

Upgrades to PSTs 

Upgrades to Aeration Tanks 

Upgrades to RAS/WAS 

Maximum 

Month 


New ultrasonic sensors in wet well, new seal water instruments for MSPs, local control panels for MSPs, local controls for new influent gate operators 

New magnetic flow meter on 8” sludge pump discharge header, timer-based local control stations for new collector drive mechanism, local timer-based controls for scum skimming, local 

controls for sludge pumps, local controls for sludge degritting equipment and storage, local controls for secondary screens. 

New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header valve to each tank 

shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 

Ultrasonic level measurement and alarm reporting to the Main Control room, new magnetic flow meter for Aeration Tanks waste discharge to thickeners, local controls for surface waste 

pumps, WAS pumps, RAS pumps. 

Upgrades to blowers 

Upgrades to FSTs 

Upgrades to Hypo System 

Upgrades to Chlorine Contact Tanks 

New blower control panels in control room. Interface with local blower speed control resistor panels provided by blower vendor. Blower discharge main air header pressure transmitter. 

Local control stations for new collector drive mechanisms, new mechanical torque switches and alarm. 

Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with high and low 

level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to chlorine contact tanks, wireless radio system to 

transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control panel. 

New colorimetric (HACH CL 17) Residual Chlorine Analyzers for influent and effluent chlorination dosing control. Flow paced residual chlorine dosage control with residual chlorine trim. 

VII



DRAFT 



Process Design Criteria for New Facilities - Full Step BNR 


VIII 

Maximum 

Month 

Maximum 

Week 

DDWF Maximum Day Peak Hour 





TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 





Tank Length (ft) 263 263 263 263 263 263 263 

Pass Width (ft) 26 26 26 26 26 26 26 

Tank Depth (ft) 17.4 17.4 17.4 17.4 17.4 17.4 17.4 










460 V, 60 Hz, 3 

phase 

461 V, 60 Hz, 3 

phase 

462 V, 60 Hz, 3 

phase 

463 V, 60 Hz, 3 

phase 

464 V, 60 Hz, 3 

phase 

465 V, 60 Hz, 3 

phase 

466 V, 60 Hz, 3 

phase 












Total Nozzles (#) 688 688 688 688 688 688 688



DRAFT 





IX 

Maximum 

Month 

Maximum 

Week 





New Primary Effluent Flow Splitter System Needed 





BioWin predicted air demand 25,495 



Design Number of blowers (N+1+1) 4 














FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 


Motor Enclosure Type TEFC TEFC TEFC TEFC TEFC TEFC TEFC



DRAFT 





X 

Maximum 

Month 

Maximum 

Week 


Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 

Assumed Methanol Dosing Concentration (%) 15% 15% 15% 15% 15% 15% 15% 

Assumed Methanol Storage Concentration (%) 100% 100% 100% 100% 100% 100% 100% 

Gallons concentrated methanol needed to denitrify (gal/d) 602 694 836 1,070 1,279 1,488 1,672 

Methanol Storage Criteria (days) 5 5 5 5 5 5 5 

Gallons of concentrated Methanol for storage (gal) 3,010 3,469 4,180 5,350 6,395 7,440 8,360 

UST Capacity (gal) 12,000 12,000 12,000 12,000 12,000 12,000 12,000 

Number of USTs to be Provided (gal) 2 2 2 2 2 2 2 

SUPPLEMENTAL CARBON METERING PUMPS 

Number of Pumps (#) 8 8 8 8 8 8 8



DRAFT 





PROCESS CONTROL 


Maximum 

Month 

Maximum 

Week 


Pump Capacity (GPH) 66 66 66 66 66 66 66 


Tank Length (FT) 298 298 298 298 298 298 298 

Tank Width (FT) 45 45 45 45 45 45 45 

Tank Depth (FT) 10.8 10.8 10.8 10.8 10.8 10.8 10.8 





Weir 

modifications, 

new automated 

scum collection 

system, two new 

scum pumping 

stations, 24-inch 

gate valve at the 

effluent end of 

each FST 









Upgrades to Thickeners 


New magnetic flow meter on 8” sludge pump discharge header, timer-based local control stations for new collector drive mechanism, local timer-based controls for scum skimming, 

local controls for sludge pumps, local controls for sludge degritting equipment and storage, local controls for secondary screens. 

New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header valve to each 

tank shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 

Ultrasonic level measurement and alarm reporting to the Main Control room, new magnetic flow meter for Aeration Tanks waste discharge to thickeners, local controls for surface 

waste pumps, WAS pumps, RAS pumps. 

New blower control panels in control room. Interface with local blower speed control resistor panels provided by blower vendor. Blower discharge main air header pressure 

transmitter. 


Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with high and 

low level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to chlorine contact tanks, wireless radio 

system to transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control panel. 

New colorimetric (HACH CL 17) Residual Chlorine Analyzers for influent and effluent chlorination dosing control. Flow paced residual chlorine dosage control with residual chlorine 

trim. 

New local controls for thickener rake mechanism drive. 

XI



DRAFT 





Maximum 

Month 

Maximum 

Week 


General Upgrades 

Integrated state-of-the art Distributed Control System (DCS) with Area Control Stations (ACS) located throughout the Plant with industrial PC Operator Interface, including local 

control panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This system will use a combination of 

local control panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for data collection and process control. The plant 

telephone system will be a plant wide PC based PBX system, including fiber distributed architecture for modular expansion between buildings, and digital communications and 

networking for voice and data, and wireless phones for designated personnel. The plant two-way radio system will extend communication coverage to all plant areas, including tunnels 

and dead spots locations. The base station will be installed in the Main Control Building. 



Process Design Criteria for New Facilities - Full Step BNR w Solids Filters 


Minimum 

Month 


Maximum 

Month 






TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 





Tank Length (ft) 263 263 263 263 263 263 263 

Pass Width (ft) 26 26 26 26 26 26 26 

Tank Depth (ft) 17.4 17.4 17.4 17.4 17.4 17.4 17.4 








XII



DRAFT 





Minimum 

Month 


Maximum 

Month 




460 V, 60 Hz, 3 

phase 

461 V, 60 Hz, 3 

phase 

462 V, 60 Hz, 3 

phase 

463 V, 60 Hz, 3 

phase 

464 V, 60 Hz, 3 

phase 

465 V, 60 Hz, 3 

phase 

466 V, 60 Hz, 3 

phase 












Total Nozzles (#) 688 688 688 688 688 688 688 









Biowin predicted air demand 25,495 

















FROTH HOODS 





XIII



DRAFT 





Minimum 

Month 


Maximum 

Month 














Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

XIV



DRAFT 





Minimum 

Month 


Maximum 

Month 


Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 













Tank Length (FT) 298 298 298 298 298 298 298 

Tank Width (FT) 45 45 45 45 45 45 45 

Tank Depth (FT) 10.8 10.8 10.8 10.8 10.8 10.8 10.8 





Weir modifications, new automated scum collection system, two new scum pumping stations, 24-inch gate valve at the effluent end of each FST 

SOLID FILTERS 







Grain Size (mm) 2 2 2 2 2 2 2 









WATER BACKWASH PUMPS FOR FILTERS 

Quantity (#) 3 3 3 3 3 3 3 

XV



DRAFT 




SCOURGE AIR BLOWER FOR FILTERS 




Minimum 

Month 


Maximum 

Month 


Capacity (GPM) 4400 4400 4400 4400 4400 4400 4400 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 50 50 50 50 50 50 50 


Quantity (#) 3 3 3 3 3 3 3 



















Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with high and 

low level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to chlorine contact tanks, wireless radio 

system to transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control panel. 


trim. 



Integrated state-of-the art Distributed Control System (DCS) with Area Control Stations (ACS) located throughout the Plant with industrial PC Operator Interface, including local control 

panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This system will use a combination of local 

control panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for data collection and process control. The plant telephone 

system will be a plant wide PC based PBX system, including fiber distributed architecture for modular expansion between buildings, and digital communications and networking for voice 

and data, and wireless phones for designated personnel. The plant two-way radio system will extend communication coverage to all plant areas, including tunnels and dead spots 

locations. The base station will be installed in the Main Control Building. 

XVI



DRAFT 



Process Design Criteria for New Facilities - Full Step BNR w Microfiltration/Ultrafiltration 






TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 





Tank Length (ft) 263 263 263 263 263 263 263 

Pass Width (ft) 26 26 26 26 26 26 26 

Tank Depth (ft) 17.4 17.4 17.4 17.4 17.4 17.4 17.4 










460 V, 60 Hz, 3 

phase 

461 V, 60 Hz, 3 

phase 

462 V, 60 Hz, 3 

phase 

463 V, 60 Hz, 3 

phase 

464 V, 60 Hz, 3 

phase 

465 V, 60 Hz, 3 

phase 

466 V, 60 Hz, 3 

phase 












Total Nozzles (#) 688 688 688 688 688 688 688 


XVII



DRAFT 
















100% of design 

flow 









FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 









XVIII



DRAFT 











Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 













Tank Length (FT) 298 298 298 298 298 298 298 

Tank Width (FT) 45 45 45 45 45 45 45 

Tank Depth (FT) 10.8 10.8 10.8 10.8 10.8 10.8 10.8 











XIX



DRAFT 


Microfiltration/Ultrafiltration tank length (ft) 100 100 100 100 100 100 100 

Microfiltration/Ultrafiltration tank width (ft) 21 21 21 21 21 21 21 

Contact Surface Area per Microfiltration/Ultrafiltration tank (ft2) 326,400 326,400 326,400 326,400 326,400 326,400 326,400 

Number of Microfiltration/Ultrafiltration Tanks in Operation (#) 10 10 10 10 10 10 10 


Design Number of Microfiltration/Ultrafiltration Tanks (N+1) (#) 11 11 11 11 11 11 11 

Microfiltration/Ultrafiltration Tank Footprint (ft2) 2,100 2,100 2,100 2,100 2,100 2,100 2,100 

Total footprint occupied by Microfiltration/Ultrafiltration (ft2) 23,100 23,100 23,100 23,100 23,100 23,100 23,100 

MEMBRANE AIR 


Microfilter Air Requirement (Method 1) 

cfm/100 sf Surface 

Area 1.4 1.4 1.4 1.4 1.4 1.4 1.4 



















New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header valve to each tank 

shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 









trim. 


Integrated state-of-the art Distributed Control System (DCS) with Area Control Stations (ACS) located throughout the Plant with industrial PC Operator Interface, including local control 

panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This system will use a combination of local control 

panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for data collection and process control. The plant telephone system 

will be a plant wide PC based PBX system, including fiber distributed architecture for modular expansion between buildings, and digital communications and networking for voice and 

data, and wireless phones for designated personnel. The plant two-way radio system will extend communication coverage to all plant areas, including tunnels and dead spots locations. The 

base station will be installed in the Main Control Building. 

XX



DRAFT 



Process Design Criteria for New Facilities - Full Step BNR w Denitrification Filters 

Parameter Units Minimum Week Minimum Month 

XXI 

Annual 

Average 

Maximum 

Month 

Maximum 

Week 






TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 





Tank Length (ft) 263 263 263 263 263 263 263 

Pass Width (ft) 26 26 26 26 26 26 26 

Tank Depth (ft) 17.4 17.4 17.4 17.4 17.4 17.4 17.4 










460 V, 60 Hz, 3 

phase 

461 V, 60 Hz, 3 

phase 

462 V, 60 Hz, 3 

phase 

463 V, 60 Hz, 3 

phase 

464 V, 60 Hz, 3 

phase 

465 V, 60 Hz, 3 

phase 

466 V, 60 Hz, 3 

phase 












Total Nozzles (#) 688 688 688 688 688 688 688 

AERATION TANK MODIFICATION: FLOW DISTRIBUTION



DRAFT 





Annual 

Average 

Maximum 

Month 

Maximum 

Week 




New Primary 

Effluent Flow Splitter 

System Needed 






















FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 



XXII



DRAFT 





XXIII 

Annual 

Average 

Maximum 

Month 

Maximum 

Week 


Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 










Pump Capacity (GPH) 66 66 66 66 66 66 66



DRAFT 





Annual 

Average 

Maximum 

Month 

Maximum 

Week 




Tank Length (FT) 298 298 298 298 298 298 298 

Tank Width (FT) 45 45 45 45 45 45 45 

Tank Depth (FT) 10.8 10.8 10.8 10.8 10.8 10.8 10.8 






DENITRIFICATION FILTERS 

Filtration Rate (GPM/SF) 1.6 1.7 2 2.4 3.0 4.0 4.7 






Grain Size (mm) 2 2 2 2 2 2 2 









WATER BACKWASH PUMPS FOR DENITRIFICATION FILTERS 

Quantity (#) 3 3 3 3 3 3 3 

Capacity (GPM) 4000 4000 4000 4000 4000 4000 4000 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 50 50 50 50 50 50 50 


SCOURGE AIR BLOWER FOR DENITRIFICATION FILTERS 

Quantity (#) 3 3 3 3 3 3 3 



Upgrades to Raw Sewage Pump Station New ultrasonic sensors in wet well, new seal water instruments for MSPs, local control panels for MSPs, local controls for new influent gate operators 




New magnetic flow meter on 8” sludge pump discharge header, timer-based local control stations for new collector drive mechanism, local timer-based controls for scum 

skimming, local controls for sludge pumps, local controls for sludge degritting equipment and storage, local controls for secondary screens. 

New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header valve to 

each tank shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 



XXIV



DRAFT 










Annual 

Average 

Maximum 

Month 

Maximum 

Week 



transmitter. 


Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with high 

and low level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to chlorine contact tanks, wireless 

radio system to transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control panel. 

New colorimetric (HACH CL 17) Residual Chlorine Analyzers for influent and effluent chlorination dosing control. Flow paced residual chlorine dosage control with residual 

chlorine trim. 




control panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This system will use a 

combination of local control panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for data collection and process 

control. The plant telephone system will be a plant wide PC based PBX system, including fiber distributed architecture for modular expansion between buildings, and digital 

communications and networking for voice and data, and wireless phones for designated personnel. The plant two-way radio system will extend communication coverage to all 

plant areas, including tunnels and dead spots locations. The base station will be installed in the Main Control Building. 

XXV



DRAFT 



Process Design Criteria for New Facilities - MBR 






TSS load (lb/d) 51,000 56,000 71,438 88,000 109,000 127,000 143,000 



CBOD load (lb/d) 47,000 54,000 65,000 83,200 99,500 115,700 130,000 



TKN load (lb/d) 6,600 7,600 9,100 11,600 13,900 16,200 18,200 


NEW MAIN SEWAGE PUMPS 

Design Condition 

New main sewage pumps will be installed in existing MSP pump stations; capacity will be increased to account for additional headloss 

PRIMARY SCREEN DESIGN CRITERIA (before PSTs) 

Size mm 6 6 6 6 6 6 6 

Type Band Screens Band Screens Band Screens Band Screens Band Screens Band Screens Band Screens 

Screen Design Capacity mgd 30 30 30 30 30 30 30 

Discharge Velocity ft/s 1.87 1.87 1.87 1.87 1.87 1.87 1.87 

Projected Headloss inches 4" to 8" 4" to 8" 4" to 8" 4" to 8" 4" to 8" 4" to 8" 4" to 8" 

Channel Depth ft 12 12 12 12 12 12 12 

Channel Width ft 10.5 10.5 10.5 10.5 10.5 10.5 10.5 

Theoretical Maximum Solids Loading Rate mg/L 120 120 120 120 120 120 120 

Anticipated Solids Removal Rate ft3/hr 20 20 20 20 20 20 20 

Calculated Number of Units # 4 4 4 4 4 4 4 

Number of Primary Settling Tanks # 4 4 4 4 4 4 4 

Number of In-Service Screens Per PST # 1 1 1 1 1 1 1 

Number of Spares Per PST # 1 1 1 1 1 1 1 

Total Number of Primary Screens # 8 8 8 8 8 8 8 

PRIMARY SETTLING TANKS 


Existing primary settling tanks will be demolished and rebuilt 6 feet higher to account for increased headloss 

SECONDARY SCREEN DESIGN CRITERIA (after PSTs) 

Size mm 1 1 1 1 1 1 1 


Screen Design Capacity mgd 15 mgd 16 mgd 17 mgd 18 mgd 19 mgd 20 mgd 21 mgd 


Projected Headloss inches 1 1 1 1 1 1 1 


Channel Width ft 12 12 12 12 12 12 12 


XXVI



DRAFT 






Calculated Number of Units # 2.0 2.1 2.5 3.1 3.8 5.1 6.0 




Total Number of Secondary Screens # 12 12 12 12 12 12 12 

EXISTING AERATION TANK DIMENSIONS 

Number of Aeration Tanks # 4 4 4 4 4 4 4 

Average Aeration Tank Length ft 263 263 263 263 263 263 263 

Average Aeration Tank Width ft 104 104 104 104 104 104 104 

Total Aeration Tank Surface Area ft2 109,408 109,408 109,408 109,408 109,408 109,408 109,408 


BioWin tells us that we can cut out 25,200 of aeration tank footprint and put the MBRs there 

MBR TANK DESIGN CRITERIA 

Nominal Pore Size (microns) 0.04 0.04 0.04 0.04 0.04 0.04 0.04 

Membrane Surface Area per Zenon MBR Cassette (ft2) 340 340 340 340 340 340 340 

Zenon 500D Cassettes per Module (#) 48 48 48 48 48 48 48 

Contact Surface Area per Zenon MBR Cassette (ft2) 16,320 16,320 16,320 16,320 16,320 16,320 16,320 

Modules Per MBR Tank # 20 20 20 20 20 20 20 

Length of MBR Unit ft 100 100 100 100 100 100 100 

Width of MBR unit ft 21 21 21 21 21 21 21 

Total Number of MBR Tanks (By Plant) # 12 12 12 12 12 12 12 

Number of MBR Tanks Per Aeration Tank # 3 3 3 3 3 3 3 

Total Number of Modules # 240 240 240 240 240 240 240 

Calculated Flux (Assuming One Tank Offline) gallons/square feet/day 9 9 11 13 16 21 25 

Design Criteria (Maximums) gallons/square feet/day 10-12 17 28 

MBR Tank Footprint square feet 25,200 25,200 25,200 25,200 25,200 25,200 25,200 

PROCESS AIR 

Required Blower Demand cfm 29,558 50,249 

Exisiting process air blowers # 4 4 4 4 4 4 4 

Capacity of an Individual Blower (SCFM) 24,000 24,000 24,000 24,000 24,000 24,000 24,000 

Existing Capacity (N+1+1) (SCFM) 48,000 48,000 48,000 48,000 48,000 48,000 48,000 

Additional Blower Demand Needed cfm/day 2,249 

Additional Blowers needed # 1 

Assumed Blower Size cfm 24,000 

Design Number of Blowers #, N+1+1 5 

MEMBRANE AIR 

Membrane Air Requirement (Method 1) cfm/100 sf Surface Area 1.4 1.4 1.4 1.4 1.4 1.4 1.4 


Membrane Air Requirement (Method 2) cfm per module 230 230 230 230 230 230 230 


Assumed Blower Size cfm 12,000 12,000 12,000 12,000 12,000 12,000 12,000 12,000 


XXVII



DRAFT 





RAS PUMP CRITERIA 



Design Standard 3Q 3Q 3Q 3Q 3Q 3Q 3Q 3Q 

Design Condition mgd 92 95 114 139 171 180 229 270 


RECYCLE PUMP CRITERIA 

Number of Recycle Pumps (#) 10 10 10 10 10 10 10 10 

Number of Recycle Pumps assuming 1 offline for O&M (#) 8 8 8 8 8 8 8 8 

Design Standard 4Q 4Q 4Q 4Q 4Q 3Q 4Q 4Q 

Design Condition mgd 123 127 152 186 229 240 305 360 


METHANOL STORAGE FACILITY DESIGN CRITERIA 

Demand Methanol Consumption gal/day 760 876 1,056 1,352 1,616 1,880 2,112 

5-Day Storage Requirement gallons 3,802 4,382 5,280 6,758 8,078 9,398 10,560 

Design Capacity, Methanol Storage Tank gallons 12,000 12,000 12,000 12,000 12,000 12,000 12,000 

Calculated Number of UST Storage Tanks # 0.3 0.4 0.4 0.6 0.7 0.8 0.9 

Design Number of Tanks (N+1) # 2 2 2 2 2 2 2 

SODIUM HYDROXIDE STORAGE FACILITY DESIGN CRITERIA 

Alkalinity Demand mg/L 80 80 80 80 80 80 80 

Daily Consumption of Alkalinity moles 434,000 448,000 537,000 656,000 806,000 1,075,000 1,075,000 

Mass of 50% Sodium Hydroxide needed to meet demand kg 24,800 26,100 30,700 37,800 46,500 62,400 62,400 

Gallons of 50% Sodium Hydroxide Needed Per Day gallons 6,600 6,900 8,100 10,000 12,300 16,500 16,500 


Design Capacity, Sodium Hydroxide Storage Tank gallons 25,000 25,000 25,000 25,000 25,000 25,000 25,000 

Calculated Number of FRP Storage Tanks # 1.3 1.4 1.6 2.0 2.5 3.3 3.3 


XXVIII



DRAFT 

APPENDIX B 

Design Drawings 

XXIX


Red Hook 



June 2007 

DRAFT


Red Hook Water Pollution Control Plant 

DRAFT 



1 RED HOOK WATER POLLUTION CONTROL PLANT 1-1 



1.2.1 Plant Hydraulics 1-1 

1.2.2 Influent Screening and Main Sewage Pumping 1-2 

1.2.3 Primary Settling 1-2 

1.2.4 Primary Sludge Pumping and Degritting 1-3 

1.2.5 Aeration 1-3 

1.2.6 Final Settling Tanks 1-4 

1.2.7 Disinfection and Outfall 1-4 

1.2.8 Return Activated Sludge 1-4 

1.2.9 Waste Activated Sludge/Mixed Liquor 1-4 

1.2.10 Sludge Thickening and Elutriation 1-5 

1.2.11 Anaerobic Digestion 1-5 

1.2.12 Sludge Storage and Transfer 1-5 
























4.9.2 Carbon 4-3 

TOC-1



DRAFT 



























5.9.2 Carbon 5-3 


















TOC-2



DRAFT 










6.9.2 Carbon 6-12 



























7.9.2 Carbon 7-6 









TOC-3



DRAFT 



















8.9.2 Carbon 8-3 



























TOC-4



DRAFT 

9.9.2 Carbon 9-3 



























10.9.2 Carbon 10-3 

















TOC-5



DRAFT 











11.9.2 Carbon 11-7 









APPENDIX A 

I 

TOC-6



DRAFT 



Figure 15-1: MBR Setup............................................................................................................ 11-9 



Table 1-1: Red Hook Design Flows............................................................................................. 1-2 

Table 6-1: Operating Flow Distribution Assumptions for ABBNR ............................................ 6-2 

Table 6-2: Anticipated Inter-Zone Baffle Wall Locations for ABBNR ...................................... 6-3 

Table 6-3: Anticipated Mixed Liquor Concentrations for ABBNR ............................................ 6-4 

Table 6-4: Anticipated Mixing Zone Sizing (per tank) for ABBNR ........................................... 6-5 

Table 6-5: Anticipated Number of Anoxic Zone Mixers for ABBNR ........................................ 6-5 

Table 6-6: Diffuser Requirements for ABBNR ........................................................................... 6-6 

Table 6-7: Future 2045 Air Requirements for ABBNR............................................................... 6-7 

Table 7-1: Operating Flow Distribution Assumptions for FSBNR ............................................. 7-1 

Table 7-2: Anticipated Inter-Zone Baffle Wall Locations for FSBNR ....................................... 7-2 

Table 7-3: Anticipated Mixed Liquor Concentrations for FSBNR ............................................. 7-2 

Table 7-4: Anticipated Mixing Zone Sizing (per tank) for FSBNR ............................................ 7-2 

Table 7-5: Anticipated Number of Anoxic Zone Mixers for FSBNR ......................................... 7-3 

Table 7-6: Diffuser Requirements for FSBNR ............................................................................ 7-3 

Table 7-7: Future 2045 Air Requirements for FSBNR................................................................ 7-4 








Table 12-1: Secondary Effluent for Each Level of Technology................................................ 12-1 

Table 12-2: Capital Construction Costs for Levels of Treatment.............................................. 12-1 

TOC-7



DRAFT 

1 RED HOOK WATER POLLUTION CONTROL PLANT 


The Red Hook Water Pollution Control Plant (WPCP) is permitted by the New York State 

Department of Environmental Conservation (NYSDEC) under State Pollutant Discharge 

Elimination System (SPDES) permit number NY-0027073. The facility is located at 63 Flushing 

Avenue, Brooklyn, NY, 11205 in the Red Hook section of Brooklyn, on a 19-acre site adjacent 

to the East River bounded by Flushing Avenue and Navy Street. Drawing 2 shows the limits of 

the service area of the Red Hook WPCP. 

The Red Hook WPCP serves an area of approximately 3,054 acres in the Northwest section of 

Brooklyn, including the communities of Red Hook, Gowanus, Carroll Gardens, Cobble Hill, 

Vinegar Hill, Fulton Ferry, Brooklyn Heights, Downtown, Navy Yard, Clinton Hill, Fort Greene, 

Boerum Hill, Prospect Heights, and Crown Heights. The total sewer length, including sanitary, 

combined, and interceptor sewers, that feeds into the Red Hook WPCP is 137 miles. Drawing 3 

shows the current layout of the Red Hook WPCP. 

The Red Hook plant was opened in 1987 with a step aeration design capacity of 60 MGD. The 

Red Hook WPCP has been providing full secondary treatment since 1989. Processes include 

primary screening, raw sewage pumping, grit removal and primary settling, air activated sludge 

capable of operating in the step aeration mode, final settling, and chlorine disinfection (see 

Figure 3-2). The Red Hook WPCP has a design dry weather flow (DDWF) capacity of 60 MGD, 

and is designed to receive a maximum flow of 120 MGD (2 times DDWF) with 90 MGD (1.5 

times DDWF) receiving secondary treatment. Flows over 90 MGD receive primary treatment 

and disinfection. The daily average flow during Fiscal Year 2005 was 31 MGD, with a dry 

weather flow average of 27 MGD. During severe wet weather events in 2005, the plant treated 

up to 125 MGD. 


The Red Hook WPCP is a secondary treatment plant that provides preliminary screening, 

primary settling, biological treatment through a step-feed activated sludge process, secondary 

settling and disinfection. The combined primary and waste activated sludge flow is gravity 

thickened, anaerobically digested, dewaterered via centrifuges, and treated sent to the head of 

Pass A of aeration tanks. 

1.2.1 Plant Hydraulics 

A 102-inch interceptor delivers flow to the Red Hook WPCP. The influent throttling chamber is 

located at the terminus of the interceptor and is connected to the screening forebay by a 9-foot by 

7-foot influent conduit. At the entrance to the conduit, there is a set of stop log grooves that can 

isolate the flow to the treatment plant. Downstream of the stop log grooves is a 108-inch by 72- 

inch hydraulically operated flow throttling gate used to regulate or shut off flow from the 

influent chamber. High velocities from under the throttling gate are dissipated within the 

1-1



DRAFT 

influent conduit, prior to entry to the screenings forebay, due to the extensive length and a 90- 

degree bend in the influent conduit. 

The plant is permitted to accept up to 120 mgd, or two times the 60 mgd Design Dry Weather 

Flow capacity, as shown in Table 1-1. 

Table 1-1: Red Hook Design Flows 

Red Hook Plant Capacity 

Design Dry Weather Flow 

60 mgd 

Design Wet Weather Flow 

120 mgd 

1.2.2 Influent Screening and Main Sewage Pumping 

At the screenings building, there is a set of stop log grooves in the influent conduit and a 108- 

inch by 72-inch main influent sluice gate that can isolate the flow into the screenings forebay. 

Four screening channels connect the screenings forebay to the wet well. Each screening channel 

has an influent sluice gate and an effluent sluice gate that can isolate the channel when the screen 

is not needed or in the event that screen or channel repair work is necessary. The screens are 6 

feet wide with 1-inch openings and are cleaned with a vertical traveling rake. Each screen is 

designed to handle 53.3 MGD, however, this capacity can be negatively impacted by heavy 

loadings of debris. During wet weather events, plant personnel occasionally flood the screening 

channels to maximize flow and reach 120 MGD. A set of manually operated velocity control 

gates is located in each screen channel, downstream of the screen, to maintain low velocity 

through the screen. 

There are five vertical, centrifugal, mixed-flow, bottom suction, flooded suction main sewage 

pumps, rated at 30 MGD each, at a total dynamic head of 50 feet. Each pump draws flow from 

the wet well via a 36-inch suction line. Discharge from each pump is via a 30-inch line that 

includes a cone check valve and gate valve. The 30-inch lines connect to a 66-inch discharge 

line that conveys the flow to the primary settling tank distribution structure. There is a venturi 

meter on the 66-inch line for flow measurement. 

1.2.3 Primary Settling 

Screened flow is pumped from the Main Sewage Pump Station to a splitter box that distributes 

primary influent to the four primary settling tanks. Flow to individual PSTs can be regulated by 

adjusting influent gates to each of the PSTs. Each PST influent channel serves two PSTs for a 

total of eight PSTs. Each of the four PSTs is 146 feet long and 53 feet wide. The average 

sidewater depth in each rectangular clarifier is 14 feet. Chain and flight mechanisms collect 

grease and other floatables from the top of the tank and sweep primary sludge to the far end of 

the tank where it is pumped to sludge storage and thickening. A primary settling tank effluent 

channel collects PST effluent and sends it through a gallery to the aeration tanks on the other 

side of the street. 

At the Red Hook WPCP, wastewater flows by gravity from the four primary settling tanks, 

through a primary effluent channel that feeds the four aeration tanks. Primary tank effluent is 

1-2



DRAFT 

conveyed to the aeration tanks in a primary effluent channel. During wet weather events, the 

plant uses a secondary bypass channel, which conveys primary effluent to the chlorine contact 

tanks when the flow into the secondary treatment process exceeds 90 MGD. The bypass gate 

automatically opens at a plant flow of 90 MGD. 

1.2.4 Primary Sludge Pumping and Degritting 

Six centrifugal primary sludge pumps are installed at the Red Hook WPCP, each with a capacity 

of 350 gpm. Primary sludge flows through a parshall flume into the Waste Sludge Well. In the 

Waste Sludge Well, the primary sludge is blended with Waste Activated Sludge and balance 

water, and pumped to the Thickeners. 

1.2.5 Aeration 

The flow rate is controlled at each pass by influent sluice gates. The layouts of each of the four 

Aeration Tanks are identical. The assumed flow split of primary effluent among the four passes 

is 0:33:33:33, with centrate, RAS, and gravity thickener overflow being sent to pass A. The 

AWT Team’s Phase I process investigation found that a preponderance of flow heads to Pass D 

and it is difficult with existing infrastructure to achieve this idealized flow split. Flow 

distribution and control is an important factor that can affect nitrogen removal performance of 

any BNR process. The constraints for flow distribution at Red Hook WPCP include the existing 

hydraulic profile, tank size, channel internal structure, and flow requirements. 

The Red Hook WPCP has four, four-pass step-feed ATs. Each pass is approximately 260 feet 

long and 12.5 feet wide with an average side water depth of 22.5 feet deep. Flow travels from 

Pass A to D through a series of openings and baffle walls. Flow travels through an opening in the 

bottom of the shared walls between passes as it moves through the four passes. Flow leaves Pass 

D through effluent troughs that meet flow from the four aeration tanks in the common aeration 

tank effluent channel. 

The current air distribution system was originally designed for BOD removal only. Four process 

air blowers each supplying 9,500 SCFM are available at the facility. During a plant investigation 

related to HEP, plant staff reported that the plant process air header vibrates to an alarming 

degree with a single blower online. Plant staff are uncomfortable running more than one blower 

at a time due to potential damage to the process air header and/or the diffuser grid. It is assumed 

that these operational issues will be corrected prior to the HEP upgrades via a stabilization 

contract, and all four process air blowers will be available as an existing condition for this 

project. Similarly, it is highly unlikely that the existing process air blowers will still be 

operational in 38 years, but the team assumes that they will be replaced by identical blowers via 

a stabilization contract. 

The Team assumes that the existing 9,500 scfm blowers will be replaced in kind prior to the start 

of HEP work, as the HEP design year (2045) is well beyond the usable lifespan of the existing 

equipment. 

1-3



DRAFT 

Currently, Red Hook has 7” diameter ceramic dome type diffusers. The diffusers are distributed 

evenly through the four aeration tanks (i.e., not a tapered design as is seen in the Upper East 

River plants). 

Aeration tank effluent is conveyed to the eight rectangular final settling tanks in an aeration tank 

effluent channel. The total volume of the final settling tanks is 10.5 MG with a surface overflow 

rate of 600 gpd/sf at average design flow. The eight rectangular final settling tanks (FSTs) are 

fed mixed liquor from a single aeration tank effluent channel. It is assumed that aerator effluent 

is distributed evenly to each online FST, although flow instrumentation and control are not 

available at the plant. The tanks are not covered and are fully equipped with sludge collection 

and scum removal equipment. The sludge is collected and directed to wet wells where sludge is 

either returned to the aeration tanks or wasted. Captured scum is directed towards the head of 

the plant through the plant drain. 

1.2.6 Final Settling Tanks 

The aerator effluent (from all four tanks) flows to one common aerator effluent channel, which 

enters the final settling tanks. Flow to the eight final settling tanks is balanced by manual 

adjustment of gates. Each final settling tank is divided into three bays. Each final settling tank is 

250 feet long, 50 feet wide, and has an average sidewater depth of 14 feet. A total of 550 feet of 

discharge weirs is available per final settling tank. 

1.2.7 Disinfection and Outfall 

The disinfection system includes two double pass chlorine contact tanks, three 10,000 gallon 

sodium hypochlorite storage tanks, four metering pumps, and an automated control system. The 

two tanks have a total volume of 1.72 MG and a detention time of 20.6 minutes. The chlorine 

contact tanks are sized such that one tank operating at 120 MGD will provide sufficient contact 

time (greater than 15 minutes). 

Chlorinated effluent is discharged to the East River via a 96-inch outfall. 

1.2.8 Return Activated Sludge 

Return activated sludge (RAS) is conveyed from the final settling tanks to the RAS pumping 

station by gravity and pumped from the wet well into Pass A of the aeration tanks. RAS flow is 

measured on the common RAS line and the lines to the individual aeration tanks. Four RAS 

pumps are installed at the Red Hook WPCP, each with a capacity of 12.1 MGD. Typically one 

or two of these pumps is in operation. 

1.2.9 Waste Activated Sludge/Mixed Liquor 

Waste activated sludge (WAS) is continuously pumped from the RAS stream, flowing through a 

parshall flume to the wasting sludge well, where it is blended with primary degritted solids and 

balance water and pumped to the thickener tanks. There are 3 WAS pumps, of which 2 are 

typically in service. 

1-4



DRAFT 

1.2.10 Sludge Thickening and Elutriation 

Degritted Primary sludge, waste activated sludge and balance water are combined in the wasting 

sludge well. From here the sludge flows through secondary screens and into a splitter box where 

the flow is split to the thickener tanks. Thickener overflow is piped to the aerator influent lines 

(primary effluent) of each aeration tank. If necessary, it can also be diverted to the head of the 

plant. 

Four gravity thickeners are available at the plant, of which two are typically in service. The 

thickeners have a diameter of 60 feet and a surface water depth of 10.25 feet. Two Lobe pumps 

pump the thickened sludge from each tank. The target SVR is typically 0.5 days, but is increased 

to 1.0 days during the winter. 

Elutriation is not practiced at the Red Hook WPCP. 

1.2.11 Anaerobic Digestion 

Thickened sludge flows from the thickener tanks to the digester tanks. Six digesters are 

available at the plant. Typically four are in service, with three serving as primary digesters and 

one as a secondary digester. Each digester has a 60 foot diameter and is 20 feet deep. The target 

HRT for the digestion process at Red Hook is 15 days. 

1.2.12 Sludge Storage and Transfer 

Two sludge storage tanks are provided for the storage of digested sludge. 

Digested sludge is typically dewatered on-site. There are 2 dewatering centrifuges available, of 

which 1 is typically in service. The dewatering operation is based on sludge availability, and 

typically centrifuges are operated 4-7 days-per week. For long periods of time, the centrifuges 

appear to be are operated continuously. Centrate normally flows to the thickener overflow line, 

but can be diverted to the head of the plant if necessary. Digested sludge flows to each centrifuge 

are measured permitting the calculation of the total centrate flow per day. Ferric chloride is 

added to the centrate in the centrate well to control struvite formation and reduce the potential for 

hydrogen sulfide odors. 


Table 1-2 shows a summary of the existing facilities and equipment at the Red Hook WPCP. 

Table 1-2: Red Hook WPCP Existing Facility Description 


Flows 

Average Dry Weather MGD 60 

Maximum for primary treatment MGD 120 

Maximum for secondary treatment MGD 90 

1-5



DRAFT 


Process Headworks 

Interceptor length in 102 

Influent conduit ft x ft 9 x 7 

Influent sluice gate in x in 108 x 72 

Screening 

Screen Channel Width ft 6 

Number of screens 4 

Width of the screen ft 6 

Bar Thickness in 0.5 

Bar Depth in 4 

Clear opening in 1 

Inclination from horizontal degrees 75 

Sewage Pumps 

Number of MSPs 

5 (1 standby) 

Type 

Vertical, mixed-flow 

Pump Speed rpm Variable, 585 (max) 

Capacity MGD 30 

TDH ft 55 



Number 4 

Number of Bays per Tank 3 

Length ft 154 

Width per Tank ft 16 


Total Surface Area - All Tanks ft2 30,360 

Weir Length – All Tanks ft 720 

Weir Loading at Design Flow gpd/ft 83,000 

Surface Loading Rate gpd/sq ft 2000 

Hydraulic Retention Time hrs 1.2 

Primary Sludge Pumps 

Number 


Type 

Centrifugal (Vortex) 

Maximum speed rpm 700 


TDH ft 45 

Unit HP hp 15 

1-6



DRAFT 


Grit Removal 

Number 6 

Type 

Cyclone Degritters 

Rated pressure drop psi 1 

Cyclone Capacity, Each gpm 340 

Design Grit Removal Mesh Size mesh 150 


Number 4 

Number of Passes per Tank 4 

Length ft 260 

Width per Pass ft 50 



Blowers 

Number 4 

Rated Capacity (each) scfm 9,500 

Discharge Pressure psig 10.6 

Unit HP hp 600 

Diameter of Diffuser Tubes in 7 

Number of Diffuser Tubes per Tank 16,650 

Average Height Above Bottom in 9 


Number 8 


Length ft 250 

Width Per Tank ft 50 


Total Volume, All Tanks ft3 175,000 

Surface Area, All Tanks ft2 100,000 

Weir Length (per tank) ft 550 

Chlorine Contact Tanks 

Number 2 

Length ft 210 

Width ft 44 



Weir Length, Per Tank ft 150 

1-7



DRAFT 


Hypo Tanks 

Number 4 

Nominal Capacity, Each gal 12,500 


Height ft 12 

Plant Outfall 

Length ft 1260 

Diameter ft 8 


Number 4 


Side Water Depth ft 10.25 

Center Cone Depth ft 6 

Surface Area per Tank ft2 2,830 

Thickened Sludge Pumps 

Number 8 

Type 

Triplex Plunger 


TDH ft 40 

Unit HP hp 2 

Motor speed rpm 1750 

Digesters 



Volume (each) ft3 90000 

Sludge Heat Exchangers 

Number 8 

Type 

Tube-in-tube 

Capacity of Each BTU/hr 600000 


A key challenge of the Harbor Estuary Plan effort is designing conceptual upgrades for an 

implementation year of 2045. It is highly likely that conditions at the Red Hook WPCP would 

be significantly different if and when a detail-level design to produce biddable plans and 

specifications would be implemented. Existing pumps, blowers, and other equipment will likely 

have been replaced via a stabilization contract, and the NYCDEP will likely have implemented 

1-8



DRAFT 

new technologies to meet new regulatory limits that are not even on the horizon at this time. The 

purpose of this assignment is to produce generalized conceptual designs based on existing 

conditions, but clearly the NYCDEP cannot fully anticipate conditions at its treatment plants 30- 

40 years in the future. 

The AWT Team is not aware of any major capital upgrade at the Red Hook WPCP in the 10-year 

capital plan. Red Hook is included in the Total Residual Chlorine Program, but is only slated for 

optimization upgrades; dechlorination and/or UV disinfection technologies are not currently 

slated for Red Hook. The Team visited the plant and interviewed key staff at the initiation stage 

of this project; plant staff concurred that there were no major upgrades on the horizon for Red 

Hook that would alter the character of the plant. Therefore, the Team used existing conditions as 

its starting point for designing upgrades related to HEP. 

Plant staff report that the existing process air system is in poor condition at the Red Hook WPCP. 

Only one of the four process air blowers can be placed online at a time; plant staff are concerned 

that putting an additional process air blower online could further damage the air header and 

distribution system. It is assumed that these existing limitations will be fixed via a stabilization 

contract well before the anticipated HEP construction start date of 2020. 

Red Hook is a unique treatment plant. The plant operates well below its 60 MGD design dry 

weather flow capacity; the average daily flow in 2005 was 31 MGD. However, the Red Hook 

service area is expected to have significant population and employment increase over the next 

10-15 years to do a construction boom in the area. The plant has severe space constraint 

limitations. Much of the existing footprint is occupied by buildings and tankage. Most of the 

area without tanks/buildings has subsurface galleries, making construction of buildings in this 

area unlikely due to civil/structural limitations. The plant is surrounded on three sides by the 

Brooklyn Navy Yard, making the acquisition of new land unlikely. For technology options that 

require additional footprint (options with solids filters, denitrification filters, microfilters, and 

MBRs) the only option would be to fill a portion of the East River directly to the North of the 

plant. This portion of the East River lies within the NYCDEP property line. The existing slip 

for a sludge storage vessel will have to be relocated. 

The Team assumes a construction start date of 2020 and a 40 percent design contingency in its 

cost estimates. However, both the cost of expanding into New York Harbor and the associated 

permitting and approval process are unknowns with significant risk to delay construction. If 

HEP was to advocate levels of treatment that would necessitate plant footprint expansion, 

regulatory coordination and permitting would become a priority project challenge. 

1-9



DRAFT 


Plant wide process flow diagrams and mass balances for each level of treatment described in 

Section 2.0 are included in the attached drawing packet. The nodes identified along the top of 

each drawing correspond to those shown in the process flow diagram. 

2-1



DRAFT 









• Screening 






Diffusers 










Alkalinity 

Carbon 












analysis. 

3-1



DRAFT 



A description of Red Hook’s PSTs was provided in Section 1. The principal function of the 

primary settling tanks is to removal particulate material to reduce the load on the secondary 

system. In addition, the PSTs contribute to the overall hydraulic profile of the facility. In order 

to implement improvements in downstream facilities such as increased screening and aeration 

tank flow distribution, minor modifications may be needed that may have limited impacts on 

plant hydraulics. For the Existing Conditions with Solids Filtration level of technology, there are 

no modifications necessary. 


There are currently no fine screening units installed at the Red Hook WPCP. No fine screens are 

needed for the Existing Conditions with Solids Filtration level of technology. 


A description of Red Hook’s Aeration Tanks was provided in Section 1. The principal function 

of the aeration tanks is to provide a reactor volume for the activated sludge to take up nutrients, 

thereby removing them from the wastewater. Several operational components of the aeration 

tanks are discussed below. 


Flow distribution and control is an important factor that can affect treatment performance. The 

constraints for flow distribution at Red Hook WPCP include the existing hydraulic profile, tank 

size, channel internal structure, and flow requirements. There are no modifications for the flow 

distribution and control necessary for the Existing Conditions with Solids Filtration level of 

treatment. 



treatment. 



of treatment. 


Air distribution and control is an important factor that can affect treatment performance. There 

are no modifications for the air distribution and control necessary for the Existing Conditions 


4-1



DRAFT 


Diffusers deliver process air to the aeration tanks and also provide a means to keep solids in 

suspension in aerated sections of the aeration tank. There are no modifications for the diffuser 

system necessary for the Existing Conditions with Solids Filtration level of treatment. 


A description of Red Hook’s Process Aeration System was provided in Section 1. The objective 

of the process aeration system is to ensure sufficient air is provided to the biomass. There are no 

modifications to the process aeration system necessary for the Existing Conditions with Solids 

Filtration level of treatment. 


A description of Red Hook’s Final Settling Tanks (FSTs) was provided in Section 1. The 

function of the FSTs is the removal of particulate material to provide high quality treated effluent 

and to return biomass to the aeration tanks to maintain the overall treatment process. No 

modifications to the Final Settling Tanks are needed for the Existing Conditions with Solids 



A description of Red Hook’s RAS system was provided in Section 1. The principal function of 

the RAS system is to maintain the solids inventory in the aeration tanks and return acclimated 

biomass to treatment. No modifications to the Return Activated Sludge System are needed for 



A description of Red Hook’s WAS system was provided in Section 1. No modifications to the 

Waste Activated Sludge System are needed for the Existing Conditions with Solids Filtration 




Currently, spray water is used to control frothing problems; it is only used approximately six 

times a year for a maximum of a week at a time. Froth Control Hoods are not recommended for 



The Red Hook WPCP has an existing sodium hypochlorite storage and feed system, which 

provides chlorine for effluent disinfection. It is assumed that the existing disinfection system 

4-2



DRAFT 

cannot be used for froth control. No additional RAS chlorination measures are recommended for 



There is currently no surface wasting capabilities at the Red Hook WPCP. Surface wasting is 

not recommended for the Existing Conditions with Solids Filtration level of technology. 





4.9.2 Carbon 


technology. 


An intermediate pump station will be provided for this level of technology. It will be located in 

the North section of the WPCP near the filters and will provide eight feet of additional head to 

account for headlosses from this new add-on process technology. A sufficient number of pumps 

will be provided to pump 1.5 times the plant’s design dry weather flow capacity with an N+1+1 

level of redundancy. These pumps will be placed inside a small headed building in parallel to 

each other. Best efforts were made to place this pumphouse in an accessible location to account 

for equipment maintenance and replacement. Emergency power will not be provided for this 

facility; in the event of a blackout, current NYCDEP policy calls for main sewage pumping, 

settling via primary settling, and chlorination along with the powering of vital environmental, 

health, and safety (EH&S) assets. 



Filtration is a process that is installed down stream of a secondary treatment process to enhance 

removal of particulates within the wastewater, including solids, particulate BOD and TKN. 

There are currently no secondary effluent filters at the Red Hook WPCP. 

The addition of conventional filtration after the final settling tanks will achieve lower levels of 





4-3



DRAFT 

The Filters will be placed downstream of the FSTs and upstream of disinfection at Red Hook, 

although the physical location of the filters will be in the newly filled area immediately to the 

North of the existing plant footprint. 

To maintain the efficiency of the Filters, periodic backwashing must be performed to remove the 

accumulated solids. Backwash will be discharged to the head of primary settling tanks. 

Equipment will be provided that will flush the media by recycling the treated effluent to serve as 

wash water. A blower system will also be provided for air scouring of the media when the filter 

units are not operating in a downward flow mode. 

Solids filters were designed for a maximum annual average flux rate of four gallons per minute 

per square foot and a max week flux rate of six gallons per minute per square foot. 

The Team assumes twenty percent of the filters will be offline at any given time for backwash 

and O&M requirements. This translates to a design surface area of 6,283 square feet. The team 

assumes circular denitrification filters, with each filter providing 630 square feet of contact 

surface area. A total of 10 of these filters will be provided. Sand will be the medium of choice. 

The team assumes a grain size of 2 mm and a filter depth of 6 feet. 






be provided, each with a capacity of 3,500 scfm. 



technology. 



technology. 



technology. 




internal environmental evaluation of NYCDEP projects. For all levels of technology, the four 

aeration basins at the Red Hook WPCP will be covered as an odor control provision. Given the 

4-4



DRAFT 

dynamic nature of this field, a placeholder cost was included for odor control provisions, with 

the understanding that appropriate technologies will be implemented at the time of detailed 

design after consultation with BEPA. 

4-5



DRAFT 







2 mm fine screens are recommended for this level of technology; they will be placed in the 

secondary effluent immediately upstream of the intermediate pump station prior to the 

microfiltration/ultrafiltration tanks. 


screen has a design capacity of 15 MGD and assumes discharge velocity of 0.87 feet per second. 



was designed conservatively in order to minimize fouling and required plant O&M activities. 

Through information supplied by the manufacturer, the anticipated solids removal rate is 15 

cubic feet per screen per hour. This volume is used to calculate the additional screenings 

processing infrastructure needed as well as the impact on the O&M disposal costs for grit. A 

total of 12 secondary screens will be installed, three for each of the four PSTs. The screens are 

of sufficient capacity that two would be sufficient under a max flow condition, with one screen 

per tank offline for O&M. 














5-1



DRAFT 





















No additional RAS chlorination measures are recommended for the Existing Conditions with 







5-2



DRAFT 



5.9.2 Carbon 





the North section of the WPCP near the filters and will provide ten feet of additional head to 







settling via PSTs, and chlorination along with the powering of vital EH&S assets. 






Microfiltration/ultrafiltration is a process that is installed down stream of a secondary treatment 


be beyond those capable with conventional filtration. There are currently no secondary effluent 

microfilters at the Red Hook WPCP. 

The addition of microfiltration/ultrafiltration after the final settling tanks will achieve lower 

levels of particulates in the waste stream. The objectives include: 




This conceptual design will be based on the Zenon membrane system, but other vendors should 

be considered during subsequent design phases. The membrane system consists of membrane 

units and an air scour system. Each membrane unit is 68 ft. long, 18.5 ft. wide, and 12 deep. 

Three membrane units will be installed in each tank. The membrane unit consists of a cassette, 

support frames and support beams. The Zenon process connects ZeeWeed membrane cassettes 

to the support frame. Permeate will be pulled from the top of each ZeeWeed cassette into a 

5-3



DRAFT 

common permeate header. Connected to the header is a back pulse header that provides 

intermittent cleaning of the membranes. Permeate will be pulled by the permeate pump system 

provided by the vendor and discharged to either the back pulse storage tank or the disinfection 

tanks. Below each membrane cassette are air scour diffusers that draw air from an air header that 

extends along the top of the tank. The air supply originates at new process scour air blowers 

The nominal pore size of membrane cassettes is 0.04 microns. 340 square feet of contact surface 

area will be provided per cassette, and a total of 48 cassettes will be provided per module. 

Twenty modules will be provided per MBR tank. The target MLSS for entry to the MBR tank is 

8,000 mg/L, with an exit MLSS of 10,000 mg/L. Each MBR tank will be 100 feet long and 21 

feet wide. A total of 11 MBR tanks will be provided. This allows for annual average and 

maximum flux rates in line with the manufacturer’s recommendation with one MBR tank offline. 

The basis of design was providing 1.4 cfm of air per 100 square feet of contact surface area, as 

per the manufacturer’s recommendation. This translates to an anticipated scour air demand of 

50,000 scfm. Six 12,000 scfm blowers will be provided. 










internal environmental evaluation of NYCDEP projects. For all levels of technology, the four 

aeration basins at the Red Hook WPCP will be covered as an odor control provision. Given the 

dynamic nature of this field, a placeholder cost was included for odor control provisions, with 

the understanding that appropriate technologies will be implemented at the time of detailed 

design after consultation with BEPA. 

5-4



DRAFT 



The principal function of the primary settling tanks is to removal particulate material to reduce 

the load on the secondary system. In addition, the PSTs contribute to the overall hydraulic 

profile of the facility. In order to implement improvements in downstream facilities such flow 

distribution in aeration tanks, minor modifications will be needed that may have limited impacts 

on plant hydraulics. A complete reassessment of plant hydraulics is beyond the scope of this 

conceptual study. 






performance of any BNR process. The constraints for flow distribution at Red Hook WPCP 


requirements. The following are the major design objectives and parameters for Advanced Basic 

BNR treatment. 

Objectives: 



pass 



Parameters: 



Pass A: 0 - 30 mgd (0 to 30 %) 

Pass B: 6 - 45 mgd (20 to 50%) 

Pass C: 6 - 45 mgd (20 to 50%) 

Pass D: 0 - 32 mgd (0 to 35%) 



distribution assumptions can be seen below in Table 6-1. Gate positioning will be optimized to 

ensure that the flow distribution to each pass meets the requirements shown below. Several of 

6-1



DRAFT 

the existing influent sluice gates to aeration tank passes are broken and cannot be adjusted in the 

field. It is assumed that these gates will be fixed via a stabilization contract well before any 

HEP-related upgrade is constructed. 





Gate positioning will be optimized to meet a 0:33:33:33 flow split to Passes A, B, C, and D. The 

gate to Pass D will require the installation of a motorized gate control containing an automated 

actuator to provide rapid response during storm events. This automated gate control actuator 

will open the gate fully to allow all Aeration Tank flow to enter into the head of Pass D. A gate 

controller will be tied into the plant SCADA control system to allow for either flow paced or 

manual control. 





baffle wall 






• Flow assumptions from Table 6-1: Operating Flow Distribution Assumptions for ABBNR 


anoxic, and oxic zone within each Pass. The anticipated baffle wall locations for Advanced 

Basic BNR are seen below in Table 6-2 and a sketch of these locations is seen in the attached 

drawing set. 

6-2



DRAFT 

Pass 

A 

B 

C 

D 




zones 


(between Oxic 





zones) 


Pass) 

1/6 length of 

5% from end 


N/A 

pass 

of pass 

1/6 length of 

5% from end 


N/A 

pass 

1/6 length of 

pass 

1/6 length of 

pass 


of pass 

10% from end 

of pass 

N/A 

1/3 length of pass N/A N/A N/A 

The major design differences between the treatment levels are a function of the complexity of the 

proposed BNR system and associated zones. A common component in each of the proposed 

upgrades is the type of new baffle walls. 

Each level of technology requires new inter-zone baffle walls to separate the treatment zones. 

These baffle walls will be installed across the entire width of each pass and will be modular in 

nature but sufficiently stable to withstand the applied forces and the corrosive nature of the 

wastewater. The walls will have removable sections to allow changes in the process. The height 

of the baffle walls will be determined and adjusted in the field based on the flow through each 

pass to achieve a minimum velocity of 1 foot per second across the wall. 

The lower section of the walls will be permanent from tank bottom to approximately 19.5 feet. 

On each end, the existing Y shaped walls will be squared off from the top of the Y down 

vertically to the new permanent wall section. Concrete columns with channels will be installed 

parallel to the squared off portion and extend from the top of the permanent wall to the full 

height of the aeration tanks. The channels will allow baffle sections to slide into place in order 

to achieve desired baffle wall height. These sections will be made of wood or FRP and will be 

accessible through a removable hatch to be constructed above each new baffle wall. In order to 

install these new baffles, a sizable section of the aeration tank ceilings will have to be excavated 

and removed. In addition, the permanent wall section will include three 1-foot by 1-foot 

openings at the floor of the tank to allow filling and draining of the tank. 

The design of the advanced basic BNR baffle walls will take advantage of existing wall 

locations. Eleven (11) new baffle walls will be installed in each tank to separate the different 

pre-anoxic, anoxic and oxic zones. There will be no other baffle wall modifications as this 

option mandates no changes be made to existing equipment or process structures (i.e. baffle 

walls). 

6-3



DRAFT 



given below: 

Objectives: 




Parameters: 



• Mixed Liquor Suspended Solids (MLSS) concentrations: 

Pass A: 4,000 to 8,000 mg/L 

Pass B: 2,000 to 6,000 mg/L 

Pass C: 1,500 to 4,000 mg/L 

Pass D: 1,000 to 3,000 mg/L 

Target AEMLSS Concentration: 2,000 mg/L 

Mechanical mixers are proposed for installation in the Aeration Tanks to keep the mixed liquor 

in suspension in the anoxic and pre-anoxic zones. Submersible stainless steel mixers are 

proposed for this conceptual design. Each mixer will have 7 hp and a propeller speed of 180 

rpm. The mixers will be connected to a local control panel to provide on/off control. The 

control panel will have the capability to send a signal to a central location (SCADA) to monitor 

the status of the mixer. It is estimated that two mixers will be required in each anoxic zone, and 

that 2 spare mixers per anoxic zones will be kept as replacements, resulting in a total of 44 

mixers per tank for the ABBNR technology. Each mixer will be mounted from the top of the 

reactor with a supporting structure as suggested by the vendor. 











6-4



DRAFT 




Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 12,200 12,200 45,800 3,700 

Pass B 12,200 12,200 45,800 3,700 

Pass C 12,200 12,200 42,100 7,400 

Pass D 12,200 12,200 49,500 





of anoxic zone mixers necessary is shown below in Table 6-5. 

Pass 


Number of Mixers Per Zone Per Tank – (88 Mixers Total) 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 




Pass D 2 2 N/A 


With the new Advanced Basic BNR technology design levels, air requirements are anticipated to 

increase. The air distribution system will need enhancements to supply the increased air volume 

that will be directed into the aeration tanks. The objectives of the process aeration upgrades are 

to ensure sufficient air is provided for nitrification and to optimize the control of DO levels. 

These objectives include: 





6-5



DRAFT 

Under the Advanced Basic BNR design level, the 54 inch main air header will continue to run 

along the East Aeration Tank influent channel and distribute air to eight smaller pass header 

lines, located in the Y-walls separating the A/B and C/D passes in each tank. The smaller header 

lines will feed droplegs that will provide process air to the diffusers covering the floor of each 

aeration tank. The main header decreases in diameter from 54 inches to 24 inches as it feeds the 

smaller headers. The smaller headers decrease in diameter from 24 inches to 8 inches as they 

feed the aeration tank. Motorized butterfly valves will provide the aeration tank headers with 

increased flow control and allow for an aeration tank to be taken offline. 

Six droplegs will branch off of the pass headers into each pass. In the ABBNR design, for 

Passes A, B, C, and D, both switch zones at the head of the pass will have a dropleg and 

connected diffuser grid and the remaining four droplegs will service the oxic zone. Each dropleg 

will be provided with a butterfly valve. 


With the increase in the aeration capacity under the new Advanced Basic BNR design upgrades, 

the diffuser grids will be redesigned to provide a distribution of air throughout the aeration tank 

oxic zones and switch zones. The objectives of the process aeration upgrades are to ensure 

sufficient air is provided for nitrification and to optimize the control of DO levels. These 

objectives include: 


• Provide flexibility for different process operating conditions, including the implementation of 

switch zones 


The quantity of diffusers required for each design level was based on the air requirements that 

will be shown in the next section. The selected diffuser type was the 9” diameter fine bubble 

membrane disc diffuser with a manufacturer recommended air flow range of 1 to 3 scfm per 

diffuser. An average flow of 1.5 scfm per diffuser was initially assumed under average loading 

conditions. Anticipated variations in loads were evaluated to ensure sufficient capacity was 

available and that the diffusers operated within their appropriate manufacturer-suggested typical 

range. Table 6-6 shows the required diffusers. 




(scfm) 


Required (1) 



The Team checked that the available floor area in the aeration tanks is sufficient to provide the 

required oxygen demand at the above air flow rates. It appears that there is sufficient space 

available, but further refinement of the tapered diffuser design should be pursued to ensure 

proper configuration of the diffuser grid. 

6-6



DRAFT 






new air requirements and allow the facility to fully utilize the new technologies, the process air 

blower system will need to be enhanced. 


nitrification and to optimize the control of DO levels. These objectives include: 






conditions 






Level of 

Treatment 

Table 6-7: Future 2045 Air Requirements for ABBNR 

Aeration 

Current Blower 

Tank BioWin Predicted Capacity 

Loading Air Demand (scfm) (2 offline) 

Condition 

(scfm) 

Additional 

Blowers 

Needed 

Advanced Average 15,570 19,000 0 

Basic BNR Peak Hourly 26,469 19,000 1 



The existing system was evaluated and one additional process air blower is needed to provide the 

spare and standby requirements identified in the BNR design guidance documents (N+1+1) for 

the Advanced Basic BNR level of technology. 

It is assumed for this conceptual design that a single additional process air blower can be 

shoehorned into existing facilities and/or galleries, and an additional building or gallery will not 

be necessary. 

6-7



DRAFT 

It should be noted that civil/structural concerns were accounted for when evaluating the Main 

Building at the Red Hook WPCP in addition to other buildings on site. This level of technology 

is not expected to increase loads on existing structures by more than 10 percent. 



technology. 





Objectives: 






Parameters: 




The required RAS capacity of 30 MGD total can be achieved with a single additional RAS 

pump. It is assumed that this additional pump can be shoehorned into the existing gallery near 

the existing RAS pumps rather than constructing an additional structure for this unit. The 

installation of magnetic flow meters for accurate flow control is recommended. Respective 

suction and discharge piping for each pump must also be replaced. Furthermore, the existing 

suction and discharge headers may be insufficient to handle the proposed flow and may need to 

be replaced by larger piping and valves. 



Objectives: 



6-8



DRAFT 


Aeration Tank 




Parameters: 



• Design flow operating range: 

WAS: 0.6 – 2.4 mgd 

Aeration Tank Effluent: 3.0 – 12 mgd 

For the Advanced Basic BNR alternative, sludge will be wasted from the final settling tank 

underflow, as opposed to the aerator effluent mixed liquor line. This will result in a higher solids 

concentration in the waste flow, reducing the overall waste flow volume. The BNR treatment 

alternative includes increasing the solids inventory of the aeration tanks to provide more biomass 

for nutrient removal. Thus, there is a reduced wasting rate from current conditions. For this 

level of treatment, the existing WAS pumps are sufficient to handle the new operating 

conditions. New flow meters will be installed in order to accurately measure the wasting rate to 

enable better process control. 







Once at the surface, the froth tends to stay there, causing the operational problems. 










follows: 

6-9



DRAFT 


pass length 








A typical froth control hood includes chemical storage and feed, dilution water pumping, 

distribution system, nozzles to spray the chlorine solution onto the water surface and protective 

enclosures to avoid personnel contact with the chlorinated spray. The chemical storage and feed 

facility will be described in the RAS Chlorination section. 

As indicated above, a total of four froth control hoods will be required per tank. The spray 

headers installed will have connectors, nozzle pipe leads, nozzle fittings and nozzles to apply the 

chlorinated spray. The distance between nozzle connections will be determined by the nozzle 

type and dose requirements. It can be assumed that approximately six nozzle connections will be 

installed per hood. The spray nozzles will be installed at approximately 3 feet above the water 

surface to provide enough elevation for sufficient spray coverage. Each individual spray nozzle 

pipe lead will be provided with individual quick disconnects or unions to facilitate removal for 



main. There will be distribution piping extended from the main to the side of each of the hoods. 

From there it will be divided into each of the nozzle pipes. 

Hatches will provide personnel access to the sliding retractable baffle segments. These segments 

will be lifted in unison by an actuated mechanism located atop the hood structure. These 

adjacent flaps will span the width of the pass and extend below the water surface to trap the foam 

within the enclosed hood area. The flaps will facilitate the trapping of the froth to ensure 

effective chlorination. They shall be retractable by mechanically sliding them up to allow any 

trapped material to flow freely on the surface of the water when the hood is not in use. A 

mechanism will be included to lock the flaps into place when raised by personnel. 

Chlorine storage, feed and distribution throughout the plant is included in another section. 

Piping will be used to bring the chlorine solution from the distribution main to each hood. A 

dual strainer will be installed for each aeration tank with an interconnection that will allow it to 

serve two tanks, providing sufficient redundancy. 



formation and poor settling secondary solids. It is assumed that the existing disinfection system 

will not be sufficient for froth control at the increased RAS flow rates. Instead, a dedicated 

chemical storage and feed facility will be constructed over an existing parking lot at the West 

6-10



DRAFT 

end of the facility. This facility will include alkalinity, chlorine for froth control, and 

supplemental carbon for appropriate alternatives. 






Assuming a target chlorine dose of 2.0 mg/L in the aeration basins, an assumed sodium 

hypochlorite storage concentration of 15 percent, and a 5-day chemical storage requirement, the 

Team calculates a design storage volume of 12,576 gallons. This will be provided via four 

4,000-gallon aboveground storage tanks (ASTs). All tanks will comply with New York State 

Chemical Bulk Storage regulations, such as secondary containment, spill protection, and leak 

detection systems. 

The Team assumes two hypochlorite metering pumps, each with a capacity of 189 gallons per 

minute. Each pump will be powered by a 1 hp motor equipped with a VFD. 



froth formation and provide SRT control. Currently there is no surface wasting capabilities at 

the Red Hook WPCP. Implementation of surface wasting to control the secondary treatment 

process reduces the potential for froth formation. The design objectives as described in the 

BNR design guidance document include: 






• Allow for the wasted solids to be accounted for within the SRT calculations 

Adjustable downward opening gates are recommended for surface wasting for the Red Hook 

WPCP. The downward opening gates will be mounted on two new surface wasting pump sumps 

built at the end of each Pass A. Lowering a gate(s) will allow the froth and/or MLSS to overflow 

the weir into the surface wasting pump station(s). The surface waste will be pumped to the 

existing waste activated sludge wet well near the Final Settling Tanks for further delivery to 

sludge processing. The flow and TSS concentration of the surface waste will be measured and 

totalized. The flow and TSS data will dictate time based operation of the pumps to preventing 

overwasting. The elevation of the downward opening gates will be operated either automatically 

or manually based on the aeration tank wastewater elevation. 

6-11



DRAFT 



New York wastewaters are low in alkalinity and nitrification can consume significant amounts of 

alkalinity. Consumption of alkalinity can decrease pH, which can, in turn, decrease the rate of 

nitrification. Therefore, alkalinity addition is an important component of BNR strategies. 

The design objectives for Advanced Basic BNR include the following: 


• Maintain 50 to 100 mg/L CaCO 3 in all passes 




New Sodium Hydroxide tanks will be placed in the aforementioned new chemical storage and 

feed facility, which will also feature sodium chloride storage and feed, and methanol storage and 

feed. 

The Team conservatively assumes no alkalinity credit for denitrification. The Team assumes an 

alkalinity consumption of 7.1 mg CaCO3 per mg of TKN. The Team assumes a Sodium 

Hydroxide storage concentration of 25 percent and a target residual alkalinity concentration of 

75 mg/L as CaCO3. Based on a 5-day storage requirement, the Team calculates a need for 

125,960 gallons of storage. This will be provided by 6 25,000-gallon storage tanks. Each tank 

will have a diameter of 13 feet and an effective height of 25 feet. 

Four alkalinity metering pumps will be provided. Each pump will have a design flowrate of 833 

gallons per minute with a design backpressure of 75 psi. Each pump will be powered by a 1 

horsepower motor. 

Two alkalinity transfer pumps will be provided. These pumps will have a 150 gallon per minute 

flowrate. Each pump will have a 3 horsepower motor and be able to provide a total dynamic 

head of 75 psi. 

6.9.2 Carbon 






6-12



DRAFT 










The four aeration basins at the Red Hook WPCP are located indoors as an odor control 




6-13



DRAFT 



No modifications to the Primary Settling Tanks are needed for the Full Step BNR level of 

technology. In order to implement improvements in downstream facilities such as enhanced 

flow distribution in aeration tanks, minor modifications will be needed that may have limited 

impacts on plant hydraulics. A complete reassessment of plant hydraulics is beyond the scope of 

this conceptual study. 











Full Step BNR 10% 40% 30% 20% 


distribution and gate setting. Gate positioning will be optimized to meet a 10:40:30:20 flow split 

to Passes A, B, C, and D. The gate to Pass D will require the installation of a motorized gate 


automated gate control actuator will open the gate fully to allow all Aeration Tank flow to enter 

into the head of Pass D. A gate controller will be tied into the plant SCADA control system to 

allow for either flow paced or manual control. 




are seen below in Table 7-2 and a sketch of these locations is seen in the drawing set. The only 

difference between the baffle wall design from the Advanced Basic BNR to the Full Step BNR 

technology is the number of walls installed in Pass D. 

7-1



DRAFT 

Pass 

A 

B 

C 

D 




zones 


(between Oxic 





zones) 


Pass) 

1/6 length of 



N/A 

pass 

pass of pass 

1/6 length of 

5% from end 


N/A 

pass 

1/6 length of 

pass 

1/6 length of 

pass 



1/2 length of 

pass 

of pass 

10% from end 

of pass 

N/A 

N/A 

N/A 











Full Step BNR 6,558 3,810 2,899 2,500 




Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 12,200 12,200 12,200 32,900 3,700 

Pass B 12,200 12,200 45,100 3,700 

Pass C 12,200 12,200 41,400 7,400 

Pass D 12,200 12,200 12,200 36,600 

7-2



DRAFT 






Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 2 2 2 N/A 2 








The anticipated mixed liquor concentrations are shown below. The stainless steel mixers are 

assumed to draw 7 horsepower each. The propeller speed is assumed to be 180 rpm, and the 

electrical service is assumed to be 60V, 60 Hz, 3 phase. 


With the Full Step BNR technology design levels, air requirements are anticipated to increase 

slightly from those needed at Advanced Basic BNR. The air distribution system will need minor 

enhancements to supply the increased air volume that will be directed into the aeration tanks. 

Detailed design of this distribution system is beyond the scope of this conceptual report. 













(scfm) 


Required (1) 

7-3



DRAFT 

Full Step BNR 29,997 19,998 














Level of 

Treatment 

Full Step BNR 


Current 



Condition 


(scfm) 

Additional 


Average 17,645 19,000 0 

Peak Hourly 29,997 19,000 2 




using the existing blowers. The Team assumes that the two additional process air blowers 

needed to meet the spare and standby redundancy requirements can be shoehorned into existing 

facilities and/or galleries, and an additional building or gallery to house the additional process air 

blowers will not be necessary. 



technology. 


7-4



DRAFT 




Objectives 





Parameters 





To achieve desired flow capacity with the same number of units in operation and standby as the 

existing operational scheme, additional RAS pump capacity is needed. Three additional 12.1 

MGD RAS pumps are needed, bringing the total RAS capacity to 84.7 MGD. With one pump 

offline for repairs and one pump offline for maintenance, the RAS pumping capacity would be 

60.5 MGD, greater than the DDWF of 60 MGD. 


No modifications to the Waste Activated Sludge System are needed for the Full Step BNR level 

of technology, as per the Advanced Basic BNR Design in Section 6.7. 












7-5



DRAFT 


A description of the Alkalinity addition design needed for the Full Step BNR level of technology 


7.9.2 Carbon 

New York City wastewater has a relatively low readily biodegradable carbon content and the 

carbon available in the wastewater may be insufficient to promote sufficient denitrification to 

meet low levels of nitrogen. Supplemental carbon addition will be required for this level of 

technology. The Red Hook WPCP does not have existing supplemental carbon addition 

facilities. 

Supplemental carbon addition will be incorporated at the Full Step BNR, Full Step BNR with 

denitrification Filters, Full Step BNR with solids filters, Full Step BNR with microfilter, and 

Membrane Bioreactor Tank levels of treatment. The design objectives and features as described 

in the BNR design guidance include the following: 

• Provide supplemental carbon to enhance denitrification. 

• Provide capability to feed to the head of all anoxic zones. 


BOD, and TKN with a feedback bias based on residual nitrate measurement. 

• Provide mixing at dosage points. 

• Provide 4 to 5 days of chemical storage under average conditions. 




systems are subject to the regulations of several entities including the Department of 


guidelines provided by independent associations such as the National Fire Protection Association 

and the Manufacturing Chemists Association; and precautions and requirements imposed by 

insurance providers. It is important to recognize that, in addition to basic system requirements 

identified by the conceptual design needs, a methanol system will have ancillary requirements, 

such as the need for explosion proof equipment and lighting, which will contribute significantly 

to the cost of the installation. 




chemical in the process stream. A separate chemical mixing device will not be provided. 

The Team assumes a design methanol storage concentration of 100 percent and a methanol 

dosing concentration of 15 percent. Based on a 5-day storage requirement under maximum 

loading conditions, the Team calculates a design storage volume of 9,340 gallons. A single 

12,000 gallon underground storage tank will be provided for the FSBNR alternatives. 

7-6



DRAFT 



technology. 















7-7



DRAFT 




Filtration level of technology. In order to implement improvements in downstream facilities 

such flow distribution in aeration tanks, minor modifications will be needed that may have 

limited impacts on plant hydraulics. A complete reassessment of plant hydraulics is beyond the 

scope of this conceptual study. This option includes an intermediate pump station after 

secondary clarification to provide sufficient head for the add-on filtration process. 
















BNR with Solids Filtration level of technology was provided in Section 7.3.4 for the Full Step 







8-1



DRAFT 













Solids Filtration level of technology, as per the Advanced Basic BNR Design in Section 6.7. 













option. 






8-2



DRAFT 

8.9.2 Carbon 




















technology. 



technology. 



technology. 






8-3



DRAFT 




Microfiltration/Ultrafiltration level of technology. In order to implement improvements in 

downstream facilities such flow distribution in aeration tanks, minor modifications will be 

needed that may have limited impacts on plant hydraulics. A complete reassessment of plant 

hydraulics is beyond the scope of this conceptual study. This option includes an intermediate 

pump station after secondary clarification to provide sufficient head for the add-on filtration 

process. 





















the Full Step BNR treatment option. 


9-1



DRAFT 

















Microfiltration/Ultrafiltration level of technology, as per the Advanced Basic BNR Design in 

Section 7.3.7. 














9-2



DRAFT 






9.9.2 Carbon 






the North section of the WPCP near the filters and will provide ten feet of additional head to 











technology. 









9-3



DRAFT 








9-4



DRAFT 




Denitrification Filters level of technology. In addition, the PSTs contribute to the overall 

hydraulic profile of the facility. In order to implement improvements in downstream facilities 

such flow distribution in aeration tanks, minor modifications will be needed that may have 

limited impacts on plant hydraulics. A complete reassessment of plant hydraulics is beyond the 

scope of this conceptual study. Options including an add on filtration technology include an 

intermediate pump station to provide sufficient head for the additional process. 



technology. 




















10-1



DRAFT 














Denitrification Filters level of technology, as per the Advanced Basic BNR Design in Section 

6.7. 









option. 




option. 



10-2



DRAFT 



option. 

10.9.2 Carbon 



This technology includes the process flexibility to dose both the denitrification filters and the 

anoxic zones of the aeration tanks with supplemental carbon. 














technology. 



technology. 


Serving as an enhancement to the Full Step Feed BNR design, Denitrification Filters can be 

added downstream of the final settling tanks to treat nitrified secondary effluent. There are 

currently no Denitrification Filters at the Red Hook WPCP. 

The addition of Denitrification Filters to the Full Step Feed BNR design level will achieve lower 

levels of nitrogen and provide filtration to remove additional particulate matter from the waste 

stream. The addition of denitrification filters allows the step feed process tanks to operate with 

additional aerated zone volume to enhance the nitrification process. Enhanced levels of 

denitrification can be achieved in the denitrification filters. The objectives include: 

10-3



DRAFT 





The Denitrification Filters will be located downstream of the FSTs and upstream of disinfection 

at Red Hook. The filters will be constructed on newly filled footprint to the North of the existing 

plant site. The design condition of the denitrification filters is a flux rate of 4 gallons per square 

foot per minute on a max day condition. 


secondary effluent flows through the biomass-enriched media, denitrification will occur, as well 

as removals of particulate matter. The denitrification process will be supported by maintaining 

an anoxic state within the filters and by having a supplemental carbon addition point upstream of 

the filters. The biomass responsible for denitrification will utilize the supplemental carbon and 

any inherent carbon in the secondary effluent. 

Denitrification filters were designed for a maximum annual average flux rate of two gallons per 

minute per square foot and a max day flux rate of four gallons per minute per square foot. 

To maintain the efficiency of the denitrification filters, periodic backwashing must be performed 

to remove the accumulated solids from between the media particles. Backwash will be 

discharged to the head of primary settling tanks. Equipment will be provided that will flush the 

media by recycling the treated effluent to serve as washwater. A blower system will also be 

provided for air scouring of the media when the filter units are not operating in a denitrification 

mode. 

The Team assumes ten percent of the filters will be offline at any given time for backwash and 

O&M requirements. This translates to a design surface area of 12,566 square feet. The team 

assumes circular denitrification filters, with each filter providing 700 square feet of contact 

surface area. A total of 18 of these filters will be provided. Sand will be the medium of choice. 

The team assumes a grain size of 2 mm and a filter depth of 6 feet. 






be provided, each with a capacity of 3,500 scfm 



technology. 

10-4



DRAFT 






10-5



DRAFT 



A major source of head loss with the new MBR option will be the new 6 mm and 2 mm screens 

which will be installed as part of this alternative. To gain a portion of that head loss, it is 

proposed to demolish the existing PSTs and rebuild them at an elevation 6 feet higher than their 

current level, as was done on the Jamaica Bay LOT study. One PST will be taken offline at a 

time, demolished, and rebuilt. A series of temporary pumps shall be used to keep the flow 

balanced to online PSTs during the period when some PSTs have been reconstructed at their new 

height. All PST-related equipment (such as chain-and-flight mechanisms, primary sludge 

collector systems, etc) will also be rebuilt at the higher elevation. 


Membrane bioreactor technologies require more-advanced removal of influent solids than is 

typically achieved by conventional settling. Fine screens can be used to remove solids from 

process effluent that may cause clogging of the membranes reducing their treatment efficiency 

and increasing maintenance requirements. 

The design objectives of the fine screening process for Membrane Bioreactor Tanks include: 

• Remove particles larger than 2 mm from primary effluent for Membrane Bioreactor Tanks. 

• Collect screened solids and remove them from the plant. 

• Account for typical variations in wastewater flows. 


screens will be placed at the upstream end of the primary settling tanks. Each screen has a 

design capacity of 20 MGD and assumes discharge velocity of 1.65 feet per second under annual 

average conditions. The projected headloss for a screen of this size is three to six inches, 

depending on the overall flowrate to the plant. The Team assumes a channel depth of 12 feet and 

a width (per screen) of 9 feet. Through information supplied by the manufacturer, the 

anticipated solids removal rate is 13 cubic feet per screen per hour. This volume is used to 


O&M disposal costs for grit. A total of 12 primary screens will be installed, three for each of the 

four PSTs. The screens are of sufficient capacity that two per PST would be sufficient under a 

max flow condition, with one screen per tank offline for O&M. 


screens would be placed at the downstream end of the primary settling tanks. Each screen has a 

design capacity of 15 MGD and assumes discharge velocity of 0.87 feet per second under annual 

average conditions. The Team assumes a channel depth of 11 feet and a width (per screen) of 12 

feet. Through information supplied by the manufacturer, the anticipated solids removal rate is 15 

cubic feet per screen per hour. This volume is used to calculate the additional screenings 

processing infrastructure needed as well as the impact on the O&M disposal costs for grit. A 

total of 12 secondary screens will be installed, three for each of the four PSTs. The screens are 

11-1



DRAFT 

of sufficient capacity that two per PST would be sufficient under a max flow condition, with one 

screen per tank offline for O&M. 



Several of the existing influent sluice gates to aeration tank passes are broken and cannot be 

adjusted in the field. It is assumed that these gates will be fixed via a stabilization contract well 

before any HEP-related upgrade is constructed. 





below. 





The entire flow distribution of the aeration tanks will change. It is recommended that an 

additional gate is added to Pass A of existing aeration tanks to accommodate the addition flow. 

To implement the MBR process, Primary settled flow will first be sent through 2 mm secondary 

screens. Screened effluent will be combined with aeration tank effluent (internal recycle) and 

pass through new pre-anoxic tanks for partial denitrification. Flow will continue to a new wet 

well where it will meet the MBR RAS flow. The combined flow will be pumped by a new 

intermittent pump station to the head of the aeration tanks for subsequent nitrification. A portion 

of the aerated effluent will be returned by a gravity channel back to the pre anoxic tanks and the 

remainder will continue to the post anoxic tanks and then the membrane filtration facilities (both 

constructed within the existing final settling tank footprint). 

The existing aeration tanks will be modified to include a new influent and effluent channel, and a 

pre-anoxic zone. Each aeration tank will be modified such that all of the flow moves in the same 

direction. The existing common influent channel is not sufficient to handle the expected increase 

in flow the MBR process will create. Furthermore, the channel must be maintained and isolated 

so that primary effluent flow can be drawn and moved by gravity to the off-site treatment area. 

Therefore, the influent channel for the ATs must be expanded and built within the existing 

tankage. To achieve required capacity and allow for the incoming piping, a 20’ wide by 20’ tall 

influent channel must be constructed. The effluent end of the ATs will be modified to allow the 

aerated effluent to travel over weirs and into the effluent channel. The effluent channel must 

also be expanded to allow free flow over each weir segment. Demolition of the existing stepfeed 

influent channel is not recommended due to its structural use. 

11-2



DRAFT 





locations is seen in the drawings. 

Pass 

D 


Baffle 1 

(between successive Anoxic/Oxic zones) 



















Pass A 0 73,200 

Pass D 36,600 36,600 






11-3



DRAFT 




Pass A N/A 6 

Pass D N/A 3 




BNR designs. One difference is that with Pass A and the first half of Pass D being converted to 

totally anoxic zones, there will be no droplegs servicing those two areas. Passes B and C will 

have six droplegs, which will be evenly spaced along the pass length. The last half of Pass D 

will have three droplegs, evenly spaced along the remainder of the pass length. Another 

difference will be an increase in the pipe diameters of the air headers, as more air must be 


the consequential reduction in the oxygen transfer efficiency. As with the BNR designs, a detaillevel 

design is beyond the scope of this study. 












(scfm) 


Required (1) 






An evaluation was performed to determine the future air requirements for the Membrane 

Bioreactor design level based on the projected flows and loads from the Introduction and the 

projected mass balance for 2045 in Section 2.0. The calculated air requirements can then be 

11-4



DRAFT 

compared against the existing process aeration system to determine the necessary increase in 

aeration capacity that must be provided. Table 11-7 presents the calculated air requirements. 

Level of 

Treatment 


Current 



Condition 


(scfm) 

Additional 


Membrane Average 21,295 19,000 1 

Bioreactor Peak Hourly 36,202 19,000 2 




using the existing blowers. A new process air blower will be required as part of the MBR 

alternative. 

The two new blowers for the MBR alternative were chosen to be the same size as the existing 

process air blowers (9,500 scfm) to provide redundancy and flexibility. It is assumed that the 

additional process air blowers can be shoehorned into existing facilities and/or galleries, and an 

additional building or gallery to house the additional process air blowers will not be necessary. 



will be demolished sequentially and replaced with membrane bioreactor tanks. The required 

MBR tank volume (and associated requirements such as a scour air blowers) are greater than the 

existing footprint of the final settling tanks. Some land North of the facility will need to be filled 

to provide this additional footprint. 




objectives and parameters for MBR treatment. 

Objectives 


• Internal Recycle: Recycle nitrified effluent to the anoxic zones to facilitate denitrification 

Parameters 

• RAS concentration 8,000 – 10,000 mg/L 

11-5



DRAFT 

• RAS capacity: 3 times DDWF (180 mgd) 

• Internal Recycle concentration 8,000 – 10,000 mg/L 

• Internal Recycle capacity: 4 times DDWF (240 mgd) 


RAS facilities cannot be used to meet the RAS and internal recycling flow requirements. New 

facilities must be constructed to house additional RAS and recycle pumps. 


Flow will be directed to the expanded sludge pumping building. Ten 22.5 mgd RAS pumps will 

be needed to meet the design standard of 180 mgd, with two pumps offline. New suction and 

discharge piping for each pump must be installed. The installation of magnetic flow meters for 

accurate flow control is recommended. 

Internal recycle flow will be collected from the end of Pass C and be directed to the expanded 

sludge pumping building. Ten 30 mgd RAS pumps will be needed to meet the design standard 

of 240 mgd, with two pumps offline. New suction and discharge piping for each pump must be 

installed. The installation of magnetic flow meters for accurate flow control is recommended. 


No modifications to the Waste Activated Sludge System are needed for the Membrane 

Bioreactor level of technology, as per the Advanced Basic BNR Design in Section 6.7. 



A description of the Froth Control Hoods design needed for the Membrane Bioreactor level of 



A description of the RAS Chlorination design needed for the Membrane Bioreactor level of 




technology was provided in Section 6.8.3 for the Advanced Basic BNR treatment option. The 

only difference between the Advanced Basic BNR design and the MBR design is that the 

adjustable downward opening gates recommended for surface wasting will be located at the end 

of aerated Pass B instead of mounted on two new surface wasting pump sumps built at the end of 

each Pass A. 


11-6



DRAFT 




11.9.2 Carbon 


technology was provided in Section 7.9.2 for the Full Step BNR treatment option. However, 

based on a 5-day storage requirement under maximum loading conditions, the Team calculates a 

design storage volume of 12,380 gallons for the MBR alternative. Two 12,000 gallon 

underground storage tanks will be provided for the MBR alternative. 












The Membrane Bioreactor process is used to achieve low levels of nitrogen, solids and 


but will replace the secondary clarifiers with a membrane filtration process. Because this will be 

a filtration process that doesn’t depend on the capability of solids to settle, the membrane process 








11-7



DRAFT 

The Membrane Bioreactor (MBR) process will require new fine screening facilities, a new 

Intermittent Pump Station, modification of the existing aeration tanks, new Membrane 

Bioreactor facilities and other supporting equipment. The facilities will be constructed in the 

existing aeration tank volume. Modification of the aeration tanks, including addition of 

Membrane Bioreactors, will be discussed in this section. 

At the other three WPCPs included in this study, MBR tanks are included in footprint currently 

occupied by aeration tanks. However, BioWin modeling of the Red Hook WPCP under the MBR 

option demonstrated that existing aeration volume cannot be reduced if target SRT and MLSS 

concentrations are to be achieved. Therefore, at Red Hook MBRs are placed in the footprint 

currently occupied by final settling tanks. The Team looked into stacking MBR tanks on top of 

each other, however, this option was discarded due to structural concerns and issues with 

accessing the bottom tank for O&M and to clean and replace MBR cartridges. 

The MBRs will be located in the footprint previously occupied by the existing final settling 

tanks. Construction will be staged to ensure that aerator effluent is either passed through online 

FSTs or MBRs prior to disinfection and discharge. 

This conceptual design will be based on the Zenon MBR system, but other vendors should be 

considered during subsequent design phases. The MBR system consists of membrane units, 

permeate pumping system, membrane air scour system, membrane cleaning system and 

associated ancillary equipment and controls. Each membrane tank is 100 ft. long, 21 ft. wide, 

and 12 deep. A total of 12 MBR tanks will be provided. The membrane unit consists of a 

cassette, support frames and support beams. The Zenon process connects ZeeWeed membrane 

cassettes to the support frame. Permeate will be pulled from the top of each ZeeWeed cassette 

into a common permeate header. Connected to the header is a back pulse header that provides 

intermittent cleaning of the membranes. Permeate will be withdrawn by the permeate pump 

system provided by the vendor and discharged to either the back pulse storage tank or the 

disinfection tanks. Below each membrane cassette are air scour diffusers that draw air from an 

air header that extends along the top of the tank. The air supply originates at new process scour 

air blowers. 

The nominal pore size of the membrane modules is 0.04 microns. 340 square feet of contact 

surface area will be provided per module, and a total of 48 modules will be provided per cassette. 

Twenty cassettes will be provided per MBR tank. The target MLSS for entry to the MBR tank is 

8,000 mg/L, with an exit MLSS of 10,000 mg/L. Each MBR tank will be approximately 100 feet 

long and 21 feet wide. A total of 12 MBR tanks will be provided. This allows for annual 

average and maximum flux rates in line with the manufacturer’s recommendation with one MBR 

tank offline. A diagram showing the MBR set up is shown in Figure 11-1. The target MLSS for 

entry to the MBR tank is 8,500 mg/L. 

11-8



DRAFT 

Figure 11-1: MBR Setup 

Red Hook 

Aeration Tank 1, 

Western end 

(not to scale) 

Pass 

A 

Pass 

B 

Pass 

C 

Pass 

D 

MBR Module, 20 

modules per tank 

MBR Tank 1-A 

MBR Tank 1-B 

MBR Tank 1-C 

MBR Cassettes, 48 

cassettes per 

module 

MBRs were designed for an annual average flux rate of 10-12 gallons per square foot per day, a 

max week flux rate of 17 gallons per square foot per day, and an instantaneous peak of 28 

gallons per square foot per day. 

Three air scour blowers will be provided. The basis of design was providing an average of 1.4 

cfm of air per 100 square feet of contact surface area, as per the manufacturer’s recommendation. 

This translates to an anticipated air scour demand of 50,000 scfm. Six 12,000 scfm blowers will 

be provided. 






11-9



DRAFT 




Flow CBOD TSS 



TN 

(mg/L) 

Base Case 60 30 25 20.6 

Existing Conditions 31.0 8 8 15.5 




Full Step BNR 32.9 10 – 15 12 – 15 6 – 10 





A capital cost estimate for each level of technology was developed based on the conceptual 

designs presented in this document and the attached drawings. Table 12-2 provides a summary 

of anticipated capital construction costs for each level of technology at the Red Hook WPCP. 

The project executive summary provides details into the contingencies used, key cost 

assumptions, and overall approach to cost estimation. The detailed cost estimates for eight 

technologies at each of the four WPCPs in question can be found in their entirety after the four 

plant-specific conceptual design reports and drawing sets. 










Full Step BNR with Microfiltration/Ultrafiltration $704 

Full Step BNR with Denitrification Filtration $682 


12-1



DRAFT 

APPENDIX A 

Basis of Design Spreadsheets 

I

Red Hook WPCP 


Process Design Criteria for New Facilities: Solids Filtration 

Parameter Units Minimum Week Minimum Month Annual Average Maximum Month Maximum Week Maximum Day Peak Hour 


influent flow (mgd) 26.5 27.4 32.9 40.1 49.4 65.8 90.0 


TSS concentrations (mg/l) 179 190 199 202 204 178 146 

TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 


CBOD concentrations (mg/l) 126 141 142 149 145 126 104 

CBOD load (lb/day) 28,000 32,300 38,932 49,800 59,600 69,300 77,863 


TKN concentrations (mg/l) 28.4 31.5 31.7 33.1 32.3 28.2 23.2 

TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 


SOLIDS FILTERS 







Grain Size (mm) 2 2 2 2 2 2 2 



Percent of filters being backwashed (%) 20% 20% 20% 


20% 20% 20% 20% 






Quantity (#) 3 3 3 3 3 3 3 

Capacity (GPM) 3800 3800 3800 3800 3800 3800 3800 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 50 50 50 50 50 50 50 


SCOUR AIR BLOWER FOR DENITRIFICATION FILTERS 

Quantity (#) 3 3 3 3 3 3 3 

Unit Capacity CFM 3,150 3,150 3,150 3,150 3,150 3,150 3,150

Red Hook WPCP 


Process Design Criteria for New Facilities: Microfiltration/Ultrafiltration 






TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 


PRIMARY SCREEN DESIGN CRITERIA (before MFs) 

Size mm 6 6 6 6 6 6 6 


Screen Design Capacity MGD 20 20 20 20 20 20 20 


















Microfiltration tank length (ft) 100 100 100 100 100 100 100 

Microfiltration tank width (ft) 21 21 21 21 21 21 21 

Contact Surface Area per Microfiltration tank (ft2) 326,400 326,400 326,400 326,400 326,400 326,400 326,400 

Number of Microfiltration Tanks in Operation (#) 10 10 10 10 10 10 10 


Design Number of microfiltration Tanks (N+1) (#) 11 11 11 11 11 11 11 

Microfiltration Tank Footprint (ft2) 2,100 2,100 2,100 2,100 2,100 2,100 2,100 

Total footprint occupied by Microfiltration (ft2) 23,100 23,100 23,100 23,100 23,100 23,100 23,100 

MEMBRANE AIR 

Microfilter Air Requirement (Method 1) cfm/100 sf Surface Area 1.4 1.4 1.4 1.4 1.4 1.4 1.4 





Scourge Air Blowers # 3 3 3 3 3 3 3

Red Hook WPCP 


Process Design Criteria for New Facilities: Advanced Basic BNR 






TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 





Tank Length (ft) 260 260 260 260 260 260 260 

Pass Width (ft) 12.5 12.5 12.5 12.5 12.5 12.5 12.5 

Tank Depth (ft) 22.5 22.5 22.5 22.5 22.5 22.5 22.5 



AERATION BASIN MODIFICATION: SUBMERSIBLE MIXERS 






Electrical Service - 460 V, 60 Hz, 3 phase 461 V, 60 Hz, 3 phase 462 V, 60 Hz, 3 phase 463 V, 60 Hz, 3 phase 464 V, 60 Hz, 3 phase 465 V, 60 Hz, 3 phase 466 V, 60 Hz, 3 phase 












Total Nozzles (#) 688 688 688 688 688 688 688 





Number of Existing Process Air Blowers (#) 4 4 4 

Current infrastructure sufficient 

4 4 4 4 


Total Capacity (Assuming 1 Blower Offline for O&M) (SCFM) 28,500 28,500 28,500 28,500 28,500 28,500 28,500 

BioWin Predicted Demand (SCFM) 15,570 26,469 

Assumed Blower Size (SCFM) 9,500 9,500 9,500 9,500 9,500 9,500 9,500 

Number of blowers needed (#) 

1 


Number of RAS Pumps (#) 4 4 4 4 4 4 4 

Capacity of an individual pump (MGD) 12.1 12.1 12.1 12.1 12.1 12.1 12.1 

Capacity of system (Assuming 1 pump offline for O&M) (MGD) 36.3 36.3 36.3 36.3 36.3 36.3 36.3 


Design Condition (MGD) 13.3 13.7 16.5 


20.1 24.7 32.9 45.0 

Addititional Capacity Required (MGD) 0.0 0.0 0.0 0.0 0.0 0.0 8.7 

Number of Additional RAS Pumps Needed (#) 1 1 1 1 1 1 1 




Total Capacity (Assuming 1 pump offline for O&M) (MGD) 6.8 6.8 6.8 6.8 6.8 6.8 6.8 


FROTH HOODS 

Number of Froth Hoods per Aeration Tank (#) 4 4 4 


4 4 4 4 



Emergency Dose Equivalent (mg/L) 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0 4.0-8.0




Required Mass of Sodium Hypochlorite (lb/d) 928 959 1,151 1,404 1,726 2,301 3,147 









Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 




Given small volume of centrate (0.1 - 0.15 MGD), we assume Pass A addition rather than a dedicated SCT 




Assumed Sodium Hydroxide Concentration (%) 25 25 25 


25 25 25 25 










Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



No supplimental carbon in ABBNR 



Tank Length (FT) 250 250 250 250 250 250 250 

Tank Width (FT) 50 50 50 50 50 50 50 

Tank Depth (FT) 14 14 14 14 14 14 14 

Total Volume (CF) 1,400,000 1,400,000 1,400,000 1,400,000 1,400,000 1,400,000 1,400,000 


Surface Overflow Rate (GAL/SF/D) 265 274 329 401 494 658 900 


No Upgrades to FSTs planned in ABBNR 























New colorimetric (HACH CL 17) Residual Chlorine Analyzers for influent and effluent chlorination dosing control. Flow paced residual chlorine dosage control with residual chlorine trim. 

New local controls for thickener rake mechanism drive.

Red Hook WPCP 


Process Design Criteria for New Facilities: Full Step BNR 






TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 





Tank Length (ft) 260 260 260 260 260 260 260 

Pass Width (ft) 12.5 12.5 12.5 12.5 12.5 12.5 12.5 

Tank Depth (ft) 22.5 22.5 22.5 22.5 22.5 22.5 22.5 





















Total Nozzles (#) 688 688 688 688 688 688 688 









BioWin predicted Air Demand 17,645 29,997 

Needed Number of Blowers (#, N+1+1) 6 

Additional Blowers to Install 2 2 2 2 2 2 2 







Design Condition (MGD) 26.5 27.4 32.9 40.1 49.4 65.8 90.0 









FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 



Gallons concentrated methanol needed to denitrify (gal/d) 672 775 934 934 1,429 1,663 1,868 










Tank Length (FT) 250 250 250 250 250 250 250 

Tank Width (FT) 50 50 50 50 50 50 50 

Tank Depth (FT) 14 14 14 14 14 14 14 









New magnetic flow meter on 8” sludge pump discharge header, timer-based local control stations for new collector drive mechanism, local timer-based controls for scum skimming, 


local controls for sludge pumps, local controls for sludge degritting equipment and storage, local controls for secondary screens. 

New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header valve to 


each tank shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 






transmitter. 



Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with high 


and low level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to chlorine contact tanks, wireless 

radio system to transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control panel. 



trim. 





control panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This system will use a combination 

of local control panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for data collection and process control. The 

plant telephone system will be a plant wide PC based PBX system, including fiber distributed architecture for modular expansion between buildings, and digital communications 

and networking for voice and data, and wireless phones for designated personnel. The plant two-way radio system will extend communication coverage to all plant areas, including 

tunnels and dead spots locations. The base station will be installed in the Main Control Building.


Red Hook WPCP 


Process Design Criteria for New Facilities: FSBNR + Solids Filtration 





TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 





Tank Length (ft) 260 260 260 260 260 260 260 

Pass Width (ft) 12.5 12.5 12.5 12.5 12.5 12.5 12.5 

Tank Depth (ft) 22.5 22.5 22.5 22.5 22.5 22.5 22.5 





















Total Nozzles (#) 688 688 688 688 688 688 688 



























FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 













Tank Length (FT) 250 250 250 250 250 250 250 

Tank Width (FT) 50 50 50 50 50 50 50 

Tank Depth (FT) 14 14 14 14 14 14 14 









New magnetic flow meter on 8” sludge pump discharge header, timer-based local control stations for new collector drive mechanism, local timer-based controls for 


scum skimming, local controls for sludge pumps, local controls for sludge degritting equipment and storage, local controls for secondary screens. 

New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air 


Header valve to each tank shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 

Ultrasonic level measurement and alarm reporting to the Main Control room, new magnetic flow meter for Aeration Tanks waste discharge to thickeners, local controls 


for surface waste pumps, WAS pumps, RAS pumps. 

New blower control panels in control room. Interface with local blower speed control resistor panels provided by blower vendor. Blower discharge main air header 


pressure transmitter. 



Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level 


gauge with high and low level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to 

chlorine contact tanks, wireless radio system to transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control 

New colorimetric (HACH CL 17) Residual Chlorine Analyzers for influent and effluent chlorination dosing control. Flow paced residual chlorine dosage control with 


residual chlorine trim. 



Integrated state-of-the art Distributed Control System (DCS) with Area Control Stations (ACS) located throughout the Plant with industrial PC Operator Interface, 

including local control panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This 

system will use a combination of local control panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for 


data collection and process control. The plant telephone system will be a plant wide PC based PBX system, including fiber distributed architecture for modular 

expansion between buildings, and digital communications and networking for voice and data, and wireless phones for designated personnel. The plant two-way radio 

system will extend communication coverage to all plant areas, including tunnels and dead spots locations. The base station will be installed in the Main Control 

Building. 

SOLIDS FILTERS 







Grain Size (mm) 2 2 2 2 2 2 2 










Quantity (#) 3 3 3 3 3 3 3 

Capacity (GPM) 3800 3800 3800 3800 3800 3800 3800 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 50 50 50 50 50 50 50 



Quantity (#) 3 3 3 3 3 3 3 



Red Hook WPCP 


Process Design Criteria for New Facilities: FSBNR with Microfiltration/Ultrafiltration 





TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 





Tank Length (ft) 260 260 260 260 260 260 260 

Pass Width (ft) 12.5 12.5 12.5 12.5 12.5 12.5 12.5 

Tank Depth (ft) 22.5 22.5 22.5 22.5 22.5 22.5 22.5 





















Total Nozzles (#) 688 688 688 688 688 688 688 



























FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 













Tank Length (FT) 250 250 250 250 250 250 250 

Tank Width (FT) 50 50 50 50 50 50 50 

Tank Depth (FT) 14 14 14 14 14 14 14 












New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header valve 


Ultrasonic level measurement and alarm reporting to the Main Control room, new magnetic flow meter for Aeration Tanks waste discharge to thickeners, local controls for 






Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with 







PRIMARY SCREEN DESIGN CRITERIA (before MFs) 

Size mm 6 6 6 6 6 6 6 




















Microfiltration tank length (ft) 100 100 100 100 100 100 100 

Microfiltration tank width (ft) 21 21 21 21 21 21 21 

Contact Surface Area per Microfiltration tank (ft2) 326,400 326,400 326,400 326,400 326,400 326,400 326,400 

Number of Microfiltration Tanks in Operation (#) 10 10 10 10 10 10 10 


Design Number of microfiltration Tanks (N+1) (#) 11 11 11 11 11 11 11 

Microfiltration Tank Footprint (ft2) 2,100 2,100 2,100 2,100 2,100 2,100 2,100 

Total footprint occupied by Microfiltration (ft2) 23,100 23,100 23,100 23,100 23,100 23,100 23,100 

MEMBRANE AIR 


Required Air Scour Demand (Method 1) cfm 50,266 50,266 50,266 50,266 50,266 50,266 50,266 

Membrane Air Requirement (Method 2) cfm/module 230 230 230 230 230 230 230 




Total Blower Capacity (1 Unit OOS) cfm 60,000 60,000 60,000 60,000 60,000 60,000 60,000


Red Hook WPCP 


Process Design Criteria for New Facilities: FSBNR with Denitrification Filtration 





TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 





Tank Length (ft) 260 260 260 260 260 260 260 

Pass Width (ft) 12.5 12.5 12.5 12.5 12.5 12.5 12.5 

Tank Depth (ft) 22.5 22.5 22.5 22.5 22.5 22.5 22.5 





















Total Nozzles (#) 688 688 688 688 688 688 688 



























FROTH HOODS 

















Flow (GPM) 189 189 189 189 189 189 189 



Motor Size (HP) 1 1 1 1 1 1 1 



















Quantity (#) 4 4 4 4 4 4 4 

Flow (GPM) 833 833 833 833 833 833 833 



Motor Size (HP) 1 1 1 1 1 1 1 




Quantity (#) 2 2 2 2 2 2 2 

Capacity (GPM) 150 150 150 150 150 150 150 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 3 3 3 3 3 3 3 



Carbon Source 

Methanol 













Tank Length (FT) 250 250 250 250 250 250 250 

Tank Width (FT) 50 50 50 50 50 50 50 

Tank Depth (FT) 14 14 14 14 14 14 14 











skimming, local controls for sludge pumps, local controls for sludge degritting equipment and storage, local controls for secondary screens. 

New non-membrane type DO probe/analyzers. One probe per pass will be installed in Passes B and C of Aeration Tanks. Automatic adjustments to the Main Air Header 


valve to each tank shall be implemented. new magnetic flow meters for 30” RAS flow to Pass A of each Aeration Tank 

Ultrasonic level measurement and alarm reporting to the Main Control room, new magnetic flow meter for Aeration Tanks waste discharge to thickeners, local controls for 


surface waste pumps, WAS pumps, RAS pumps. 



transmitter. 



Local control panel for automatic and manual control for hypochlorite storage and delivery systems, including storage tank ultrasonic transmitter and backup level gauge with 


high and low level alarms, chemical metering pump local controls, storage tank truck fill alarm station, magnetic flow meter for hypochlorite feed line to chlorine contact 

tanks, wireless radio system to transmit flow data of existing venturi from raw sewage pump discharge line to sodium hypochlorite system local control panel. 



chlorine trim. 




Integrated state-of-the art Distributed Control System (DCS) with Area Control Stations (ACS) located throughout the Plant with industrial PC Operator Interface, including 

local control panels equipped with programmable logic controllers (PLCs) and a Windows based Human Machine Interface (HMI) software package. This system will use a 

combination of local control panels for vendor packaged equipment, local control stations for manual control, and Distributed Control Units (DCU) for data collection and 

process control. The plant telephone system will be a plant wide PC based PBX system, including fiber distributed architecture for modular expansion between buildings, 

and digital communications and networking for voice and data, and wireless phones for designated personnel. The plant two-way radio system will extend communication 

coverage to all plant areas, including tunnels and dead spots locations. The base station will be installed in the Main Control Building. 


Filtration Rate (GPM/SF) 1.6 1.7 2 2.4 3.0 4.0 5.5 






Grain Size (mm) 2 2 2 2 2 2 2 










Quantity (#) 3 3 3 3 3 3 3 

Capacity (GPM) 4200 4200 4200 4200 4200 4200 4200 

TDH (FT) 35 35 35 35 35 35 35 

Motor Size (HP) 50 50 50 50 50 50 50 



Quantity (#) 3 3 3 3 3 3 3 


Red Hook WPCP 


Process Design Criteria for New Facilities: MBR 





TSS concentrations 

(mg/l) 

179 190 199 202 204 178 146 

TSS load (lb/day) 39,600 43,500 55,000 67,700 84,200 97,900 110,000 






TKN load (lb/day) 6,300 7,200 8,700 11,100 13,300 15,500 17,400 


NEW MAIN SEWAGE PUMPS 


New main sewage pumps will be installed in existing MSP pump stations; capacity will be increased to account for additional headloss 

PRIMARY SCREEN DESIGN CRITERIA (before PSTs) 

Size mm 6 6 6 6 6 6 6 














PRIMARY SETTLING TANKS 


Existing primary settling tanks will be demolished and rebuilt 6 feet higher to account for increased headloss 

SECONDARY SCREEN DESIGN CRITERIA (after PSTs) 

Size mm 1 1 1 1 1 1 1 


Screen Design Capacity MGD 15 MGD 15 MGD 15 MGD 15 MGD 15 MGD 15 MGD 15 MGD 


Projected Headloss inches 1 1 1 1 1 1 1 





Calculated Number of Units # 1.8 1.8 2.2 2.7 3.3 4.4 6.0 




Total Number of Secondary Screens # 12 12 12 12 12 12 12 

EXISTING AERATION TANK DIMENSIONS 

Number of Aeration Tanks # 4 4 4 4 4 4 4 

Average Aeration Tank Length ft 260 260 260 260 260 260 260 

Average Aeration Tank Width ft 50 50 50 50 50 50 50 

Total Aeration Tank Surface Area ft2 52,000 52,000 52,000 52,000 52,000 52,000 52,000 


Keep all four aeration tanks as is, put the MBRs where the FSTs currently reside 

MBR TANK DESIGN CRITERIA 

Nominal Pore Size (microns) 0.04 0.04 0.04 0.04 0.04 0.04 0.04 

Membrane Surface Area per Zenon MBR Cassette (ft2) 340 340 340 340 340 340 340 

Zenon 500D Cassettes per Module (#) 48 48 48 48 48 48 48 

Contact Surface Area per Zenon MBR Cassette (ft2) 16,320 16,320 16,320 16,320 16,320 16,320 16,320 

Modules Per MBR Tank # 20 20 20 20 20 20 20 

Length of MBR Unit ft 100 100 100 100 100 100 100 

Width of MBR unit ft 21 21 21 21 21 21 21 

Total Number of MBR Tanks (By Plant) # 12 12 12 12 12 12 12 

Number of MBR Tanks Per Aeration Tank # 3 3 3 3 3 3 3 

Total Number of Modules # 240 240 240 240 240 240 240 

Calculated Flux (Assuming One Tank Offline) gallons/square feet/day 7 8 9 11.2 14 18 25 

Design Criteria (Maximums) gallons/square feet/day 10-12 17 28 

MBR Tank Footprint square feet 25,200 25,200 25,200 25,200 25,200 25,200 25,200 

PROCESS AIR 

Required Blower Demand cfm 21,295 36,202 

Existing Capacity CFM 38,000 

Assumed Blower Size cfm 9,500 

Design Number of Blowers #, N+1+1 6 

Additional Number of blowers needed 2 2 2 2 2 2 2 

MEMBRANE AIR 



Membrane Air Requirement (Method 2) cfm/module 230 230 230 230 230 230 230 




Total Blower Capacity (1 Unit OOS) cfm 60,000 60,000 60,000 60,000 60,000 60,000 60,000 

RECYCLE PUMP CRITERIA 

Design Standard 4Q 4Q 4Q 4Q 4Q 4Q 4Q 

Necessary Recycle Pump Flow Rate MGD 106 110 132 161 197 263 360 

Necessary Recycle Pump Flow Rate gpm 73,720 76,157 91,389 111,494 137,083 182,778 250,000 

METHANOL STORAGE FACILITY DESIGN CRITERIA 

Methanol, Sodium Hydroxide sections Need to be updated post-BioWin 

Demand Methanol Consumption gal/day 891 1,028 1,238 1,585 1,894 2,204 2,476 


Design Capacity, Methanol Storage Tank gallons 12,000 12,000 12,000 12,000 12,000 12,000 12,000 



SODIUM HYDROXIDE STORAGE FACILITY DESIGN CRITERIA 

Alkalinity Demand mg/L 44 44 44 44 44 44 44 

Daily Consumption of Alkalinity moles 91,000 94000 112000 137000 169000 225000 225000 

Mass of 50% Sodium Hydroxide needed to meet demand kg 5,600 5,700 6,000 7,500 10,000 13,100 13,100 

Gallons of 50% Hypo Needed Per Day gallons 1,500 1,500 1,600 2,000 2,600 3,500 3,500 


Design Capacity, Alum Storage Tank gallons 8,000 8,000 8,000 8,000 8,000 8,000 8,000 



EXISTING FST DIMENSIONS 

Number of Tanks # 4 4 4 4 4 4 4 

Average Tank Length ft 250 250 250 250 250 250 250 

Average Tank Width ft 57 57 57 57 57 57 57 

Total FST Surface Area ft2 57,182 57,182 57,182 57,182 57,182 57,182 57,182 

FST Design Condition 

Demolish all Final Settling Tanks to Create Footprint for MBRs

~ ~~ 

i 

~ 

~ 

~ 

;; 

~ 

l 

~ 

l 

j~ 

~ 

! 

Ii 

l ". 

;; 

HAEN AN SAWY 

Environment EngIne & Sc 

CITY OF NEW YORK 

DEPARTMENT OF ENVIRONMENTAL PROTECTION 

BUREAU OF ENGINEERING, DESIGN, AND CONSTRUCTION 

RED HOOK WPCP 

CONCEPTUAL DESIGN 

ADVANCED TREATMENT TECHNOLOGIES 

MAY 2007 

~7-~

§ 

~ 

g 

~ 

5 

ß 

S 

~ 

~ 

~ 

l 

!~ 

~ 

~ 

g i: 

§ ~" 

~ 

l " 

~ 

~ 

DRAWING INDEX 

DRAWlNG NO. 

GENERAL 

SHEET 

DRAWlNG TiTlE 

NO. 

DRAWlNG NO 

SHEET 

NO. 

DRAWlNG TiTlE 

FULL STEP BNR WI DENITRIFICATION FILTERS 

RHGGOOO - COVER SHEET 

RHGG010 1 DRAIING INÓEX 

RHGC010 2 LOCATION ?tN 

RHGC020 3 EXSTING PLA 

ADVANCED BASIC BNR 

RHABBOlO 4 flOW DIAGRAM - MAS BALACE 

RHABB020 5 EXSTING SITE PLA - UMITS OF COSlRUCTIDN 

RHABB070 6 AEATION TANKS - TOP PLA - WEST HAL 

RHABB08D 7 AEATION TANKS - TOP PLA - EAT HAlf 

RHFSD34 26 flOW DIAGRAM - MAS BALACE 

RHFSOJ50 27 CIi"L - EXISTING SITE PLAN - UMITS OF CONSlRUCTION 

RHFS360 28 CML - PROPOSE SITE PLA 

RHFSD361 29 MECHANICAl - AEATION TANKS - TOP PLAN - WEST HAL 

RHFS362 30 MECHANICAl - AEATION TANKS - TOP PLA - EAST HAlF 

RHFSD370 31 ARCHITECruRAl - GROUNO flOOR 

RHFS0360 32 MECHANICAl - GROUND flOO 

RHFS390 33 MECHANICAl - SECTION - SHEE 1 

RHFSD40D 34 MECHANICAL - GROUND flOO - DETAIL PLA 

RHFSD410 35 MECHANICAL - SECOD flOO - DETAIL PLAN 

RHFSD42D 36 MECHANICAl - SECTION 

FULL STEP BNR 

RHFS09D 8 flOW DIAGRAM - MASS BALACE 

RHFSB10D 9 EXSTING SITE PLAN - UMITS OF COSlRUCTION 

RHFSB120 10 AERATION TANKS - TOP PLA - W£ST HAL 

RHFSB130 11 AEATION TANKS - TOP PLA - EAST HAlf 

RHFSB140 12 ARCHITECruRAl - GROUND flOO 

RHFSB15D 13 MECHANICAl - GROUND flOO 

RHFSB160 14 MECHANICAl - SECTION - SHEET 1 

FULL STEP BNR Wi SOLIDS FILTRATION 

RHFSS210 15 FUll STE BNR '" SOUDS F1L TERS - flOW DIAGRAM - MASS BALNCE 

RHFSS220 16 EXSTING SITE PLAN - UMITS OF COSTUCTION 

RHFSS230 17 PROPOSE SITE PLA 

RHFSS240 18 AERATION TANKS - TOP PLA - W£ST HAL 

RHFSS250 19 AERATION TANKS - TOP PLA - EAST HAlf 

RHFSS260 20 ARCHITECruRAl - GROUND flOOR 

RHFSS270 21 MECHANICAl - GROUND flOO 

RHFSS280 22 MECHANICAl - SECTION - SHEET 1 

RHFSS290 23 MECHANICAl - GROUND flOO - DETAIL PLA 

RHFSSJO 24 MECHANICAl - SECOND flOO - DETAIL PLAN 

RHFSS310 25 MECHANICAL - SECTION 

FULL STEP BNR WI MICROFILTRATION 

RHFSM450 37 NEW - flOW DIAGRAM - MASS BALNCE 

RHFSM4ôD 38 CIi"L - EXISTING SITE ?tN - UMITS OF CONSlRUCTION 

RHFSM470 39 CIi"L - PROPOSE SITE PLAN 

RHFSM48 40 MECHANICAl - AEATION TANKS - TOP PLA - WEST HAL 

RHFSM490 41 MECHANICAl - AERATION TANKS - TOP PLAN - EAST HAL 

RHFSMSO 42 ARCHITECruRAl - GROUND flOOR 

RHFSM51D 43 MECHANICAl - GROUND flOO 

RHFSM52D 44 MECHANICAl - SECTION - SHEET 1 

RHFSM530 45 MECHANICAl - GROUND flOO - DETAIL PLA 

RHFSM54 4ô MECHANICAL - SECOND flOO - DETAIL PLAN 

RHFSM550 47 MECHANICAl - SECTION 

MBR 

RHMBR540 48 MEMBRANE BIOREACTORS - flOW DIAGRAM - t.ASS BALNCE 

RHMBR550 49 CIi"L - EXISTING SITE PLAN - UMITS OF CONSlRUCTION 

RHMBR580 50 CIviL - PROPOSE SHE PLJ 

RHMBR570 51 ARCHITECruRAL - GROUND flOOR 

RHMBR580 52 MECHANICAl - GROUND flOO 

RHMBR590 53 MECHANICAl - SECTION - SHEET 1 

RHMBR600 54 MECHANICAL - GROUND flOO - DETAIL PLAN 

RHMBR610 55 MECHANICAl - SECONO flOO - OET AIL PLAN 

RHMBR620 58 MECHANCAl - SECTION 

.. 

IT tS A \QTl (S S£ 72.2 a: n£ f£ YO STATE 

EDll LAW F' AN P£. UIl ACNG UIC lM 

DI a: A LI PR ENNE, 10 ALTE .. 

Nf WAY Pl, SPTl PlTS Of RETS TO 'I 

1l S£ Of A ~AL Et HA BE N' If ~ 

Il 8EHG THE .5 Of A PR EN IS ALTE, 

TH ALTE EN Sl AfX 10 1l nn l- .5 lR 

TH NOTAlO 'AlTE BY Fa BY tI Sll1 TH 

DATE NO A SP DE Cf TH ALlET1 

DEGNED NB 

ORA~ 

NO. DATE ISSUED FOR BY PROJENGR, 

EG 

SCALE 

APOVE FOR THE CIT OF NEW YORK #crrD~~ CIT OF NE YOR 

HAEN AN SAWY ~'- :t.y.l 

DEPARTMENT OF ENVIRONMENTAl PROTECTION 

P.E. 

BUREU OF ENGINEEING, DESIG, AND COlRucN 

~ DI:P a. 

RED HOOK WPCP 

HA AND SAWYR, P.C. P,E. ~ 

498 CONCEPTUAL DESIGN 

SENl AVE . NEW YORK NEW YORK 10018 CHIEF, DISION OF FACIlES DESIGN- o""8/TAL",D~ 


CHECKE NB 

En Enrs & Scri PRECT MAGER 

AS NOTED 

SECT.HIE ~ 

\.~" 

POS P.E. 

DATE MAY 2007 

DRAWING INDEX 

SHEET-l OF~ 

DWG. NO. 

RHGG010

.... i-""":'!1mt~U€Y4f~l17~~~~~" ::s§~~mi "~'-~ AŠJ 

~t / ~r§l'" ~~~~ ~~~~ ~ ~~O~'~)a\)§\~~rnUU .~--.--.~ -l~1 

. ': ~~ . ~f $4p~I-'~"'tt~g;~~ .,i ~~~~Q ~"'~~¡-- 

! ~l "Ol2'0tJ r~~ fl¡ A~\\\0~ 0~ ~ L~# \l.Ì".----~ 

: ~ Ii wJi~,,~w;fØ ~ r ¡~~~ :o1'aIiUOÒl~ ---)~~() If . '"~ ~~..,~\\\)GO\\rD~1¡f r ~ ~ ~",vf/,')~ Ii t'~ -~~:. Wl ::),\ '~ , ,,_ 

1 

¡, 

l 

~ß5~ 

~ 

~ o 

~ 

- 

S EIll LAW Fa ~ PE, UN AC Ul 11 

:5 DlRE a A UC PR Dl, TO ALTE ~ 

õ Nf WAY Pl. SPTI F'TS OR R£ TO lH 

~ 11 SE OF A PRAl EN HA BE AP. F AN 

i 

~ 

l 

š 

~ lIT ts A w:lJ a SE 72.2 Cf TH NE YO STATE 

g ~~~~~~:i~:::O' 

g TH HOT..ii~ . AlTE BY FW BY tI SlQlTI l1 

¡; DATE NC A SP 0£ CF TH AlTETI 

~ ". 

'"c: 

K 0; 

N 

. I '~ ~~~~fJoÆOjoo11(Jodlj¡~Ø ~ ,,M.~~~~'!=8~ ~ i 

"~... ....... . ~~I~(~~/'~!ß¿r() ~ ".. tj &%~'l ~ 't~~ (If)!'i!Ø ~ VBf-diJ~¡¿o.oO~07l~'f '. "., ~ 1/ ~ ~~ ~.. .~ ,~~~~. . ~~~~~~~- "'~s . ClOD ~ ~~6d :-~Bc:o' .' ~ k~ :3~\ :.'~, 

I ,~~, j~§&ft~ ~;: §888B~~ ~ ~ '~ 

. ~J ~ ~;,q ~~ ~ I "'(~~~f- U U U ~ r- ~Q R£;çs ,-. ~ ~C"ll,. OClOCJD~-- ooooo?" 4~\ b.\~~ \" 

' ~.. ffJu, RED 

' . PLANT SITE- 

HOOK 

L' '\i 

;~' 

~y 

I' ~ 

'r 

~=§OOOO 

~ OOClOgrr ~ 

~a 

~ I "I 0 ~ ~ ",,-IU' ~ , 'I-) ~'i ,c 80 

'UTFAl1'f '. '- c:OOClc:MJ;= ~\-.d .~~ 

il ,'U e.i , ~ - -~ 1 ~~~Ú?~ ~OO~O~~~ ~~ y~~ 

~ ,~. ~ I ~I . ~ . IV' 'lL "" ~.l\ '- ,1-\ ~ Ii ii' . fJ "A~-: ,~88N . i c IIIOO.LVN ~ ~ ~~~~' '~~~0 i,,~ _CJ-\~ ~ ~I;: ¡: §;h,!~~w '(, ~~' ~ 

~' ~, \ ' l'~',\ _I. ~' ~ . I) IJI/~ "-- NAVVYARD ~~ ~X~ .6,"; ,:yij ~~ ;- ,~~~ 

C) /, \ ,.~' . ~ 'C: ~. ~~ 

~,' : ,\ a" ji~!¡)/i -;fl$ßA QIO~fl - a~~.illLUII' =-!! i l lìnlìnmi T~n Dr~DD E: v'" q~~~ 

~ ~ \ ~ 00 I&~ Ti §&: fdb.~:: .., ' ii, ~DOuuuuw t:c=8~ ~D: 

~~ 

~ 

Gonoo 

I_~ 

~lr§~~&~~ Q'" nnnu Pr~~~=§8a§aõE ~ 

c..."\,~ 

~ .~~ 

~ r. ~~LS~~ 

&~~~~~ 

DBQ 

il DDDD 

\(00 lìnnm~ir:'b~ri~ 

~Br- ~~§S§§§ 

5 B8ã B§Ea~ 

~ 

"'~~~""I~,(~~PUNRlATI&-~ . j UUULnJ\Jd~t:~c: BBc: Bc:Bc: 

'~POItC.IlIN "-" ~ ' ~~ . ~ s ~~ ì li: ~ ¡. Edc: ~~c: c:c:EdL.l- 

, 

t~' 

~~~ 

~. 

~~ 'J,:II.~')") 

~~~~ ~':è'~i?S6~ 

:: ~ .~ ~ ~ ¡; p--: 

-"~~~ 

c: --BE:EdBl 

~~ VANBRUNT PUNt STATIÓI í ~~ "Yci ~ ~"""' '/) ~ 1f. ~ ~~ ~~~~~ h~.. ~ . ~ ¡- ~ r:¡: ~ --:L. W~~ Ç:Ç5Ç:ç:ç: _ -- ir II ,r: rgJfff 

~y"(J~~ i¡ 'JA~l~~~ "-(:.~~"" 0 ¿~i.~ ~t,"" dt:Ç5§Ç:~~ 

'¿~?§fi'~'!. .. l~ "" ~/.-l.,~.."-( ~ ~..~;:~ e ~~ ~ l; .. '-8 ,dï Ç5G:~c:§l 

~ir~ l\ ~/¡) G/ i Ii ?§~ ~ .~~~~~~'= BROKLVN ~ ~a8if~=a~Qå§8§§8É 

ê!/= 8 ~ ~f5Q5C5C588DC5D 

i \i'~/!/ /~ 0t ~~~~$~ ¡~,R?sÆaË~~~~88¥1§m 

~:",~~~~~ng) \ \D~J ~ ~~iaRS§~' a~~i 

......, "',,~~~~ ~.~.~.#I~ 1ROS:'::jr~:i~=~ ~~tI8,~~c . ~"D. 

, l-:'-~:-"'~'P~ ') 'i ~~ ~~~~~~~.~~ ~~ \'c:~c: _. c=B~ ~~ ~ .~ ~~ '~ ~ ~~~ ,,,~~~~ "~~,, t\\J~~~ 

,'\ ~,""~)( J 4 ~) ~~.. ~c:i==c=c=CJc=c:c= ~~ .., .~ ~t'(\. ~~ 

~~~.~\t~J "'~~~, "',) # A~ // /;1( o~vy~la~", ~ ~"" ~ P, AR .".\ K 1'S.c- _ oc:CJc=i=i: ~_ Ll i§=qpnriLrrll.fk~~~~ 

~ .~ ~'~;~~ ~ ~ t 

DESIGNED -- 

DRA~ -- 

CHECK ~ 

SECT.CHIEF ~ 

BY I PROJ,ENGR, ~ 

SCALE 

AS NOTED 

HAEN AN SAWY 

APPROVE FO THE CI OF NEW YORK 

En~ronmeta Eneers & Scti PROJEC MAER 

HAZEN AND SAWYR. P,C, 

P.E 

~ P,E, I 498 o I NO, DATE ISSED FOR 

SEVNT AVE . NEW YORK. NEW YORK 10018 CHIEF. DIVSION OF FAClLmES DESIGN- 

P~E~ 

CIT Of NEW YOR 


BUREU OF ENGINEERING, DESIGN, AN CONSmUC 

RED HOOK WPCP 



oc". 

....L. 

I. . ."LCS 

.,iinr... 

... 

PLANT LOCATION 

LEGEND 

__ RED HOOK SERVICE AREA 

. PUMPING~~STATION 

-- FORCE MAIN 

PROPOED 

t 

OR UN 

1 

_ _ _ INTERCEPTOR ~ CONSTRTIN , 

SCALE 

100 - 0 100 ZLX Sl PT 

SITE WORK 

GENERAL 

LOCATION PLAN 

:, l' 

.~ 

, ~ 

DATE MAY 2007 

SHEET-- OF~ 

DWG, NO, RHGC010

I 

i 

, 

\ 

\ 

\ 

~ 

¡; 

l 

~sC¡¡ 

~ 

~ o 

~ 

1; 

8 

l 

~ 

~ 

5 

l 

¡ 

:i ".i 

¡¡ 

ä. 

:; 

" 

~ 

~:3 

NO. DATE ISSUED FOR 

z. 

.. 

IT IS A VKT1 N' SE 722 a: TH NE YO STAlE 

EIT1 LAW FO Nf PE, IJ AC UN THE 

DRQl CF A UC PRAi EH, TO ALlE N 

Nl WA,Y Pl SPClT1 PUTS æ RE 10 'M 

iT 

TH 

El 

SE 

TH 

(: 

S£ 

A F" 

fF 

EH 

A PR 

HA 

EH 

BE 

IS 

.l If 

AlTE, 

AN 

TH AlTE Dt SH Af TO 1H nai tI SE AN 

TH HOTATK "Allt BY fC BY I4 SlT1 11 

DAlE Nl A SP DETl 0" TH ALTETI 

woo. CO 

~ 

BY 

i: 

r i: 

QJ 

i 

Ji 

I 

cr 

i 

0I1 

AERATION TANKS 

DESIGNED -- 

ORAi' ~ 

æECKED ~ 

SECT.æIEF ~ 

PROJ.ENGR. ~ 

SCAl 

AS NOTED 

GALLERY 

EXISl1NG 

PRIMARY SETlNG 

TANKS 

r- - 

I 

I 

I 

-l 

EXISTING 

I.AIN BUILDING 

I 

______0 

I 

L_ 


BLDG. 268 

P,E~ 

HAN AN SAWYR 

Eiiwomneii Ei & Sc 

HAN AND SAWYR, P.C. 

498 SEV AVE ' NEW YORK NEW YORK 10018 

APOVE FOR TH CI OF NEW YOR 

PROJECT MAGER 

PE. 

PE. 

CHIEF, OMSIO Of FAClunES DESIGN- 

\i- 

-'-- - --- 

EXISTING 

CHLORINE CONTACT 

TANK 

CIT OF NEW YORK 


BUREU OF ENGINEERING, DESIGN, AN CONSTRUCON 

RED HOOK WPCP 



----- 

EXISTING BARGE SUP 

i- 

, , 

------- - 

I 

1'=30'-0' 

CIVIL 

EXISTING SITE PLAN 

30 

L. 

15 

.. 

0 30' 

I 

DATE MA Y 2007 

SHEET~OF~ 

DWG. NO. RHGC020

§. 

l 

~ 

l 

¡¡ 

~ 

~ 

~ o 

Ë 

o 

i 

l 

WA 

fß~ 

l 

" § 

.. 

IT lS A. \lT1 a' 5£ 72.2 or TH HE 'i STATE 

EDll lAW' Fæ Nf PE, UNl AC t. TH 

OÆCT a' A lJ F' Dl, TO ALTE .. 

IN WAY Pl, SP1I PLTS æ RETS TO 'M 

Tl S£ Of A PRAL EH HA BE N' FAN 

IT B£ TH SE CS A PR EN IS AlTE, 

TH AL1E a. SH AFX 10 1l rt ll SE .l 

Tl NOTATI 'ALTE BY FU BY Hl SlTU TH 

DATE .l A SPCF OET1 a: THE .l1ETD 

~ 

l 

l? 

~I NO. DATE ISSUED FOR 

Red Hook Advance Basic BNR 

PLAT INFLUENT 

Annual Average Conditions 

PRIMARY SENG TANK INFLUENT 

PRIMARY SETWNG TANK GRAVITY lHlCKENER AEATION TANK AERTION TANK FINAL SETWNG 

EFUENT 

FINAL ~¿i~ TANK I PLAT EFUENT 

OVEFLOW 

CETRA TE RAS WAS 

INFLUENT EFFUENT TANK INFLUENT 

FLOW (MGO) 32.9 36.2 34.9 4.5 0.1 16.9 0.5 39.5 56.4 56.4 39.0 39.0 

TS (m9lL) 199 181 111 150 186 6,446 6,44 116 2,002 2,002 13.3 13.3 

TSS (ibid) 54,700 54,700 32,40 5,700 180 909,50 28,80 38,280 942,30 942,300 4,300 4,300 

CBoo (mglL) 142 129 111 68 65 2,106 2,106 106 655 655 12.5 12.5 

CBoo (Ib/d 39,000 39,00 32,40 2,600 63 297,100 9,400 35,063 30,30 30,JOO 4,100 4,100 

TN (mglL) 31.7 28.8 26.5 25.0 547 415 415 27.7 135 135 10.0 10.0 

TN (ibid) 8,700 8,700 7,700 900 530 56,500 1,900 9,lJO 63,600 63,600 3,300 3,30 

ALKAUNITY 

TANKS 

(6) 

PLAT 

INFLUENT 

MECHANIC, 

BAR 

SCREES 

(4) 

SCREENINGS 

TRUCKED 

~~ 

,.~ 

1 MAIN SEAGE 

I PUMPS (6) 

1 

I 

1 

PRIMARY 

SETNG 

TANKS 

(4) 

PRIMARY 

SLUDGE PUMPS 

(6) 

i-----~ SECONDARY 

I BY-PASS 

1 

I 

I 

I 

r---------- 

AEA nON 

TANKS 

(4) 

ALAUNITY PUMPS 

(4) 

1 CHLORINE 

WAS PUMPS 

(3) 

FINAL 

SETTNG 

TANKS 

(8) 

I 

I 

1 

I 

RAS PUMPS I 

(4) 1 

.i 

CONTACT TANKS 

(2) 

,i 

I 

I 

I 

1 I 

1 

I 

l 

r----.-..---1 

1 

I 

--------------------------------------______1 

, T 

I 

T 

I 

1 ----~--.-------------------------------------------------------------------------------~ 1 

I 

I 

----------------------------------------------------------------------______________J 

(2) 

(2) 

SLUDGE CAKE 

DISPOSAL 

BY 

DESIGED -- 

DRAWN ~ 

CHECKED -- 

SECT.CHIEF ~ 

PROJ.ENCR. ~ 

SCALE 

AS NOTED 

P.E. 

HAN AN SAWYR 

Enri Enrs & Scn1 

HAN ANO SAWYR, P.C. 

498 SEVNT AVE . NEW YORK NEW YORK 10018 

APOVED FO THE CIT OF NEW YO 

PROJECT MAGER 

P.E. 

P.E. 

CHIEF, DMSIO OF FACIS OESIG 


DEPARTMENT OF ENViRONMENTAL PROTECTION 

BUREU OF ENGINEERING, DESIGN, AN CONSUCON 

RED HOOK WPCP 




FLOW DIAGRAM 

MASS BALCE 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHABB010

I 

I 

i 

I 

\ 

-'- 

g !! 

g ~ 

~ 

~ 

l 

~ 

~ 

~ 

g 

~ 

8 2' 

S 

:ö 

i¡ 

" 

g 

; 

l 

l~82' 

w_ 

IT IS A w:TI CE S£ 72.2 CE T1 NE YO STATE 

ED11 LAW Fæ Nf PE, UN ACT l. TH 

DlCT or A UCSE PR EH, TO AllE ll 

JN WAY Pl SPOATK PlTS OR RE TO 'M 

TH SE OF A PR ENEE HA BE AP F 1M 

IT BE 1) SE Of A P' EN IS AlTE, 

l TH ALTE EN 9W J. TO TH lT tI SE AN 

TH NOATX °ALTE BY F' BY HI 9CNTU TH 

DATE AN A SPCF 0E Q" Tl AL1E11 

¡ 

~ ~ 

l 

~ 

~ NO. DAlE ISSUED FOR 

~z, 

waoo.oo 

L! 

GALLERY 

EXISTING 

PRIMARY SETTNG 

TANKS 

r-- 

I 

I 

I 

.J 

EXISTING 

MAIN BUILDING 

T i: 

I 

L 

QJ 

NEW PUMPS, ALKAUNITY STORAGE ANO 

FE IN EXISTING GAU£Y 

i 

I 

FINAL SETTUNG TANKS 

Li 

QJ 

i 

KS 

woo.oo 

BLDG. 268 

BY 

DESIGNED ~ 

DRA\\~ 

CHECKED ~ 

SECT.CHIEF ~ 

PROJ.ENGR. ~ 

SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Enviri Enin & Sd 


498 SEVNT AVE . NEW YOR NEW YOR 10018 

APOVED FOR THE Cf OF NEW YORK 

PROJECT MAGER 

P.E. 

P,E, 

CHIEF, DMSION OF FACLmES DESlGN 

\ i- 

-- 

EXISTING 


TANK 

CIT OF NEW YOR 


BUREU OF ENGINEEING, DESIGN, AN COUCON 

RED HOOK WPCP 



-- 


J 

ii 

i 

.~~_~_.J, 

, I 

--I 

1'=30'-0' 

CIVIL 


EXISTING SITE PLA 

LIMITS OF CONSTRUCTION 

30 

L... 

15 0 30' 

i 

DAlE MAY 2007 

SHEET~OF~ 

DWG. NO. RHABB020

t ¡ 

g 

l 

~ 

~ 

~ 

i 

g 

~ ;i 

~ 

~ 

~ 

~ 

:2 

l 

~ 

~ 

~ 

G 

i¡ 

" 

~ 

o y to ~ \V T 42' ~ Ð-T,~~ï~~~.~ ReP. PRIMARY I l" \! 

¡ M~ I '~3~ 

, i I I I I 

, ø- . iA' ~ o 

Vt\U..lA.R'f SETLINl.- 

TANKS 

.. 

N!GOl) 

I 

o "N~ 

'" 

ẓ 

. 

!7'-6' 

t6' 0J'_G,' in'p') 

I.r-------t------:------- I AERATION ----- TANKS -------¡------ GALLERY -----~------------ 

. ~ 'f, i r':;So , T¡iK AIR HEAR I DR"'. TYPE. il DIFFUSER SUICE I ~ ~F1RE I GATE OPTO 

ROOF HYDR lTR) __ ,-1 

~ ; 

! . I '/ \ i i l j i f DETÄl.oiDWG.II~77 iL EL.I,".o ARRANGEMEi WArER(TYP) (SEE i SEECE!AILON i 8IlSPRA'l 'i ~_--~£'_____. VALVE BO(TVP) \I~.l -- ~ 

_ ,. i "'I! rl ' I i DWG. II 57! I(TYP) (TYP.) : 

-¡:: 

¡ 

i : - - - - r ~ I L I EFFLUE.T CHNNEL I- 1~1-4l''crfEl, rn'P1tcc:-1 

~ 1/11 \ i tó'(Tp.) i =.oa ~ d~ FLO'UL.7'.;0-- ... i. r~.",' nl~o ~ , ! ' (T) 

-ii 

~ 

n!ßr.blr.c~ON I ~ ~ ~ -=1:",,,"'.. S ~ . i~- 

~wi¡~~~1 ~ (~ 3 ~~i;s I ~ (~ ~ OWG. ~2~;~ l ~ ~ ,I ~ ~ ~ Vl-"., 

, I~ ' S-O I .3'-010PIN! I "¡/GlATINGITY) ,0'''5. ì! AIR I I I 1 I I 

i 45P NOZ! I I HE=s crYP.) I I f 

II. ' '.~~~ ~~ ,I I-I ;r~ ,I II ~ : 

, ~ I I ------------,. 

- ---- ---, I .. i 

, I ---- --- 5 '" '" 

~ i;! i -i ____ ---- ___ I ____ i.AIT-2D3-C) ___' IAE:;zrCr I ---- I --- ~ I ~ -~ I -~ L 

I I , ------------ I I æs I I i ------------ 5~ ~f:",__ I ~ I .1 

~ 

~I 

. ¡¡ 

~ 

I i Io'TtPe'C' I z'-' I I "J ¡TYP.) I 

¡ ~PUN6(TY') I I '" i I ,,~ i I j ~ 

! I ~ ì! I I i I ì! I ' I ii ~ - 

i I I ,"¡"-FLOW' 

~E.TEii 

1 I¿. 

:T"(P. 

I 

- 

I 

" 

r' 

OF' 

I ~-,--- 

STRUT 

1:" l- 

i 

I I 

'r-- 

~ ~ ¡ I I ('''ST''"'- 

I II I 

uPRIGHT) 

1EU1i: 

I I ~~~F 

i 

I I 

i 

i IF 

. 

.,' , g.. I I I i, 

"'! 'lt~ )(':'JO.5z .. 

~n¡ I tI ;¡ 1, i . i ~ __-4-90'5,5- 

_-: -¡~ ~:, +- i I ' I _ _ I I I ELbDl\tTVP) 

-, "H ~ on -l ~ft , I I '-;.w.-Er.Et. ELFOW (TYP' , i ~ -T'PE (_.,;.) 

FROlH 8 TOTAL 

eo DiFFUSER 

, ~~ HOOD ~ I j ~ (TY) ~ I, i I Sl riMOuiCOHc tJKb I CTrP) I I '-4'~ I I '11,~ TEE I (~E (TYP) I I 

~TA'_;' ~¡, ",,~'? 

AER4T!ON T.4r.K NO,320! ! ¡ AERAT!ON I I TANK 

I 

NO,3202 

i I 

AERATION' 

i 

1ÄNK 

I 

NO 

II 

320-3 AERATION 

,-4'BUTTERFL' 

I i T.4NK NO.320't ~ I . VALVf(TYP) 

, , I t I 

I I ~.I i I I i 111 I ------------ I -'" _8'L~"" '"- 

~~J'Al (TY) :. 

~~~~~~~ 

~ I 1)! I 

I 

---- 

---- --- I 

i 

i 

: 

____ 

~ ---- 

___ 

---: i ~ HUDER 

IlT"'L ON OWc"M-37) I ------------ I I ------------ I I 

i ' I QÐ.l,OLE !:ON. I I I ,I 

MIXE (Tì) I I I 1":i I (TP') I eM..."'.. 

I I I I - c.ï=Fl.UENT 

I I i I I 

I I I I 

20 TOTAL ,,'(Tf?' I 100V EL ~~:i 

, I I 3Z0lD5 - MATCH 

I ..~TI.G ~d.~,3-0 I LlfoE ITYP) OPEIN :!e04DS 

I 

(fOR 

I I I 

-- -- - - I - SEE. OW. M-33) CCI. 

: II- i , ~i 

NOTES' 

- 

~. 

~ 

!! C 1,- . 

DEES fiXED PIPE 5UPPO 

i 

13 

'1-31 a.. c D£E& 5L10& PIPE SUPPOR 

~ I 

IT IS A -.TK CF S£ 72.2 Of TH NE '\ STATE 

5- EDT1 LAW FO Nf PE, UJ AC UND TH 

oiRE~ r: A. I. PR EN. TO ALTE 1M 

g lH WAY Pl, SPlK PlTS OR RE TO Ii 

Tl SE Of A PRAI fH HA BE AP. F AA 

ri æA TH SE rE A f' £N IS ALTE, 

Tl ALTE EN SJ AfX 10 lH nD ll SE AN 

~-I&C'.(~"""'tD 

TH NOTATI 'AlTE BY fC BY Il SITU TH 

i DO::~ I 

DATE .w A SP 0E Cf TH AllETM 

f, 10 8 6 4 2 0 11' 

I. _DATE: 

i' 

3/32'=1'-0' 

~ 

DESIGNED -- 

SCALE 

APOVE FOR THE CI1 Of NEW YOR 


DRAII -- 

HAEN AN SAWY 


DATE MAY 2007 

j 

CHECKED -- 

P.E. 

~ En Eniii & Så 

PRECT MA 

BUREU OF ENGINEERING, DESIG, AN CONSUCON 

AS NOTED 

MECHANICAl 

SECT.CHIEF -- 

RED HOOK WPCP 

~ HA AND SAWYR, P~C. 

BY I PROJ~ENGR. ~ 



in NO. DATE ISSED FOR P.E. 

P~E 

498 SEVNT AVE ' NEW YORK NEW YORK 10018 CHIEF, DIVISI OF FACIES DESIGN 

DWG. NO. 


TOP PLA - WEST HALF 

RHABB070 

p.N. 

SHEET~OF~

If 

~ 

~ 

~ 

ii 

~ 

~ 

~ 

íi 

l 

~ 

l 

~ 

~ 

¡¡ 

.." 

~ 

~ 

~ .5 

l 

~ 

w_ 

l LIT EDTI ts A LAW WJ1I ~ Fæ SE Nf 7:.. P£, Of LN 1H ACG NE Yt UH STATE TH 

51 

~ DRC1 

AH WAY 

Of A 

Pl 

UC 

SP1J 

PR 

Pl15 

D+EE 

æ: 

TO 

RETS 

ALTE 

TO 

IN 

wt 

". 1H S£ Of A f' EN HA Ba AP. F AH 

g: ~~~~~~::~. 

g I 1H DATE NOATI AH A "1i1æ SP DETI BY Fl Of BY TH tI ALTETI SlruR( TH 

;0 " 

~ 

~ 

~ 

~ 

~I NO. DAlE ISSUED FOR 

1 

FROTH HOO (l' 

8 TOTAL 

, I i 

, 

'lk 

~ 

i; 

-:l: 

¿lAIR PI CHNE J 

CRAIN ~ 

-.0 I L.1!f\ 

t 

-c: 1~ 

~ 

DESIGNED ~ 

ORAI'~ 

CHCKED -- 

SEClCHIEF ~ 

BY I PROJ.ENGR. ~ 

~- ~ d'SPY 

WATE HeAER 

t EL '7.00 

SCAl 

AS NOTED 

P.E. 

HAEN AN SAWY 

Emmen1 Enne & Sceili 


498 SEVNT AVE . NEW YORK NEW YOR 10018 

~I ~ 

APOVE FOR TH CI OF NEW YOR 

PROEC MAGER 

P.E. 

P.E 

QiIEF, DISION OF FACIUES DESIGNim 

NOE:: 

I." ~OR NOTES SEE D'G.l--32. 

3/32'=1'-0' 

10 8 6 4 2 0 11' 

U-W I 



BUREU OF ENGINEERING. DESIGN, AN COSTUC 

RED HOOK WPCP 


ADVANCED TRTMENT TECHNOLOGIES 

:~::'''' M,ciira",!o i 

'~"-2/~ 

MECHANICAL 


TOP PLAN - EAST HALF 

P.N. 

DATE MAY 2007 

SHEET-i OF~ 

DWG. NO. RHABB080

l 

~ 

f 

S5- 

S 

i 

~ 

~ 

1; 

¡¡ 

I! 

~ ;. 

-- 

~ 

l 

l¡~" 

~ 

e 

~ " 

rT is A wxTK OFSEC'T 72 OF TH NE 'i STATE 

EDlI LAW F1 AN PE, UIl AC Ul TI 

0l Of A UC PR ENNE. TO AlTE i' 

AH WAY PI, SPlK PLlS OR RETS TO -l 

n£ SE Of A PRCH 0l HA El AP. If Nl 

ITD BE TH SE Of A PR EN ts AlTE, 

TI AlTE EN SH AF 10 TH I1 IC SE AN 

TI NOTAll 'AlTE BY f' BY l- SIGNA:nlR, Tl 

DATE lH A SP 0E Of TH ALlElK 

~ 

~I NO. DATE ISS FOR 

Red Hook Full Step BNR 

PlAT INFLUENT PRII.ARY SETTNG TANK INFLUENT 

PRlI.ARY SETTNG TANK GRA VlTY THICKENER 

CENTRA TE RAS 

AERATION TANK 

WAS 

AEATION TANK 

Annual Average Conditons FINAL SENG FINAL ~~~ TANK ¡PlAT EfUENT 

EFFUENT OVEFLOW INFLUENT EFFUENT TANK INFLUENT 

FLOW (MGD) 32.9 36.2 34.9 4.5 0.1 34.2 0.7 39.5 73.7 73.7 36.8 36.8 

TSS (mg/L) 199 181 11 150 186 5,271 5,271 116 2,502 2,502 13.3 13.3 

TS (IbId) 54,700 54,700 32,40 5,700 180 1,502,700 31,200 36,280 1,538,100 1,536,100 4,300 4,300 

æOD (mg/L) 142 129 111 68 65 1,915 1,915 106 910 910 125 12.5 

CBOD (ibId) 39,000 39,00 32,40 2,600 63 54,000 11,30 35,063 559,30 559,300 4,000 4,00 

TN (m9/L) 31.7 28.8 26.5 25.0 547 354 354 27.7 171 171 6.7 6.7 

TN (ibId) 8,700 8,700 7,700 900 530 100,800 2,100 9,130 105,100 105,100 2,200 2,200 

PlT 

INFLUENT 

MECHANIC. 

BAR 

SCREENS 

(4) 

SCREENINGS 

TRUCK 

",'" 

¡,'" 

PRII.ARY 

SETTNG 

TANKS 

(4) 

I.A1N SEWAGE 

PUI.PS (6) PRII.ARY 

SlUDGE PUMPS 

(6) 

r--'- SECONDARY 

1 BY-PASS 

1 

1 

1 

1 FINAL 

SETTNG 

TANKS 

(8) 

WAS PUI.PS 

(3) 

RAS PUI.PS 

(9) 

CHLORINE 

CONTACT TANKS 

(2) 

,1 

1 

ì 

T 

1 i--------'---i I 

, 

1 

t 

--------------------------------------______1 I 1 -------------------------------------------------------_______________________J 1 

I 

1 

----------------------------------------------------------_________________________J 

(2) 

SlUDGE CAKE 

DISPOSAL 

(2) 

BY 

DEGNED ~ 

ORAWN -- 

CHECKED -- 

SECT.CHIE ~ 

PROJ.ENGR. ~ 

SCALE 

AS NOTED 

P.E. 

HAN AN SAWY 

Erme Engne & Sc 


498 SEVNT AVE 'NEWYORKNEWYOR 10018 

APOVE FO THE CI OF NEW YOR CIT OF NEW YORK 


PROJEC fM 

P~E. 

P.E. 

CHEF, DION OF FACH.ES DESIGN 

BUREU OF ENGINEERING, DESIGN, AN CONSUC 

RED HOOK WPCP 



FULL STEP BNR 

FLOW DIAGRA 

MASS BALNCE 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSB090

I 

I 

I 

I 

\ 

- 

~. 

\l 

l 

~ 

~ 

~ 

~ 

~ 

l 

~ 

~ õ:: 

£ 

~" 

~ 

8 

~ 

l 

~ 

~ 

~ 

~ 

g¡ 

g 

~ 

"~'" 

! 

¡¡ 

~ 

~ 

z-~ 

c: 

GAllRY 

r-- 

I 

I 

EXISTING 


TANKS 

-l EXISTING 

'MAIN BUILDING 

T u: 

i 

I 

L_ 

Lj 

I 

I 

Q 

~I 

WOO.DO 

.. 

IT IS A 'w11 f: SECT 72.2 Of TH NE 'i STA~ 

EDTX LAW F' Nf PE, UlI ACNG UH TH 

DICT OF A lJ PR ENNE, TO ALTE '" 

Nf WAY PI, SPl), PlTS OR RE TO Yi 

Tl SE Of A. F'AL EH HA BE N' F AN 

I1 BENG TH SE or A PR DI IS ALlt, 

TH ALTE DiEE SH AFX 10 Tl rn ll SE AN 

n£ NOTAllCl 'AlTE BY I' BY liS Sl1I TH 

DAlE AN A SPCf DElK aF tHE ALTETI 

BLOG. 268 

DESIGNED NB 

DRA\\ NN 

NO. I DATE -1 ISSUED fOR I BY I PROJ.ENGR. ~ 

SCALE 

HAEN AN SAWY 

APOVE FOR THE CIT Of NEWYOR 

CHECKED NB En Enrs & Sc PROJECT MAGE 

AS NOTED 

SECT.CHIEf ~ 

HA AND SAWYR, P.C. P,E. 

P.E. 

498 SEVNT AVE . NEW YOR NEW YOR 10018 CHEF, DMSIO OF FAClmES DESIGN 

P~E. 

NEW CHEMICA HANDUNG BUILDNG 

\i- 

--- 

- 

EXISTING 8ARGE SUP 

i' 

¡i 

___~~___,____~_________~___~. 1;T- 

~-----I 

, , 

EXISTING 


TANK 

I 

_ _ _ _ _ -- _ 

~ 

I2 UMITS Of CONSlUCllON 

1'=30'-0' 

30 15 0 30' 

i. _i-_.. i 



BUREU OF ENGINEERING, DESIGN AN COUCN 

RED HOOK WPCP 

CONCEPTAL DESIGN 

ADVANCED TREATMENTTECHNOLOGIES 

CIVIL 



DAlE MAY 2007 

SHEET-- OF~ 

DWG. NO. RHFSB100

i 

0-.~' 

1'~IMARV SEt.INt;- 

rANKS 0"' oÑ- 

'" z: 

'- 

NSG0t. 

"-;! - , 

t.¡ 

! . 

, 

~ DcÏÄl ON 

~c; "-37 Jß; I . ,ti .: 

i ! 

I N 

¡ ~;i 

7;! -, 

I 

I , 

I ! 

¡ I 

i ! 

'~i l- 

~; I 

FROTH HooO (T)) 

8 TOTAl 

~ 

i 

BAF WAl (T)) 

28 TOTAl 

~ 

i 

l~ 

~ 

MIXER (T)) 

¥ 

20 TOTAl 

l 

ß2' 

¡¡ 

! 

i¡ 

~ 

1; 

~ 

l 

l~ 

~ 

IT IS A 'wTI or ~T1 72.2 or DE NE 'I STATE 

EDTI LAW Ft Nl PE, Uhl ACNG UIl n£ 

D1RECT or A IJ PR D+NE, 11 AI TE H 

Nf WAY Pl. SPTI, PlTS OR RETS 10 \I 

11 S£ Of A PRAL EN HA BE AP. f' A, 

fl SE TH SE Of A f" EH IS ALTE, 

TH ALt¡ fN SH N'X TO TH lT ll SE IH 

n£ NOTAlIa. 'ALTE BY fW BY HIS SlAlO TH 

DATE lH A SPa: OETi Of TH ALTETK 

l 

i 

.. 

" , '" 

OESIGNEO -. 

'" 

SCALE 

DRAWN -- 

Ii 

~ 

CHECKEO -- 

~ 

âi NO. DAlE ISSUEO FOR 

SECT.CHIEF ~ 

BY I PROJENGR. ~ 

AS NOTED 

~ 

P.E. 

T~ 

, . 

~ 

HAEN AN SAWY 

Ei En & Sc 

HAEN AN SAWYR, P.C. 

498 SEVNT AVE ' NEW YORK NE VOR 10018 

APOVED FO THE Cf OF NEW YOR 

PRECT MAGE 

P.E. 

P.E 

CHIEF, DIVIION OF FACIUES OESlGN- 

P.N. 

NOTES' 

1.- A DENOTES I'XEO PIPE SUPPO 

2," A DENOES 5lICE PIPE SUPPOR 

3/32'=1'-0' 

i.W I 

10 8 6 4 2 0 11' 



BUREU OF ENGINEERING, DESIGN, AN CONSTRUC 

RED HOOK WPCP 



r-OO--~~i f,~t';:tilJl.w I O'T£:~ I 

MECHANICAL 




SHEET~OF~ 

DWG. NO. RHFSB120

i 

¡ 

I 

¡ 

i 

, 

P.N. 

i5 

~ 

~ 

i 

5 ii 

~ 

~ 

~ 

5 

~ o 

5 

- , 3~ -r__ 

I I J S40BS' 

_ MATCH L'Ntõ (FO"- cc'"~ SEe DWG.M-S2) 

I I IT-~~02-e, ~ ~Al-~ll-~ ~ " - I ,,æ)-e,~ 

) ) COAI~ED SLuice SELF L ) '320-i: 

~ ( RfMO'A&E CO. ~ (¡ G.ln. CT,.P.) ~ (, 

'I -3202-/, I AE-~¡; s-J!?1.o' 

. , I FLANK&CI.,P.l I 

tiGRA"TING(TYP.) ! 

, i 

~ ii ,I .1 i i - 

"' 

~ 

I 'N ~ I I I I ! ~ I I -9 í? 

FROTH HOOD (l)) 

B TOTAl 

i l ~~ 1 ~~~!i~ 

I 

~ 

-ZI 

'" 

I II 

I 

I 

u 

I 

~ 

H 

I 

---- 

!J1 uj, 

--- 

OF" 

I ~¡1 

STRT __ EFFlT 

k ~1 Z' ,V.lWS,T'!P.) t" I I .-- i I I ¡-, , I 

4~45' ~ ~ I I -i I I 41Ai Pi CHANNE f:h 

I 

oi..IN 

a,¡ I -"'t\ 

t 

J iii 

I I I ....!'OW 

~II 

MeT..R 

ll~11 

- 0'; 111=1' 

-c: -n 

!! 

I .c - HEADER 

Ñ t i wi i ~ 

'- 

i 

I 

õ 

-i I I 

ll 

II 

I _ 

91 

U) 

l 

I .hIRP'P'NGCHANNEL 

ORAIN,iYP'1 " I II ;; 

I 

.1' 

! 

I 

- 

I õ 

1'$ ! III I ~ Ii" I I 11,1 "\ II, I I I ~ i~ iii I II I "\ ~ 

BAF WALL (l)) 

24 TOTAL 

MIXE (l)) 

24 TOTAl 

J ~ AARANMENT (see 

I 

I 

. 

I 

I 

I 

I 

i, 

I 

t 

~ 

i' 

, 

-,¡ 

I DETAIL 

E. __TYPE 

1l6. 

.~ DtFFU&ER 

""-37) 

- I I I I ~ , .----------- , I S- 1£1 I t I _ .9 ,. ~ ELBOW 4'.'l"~. 

I :i.ø I I ---- %0 1""1 --- oJ C1c _ (TVP.' '" 

, _ _ I I I lo"S.S.I"Qc...~ I I 0: ------------ I Si I me'c" 

I \ I I AlII ~ ~el..'il.oo I tl' S~5 ;¡ I ~ All" I CQPLlWCiIT1P.) 

~ ul úl 

;i 

I ~ C,.YP.lCINST..U. r.' I ,.yp. I 10' I lOe.iiF'''v UPI",) -,ö I t I It I "'EL~ 

I I I 

ia, 

i 

00 

ri (~~?¡ ~ 1, r I I 11 i: 1~,'(TY) I I 1 r I I !'~l~S't"'"NEL 

i Ii' ~', ,Ii ~ , I ---- i "Y I --- I ~ 1'1 I I ~ III ~ I' ---- i I --- ~ ~ 4e:Aoi:a ì!Ut.~ I - B"SS. TO TAN"-: F"'NAL "Ill 

I ',i II. I i I 1,1 l I ------------ ---- --- I I ii ii I ------------ I ---- --- I I i ~ 

!~ I I., II !:i'i II IIi II ~ 

~.. I AERATION lANK NO.3401 Ii i AERATION I I TANK NO.3402 i¡l,i AERATION I I TANK NO.3403 II1 AERATION TANK NO.3404 ~ : ~ ~ I ii~l , I I ;:'J11 I I III I I IX 

1 

1 

" ~I 

~ 

I', I I IIi i' "' i' II, I L 

II s-o'd-O'OPENING 

I I W/GRATI~G(TYP.) 

ii ~;I~i!gJ1l.. 

III I I '..E.(TV,1 

II 

I I 

III i I I III I I I ' I i II, I I I ; ~ 

B C 

,,'DRNN IN ALL COMPAitErlT5) VALve (T"PICAL. ~ 

~ 

1"-3, M-!G 

S 

iõ 

i¡ 

o 

~ .i 

NOE' 

I.- ~OR NOTES SEE DWG.M-32. 

~ 

5 

II 

~ 

~ 

... 

IT IS A WlTI ey SE 72O!U c: Tl NE 'Y STA'l 

ii I ED TI LAW Fæ NlY PE, lH AC l. ni 

~ ORCW CF A lJ P'Al EN 10 AlTE IN 

g ';:i~~~~:.~, 

5 AH WAY Pl, SPCI11, PllS æ R£TS 'T ¥H 

:; Di SE OF A PR El HA BE AP F AN 

g Tl NOTATI .ALTE BY F' BY I- SlTU 11 

§ DAlE AN A SPCl DE Of Tt ALTETK 

~ ~ 

~ 

DESIGNED -l 

DRAVi ~ 

& '" æECKED ~ 

SECT.æIEF ~ 

~ 

a I NO. DATE ISSUED FOR BY I PROJ.ENGR ~ 

SCAl 

AS NOTED 

P.E. 

HAN AN SAWYR 

Enme 8iin & Så 

HAN AND SAWYR. P.C. 

498 SEVNT AVE . NEW YOR NEW YORK 10018 

APOVE FO 1l CITY OF NEW YOR 

PROJECT MAGE 

P,E. 

P.E. 

CHIEF. DMSION OF FACIUTS DESIG 

3/32'=1'-0' 



BUREU OF ENGINEERING. DESIG, AN CONSTRN 

RED HOOK WPCP 



10 B 6 4 2 0 11' 

U-W I 

OOCÙ..,,~ '''CJrllN.!D Î 

c'."r~~ 

MECHANICAL 


TOP PLA - EAST HALF 

DATE MAY 2007 

SHEET-- OF ~ 

DWG. NO. RHFSB130

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

?i 

~i 

~i 

~ 

(2 

j 

~ 

l 

~ 

~- 

ïi 

l 

i 

~~ 

l 

l 

ïi 

~ 

~ 

8 ~ 

~ 

l 

ïi 

l 

~ 

~ 

~ 

~~ 

~ 

l 

~8 

¡ 

~~ 

~ o 

~ 

¡; 

'¡ 

~ 

l 

51 

~ 

~ 

l 

l 

¡:i 

" 

~ 

CD 

CD 

.. 

IT IS A ~OlTi OF SECT 72.2 Of It NE 'l STATE 

EDTK LAW ft Nf PE, UN AC1 tJ Tl 

DÆ fI A LI PR EH, TO ALTE l0 

#N WAY Pl, SPTk PLlS OR RE TO 'M 

TH SE OF A PRAL eiEE HA BE N'. F AN 

IT æA TH SE Of A PRCK EH IS ALTE, 

TH ALtt EN SH AF TO T1 IT HI SE Nl 

TH NOTATX 'AlTE BY Rl BY HIS SQTU TH 

OAT£ Nl A SPa' OETK OF TH ALlET1 

OESIGNED ~ 

DRA\\ -- 

:; 

l 

CHECKED ~ 

~ 

SECT.CHIEF ~ 

81 NO. OAlE ISSUED FOR BY I PROJ.ENGR. ~ 

GROUND FLOOR PLAN 

3/16'=1'-0' 

SCAl 

3/16'=1'-0' 

P.E. 

cpi 

68'-6' 

HAEN AN SAWY 

Enro Enin & Så 

HAEN AND SAWYR, P.C, 

498 SEVNT AVE . NEW YORK NE YORK 10018 

~i 

I 7'-8' I 

~i 

~i 

~i 

"0 



BUREU OF ENGINEERING, OESIGN, AN CON 

RED HOOK WPCP 



~i 

~I_- 'Y" 

3/16'=1'-0' 

6 

L.U 

4 2 0 5' 

i 

/:T-nU-I_. ._",,_.JU '-~~ r---.. ~.'" i 

~~i--l ~ ~~ L 

!! il._~_ i L~_._j &g:: '-J 

,. II" p ~ il ,. 

i ~ 

.~!r-r-'''--n~ r 

ib L__=~_ 

KEY PLAN 

GROUND FLOOR 

DATE MAY 2007 

CHEMICAL HANDLING BUILDING 

ARCHITECTURAL 

SHEET-- OF~ 

DWG. NO. RHFSB140

i 

I 

i 

I 

i 

I 

I 

'f 

~ 

i¡ 

l 

~ 

~ 

l 

~ 

2- 

j 

~ 

l 

~ 

~ ~ ~ r ~ 

i i 

i I 

6' CONTA'N~ENT PIPE 

r,._~'". 

2' Flll IN 4' . 

r CONTAINMENT PIPEi i 

i c~- iF -"'""~ ~oo i 

,. TO INLET CHANNEL, Cl EL 5.0 

,. CHLORINE CONTACT TANK 

SAMPUNG UNE, CL EL 6.0 

-~ 2' TO CHLORINE TANKS, Cl EL 5.0 

'1 

~ 

'2' TO 54' RAS, CL EL 5.0 

i¡ 

2' TO AEA llON TANKS, 

l CL EL 5.0 

~ 

~ 

l 

~ 

~i 

ri 

~i 

?i 

l- 

i¡ 

l 

~ 

~ 

l 

~ 

l 

:e 

l 

~ 

8 ~ 

S 

l s:; 

g 

gi¡ 

l 

~ 

~ 

~ 

o 

~ 

~ 

Ii 

~ 

l 

II 

~ 

~ 

l 

l 

¡ 

" " 

~ 

l '" 

R. 

~I NO. 

2' TO C£ TANKS, 

CL EL 5.0 

3' TO AERAllON TANKS, 

CL EL 5.0 

WA 

IT IS It ~~ CF SE 72.2 Of lH HE "l STAlE 

EDTI LAW FO /o PE, UN AC l. ll 

0Il1 Of A UC PR 9lE£ TO AI TE .. 

Al WAY Pl SPCATi, PlTS OR RETS TO 'M 

TH SE Of It PR EH HA 8E AP F AN 

ri Elc ll SE CF A PR EJ IS ALlE, 

Tt Al TD EN SH Am TO TH l' tI SE AN 

n£ NOTAll "AllE BY' FCWE BY tI SKTU TH 

DATE AN A SP CE CF 1H AI lE ne 

DAlE ISSUED FOR BY 

DESIGNED ~ 

DRA\\ -- 

CHCKED -- 

SECT.CHIEf ~ 

PROJ.ENGR ~ 

SCALE 


3/16'=1'-0' 

HAEN AN SAWYR 

En,;ri Enri & Så 

APOVEO FOR THE CI OF NEW YOR CIT OF NEW YORK 


PROJT MAGER 

BUREU OF ENGINEERING. DESIG, AN CON 

2' Fliiij 4' 

CONTAIN ENT PIPE (TY) 

3' TRANSFR Flll IN 

6' CONTAINMENT PIPE (TY) 

P£ CHEMICAL HANDLING BUILDING 

MECHANICAL 

RED HOOK WPCP 

CONCEPTUAl DESIGN 


3/16'=1'-0' 

6 

I. 

4 2 

i. 

0 5' 

I 

,-Ì7-:::._r-~---- 

f:~""'-'' ('i-QQ() r-~ 

ir=-' XX~~-'=i' .' 

I~~ ~~J~/ 

IT f"'l( i 

L -'--- ,. 

I . ¡ . ,i" H 

¡ _ .J.--c,--i-_~ 

KE PLAN 

3/16'=1'-0' SHEET -- OF~ 

HAZEN AND SAWYR, P.C. 

P,E. P.E~ 

498 SEVNTH AVE ' NEW YORK NEW YORK 10018 CHIEF, DMSIO Of FACIUTIES DEIGNOU 

GROUND FLOOR 

DATE 

MAY 2007 

DWG. NO. RHFSB150

I 

I 

I 

I,,,,,I 

l 

, 

, 

I 

, 

I 

c 

15'-0' 

2' FlLL IN 

4' COTAINMENT PIPE, 

INV El 34.91 

I , CAGED lADE ACCESS (-l) 

, 

\ 

rii 

~' 

;i 

l 

II 

:; 

~ 

l 

~~. 

i 

j; 

1 

~ 

l 

~ 

~ 

;i 

~ 

j; 

~ 

l 

~ 

~ 

~ 

l 

~ 

~ 

~ 

~ 

~ o 

~ 

'" 

I 

mIiI 

25,000 GALLONS 

50~ ALKAUNITY 

STORAGE 

TANK NO 

'- 

CHB270020 

L 

-$ 

/ " 

PUMP SUCT, 

CL El 7.42 

1r4' TRANSFER 

~ 

l 

II 

¡ c 

! 

i§~'" 

~ 

E 

¡¡ 

'" 

~ 

l 

.. 

IT IS A \1T1 a" SEC1 72.2 CF TH HE Ya STATE 

£DlI LAW FO lH PE, UH Ac; ON TH 

DICT OF A lJ PR Di, TO ALT! il 

AN WAY Pl, SP11. PlTS OR RE TO Vi 

1l SE OF It ~Al EN HA 8E AP. If AN 

IT BE lH SE CF A PR EN IS AlTE, 

1) ALTE EN SH .lX TO TI IT l- SE AN 

1l NOlAna 'AlTE BY f' 8' Hl 9CTU, n£ 

DAn: IH .. SP OETK CF DIE AllET1 

DRAI'~ 

DESIGNED NB 

CHECKED NB 

NO. I DATE I ISSED FOR I BY I PROJ.ENGR 

I SCALE 

SECT.CHIEF ~ I 1/4'=1'-0' 

PDS 

P.L 

D 

E 

F G 

18'-6' 

18'-0' 

13'-3' 14'-0' 

ll 

=====1 I 

II 

" 

-----'/' 

/ 

IN 6' CONTAINMENT PIPE 

INV El 34.91 

r3' TRANSF FlLL 

"" ::========::~~~ 

111 

ii III 

----------"'hl 

111111 

l- (,~t 

Ili 

('~l. 

111111111 ILL 

't'W i¡ '1'11'11' 'II 

.. 

-- 

i I !J! '41 it 

1.1 III 111111 i 1.1 HI it i 

111111111 111 

V4'OF 

I, 3' TRANSFF FIL 

ill IIIII1 III 

/ 

I 

111111111 III 

111111111 Ili 

111111111 III 

111111111 III 

111111111 III 

111111111 JlI 

ILL 111111 Ili 

III 111111 Ili 

IIllliiil III 

1I111111i IIi 

iii 111111 III 

ILL ILL 

III 111111 III 

Ili 111111 III 

III Ili III Ili 

ill 111111 III 

Ili lilli' III 

TPa~ ~ ~ l,ø 

IN 6' CONTAINM 

251_~Xu'tm~5 

50 LKAUNITY 

S-¡ AGE 

I NO 

CH 70040 

wll- 

I 

tg -$ ~ METERING PUMP 

Ell 

-= 

H1 H1 H1 ~ii ~I 

,("("("1' 1j 

If' If I ',' III :iJ 

:i: Iil:': III ~ 

Illlllllilf '" 

iii III IIIII -lI 

't 't 't ~ ""I 

IJIII~ 

_ .. 

y- 

, 

ț 

~ ~ 

113'-10' 

l' CAUBRA TION O'ÆFLOW 

a. El 35.25 

3' TRANSF IN 6' COTAINMENT PIPE 

2' FlLL IN 4' CONTAINMENT PIPE 

INV EL 33.41 

3' EW, a. EL 20.08 

EL 23.50 

U;4' EW, a. El 20.67 

/1/ 

II~ 

/- 4' EW 

In ': a. El12.95 

trl CAUBRATION UNE 

4' 

a: El 8,87 

4' METING PUMP SUCl 

CL EL 7.42 

1'-8' 

4' EW 

CLEL~ 

4' EW TO CE TANK , 

F a. EL 20.00 2' METRING PUMP DISCH 


CL EL 18.41 

2' METRING PUMP DISCH 


a. EL 15.83 

2' RElEF VAVl DISCH 

l' CAUBRA T10N UNE-- 

2' METEING PUMP SUCT 

i 4 

4' TRANSF PUMP SUCL' 


a. EL 7.42 

I 

, 

~ 

!li 

~ 

~Hi 

t~1i/ --- ----;-:t=~ 

l:f--I-~~~~3!~~- -- 

~!~î 

4' OF 

m 

a. METERING POMP 

1\ ~ 

~ 

fo 


INV El 34.91 

-l3' TRANSFR FlLL 

4' OF 

J. 

W"I 

~ 

-~ - 

'lt 

, I 

'" 

1'-6' 10 4'-0' 

SECTION A 

1/4'=1'-0' B-M 

HAEN AN SAWY 

En Enii & Sc 

HAEN AND SAWYR, P.C. 


APROVE FO THE CI OF NEW YOR 

PRECT MAGE 

P.E 

P~E. 

CHIEF. OIVSION OF FAClES DESIGN 



BURE OF ENGINEERING. DESIGN. Nl CONSUCON 

RED HOOK WPCP 



H 

12'-7' 

cp 

/ 

IN 6' COTAINMENT PIPE 

INV EL 34,91 

, r 3' TRANSF FILL 

I 

, 

I 

, 

I 

, 

4' 'I 

a. El 34.67 

(3)2' METERING PUMP DISCH 

----~.====l==~=======ii :~v4~ ~~~NMENT PIPE EACH 

I~ 

.t 

~-j 

, : 

n' J i 

M' 

r , 

I , 

I 

/ 

iii l' CHLORINE CONTACT TANK SAMPUNG UNE 

iil a. EL 19.50 

it l' NaOa. IN 3' CONTAINMENT PIPE, 

!I! a. EL 14.87 

=-=__=~I: 

----I 

~ 

mi.i 

~ 

il 

i- 

2'-7' 

l% 

l' CHLORINE CONTACT TANK SAMPUNG UNE 

a. EL 20.50 

I~ TOP OF Ell1.87 PARAPET 

~ (2) l' CHLORINE CONTACT TANK 

EL 925 SMIPUNG UNE, a. EL 6.00 

. GRADE 

'~~:Y EL 7.25 

(1 l HYPO IN 2' COTAINMENT PIPE (FAR) 

3 2' EW YPO IN 4 ' CONTAINMENT PIPE 

El 5.0 - 

EL 2,00 

1/4'=1'-0' 

1 0 1 2 3 7' 

~W I 

BLOWER BUILDING 

MECHANICAL 

SECTION 

SHEET 1 


SHEET-- or~ 

DWG. NO. RHFSB160

I 

Red Hook Full Step BNR w 

Solids Filtron PLANT INFLUENT PRIMARY SENG TANK INFLUENT 

Annual Average Conditons 

GRA 1¡1Y THICKENER 

AERATION TANK AERATION TANK RNAL SETING RNAL SETING TANK RLTE INFLUENT I PLANT EFFUENT 

I PRIMARY 

EfUENT 

SENG TANK I 

OVEFLOW INFLUENT EfUENT TANK INFLUENT EFFENT 


I I I I I I I i I RL TE EFLUENT 

FLOW (MOO) 329 36.2 34.9 4.5 0.1 34.2 0.7 39.5 73.7 73.7 38.8 38.8 38.8 39 

15S (mglL) 199 181 111 150 186 5,271 5,271 116 2,502 2,502 13 13 4.0 4 

TS (Ibid) 54,700 54,700 32,40 5,700 180 1,502,700 31,200 38,280 1,53,100 1,53,100 4,30 4,30 1,30 1,30 

æoo (mglL) 142 129 11 68 65 1,915 1,915 106 910 910 12.5 12.5 4.0 4 

æoo (Ibid) 39,000 39,00 32,40 2,600 63 546,00 11,300 35,063 559,300 559,30 4,00 4,00 1,300 1,300 

TN (mglL) 31.7 28.8 26.5 25.0 547 35 354 27.7 171 171 6.7 6.7 6.1 

TN (Ibid) 8,700 8,700 7,700 900 530 100,800 2,100 9,130 105,100 105,100 2,200 2,200 2,00 I 2,000 

PLAT 

INFLUENT 

t.ECHANICA 

BAR 

SCREENS 

(4) 

SCREEINGS 

TRUCKED 

..~ 

.. .... 

I MAIN SEWAGE 

I PUMPS (6) 

I 

I 

I 

I 

I 

PRIMARY 

SETING 

TANKS 

(4) I 

PRIMARY 

SlUOGE PUMPS 

(6) 

,._.- SECONOARY 

I BY-PASS 

I 

I 

I 

I RNAL 

SENG 

TANKS 

(8) 

I 

I 

I 

I 

I 

I 

I 

I 

I 

I 

CHLORINE 

COTACT TANKS 

(2) 

~ 

~ 

i 

13 

~ 

!; 

~ i¡ 

~ o!l 

l: 

1; 

¡; 

i. 

!l 

~ 

II 

~ 

~ 

l 

¡:i 

" 

~ 

l Ñ 

~ 

.. 

IT IS A \ØT1 CF SE '7.2 Of 1H NE 'l STATE 

EDT1 LAW Fa Nf PE, Ul ACNG UHO TH 

0I Of It lJ PR EN TO ALTE il 

Nf WAY Pl, SÆORno, PlTS OR RE TO \H 

Tl SE Of A PRAL EN HA El N' F AN 

iT El TH S£ Of A PR EN IS AlTE, 

TH AL1t EH SH AFX TO TH l1 !- SE AN 

Tl NOTATION "ALTE BY f1 BY tlS 9ûll TH 

DATE AN A SPCl DETI Of 1H AlTEno 

~I NO. DATE ISSED FOR 

BY 

DESiGNEO ~ 

ORAII -- 

CHECKED ~ 

SEC1CHIEF ~ 

PROJ.ENGR. ~ 

SCALE 

AS NOTED 

I I 

li 

I i----r--~--' 

_________ ________________ T , l 

_____________________________________::::::::::::_-_-:------~ i i 

J I 

-------------------------------------------------------------------~~~~~------j 

P.E. 

HAEN AN SA\W 

Er En & Sc 

HAEN AND SAWYR. P.C, 


(2) 

APVE FOR THE CI OF NEyoRK 

PREC MAGE 

P.E. 

P~E. 

CHIEF, DIVSION OF FAClmES OESIGN 



BUREU OF ENGINENG, DESI. AN CONSUCoN 

RED HOOK WPCP 


ADVANCED TRETMENT TECHNOLOGIES 

FULL STEP BND & SOLIDS FILTERS 

(2) 

FLOW DIAGRAM 

MASS BAlNCE 

SLUDGE CAKE 

DISPOSAL 


SHEET-- DF~ 

DWG. NO. RHFSS210

i 

I 

~- 

¡; 

i 

~~ 

m' 

!l 

I! 

~ 

~ 

~ 

~ 

~ 

~- 

;¡ 

l 

~ 

~ 

¡; 

i: 

i 

i¡ 

. 

~s 

j :i 

i 

~¡: 

i 

¡ 

~ " 

'" 

~ 

E 

* '" 

~ 

.. 

IT IS A \MTI or SECTI 72 (E THE NE 'l STATE 

EOTD LAW FO Nr PE, UN. AClHG UIC T1 

D1RE Of A UC PR EN, TO ALTE IN 

N4 WAY PI. SfCIlK, PlTS OR R£ TO \H 

TH 5E Of A PRAl EH HA BE AP. F AN 

ITD El TH SD or A PR 0l IS AlTE, 

TH AlTE EN 5H Am TO lI I1 HI SE Nl 

TH NOTATla- "AlTE BY Fa BY lI SKlU, TI 

DATE, li A SP DEno or TH Al1Ell 

~I NO. DATE ISSUED fOR 

woo.oo 

BY 

;z. 

C: 

T i: 

QJ 

i 

I 

Q 

I 

cr 

i 

DESIGNED ~ 

DRA\\ -- 

CHECKED ~ 

SECT.OlIEr ~ 

PROJENGR. ~ 

SCALE 

AS NOTED 

GALLERY 

EXISTING 


TANKS 

BLDG. 268 

P.£. 

EXISTING 

MAIN BUILDING 

I 

L 

HAEN AN SAWY 

En Ei & Sc 

HAEN AND SAWYR, P~C~ 

498 SEVNT AVE ' NEW YORK NEW YORK 10018 

APOVED FOR THE CI OF NEW YOR 

PROJECT MA 

P.E 

P.E 

CHEF, OMSION OF FACiiIES DESIGN- 

NEW CHEMICAL HANDUNG BUILDING 

\ -'- - - 

EXISTING BARGE SLIP 

fOOlPRINT fOR NEW 

SOLDS FILTERS 

EXISTING 


TANK 

1'=30'-0' 

30 15 D 30' 

L._"-_-' I 

--IilT~--~ 

ìF4 .i i '-1 100 

'I I 00' 

it-_--v L_J W 

ii I L~ i ii ¡if I 

i l-l ~ ~ ;i /'" 

l-~..___.J 

KEY PlA 



BUREU OF ENGINEERING, DESIG, AN COUCON 

RED HOOK WPCP 



CIVIL 



DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSS220

2 

j 

~ 

~ 

~ 

1.- 

g Ii 

~ 

~ 

~ 

~ 

:t 

l 

~ 

~ 

~ 

j.- 

:l 

l 

~ 

~ 

~ 

-;' 

¡¡ 

g Ii 

~ 

~ 

s~~ 

§ 

~ 

l 

~o~ 

S 

~ 

o 

~ 

il 

¡¡ 

~ ~ 

~ 

l 

¡: 

~ 

g¡ 

§ ~" 

~ 

l " 

¡ 

a I NO. DAlE ISSED FOR 

EXISTING 

"" 

IT IS A ~1l CI sa 72.2 or Tl NE 'I STATE 

EDTI LAW FO lN PE, UNl AC UND TH 

0lRE Of A LI PR £N 10 AllE .. 

Nf WAY Pl, SP~ PlTS OR RETS 10 -l 

1H SE or It PR EN HA El AW. F AN 

ITD BE TH SE or A PR EN IS AlTE, 

TH ALTE EN SH .¥ TO 1H ITD I- SE AN 

Tl NOTAlO 'AlTE BY Ft BY Hl Sllt T1 

0AlE N¥ It SPCF DETK a TH AllEno 

SLUDGfc STORAGE 

AND 

CENTRIFUGE BLDG. 

---------------l 

SODS FILTES 

27" PER FILlER 

6' FILlER DEPTH 

EXISTING 


TANK NEW BUILDING FOR SCOURGE AIR BLOVÆS 

WAlER BACKWASH PUMPS FOR SOUDS FILTES 

DESIGNED -- 

DRA'I -- 

CHECK -- 

SECT.CHIEF ~ 


SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Eiom Enrs & Sd 

HA ANO SAWYR, P~C. 


APROVE FOR THE CI OF NE YORK 

PROJECT MN 

P.E 

P.E. 

CHIEF, DIVISION OF FACIES oeSiGN 

o oci 

N 

o 

Z 

1'=20'-0' 



BUREU OF ENGINEERNG, DESIG, AN CONSUCON 

RED HOOK WPCP 



CIVIL 

PROPOSED SITE PLAN 

20 

L .. 

10 

.. 

0 20' 

I 

t~.=..--= 

-'r= ID~Ù" i q 

It~J L---i M ':V.--i 

r-- 

ill -rn( 

-- '7 ¡ 

i 

l.- _l_ UL_ I 

KEY PLA --- 

DAlE MAY 2007 

SHEET-l OF~ 

DWG. NO. RHFSS230

¡' 

~ 

~ 

t 

~ 

l 

~ 

~ :; 

g 

~ 

l 

~ 

~ 

~ 

IT IS A '-TK or SE 72.2 OF TH NE YO STATE 

ED1' LAW FO lH PE. UN AC UH n£ 

OlRE OF A UC Pf DlNE, 10 ALTI II 

N( WAY PL, SPll, flTS DR RE 1' Yi 

mE SE Of A ~AL EN HA BE AP lf AN 

JT B£ Tl SE OF A f" 0K IS ALTE, 

TH ALlë ENEE SH AFX TO TH ITD HI SE N¥ 

T1 NOTAll "Allt BY Ft B' Il solI 11 

OAT£ Al A SPCF D£l1 OF TH ALTETI 

""IMAR\' 5£LINi;- 

l'ANKS oÑ~ 

Q 

.. 

RN. 

~ 1 ~ 1''36 I ~iTh~~~~,?O '13'" I 

~ 42' 

I 

R.P. PRIMARY 

I: 

I 

l 

0- IA' (! 

, I 

ø 

lI '! -i I 

~ 

f i i ' 

. 

CE o 

27'-6' 

. _-;! 

z: 

~ t6' .i~(i' . 'n~p.l 

-I 

¡:; 

! ! \; I 

= 

I' !. '., 

DWG.M == &7--! 

/. 1 1(T") / .... 

(TYP.) i _ , 

\ 

111:---- --i--- - ----- ----- -f--- -- ~-;;'ON TANIC-;ALLERY--obF -- - - - - T- - - -- - -------~ -- - -- 

. I'll '! i ., r7 ' rlt II!:L 'I 5.5. ¡I. i~.o AIR HEAR i ARRANGMENT 00 'TYPe.:. I TNlK (SEE oiFFU5E.R DRI\ i a.SPRAY ~ GATE SU 'VÆ-VE ~ OPTOR F111 . BOxCTVP)' ITP.,__ HYDR --I ; i ,- ~. ~ 

! II / \1 i l I DET/OL5 ON OWG.II~77 rWATER (np.) 'SEE OE!AIL ON I I- _--!£,_ ____.l. II~~ J l j 

: ..: E.FFLU~T CHEL f- 1~-4l'tT'fl. 'Nci;_ 

¡ \ ~ ~ _ _ _ _ _ J I / L. ¡-'(TYp.) -- ícæt¡i'tr~) lý FI~EL:r,.o ~ ~ ,~i ~ ! L (TY) '-FLOOR ~+~ t \ -1 

~ r- i 1, /! i i . i '. --T"' i ~ ,-, , '1fi!3! ~/I 1 1t,: ''f ! I ,. I . ";, ii1 .rT''c.'COItG 

1 l(t I.~--., tI- f-r~.JiT.. ~~_-.. r- ~~r': .., '-.!' 'R' . --iii,~---.1-=' ~l.:~rRRFr --i!l-i--;. , __1.~. _1.L:.1:l ¡qi~' 

¡ , " i L.I~O'(TYPJ-"'£ r" .11 0Q '-.i . ~ i.. r- co RETl- ¡SLUDG 'i: , ;,~-l .i :, -1= 1i ~ I . ~ . / £_ lT1P.) 

SE D£Th , 32 

..4 

o~ ~ I "I ll~n'æiC:EA1I:CONN. ~ i t l ~ (~,l I 3~" l ~ ~ l"i ~ ~ V DWG æE. ~~~ M-37 ',~ ~,. l ~ 3204A5 i IT . I I ~l / ~ '~-::& ~ r.~ 3 

:iWG M'3'7 I ì! ~ I I- ~ J ~ 320:1AS I' - I- - ì! 3203AS II- i- ~, - ilD SELl' i i- "1 ( 

I I- ,i " s-o .i/GQATINITYP)-- SPRY 13'-010PEIN I I ' - I- - I l, II- \ i- IT r- 5LU GATEI:- - -- .; - ....:; , 

I ' '.. _ i i I I ~~o'..s~ AIR I I '1 I II- -~ itL~s' 

! i -¿~ 4; i EL 45P ii Nlll -. -¿'- . HE.i-~S 'I - I, I (TYR) I EFFLUEII "~1 i I (AJT-3204_C) i i- I 

I II I i -- (T)I I 3~~~ .b" I(TY ,. ,,~ I I c¡~~-32OZ-C:) ~j I (At:-320N . I I TIC'.G"'S(n'p~ 1..- -I I I '6 ,. I ~ t i J. ~ n '" -jf- '" ~:i£ ,. 

I . I ------------ i- - -i 1-.. . t; 

__ - ____________ ". z: ~.. _ 

I ' . . i I ------------ I i z~ ------------ l- 91 nl''c' :i -I 

I~ -:, 

''' ~ . AI'~I- 

_ .--~ __ I i I ;" 

~ (Ãif~ïãi=ë ____ 

I i i--i 

___ .--- I 

, 

i I --- r~E-320-c: 

I I '.A--~03-C)" ~ ~ I ~ i I ~/ ~ , I ;:~ íi 

-~ 

I II ~ 

"0 

¡- f I -~, 

l ~ å1 i -,' ~ ..: ~'?¡ ¡- 

5 

, ~ 

I I ,/ " f I I i ---- --- I "0 ---- --- I õ~ :i: ~ ~ 

. -~-q i I I !!.. I 15211 COutCINc; -- § i 

I _ 1'! ~ i I i( ~PU"G(-r) I I Q ~ tJ!. i I ~~ ~ * I :~+ii"vb I -~ ; 

I 

i I. ! ~) ~ I I I 1C ~IO.T1Pf'C. ,'i ~ J !l-tiR5Et.~ilJg5 z'-" ~ I I I I i~ I ; I l 3~ i lTYP,) II r' ii ~ ~L!, 80: ~ . l - 

I. , 

i 

Ll" I 

"~"5.!l 

I I , ~ I , ~:M~'l~TP. I I 

N 

(IN5TALl- 

I i 

- 

I I "..16HT) .I 

TAN" 

I m in J(ioPOF I 

1 

,,4: I "õi,U i 1 I I~. I i I- I . 

, vi r- = , Ii I ,I, EL17ï: i · . 

, I l- -I I . 

, , ELS N" i I , lo'6lJTeltLY I I .~-4-9C55 

_~; L..! ., i ~ i (TYP.) -1- .. ~ ~ GJ I ~~ I i I-+' 10- I I I' _ ' ':iO~~ V~ALV"(""P.) " . tl I ¡ I.~ i _~ I i I + I .. ~ i - + -'. i - ELbOW . (TTP) . 

-, ; '" I I ' I I ELf 

OW (1'p) ,TYRI , ,. . , I -T~.pe ~ DIFF~""!, 

¡ii" . J.. , Arioiu~EMEt.. (, '(Q) 

i I ~!í I I ~ I I ~ I, iI I ~ b--~ ~12eMO"'i:!;HC I '4'SS f 'iif,~ ~~"-~ - .0' 

FROTH 8 TOTAl HOO ¡ I 

(T') I I i; I ~ 

I PLNKtl I , (TrP) I ¡. I 

~ 

TEE . -I .,1 

(TYP)-. I '- · I 

i I ' . I i"" t I V 

¡' : AERATION i' I TANK NO.3201 ! ! AERATION I TANK NO.3202 AERATION! 1ÄNK NO 3203 L i AERATION II TANK NO,320t .. 1i /-"v:-k1.;~) 

:: :- i J I I ' I I ' I -,,~:i .-F' , 

~~A~AU(T') , s' ;.: 

I - I lh 

NOZZLS I ~I/~ l-SAAY ¡ ¡\~ W"TER .--- 

(5EE. ---- ¡ --- I ~ ---- 

'r=' r" --- =~ 

--- 

i" I ~~ - ~ . 

V'f 

, 

-'.~ 

~ I I -D' ~-~"".-'" Î I I i i ' I ----------- I !- -ri6eiu: i I ¡;. __m_______ I I I i' I I im , - , ~ 

MIXE(T') 20 !; 

¡ TOTAl , i 

¡ 

I ~ ;;! I .. 

i 

t- PL""~ ~ I 

i ~'(Tt?\ I 

, 

C1P.) I I I I . I I~O. 

:! ! ~~ I I - ~ I I 

__ 

I IÁ'-'20.-A) I I i , , . I i 

. lI'~20I-.. - A s-o'. 3-0 OPEII ' ~,-.. 

__ 

~~ 3'0 .~.o 

- 

SUP 

- 

~ _ 

l- 

!i (~ I _~I - ç E-'2ri-.ò) , IIII d"WlGRT1tJITYP) '~ÃË'3203-.ò) I Jj' J~~A'l~~CUICE K~~io4 I ()~ 

..~ 

':S: 

I 

. 

~32010S 

, rrm ii 

(,:I"-~rEf.L 

-:z 

l 

n.Wo;b''" 

"iHlIHÍii 

. i 

I 

!t' 

¡~ 32021)5 

J¿___ "I 

~ 

32030. 

ì! 

' 

! i-.., 

:~E-320-L\) 

ri 

OIITYP.. 

í 

I 

I 

~041l5 

i 

, 32021\~ ,3203&5 l! i ' 32041\5 

~ 3iol&5~ 

~ 

l 

l 

~ 

~ 

g¡ 

¡ =" 

'" 

~ '" 

~ 

l. NO. 

OATE 

.- 

ISSUEO FOR 

~ ~,.~ I 

f , MATCH LIll€. (FOR CCNT. 

DESIED -- 

ORA'i~ 

CHECK ~ 

SECT.CHIEF ~ 


SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

En En & Sc 


498 SENT AVE 'NEWYORNEWYORKl0018 

APVE FO THE CIT OF NEW YOR 

3/32'=1'-0' 

NOTES' 

I.- 6 DEES ,!XED PIPE 5UPPOIn 

a.-cOENOES 5UCE PIPE 5UPPO! 

t . ~iv 

IIIi 

tI, 

10 8 6 4 2 0 11' 

L.W I i=~'~w i 



BUREU OF ENGINEENG, DESI, AN COUC 

RED HOOK WPCP 



P£ 

PREC MAGER MECHANICAL 



1 

- e.;:Fl.VENT 

CHAN"'~ai- 

INV Ei. ~~~ 

SEI! DW. M'~~) 

DATE MAY 2007 

SHEET~OF~ 

P.E. 

CHIEF, DMSION OF fACiiS DESIGN- DWG. NO. RHFSS240

RN, __ 

ci 

i 

~ 

~ 

~ 

~. 

~ 

l 

~tl 

~ 

~ 

~ 

~ o 

m 

, , II 

FROTH HOO (T') ~ ¡ I 

8 TOTAL l' 

BAF WAL (T') 

24 TOTAL 

MIXER (T') 

24 TOTAL 

1 

~ 

-~! ,. 

",I 

~-;~ 

~ 

3DS , 

~I 

" 

~ 

- 

~ 

J 

_ 

I" 

I 

MATCH 

) 

i 

-'?ZON, 

I ';-~OZ'~5- 

L1HE (FO". 

) 

. 

~ 

ccvr. 

" 

J 

' 

':3-1: 

I 

SEe 

~~.~~ 

OWe-.M-52) 

11~i r. I, ~ ( 

i , ~ 

I (¡ 

I ~ . 

I i ~ 

- 

, "I , I - I ( -~~ 

I I I I I I Iii - t " __TVPE i I :~ e OtFFU&ER ~ . . 

, . i I ~ i J ( I~I I DETAIL _ .. 4'-~'~. DW4 M-37) 

I -- I -- I %0 I I~J I ~ ~J '" ltl -" t; ,_~V"' 

i l:i "I ~ I I ILl!! ---- "''':t I !J1 --- ~ OF -' STRT C..NEl 

__ _ EFFUJENT 

I - II 2.o'Cl1P.1 I' a: ------------, ;;~ 14: I T1-E'C'CO~iNe ll:i ~ ---- I (T-lf.) 

--- :r r ,NY. ,. EL 5~~ 

i lo"S.S. AIR. PROC.e.2i Ui..'1I.o0 I 4 rr ~, % COPLl-CHT1P.) 

:riPE 'c" 

I I .om ' I ~Wi)ONSTALi. 

AiR. I I !'Cl I J I Go M~T"'" !j , i ! 

- 

It ~ii i II I 

I 

'iELlcãOO 

I 5.5 - II HEADER AlP 

t . I 4~45' ir' i VIoWD (.TYP.) , 10' o.=Rii.., , h__ I -l I i I i I I ¡- , I 't~j I I 1 , r r- I I 1, r: I~"(TY) I I 1 r I I 

? 

1 

-- - 

i! 

,',I" 

I 

,Ii 

~ 

- 

I 

-- 

I 

II" 

i! 

'11111 

I 

~ 

, 

i I, 

i! 

" ,Iii 

;'E, 

t:~ i 

TLING 

i, " -~~!Õi;~~OFlrfAL 

TAH¡(5 

' I I ii -- - I II I i I l I , iii ---- ------------ I I 'i I ---- i ------------ I I ~el.".oo I i i 

AERATIO I I TANK NO.3401 I, AERATION I I TANK NO.3402 ~III AERATION I I TANK NO.3403 iI AERATION I I TANK NO.3404 ~ 

I i I I~ I I Gill i I II I I ~ 

I II I I :lj'l i i II I ~ 

I I If i I âi l t.~I~I~~rANNEL i I r i I i 3 

1'1" II' i I" III Ii " Jl ii " ! 

I I III II I i 11,1 i II1 I i I i ~ ii, i I I I I i; ~ 

i I r 

I 

I 

III 

iii 

I I ii I I I I :i 

I II ¡ I III WI~ATING(TVP.) I 5'-0" 3'-0'OPNING III I i II' "'AT. I i (T1P.) ~;J~g's::L¿E I I i' i I i. 

I 

i 

~ ~ 

NOE: 

1.- roi NOTES 5EEClG.M-32. 

5l 

~ 

l 

;~c 

WNII 

lIT IS A. VITI Cf SETK 72 CF TH HE 't STAlE 

:i ED1K LAW Fæ lH PE, UN ACT UN Tl 

-: r:~~~~~~~:~. 

-: DlCl CF A UC PRAL ~. TO AllE Jr 

:1 AM WAY Pl, SPCFTI, PllS CI R£ TO ¥H 

g: 1H AllE EH SH Af TO 11 IT tI SE NC 

'l TH NOAT1 "Alli BY f' BY HIS 9GTU TH 

g DAlE AN A SP DE CF TH AlTEll 

~ " 

~ 

~ 

~ 

~ 

~I NO. DATE ISSUED fOR 

DESIGNED ~ 

ORA'i -- 

CHECKED ~ 

SECT.CHIEf ~ 

BY I PROJ.£NGR. ~ 

SCAL 

AS NOTED 

P.E. 

HAEN AN SAWY 

Enme Er & Sc 


498 SENT AVE . NEW YORK, NEW YORK 10018 

APOVE FOR TH CIT OF NEW YOR 

PROCT MA 

P.E. 

P.E, 

CHIEF, OMSIO OF FAClunES OESlGN 

10 B 6 4 2 0 11' 

3/32'=1'-0' L.'; I 



BUREU OF ENGINEERING, DESIG, AN CONSlJON 

RED HOOK WPCP 


ADVANCED TREATMENTTECHNOLOGIES 

:':_""¡.' "'Cl""," ì 

,...,~~ 

MECHANICAL 


TOP PLA - EAST HAF 

KEY PL 


SHE£T~Of~ 

DWG. NO. RHFSS250

I 

i 

I 

i 

I 

i 

I 

i 

, 

I 

I 

i 

I 

i 

I 

i 

~ ~;s 

~ 

~ 

(2 

~ 

"f 

if 

¡¡ 

l 

~ 

~ 

~ 

~ 

~~ 

i¡ 

l 

~ 

~ 

l 

~ 

g 

g~ 

l 

~ 

~ 

¡¡ 

~ 

~ 

t 

;¡ 

l 

~ 

~ 

CD 

s 

:; 

I' 

" 

!¡ 

i. 

! 

;~ 

l 

l 

g~r, 

¡¡ 

E 

~ '" 

l 

?i 

~ 

fi 

~i 

~i 

I 

i 

o 

6B'-6' 

6'-4' 

I 7'-B' I 

"" 

IT IS A 'ill Of SECT 72.2 a: 1H HE 'i STATE 

EDTI LAW ft Nf PE, Ul ACTI lH TH 

OIcn Of A IJSE PR Dl Tt AlTE Ii 

Nl WAY Pl SPT1 Plts OR RE TO \l 

TH 5£ Of A ~Al EN HA 8E AP. F AN 

IT 8E TH SE Of A PRcw EN IS ALn:. 

nl Al.ERING EJ SH AF TO me fl as SE Ni 

nlE HOTATK "AllE BY Ft BY Kl SlTU n£ 

OATE AK A SP DE CI 1l ALlETK 


3/16'=1'-0' 

DESIGNED NB 

ORA\\ NN 

NO~ I DATE I ISSUED FOR I BY I PROJ.ENGR. ~ 

SCALE 

HAEN AN SAWY 

APRO\l FO THE CI OF NEW YORK 

CHECKED NB 

Ennt En & Sc PRECT MA 

SECT.CHIEF ~ 3/16'=1'-0' HA ANO SAWYR. P~C. P~E. 

P.E. 

498 SENT AVE ' NEW YORK NEW YORK 10018 CHEF, OMSIO OF FACES IJ 

P.E. 

~I 

fi 

~i 

o 



BUREU OF ENGINEERING, DESIGN, AN CONSN 

RED HOOK WPCP 



~i 

~I_- 'Y' 

3/16'=1'-0' 

6 

LJU 

4 2 0 s' 

i 

1. ,';L:JÙU¡-,r--- 

¡~ ,,_r---' ._- 

,I . d i X?8"0£ !:.: 

IIL"nr 

jl.=-=.- . ,d '-CG~-- 

¡~ ¡' 1, 

. . ¡ ""~ JL . I 

KEY PLA ~__.. 

OATE MAY 2007 


ARCHITECTURAL 

SHEET~OF~ 

GROUND FLOOR 

DWG. NO. RHFSS260

I 

I 

I 

¡ 

IJ 

t 

é 

l 

~ 

l 

~ 

;f 

? 

1; 

~ 

~ 

~ 

,:' 

~ 

i¡ 

! 

~ 

~ 

~ 

1" 

'f 

i¡l 

~ 

~ 

~ 

~ 

~. 

i¡l 

~ 

~ 

~ 

~ 

~ 

;¡ 

l 

~ 

Ej 

~ 

~ 

.l 

¡¡ 

~ 

~ 

~ 

~ 

i 

Ej 

~ 

l 

g". 

" 

~ 

E ,I ;; 

l 

âi NO. 

~ T T T 

i i 

I 

I I 

i i 

~ .-J . 

i 

1 

, TO CEN TANKS, 

La 5.0 

3' TO AERA llON TANKS, 

CL a 5,0 

3 

2 

.. 

ò 

¡" 

Iii 

III 

III 

IiI 

III 

Ilijl 

III 

III 

~: UP 

IT is A \QTI or SE 72.2 a: ltE NE YC STATE 

EDTI LAW FO Nl PE, U!l AC Uf n£ 

OICT Of A lJ Pf EN 10 AllE IN 

Nl WAY Pl, SPTl PlTS Of RE TO 'i 

n£ SE Of A PRAL DØ HA BE N' F AN 

nn BENG Di SE or A PR ENEE is AlTE, 

n£ AlTE EH SH AfX TO Tl IT HI S£ NI 

TH NOTAl1 'AlTE ir Ft BY tI Sll1 Tl 

DATE lN A 5P 0E or TH ALlET1 

DATE 

il BRO 7.5' EA 

iii no 10.5' EA 

L 

EL I1.B7 

FIBERGLASS 

STAIRS 

I ii!~:i 

6' CONTAINMENT PIPE 

2' FIll IN 4' 

ii"~'"' iLG/LSH 

i ~æm_ i r"~'''~~ 

r CONTAINMENT PIPE 

II I '""j 

.31 "D 

.i 

-l 

". .. 

'" 

, i- 

ISSUED FOR 

DESIGNED ORA\\ ~ 

CHECKED -- 

SECT.CHIEF ~ 


SCALE 

3/16'=1'-0' 

L-FlBERGlSS 

RAIL (rt) 

I ~i 

P.E. 


3/16'=1'-0' 

HAEN AN SAWY 

Ei Enrs & Sc 

HAZEN AN SAWYR. P~C. 

498 SEVNT AVE ' NEW YORK NEW YOR 10018 

J 

T 

~ 

F~ tt 

SRO 6.4' E 

4TO 11.5' 

CONCRETE CURB-SEE 

SlRUCTURAL- 

r-------jI 

I 

l-~ 

u 

~" 

APOVED FO TlE CI OF NEW YO 

PRECT MA 

, , , 

ii'~ 

~lJ 

II 

L~ 

I 

i 

I \l 

CL a x.xx 

L4' EW 6' TO EW CE TANKS, 

HEAT lRAONG CL El 5.74 

P£ 

P~E. 

CHIEF. OMS/ON OF FAClLmES OESIGN- 

~ T T ~ 

~ I 

l TO INLET CHANNa, CL a 5.0 

l CHLORINE CONTACT TANK 

SAMPUNG UNE, CL a 6.0 

-~ 2' TO CHLORINE TANKS, CL EL 5.0 

CL a 5.0 

I 2' FIll j 4' 

COTAIN ENT PIPE (rt) 

2' METING PUMP SUCllON 6' COTAINMENT 

3' lRANSFER FIll 

PIPE 

IN 

(rt) 

3/16'=1'-0' 



BUREAU OF ENGINEERING, DESIGN, AN CONSUCON 

RED HOOK WPCP 



L. I 

6 4 2 0 5' 

~-i'-~'-~QÇ\ r-~ ~r-'- 1 

iDI~ gg8dl.~ 

Ir'~-i 

L--=-_J i I M( ~ V i I 

KEY PLA 

DATE MAY 2007 


MECHANICAL 

SHEET-i OF~ 

GROUND FLOOR 

DWG. NO. RHFSS270

I 

i 

I 

I 

, 

, 

I,, 

I 

I 

, 

I 

, 

I 

I 

, 

I 

2'FlLLIN~ 

4' CONTAINMENT PIPE, 

INV El 34.91 

c 

15'-0' 

o 

18'-6' 

E 

18'-0' 

F G 

13'-3' 14'-0' 

H 

12'-7' 

cp 

, 

I 

, 

i 

I 

l 

g , 

~ 

~ 

I 

l i 

~ 

51 

~ 

l 

~ 

~ 

¡¡ 

5- 

~ 

2 

, 

Ii 

l 

II 

~ 

~ 

¡¡ 

5- 

~ 

i 

"'i 

l 

~ 

¡¡ 

5- 

S 

~ 

~ 

!¡ 

tl 

~ II 

"tt 

W 

tit 

, I LADER CAGE ACCSS (T') 

, 

-i 


50% AlAUNITY 

STORAGE 

TANK NO 

CHB270020 

-$ ~ 

/ '" 

~ 

\ 

PUMP SUCT, 

Q El 7.42 

I r4' ìRANSFR 

/ 

I- 

L- 

-T 

/ 


INV El 34.91 

r3' ìRANSF FILL 

-~-"Î-----:: =3=====1 r -----------"ì, , =====~==~~~~ h-l-? i-' I 

tß -$ 

i J Ii 111111111 III 

111111111 III 

" I i¡ !J! '11'1"11 1.1 1.1 'ti 'I' 

I 111111111 III 

1.1 

111111 III (II 

" / 

111111111 III 

111111111 III lit III III 

ILL lilli' III 

Ili III III III 

111111 Ili III 

111111111 III 

lit III III III 

4" OF ll: ::i n: :ll 

iiriii III IIi 

IIJ 111111 iii 

111111111 III 

111111111 III 

1I11lilli Ili III Ili ill 


I. .l 

T PIPE .~ 

fififiPi.~! 

'l' 

i i I 

'l' 

I 

,¡"I, 

'fl 'ai 

r,l 

iii 

:i: :,: :.: Ii' ~ 

1111111111 I11 

Hlllllllli .!! 

.. 1ì:! 

METR'NG PUMP 

C Ell?Jl 

nA 

~-~ 

I 

l" 

1'-6' 10 

/ 

I 

4'-0' 

, 

ț 

~ ~ 

/13'-10' 

wv 

l' CAlBRATION OVEflOW 

Cl El 35.25 

3' ìRANSFR IN 6' CONTAINMENT PIPE 

2' FlLL IN 4' CONTAINMENT PIPE 

1I 

3' EW, Cl El 20.08 

El 23.50 

Ut4' EW, Cl El 20.67 

4' Fè TO CE TANK 

Cl EL 20.00 2' METERING PUMP DISC 1 ~ -~::::::3!:::::::: 

1:1 

SECTION A 

1/4'=1'-0' B-M 

1'-8' 

~ ~ ~~4~AlNMENT PIPE ~ 

2' METERING PUMP DISC 


Cl El 15.83 

I 

, 

, 


INV El 34.91 

-l3' ìRANSF FILL 

J. 

:, l¡ fe 

i 

Pln 

1° 

~ 

I Cl METING P 

4' EW 

2' RELEf VAVi DlSCHl' 

CAlBRATION UNETI 

~ MP I 

In v Cl El 1295 

~ 

rrl CAUBRATION UNE 2' METERING PUMP SUCT 

¡. 

~ 

4' 

, 

~ 

, 

Cl El 8.87 

4' ìRANSFR PUMP sun' 


2' METERING PUMP SUCT 

Cl El 7.42 

/ 

Cl El 7.2 

LJL. 

I I I ¡ 

'" 

i r I 

~ 

4' OF 

I , / "' 

m' r, r, 

i'i 

I 

4' OF 

~ 

IrT,1 r 

::~/ 

,,,,III 

L-1L I~ (0 i 

-4 

'" 


I r3' ìRANSFR INV El 34.91 FILL 

i , 

I. 

It 

" , , 

, 

-. 

¡.~41 ~", ~A:ON 

H ORITE 

r 

! K NO 

II CH 2600 

~~~~~~~~~f~~~~~~~~~~~ 

,', 

,', 

,', 

,', 

,', 

ili 

m 

-__=d" 

=----11: 

! 

~ 

~ 

ṃ . 

m 

* 

,', 

il 

IIJ 

~ 

2'-7" 

f- 

vr 

l- 

4' VE 

~ Cl EL 34.67 


Cl EL 20.50 

(3)2' METNG PUMP DISCH 

IN 4' CONTAINMENT PIPE EACH 

INV El 19.83 


Cl El 19.50 

l' NoOC IN 3' CONTAINMENT PIPE, 

Cl El 14.87 

I~ ~OP11o;/ARAPET 

(2) l' CHLORINE CONTACT TANK 

EL 9 25 SAMPUNG UNE, Cl El 6.00 

. GRADE 

'~";7 El 7.25 

'1)1' H'iO IN 2' CONTAINMENT PIPE (FAR) 

3)2' EW!H'iO IN 4' CONTAINMENT PIPE 

ICl EL 5.0 

El 200 

:; 

~ 

l 

g. 

~ 

¡¡ 

~ 

l 

g~., 

,; 

;; 

! 

~ 

IT ts A W1Ti Of SECT 72.2 CF TI HE YO STA'T 

EDTl LAW FO AH PE, UN AC lM n£ 

MtC1OH OF A UC PR ENEE, TO AI 1E .. 

lK WAY f' SPCF1l, PlTS æ RETS 10 'l 

TH SE Of A PR El HA 8f AP F AN 

nOl !IG TH SE CF A PR EN IS AllE, 

Tl ALTE £N 9W Af TO Tl IT HI S£ AN 

TH HOTATJ °ALlE BY" Ft BY ll SITU TH 

DATE AH A SPQF D£11 Of TH AlTET1. 

0: 

w.. 

~I NO. DATE ISSUED FOR BY 

DESIGNED -- 

DRA\\ ~ 

CHECKED -- 

SECT.CHIEf ~ 

PRO.LGR. ~ 

SCALE 

1/4'=1'-0' 

P.E. 

HAEN AN SAWY 

Er Enne & Scen 



APVE FOR THE CI OF NEW YOR 

PROECT MA 

P~E. 

CHiEf, OMSION OF FAGIUTES OESIG 

P.E. IlØOI'CllYD~~" it :e'''' 

~ D- =iP# go 

n", 

O/f.,~¡..é¡¡~ 

0+ 



BUREU OF ENGINEENG. DESI, AN COUC 

RED HOOK WPCP 




MECHANICAL 

SECTION 

SHEET 1 

1/4'=1'-0' 

1 

i..LI 

0 1 2 3 7' 

i 

DATE MAY 2007 

SHEET-- OF~ 

DWG. NO. RHFSS280

j 

I 

i 

I 

I 

i 

i 

-i A B c D E F F.1 G H 

170'-0' 

z 

1- 

L 

l 

~ 

l 

~ 

~- 

o 

~ 

l 

;~ 

l 

l 

¡~'" 

~ 

l 

:; 

~ 

8 

~l 

~¡¡ 

i 

~I NO. 

, ~ 

3: 

'" 

~i ' 

"' 

;, 

I 

~ ,- 

20'-0' 14-0' 29'-0' 29'-0' 29'-0' 18'-4' 10'-8' 20'-0' 1. FOR ABBREVIATIONS, SYMBOL AND GEERAl 

NOlES SEE DRA\\NG 2G-PFD-GEN-F01 

c= c= c= c= c= 

/swna-GE 

o 

i 

_~¡wÌ\ ~ i- 

:: 

I 

bb :: 

i ROOM i 4' SII Ell1.50 i 3' i 3' 

L 

o oij ~ 

MCC ROOM i 

1 '''''''''''/= ~D 

~ íV i 3' 

NOTE: 

2. COUPUNGS SHAl BE: 

FIXE X EXANSION (m) 

FlBl, AIR TIGHT (EXE 

AS SHO\\. 

f1 . INDICA lES FIXED rr 

PIPE SUPPORT 

¥ fL 

~ --3:J:_ ==3:~-- 

2'-2'(rr) 

1'-O'(rr) 

v~-- 

~ 

_'ii~ 

o INDICA lES SUDING rrE 

PIPE SUPPORT 

36' DISCARGE Sll£CE (rr) 

-l-~. ~ U "' "" "' 

TO RSP BREAK 

TANK, SEE DWG NO. 

2G-CVL -UTL -C21 __ 

T B\i~ T LJ IT/CONCRET 

am'" 

4' 

, 

'- ;, i i ~If ~ 

-, in 

, 

~ 

i 

~ 

CS-08J113 I / 

"i 

,CS-08Jl11 :: 

l 

~ 

DISCHARGE PIT 

~ 

¡; 

./ 4 

'f 

I 

;, 42' INLE SILENCE (Tl) 

;. 

i 

1 

!; 

~ 

¡¡ 

~ 

~ ~a i 

a i 

. 

-c ~ 

.. ~I 

6 

I I r UNOER ~ ~~ CONTRACT 

l 

~ 

l 

¡j 

~ y¡ 


l 

~ 

"-":) 

I I ~ .. -~ 

~ 

fH 

'flf 

P - - 42' ~=~ - 24' UP TO OISCHARGE BLOWER (Tl) (Tl) 396100 FE 

3' SII UP (Tl) .: Ë 

36' 

396100 

BLOWER COONG 

WATE SYSlEM 

FOR INSTRUMENTATION 

SE owe. 2G-1 & C-BLW-IO 

I 24' 'I BLOW-Off A 10'-7' W-M 7'-0' (Tl) SEE (Tl) 2P Fl-3901oo PLUMBING 

(Tl) 

8 6 4 2 0 8' 

1/8'=1'-0' L-.. I 

- 

/:'1:r"_J r -(3 

i:r-"-fr-i --i 2Qqg~'9 -i 

!¡ , J v-v~r , 

IT is A W1TK Of SE 72.2 Of Tl NE 'l STATE 

EDno lAW f' Ni PE. UlU AC Ul TH 

DICT Of A. 1J ~ EN 10 ALTE ii 

Ni WAY Pl, SPTI Plts OR R£ TO Mi 

TH SE Of A. PRH. EN HA BE N" F AN 

I1 8E Tl£ S£ Of A f' EN lS ALTE, 

TH AlTE ENEI SH AF TO Tl I1 HI SE JH 

TH NOA"n "ALTE BY F' BY ll SGTU TH 

OAT£ AN A SP DETK Of nl AL1ëTI 

DAlE 

ISSED FOR 

DESIGNED ~ 

DRA\\~ 

CHECK -- 

SECT.CHIEF ~ 

BY I PROJ.ENGR~ ~ 

SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

En En & Sc 

HAN AND SAWYR. P~C. 

49 SEVNT AVE ' NEW YOR. NE YORK 10018 

APOVE FO THE CI OF NEW YOR 

PROJEC MAGER 

P.E. 

P.E. 

CHIEF, DIVIIO OF FACIlS DESIGN 



BUREU OF ENGINEERNG, DESIGN, AN CONS 

RED HOOK WPCP 




MECHANICAL 

GROUND FLOOR 

DETAIL PLAN 

" '-,,--, ,.1' I 

¡ir i' i ~ i ( -- I 

".,__~-- .-----.A~. -, , 

II 

1.. KEY 

'. 

PLA 

=UL_~ 

DATE MAY 2007 

SHEET~ OF~ 

DWG. NO. RHFSS290

I 

1 

I 

I 

I 

1 

II 

I 

i 

I 

A B c D I 

~ ~ 

170'-0' 

F.1 

G 

H 

z 

~. 

~ 

g 

~ 

~ 

l 

~"II 

~ 

~ 

~ 

~ 

l 

~tl 

2' 

~ 

'" 

.i 

~ 

~ 

i 2 -~ 

l 

i2 

~ 

l 

tl 

2' 

~ 

i" 

l 

~ 

~ 

~ 

~ 

'1 

l~ 

ï, 

tl 

2' 

~ 

t 

i 

~æ 

./ 

D-1 

1 

1: 1 

IÕ 1 

'" 1 

~ 

0 

:; ~ 

~ ~I~ ,_ 

1: 1 

~ 

~ 

I 

~lÆ 

-- 

---UH 

----IH 

'ic--i 

5 Ì- ___ ,H _ 

~I 

BL 

6 J ' , 

~~ 

T1 

I 

I 

20'-0' 14'-0' 29'-0' 

~ 

80110Tcp~3OTcp~~ 

LCP-080120 LCP-080140 F 

~ 

29'-0' 

t-" 

it- ~ if 

ACS-02 .. L 

COTROL ROOM ~ 

UPS-BLW-051 ~ 

ON I 1 I 1 I II IIIIIIII UPS-BLW-OSO 

SECURITY HARDWARE REMOTE I/O 

NEMA 12 ENO-OSURE ~110 REMOTE I/O 

, fllllll ~ _'00 J ;, -:'~ 

----LT/CONCRTE 

EL 29.50 L 

29'-0' 

IDDDDDI 

II 

MCC ROOM 

drlI 

REMOTE I/O REMOTE I/O 

':lM~='~~ 

HVAC ROOM 

f\ b °bn 

---t-- 

i 

i 

I 

r----------i 

I 

i: 

11 

1 

: HRU 

1 

11I,11I1 

1 089010 

¡ l REMOTE I/O 

1__J W I 

: FLOO MOUNTED 

H--- ___ LCS-~l1 

I "J 

.. 

PREFLTE!(TY)~ 

086010 

-02 

I PDlSH 

-- 

PROCSS AIR FlLTERS (TY.' 

INSTRUMENTATION SHOv. 

ONE m TE SYSTEM 

FOR OTHER FILTE SE 

DWG. 2G-1 ol C-BLW-IOl 

~W-M 

BLW080330 

7'-0' 

(TY) 

*5' 

BLW08Dn n 

RI~ 

,,,1-- 

H 1 

-- 

T 

i 

( I~ 

n 

18'-4' 

-- - -~'J 

UPPER BLOWE ROOM 

BLW002~ "i 

FLOOR MOUNTED = 

LCS-Q8031 ~ BLOWER 

REMOTE I/O BL W0140 

089030 

riA 

~~ 

h 

iI 

( ,,~ 

~U! 

lAIR INJE \ 

:¡ r)J 

c' "' r 

"" 

~~ ~I 

'" , 

IL1L 

"'.'T ~~ ~ (~) 

10'-S' 

I 

I 

L i- 

~lt 

BLW0802~ ~ n 

~ 

Lm 

-T1 

~ 

20'-0' 

STORAGE 

E 

i- 

i.1If--- 

îbHUI--- 

rrHIl--- 

H -- 

NOlI: 

SW TO OIL COO (TY) 

S\ (TY) 

LUBE OIL SYSTE (TYl 

SE DWG. 2G-1 ol C-BL'Ñ-103 

FOR INSTRUMENTATION, 

24' DISCARGE (TY) 

42' INLE (TY) 

H 

~ 

-- 

E 15 TON BRIDGE CRANE 

filll--- 

T 

1 

I 

SE DWG. 2G-1 ol C-BLW-102 

FOR INSTRUMENTATION. 

(TY) 

1/8'=1'-0' 

8 6 4 2 

~ 

0 

1 

8' 

~ 

! 

l 

~ 

l 

¡;i 

'" 

~ 

~ .. 

~ 

~I NO. 

.. 

IT IS A i.T1 OF st 72.2 CS Tl NE 'r STATE 

EDTI LAW FO Nl PE, UN AC UM TH 

~ OF A lISE PR EH. TO ALTE .. 

AN WAY PU, SfTK PlTS OR R£ TO 'M 

T1 SE Of A. f'AL ENEE HA El AP. F ~ 

rI 8E TH SE OF A PR El IS AlTI, 

nl ALlE Dl Sl NF TO TH rI HI SE Nf 

1H NOTAl) 'ALlE IJ Fa BY Hl SITU Tt 

DATE AN A 9' DEnc OF TI AllETK 

DATE ISSED FOR 

DESIGNED ~ 

DRAv.~ 

CHECKED -- 

SECT.CHIEF ~ 


HAN AN SAME 

En Enrs & Sc 

SECOND FLOOR PLAN 

SCALE APOVE FOR TH CIT OF NEW YOR 


AS NOTED 

P.E. 



PRECT MA 

P£ 

P£ 

CHIEF, DMSIO OF FAciES OESIGN-OU 


BUREU OF ENGINEERING, DEIGN, AN CONSUC 

RED HOOK WPCP 




MECHANICAL 

SECOND FLOOR 

DETAIL PLAN 

L ,-¡-f7V--.-.r-----i 

..r-~ - -- "vOO ~ 

J i L ~ j 8.8.J'1"rlF9-' 

¡rr_-ll~ 

" ç;' ~ 

KEY PLA 

DATE MAY 2007 

SHEET -- Of~ 

DWG. NO. RHFSS300

I 

I 

i 

, 

i 

I 

l 

I 

I 

i 

I 

i 

, 

I 

i 

i 

i 

I 

I 

i 

I 

i 

i 

I 

l 

I 

I 

i 

I 

TOP Of ROO 

EL 57.83 

TOP Of ROO 

EL 47.50 

TOP Of 5LB 

EL 29.50 

8' 

~ 

l 

~ 

l 

~ 

~ 

l i 

i¡ 

ḷ , 

¡¡ 

l i TOP Of "'AT 

EL 11.50 

ī¡ 

~~'N," ' 

l 

~ 

~ 

r 

~ 

o 

~ 

l 

~Š:I 

IT IS A WlTI CF SE no.i a TH NE YO STATE 

l ==~~~~~EN~~~IN 

Q Nf WAY Pl, SPna PlTS OR RETS TO \l 

~ Tl S£ OF A PRAL Dl HA BE .l F N4 

.: nD BENG THE SE Of A F' £H IS ALlE. 

m TI ALTE EN 5H N' TO T1 IT tI SE Nl 

m 1) NOTATK "AtTE BY f' BY I4 SITU, me 

§ DAlE lK It SP D£ CF mE AI lE Tl 

". 

" 

~ 

.. 

L. 

~ .. 

i. NO. DATE ISS FOR 

~ 

9i 

~i 

~ ~ 

NOTE: 

. INDICATES FIXE T' 

PIPE SUPPORT 

o INDICATES SUOING T'E 

PIPE SUPPORT 

f- T 

1+ 

f. 

L. 

/-7/Y 

r~~ v~ v\" ' 

SWITCHGER 

15 TON BRIDG CRNE 

1 1 

MCC ROOM I I 

L. 

o 

36' 

~ 

I 

i 

0 

~ 

Cl 22,50 

Cl 21.50 

DISCHARGE 

Cl15.17 

1+ 

UPPER 

BLO\\ 

ROOM 

36'x24' REUCER 

I 

i 

L. L. L. 

J 

IÖ' biSCHARGE Jl 

~lECER (T') 

L. 

I II 

i 1 1 

li 

1 

~ I 

.. , 

IJ 

11 II I II ~ 

BLOII 

BLWOB0130 

(NOTE 1)i- 

-= 

Eh 

~ 

1 

I~~ 

-+ 

~.~~r--- 

~~ 

42' LR 90' - 

BENO (T') 

P 

I 

! 

$-- 

J5 

-lHT 

o 

L. 

1J -1 

1- 

r--- - I 

,r-_L. 'L~--= ==~:JÍì I -i . . I i 

I i 

o 

~ 

'lI 

I 

8& 

W 

L 42' 

Ld 

INLET 1 

L. 

SILENCE (T') 

SECTION G 36' OISHHARGE 

i - 

o o o 

L. 

I- 

~itl 

1/~~' I 

V'~~ 

-L 

i 

TOP Of CRA 

EL 48.83 

T =1- 

. 

. 

"ttr~1 

rm~ID 

i 

11~24'B' Cl 23.17 

i 

'l II tl~ I hCl21.B3 n' ,m 

L. 

EXPANSION 

JOINT (T') 

~ 

~\.)/l 

AIR ~ 

PLEUM 

Lc 

L. 

60' AIR HEAOER 

Cl15.17 

";~\.'Y" ' 

l 

OF 

E RAIL 

1/4'=1'-0' 

DESIGNED ~ 

DRA\\~ 

æECIED -- 

SECT.æIEF ~ 

BY i PROJ.ENGR. ~ 

SCALE 

AS NOTED 

P.E~ 

HAN AN SA\W 

En En & Sc 


49SENTAVE' NEW YOR NEW YORK 10018 

APVEO FOR THE CIT OF NEWYOR 

PRCT MA 

P.E 

P.E. 

CHIEF. OMSIO OF FACIUS OESIGN 



BURE OF ENGINEEING. DESIN, AN COUCN 

RED HOOK WPCP 




MECHANICAL 

SECTION 

10123 

i..-UW 

7' 

i 


SHEET~Of~ 

oWG. NO. RHFSS310


DENITRIFICATION 

Denitficaion Filtrs PlT INFLUENT PRIMARY SETING TANK INFLUENT PRIMARY SENG TANK GRA\ITY THICKENER AEATION TANK AEATION TANK FINAL SENG FINAL SENG TANK FILTE INFLUENT 

EfUENT O~RFLOW 

CENTRATE RAS WAS 

~~TR~~~T I PLAT EfUENT 


INFLUENT EfUENT TAN INFLUENT EFFLUENT 

FLOW (MGO) 329 36.2 34.9 4.5 0.1 34.2 0.7 39.5 73.7 73.7 39 39 39 39 

TS (mg/L 199 181 11 150 186 5,271 5,271 116 2,502 2,502 13.3 13.3 4.0 4 

TS (ibid) 54,700 54,700 32,400 5,700 180 1,502,700 31,200 38,280 1,53,100 1,538,100 4,300 4,30 1,300 1,30 

CBOo (mgjL) 142 129 111 68 65 1,915 1,915 106 910 910 12.5 12,5 4.0 4 

æoo (ibid) 39,000 39,00 32,40 2,600 63 54,000 11,300 35,063 559,300 559,300 4,00 4,00 1,300 1,30 

TN (mg/L 31.7 28.8 26.5 25.0 547 354 354 27.7 171 171 6.7 6.7 5.0 5 

TN (ibid) 8,700 8,700 7,700 900 530 100,800 2,100 9,130 105,100 105,100 2,200 2,200 1,600 1,600 

PLAT 

INFLUENT 

MECHANIC 

BAR 

SCREES 

(4) 

SCREENINGS 

TRUCKED 

,,' 

"" 

""'' 

I MAIN SEWAGE 

I PUMPS (6) 

I 

I 

! 

I 

I 

PRIMARY 

SETING 

TANKS 

(4) 

ï-'- 

I 

I 

I 

I 

I 

PRIMARY 

SLUDGE PUMPS 

(6) 

SECONDARY 

BY-PASS 

FINAL 

SETING 

TANKS 

(8) 

CHLORINE 

CONTACT TANKS 

(2) 

~ 

~l 

~ 

l 

~ 

~ i¡ 

~ 

~ 

~ 

êl 

~ 

~ 

~ 

l 

¡~'" 

.. 

IT IS A i.TI a" SE 72 CF THE NE '\ STATE 

EDTI LAW FO Nl PE. UHl AC UH n£ 

DI Of A. lJ PR ENHE, TO AlTE IN 

Nl WAY ~. SPCl1l, PLTS OR RE 10 'I 

TH SE OF A PRAl EH HA Ba AP. IF AN 

fl BENG TH SE CF A PR EHEE IS AI TE, 

TH AL1I EH SH Af 10 TH na HI SE N¥ 

1) HOTAno "ALn: øv FC BY HI SllV, TH 

OATE AN A SP DETI N¡ TH AllETl 

I I 

T 

i 

I -----T-- L.___ 

l i l I T 

-~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~---j 

-------.. I I 

(2) 

(2) 

SLUDGE CAKE 

DISPOSAL 

.l '" 

~ .. 

¡: I NO. DATE ISSED FOR 

BY 

DESIGNED ~ 

DRA\\~ 

CHECKED ~ 

SECT.CHIEF ~ 

PROJENGR. -l 

SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Ei EnIS & Sc 

HA AN SAWYR, P~C. 

49 SEVNT AVE . NEWYDRK NEW YOR 10018 

APPROVED FOR THE CI OF NEW YOR CIT OF NEW YOR 


PRECT MAR 

P,E. 

P.E. 

CHIEF, oMSIO OF FAcaES oESIGN 

BUREAU OF ENGINEERING, DESIGN, AN COSTUC 

RED HOOK WPCP 



FULL STEP BNR & DENITRIFICATION FILTERS 

FLOW DIAGRAM 

MASS BALNCE 

DATE 

MA Y 2007 

SHEET~OF~ 

DWG. NO. RHFSD340

I 

I 

~ 

!; 

~ ~ 

~ 

l 

~ 

B 

i' 

7 

l 

~ 

el 

~ 

!i: 

i¡ 

~ o 

~ 

ii 

Ii 

l Ii 

~ 

~ 

el 

:¡ 

l 

g;i 

" 

~ 

! '" 

~ 

WAR'" 

IT IS A. WlT1 Of S£ 72.. Of 1) NEW Yæ STA.TE 

EDlK LAW Ft li PE, UH AC lM Tl 

OION Of '" I. PRAl ~EE ro N.Tm ~ 

AN WAY Pl SÆlK PllS al RETS 10 vt 

Tl 

rm 

SE 

ll TH 

(: A 

SE 

PR 

Of 

EH 

A 

HA 

PR 

BE 

EN 

AP 

IS Al1E, 

F AM 

11 ALlE EN 5H AF 10 1) IT l- SE ~ 

TH NOAT1 'AllE ~ fU BY HI SlTU Tl 

DAl! AM A SP Cl Of lH AlTETI. 

~ NO. DAlE ISSUED FOR 

Woo.DO 

BY 

~z. 

NEW CHEMICAL HANDUNG BUILDING 

\ 

- -- - 

EXISTING BARGE SUP ~ 

GALLRY 

~ 

C: 

EXISTING 

PRIMARY SETING 

TANKS 

EXISTING 

MAIN BUILDING 

Ii 

ii 

'i 

it 

¡¡ 

~ 

T w 

i 

i 

L 

FOOllRINT FOR NEW 

DENITRIFICATION FILlERS 

LJ 

i 

I 

Q 

EXISTING 


TANK 

LJ 

i 

BLDG. 258 

1'=30'-0' 

30 

1_1... 

15 0 3D' 

I 

DESIGNED -- 

DRA~ ~ 

CHECK -- 

SECT.CHIEF ~ 

SCAl APOVE FO TH Cf OF NEW YOR 

DAlE MAY 2007 

AS NOTED 

HAEN AN SAWY 

Ei En & Så 

HA AND SAWYR, P.C. 

498 SE AVE . NEW YOR NEW YORK 10018 

PROJCT MAGER 

P.E. 

P.E. 

CHIEF. DMIO OF FACiuES DESf 

CIl OF NEW YORK 


BUREU OF ENINEERNG. DESIG. AN CONSN 

RED HOOK WPCP 



P.E. 

DWG. NO. 

PROJ.ENGR ~ 

RHFSD350 

CIVIL 



SHEET~ OF~

í 

I 

I 

I 

l 

vi 

l 

~ 

~ 

~ 

~ 

'f 

~ 

~ 

~ 

l 

~ 

't 

l 

;~ß~~ 

of 

Ii 

g 

~ 

~ 

ß ~~ 

~ 

j 

~ 

ß ~~ 

i 

;: 

" l 

i 

5~~"' 

i¡ 

~ 

~ 

êl 

¡; 

~ 

~ 

l 

l 

~;i 

~ 

~ 

E 

~ 

ài NO. DAlE ISS FOR 

,z 

IT IS A WlT1 a: S£ 72.2 Cf TH NE YO STATE 

EDTI LAW FO N( PE, UtU AC Ul ll 

OlOfAl.PROFDfTOAlTEIN 

~y WAY Pl, Sfll PLts OR RETS TO lH 

1l SE c: A PRAL EN HA fl AP F AN 

im El TH SE OF A f' EN IS AlTE, 

1l AlTE aQ SH AfX TO 1H lT lt SE Nl 

Tl NOAlI "ALTE BY ft BY tI SlTU TH 

DATE JH It SPaF OETl Of TH ALTET1. 

~ " 

.. 

BY 

EXISTING 

SLUDGE STORAGE 

AND 


-------- ______-i 

EXISTING 

CHLORINA TION 

BLDG. 

EXISTING 


TANK 

o 

aoN 

Z 

DESIGNED -- 

ORA\\ -- 

CHECK ~ 

SECT.CHIEF ~ 

PROJ.ENGR ~ 

SCALE APPROVED FO TH CrT OF NEW YOR 


AS NOTED 

P.E. 

HAEN AN SA\W 

En En & Sc 


498SENTAVE. NEWYDRNEWYOR10018 

PROJECT MAGER 

P.E. 

P.E. 

CHIEF. DMSION OF FAClLmES DESIGN- 


BURE OF ENGINEERING. DESIGN, AN COlRUCN 

RED HOOK WPCP 



NEW DENITRIACA nON ALlES 

29'Ø PER ALlE 

6' ALlE DEPlH 

SCOURGE AIR BLOI' AND WA lER 

BACKWASH PU~P BUILDING 

20 I .. 10 .. 0 20' I 

1'=20'-0' 

~ ¡ ..-'--~~ .-' 

--J" ~ '700Cj ~..i 

. , . ! II L. i!l i 

~~'¡L___..._._,_.. 

KEY PLA 

i~-i LJ L. - &88.grf----j ~cs7 L-1 

!l I ----i/': ! '. ¡ i 

CIVIL 


DATE MAY 2007 

SHEET~ OF~ 

DWG. ND. RHFSD360

! 

I 

0.ti. 

l-t\...l AR'ISELINi;-" j: 

TANKS g -~e' 

Ñ 11-G' 

.. z: 

i- 

N !l0t. 

; 

i 

i 

~'ij 

r-! 

NO 

z7'-6' 

i TYP.) 

tC 'Y ~ fi 

"~, 

\! T ~ 42' Ð-T;~~~~ ReP. 

I ,~" 

PRIMARV i:~~,~,i;o I 

in 

r. ~ 

i I I I l. i I I r: l 

'1 I I I 

o ø 

I. r------+-----~---~-- ------ -------¡------l------.:------------ 

'i AERATION TANKS GALLERY ROOF 

~ i \ i / ,or I 1 iL I DETÄLS EL '''.0 ON ARRANGMENT DWG. ",~77 (SEE WArEIl i a'SPRAY (TYP.) VAJVE i SEDWGE BDX(TYP) CJ!Al!~L Ot- ~_~~~_ ___, 

__~~ (;'(TYP.) r- FL"'EL:7..O~ _! lTJ 

! '" i. I (TYP) 

I M . 'l,: i 5.5. AIR HEAR I TYP ~ DIFFUSER I EL,ID.OO I ~~ =~ 

,J" EFFLUENT ClNEL r~'-4 'CTVPI. rTV'CCc 

P.N. 

i 

~ 

~ 

~ 

¡¡ 

~ 

~ 

~ 

;¡ 

l 

~ 

¡¡ 

o !I 

ii 

;; 

¡¡ 

~ 

6l 

l l 

¡=" 

" 

.. 

FROTH HOOD (TY) 

8 TOTAL 

IT IS A 'iTK Of SE 72.2 Of TH NE YO STATE 

EDTI LAW FO NN PE, Ul AC lJ n£ 

Dlcn Of A UC PR EHNE, TO ALlr fi 

N( WAY PI. SPCI1K PllS OR RETS TO 'M 

n£ SE Of A f'Al EH HA BE AP F ~ 

rn eE TH SE Of A PR ENEE IS AI TE, 

TH AL~ ai SH Ii TO TH ITD l- SE NC 

TH NOTATI "ALTE BY F' BY tiS SllL ll 

DAlE AN A SÆ D£Tl Of TH AllETI 

~ 

l 

~ 

l. NO. DATE ISSED FOR 

¡ I i 

i - 

&E Dcï'L ON 

jJ..~~ 

~~" . i 

I I' 

· ' 

i 

I 

! : 

BAF WAU (TY) 

28 TOTAL 

~.: .-..~ 

~; 

.~ 

; 4i~ 

MIXER (TY) 

20 TOTAL 

~ 

¡¡ 

¡¡ 

i: i¡ 

"~rll,!~i¡n i!~~~ ,~~~ I¡¡¡ I! ",.~ 

i 1.-8 0' I 4SP 0 'n . llZl I I 'l-& HE.N)~S lo'S5.AIR EFF (TY?) ua 

I l I 

- I I I ---- --- I ~ 

I (T " 3;.'l~f" ~ .___________ I ,1-_ --I .___________ I TICO':HS (7-rP) . . ,I ---- --- I ------------ ¡: I 

~II I I i -i . I i ¥l I ~9 

- - - ii i ------------ 

-===_____===_ 

I 

i '1'-' I 

i: 

( 

i 

I 

I 

------------ "I 

i COuPLI"'" 3e "I 

I 

l- 

(TYP.) 

---- 

5 

~ 

--- 

I TVpe'C' 

I 

i 

gi 

__ 

I ~ 

f11' I i I I AiR i i FLow i lrE.TE~ i I. I :T'fP) ¿. ì! I - I ~ I r OF I i 4: 5T'UT I -,--- 

"'~" 'I I i I I (1"57""'- uPR'5HT) I :rPOF I I I 

~4~45' ~ ;. J I TAN. 

Eis i: = I I I II I I ELn.5O I I 4' 9O'S5 

(TYP.) ,,"' ~: -+ i I i ,I I .(: - ~ I' i , - -~- - E~bOlV (TVP) 

. t " li i ii I ") 10' ELf'oW - .,o's. I (TYP' M~"N.ÚiEr,E'.: I I. 1 ! i. I I -nPE 'r: (i DIFFo/seR o(~) 

.. 

"i '" 

i I ~ ~ I i 

~ 

I 

1-- ¡. 

r2MOA-ue '~-I I 

C;KC 

- I" 

~ TEE ~. 

4' 

PLNK~ 

~~ 

I 

(SE£ 

(TVP) 

(Tl') 

I 

D£ TA'_ 

I , 'i~. 

ON """ 

. 

.. ',.? 

i i i I I. - -: I ~-~'Ilo/TTERFL' 

I ' i I 1 I: 

TANK 

I ¡ 

NO.3201 

I i 

! AERATION 

I I ' TA~.K 

~I I 

NO.3202 AERATION' 

I =1 ' 

mNK NO 3203 i I '" , 

l AERATION 

".' i:ANK 

~.~.. 

NO.3Z0T ~ VAl~lTVP) 

I -- I i I -' ,. HEADeR 

i I I 

i I -===_____===_ ~ 

I 

i -- 

I 

--- 

------------ 

I i ~ I ---- i --- i --- I 

I 

~ -: I/;I I 

b 

I i I QEM.60LE COI. I, 

. 

I i I PL:i CTP.) I I I I~O' -- 

r - 

i ¡ i, I i I 

I i 

!:r-FLUENTCHANIt.r.L 

, i I 

I 

I 

s-o'd-DOPING 

I ~04DS 

I I I I 

IIG1T'NG ITYP¡ 

I I ,i I I , I ''IV Et ~~~ 

· l- - - I I -- MATCH - I - L1!\f. SEi: DW. (F~ M-~!) CONT. 

DESIED 

DRAVr 

!! 

NN 

NB 

O1ECKED 

SEcr.01IEF ~ 


v-4' SP'f 

,~ He 

t EL ri"" 

~~ 

SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Er En & Sd 


498 SEV/' AVE " NEW YORK NEW YOR 10018 

=- .. 

1 

~i 

NOTES' 

C I." AOCES FillED PIPE SUPPO 

!o-3£ a."cOENOE& ll1CE PIPE SUPP 

3/32'=1'-0' 

10 8 6 4 2 0 11' 

i.W I 



aUREU OF ENGINEEING. DESIGN, AN COON 

RED HOOK WPCP 



r-, ""O'-"~"¡Jr.", I 

I :~~ i 

APOVE FOR TlE CI OF NEW YORK 


P.E. 

PRECT MAER MECHANICAL 

SHEET~OF~ 

P.E 


TOP PLAN - WEST HALF 

CHIE. DM OF FAciES OESIGN DWG. NO. RHFSD361

05- 

~ 

;l 

~ 

~ 

~ 

~' 

:0 

l 

~ 

8 5- 

S 

~ 

o !i 

ß 

FROTH HOl (T') 

8 TOTAL 

BAF WAU (T') 

24 TOTAL 

MIXER (T') 

24 TOTAL 

J, 

'" -- __ _ MATCH 

305 , 

LINt; 

,,/ 

(FO" 

"4.4D5 

cr.", 

, 

SEe 

I J 

OWG.M-32) 

. I ~ ~I i I ~ i . I ~ ~AI-~2r-e,~ I 1l-32f, ~ i I '(Ai;Y-e.) I ~ I 

p.N. 

) ) ) ~ J 

'1111 

I (, ~ 

I 

~ i ( I REHOYA&E 

II 

I FUNK&(TfP.l 

I 

CO. 

i 

~ (¡ ii ~ .1 (, 

~GQ""TINGtTY?' I I I 'i i I - 

",," 5PY 

WATER i-!!ER 

to EL 17.00 

'l t 

-;i¡ 

1 

41.,i; 

DIA'N 

PlCH 

~ 

i 

, I , 

II 

~11t: 

c'" I L.1!f\ 

-Ji r~ 

!l 

III I II "I i I II r J i " r I I ~ :~ ---- ~ TYPE "RRAlMENT 'e: ~FFU$ER 

I . i ~ I I ( -S I DETAIL L~I _ DWG. ~ 4'.~'~. "'.-37) (sa 

~"I 

i 

I -- 

1 

I , I 

I 

~~ 

~ .___________ 

---- --- 

ltl 

1::1 

_9 ~ 

.. 

ELI3(TYP.' 

1 o~ I~I \OF5TRT __~~T _ "c " 

~II I ' II i 210'tt"P.1 . i . I ~ ------------ i loHs.s.PRoc.=-$ h I "'iu I Õ I Z T1PE.'~S~l'1Nß 1-1 IN' 

(t 2 :r"'Æ'e" 

EL 5~~ . 

I I ..,.. ~..i..'1'.oO I ;; I ~ I CQPLIlc:lTP.) 

u: i/I: ¡ '! I i ",' i I (T~f.1QN$T"Ll TYP. I - - I i V~"HT) 

.... I ~ FLOW I -~ M!.T.... 

~ 'ž ¡: I I I 

I Iii' (1, - 00; 'ieL~ - 5.5 i-E:A ltO AiÇ' Dei: 00 

:z IH -; I t" I I I VALVa ~~ - - 'TYP.) -- I . t- I I 

L .~.s' ~ ;; ~ i ~ 10' I ""6R~i."I I I I i I I tT~ ?i ~ I I 1, r I I 1 i: 1~i;'(TY) I I 1 r I i 

T' ¡ ¡',I i! "Ill I I II 'i I " i!' ' I,!! 1,1 'i! ~= ---- i I I, i '" I ¡i! i! III = ~iUt.~8 i I '" -,;ii,~so""" 

--- TAN"-5 

i, I I iii ------------ I 'i ------------ I I i ~ t 

AERATION I I TANK NO.3401 II AERATIO I I TANK NO,3402 llil AERATION I I TANK NO.3403 Ii : AERATION I I TANK NO.3404 ~ 

I I I~ I I t,¡ II I 1 IIi I I ~ 

I I I1I 1/1, I I I i I i i I. ¡ !~ i. III ' I I I ~ ~ 

II" I 

il, 

I, 

i 

i 

I 

I 

~ 

:Ijl 

i I ¡ 

i 

i 

i 

"iil 

i III 

¡.¡ 

I 

" g 

~ 

I I i t I I ~I l ~li~';~f"ANNEL I I I r i I ! 3 

I I iil I i I I I ¡ii I I ~ 

I i'i I I S'-O"3'-O'OPENING I I i I ~;~!gs!5,¿i; III i I i. 

i III i I 3'O~CS III I I W/GR..TIlGtTYP. III ~~:320-e) I I I ....TE. (T~P.l I 34'4C& 

I I i'l L.________-. \ I I \ DO ~ _______.. ill' -~-e- 

I I _ I I 

i 

. L_______--L-iL-_______..T 

II I L . 

---,; -:- - _-iL-iLii 

-----..:l 

L L_"'__ 

1-TOPOF TAl"i(S 

____ 

4'ORAIri IN AL.L. B 

VALVE: COMPARTMeNT5) C 

(T'PICAL. ~ ~ ~'~Ô~3 . . 

EL.1750-- 

"'~ 11-:i; 

NOE' 

1.- ~oi NOTES SEE D'.M-3Z. 

- 

¡¡ 

é1 

l 

~ 

~ 

81 a: IT EDTI IS A LAW W1TK fC Of JN SE 7201U PE, UM (S ACT tH NE UM 'I TH STATE 

OICT Of A uc PRAL EN TO ALlE fo 

~ Nf WAY Pl, SÆT1 Plts OR RETS TO 'M 

-: ;r~~~~=l~~, 

~ Tl AlTE DI SH AF TO 1H m: ll ~ AH 

'f 1H NOTATI 'AlTE W Ft BY Ht !DTU TH 

8 DATE AN A Sf OETI a" Tl AlmlTI 

~ " 

~ 

! 

;; 

"- 

~I NO. OAlE ISSED FOR 

DESIGNED -- 

ORA \\ -- 

CHECK -- 

SEClCHIEF ~ 


SCALE 

AS NOTED 

P~E. 

HAN AN SAMER 

Envime Enine & Sc 


498 SENT AVE ' NEW YORK NEW YORK 10018 

3/32'=1'-0' 

APOVE FOR TH CI OF NEW YOR CIT OF NEW YORK 


PROECT MAGE 

P~E~ 

P.E, 

CHIEF. OlSION OF FAClU1ES DESlG/ 

BUREU OF ENGINEEING. DESIGN. AN CONSUCN 

RED HOOK WPCP 



1?_~ ~ 1 ~ ? 1r 

IbiJ-lJ .~ 

~ UY~ 

~f!. 

c-oev",'7 ,'~" ~£. 1'''OI'aM¡O 1 

MECHANICAL 


TOP PLA - EAST HALF 

OATE MAY 2007 

SHEET~ OF~ 

OWG. NO. RHFSD362

I 

I 

i 

I 

i 

I 

i 

~. 

~ 

~ 

~ 

~ 

'1 

~ 

ïl 

~ 

~ 

~ 

~ 

1 

~ 

ïl 

~ 

~ 

fl 

5 

~ 

l 

ï 

l 

II 

~ 

~ 

fl 

~ 

¡¡ 

~ 

~ 

i 

~~ 

~ 

~ ü 

~ 

¡¡ 

l 

51 

~ 

~ 

~ 

l 

g~" 

~ 

~i 

~i 

~I 

~i 

?i 

I 

i 

cp 

i 

I 

i 

cp 

i 

I 

i 

cp 

i 

I 

i 

, 

I 

cp 

i 

I 

i 

o 

UP 

!8RC 7.5' EA 

7TO 10.5 EA 

CD 

~I__ T" 

CD 

68'-6' 

I 7'-8' I 

3/16'=1'-0' 

~i. I 6 4 2 0 5' 

l '" 

L 81 NO. 

(0 

.. 

lT IS A IAll (J SE 12.2 Of lH NE 'r STATE 

EDTI LAW fO Ni P£, lH ACTI UN TI 

DI (J A IJ PR DØ TO ALTE t. 

Nf WAY Pl SPTI, PLn; OR RE TO 'M 

Tl SE Of A PRN. El HA BE N'. IF Ni 

Il BE TH SE OF ,. PRCI Dl IS ALTE, 

TH AI lD EH SH N' TO me Il l- SE Nl 

TH HOTAll "ALTt BY Fa BY HIS SlTl Tl 

DA1E Nl A SP OEl1 (J TJ ALTE11 


3/16'=1'-0' 

.._~l.ui-...__ /--,--1171;,,--3--- 

, ¿.-.¿.. _MJ 

!1 i i 0"06 ---- 

'a--~ ¡~_ L..~_.J ---i. . (j~.()0(yr--1 .~. 'L) ( i 

¡ 

r-T--'-n ( 

L~ _-I.JL----1 

KEY PlA 

DATE ISSUED FOR 

DESIGNED -- 

DRA\\ -- 

CHECKED ~ 

SECT.CHIEF ~ 

SCAl 

3/16'=1' -0' 

P.E. 

HAEN AN SA\W 

En En & Sc 

HAEN AND SAWYR, P~C. 

APOVED FO THE CIT or NEW YORK 

PROJECT MA 

P~E. 

P.E 

CHIEF. DMSION or FAcumES DESIGN 



BUREU OF ENINEERING. DESIGN. AN COON 

RED HOOK WPCP 



BY I PROJ.ENGR. ~ 498 SEVNT AVE . NEW YOR NEW YORK 10018 

GROUND FLOOR 

DATE MAY 2007 


ARCHITECTURA 

SHEET~or~ 

DWG. NO. RHFSD370

I 

I 

i 

I 

I 

I 

~ ~ r r 

i- 3' TRNSFER FlLL IN 


r- CHB273020 I' 

4' METERING PUMP SUC110N 

r 

~ r r ? 

r- 2' FlLL IN 4' 

CONTAINMENT PIPE 

'f ¡¡ 

g 

l 

~ 

~ 

l 

~ 

~ _II II I II 

1; 

i I 

l~ 

., 

i¡ 

:5 

l 

~ 

~ 

l 

~ 

of 

i¡ 

:5 

l 

II 

!? 

~ 

l 

~ 

g 

¡: 

II 

:5l 

!? 

~ 

l 

~ 

i 

ii 

~ 

l 

~S~ 

S 

~ 

~ 

~ Ii 

II 

ê 

l 

fi 

!? 

~ 

i 

~g¡ 

l " 

~ 

iii 

III 

III 

III 

III 

III 

III 

", 

II UP 

:1: BRO 7.S' EA 

iii no 10.5' EA 

L 

I ~ 

i~' 

b 

2 e. 

/ If -t- - 

'" 

L-FlBERGlSS 

RAIL (TY) 

2' TO CE TANKS, 

CL EL 5.0 

3' TO AERA l10N TANKS, A 

Cl EL 5.0 

3 

=I 

I i 

.. 

IT IS A \llI Cl SE~ 72.2 Of TH NE 'l STATE 

EDTØ LAW FO lH PE, UNl ACNG UH nl 


0t Of A l. PR EHNE, TO ALTm li 

N( WAY Pl, SPll, PLTS OR RE TO \l 

Tl SE Of It PRAL EN HA BE AP F AN 

rT EING TH SE Of A PR 0l ts AI TE, 

lH ALTE EN SH NRX TO n£ ITD HI SE AN 

Tl NOTAlJ 'N.TE sv Ft BY tl SITU, lH 

OAlE N¥ It SP D£ Of TH ALTmT1 

DESIGNED -1 

SCALE 

ORA\\ -- 

~ '" CHECKED -- 

3/16'~i'-O' 

~ 

SECT.CHIEF ~ 

â" i NO. 


BY I PROJ~ENGR. ~ 

P.E. 

3/16'~i'-O' 

HAEN AN SAWYR 

Ei Enrs & Sc 

HAN AND SAWYR, p,c, 


~ 

~~ 

5RO 

ij 

6.4' E 

4TO 11.5' 

b 

Ie "" 

APOVED FOR TH CIT OF NEW YOR 

PROJCT MAER 

CONCRETE CURB-SEE 

SrnCTURAL 

,II 

L. 1'' 

III 

\t 

~i 

Cl EL X.XX 

L4' EW 6' TO EW CE TANKS, 

HEAT TRAONG Cl El 5.74 

P.E 

P.E. 

CHIEF, DMSIO OF FACES DESIGN- 

IJ 

-~ 

CONT AI FlLL IN 

" "~,, ~~ j \j" ,".t,,~ (r 

~: =:~ENT PIPE (TY) 



BUREU OF ENGINEEING. DESIGN. AN CONSON 

RED HOOK WPCP 



II 

~ 

4'OF~ 

(T') III III- 

FIBERGlSS i 

STAIRS 

, TO INLET CHANNEL, CL EL 5.0 

,. CHLORINE CONTACT TANK 

SAMPUNG UNE, Cl EL 6.0 

-1 2' TO CHLORINE TANKS. Cl EL 5,0 

'2' TO 54' RAS, Cl EL 5.0 

2' TO AERA l10N TANKS. 

Cl EL 5.0 

-~ 

LE 

266041 

3/16'=1'-0' 

L. i 

6 4 2 0 5' 

~.=-_r"--'-i 

r-(9( I 

L.. L_.. 7 

ìF=--i g:~ 9 

I' i i 'I ¡ 

L.~l-~L"~_~h"__.J 

KEY PLA 

DATE MAY 2007 


MECHANICAL 

SHEET~OF~ 

GROUND FLOOR 

DWG~ NO. RHFSD380

I 

r 

, 

iIi 

I 

I 

, 

I 

, 

1i 

l 

~ 

~ 

l 

~~. 

~ 

1i 

l 

~ 

~ 

¡¡ 

2 

~ 

1i 

l ~ 

~ 

¡¡ 

~ 

~ 

~ 

;0 

l 

~ 

~ 

¡¡ 

c ~ß 

~ 

l 

~ ~ 

~ 

l 

i" 

~ 

~ 

:¡ 

.. 

l 

c 

D 

E 

15'-0' 

18'-6' 

F G 

H 

18'-0' 13'-3' 14'-0' 

12'-7' 

cp 

~ 

~ 

1 

!I 

~ i¡ 

""~ 

ili 

~ 

I CAGE LAODER ACCE (1') 

, 

~~ \ 

3-IF \ ~ ------------ ----------~ ---- 

rr-~ -----------X-h-- 

'01 

u m~ 


50% ALAUNIT 

STORAGE 

TANK NO 

I- 

CHB270020 

L- 

-$ 

PUMP SUCT, 

1r4' TRANSFER 

CL El 7.42 

-----1 II 

I 

" 

/ 


INV El 34.91 

r3' TRANSF Fill 

====='1' 

"' 

LV .. 

F ii ::====~==~~~ 

111111111 Ili 

111111111 III 

't'W i¡ '11111'1' III 

i I !J! 1'1 1.1 i1i 1.1 

Iil 111111111 III 

1r4' Of 

I ' 

IN 6' COTAINM 

~Xicf~5 

LKAUNITY 

AGE 

NO 

70040 

~ 

a 

-$ 

ei 

"" 

/~if~;~ 

i I I i 

III 111111 ili 

111111111 ILL 

111111111 ILL 

111111111 III 

ILL iIi III III 

111111111 III 

111111111 ILL 

111111111 11/ 

111111111 III 

llflll III IIi 

111111111 III HIIlI III 

111111111 ILL 

III lIi 

111111.11 

Ili Ili 

III 

111111 III III 

111111111 Ili 

111111111 iii 

111111111 III 

T PIP~~ ~ $. f.ø. l 

METEING PUMP 

El l? ~R 

M M M i11~ 

Itr ili It' iii d: 

:i::i::i: 

1I1t1lii11A 

:11 

II1 

~ 

ml~D ~! 

I ~ 

1'-6' 

7 

_ -- 

~'101 4'-0' 

y- 

ìI 

t, 

UJ 

~ ~ 

113'-10' 

II 

l' CAUBRA l10N OVEflOW 

a. El 35.25 

3' TRANSF IN 6' CONTAINMENT PIPE 

2' Fill IN 4' CONTAINMENT PIPE 

INV El 33.41 

W r3' 4' EW, a. El 23.50 El 20.67 20.08 

4' EW 

irl V a. El 12.95 

ii l' CAUBRA l10N UNE 

4' 

Cl El 8.87 

4' METING PUMP SUCT 

CL El 7.42 

~ 

7 

SECTION A 

1/4'=1'-0' B-M 

I 

I 

.. 

/ 


INV El 34.91 

r3' TRANSFR Fill 

i : 

1'-8' 

, l' 

le 

4' EW II 

: i 

!t ., 

Cl El 20.67 

~ 4' EW TO CE TANK ___ 

a. El 20.00 2' METING PUMP DISCH === 


a. El 18.41 4' Of 

2' METEING PUMP DISCH a 


a. El 15.83 

2' REEF VA'I DISOi ~ 

~ 

Cl METERING P MP 

l' CAUBRAllON UNE I :i a ri 17 ~ 

, 

4' TRANSF PUMP SUC1' 


Cl El 7.42 

'"~ 

III 

2' METING PUMP SUCT 

le 

, 

, ' 

llU-- 

ili 

I 

I: 

/ m 

'" / 

/ 


i r3' 1RANSF INV El 34.91 FIll 

I , 

I.. 

11..~tTlll J f 

(3)2' METERING PUMP DISOi 

----~~====f==~=======, :~V4~i~~NMENT PIPE EACH 

M I 

~II '' ! 

'" 

, 

I 

~ 

R' 

, , 

-4 

r , 

i I 

/ 

~ 

II: l' CHLORINE COTACT TANK SAMPUNG UNE 

II: a. El 19.50 

~ l' Noaa IN 3' CONTAINMENT PIPE, 

!I! a. El 14.87 

=ge-_=:!I: ----¡ 

U' 

~ 

m i .- 

:r 

in 

Hl 

I)~ 

~r' r, 

I , 

~ 

4' \Æ 

Cl El 34.67 

I 

, 

I 

, 

I 

, 

l' CHLORINE COTACT TANK SAMPUNG UNE 

Cl El 20.50 

TOP Of PARAPET 

I~ 

El 11.87 

El 925 SAMPUNG UNE, a. El 6.00 

I (2) . l' GRADE OilORINE CONTACT TANK 

'~~7 El 7.25 

(1)1' H'lO IN 2' CONTAINMENT PIPE (FAR) 

R)2' El EW/H'lO 5.0 IN 4' CONTAINMENT PIPE 

El 2.00 

.. 

IT IS A i.TK (K SECT 72 Of THE NE 'l STATE 

EDll LAW FO Nr PE, Ul AC UN Tl 

D1R£ Cf A UC PR EN, 10 AlTE IN 

Nr WAY PI, SP'T, PLTS OR RE TO -l 

ll SE Of A P' EH HA BE AP. If No 

I1 BE TH SE Of A PR EN IS AlTE, 

TH AI TE 0l Sl lo TO TH ri HS SE AM 

TH NOTA'D .ALTE BY Fa BY ll stATU. Tl 

DATE Nl A SP OETI Of TH ALTE'O 

1/4'=1'-0' 

1 

I...uW 

0 1 2 3 7' 

I 

DEIGNED NB 

DRAYr -- 

NO. I DATE I ISSED FOR I BY I PROJ.ENGR. 

I SCALE 

OiECKED NB 

SECT.OiIEF ~ I 1/4'=1'-0' 

PDS 

P.E. 

HAEN AN SAWYR 

Er En & Sc 


498 SEVNT AVE 'NEWYORKNEWYOR1001B 

APVED FOR TlE CI OF NEW YOR 

PRECT MAGE 

P.E. 

CHEF, DIION OF FACIU OESIGN 

I~~ 

I~~) 

P,E~ 

~ON""'TAL~~ 



BUREU OF ENGINEERING, DESIGN, AN CO 

RED HOOK WPCP 




MECHANICAL 

SECTION 

SHEET 1 

DATE MAY 2007 

SHEET 33 OF 56 

owe. NO. RHFSD390

, 

, 

, 

l 

, 

, 

A B c D E F F.1 G H 

~ 

i- 

170'-0' 

20'-0' 14'-0' 29'-0' 29'-0' 29'-0' 16'-4' 10'-6' 20'-0' 

~ 

I 

1 

11 

f/ 

i: i: i: i: i: 

b m 

ir 1'- 

"I 

Tl 

åo , 

~ 

o 

dl \: 

!D 

UP-i 

v--/ 

2' -2'(ll) 

l-O'(ll) 

LCP 390100 

l r\ ~I 

- -- f+ 

TO RSP BREAK 

TANK, SEE OWG NO. 

LA fV 

'" , r 

2G-CIi-UTL-C21 __ 

4' 

~I , 

3' 

2' 

.a 

3' 

i 'i i 11 : , 

: i 

, 

~~":l 

, , , 

~CS-063113 ~ 

,CS-063111 ~ 

o 

~ 

~ 

4.. 

B . 

I 

.. 

Df 

b, 

~I b l 

~ 

.. j I 

l 6 

~ 

~ 

a; 

l 

~ii 

~ :; 

-. 

g 

~ 

~ 

l 

~ 

"f 

i ,. 

~ 

~ 

ii 

"f 

i ~ 

~ 

~ 

l 

~ 

l' 

i 

~6l 

~ 

~ 

'Ï 

ö: 

,¡ 

60' AIR HEADER 

~ 

TO AERATION 

~ 

TANK 

~ 

8 ~~I 

~ 

o 

~ 

~ 

fi 

l 

~ 

~ 

ii 

~ EDl1 LAW FO Nr PE, UIl AC UN TH 

OÆCT' CF A UCSE PR Dl TO AlTE .. 

Nf WAY Pl, SFClTl PLTS Of RE TO 'f 

l JT 

THSEOfAPRALfJ!iEl 

Bi 'T 5E Of A PR EN 

AP. 

IS Al1I, 

FAN 

Tl AlTE EH SH Af TO DE IT H: SE AN 

TH NOAlION °AI.:lE BY Fl BY H: SllU, TH 

¡~" 

DATE AN A SPCI DETI Of 'T ALTET1 

,; '" 

DESIGNED ~ 

~ 

~ 

~ 

â"i NO. OATE ISSED FOR 

- 

fT IS A \1Tl a: Stll 72.2 Of 'D NE '1 STATE 

h--1H, c -- :¡ ¡e ~ ,--:¡1I -- 

ORAVI ~ 

CHECKE -- 

SECT.CHIEF ~ 


SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Enviom En & Sc 


49 SENl AVE . NE YORK NEW YOR 10016 

D ~ 

MCC ROO , 

IIIIIIIII"F ~ 

, 

I~ 

I ? i ;~~:;: 

APROVE FO THE CI OF NE YOR 

PROJECT MAGER 


P£ 

P~E. 

CHIEF, DIVIION OF FACmES DESIGN 

CI OF NEW YORK 


BURE OF ENINERING, DESIGN, AN COlRUCON 

RED HOOK WPCP 



l 

lf+ 

, 

, 


MECHANICAL 

GROUND FLOOR 

DETAIL PLAN 

NOTE: 

1. FOR ABBRE'A TIONS, SYMBOL AND GEERAL 

NOTES SE DRAIING 2G-PFD-GE-FOI 

2. COPUNGS SHAL BE 

FIXE X EXANSION (FX) 

FlBl, AIR TIGHT (EX) 

AS SHOVI. 

42' INLE SILENCE (ll) 

. INDICA lE5 FIED llE 

P1Æ SUPPORT 

o INDICATES SLDiNG TY 

PIÆ SUPPORT 

36' DISCARGE SIlECE (ll) 

2' SW UP TO OIL COOL (ll) 

'b 

.¿i 

..1 Ï" 

i 

in ~If ,~ 

)if -- .... :r!f "" 

3' SVr UP (ll) ~ i~ 

24' DISCHARGE (ll) 

42' UP TO BLOWER (ll) 

EQUIPMENT ACCES (ABOVE) 

36' DISCHARGE 

FE 

396100 

PIT 

396100 

BLOWER COONG 

;. l ~ WA Ó~TR~~~~ii~i¡W_IO 

lE SYTEM 

BREAK TANK 

FOR CONTINUATION 

UNDER CONTRACT 

SEE 2P PLUMBING 

F1-390100 

1/8'=1'-0' 

~ i 8 6 4 2 0 8' 

f_,.._.L:;::rrù~~ 

ir"'=iL' ¡L_," -'--1 ~~ _.l f52~ VII q 

i..-"---.--- ,. 

lb-; ii rLJ:, L__ 1r . i 

KEY Pl 


SHEET~OF~ 

DWG. NO. RHFSD400

t 

~ 

~ 

~if 

- 

!i 

l 

;¡ 

l 

~, 

ii 5- 

~ 

'" 

~ 

~ ~ 

~ 

~ 

ii 

5- 

~ 

~. 

,¡ 

5 

~ 

61 

~ 

l 

~ 

t 

i~~if 

!i 

l 

ti5 

l 

ii 

S 

~ 

o 

~ 

ê 

l 

~ 

~ 

ii 5- 

l 

¡;i 

" 

~ Ii 

j 

~ 

~ 

~ 

" " '- '-~ '"' , md .' ./ 

'- 

20' O' 14' ~M 

29' 

I 

O' ~ i 

29'-0' 

29' O' 

lB' 4' 10 B 

'- I i cr ;¡ Ii- Ilí T i r In ~~ Ii W. ~ 

§ 

~ 

l 

~ 

l 

~ 

I I L: I "" Ifr ~I f--- 

I \ =,F '" ( 0- ~~ ~ t= 

cæDCR ': CO RO ~~~~ ~ "CO RO ~ t= h 

i ii ~ om iõ ~rn " F'.¡ ~oo," ~:---081~ 10 0 0 0 01 HVAC STORGE 

11l¿" C h -- 1- 1!:.~..,, ,~-~ ROO '- ~ 

. ' UPS-BLW-OSOI-;J ~o.. /:LE80SO /0 REMOTE I/O 0 ~VI 

· '" WON 1'1.1111 ~- ~"rn~ U ~o"jO ~,... ='/0 -" ,-' r--~ ~"jO couu~ L' if1 ~ f--- 

~ ~~ ~oo C. ', ': ~ I.. A gi A " ~ =i 

o - 

'- 1\ ~r D 

~--- 

i ~ : èii j é! J\ i f 

v 

L-= ____ 

- 

7'-0' _ 

(~) 

L UPPER ~ __p- BLO'i 

~~ 

~ ROO -, 

liH 

I " 

S ~ . i EL -------"r¡ , 29.50 " -i '- BLWOOzii- ~--"' '" n n k El -i j ~ _ b= 

ir 

_ 

___ 

~ ,I Ë ¡- EI n _ AUX OIL PUMP (TY) r;í.r __ L- 

- : '''., .~"'~~ ~ ~Î. n _ 

--- H i = .""_ "'t;o- ~ "_.j in-æ~-- alli- 1;~1"" i-§ ~ 

' 

"D y 

~ 

n~1 i: ~ 

't 

LCS-08034-n .""- ~r;~, 

" " 

;.~ ~W~-i" 

""'.' 

~-V' __ § ß. II i- -- h 

" ,~~o -- ,n'; " i ~_oo-" 1L51 ~ r- ~ ~ r- 

? ~ 

, -- .~ H .~,~~ 'OO"~ _ Är' ¡¡ "III~ _ __ 

. - !Ê. in.""-- L , J _, '_-- 

~"'jO ~"jO .-" -co - 01 

:Q~' ~.,,~ 

FLOOR 

LCS-0802~ 

MOUNTED 

BLOWE 

r-' 

REMOTE 

LCS-08JOJ~ FLOOR 

/1\ 

I/O MOUNTE BLW080140 

-- 

BlOViR LCS-08301 F508904 

~ 

REMOTE 

- 

~ l 

m 

I/~OLWOOI50 BLOWE 

"' 

i ~ !S I 

~ . ~ 01\' ::j tl LCS-OBOI40 UL Lû)J U L_ - 

'/ I - LCS-08~11 -~- r. --~'-~ Jf BLWO~03Oi i ~hmV 

¡. ' ------ i ----H---j i fi III ~ --BLWOB9010..- I! i = V \FlLTERSíl I "III~ 

1 

f" 

~ 

FlLTRŠ? _rJ ~-~ 

~l 

1__ 

I 

-.,,-? L- 

W: 

': _ r 8' 

':Xi, 

J H~ 1 _, __ : 

~¡ 

J ~ ~i g i :- 

i 

~ _ r ~ 

'J , ¡ j~ r :.r t ~ ~r r . ~ or r = 

BIt ~ ~ ~~ j ~ ~ ~¡ I ( ¡; ai~ ! --= (I~ r ~ I = JFii- 

IXJ OB6010 i ff :: (i. ai ~ L 1-- ¡. L I +' L -l i-IIIL 

~ - ~ , kK" '~ j ~ e, ,~ 'I' r l ~ " , l, -- ' I I 

~ I JFi '~-~ I AlRINTAE¡ i I 

DAMPER (TY) 083011 08012 0Wbt i 

i I !POISH \~ I 

I ~O W:) 

'\ - - i L zsc/ zSC/ zSCf (ABO'Æ) IT AIR SHAf (ír) 

.I T! PREFlLTRI¡j/TY7 / "-FINAL FlTE (;i~i 01/02 01/02 I I 

.. 

IT IS A wiTK (s SECTI 722 Of næ NE "i STATE 

ED1I LAW F' Nf PE, Ul ACNÇ UlC TH 

Il a: A l. PR EN 10 AlTE II 

N( WAY Pt, SPClT1, PlTS OR RE TO 'M 

lH SE Of A Pf.l EN HA BE N'. f' Nl 

mi 8£ THE SE Of A PR DQ IS ALTE, 

TH ALTE EN SH AF 10 TH rT HI SE 1S 

Tl NOTATla- "AlTE BY Fa BY tI SGlV, n£ 

DATE lM A SPCF D£SC Of nl AllEll 

PROCSS AIR ALTRS (TY.) 

INSTRUMENT A l10N SHO\\ 

ONE FlL TE SYSTEM 

FOR OTHER FlL TERS SE 

owe, 2G-lolC-BLW-IOl 


NOTE: 

SW TO OIL COOR (TY) 

S\ (TY) 

LUBE OIL SYSTE (TY) 

SE owe. 2G-1 ol C-BLW-IOJ 

FOR INSTRUMENTA11ON. 

2~' DISCHARGE (TY) 

42' INLE (TY) 

15 TON BRIDGE CRANE 

SE owe. 2G-1 ol C-BLW-102 

~ 

FOR INSTRUMENTA l1ON. 

(TY) 

l 

~ 

8 

I. 

6 4 

.. 

2 0 

I 

8' 

1/8'=1'-0' 

,r ~ I 

i '--- II / ' 

L.LJ1Jrrc:;:, ~rl 

~ir-=rU GGQgr---l 

IL_J IJ___J 

,---- ~ KEY PlA 

DESIGNED NB 

ORA\\ NN 

NO. I DATE I ISSED FOR I BY I PROJENGR. ~ 

SCALE 

HAEN AN SAWY 

APROVE FO THE CIT OF NEW YOR 

CHECKED NB En En & Scnti PROJECT r.R 

AS NOTED 

SEC1CHIEF ~ 

HA AND SAWYR, P,C, P.E. 

P.E. 

~9BSENTAVE' NEWYORKNEWYORK1001B CHIEF, DlON OF FAClLmES DESIGN-OU 

P.E. 



BUREAU OF ENGINEERING. DESIGN, AN CONSlRucON 

RED HOOK WPCP 




MECHANICAL 

SECOND FLOOR 

DETAIL PLAN 

DAlE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSD410

I 

i 

I 

i 

I 

i 

i 

I 

i 

I 

I 

i 

I 

I 

I 

i 

¡ 

ì 

i 

i 

I 

i 

I 

I 

i 

I 

TOP Of ROO 

a 57.83 

TOP Of ROO 

a 47.50 

TOP Of SlB 

a 29.50 

§ 

~ 

~ 

l 

~ 

,¡ 

¡¡ 

! 

i 

t¡ 

t '" 

., 

¡¡ 

;j 

?~" 

~ 

TOP Of MAT 

aii.50 

- 

t¡ 

l 

~ 

,,)\).~ V,,,' 

~ o 

~ 

,//y 

r 

~ 

~ ~ 

ß5 

l 

¡ 

~ " 

~ 

w"" 

rr IS A i.l1 Cf SEl1 72.. Cf lH NE 'R STATE 

~(¥:~~~=.U~~.. 

Nl WAY Pl. sPClno PlTS Of R£ TO 'M 

TH S£ (X A f"H. EH HA Sf AP F' Nl 

IT El TH SE Cf A f' ENEE IS ALTE. 

TH ALTE EH SH AfX TO Tl IT Il SE Ii 

TH NOT..TI 'AlTE BY FC BY liS Sln. TH 

DATE N( A sPCF OEll Cf nu ..mvTI 

L. 

~ ~ 

;: 

~I NO. DATE ISSED FOR 

~ 

~ 

f 

~i 

cpi 

T T 

NOTE: 

. INDICATES FIXE TlE 

PIPE SUPPORT 

o INDICATES SlDING TlE 

PIPE SUPPORT 

L. 

1 

J~\'Y' ". 

SWITCHGEAR 

1 

MCC ROOM 

Lo 

15 TON BRIDG CRANE 

o 

1J 

o 

R 

1 

Q 22.50 

CL 21.50 

36' DISCHARGE 

Q 15.17 

Lo L. L. 

UPPER 

BLOWE 

ROOM 

36'x24' REDUCE 

J 

I 

i 

I 

, i 

~ 

i 

4 

îl 

Is biSCHARGE I I / 

~inCER (Tl) -l i 

1/ 

Lo Lo 

BLOWE 

BLWDD13D 

(NOTE 1) 

r- 

-= 

. 

,1-1 - 

& 

~ -l 

II 

T 1T 1 i- 

,--- 

c=~=I=~=Jlll 

~i 

i 

-\ 0 

~III i 

II 

t 

r:/~'!\') . ( 

d~======~ II 

I 

i 

ì 

~ 

~Jh 

I- 

42' LR 90' - 

BEND (Tl) 

I 

$-- 

I 

8& 

ir-\+, 

--~ I 

. o o o o . 

I \ 

W 

L 42' 

W 

INLET i 

L. 

SILENCE (Tl) 

SECTION ~ 3S' DISHHARGE 

I ~'~~~ 

PENTHOUSE i 

T 9 1- 

. 

AIR 1- 

PlEUM 

ru~ 

I 

i 

TOP Of CRAN E RAIL 

a 48.83 

· 24' BLOW-OF 

Q 23.17 

.)\ /,:(yi ")~, v'i" 

~l~~ 

L. L. 

L. 

so' AIR HEADER 

Q 15.17 

")\--)\V,,,, ,//y 

L 

1/4'=1'-0' 

DESIGNED -- 

DRAII ~ 

CHEo(ED ~ 

SECT.CHIEF ~ 


SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Ei Eninrs & Sc 


49SEVffAVE ' NEW YORK NEW YORK 10018 

APPROVED FOR THE CfT OF NEW YORK 

PROJECT MAGER 

P.E 

P.E. 

CHIEF. OMSION OF FACILES DESlGN- 

CIT OF NE YORK 


BUREU OF ENGINEERNG. DESIG. AN CON5ON 

RED HOOK WPCP 




MECHANICAL 

SECTION 

1 

i.W 

0 1 2 3 7' 

i 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSD420 

~~ 

Ii 

Ii 

i' 

L 

r 

ii 

Ii

I 

I 

I 

I 

I 

I 

~ 

1 

l 

~ 

8 ~¡¡ 

i: 

i 

I1 

" 

!l 

S $ 

:; 

~ 

l 

i' 

~ 

~ 

8 ~ 

l 

¡~" 

~ 

l 


Microfilton PLANT INflUENT PRIMARY SENG TANK INflUENT PRIMARY SETTNG TANK GRA ',TY THICKENER 


CETRAlE 

RAS 

AERATION TANK 

WAS 

AERATION TANK 

EfUENT OVEflOW MlæOfllE MICROFllER 

INflUENT EfflUENT I TANK fiNAl SETTNG INflUENT I fiNAl EffUENT SETTNG TANK I INflUENT EfUENT 

I PLANT EfUENT 

flOW (MGD) 32.9 36.2 34.9 4.5 0.1 34.2 0.7 39.5 73.7 73.7 38.B 38.8 38.8 I 39 

15S (m9/l) 199 181 111 150 186 5,271 5,271 116 2,502 2,502 13 13.3 1.0 

T5S (IbId) 54,700 54,700 32,40 5,700 180 1,502,700 31,200 38,280 1,53,100 1,538,100 4,30 4,300 300 30 

æoo (mg/l) 142 129 111 68 65 1,915 1,915 106 910 910 12.5 12.5 1.6 2 

æoo (IbId) 39,00 39,000 32,40 2,600 63 54,00 11 ,30 35,063 559,300 559,300 4,00 4,00 50 50 

TN (mg/l) 31.7 28.8 26.5 25.0 547 35 354 27.7 171 171 6.7 6.7 5.9 6 

TN (IbId) 8,700 8,700 7,700 900 53 l00,BOO 2,100 9,130 105,100 105,100 2,200 2,200 1,900 1,900 

sæEENINGS 

TRUCKED 

",'" 

(''' 

1 MAlN SEWAGE 

1 PUMPS (6) 

1 

1 

1 

PRIMARY 

SETTNG 

TANKS 

(4) 

PRIMARY 

SlUDGE PUMPS 

(6) 

r--~ SECONDARY 

I BY-PA5S 

1 

I 

I 

I 

MICROfl TRA TION 

TANKS 

(11) 

fiNAl 

SENG 

TANKS 

(8) 1 

I 

1 

I 

I 

I 

CHLORINE 

CONTACT TANKS 

(2) 

li 

I 

I 

I 

I 

I 

l 

1----.-..---1 

. f 

1 

I 

f 

I 

t 

I 

-------------------------------------______1 I ----------------------------------------------------------------_____________J I 

i 

I 

---------------------------------------------------------------------_____________J 

(2) 

WAR 

IT IS A 'w~ a: S£ 72.2 a: Tl HE 'l STATE 

EDTI LAW Ft Nl P£, Ul AC I. ll 

Dl OF A uc PR EN TO Al.:rm .. 

Nl lIY Pl, SfCITK PlTS OR RE 10 -l 

DE SE Of A PRAL EN HA SE AP F 1M 

im 9£ TH 5£ Of It PR EN IS ALTE, 

n£ AlTE EN SH Af 10 TH IT HI SE AM 

Tl NOTA1\ "Altt Er Fa BY tI 9GATl 11 

OATE AN A SPCl D£ OF TH ALlEll 

~ .. 

(2) 

SlUDGE CAKE 

DISPOSAL 

DESIGED NB 

DRA'I EG 

NO. i DAlE I ISS fOR I BY I PROJ,ENGR. ~ 

SCALE 

HAN AN SAWY 

APOVE FOR TH CI OF NE YOR CIT OF NEW YOR 

DEPARTMENT OF ENVIRONMENTAL PROTECTION DAlE 

P.E. 

CHECKE NB 

Et EiIS & Sc PROJECT MAER BUREU OF ENGINERING, DESIGN, AN CONS NEW 

SHEET~OF~ 

SECT.CHIEf ~ AS NOTED RED HOOK WPCP 

HAN AND SAWYR. P~C. P.E. CONCEPTUAL DESIGN FLOW DIAGRAM 

P.E. 

498 SEVNT AVE . NEW YOR NEW YORK 10018 CHIEF. DISION OF FAClS DESIG DWG. NO. RHFSM450 

ADVANCED TREATMENT TECHNOLOGIES MASS BALCE 

MAY 2007

I 

i 

I 

\ 

¡; 

!l 

~ 

l 

~ 

!( 

~ 

~ 

~ 

l 

~ß 

! 

~i¡ 

~ " 

~ 

~ 

i! 

l 

~ 

~ 

ß~ 

l 

i'" 

~ 

~ .; 

~ 

WA 

IT IS A ~TI Of SECT 72 Of 1l HE 'Y STATE 

EDTK L.W FO N( Pf, UN A. UIU TH 

tl Of A l. PRENNE TO ALTI.. 

JH WAY Pl, SPClTO, PLTS OR RUTS 10 Yi 

1l 

na 

S£ 

~ 1l 

Of 

SE 

It PRAl 

Of A 

Dl 

PR 

HA 

EH 

IH 

IS 

N" 

AL.:re, 

F AN 

TH ALTE EH SH AF TO TH lTEI ~ 5£ Nl 

TH NOTAlIO\ 'AlTE BY fC BY tI Sll1. TH 

OAT! Jo A SP DE Of TH ALlDTI 

~I NO. DATE ISSUE FOR 

WO.CO 

BY 

~z. 

GALLERY 

c! 

EXISTING 

PRIMARY SETlNG 

TANKS 

T 

Ci 

LJ 

i 

I 

Q 

QJ 

i 

BLOG. 268 

DESIGNED ~ 

ORA~ -- 

CHECKED ~ 

SECT.CHIEF ~ 

PROJ.ENGR. ~ 

SCALE 

AS NOTED 

P.L 

NEW CHEMICAl STORAGE AND HANOUNG BUlLONG 

\-\ 

-'--- - - 


EXISTING 

MAIN BUILDING 

AODIlONAL RAS PUMPS 

. IN EXSTING GALLY 

I 

L 

EXISTING 


TANK 

1'=30'-0' 

HAEN AN SAWY 

Er En & Sc 


49 SEVNT AVE . NEW YOR NEW YOR 1001S 

APROVE FOR TH Cf OF NEW YOR CIT OF NEW YORK 


PROJECT MAER 

P.E 

P.E. 

CHIEF, DI OF FACIES DESIGN- 

BUREU OF ENINEERING, DESIGN, AN COUCON 

RED HOOK WPCP 



CIVIL 



FOOlPRINT FOR 

MICROFL 1M TlON TANKS 

I. 

~ UMITS Of CONSTRUCTION 

30 15 0 30' 

L .. __ I 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSM460

I 

I 

I 

i 

I 

'1 

i 

~ß~~ 

=J 

:¡ 

l 

~ 

J 

~ 

'f 

i ~ 

~ 

~ 

J 

~ 

1- 

:¡ 

~ i 

~ 

~ 

~ 

j 

~ 

~ 

~ 

i2 

i 

¡ 

i 

ß~~ 

~ !! 

~ 

~ i: 

I' 

~ 

l ~~ 

~ 

~ 

l 

l;0 

.. 

IT IS '" i.ll CF SE 722 Of 1H HE YC STAlt 

£OT1 LAW fO AN PE, lM ACTJ lH TH 

DlC1 Of A uc PR £HEI, TO AI"Æ IN 

Nl WAY Pl SPTI PlTS OR RfTS TO \I 

TH 

I1 8E 

SE 

TH 

Of 

SE 

A Pf 

OF 

EH 

A PR 

HA 

EN 

El AP 

IS AlTE, 

F AH 

n£ AL TE EN SH Af TO TH JT )I SE AN 

TH NOATI "ALTE BY" FO BY ll SDll tH 

D. TE AN A SP 0€ Cf TH Al TE'1 

~ 

~ '" 

~ 

iì i NO. DATE ISSED FOR 

I 3 

,-- 

-r V SLUDGE EXISTING 

STORAGE ~ 

AND 


r 

QASli 

HOLDER tf I 

4'-0' 

IT 

I 

--------------~ ~ 

-. ~ 't7 

EXISTING 

CHLORINATION 

BLDG. 

l 

~ 

21't-0' 

b 1 

ê 

:: 

EXISTING 


TANK 

- 

- -- 

- 

,-IV 1 

G 

c I 

+ 

1 

1 

I 

~¡J~ 

+I,,1 

. 

I I 

1 1 

r- 

t1llllillllllll ,nm~ I 

inI! 

)111 

i 

:' 

, 

, ~i¡' 

~ h 

wm~i¡¡ 

, 

h 

~ rp~11D 

,~_, ~_ ~ ,,*,37 

o oci 

o N 

Z 

DESIGNED -- 

DRAI'~ 

CHECKED -- 

SEClCHIEf ~ 


SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Emro Enne & Sc 


498 SEVTH AVE' NEW YOR NEW YORK 10018 

APOV FOR TH CI OF NEW YOR 

PRCT MAER 

P~E~ 

P.E~ 

CHIEF, DMSIO OF FACßJES IJSlGtI 



BUREU OF ENGINEEING, DESIG, AN CONSUCON 

RED HOOK WPCP 


ADVANCED TRETMENTTECHNOLOGIES 

z 

VNEW MICROFILTRATION TANKS 

~-i 

1'=20'-0' 

20 I .. 10 .. 0 20' I 

~,l U U l....:..--- 

I L ii r"-l ¡ S0)xQl~? CTt--1 ¡j 

IT ~~(1 

___io ,Ji J 

KE Pl --'-'" 

CIVIL 

PROPOSED SITE PLA 


SH£ET~OF~ 

DWG. NO. RHFSM470

I 

r 

I 

I 

I 

I 

I 

i 

I 

i 

~ 

i ~ 

~ 

~ 

~ 

~. 

~ 

l 

~ 

ß ~~i~ 

~ o 

~ 

~ i! '" 

~ 

~ 

~ 

ß ~ 

l 

¡:l 

", 

' 

" 

~~- ~~ 

..,,1M 

g ~ 

~ % 

~~ 

'- 

0N!!0P 

! 

i 

~'i¡ 

..' N' 

! - 

, 

lß, -rÎ .: 

!ô D£"DL il 

:iWG "'-3'" I : . 

I1 

i 

' .. -I 

Î ~ 

, "'I 

''' 

I I 

I ! 

I ! 

¡ I 

) 1. 

~~ ¡ 

; 

FROTH HOOD (ì') i; 

~ i 

8 TOTAl 

j . I 

8AF WAl (ì') 

28 TOTAL 

.. 

MIXE (TY) 

20 TOTAl 

IT IS A \KT1 ci SE 72.2 Of Tl HE 'I STAlE 

ED1I LAW Rl Nl PE, UIr ACNG UH mE 

Dl CF A UC PR EHH£, ro ALTm .. 

mY WAY Pl, SPT1. PlTS Of R£ TO 'I 

TH S£ Of A PR EN HA BE AP. F AN 

IlD BENG nl SE Of A fI Dl IS AllI, 

ll ALTE EN SH Nm TO TH rr lC SE AN 

1) NQTA"J "ALTE BY Fa BY tiS SlT\. Tl 

DATE AN A SP D£l1 Of TH Al1Eno 

DEIGNED 

ORAI\ 

l 

la 

I NO. 

DAlE ISSED FOR 

, I i I ~ 1''3 ~ If' I ~iI:i~l~~.?O I .136. I 

~ 42" Ref. 

I 

PRIMARY 

: 

I 

i 

. o 

~ ,\ 

i / 

I I 

r------, ----- I. ~ AERATION TANKS GALLERY ROO: --- 

. i . T.lK DRI\ SUIC . FIRE HVOR ; 

, 'l., If 5S AIR HEAR I TYPE. ~ OIFFUSER I I GATE OPETO 1õP. -- ,-1 l 

I. t- -------- ------ ------j------- -----~--------- 

! /1 OWG. M 117! (TYl,) i 

\ - 

, i I Y 'r I DETAlLS ~ EL, '".0 ON DWG. ARR~NGEMENT M-~77 i (SEE , DE!AIL VN-VE ON BOX I. (TVPI II~~ -- .. . lW' 

i i.4'5PMY ~ ~- He 10' I 55. i AIR I, I I 

4; EL rzOO"" HEi=S (TYP.) I I 

I 

'1~i.-_- 

---- 

__ 'ii ;E===-----===- 

-- I 

¡ 

____ 

~--'-';E===-----===- i 

___ 

: TRC\JHS(T'P) I EFFUÐlT ¡o 

I I -i./ I ~ 

;s===-----===- 

~ g 

, ,( 

i I 

f I i 

, 

k. 

I I I.. T . 1 ",'" 2~ I I ~ i 7,\ i~ .. 3 

I..!: Z -' ,. 

IT'P.) I "'a: . .- 

, ------- - iI ---------___ I i -===-----===_ ,I i ~; -===-----===- ~ i T'fpe'C' 

I õ: . i5 I COuPLIN'" __ 

Il~" 

41.d5~ ~ -~ 

VCTl'P.) 

~ t:ñ 

:z ~ 

. f~" 

'" II 

i 

~ íi I 

.. '" I 

AERATio.N l I 

~¡ 

~~s:¡ 

i 

IIIT 

~. 

If."" 

-- i I 

,.... U2i11 

,~ 

"" 

¡ . 

II 

. , II 

¡ ~ : ¡ I 

i 

!! 

~ 

OiECKED NB 

SECT.HIEf ~ 

8Y I PROJ.ENGR. ~ 

z7'-6" 

'n.p.) 

~~ Iif 

~ à 

SCALE 

AS NOTED 

o ~ ~ G) 

I ","PLOW ..'!TElê ~T'fP. It., - " I OF r' II STRUT 4:---- ~~ l 

¡ I ('",5T"",- 

II iELJ7ï: 

UPRlGHT) I ~~~F I 

i 

" -+ ~LFOW I io~"0'5.b (T"') I I " - " - -. I I " +I! 

"' , ì! ì! r2EMO~ i:HC '1 4' S5 

I 

I I 

~ -I 

I 

PLNK~Tj:rP 

1-' -I 

I TEE 

I 

(TvP)~ 

AERATlo.N 'I TANK No..32o.2 AERATlo.N! I mNK NO. 3203 ¡ -: AERATION II TANK No..32o.1 

TANK No..32o.l 

111'111 

I I i I 1 I ~ 

". ~ '=1 'i = ¡I'i 

i ------------ i I ------------ I 

I, riEMlIOLE F':' (TR) I I !:il. 1 I II 

r 

" i 

"., Ii 

-"'i1 -iIb 

D£T¡IL ON DWú.M-37) 

~AY WATER 

NOZZLS (5EE 

,,'(up) 

P.E 

HAN AN SAWY 

En En & Sc 

HA AN SAWYR, P.C. 

498 SEVNl AVE " NEW YOR NEW YOR 10018 

I I 

I I 

I I__ _ _ l _ 

I sWl- GlATlNG ITYP) 0' d-o OPEING I I I 

~ ~ 

320~e.$ 

3/32' =1' -0' 

LJ I 

10 8 6 4 2 0 11' 

APOV FOR THE CI OF NEWYDRK CIT OF NEW YORK 


PRECT MAGE 

P£ 

P~E. 

CHIEF. DIVISION OF FAClES DESIGN 

BUREU OF ENGINEERING, DESI, AN CONSN 

RED HOOK WPCP 



NOTES' 

1.-" DEES FIXED PIPE 5UPPl 

2.- c DENOES 5Ull PIPE SUPP 

, " 

.,0 

.-, I OOv.~.1 "-F.(~"l!.. ..... I 

L~=~ 

MECHANICAL 

RHo 



.-4'- 90'S5 

I ELbOW (TYP) 

~~, I -T'lpe'~ OIFF\J5e:R 

I Añ,:D.~Ei,Et~: (i .,-=) 

. Jv-'~1f~\ 

l/ ~ -8H~O~: 

~I 

lMl'l 

c 

~I 

rl~'" 

-nl 

i. 

- ëi=FLUENT 

CHAo",:aL 

IIiV E,- :i~:! 

MATCH L1",i; (FOR CClT. 

5E DW. M-~3) 


SHEET~OF~ 

DWG. NO. RHFSM480

i 

I 

¡¡ 

~ 

~ 3- 

~ 

l 

~ 

~ 

l 

~ 

l 

s 

~ 

~ 

o !I 

S ~ 

~l 

il 

~ 

~ 

w"" 

C liT IS It 'fTK OF SE 72 Of TH NE 'l STATE 

./ l: EDTJ DI OF LAW A FOR uc NlY PR El, PE, Ul TO AC ALTE I. lH ll 

ã N( WAY PL SPQfll PLTS DR RE TO 'MlC 

t: ~~~~~=l~~. 

¡ ~~nc~~~~,:=~ 1l 

:: 11 AlTE Dl SH Nf TO lH ITD tI SE AN 

~ 

'" 

~ 

E 

~ 

~ 

~I NO. DATE ISSED fOR 

)~ 

, i . 

I ¡ 

FROTH HOO (m 

8 TOTAL 

BAF WAL (T') 

24 TOTAl 

MIXER (T') 

24 TOTAl 

~~~ 

t 

:f _", I t1l\ n 

!2 

DESIGNED -- 

DRA\\ -- 

CHECKED ~ 

SECT.CHlEf ~ 


! 

~ i- 

-i! 

i ~ I ~ I 4 ii 'j i' . ': 

-.!~, 

-"'.' I 

I~~J'~ 

i~' ¥2IDS 

, " 

-. 

I ' 

~ 

~ 

ii 

1_ 

f\ 

I 

l4.UlS 

~_ _ '~II 

I ii 

. 

rl 

~ 

p;t.os 

_ ~ IIrMATCHLIHE(FOi.cc'I.5EeOWG.M-:;Z) 

, , II! Wi ~4.4DS' ! I 

t.4OBS - " . ~ : i ~, "'6'WALMW''Æ I AFFLE ~ :!, "'T-~2Dz-i; / t..~ I == , A1-=-i;)~" j-D1ITP.I I. i (Ai':!-i;) '340B~ I ¡;¡ I ; ,i 

11~ " I II~ ~., ~ ~~-32oiei). I ) ì'l. ÄE-3ZOI-E; (, - ~ LL(TY")' ( REMoA&E ) ll-32D2-P, ~ ~ CO. ) ~ ~ ,,'~I COAIIEDSLUlCe (¡ GIoTEIT'lP.)- f i ~ ?l~?J'o'S£L~ ~ ;) I (, ) ~ i "'i ,~. b,l! c I W/GRATINGITYP.;"' 

~ i s- I I FUNKs 

I ,~ 

tT1P.~ 

/lo'S.5AJ 

I 

I 

I II 

i ., 

¡: 

~i 

j , I I I I ~ "Á HEA(TYP.l I I rd I 

i 

~"II ~ II i ~ ii I" 'I y~ ~.ii .. 

~ '- I ~ i' 4" WATE ':y I I HEA I I I I' I 'i I i I - L .t -- ~w. OJRANIIENT I .-TYPE ;¡ DlFFUSE.R (SEt 

- t EL.17,OD I . i i i ( I ; I DeTAIL ow,, ...-~7) 

Iii ~ i i I I I J 1£1 _ '" --4'.'1'55. 

I - I I -- - I I l = ltl -" I i I ELBOW (TYP) 

ii= 

i~"'--- 

I 

-~ 

~ 

I 

I "" 

i 

~ 

G~ 

I I 

r- 

g 

i 

I 

-:"" 

--t 

/" I 

OFsTlT 

I ~~ ____ 

- 

___ 

I 

I~I 

..__ 

"'t: 

EFFuT 

_ _ 

I ~~ 

~. 

"" -, 

''i 

." 

z'.o'ClYP-1 

_ - ~~ I I 

i~ 

~2 

I 

-===_____===_ 

I ~~ I~i 'TYPE'C"COPLtl~ 

~ (TYP.) ~.. 

I.. 

;"; 

;::':~,,, 

I ~ I I ios.s.f'oce~' i -". 0: /",1 l-TYÆ'c" i 

/. 1i ~.) I I A1R'tEL.,'ii,.,o~ IA ~5' I I ~ l!!l -- ~'ii COPLIlc¡(TYP.) 

ii 

~ , I i.1R!'OW '! 

I ii -l 

C'(TYP) 

I (TYi'.)(INSTi.U. i rl METeR 

I 

, 

uf'"tl) 

I -, _ AI I , -,; 

i 

I~I .00: 1: 

~ I 

I ii'S5 It .e 

i 

I 'tEL 

I 

- 

i 

HEADER 

''' AI:__ 

__ 

00 

4"IlUTTERFL"f 

i f:~ I 1= 'i I 

~ ¡; I i I I 10' ..&fly" I I i I I i I 1 ~ vALVE. (TYP) 

w. í I I ,-- I I ~_ " 

t ~ :; I A' '.L VALVHTYPY-' ! c! i I _ 1 w. I 

. 4~4S' ~ ~ I i 'I I- I I -- I I T ~ I I I T - ! ~' i- 

rl (~w g I I j lT r- I I ~iT I~"(TY) I I w i i ~iT i ~ Vw.f.~~~,'lAHHEL 

i ~,/ I I" II, ii, :¡~ii." I I "''i ¡II ~' i, -__~ "ill i i I ii: I " ~~ ii~' i i Ii ¡I: /~ = i 4EAOi:~ i Ii't' TO _,'".. 

~ "N ~ "N I I "N II "N V :;i;TTcIN6 TANic5 FINAL 

~ ,.11"' I Iil ~ I I iii --- I i f I I I ,. II , i I ~eL.IIú.oO 

I II - I I ',i ------------ i I ii ------------ I i ~ ~~ -4 +1 i 

I AERATI I TANK NO.3401 III AERATION i I TANK NO,5402 ~III AERATION I I TANK NO.3403 Ii : AERATION I I TANK NO.3404 II = I l i I I i' iii i l~ i ;;IJ ,I I ~: I I I i i II I i II I' Ii :lJ Ii 1 !' I ! i l- ~ 

I i I it! I I §llt+L-~~I~¡+~f"ANNEL 1 I if i I I II ~~I I 3 

~ 

i I 

II 

i i" 

III 

il 

I 

i i 

I 

i" 

11.1 

III ¡ 

I 

i 

I 

"iil 

J~i 

: i " 

I 

I: 

I, 

i' 

I 

I E 

i I ~ : I I i I I i-tf III III I i I II I I / i: I i I ¡ i II III I I , I II ''i c iE I ~ 

~i .~;;'2I-ei)' I 4-0' 4SPRA'iNO';:::l IIII " I, r~f-~~l~~.flNG III Ii 11¿~~~J~g~t5.E 11,1 II , ¡Ii i' ~ /' 

~~ "(~ ""-- i G 

i n 13-(; TY~ ~'3202-E;\ -IMn203 i; 'Af-320-i;) . 

,= J.~ sp¡.s S4"(" II / II i¡ATEIT'fP.) II 1 I _ rE'L 14,0 I 

I ~),l~_ It ~t.40Ies I I'I ~~ ~ ~2CS III ~~~ - IWi ~403CS iii A,k-~ ii~~oW4CS IllG4- ",-W 

1 L.-___l-_+.. 'x, ~:i =r~. ~ ~ L.---____.J.iIL iei x. ii i ~,Of.' 'L ll " i J.¿L II ?F,~zø-i;) -iL..i- I .+L_______~L_'________ .~ :~i~ III CF 32i; ~~~ ': '~~6m- III\~ /I~iy 

IN ALL 

" 'tl'-------- ~-------- '" ---;--- .~------il l-TOPOFTANi:5ELI750- -i /'- 

'-4' DRAIN 

B COMPAI/ENT5) VALVE 

C 

~ .~, 

(T'(PICAL ~ ~ . ~'.ri:Si.i.~3J1 *f 

~~, M~(' 

SCALE 

AS NOTED 

P.E. 

HAN AN SA\W 

Env Ei & Sc 


498 SEVNT AVE " NEW YORK NEW YORK 10018 

APPR FOR THE CI Of NE YOR 

PR MA 

P.E. 

P.E. 

CHIEF, DISION OF FACUTES DESIGN 

NOE: 

L- rOR NOTES SEE. OWG.M-3e. 

10 8 6 4 2 0 11' 

3/32'=1'-0' L.~ i 



BUREU OF ENGINEEING, DESIGN, AN CONSUCON 

RED HOOK WPCP 



''Xu",,, M'CRO'a.,¡o 1 

c",~r J'~ 

MECHANICAL 


TOP PLAN - EAST HALF 

RN.-= 

~~-- IOU~~fJ' ' 

I~TIr , 

KEY PU .~ 


SHEET~Of~ 

DWG. NO. RHFSM490

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

j 

~ 

l 

~ 

f 

2 

l 

~ 

l 

~ 

l" 

õ 

l. 

II 

:; 

~ 

l 

~ 

~. 

õ 

l 

~ 

~ 

l 

~ 

~ 

:; 

l 

~ 

S 5~ 

~ 

~ c 

~ 

¡j 

~ 5 ~:; 

~ 

S 

5 

¡¡ 

¡ 

¡ 

~ " 

~ ?i 

~i 

~i 

8 

UP 

'8RC 7,S' EA 

7TO 10.S' EA 

CD 

CD 


w_ 

rr IS A \tOlno CF SETI ~.2 (K TH NE '\ STATE 

EDTI LAW Fæ lN P£, ut ~ UN TH 

DlCT CF A LISE F' EN. TO ALTE -l 

N4 WAY PU. ft'I, PLTS cø RE TO Yi 

nI sv Of A PRAL EHEE HA SE AP F AN 

rT ll ll SE Of A PR DK IS ALTD. 

TH ALTE EH SH NF TO Tl Il H: SE AN 

TH NOTA'1 .ALTE BY Fa BY HI SllU 1H 

DATE AN A SP DE OF TH ALlET1 

3/16'=1'-0' 

! '" 

l 81 NO, OATE 

DESIGNED NB 

ISSUED fOR 

DRAYi ~ 

CHECKE ~ 

SECT.CHIEf ~ 

BY I PROJ,ENGR. ~ 

SCAl 

3/16'=1'-0' 

P.E. 

~i 

68'-6' 

HAEN 

Em En 

AN 

& Sc 

SA\W 


498 SEVNl AVE . NEW YOR NEW YOR 10018 

~i 

~i 

~i 

~i 

o o 

I 7'-8' I 

APOVE FO TIE CI OF NEW YOR CIT OF NEW YORK 


PRECT MAGE 

P.E 

P,E. 

CHIEF, DMSlON Of FAC DESJ 

BUREU OF ENGINEERING, DESIGN, iW COUC0N 

RED HOOK WPCP 



~i 

~1__7" 

3/16'=1'-0' 

LJi. I 

6 4 2 0 S' 

..~!._,__ f~wrl""n"'n-__~=---...~ (J-o''') r-i 

-¡41---- ¡ . .. l r:.'~'" "7 r 1. ~y i" . .'" ~ 1. '- £ 

! , ! -,' ;:';t~. t-1 

i. 

-1 

l i 

; 

t ~.~_.. ~.-...,_."" i ()...Jh¿l 

li 

- - "i ~ 

¡r--ll-'~'-'-~-r~-t~/' I 

. I r'''' 

Ii 1 Il i 

iL ii~__J_-4-- 

KEY PlA 


ARCHITECTURA 

SHEET~ OF~ 

GROUND FLOOR 

DATE MAY 2007 

DWG. NO. RHFSM500

I 

, 

, 

, 

¡ 

i 

r- 3' TRANSFER FIll IN 

~ ~ ~ 5' COTAINMENT PIPE T 

r- CHB273020 I' 

r- 2' FIll IN 4' 

COTAINMENT PIPE 

4' METERING PUMP SUCllON 

~ 

~~ 

II 

l5l 

~ 

~ 

8~~ 

~. 

~ 

~ 

~ 

~ 

'1 Ii 

l 

~ 

~ 

g 

~ 

~ 

~- 

ïi 

l 

~ 

~ 

l 

~ 

g 

ii 

ïi 

l 

~ 

~ Q 

~ 

~ 

il 

~ 

l 

~ 

~ 

i2 

i 

~ o 

~ 

l 

il 

~ 

~ 

l 

II 

~ 

¡ 

~ "ċ 

5.0 

2' TO CE TANKS, 

Cl B. 

Ell1.87 

FIBERGlSS 

STAIRS 

.A 

3' TO AERATION TANKS, 

Cl B. 5.0 

'0 

2 

On 

.. 

3 ) I 

.. 

IT IS A 'dOO a: SE no.2 a: TH NE YO STATE 

ED'O LAW fO Nf PE, Ul ACtl UN TH 

DlC1 a: A UC PR ENNE, TO AlTE ~ 

Nf WAY Pl, SPlK, PlTS OR RETS TO \I 

Tt so ~ A PRAl EH HA 8E N". F AN 

ITE 9E TH SE OF A PR 9I IS ALTE, 

TH ALTE aK 9W AFX 10 n£ ITI ll SE AN 

Tl NOTAlICt "AlTE BY Ft BY tI SKlU TH 

DATE ~ A SP OEl1 a: ni ALlET1 

¡ I 

DESIGNED -- 

ORA'I~ 

CHECKED ~ 

SECT.CHIEf ~ 

BY i PROJ,ENGR. -l 

fY 

SCALE 

'-FIBERGLASS 

RAil (Tl) 

Ii 

JI 


3/16'=1'-0' 

- - 

HAEN AN SAWY 

Enta Etrs & Så 

l\íl 

lilltrtl tt 

5RO 6.4' 

4TO 11.5' 

~ 

1 

HEAT TRACING 

APOVED FO THE CI Of NE YO 

& '" 

i 

8'1 NO. 

P~E. 

DATE ISSUE fOR 

3/16'=1'-0' 

P.E. 

HAEN AND SAWY P.C. 

498 SENT AVE 'NEWYORKNEWYORK10018 

PRECT MA 

P~E. 

CHIEF, DION OF FACIUES OESIGN 

COCRETE CURB-SEE 

STRCTURAl 

ì 

---,I 

i 

~ ~ ~ ~ 

,. 

II !iiiBi;, 

. . 

\\l ~'\ ~: 

'~ i 

~N -~ 

~.. 

~ 

ii 

I __1' TO INLET CHANNa, CL B. 5.0 

i. ~1' CHLORINE CONTACT TANK 

/' SAMPUNG UNE, Cl El 6.0 

-~ 2' TO CHLORINE TANKS, Cl EL 5.0 

2' TO 54' RAS, Cl EL 5.0 

I 

¡. 

__2' 

Cl 

TO 

B. 

AERAllON 

5,0 

TANKS, 

~ 

LE 

255041 

~ 

_3 

,(I 

2' FIll j 4' 

COTAIN ENT PIPE (Tl) 

3' TRANSFER FIll IN 

5' COTAINMENT PIPE (Tl) 

3/15'=1'-0' 

5 

LJi. 

4 2 0 5' 

i 

,._-l....--..-- 

~lF-=~pil oo~ cj 

l~--.- i 

it i ó- T--¡ 

ll-i-( ì 

II "~: ,~" iJ _~____J 

KEY PLA 



BUREU OF ENGINEERING. DESIGN, AN CONSlRUC 

RED HOOK WPCP 




MECHANICAL 

GROUND FLOOR 

DAlE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSM510

I 

/ 

I 

II,III, 

l 

I 

I 

I 

, 

I 

i 

I 

I 

i 

I 

, 

I 

I 

i 

I 

, 

I 

~ 

IS 

~ 

II 

t 

fi 

¡¡ 

IS 

~ 

II 

~ 

~ 

l 

2 

, 

IS 

~ 

~ 

~ 

fi 

5 

~ 

~ 

~ 

i 

~ 

~ 

ïi 

~ o 

~ 

~ 

l 

ii 

~ 

~ 

fi 

5- 

l 

¡ 

~ " 

~ 

c 

o 

E 

F G 

H 

2'FlLL'N~ 

4 ' CONTAINMENT PIPE, 

INV EL 34.91 

15'-0' 

18'-6' 

18'-0' 

13'-3' 14'-0' 

12'-7' 

I CAGE ACCESS 

i LAER (TY) 

n 

~ 

- \ - 

5 

~ 


II -------==- ___=.._-+_ 

:: ~ "'31 =========___ ___ 

- II ... 1" --~~ 1.1 -X-=---- 

-r 

m~:f: 

50% ALKAUNITY 

STORAGE 

TANK NO 

L 

L- 

CHB270020 

~ 

1 -$ 

1 

i I 

'- r+, r+, / 

~ I ~ 

PUMP SUCT, 

a. EL 7,42 

r4' TRANSf 

¥i 

8t 

3' TRANSf FILL l' CAUBRA liON OVEflOW 

IN 6' CONTAINMENT PIPE a. EL 35.25 

INV EL 34.91 

=====1 I 

II 

-----'1' II f-i=====~==3:ilhf~~ 

I" 111111111 III 

111111111 III 

:t:1I ~ :I! 

"' 

.. 

1;4' OF 

I ' 

g: METERING PUMP 

EL 1 

-$ .tC 

k4-~ 

/ ~ 

1'-6' 

:l: :l: :l: :l: 

111111111 III 

111111111 iii' 

111111111 III 

III 1I11!l ILL 

111111111 III 


111111111 III 

111111111 IIi 

111111111 Ili 

111111111 III 

111111111 III III III III 

III III iii ILL 


111111111 III 

Ili IIIIII iIi 

III JlIIII III 


111111 IIi 111 

~~~~ I 

T PIPE ' 

MMMiI1~ 

ili IlI Ili 111 :1: 

iii:i: III :ii ~ 

iiiiiiiiiil ''' 

111111111 Ii .!! 

't't't," R'i 

Ulu.... 

110 

~ 

i r I 

~'-O' 

ț 

~ 

113'-10' 

I 

~ 

II~ 

I- 4' EW 

ir ~ a. EL 12.95 

il l' CAUBRA liON UNE 

4' 

ëi EL 8.87 


a. EL 7.42 

3' TRANSFR IN 6' CONTAINMENT PIPE 

2' FILL IN 4 ' CONTAINMENT PIPE 

INV EL 33.41 ,___u_ ~- ~- 

r 4' EW, a. EL 20.67 

V r 3' EW, a. a 20.08 

EL 23.50 

4' EW TO CEN TANK 

a. EL 20.00 2' METERING PUMP DISCH 


a. EL 18,41 4' OF 

2' METERING PUMP DISCH 


a. EL 15.83 


'- 

1'-8' 

4' TRANSf PUMP SUC1' 


a. EL 7.42 

/ 



INV EL 34.91 I r3' TRANSfER INV EL 34.91 FILL 

i 

r3' TRANSf FlLL 

, 

i. 

h \ 

============ -===========1 I 

I ¡ ------------~-----------;; i 

4' OF 

~ 

rr,i 

~ ¡. I~ 

-~ i I 

, 

f4, ~ 

~ 

II 

M' 

i.. 

l- 

r , 

, I / 

I I 

~ ~ ~ 

~ ili 

rf, / '- ,+, / '- 

, 

,,, 

.. 

SECTION A 

i/4'~1'-O' B-M 

_""1l 

IT IS A 'oll Of SE 72 Of TI NE Ym STATE 

EDTJ LAW FO li PER, UH AC-mÇ UNO£ TH 

DlC1tw Of A UC PRAL ENEE, TO AllE ~ 

Nl WAY Pl SPCFTK PLTS æ RETS TO 'M 

TH 

IT BE 

SE 

TI 

Of 

SE 

A Pf 

Cf 

EH 

A PRAL 

HA BE 

DI 

AP. 

IS AlTE, 

F AN 

1H ALTE EH Sl Af 10 TI fl tI SE JH 

TH NOTATl 'Al1E BY fa. BY i- SlnÆ TH 

DATE AN A Sf DE~ Of 1H AlTETI. 

ORA \I -- 

CHCK -- 

SECT.CHIEF ~ 

PROJ.ENGR. ~ 

l '" 

i 

:31 NO. BY 

DESIGNED -. 


SCALE 

1/4'=1'-0' 

P.E. 

HAN AN SAWY 

8iWo Enii & Scen 

HAN AND SAWYR. P~C. 


APOV£D FOR TH CI OF NEW YORK 

PRT MAGER 

P.E. 

P.E. 

CHIEF, DMSION Of FACIUTES DESI 



BUREU OF ENGINEERNG, DESIG, Nl COUCON 

RED HOOK WPCP 




MECHANICAL 

SECTION 

SHEET 1 

~ 

cp 

4' 'Æ 

a. EL 34.67 

I 

, 

I 

i 

I 

i 

lí 


a. EL 20.50 

(3)2' METING PUMP DISC 

IN 4' CONTAINMENT PIPE EACH 

¡NV EL 19.83 


a. EL 19.50 

l' NaOCL IN 3' CONTAINMENT PIPE, 

a. EL 14.87 

L 

Ie- 

'1)1' HYPO IN 2' CONTAINMENT PIPE (FAR) 

'3)2' EW/HYPD IN 4' CONTAINMENT PIPE 

10. EL 5.0 

EL 2.00 

1/4'~1'-D' 

10123 i I I I I 7' I 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHFSM520

j 

, 

I rl 

, 

'Î 

g i; 

~ 

~ 

l 

~ 

~ 

., 

~ 

~ 

i 

~ i! 

~ 

8 ~ 

l 

§~" 

~ 

~ 

~ 

A 

~ , 

~ 

g 

~l 

- -- ft 

~8~~ 

, 

Ii 

l~ 

;lt 

l 

~ 

~t 

l~ 

it 

l 

~ 

4.. I 

'f' 

Ii 

g 

l 

~ 

l 

~ 

-( 

! 

~ 

~ 

~I NO. 

;. , 

vt0 i 

~j 0 , 

"0 

-. 

6 

TO RSP BREAK 

TANK, SEE DWG NO. 

2G-CVL-UTL-C21 __ 

~="~ 

LCS-OBJ113 I / 

lCS-OB311 ~ 

l 

~ 

60' AIR HEADER 

- 

TO AEATION 

TANK 

WA_ 

IT IS " \1T1 OF SE 72.2 Of TH NE '1 STATE 

EXll L.W Fa NN PE, UtI ~ lN Tl 

DI Of A UC PR ENNE TO ALTE IN 

Nf WAY PI. SPClTK, PUiS OR RETS TO \I 

n£ SE OF A PRAl EN HA BE M' f' N- 

I1 Bf THE SE OF A ~ EN 1$ ALTE, 

Tl Al1t EN SH AFX TO n£ IT HI S£ NI 

11 NOTA1l 'ALTE 9Y fa BY ll SlAll Tl 

DATE AN A SP OETK Of TH ALlETl 

DATE ISSED FOR 

B 

B c o E F F.1 

G H 

170'-0' 

~ 

, 

20'-0' 14 -0' 29'-0' 29'-0' 29'-0' 18'-4' 10'-8' 20'-0' 

1. FOR ABBREVATIONS, S'BOl AND GEERAl 

NOTES SI DRAl\NG 2G-PFD-GE-FOI 

- --:i :i 

~ c: c: c: c: c: 

'II~ 

o 

M~~E rr' 

¡ . Q, 

Lr\ 

upllll 

~ 

ID 

¡SWITCHGE 

, R~' a~ 

T BL&~ T LJ IT/COCRET 

----~l---l~-----l--l~---- 

4' 

~ 

, , I 0 0 

"""""I'F 

~ 

o 

. 

~:i~. --t:iii-- 

I 

2'-2'(TI) 

l -O'(TI) 

NOTE: 

z - 

2. COUPUNGS SHAl BE 

FlXE X EXANSION (FX) 

F1X1Bl, AIR TIGHT (EXE 

AS SHOVi. 

INDICATES FlXED TI 

PIPE SUPPOT 

INDICATES SUDiNG TY 

PIPE SUPPORT 

l 

3: 

UP Ji V 

36' DISCHARGE SILECE (TI) 

r- r- ~3: 

l---.~n"~(~) 

j r-LCP 390100 r 

3: 

VVM 4' SII '3' i 3' 

~ 

TI s.¡- 

." "" t: 

, ,- 

i. lo 

, , , , '" 

'~ ¡¡ ~-~ 3' SV IT UP (TI) ,, Ë 

II II I I 

+---+ ----+---+ 396100 

42' 

36 DISCHARGE PIT 

ii--~ir----i--ir---- i I 

ft 

_ 

:fif .. .. ~ 

v.. jjf 

UP TO BLOWER (TI) 396100 

P j' I' I' L' i" , EQ~IPMENT ACCESS (ABO'Æ) 

----lti-¡lt----i 42' INLET SILENCER (TI) 

. 

~ -~ 

LA~) )T 

3' I V I, !i 

BLOWER COONG 

WATER SYSTEM 

FOR INSlRUMENT A TION 

SE DWG. 2G-1 Ie C-BlW-IO 

, " , 'i UNDER COlRACT 

10'-7' 7'-0' 5'-5' SEE 2P PLUMBING 

I t~ilOW-OFF I I I W~M I I (TI) (TI) FlT-901oo 

DESIGNED -- 

ORAVi -- 

CHECK ~ 

SECT.CHIEF ~ 



8 6 4 2 0 8' 

1/8'=1'-0' ~.. I 

'-1irrr~_~-- '1_,"" 

r;..L - XRQ: ~ L _j 

~if~-i Ii . i ¡ ()~q8lT;~ 

o.Ok,..g/ I 

It.. 

¡r-l---ilr 

k___..,~ r 

i 

I 

ii -i ! 11 i 

lL -~;;~~,¡ 

KEY PLA 

SCALE APOVEO FOR TH CI OF NEW YOR 

DATE MAY 2007 

AS NOTED 

P.E. 

HAN AN SA\W 

Ennt Enir & Sc 

HAN ANO SAWYR, P~C. 

49 SEVNT AVE . NEW YOR NE YOR 10018 

PRECT MAGER 

P.E. 

P.E 

CHIEF. OMION OF FACES DESIGN 



BUREU OF ENGINEEING. DESIG, AN CON 

RED HOOK WPCP 




MECHANICAL 

GROUND FLOOR 

DETAIL PLAN 

SHEET~OF~ 

DWG. NO. RHFSM530

I 

i 

I 

I 

A 

B c D E 

F F.1 

G 

H iZ 

170'-0' 

~. 

i :; 

~ 

~ 

s 

j 

~ 

~l 

il 

:; 

~ 

~ 

i 

¡ 

:i 

" 

~ 

! 

% 

§ 

~ 

l 

~ 

l 

~ 

'" , 

;i 

~I NO. 

-- 

~f 

i 

~ 

L,r\ 

~ 

, 

i 

!i 

2 

.. 

b 1 

~ ~If I ~ 

~ 

D-1 

---IH 

i 0 

~~ 

.. .i 

i 

l 

~ 

ei 

5- 

õ :: 

t 

l 

~ 

l 

~ 

t 

i 

i~ 

l 

1 

j¡/ 

I tlÆ 

b , 

;i 

-- 

'E- H 

5 ¿ --- H _ __J 

~I 

BL 

6 1 ' , -JI~ 

- 

IT tS A \4TI Of ~ 72 rs TH NE Yæ STATE 

EITK LAW fæ NN PE. UM ACl UN TH 

OIC1 Of A UC f' OlNE, TO ALTE IN 

N( WAY Pl, SPCl11, PlTS Of RE TO 'M 

Tl SE Of A PRAL EN HA SE AP. F AN 

IT 8E TH SE rs A PR EHEI tS Al1I, 

Tt AlTE EH 9i NF TO Tl IT ll SE NC 

Tl HOTATK 'AL1I ~ FO BY Hl Slni, TH 

DATE IH A SP 0E Of TH ALTET1 

DATE 

ISSUED FOR 

T 

i 

I 

20'-0' 

II T99 rI 

IAI 110Tcp-080130 i LCP-0815C 

LCP-080120 LCP-08140 i- 

b 

ON 

L---~1 

I1 

r---------.. 

c: 

HRU 

DESiGNEO ~ 

DRA\l~ 

CHECKED ~ 

SECT.CHIEf ~ 


SCALE 

I 

AS NOTED 

14'-0' 29'-0' 29'-0' 

II 

(A 

~~ 

D-LCP 390100 

IrI 

PREFLTR! (TY) ~ 

P.L 

ACS-02 J L 

CONTROL ROO r 

REMOTE I/O 

089010 

FLOO MOUNTED 

__--___ LCS-O~l1 

m 

086010 

-02 

I PDISH 

SECURITY HARDWARE REMOlE I/o 

NEMA 12 ENa.OSURE ~110 REMOTE I/O 

~ ~120 

I ) 

~~~=~:=~~::i 

PROCSS AIR FlLTRS (TY.) 

INS1RUMENT A TlON SHOII 

ONE FlL TE SYSTEM 

FOR OlHER FlL TERS SE 

DWG. 2G-I.I C-BLW-IOl 

HAEN AN SAWY 

Ei En & Sc 

HAEN AND SAWYR, P~C. 

498 SEVNT AVE . NEW YORK NEW YORK 10018 

~ 

I 

IDDDDDI 

MCC ROOM 

L T/CONCRET 

EL 29.50-i 

BLW0803J 

~ 

I í: 

,~ 

L 1 

APVE FOR TlE CI OF NEW YOR 

PROJECT MA 


P.E. 

P.E. 

CHIEF, OMSI OF FACIS DESiGNOU 

1 

1 

( ~ 

-W 

T 

1 

, 

29'-0' 

6J 

UPPER BLOWE ROO 

BLWOao2~ ~ 

r 

I 

18'-4' 

HVAC 

ROO 

D~ 

-i .. 

A .. 

I: 

§ 

LAIR INTl 

(MMIr 

1 

J 

ru 

i- 

~ILi 

BLW0802~ ~ n 

~~ 

-- 

~WE 

BLW080150 

~ ;¡ff ~ 

i gr 1 

I ",i 

J;~' 1 

( ii~ "r J~ 

-f ~ L i 

AIR SHAF (TY) 

10'-8' 



BUREAU OF ENGINEERING, DESIGN, AN CON 

RED HOOK WPCP 



i- 

Lw 

T1 

I 

u 

20'-0' 

STORAGE 

i- 

i- 

-i1Il--- 

-iHIIl--- 

NOTE: 

f(i i- 

SW TO OIL COOR (TY) 

"ìiii--- 

T 

i 

I 


MECHANICAL 

SECOND FLOOR 

DETAIL PLAN 

S'M (TY) 

LUBE OIL SYSTE (TY) 

SEE OWG. 2G-I.lC-BLW-103 

FOR INSTRUMENTATION. 

24' DISCHARGE (TY) 

42' INlE (TY) 


SE OWG, 2G-I.I C-BLW-102 

FOR INS1RUMENTA TlON. 

(TY) 

1/8'=1' -0' 

8 

L... 

6 4 2 0 

I 

8' 

.. ...- 

~IJfJlJ~'J.---~- 

, iDC' i 0 . (i ODr~i ' . Y:: L. ~ 

l~ 

I 

~ 

r-~(r' 

i i58Qgr-~---i 

i ! Ii i I 1.1 J 

~KEY PLA 

DATE MAY 2007 

SHEET~ OF~ 

OWG. NO. RHFSM540

I 

I 

r 

I 

r 

I 

r 

I 

I 

i 

I 

i 

r 

i 

I 

i 

i 

I 

I 

i 

i 

i 

I 

I 

I 

i 

I 

TOP OF ROO 

EL 57.83 

TOP OF ROO 

EL 47.50 

B 

i2 

~ 

l 

~ 

~ 

~ 

~ 

; 

l 

- 

~ 

l 

i2 

S' 

¡ 

~ 

TOP OF SLB 

EL 29.50 

~ '" TOP OF MAT 

EL 11.50 

~ 

~ 

.//. 

~ 

ïi 

S)\;;)0y"'" " ' 

~ o 

~ 

r 

:¡ 

~ 

l 

il 

i l 

l 

§~" 

~ 

"" 

IT lS A i.no C6 SE 72.2 a: TH I£ 'l STATE 

==~~~~~Df,, ~~~ 

Nl WAY Pl, SPT1 PlTS OR Rf TO .. 

fl 

mE 

eE 

SE 

TH 

Of A 

sa 

f'AL 

OF 

EN 

A Pf 

HA 

EN 

æE 

IS 

AP. 

Al1E, 

F AN 

TH AI TE EN Sl N' TO TH I1 tI SE lH 

n£ NOA'O 'AlTE BY Fa BY llS SlnJ, 1H 

DATE N* A SP DElK Of TH AlTETI 

L. 

! 

l; 

~I NO. DAlE ISSUE FOR 

~ 

~ 

~i 

15 TON BRIDG CRANE 

1 

1 

1 

T 

hi 

i 

In 

i 'r; II 

~ 

° 

r 

II 

MCC ROOM 

UPPER 

BLO\\ 

ROOM 

36'x24' REDUCER 

R 

- 

l. 

/V/,y 

r~"" v"-" v," " ' 

SWITCHGER 

La 

o 

R 

Cl 22.50 

Cl 21.50 

36' DISCHARGE 

Cl 15.17 

l. l. l. 

J 

rJ~~ Jl 

L. 

li 

1 

DESIGNED ~ 

DRAYi~ 

CHECKED ~ 

SlCT.CHIEf ~ 


SCALE 

AS NOTED 

P.L 

HAEN AN SAWY 

En Enrs & Sc 


498 SENT AVE 'NEWYORNEWYORK10018 

NOTE: 

ri 

~ ~ 

. INDICA 1E AXE lì 

PIPE SlPPORT 

o INOICA lES SUDING n'E 

PIPE SlPPORT 

1/ 

L. 

II 

BLOWE 

BLW080130 

(NOlE 1) 

.8 

JT 1 

il 

(L 

m9 

1 

HR 

~ 

,__ ~~ 42' LR 90' 

__ _" BENO (n') 

$-- 

II 

. 

-j 

II 

T 

1 

-8- 

I 

I 

i 

I 

l- ~ I- 

__L_ r----, __L_ r., II 

iL~---I---..J1 ! I 

II 

(*1 i-nD Ir 

¿~_ ,1 (~/~/I 1 ~\ \ i L 

__~~====b II 

-ii 

L 42' INLE i 

SILENCER (n') 

:. L. L. 

SECTION ~ 36' OISHHARGE 

o o 

Le 

T 

o . 

ii~~~:: 

U JONT (n') 

I l~rnoo. I 

~ 

.)\ /.7/Y V': V'"ì' 

~'~~.. 

i 

AIR ~ 

PLEUM 

I 

Hr"""' 

I 

TOP OF CRAE RAIL 

EL 48.83 

24' BLOW-Of 

Cl 23.17 

60' AIR HEAOER 

Cl15.17 

i ~ 42' INLE 

~Cl21.83 

S~"\'Y'" 

L. L. 

L 

1/4'=1'-0' 

APOVEO FO THE CIT OF NEW YOR 

PROJECT MAR 

P~E. 

P~E. 

CHIEF. DMSJOI OF FACES DESIGN 



BURE OF ENINEERING, DESI, AN COON 

RED HOOK WPCP 




MECHANICAL 

SECTION 

1 i 0 I 1 I 2 t 3 I 7' I 

DATE MAY 2007 

SHEET~ OF~ 

DWG. NO. RHFSM550

I 

~ 

~ 

i 

~ 

~ 

¡¡ 

i¡ 

~ " 

~ 

~ 

! 

.3 

~ 

l 

!ši 

§ ~~ 

~ 

PLAT 

INFlUENT 

~ " 

~ 

âi NO. DATE ISSUED FOR 

MECHANICAi 

.. 

IT IS A -.TI (J SE 72.. a' THE NE lt STATE 

EDTI LAW FO Nf PE, Ull ACNC UH TH 

DI Of /I I. PR DI, Tn ALTE IN 

AN WAY ~, SPTl, PlTS OR RE TD 'I 

TH SE Of A. PRAl EH HA BE AP F AN 

rr BE TI SE Of A. PR EH IS AlTE, 

TH ALTE D. SH N' 10 TH nn lI SE AN 

TH NOTAllOO .AlTE BY Ft0' BY tl SllU Tt 

DA~ Al A SPCS OEl1 Cf TH AllEll 

- 

Red Hook MBR 

PLAT INFlUENT PRIMARY SENG TANK INFlUENT 

GRA i"TY THICKENER 


Annual Average Conditons I I I PRIMARY EFUENT SETING TANK I O~LOW I I I I 

AERATION TANK AEATION TANK 

INFlUENT EFFUENT 

I MBR INFlUENT I MBR EFUENT I PLAT EFUENT 

FlOW (MGO) 32.9 35.2 34.9 4.5 0.1 104. 0.2 39.5 91.7 91.7 I 39.3 I 39.3 

is (m9/L) 199 181 11 150 186 14,B71 14,871 116 8,501 8,501 

is (ibjd) 54,700 54,700 32,40 5,700 180 12,953,800 28,50 38,2BO 6,505,500 6,505,500 0 0 

CBO (mg/L) 142 129 111 68 65 3,314 3,314 106 1,895 1,895 1. 1. 

CaOD (Ibjd) 39,000 39,00 32,40 2,600 63 2,8B7,200 6,400 35,063 1,450,40 1,450,40 400 40 

1N (mg/L 31.7 28,8 26.5 25.0 547 911 911 27.7 522 522 2.5 2.5 

1N (ibjd) 8,700 8,700 7,700 90 530 793,50 1,700 9,130 399,300 399,30 BOO 800 

BAR 

SCREENS 

(4) 

SCEEINGS 

TRUCKED 

.; .;.; 

, , 

MAIN SEWAGE 

PUMPS (6) 

PRIMARY 

SENG 

TANKS 

(4) 

.._.. SECONDARY 

I BY-PASS 

1 

1 

I 1---------- 

I 

, 

1 

I 

I 

1 

1 

1 

I 

I 

I 

AEATION 

TANKS 

(4) 

MEMBRANE 

B/OREACTOR 

TANKS 

(12) 

RECYCl 

PUMPS 

I 

1 

1 

li 

I 

I 

I 

I 

1 

1 

I 

1 

I I I 

I 

..----ï--.i--ï 

i 1 I 

--~~~--~~---_~-_~~~-_~~~~~~-_~~~-_~~~~~~~~~~~~~~~~~~~~~~~~~-_-_~~-_-_~~-_-_-_-_-_-_~-_~-_~~~~~_________ 

GRIT 

TRUCKED 

l T T 

----- -------------------- ___J 1 I 

CHLORINE 

CONTACT TANKS 

(2) 

PLAT 

EFUENT 

(2) 

SlUDGE CAKE 

DISPOSA 

(2) 

BY 

DESIGNED -- 

ORAYi -- 

CHECKED ~ 

SECT.CHIEF ~ 

PROJ.ENGR. ~ 

SCALE 

AS NOTED 

P.E. 

HAEN AN SA\W 

APVE FOR THE CI OF NEW YORK 



BUREU OF ENGINEENG, DESIG, AN coNSmucN 

RED HOOK WPCP 



P.E 

Ei En & Sd PRECT MA 

MEMBRANE BIOREACTORS 


4SSEVNTAVE. NEW YOR NEW YORK 10018 

P.E. 

CHIEF, DIVISIO OF FACILS DESIGN- 

FLOW DIAGRAM 

MASS BALNCE 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHMBR540

I 

I 

\ 

- 

i 

!i 

3 

¡¡ 

~ 

~ 

S !$ 

~ 

~. 

~ 

~ 

S 

5 

~ 

~ i¡ 

" 

~ 

1; 

~ 

! 

;. 

~ 

S 5 

l 

~:i 

" 

~ 

~ '" 

~ 81 NO. OATE ISSED FOR 

'20 

.. 

rT IS It WJll Cf SE 72 fS TH NE læ STATE 

EI~ LAW Fa NN PE, UN AC UNX 1l 

DI Of A uc Pf EN, TO AiTE IN 

N( WAY Pl, SPCITI, PlTS OR iv TO -l 

Tl SE Of .. PRAL EN HA BE AP. If AN 

nE BENG TH S£ Of A PR EH ts ALTE, 

TH ALTI ENEE Sl N' 10 TH na HI SE AN 

Tl NOTA'T 'AlTE BY FW BY tI SlTI Tl 

DATt Nl A SP DE OF TK ALtETI 

woo. 00 

BY 

C: 

QJ 

i 

i 

Q 

I 

QJ 

i 

DEGNED -- 

ORAII ~ 

CHECKED ~ 

SECT.CHIEF ~ 

PROJ.ENGR. ~ 

GALLRY 

EXlSTlNG 

PRIMARY SEfflNG 

TANKS 

r- - 

I 

I 

I 

-l EXISTING 

MAIN BUILDING 

NEW ~BR TANKS IN EXISTING FST FOO1PRINT 

BLDG. 268 

MOOIFlCATIONS TO EXSTING AEATION TANKS 

SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

En Eii & Sc 

HA AND SAWYR. P.C. 

498 SEVNT AVE ' NEW YOR NEW YORK 10018 

APOVE FOR THE CIT OF NEW YO 

PREC MAR 

P,E. 

P,E. 

CHIEF, DNSIDN OF FAciES DESiGN- 

CHEMICAL HANOUNG BUILING 

\i- 

- 

EXISTING 


TANK 



BUREU OF ENGINEERING, DESIGN, AN CONS 

RED HOOK WPCP 



-- 


II 

II 

____~_ir_ 

; 

,I 

J J. 

tZ 

UMITS OF CONS1RCTION 

1'=30'-0' 

30 1_1... 15 0 30' I 

CIVIL 



DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHMBR550

i 

I 

I 

l 

'1 

~ 

l 

2' 

~¡¡ 

,. 

~ 

'f' 

¡¡ 

; 

l~ 

~ 

~ 

't 

~ 

~ 

~ 

¡¡ 

,. 

~ 

1 

g 

~ 

~ 

l 

~ 

~ 

j 

~¡¡ 

l 

B 

¡; 

G. 268 

'i 

l 

~¡; 

i 

~ 

o !l 

ß 

~ g¡ 

5! 

~ 

l 

~¡¡ 

,. 

l 

g". 

., 

~ 

! 

I- .. 

u 

r 

i 

------;-o 

r- 

~ 

- 

r 

- 

.f 

~- ~ 

=u 

UJo 

il -,. - =F- 

I 

'- 

l 

a I NO. DATE ISSED FOR 

! II 

.. 

IT IS A i.TK a! SECTK 72.2 a: T1 NE '\ STATE 

ED1I LAW FO Nf PE, Ul AC UND TH 

DlC1 Of A I. PR EN TO ALTE IN 

Nl WAY PI, SPClT', PlTS OR RE 10 Yl 

n£ SE Of A. PfAL EN HA BE N" F .- 

IT 8E nl SE Of A PR DQEt IS AL1E, 

n£ ..TE ENEE st AFX 10 1H IT l- S£ Nl 

n£ NOTATK "AlTE BY ft BY tI Sl1U TH 

DATE No A SP 0E CF TH ALmlTI 

DESIGNED -- 

ORA\\ -- 

CHECKED ~ 

SECT.CHIEF ~ 

BY i PROJENGR. ~ 

SCALE 

AS NOl£D 

EXISTING 

MAIN BUILDING 

rr= 

--,-~ 

i- 

+----.¡t 

, , 

'- ri ri ri i- r-; 

iii~' 

iI II, 

I , , 

I: 

~ 

,,-+ 

ḷi, i :1 : 

:: 

1 

i . II I!I I rr 

:1 : 

g j 

I 

, 

, , 

I 

I 

L_ --------------~ ~ 

~ -" 'D 

EXISTING 

ḍ Î 

CHLORINA TION 

BLDG. 

EXISTING 


TANK 

;: 1!J 

I 

III! 

, " ', 

r 

J 

.~ 

ii :i, 

"" , 

L- 

21'1-0' 

ê 

4'-0' 

-i 

P.E. 

HAEN AN SAWY 

Er Enrs & Sc 


498 SEVNT AVE 'NEWYORKNEYORK10018 

APVE FO THE CIT OF NEW YORK 

PROJECT MAER 

P~E. 

P£ 

CHIEF, DMSIO OF FACImES DESIGNTH 



BUREU OF ENGINEERING, DESIGN. AN CONSlUCON 

RED HOOK WPCP 



'2' 

o odoN 

Z 

20 I -- 10 -- 0 20' I 

l-~--l-- 

1'=20'-0' 

t 

I. 

l¡ i 

r 

Q-QQ/ 

Ii I II I II .. 

i. 

KEY PlA 

~LJUl- 0000 r-- 

'-FijT- XOO b¡ r-9 

I \~.-l i-.. , 

ír---i:/ ¡ 

CIVIL 


DATE MAY 2007 

SHEET~ OF~ 

owe. NO. RHMBR560

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

I 

i 

yi 

~i 

~i 

2 

/; 

(0 

'" 

~ 

l 

~ 

, 

If 

¡: 

l 

~ 

l 

~ 

If 

t 

CD 

¡: 

l 

~ 

~ 

ß 5~ 

f 

l 

¡: 

II 

:: 

~ 

l 

~ 

1 CD 

:; 

l 

~ 

5 

ß 

¥ 

i 

~ 

~ 

~ 

l~ 

l 

l 

l¡:; 

"" 

IT tS A l.TK CF SE 72.2 Of TH HE 'l STA.TE 

EDTl LAW fO Nl Pf, UH ACT UN TH 

OICT a A UC PR EH 10 ALTE .. 

AH WAY Pl, SPno PlTS OR RETS TO 'M 

ll S£ CF A PRAL EN HA BE AP F AN 

lTE SE TH SE Of A PR Dt IS Al1!, 

TH AI'T DØ 9l N' 10 TH ITD ll SE AN 

THE NOTA1I "AlTE BY" FO BY HIS SlnÆ TH 

DATE AH A SPCF OETl Of 1l AllE1I 

I 

i 


3/16'=1'-0' 

" 

DESGNED ~ SCAL 

~ 

DRAII -- 

l " CHECKED ~ 

3/16'=1'-0' 

SECT.CHIEF ~ 

~ 

ãi NO. DATE ISSD FOR PROJ.ENGR. ~ 

BY 

P.E. 

~i 

68'-6' 

HAEN AN SAWY 

Ennt ~ & Sc 


498 SEVml AVE ' NEW YOR NEW YOR 10018 

~i 

~i 

~i 

cr 

i 

"0 "0 

I 7'-8' I 

APOVE FO llE aTY OF NEW YORK CIT OF NEW YOR 


PROJECT MAGE 

P.E. 

P.E. 

CHIE, DMSON OF FACES DESIGNOU 

BUREAU OF ENGINEERING, DESIG, AN CON 

RED HOOK WPCP 



~i 

~I__ "cr' 

3/16'~l-O' 

6 

u- 

4 2 

i. 

0 5' 

i 

~~,-----, -l_jlil/L.-r~-= _ 0'00 l r - - -- ¡ ~ ~ (¡'-C) C)f.. 

il ~ ì ¡ ct.JCLrJ L l 

I r:'~T::":~:::':~'-~-p ..~r~/ I 

Ii' H !II~ 

" j ¡ 

I f, ii 

___E-."'--.-. ! 

tk_._'"____._~ 

KEY PLA 

GROUND FLOOR 

DATE MAY 2007 


ARCHITECTURAL 

SHEET~Of~ 

OWG. NO. RHMBR570

ï 

i 

~. 

¡i 

l 

~¡¡ 

l 

~. 

~ 

~ 

¡¡" 

~ 

., 

~ 

¡¡ 

t 

l~ 

~ 

~ 

l" 

¡¡ 

~ 

l 

~ 

~ 

~ 

g g 

¡¡l 3' TO AERATION TANKS, 

l~ a. EL 5,0 

~ 

~ 

~ 

i 

" 8 

S:; 

i¡ 

~ 8 

~ ~ ~ ~ ~ 

I I 

~ ~ ~ ~ 

I cm"~ I,"~~' ir ,~""~, ~~~ I 

I 

i i 

I 

I I 

i i 


2' FlLL IN 4' 

r CONTAINMENT PIPE 

i I I I 

I I I I 

I I I 

2' FlLL ,I 4' 

COTAIN ENT PIPE (TI) 

3' TRANSFER FlLL IN 

6' CONTAINMENT PIPE (TI) 

l TO INLET CHANNa, CL a 5.0 

l CHLORINE CONTACT TANK 

SAMPUNG UNE, a. a 6.0 

-~ 2' TO CHLORINE TANKS, a. EL 5.0 

2' TO 54' RAS, a. EL 5.0 

2' TO AERATION TANKS, 

a. a 5.0 

3/16'=1'-0' 

6 

L... 

4 2 0 5' 

i 

~ 

l il 

~ 

~ 

~ 

l 

¡~" 

~ 

l '" 

l 

81 NO. 

w"" 

IT IS A. IMnc Cf S£ 72.2 Cf nÆ NE 'I STAlE 

EDnc LAW FO Nt PE, UN ACHG UN lH 

DI Cf A IJ PR EH, TO AlTE .. 

IN WAY Pl, SPClTl PLTS OR RE TO 'M 

Jl 

TH 

æA 

SE 

TH 

Of Ji 

SE 

~N. 

Of 

Di 

A 

HA 

PR 

BE 

~ 

Af 

as 

F 

JrTE, 

AN 

TH .lTE EN 5l NFX TO TH IT HI SE AN 

TH NOTA'O 'AlTE BY fa BY i-s 9Gl1 TH 

DATE .. A SPCl D£no Of TH .lTETK 

DATE 

ISSUED fOR BY 

DESIGNED -- 

DRAII -- 

CHECKED ~ 

SECT.CHIEf ~ 

SCALE 

3/16'=1'-0' 


3/16'=1'-0' 

HAEN AN SAWY 

En En & Sc 

HA AND SAWYR. P.C. 

498 SENT AVE 'NEWYORNEWYOR10018 

P.E. 

PROJENGR. ~ GROUND FLOOR 

/"-rllJ~ "hÌ'''~'_~ 1 

-- ì~j--,., JtJ"'~~gg~"I 

~ ~~~_.____ ~.. '- _ 

1'F="' ! 1 0'-00 ~.; 

t-~J L~_.J O..Qgtr , 

Ii 'I H g ii . 'II 

1i--'-r~.ì-'-"--n(7J 

!);._~---~~= 

...__,"-__ ' ~ !l 

APROVED FO TIE Cf Of NEW YOR CIT OF NEW YORK 

DATE MAY 2007 


PREC MAGER 

P,E. 

P~E. 

CHEF. llSI Of FACiuES DESIGN- 

BUREU OF ENGINEEING. DESIGN, AND COUC 

RED HOOK WPCP 

CONCEP1UAL DESIGN 


KEY PLA 


MECHANICAL 

SHEET-. OF~ 

DWG. NO. RHMBR580

I 

I 

i 

I 

, 

I 

I 

, 

I 

, 

i 

, 

i 

I 

, 

I 

, 

I 

2'FlLlIN~ 

4' CONTAINMENT PIPE, 

INV EL 34.91 

c 

15'-0' 

D 

18'-6' 

E F G 

18'-0' 13'-3' 

14'-D' 

H 

12'-7' 

CT 

~ 

i5 

t 

l~ 

~ 

~ 

5i 

i5 

t 

l~CI 

!J 

~ 

2 

, 

i5 

~ ~ 

CI 

!J 

~ 

~ 

~ 

f 

!! 

s 

:ö 

i¡ 

~ o~Ii 

1 

j 

I , CAGE lAER ACCSS (T') 

25,000 GALONS 

SO% AlAUNITY 

STORAGE 

TANK NO 

CHB270020 

-$ 

~ 

L- 

PUMP SUCT, 

1ir4' Cl TRANSf EL 7.2 

3' TRANSf FIll l' CAUBRA 1l0N O'ÆFLOW 

3' TRANSf FIll 

IN 6' COTAINMENT PIPE Cl EL 35.25 IN 6' COTAINMENT PIPE 

INV EL 34.91 INV EL 34.91 

i i 

ti 

~ 

~ 

/ 

=====1 I 

" 

-----'1' " 

rli=====~==3:i1~~~ 

Id 111111 III III 

111111111 III 

:l:W ~ 

.. 

"' 

Ir 4' OF 

*~il:;~1/ 

i I , I' , 

T PlPE-i ~ ~ f,L 

METERING PUMP 

-$ -' CELl 

~ 

1'-6' 

'l' 

i i 

'l' 

I I 

'l' 

I i 

,I, 

iii 

'r 

lil 

:d:i::i: iii ~ 

1111111111 III 

III III III U A il 

110 

I 

, 

ț 

3' TRANSFR IN 6' CONTAINMENT PIPE 

2' FIll IN 4' CONTAINMENT PIPE 

INV EL j3.41 

I 

i 

, 1l*~31 =~=== 

============~===========¡ I 

J, 

ll :11 :11 IJI 

111111111 ILL 

111111 III Ili III III 

~ 

111111 lit III III III 

III 111111 IIi I 13'-10' 


i : 

111111111 III 

1'-8' 

1I1111l11 III 


Itllllill III 

II/III III ILL 

111111111 III 


III 111111 ill 

llilltlli III 

l¡ 

m 

I;; 4' EW, Cl EL 20.67 

:.: 

.. 

. r3' EW, EL Cl 23,50 EL 20.8 

111111111 ILL 

111111 III ILL 


III IIIIII III 

4' EW TO CEN TANK 

Cl EL 20.00 2' METERING PUMP DISCH 


Cl EL 18.41 

2' METERlNG PUMP DISC 


4' OF 

Cl EL 15.83 

IrT,1 

~ 

I- 4' EW 

2' REUEF VA\A DISCHl' 

CAU8RAllON UNE~ 

Cl METEING PtMP 

In "F Cl EL 12.95 

II l' CAU8RA 1l0N UNE 

-~ 

fe .a 


~ 

4' 

ëL EL 8.87 


Cl EL 7.42 

I 

~ / 

i r I 

4'-D' 

SECTION A 

1/4'~l-O' B-M 


I r3' TRANSÆR INV EL 34.91 FIll 

, 

i 

I.. 

4, S~ U 

H ORIlE 

T 

I K NO 

II CH 260040 

~Ji' ~ON 

(3)2' METEING PUMP DISC 

=-=:b--=====f==3o======='i :~V4~LC~~~'NMENT PIPE EACH 

I~ 

I 

~ 

vr' 

r 

,,,,,IỊ 

I II, 

.. 

r , 

I , 

I 

/ 

II: l' CHLORINE CONTACT TANK SMIPUNG UNE 

I:: Cl EL 19.50 

~ l' NaDeL IN 3' CONTAINMENT PIPE, 

!I! Cl EL 14~87 

__ -__=:1,, 

--~---11: 

! 

~ 

:l 

!I 

~ 

il 

4' \I 

Cl EL 34.67 

rn l' CHLORINE CONTACT TANK SMIPUNG UNE 

VI I Cl EL 20.50 

L- 

~ 

Ie- 

TOP OF PARAPET 

EL 11.87 

(2) ,. CHLORINE CONTACT TANK 

SMIPUNG UNE, Cl EL 6.00 

GRADE 

'/0').7 EL 7.25 

(1)1' HYPO IN 2' CONTAINMENT PIPE (FAR) 

~YPO IN 4' CONTAINMENT PIPE 

P. EL 5.0 

EL 2.00 

! 

~ 

~ 

~ 

l 

" ¡ ~ 

E 

oÖ 

f 

~ 

~I NO. 

w"' 

IT IS A 'lll Of SE 72 a TH NE 'I STATE 

EDTK LAW FO Nf PE, UN AC~C t,DE TH 

DlC' OF A UC PR EN TO ALtt Ii 

AM WAY Pl SfTI, PlTS OR RETS TO 'M 

rm 

lH SE 

BE 

Of 

lH 

A 

SE 

PR 

Of 

EH 

A PR 

HA 

EH 

8E AP 

IS ALlm, 

F AN 

TH AI TE EH SH AF TO lH lT HI SE JM 

TH NOTAT1 °ALTm BY Rl EN ll SlTl, TH 

DATE AH A SP DE OF TH AlTETl 

DATE ISSUED FOR 8Y 

DESIGNED ~ 

DRAVi~ 

CHECKED -- 

SECT.CHIEF ~ 

PROJ.ENGR -- 

SCALE 

1/4'=1'-0' 

P.E. 

HAEN AN SAWY 

Ei Enne & Sc 

HAEN AND SAWYR. P.C. 

498 SEVNT AVE' NEW YOR NEW YOR 10018 

APVE FOR TH CI OF NEW YOR CIT OF NEW YORK 


PROJEC MAER 

P.E. 

P.E. 

CHIEF, DMION OF FACluiES DESIGUT 

BUREU OF ENINEERING. DESIN, AN COTRON 

RED HOOK WPCP 




MECHANICAL 

SECTION 

SHEET 1 

1/4'=1'-0' 

10123 1 I r I I 7' I 

DATE MAY 2007 

SHEET~OF~ 

OWG. NO~ RHMBR590

, 

i 

, 

8 c D 

170'-0' 

NOTE: 

14'-0' 29'-0' 

~ 

29'-0' 29'-0' 10'-8' 

~ 

M 

D D L- 

, -- :E -- 

C -- :E-i- 

't 

c: c: c: c: c: 

~:EIH-- 

,IIIX 

:: rm 

'" , 

I I" I I 

." 

¡SWITCHGE 

8 

¡: 

l' 

l 

~¡¡ 

2J T Ell1.50 /CONCR R. l' '- '" . 

36' DISCHARGE SILECE (TY) 

d.1 a 

i 

D 

_~f\ ~I 

v 

4' 

1 

S\ 

r- -:: 

i 3' 3' "' ~ 

:: 

:: 

2' SW UP TO OIL CO (TY) 

I 

TO RSP BREAK 

LOVi 

ḇ TANK, SEE DWG NO. 

i 

- 

BLOViR 

2G-CVl-UTL-C21 __ 

ROOM 

~ 

4' 

I~", '" ~ 

¡ 

, 1- 

¡. "i 

i D-' LCS-0B3114~ 

t 

~ Æ5' .. - f 

~ 

~ b 

l 

, 

3' S\\ UP (TY) ~ Æ 

¡; 

~ b i 

LCS-0B3113 D 

24' DISCHARGE (TY) FE 

~. 

~ LCS-0B3111 Ti 

;k 

~ 

o 

EQUIPMENT ACCES (ABO\Æ) 

~ 

~ 

36' DISCHARGE PIT 

l 

~ 

'f 

4J 42' INLE SILENCE (TY) 

I 

", 

í 

i- 

, 

l 

~ 

. . 

~ 

~ 

1- 

¡ 

~ 

61 

I I i UNDER 

~ 

~ :: 

~ ~~ CONTRACT 

~- 

ị 60' AIR HEADER 

s TO AERATION 

TANK 

~ 

~ 

¡¡ 

5- 

¡¡ 

ï: 

b !l 

" 

~ 

8 

il 

! 

~ 

~ 

l 

l 

¡". 

" 

.: " 

E 

~ s;: 

z; 

A E F F.1 G 

H 

20'-0' 18'-4' 20'-0' 1. fOR ABBRE'IA TIONS, SYBOl ANO GEERAL 

NOTES SE DRAVtNG 2G-PfO-GE-fOl 

2. COPUNGS SHAL BE 

fiXE X EXANSION (FX) 

FlBl, AIR TIGHT (EXE 

AS SHOIl. 

I . INDICATES fiXED TY 

PlPE SUPPOT 

o INDICATES SUDiNG TYE 

PIPE SUPPORT 

'" 

v-b , 

~I b , 

ë 

-- j j 

6 

"" 

IT ts A \tTl a: SE 72.2 a: TH NE YC STATE 

EOri LAW FO JH P£. Ul AC UN TH 

Dl rE A UCSE PR Dl TO ALTE li 

Nr WAY PI, SPTJ PlTS OR RE TO \Ø 

TH S£ Of A PRAl Dl HA BE AP f' 1M 

I1 BE TH SE Of A PR DI tS ALTE, 

n£ AlTE ~ 9i AF TO TH rT tI SE Nl 

n£ NOTATl 'ALTE BY FO BY tI SllU Tl 

DATE ll A SP DE Of 1m Al1ElK 

~I NO. DATE ISSED fOR 

42' UP TO BLOWER (TY) 396100 

396100 

BLOWER COONG 

WATE SYSTEM 

fOR INSTRUMENTATION 

SE DWG. 2G-1" C-BLW-IO 

W-M (TY) (TY) f1-390100 

I I I A 10'-7" 7'-0' SEE 2P PLUMBING 

DESIGNED -- 

DRAII~ 

CHECKO ~ 

SECT.HIEf ~ 

BY i PROJENGR. ~ 

SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Ern1 En & Sd 

HAN AND SAWYR, P~C~ 

498 SENT AVE . NEW YOR NEW YORK 10018 

APOVE fOR THE CIT Of NEW YOR 

PROJECT MAGER 


8 6 4 2 0 8' 

~i-~._- 

1/8' = l' - 0' L._.... I 

~_D~(~rF("" . .~ . r~-1 ~ ¡ 

PE. 

P.E. 

CHIEF. DMSIO Of FACIlES DESlGN 



BUREU OF ENGINEING, DESIGN, AN COSTR 

RED HOOK WPCP 




MECHANICAL 

GROUND FLOOR 

DETAIL PLAN 

lr-i--( i 

i'L ~ ~. I 

¡~.,-L _n KEY PLA IL_..___j 

--IFï U ooX~\t--~~::i L- l o-õlti ~ 

DATE 

MAY 2007 

SHEET~ Of-2 

DWG. NO. RHMBR600

I 

, 

I 

I 

I 

, 

,I 

, 

,IIl,,,,I,,,,II 

, 

I 

, 

A B C D i 

'MO' r 

F F.1 G 

H 

z 

~ 

!l 

'" , 

~ 

l 

l 

~ 

8 

t 

~ 

l 

~ 

i 

~ 

~ 

ß ~~oJ 

l 

i8~ 

l 

;¡ 

l " 

,i ~ 

l i 2./ 0 ~I~ -~ £ 

D-1 

;i 

0 l 

Iõ i 

I 

~ ~ 

'rlf ..~ 

----IH 

l\ D 

~ 

20'-0' 14'-0' 29'-0' 29' O' 

29' O' 

1S'-4' 1O'-S' 

DN 

80110Tcp~30~CP~~ 

LCP-0820 LCP-080140 F 

ACS-02.. L 

CONlROL ROO ~ 

UPS-BLW-051 ~ 

UPS-BLW-OSO A 

~r ir¡i 

LCS-OS033 -- 

J. 

0 

. 

, 

Ṅ 

LCS-080130 U 

¡ 

~ 

~ 

ß ~~ 

t 4 

iil .. I ;, 

~ 

8 - m - 

~ 

l 

~ 

vi0 

i- 

i , 

~ 

f~i; 

~ j 

~ 6 

---I1:f m 

~ " 

1 

!- 

, 

PREFLTR!(TY)'- 

l 

~ 

086010 

-02 

~ 

i 

I PDlSH 

l 

~ ~W-M 

PROCSS AIR flLTRS (TY.) 

i 

INSTRUMENTATION SHOIl 

ONE flL TER SYSTEM 

~ü!¡ 

fOR OTHER flL TES SE 

DWG, 2G-1 & C-BLW-I01 

8 

i 

... 

IT IS A i.TK CJ SET1 no.2 CJ n£ NE YO STATE 

EDTl lAW Fm Nf PE, Uf AC1 UN n£ 

Dt OF A ucsm PR DQ, TO AL.TER ~ 

JK WAY PI, SPTØ PLTS OR MP TO 'f 

TH SE (; A F'Al ENEE HA æE AP F AN 

lT El 1H SE Of A PR EN IS AlTE, 

lHE AlTE EN 9l AF TO n£ I1 tI SE 1H 

TH NOTATI "ALTr BY F10' BY HI SOl1 n£ 

DATE NC A SP DE (; Tl AlTETK 

8 

l DRAII~ 

OESIGNED ~ SCAl 

APOVE FO mE cr OF NEW YOR 

HAEN AN SAWY 

P.E 

Enonn1 Er & Sc 

PROJECT MNGE 

AS NOTED 

~ sâi 

NO. DATE ISSED fOR 

W1 i- 

ILJ ~ 

L i- 

IDDDDDI HVAC 

ROOM STORAGE 

MCC ROOM 

~I 

SECURITY HAROWARE 

~ 

LJ~/ 

REMOTE I/O REMOTE I/O REMOTE I/O 

~"O """,/0 ~ ~~ "',.-- 

(I 

~ 

D~ i- 

NEMA 12 ENO-OSURE 

i 

b-LCP 390100 

') ~120 i-08140 

I ~ -- 

~-~d--~1A 

i LZ 

_ -i 

L T/COCRETE 

~;;; UPPE BLO'i ROO 

EL 29.50 -- 

25" 

BLWOSD23 

BLW002~ "\ 

BLW0802~ ~ n 

n 1''l n r 

,- Hr= ~-lA 

, 

, 

r----------I 

, 

, 

cb 

I 

,l,, 

i il 

, HRU 

CHECKED ~ 

SECT.CHIEf ~ 


P.E. 

HAEN AND SAWYR. P.C~ 

498 SEVNT AVE . NEW YOR NEW VORK 1OO1S 

BLWOS0330 - 

P.E. 

CHIEF, DMSiON OF FAcaES DESIGN- 

flOOR MOUNTED 

LCS-OS3031 ~I: BLOI' 

REMOTE I/O BLW080140 

~089D30 

II r- 

BLW089030 

~LTES , 

~ , '" áf r 

I! ai " 

( Wb I' ~r 

~~ L 

, 

T 

i 

I 


L. 

( ~ 

,"rjJ 

'" c' r 

~, '" 

~, ~ 

~~ 

ai ",LIL 

~I~ 

lAIR INTJE 

(MOT 

~ AIR SHAfT (TY) 

L , 

Lm 

CIT OF NEW VORK 


BUREAU OF ENGINEERING, DESIGN, AN CONSTRON 

RED HOOK WPCP 



-Ti 

20'-0' 

i- 

- 

-gll~-- 

îhHIII--- 

ll l- -- 

NOTE: 

SI TO OIL COOR (TY) 

SII (TY) 

LUBE OIL SYTE (TY) 

SE DWG. 2G-1 & C-BLW-103 

fOR INSTRUMENTATION. 

24' DISCHARGE (TY) 

42' INLET (i') 

~~~-' 

'jiiL- -- 

Ț 


MECHANICAL 

SECOND FLOOR 

DETAIL PLA 

SE DWG. 2G-1 & C-BLW-102 

fOR INSTRUMENTATION. 

(TY) 

8 6 4 2 0 8' 

1/8'=1'-0' L._.... I 

t-llai::::;;-..-i--'-- 

-. ¡, ¡' l- 1 r., ggCh"" ',,"' r- 1 

i'! ,,y' w-' --l 

¡Z.. L I Ó-r- õr.l--ì' 

iIT 

I" .. 

t1 

~/ 

I 

KEY PLA ____J 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHMBR610

r 

I 

, 

I 

i 

I 

i 

I 

, 

i 

I 

i 

, 

I 

I 

I 

I 

i 

I 

I 

, 

i 

, 

i 

i 

i 

I 

, 

I 

I 

i 

I 

TOP OF ROO 

EL 57.83 

TOP OF ROO 

EL 47.50 

TOP Of 5L 

EL 29.50 

~ 

:0 

l 

~8 

" 

~ 

" 

¡¡ 

.. 

i 

i~ 

l 

~. 

i! 

~ 

i 'OP Of MAT 

L 11.50 

~ 

~ '" "-~\'Y'''' 

G 

!! 

~ o 

~ 

g¡ 

l 

i .. 

IT IS A \KTl Of S£ 72.2 Of TH NE 'l STATE 

8 

" 

l 

¡ 

~ 

~ "'~ 

u 

==i¥:=~~~.~~~ 

NN WAY Pl, SÆCITI PlTS OR Rf TO Wi 

TH SE Of A PRAl Dl HA BE Nf f' AN 

fT eE TH 5E Of A ~ EH IS AlTE, 

TH ALTU fHEE SH AfX 10 nl fT tI S£ AN 

TH NOTAlJ "AlTE BY FO BY l- SilU TH 

DATE. Nm A SP 0E Of TH .lTEno 

l 

~ 

~I NO. DATE ISSUED FOR 

~ 

cpi 

~i 

~ ~ 

NOTE: 

. INDICATE FlXED TYE 

PIPE SUPPORT 

o INDICATES SUDING TYE 

PIPE SUPPORT 

k -l 

~ 

L. 

r"" V"" V,,,' 

1/0"")/ 

SWITCHGER 


1 l 

l 

I 

i 

f 

h~~ 

UPPER 

BLOWE 

MCC ROOM 1 I 

ROOM 

36'x24' REUCER 

I 

i 

0 

R 

i 

, 

L. 

o 

36' 

~ 

CL 22.50 

Cl 21.50 

DISCHARGE 

Cl 15.17 

L. L. L. 

J 

6' PISCARGE ll 

~LE~CER (TY) 

11 - n 1 I 1 

~ 

I 

~ 

,1 ',~ -& ,,' ~ 

BLOYÆ 

BLW080130 

(NOTE 1)r- 

-= 

& 

~iR 

T 

-l 

1 

-I-u 

c r- L. 

T 

lI~----- 

~ 

J 

-- ~~~ ~~- - 

I I 

$-- 

1 l- 

. o 

L 42' INLE i 

SILENCE (TY) 

lc L. 

II T r- 

-i i--"i' 

L.-:Jj ! 

i.'III 

II 

, 

I 

(;/+\ ( 

d~==l==;' II 

I 

8£ 

siCTIO~ G :: ~"AA~ 

v 

i- vii 

+ 

ll~'1 

~'~'~ 

I 

T 

~ 

1 ~ 

TOP Of CRANE RAL 

EL 48.83 

I 

r"~~ 

i 

'ó 24' BLOW-OF 

Cl 23.17 

--,. 60' AIR HEADER 

Cl15.17 

"nU' 

o o o . 

L. 

I i~~AA:: 

. 

;~\'Yl 

AIR 1- 

PLEUM 

U JONT (TY) Lc 

I- 

L. 

1/4'~l-D. 

DESIGNED ~ 

DRA\\~ 

CHECKED -- 

SECT.CHIEF ~ 


SCALE 

AS NOTED 

P.E. 

HAEN AN SAWY 

Er En & Så 


498 SEV AVE ' NE YORK NEW YORK 10018 

APOVED FOR THE CIL Of NEW YOR 

PROJECT MA 

P.E 

P.E. 

CHEF, DI OF FACu.mES DESI 



BUREU OF ENGINEERING. DESIGN. AN CONSTRUC 

RED HOOK WPCP 




MECHANICAL 

SECTION 

1 

i.."- 

0 1 2 3 7' 

i 

DATE MAY 2007 

SHEET~OF~ 

DWG. NO. RHMBR620


North River 



June 2007 

DRAFT


North River Water Pollution Control Plant 

DRAFT 



1 NORTH RIVER WATER POLLUTION CONTROL PLANT 1-1 



1.2.1 Influent Flow 1-1 

1.2.2 Headworks 1-1 

1.2.3 Primary Treatment 1-1 

1.2.4 Secondary Treatment 1-2 

1.2.5 Disinfection 1-3 

1.2.6 Odor Control 1-3 



1.4 PROJECT CHALLENGES 1-8 






















4.9.2 Carbon 4-2 

4.9.3 Polymer 4-2 












TOC-1



DRAFT 















5.9.2 Carbon 5-2 


























6.9.2 Carbon 6-17 

6.9.3 Polymer 6-17 












TOC-2



DRAFT 















7.9.2 Carbon 7-8 

7.9.3 Polymer 7-9 


























8.9.2 Carbon 8-13 

8.9.3 Polymer 8-13 











TOC-3



DRAFT 
















9.9.2 Carbon 9-3 

9.9.3 Polymer 9-3 


























10.9.2 Carbon 10-4 

10.9.3 Polymer 10-4 










TOC-4



DRAFT 

















11.9.2 Carbon 11-10 

11.9.3 Polymer 11-10 






11.11.1 Pre-Anoxic Tanks 11-11 

11.11.2 Post-Anoxic Tanks 11-12 

11.11.3 Membrane Bioreactor 11-12 


11.11.5 Intermittent Pumping Station 11-13 

11.11.6 Miscellaneous 11-14 



APPENDIX A 

APPENDIX B 

APPENDIX C 

I 

II 

IV 

TOC-5



DRAFT 



Figure 2-1: North River WPCP Process Flow Diagram .............................................................. 1-5 

Figure 6-1: Mass Balance Process Flow Diagram....................................................................... 2-2 

Figure 10-1: Existing Blower Capacity and Air Requirement Comparison .............................. 6-10 

Figure 10-2: Blower Sizing Comparison ................................................................................... 6-11 

Figure 15-1: Existing Blower Capacity and Air Requirement Comparison .............................. 11-7 

Figure 16-1: Capital Construction Costs for Levels of Treatment, North River WPCP ........... 12-1 

TOC-6



DRAFT 



Table 2-1: North River WPCP Existing Facility Description...................................................... 1-4 

Table 6-1: Mass Balance for Current Conditions (Fiscal Year 2003 – 2005) ............................. 2-3 

Table 6-2: Mass Balance for Future Conditions (Projected 2045) .............................................. 2-4 

Table 8-1: Approximate Filtration Structure Dimensions ........................................................... 4-4 

Table 9-1: Approximate Microfiltration/Ultrafiltration Structure Dimensions ........................... 5-4 

Table 10-1: Operating Flow Distribution Assumptions for ABBNR .......................................... 6-1 

Table 10-2: Anticipated Inter-Zone Baffle Wall Locations for ABBNR .................................... 6-3 

Table 10-3: Anticipated Mixed Liquor Concentrations for ABBNR .......................................... 6-5 

Table 10-4: Anticipated Mixing Zone Sizing (per tank) for ABBNR ......................................... 6-5 

Table 10-5: Anticipated Mixing Power Requirements (Per Zone).............................................. 6-5 

Table 10-6: Anticipated Number of Anoxic Zone Mixers for ABBNR ...................................... 6-6 

Table 10-7: Diffuser Requirements for ABBNR ......................................................................... 6-8 

Table 10-8: Projected 2045 Air Requirements for Advanced Basic BNR .................................. 6-9 

Table 10-9: Blower Selection at the Advanced Basic BNR Level of Treatment ...................... 6-10 

Table 11-1: Operating Flow Distribution Assumptions for FSBNR ........................................... 7-1 

Table 11-2: Anticipated Inter-Zone Baffle Wall Locations for FSBNR ..................................... 7-2 

Table 11-3: Anticipated Mixed Liquor Concentrations for FSBNR ........................................... 7-3 

Table 11-4: Anticipated Mixing Zone Sizing (per tank) for FSBNR .......................................... 7-4 

Table 11-5: Anticipated Mixing Power Requirements (Per Zone).............................................. 7-4 

Table 11-6: Anticipated Number of Anoxic Zone Mixers for FSBNR ....................................... 7-4 

Table 11-7: Diffuser Requirements for FSBNR .......................................................................... 7-5 

Table 11-8: Future 2045 Air Requirements for FSBNR.............................................................. 7-5 

Table 11-9: Blower Selection at the Full Step BNR Level of Treatment.................................... 7-6 

Table 14-1: Approximate Denitrification Filters Structure Dimensions ................................... 10-6 



Table 15-3: Membrane Bioreactor Baffle Walls ....................................................................... 11-3 



Table 15-6: Anticipated Mixing Power Requirements (Per Zone)............................................ 11-4 




Table 15-10: Blower Selection at the Membrane Bioreactor Level of Treatment .................... 11-7 

Table 15-11: Approximate Membrane Bioreactor Structure Dimensions............................... 11-14 

Table 3-1: Secondary Effluent for Each Level of Technology.................................................. 12-1 

TOC-7



DRAFT 

1 NORTH RIVER WATER POLLUTION CONTROL PLANT 


The North River WPCP is a 170 million gallon per day (MGD) average, 340 MGD peak, Water 

Pollution Control Plant (WPCP) that services the western half of Manhattan from Bank Street to 

the northern tip of Manhattan Island. It is located at 725 West 135 th Street in Manhattan, New 

York. The site spans from West 135 th Street to West 145 th Street and is bordered by the Henry 

Hudson Parkway to the east, by a park to the north, and the Hudson River to the south and west. 

The Riverbank State Park is located on top of the facility. 

Plans for the North River WPCP were initially completed in 1971. A 28-acre platform that is 

supported by caissons over the Hudson River was completed in 1978 and serves as the 

foundation for the facility. Construction was completed in a two-phased approach. The first 

phase, started in 1983, began work on the primary treatment system, which went online in March 

1986. The second phase included secondary treatment facilities construction from 1985 to April 

1991, when the system went into operation. 


1.2.1 Influent Flow 

Influent wastewater up to 2 times design dry weather flow (DDWF) or 340 MGD enters the 

facility by gravity through an influent forebay and is directed to six vertical, climber type bar 

screens via six influent channels. The screened wastewater then flows into the main sewage 

pump wet well. There are five main sewage pumps (rated at 100 MGD each) located of the 

lowest level of the facility. Each pump discharges into an individual 48-inch line that connects 

into a 96-inch common force main. The force main subsequently divides into two 72-inch lines, 

which each divide into two 48-inch lines (for a total of four) to discharge into the primary 

settling tank (PST) influent channels. 

1.2.2 Headworks 

Screenings from the climber screens are currently collected in wheelbarrows on an interim basis 

and deposited in dumpsters on an upper level by the facility personnel. A system to collect the 

screenings in basins and pump them to the dumpsters is currently under construction. 

1.2.3 Primary Treatment 

There are eight PSTs at the facility with each PST influent channel serving two PSTs. The tanks 

are covered for odor control and are fully equipped with sludge collection and scum removal 

equipment. Sixteen pumps (operating at N+1 for each PST) direct the primary sludge to ten 

cyclone degritters and five sludge classifiers. The grit is directed towards the head of the plant 

(the influent channels after the bar screens) via the plant drain or removed by truck, while the 

1-1



DRAFT 

degritted sludge is directed to the gravity thickeners via the waste activated sludge (WAS) wet 

well. PST scum is concentrated and directed into dumpsters for removal. 

1.2.4 Secondary Treatment 

The primary clarified effluent is collected and directed through two (2) primary effluent 

channels. Along the end of each channel is a secondary bypass flow control structure that takes 

flow in excess of 255 MGD and directs it through two 48-inch pipes to the secondary effluent 

channels. Downstream of the bypass structure, gravity thickener overflow is returned to the 

process stream and the combined wastewater flows through each of the two channels to a 

common aeration tank influent channel. The common channel splits into five flow distribution 

channels located down the centerline of each of the five aeration tanks. Each aeration tank has a 

two-channel, four-pass design. Flow is controlled by sluice gates of various sizes. The gates are 

typically open to provide uniform flow distribution to each pass, but under wet weather operating 

conditions, operations personnel close the gate to the first pass (Pass A) to store solids in the 

aeration tanks and reduce the potential for solids washout in the clarifiers. The aeration tanks are 

completely enclosed in concrete except for access hatches and various piping penetrations. The 

aeration system includes five 12,500-scfm blowers each with a separate dedicated engine. Air is 

distributed to the aeration tanks through a 42-inch header, which separates into five 18-inch 

headers. Each pass then receives air from a single 10” line. Dissolved Oxygen (DO) probes are 

installed at the facility. The diffuser grids consist of ceramic fine-pore dome diffusers. Note that 

the configuration of baffles and flow control gates in Aeration Tank 3205 are different from the 

remaining tanks in order to facilitate enhanced treatment during the original construction period. 

The sixteen rectangular final settling tanks (FSTs) are fed mixed liquor from the aeration tanks 

through two distribution channels. The tanks are not covered and are fully equipped with sludge 

collection and scum removal equipment. Covers over the effluent weirs are currently being 

installed for odor control. The sludge is collected and directed towards two return activated 

sludge (RAS) wet wells. Six RAS pumps (three per wet well) direct the RAS to a distribution 

box with six weir gates. Five weir gates control the RAS flow to the aeration tanks and the sixth 

gate controls sludge wasting to the WAS wet well. Captured scum is directed towards the head 

of the plant through the plant drain. 

Four WAS pumps convey the sludge from the WAS wet well to ten gravity thickeners via two 

thickener distribution boxes. Typically, six of the ten thickeners process the wasted sludge. The 

gravity thickener overflow (GTO) can be directed to the PST or the aeration tank influent 

channels. Thickened sludge is then digested in eight anaerobic high rate digesters (six operating 

as primary and two operating as secondary). The remaining (typically four) gravity thickeners 

are used to re-thicken digested sludge from the primary digesters to increase the solids 

concentration within the digesters. This rethickening process is known as elutriation. The 

elutriation effluent is directed into the aeration tank influent channels. Digested sludge is 

temporarily stored in a storage tank and then shipped by barge to dewatering facilities at another 

WPCP. 

1-2



DRAFT 

1.2.5 Disinfection 

Secondary effluent from the FSTs flows into two effluent channels. The two 48-inch secondary 

bypass lines (greater than 255 MGD) meet the secondary effluent in each effluent channel. The 

two secondary effluent channels combine and overflow to the chlorine contact tanks located 

below the secondary clarifiers. After disinfection, the treated effluent is discharged into the 

Hudson River. 

1.2.6 Odor Control 

Due to the close proximity of the facility to the residential community, North River is equipped 

with three odor control systems to treat the air collected from the primary, secondary and sludge 

processing areas. Each system consists of wet scrubbers and activated carbon adsorption units. 


Table 1-1 shows a summary of the existing facilities and equipment at the North River WPCP. 

Figure 1-1 shows the process flow through the facility. 

1-3



DRAFT 

Table 1-1: North River WPCP Existing Facility Description 

WPCP / System 

Description 

Opening 

1986 – Primary Treatment 

Upgrade 

1991 – Secondary Treatment 

Tributary Area 

5,110 acres – Western half of Manhattan between Bank St. and the 

northern tip 

Service 

600,000 (approx.) from 2000 Census 

130 MGD Actual Daily Average (FY 2003 - 2005) 

Wastewater Flows 

170 MGD Average Design Dry Weather Permitted Flow 

340 MGD Design Maximum Primary Treatment 

255 MGD Design Maximum Secondary Treatment 

Discharge Location Hudson River, 280’ away 

Main Sewage Pumps 5 (100 MGD each), vertical type 

Primary Settling Tanks 8 (175.5’ L x 84.5’ W x 12’ H) 


5 (303’ L x 63’ W x 29.6’ H), two-channel four-pass design 

Blowers 

5 (12,500 scfm each), N+1+1 capacity 

Diffusers 

Fine bubble ceramic dome diffusers 

Final Settling Tanks 16 (250’ L x 74’ W x 11’ H) 

RAS 

6 pumps (22.6 MGD each), horizontal, non-clog 

WAS 

4 pumps (14.8 MGD each), horizontal, non-clog 

10 Total (65’ dia. x 10’ H), 

Thickeners 

6 for primary and secondary sludge, 

4 for digested sludge (elutriation) 

Digesters 

8 (85’ dia. x 39’ H), 6 primary + 2 secondary 

Chlorine Contact Tanks 4 (640’ L x 114’ W x 8’ H) 

North – 9 wet scrubbers and 22 activated carbon adsorption units 

Odor Control 

South – 5 wet scrubbers and 12 activated carbon adsorption units 

West – 4 wet scrubbers and 12 activated carbon adsorption units 

1-4



DRAFT 

Grit 

to 

Landfill 

Bar 

Screens 

Primary 

Settling 

Tanks 

Wet 

Well 

Main 

Sewage 

Pumps 

Grit 

Classifiers 

Cyclone 

Degritters 

Plant 

Drain 

Elutriation Effluent 


Aeration 

Tanks 

Final 

Settling 

Tanks 

Chlorine 

Contact 

Tanks 

RAS 

Plant 

Water 

Scum 

Concentrator 

Scum to 

Landfill 

WAS 

Degritted 


Balance 

Water 

Waste Sludge Wet Well 

Plant 

Effluent 

Total 

Wasted 

Sludge 

Gravity 

Thickeners 

Elutriation 

Rethickeners 

Primary 

Digesters 

Elutriation 

Water 

Secondary 

Digesters 

Sludge 

Storage 

Tanks 

Digested 

Sludge to 

Offsite 

Dewatering 

Facility 

Wastewater Influent 

Figure 1-1: North River WPCP Process Flow Diagram 

1-5



DRAFT 


To ensure appropriate equipment is selected during this evaluation, ongoing work and planned 

upgrades at the North River WPCP were evaluated. A facilities planning project was conducted 

by CH2M-Hill and CDM to determine and prioritize the systems and items at the facility that 

required replacement and would provide a subsequent improvement to operations performance. 

As part of the project, reports were generated that described the existing conditions and 

identified the potential upgrade work. The upgrades were separated into three phases based on 

priority. The three phases included: 

• Immediate replacement required 

• Replacement in the near future 

• Replacement further into the future (and considered unfunded) 

The Task 2 Report, Facility Evaluation Report (December 2002), described the existing 

conditions of the equipment at the facility. The Task 3 Report, Evaluation of Remedial 

Alternatives (July 2004), identified the three upgrade phases and presented remedial alternatives 

for the items that required immediate replacement. The Task 4 Report, Conceptual Design 

Report (September 2005), provided a more detailed evaluation of the items listed in the first two 

phases. 

The Task 3 Report identified the following equipment as requiring immediate replacement: 

• Process Air and Main Sewage Pump (MSP) Engine Drive Units 

• MSP Replacement 

• MSP Right Angle Replacement 

• MSP Engine Backstops 

• MSP Cone Check Valves 

Based upon the remedial alternatives identified within the Task 3 Report, the Task 4 Report 

recommended to replace the five existing main sewage pumps with six new pumps, replace the 

five main sewage pump engines and five blower engines (for a total of ten) with electric motors 

and replace related appurtenances for both systems. Other facility improvement 

recommendations are listed as follows: 

• Process Performance 

Increase Aeration Capacity for a Nitrifying System 

Apply dry and wet weather flow split pattern to aeration tanks 

Install two thickening centrifuges for WAS thickening 

• Headworks 

Replace Screen Channel Inlet Sluice Gates 

Replace Forebay Equalizing Sluice Gates 

Replace Screen Channel Sluice Gates 

• Primary Treatment System 

Replace Flights, Sprockets, Bearings, Screw conveyors, Rails and Weirs 

Rehabilitate Motor Control Centers and Controls for Sludge Collectors 

1-6



DRAFT 

Replace Scum Concentration Tank Chain and Flight System 

Replace 8” Cast Iron Eccentric Plug Valves 

Replace 96” x 72” Secondary Bypass Gates 

• Secondary Treatment System 

Replace WAS and RAS Pumps, Piping and Controls 

• Sludge Handling Facilities 

Replace Sludge Heat Exchanger and Piping 

Replace Digester Sludge Mixing Pumps 

Replace Sludge Heating Pumps, Booster Pumps, Hot Water Heat Exchangers and 

Controls 

Replace Sludge Transfer Pumps and Appurtenances 

• Electrical Systems 

Replace Load Centers and Power Distribution Systems 

Replace Lighting Systems 

Rehabilitate Substation and Miscellaneous Systems 

Rehabilitate Communication and Control System 

• Heat, Ventilation, and Air Conditioning (HVAC) 

Rehabilitate HVAC System 

• Plumbing Systems 

Improve Domestic Water, Fire Protection, Structure Drainage, and Sump Pumps 

Replace Seal Water System 

Rehabilitate Service Water System 

• Civil/Site System 

Replace Ice Breakers 

• Laboratories and Healthy & Safety 

Improvements to Meet OSHA, ADA and ANSI Standards 

• Architectural Systems 

Miscellaneous Cosmetic Improvements 

Also within the Task 4 Report was a list of work performed under separate contracts. This work 

includes: 

• Aeration System (NR-33) – Replacement of Process Air Piping, and Upgrade and Increase in 

Quantity of Diffusers 

• Emergency Generators (NR-33 and NR-35) 

• Aeration System (NR-35) – Installation of a Sixth Blower and a Second Process Air Header 

• Hypochlorite Feed and Storage Systems (NR-35) 

• Instrumentation and Control of Hypochlorite System (NR-35) 

• Replacement of Secondary Bypass Weir/Circular Gate (NR-35) 

• Fire Detection System (NR-28) 

• Plant Access (NR-37) 

• Underdeck (NR-37) 

• Replacement of Mono Thickener Pumps with Progressive Cavity Type Pumps (NR-50) 

• Replacement of Sludge Degritting System (NR-54) 

• Rehabilitation of Bar Screens (NR-61) 

1-7



DRAFT 

• Gas Compressors (NR-84) 

• Reconstruct Roof Drainage (NR-86) 

• Boiler System (NR-89) 

• Reconstruct MSP Cone Check Valve Actuators (NR-90) 

• Screen Channel Outlet Sluice Gates (BWT) 

1.4 Project Challenges 

The North River WPCP is a unique treatment plant. Due to land constraints, the 28-acre plant 

was built on a platform supported by caissons in the Hudson River. There is limited to no site 

availability for new facilities construction and any new facilities will require construction in the 

Hudson River. This brings with it significant engineering and permitting requirements that 

should be considered in developing a plan to upgrade the facility. In addition, the plant is 

located directly under a park. The local community is very involved with any activity at the 

plant and a detailed public involvement effort will be required. To help address this, all new 

facilities and modification of existing facilities must account for odor control. 

The Team assumes a construction start date of 2020 and a 40 percent design contingency in its 

cost estimates. However, both the cost of expanding into the Hudson River and the associated 

permitting and approval process are unknowns with significant risk to delay construction. If 

HEP was to advocate levels of treatment that would necessitate plant footprint expansion, 

regulatory coordination and permitting would become a priority project challenge. 

1-8



DRAFT 


A plant wide process flow diagram is shown in Figure 2-1. Mass Balance calculations are 

shown on Table 2-1 for current conditions and Table 2-2 for future conditions. The nodes 

identified along the top of Table 2-1 and Table 2-2 correspond to those shown on Figure 2-1. 

Note that the WPCP has the capability to direct Gravity Thickener Overflow and Elutriation 

overflow to the head of the Primary settling tanks or the head of the aeration tanks. It is assumed 

that these recycle loads are added to the head of the aeration tanks. 

2-1



DRAFT 

1 

Grit 

to 

Landfill 

2 3 4 

Bar 

Screens 

Primary 

Settling 

Tanks 

Aeration 

Tanks 

Wet 

Well 

Main 

Sewage 

Pumps 

RAS 

11 

Cyclone 

Degritters 

7 

8 

Plant 

Drain 

Scum 

Concentrator 

10 

Scum to 

Landfill 

Degritted 


Elutriation Effluent 


Final 

Settling 

Tanks 

5 

Chlorine 

Contact 

Tanks 

WAS 

12 

Balance 

Water 

6 

Plant 

Effluent 

Total 

Wasted 

Sludge 

14 

15 

Gravity 

Thickeners 

16 

Elutriation 

Rethickeners 

21 

Primary 

Digesters 

Elutriation 

Water 

18 

19 

Secondary 

Digesters 

Sludge 

Storage 

Tanks 

Digested 

Sludge to 

Offsite 

Dewatering 

Facility 

Wastewater Influent 

9 

Grit 

Classifiers 

Plant 

Water 

13 

22 

20 

17 

Figure 2-1: Mass Balance Process Flow Diagram 

2-2



DRAFT 

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 

(1 + 9) (2 - 7) (3 + 15 + 22) (4 - 12) (5 - 9 - 13 - 20) (10 + 12 + 13) (14 - 16) 

Elutriation 

Effluent 

Elutriated 

Digested 

Sludge 

Elutriation 

Water 

Stored 

Sludge 

Dig Sludge 

to Elutriation 

Dig Sludge 

to Secondary 

Thickened 

Sludge 

GTO 

Total 

Wasted 

Sludge 

Balance 

Water 

RAS WAS 

Degritted 

Primary 

Sludge 

Plant 

Drain 

Primary 

Grit 

Primary 

Sludge 

Plant 

Effluent 

Final 

Effluent 

Secondary 

Influent 

Primary 

Effluent 

Primary 

Influent 

Raw 

Influent 

Wastewater 


Flow (MGD) 

Average 129.6 139.9 132.4 155.4 152.4 129.1 7.5 --- 10.3 7.5 43.8 3.0 4.0 14.5 13.7 0.7 0.5 0.4 0.5 9.0 0.2 9.2 

Maximum Month 148.0 158.3 150.8 173.5 170.5 147.2 7.5 --- 10.3 7.5 45.4 3.0 4.0 14.5 13.5 1.0 0.8 0.7 0.8 9.0 0.5 9.2 

Maximum Daily 181.0 191.3 183.8 206.4 203.4 180.1 7.5 --- 10.3 7.5 52.9 3.0 4.0 14.5 13.3 1.1 0.9 0.7 0.9 9.0 0.5 9.2 

TSS 

Average 

mg/l 199.6 239.8 103.9 123.7 15.0 15.0 2,643 --- 745.4 2,547 3,585 3,585 15.0 2,062 325.9 34,778 16,360 16,360 13,633 15.0 32,739 106.5 

lbs/day 215,800 279,800 114,700 160,300 19,100 16,100 165,100 6,000 64,000 159,100 1,309,600 89,400 500 249,000 37,400 211,700 69,600 53,200 58,000 1,100 46,400 8,200 

Maximum Month 

mg/l 245.0 277.6 119.5 144.7 20.7 20.7 3,462 --- 745.4 3,319 3,585 3,585 20.7 2,463 395.8 31,237 16,360 16,360 13,633 20.7 19,738 189.3 

lbs/day 302,400 366,400 150,200 209,400 29,400 25,400 216,200 8,900 64,000 207,300 1,357,400 89,400 700 297,400 44,600 252,700 105,100 95,500 87,600 1,600 82,300 14,500 

Maximum Daily 

mg/l 259.5 285.6 121.9 147.5 26.6 26.6 4,306 --- 745.4 4,091 3,585 3,585 26.6 2,863 465.9 30,887 16,360 16,360 13,633 26.6 20,563 196.6 

lbs/day 391,700 455,700 186,900 253,800 45,100 40,000 268,900 13,400 64,000 255,500 1,581,700 89,400 900 345,700 51,800 293,700 124,200 99,600 103,500 2,000 85,700 15,100 

BOD/CBOD 

Average 

Table 2-1: Mass Balance for Current Conditions (Fiscal Year 2003 – 2005) 

mg/l 166.9 166.4 89.7 117.4 12.0 12.0 1,524 --- 160.7 1,524 1,606 1,606 12.0 1,123 391.1 14,908 3,599 3,599 2,999 12.0 7,203 106.5 

lbs/day 180,400 194,200 99,000 152,100 15,300 12,900 95,200 0 13,800 95,200 586,500 40,000 400 135,600 44,800 90,800 15,300 11,700 12,800 900 10,200 8,200 

Maximum Month 

mg/l 184.4 182.9 97.9 132.1 16.0 16.0 1,894 --- 160.7 1,894 1,606 1,606 16.0 1,316 475.0 13,023 3,599 3,599 2,999 16.0 4,342 189.3 

lbs/day 227,600 241,400 123,100 191,200 22,800 19,600 118,300 0 13,800 118,300 608,000 40,000 500 158,900 53,500 105,300 23,100 21,000 19,300 1,200 18,100 14,500 

Maximum Daily 

mg/l 181.7 180.5 95.8 130.3 19.1 19.1 2,260 --- 160.7 2,260 1,606 1,606 19.1 1,506 559.0 12,583 3,599 3,599 2,999 19.1 4,524 196.6 

lbs/day 274,200 288,100 146,900 224,200 32,400 28,700 141,100 0 13,800 141,100 708,400 40,000 600 181,800 62,200 119,600 27,300 21,900 22,800 1,400 18,900 15,100 

TKN 

Average 

mg/l 29.1 29.1 27.6 28.7 18.3 18.3 54.3 --- 29.1 54.3 559.8 559.8 18.3 148.7 25.0 2,479 2,750 2,750 2,750 18.3 3,915 50.0 

lbs/day 31,400 33,900 30,500 37,200 23,300 19,700 3,400 0 2,500 3,400 204,500 14,000 600 18,000 2,900 15,100 11,700 8,900 11,700 1,400 5,600 3,800 

Maximum Month 

mg/l 30.9 30.9 29.2 30.0 22.6 22.6 65.3 --- 30.9 65.3 451.0 451.0 22.6 133.1 25.0 1,633 1,612 1,612 1,612 22.6 1,571 50.0 

lbs/day 38,100 40,800 36,700 43,400 32,100 27,800 4,100 0 2,700 4,100 170,700 11,200 800 16,100 2,900 13,200 10,300 9,400 10,300 1,700 6,600 3,800 

Maximum Daily 

mg/l 27.7 27.7 25.9 27.0 24.6 24.6 70.7 --- 27.7 70.7 190.2 190.2 24.6 82.7 25.0 748.4 639.3 639.3 639.3 24.6 390.5 50.0 

lbs/day 41,800 44,200 39,800 46,500 41,700 36,900 4,400 0 2,400 4,400 83,900 4,700 800 10,000 2,900 7,100 4,900 3,900 4,900 1,800 1,600 3,800 

2-3



DRAFT 

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 

(1 + 9) (2 - 7) (3 + 15 + 22) (4 - 12) (5 - 9 - 13 - 20) (10 + 12 + 13) (14 - 16) 

Elutriation 

Effluent 

Elutriated 

Digested 

Sludge 

Elutriation 

Water 

Stored 

Sludge 

Dig Sludge 

to Elutriation 

Dig Sludge 

to Secondary 

Thickened 

Sludge 

GTO 

Total 

Wasted 

Sludge 

Balance 

Water 

RAS WAS 

Degritted 

Primary 

Sludge 

Plant 

Drain 

Primary 

Grit 

Primary 

Sludge 

Plant 

Effluent 

Final 

Effluent 

Secondary 

Influent 

Primary 

Effluent 

Primary 

Influent 

Raw 

Influent 

Wastewater 


Flow (MGD) 

Average 136.7 147.0 139.5 163.0 159.5 136.2 7.5 --- 10.3 7.5 43.8 3.5 4.0 15.0 14.3 0.7 0.5 0.4 0.5 9.0 0.2 9.2 

Maximum Month 151.1 161.4 153.9 177.1 173.6 150.3 7.5 --- 10.3 7.5 45.4 3.5 4.0 15.0 14.0 1.0 0.8 0.7 0.8 9.0 0.5 9.2 

Maximum Daily 190.9 201.2 193.7 216.8 213.3 190.0 7.5 --- 10.3 7.5 52.9 3.5 4.0 15.0 13.8 1.1 0.9 0.7 0.9 9.0 0.5 9.2 

TSS 

Average 

mg/l 227.1 263.4 113.8 135.4 15.0 15.0 3,051 --- 745.4 2,929 3,585 3,585 15.0 2,304 363.4 40,216 16,360 16,360 13,579 15.0 33,804 109.8 

lbs/day 258,900 322,900 132,400 184,100 20,000 17,000 190,500 7,600 64,000 182,900 1,309,600 104,600 500 288,100 43,200 244,800 67,500 55,300 56,100 1,100 47,900 8,500 

Maximum Month 

mg/l 288.0 317.2 136.4 163.0 15.0 15.0 4,033 --- 745.4 3,872 3,585 3,585 15.0 2,776 445.2 36,455 16,360 16,360 13,579 15.0 18,627 179.4 

lbs/day 362,900 426,900 175,000 240,800 21,700 18,800 251,900 10,100 64,000 241,800 1,357,400 104,600 500 347,000 52,000 294,900 110,300 90,300 91,600 1,100 77,700 13,700 

Maximum Daily 

mg/l 295.2 318.3 135.5 163.4 15.0 15.0 5,045 --- 745.4 4,843 3,585 3,585 15.0 3,261 529.4 36,442 16,360 16,360 13,579 15.0 20,755 198.2 

lbs/day 470,000 534,000 219,000 295,400 26,700 23,800 315,100 12,600 64,000 302,500 1,581,700 104,600 500 407,600 61,100 346,500 123,100 100,700 102,200 1,100 86,500 15,300 

BOD/CBOD 

Average 

Table 2-2: Mass Balance for Future Conditions (Projected 2045) 

mg/l 189.9 187.9 100.9 130.8 13.0 13.0 1,807 --- 160.7 1,807 1,606 1,606 13.0 1,281 436.0 17,789 3,599 3,599 2,987 13.0 7,437 109.8 

lbs/day 216,500 230,300 117,500 177,800 17,300 14,800 112,900 0 13,800 112,900 586,500 46,900 400 160,200 51,800 108,300 14,900 12,200 12,300 1,000 10,500 8,500 

Maximum Month 

mg/l 216.7 213.1 114.0 150.6 13.0 13.0 2,251 --- 160.7 2,251 1,606 1,606 13.0 1,503 534.2 15,505 3,599 3,599 2,987 13.0 4,098 179.4 

lbs/day 273,100 286,900 146,300 222,500 18,800 16,300 140,600 0 13,800 140,600 608,000 46,900 400 187,900 62,500 125,400 24,300 19,900 20,100 1,000 17,100 13,700 

Maximum Daily 

mg/l 206.7 204.4 108.2 145.7 13.0 13.0 2,691 --- 160.7 2,691 1,606 1,606 13.0 1,723 635.3 14,931 3,599 3,599 2,987 13.0 4,566 198.2 

lbs/day 329,100 342,900 174,900 263,500 23,100 20,600 168,000 0 13,800 168,000 708,400 46,900 400 215,300 73,400 142,000 27,100 22,200 22,500 1,000 19,000 15,300 

TKN 

Average 

mg/l 32.1 32.1 30.4 31.1 18.6 18.6 63.0 --- 32.1 63.0 599.6 599.6 18.6 176.5 25.0 3,135 3,748 3,748 3,748 18.6 6,379 50.0 

lbs/day 36,600 39,400 35,400 42,200 24,700 21,100 3,900 0 2,800 3,900 219,000 17,500 600 22,100 3,000 19,100 15,500 12,700 15,500 1,400 9,000 3,900 

Maximum Month 

mg/l 35.2 35.2 33.3 33.5 18.6 18.6 75.9 --- 35.2 75.9 770.8 770.8 18.6 222.9 25.0 3,083 3,127 3,127 3,127 18.6 3,213 50.0 

lbs/day 44,400 47,400 42,700 49,400 26,900 23,300 4,700 0 3,000 4,700 291,800 22,500 600 27,900 2,900 24,900 21,100 17,300 21,100 1,400 13,400 3,800 

Maximum Daily 

mg/l 30.6 30.6 28.6 29.3 18.6 18.6 82.2 --- 30.6 82.2 679.9 679.9 18.6 204.8 25.0 2,388.9 2,555.8 2,555.8 2,555.8 18.6 2,936.5 50.0 

lbs/day 48,700 51,300 46,200 52,900 33,100 29,500 5,100 0 2,600 5,100 300,000 19,800 600 25,600 2,900 22,700 19,200 15,700 19,200 1,400 12,200 3,900 

2-4



DRAFT 









• Screening 






Diffusers 










Alkalinity 

Carbon 

Polymer 











analysis. 

3-5



DRAFT 



For the Existing Conditions with Solids Filtration level of technology, there are no modifications 

necessary. 


No fine screens are needed for the Existing Conditions with Solids Filtration level of technology. 




Conditions with Solids Filtration level of treatment. 



treatment. 



of treatment. 



Conditions with Solids Filtration level of treatment. 



Solids Filtration level of treatment. 





No modifications to the Final Settling Tanks are needed for the Existing Conditions with Solids 


4-1



DRAFT 



with Solids Filtration level of technology. 



with Solids Filtration level of technology. 



Froth Control Hoods are not recommended for the Existing Conditions with Solids Filtration 



RAS chlorination measures are not recommended for the Existing Conditions with Solids 



Surface wasting is not recommended for the Existing Conditions with Solids Filtration level of 

technology. 





4.9.2 Carbon 


technology. 

4.9.3 Polymer 

Polymer addition is not recommended for the Existing Conditions with Solids Filtration level of 

technology. 


4-2



DRAFT 


Solids filtration is a process that is installed down stream of a secondary treatment process to 

enhance removal of particulates within the wastewater, including solids, particulate BOD and 

TKN. 

The addition of conventional filtration after the final settling tanks will achieve lower levels of 





The filters will be placed downstream of the FSTs and upstream of disinfection at North River, 

although the physical location of the filters will be off-site. A new structure will be constructed 

to house the new equipment. 

Secondary effluent will be directed through a new conduit constructed on the west end of the 

facility and flow south by gravity to the newly constructed filters. The secondary effluent will be 

evenly applied to the filters at a constant flow rate per surface area and will be allowed to flow 

downward through the media. As the secondary effluent flows through the media, larger 

particulates will be physically filtered by the media. Filtered effluent will be pumped back to the 

existing disinfection system. 

To maintain the efficiency of the filters, periodic backwashing must be performed to remove the 

accumulated solids. Equipment will be provided that will flush the media by recycling the 

treated effluent to serve as wash water. A blower system will also be provided for air scouring 

of the media when the filter units are not operating in a downward flow mode. The reused 

effluent and released solids will then be pumped to the gravity thickeners. The process flow 

schematic is shown in Drawing 61. Plans and sections of the new facilities are shown in 

Drawings 62 though 65. 

Odor control will be provided within the new structure. This system will consist of chemical wet 

scrubbers followed by carbon adsorption. The odor control system will collect and treat the air 

from within the facility to remove odorous compounds prior to discharging the air to the 

atmosphere. 

In order to facilitate the required facilities for the Filtration alternative, it will be necessary to 

construct a new structure in the Hudson River on the South end of the North River WPCP. A 

flow conduit structure will also be required to be built to provide a path for process flows to and 

from this structure. This conduit will run along the West side of the building, also in the Hudson 

River. This will be a substantial undertaking that will require a new structural support system. 

4-3



DRAFT 

All structures will be constructed out of 4,000-psi reinforced concrete. Each structure will 

include a structural slab supported on caissons and structural walls. The caisson spacing will be 

approximately 18’ x 32’. 

Since the building platform will be constructed in place of the existing dock, the construction 

will also include a new dock on the South end of the new building. The approximate dimensions 

of the building footprint, height, and width of flow conduit are shown in Table 4-1. 

Table 4-1: Approximate Filtration Structure Dimensions 

Building Footprint (ft) 280 x 306 

Building Height (ft) 35 

Flow Conduit Width (ft) 29 



technology. 



technology. 



technology. 


No additional odor control measures are needed for the Existing Conditions with Solids 


4-4



DRAFT 







No fine screens are necessary for the Existing Conditions with Microfiltration/Ultrafiltration 






















5-1



DRAFT 














No RAS chlorination measures are recommended for the Existing Conditions with 









5.9.2 Carbon 





5-2



DRAFT 




Microfiltration/ultrafiltration is a process that is installed down stream of a secondary treatment 


be beyond those capable with conventional filtration. 

The addition of microfiltration/ultrafiltration after the final settling tanks will achieve lower 

levels of particulates in the waste stream. The objectives include: 




Similar to the conventional filtration design, microfilters will be placed downstream of the FSTs 

and upstream of disinfection at North River, although the physical location of the filters will be 

off-site. A new structure will be constructed to house the equipment. 

Secondary effluent will be directed through a new conduit to the filtration tanks by gravity. 

Within the tanks, membrane filters will extract the treated effluent from the wastewater, thereby 

leaving the particulate matter in the tanks. Due to the small pore size of the membranes 

(typically 0.1 to 0.2 micron), virtually all of the particulate matter will remain within the tanks. 

Permeate pumps will generate a vacuum within the membranes to draw the effluent through the 

membrane. Treated effluent will be directed to the existing disinfection system. 

To maintain the efficiency and a high flux capacity across the membrane, periodic back pulsing 

must be performed to remove the accumulated solids from the surface of the membranes. The 

permeate flow is reversed through the membrane, forcing the solids off the membrane surface 

and dislodging any particulates in the pore spaces. A process flow schematic is shown on 

Drawing 66 and plan and sections of the new facilities can be seen in Drawings 67 through 72. 

Odor control will be provided within the new structure. This system will consist of chemical wet 

scrubbers followed by carbon adsorption. The odor control system will collect and treat the air 

from within the facility to remove odorous compounds prior to discharging the air to the 

atmosphere. 

In order to facilitate the required facilities for the Microfiltration/ultrafiltration alternative, it will 

be necessary to construct a new structure in the Hudson River on the South end of the North 

River WPCP. A flow conduit structure will also be required to be built to provide a path for 

certain process flows to and from this structure. This conduit will run along the West side of the 

building, also in the Hudson River. This will be a substantial undertaking that will require a new 

structural support system. 

5-3



DRAFT 






of the building footprint, height, and width of flow conduit are shown In Table 5-1. 

Table 5-1: Approximate Microfiltration/Ultrafiltration Structure Dimensions 

Building Footprint (FT) 250 x 390 

Building Height (FT) 35 

Flow Conduit Width (FT) 29 








No additional odor control measures are needed for the Existing Conditions with 


5-4



DRAFT 



No modifications to the Primary Settling Tanks are needed for the Advanced Basic BNR level of 

technology. 





Flow distribution and control is an important factor that can affect nitrogen removal performance 

of any BNR process. The constraints for flow distribution at North River WPCP include the 

existing hydraulic profile, tank size, channel internal structure, and flow requirements. 

Objectives: 



pass 



Parameters: 



Pass A: 0 - 30 mgd (0 to 30 %) 

Pass B: 6 - 45 mgd (20 to 50%) 

Pass C: 6 - 45 mgd (20 to 50%) 

Pass D: 0 - 32 mgd (0 to 35%) 



distribution assumptions can be seen below in Table 6-1. Gate relocation was also considered 

depending on the desired level of treatment. 





6-1



DRAFT 

The requirement for this upgrade to remain within the physical and hydraulic constraints of the 

current operation limits the improvement of flow distribution and control. There is no 

recommendation for gate relocation or resizing within this upgrade. In order to provide wet 

weather flow response to Pass D, the existing gate must be able to accommodate 100% of the 

flow into one AT. The existing 42” x 42” gate accomplishes this while maintaining a maximum 

velocity below acceptable limits. The gate, however, requires the installation of a motorized gate 


automated gate control actuator will open the gate fully to allow all AT flow to enter into the 

head of Pass D. The location is shown on Drawing 6. A gate controller will be tied into the 

plant SCADA control system to allow for either flow paced or manual control. 





baffle wall 






• Flow assumptions from Table 6-1: Operating Flow Distribution Assumptions for 

ABBNR 

The baffle wall locations are determined based on the required volume of each pre-anoxic, 

anoxic, and oxic zone within each Pass. Each technology requires a certain volume for each 

zone, and a certain number of zones per pass (and tank). The anticipated baffle wall locations 

are seen in Table 6-2 and a sketch of these locations is seen in Drawings 6, 8 and 10. 

6-2



DRAFT 

Pass 

A 

B 

C 

D 




zones 


(between Oxic 





zones) 


Pass) 

1/6 length of 


N/A 

N/A 

pass 

pass of pass 

1/6 length of 


N/A 

N/A 

pass 

1/6 length of 

pass 

1/6 length of 

pass 

N/A 


pass 

1/3 length of 

pass 

1/2 length of 

pass 

of pass 

10% of end of 

pass 

N/A 

N/A 

N/A 

The Advanced Basic BNR technology requires new inter-zone baffle walls to separate the 

treatment zones. These baffle walls will be installed across the entire width of each pass (31.5 

feet) and will be modular in nature but sufficiently stable to withstand the applied forces and the 

corrosive nature of the wastewater. The walls will have removable sections to allow changes in 

the process and pass specific variations in the baffle height requirements. The height of the 

baffle walls will be determined and adjusted in the field based on the flow through each pass to 

achieve a minimum velocity of 1 foot per second across the wall. An example of a typical baffle 

wall can be seen in Drawing 11. 

The walls will be permanent from tank bottom to approximately 26 feet. On each end, the 

existing Y shaped walls will be squared off from the top of the Y down vertically to the new 

permanent wall section. Concrete columns with channels will be installed parallel to the squared 

off portion and extend from the top of the permanent wall to the full height of the aeration tanks 

(approximately 13 feet above the permanent wall). The channels will allow baffle sections to 

slide into place in order to achieve desired baffle wall height. These sections will be made of 

wood or fiberglass reinforced plastic (FRP) and will be accessible through a removable hatch to 

be constructed above each new baffle wall. In order to install these new baffles, a sizable section 

of the aeration tank ceilings will have to be excavated and removed. In addition, the permanent 

wall section will include three 1-foot by 1-foot openings at the floor of the tank to allow filling 

and draining of the tank. 

The design of the Advanced Basic Step Feed BNR baffle walls will take advantage of existing 

wall locations. Twelve (12) new baffle walls will be installed in each tank to separate the 

different pre-anoxic, anoxic and oxic zones. Penetrations will be cut in the existing roof slab at 

each installation location and the roof will be replaced with a removable air tight hatch to be 

used for access by plant personnel. There will be no other baffle wall modifications as this 

option mandates no changes be made to existing equipment or process structures (i.e. baffle 

walls). 

6-3



DRAFT 

It is anticipated that the permanent section of the new baffle walls will be a minimum of 18” 

thick lightweight concrete. The permanent section of the inter-pass walls will match the 

thickness of the existing Y-walls. The new baffle walls are thicker than the existing inter-pass 

walls in AT 3205 because of the use of lightweight concrete to minimize the additional weight 

on the existing pile foundation system. 



given below: 

Objectives: 




Parameters: 



• Mixed Liquor Suspended Solids (MLSS) concentration 

Pass A: 4,000 to 8,000 mg/L 

Pass B: 2,000 to 6,000 mg/L 

Pass C: 1,500 to 4,000 mg/L 

Pass D: 1,000 to 3,000 mg/L 

Target AEMLSS Concentration: 2,000 mg/L 

Mechanical mixers are proposed for installation in the ATs to keep the mixed liquor in 

suspension in the anoxic and pre-anoxic zones. These mixers will be installed on a vertical rail 

system with a hand-operated hoist/davit that will allow an operator to raise the mixer for repair 

or replacement. The rail system will be fastened to the bottom of the aeration tank and the 

aeration tank wall and extend to the top of the tank. A penetration must be made through the top 

of the tank and a removable air tight hatch installed to provide access for the operator to quickly 

adjust or change each mixer. The hand-operated hoist system must be portable to allow the 

hatch to be closed for odor control. A section of the system is shown on Drawing 12. 

Backup and/or redundant mixing units will not be installed in place; in the event of a mixer unit 

failure, a spare mixing head can be quickly installed onto the rail system. The mixers will be 

connected to a local control panel to provide on/off control. The control panel will have the 

capability to send a signal to a central location (SCADA) to monitor the status of the mixer. 






6-4



DRAFT 








varying process temperatures; thereby possibly changing mixer requirements. The power 

requirements per zone are shown in Table 6-5. 

Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 23,543 23,543 87,109 7,063 

Pass B 23,543 23,543 87,109 7,063 

Pass C 23,543 23,543 80,047 14,126 

Pass D 23,543 23,543 23,543 70,629 

Pass 

Table 6-5: Anticipated Mixing Power Requirements (Per Zone) 

Mixing Power Requirements (hp) 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 9.2 9.2 N/A 2.8 

Pass B 7.5 7.5 N/A 2.3 

Pass C 6.7 6.7 N/A 4.0 

Pass D 6.1 6.1 6.1 N/A 


is proposed. The number of mixers depends on the required horsepower, which is a function of 

the mixed liquor concentration and zone sizing. Based on the above operating conditions, 7.5 hp 

mixers are anticipated to best suit mixing energy requirements. The number of mixers necessary 

is shown below in Table 6-6. 

6-5



DRAFT 

Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Preanoxic 




Total 

Mixers 

80 


The facility should be upgraded to provide sufficient power for mixing. Each mixer will be 7.5 

hp. Each mixer will include a local control panel and a signal to the SCADA system. Spare 

mixers will require storage area at the plant. 


The objectives of the air distribution and control upgrades are to ensure sufficient air is provided 

for nitrification and to optimize the control of DO levels. These objectives, as identified in the 

BNR guidance documents, include: 

• Provide sufficient oxygen to satisfy all process requirements, 

• Provide flexibility for different process operating conditions, and 


minimize under-aeration and over-aeration. 

The existing air distribution and control systems will be demolished as shown on Drawing 13. 

Under the Advanced Basic Step Feed BNR, the new 70-inch main air header will enter the 

aeration tank battery under the influent channel in the northeast corner. The elevation of the 

header will be lowered to allow the larger pipe to fit within the existing space. From the main air 

header, five individual 32-inch aeration tank headers will branch off. Each header will run 

parallel to and below the main air header along the width the corresponding aeration tank, in the 

corridor underneath the influent channel. As the main air header continues to branch off into the 

aeration tank headers, the diameter will be reduced to provide a relatively constant air velocity 

between 3,200 and 3,600 feet per minute. Motorized butterfly valves will provide the aeration 

tank headers with increased flow control and allow for an aeration tank to be taken offline. 

Each aeration tank header will subsequently branch off into four 18-inch pass headers. Similar 

to the design of the existing air distribution system, the pass headers will penetrate the aeration 

tanks near the bottom. Due to the two-channel, four-pass design of the aeration tanks, two pass 

headers will penetrate Pass B to service Passes A and B, and two pass headers will penetrate Pass 

C to service Passes C and D. All four pass headers will then exit vertically through the aeration 

tank cover and pass through the spray water chamber located at the north end of the tank. The 

pass headers will run the length of the corresponding pass at a height of approximately 13 feet 

6-6



DRAFT 

above the tank surface. The pass headers servicing Passes A and D will require more piping 

because of the existing aeration tank two-channel, four-pass layout. The air velocity range for 

the pass headers is expected to be between 2,600 and 3,000 feet/minute. For the longer lengths 

of pipe that are between 16 and 18 inches in diameter, seismic pipe supports will be positioned 

approximately every 10 feet. Simple pipes supports can be utilized once the pass header 

diameter is less than 16 inches at an interval of 150 feet with a minimum of three per header. 

Galvanized steel should be used for the supports. Each pass header will be equipped with a 

motorized butterfly valve and flow meter for improved DO control. This will be connected to 

the SCADA system. 

Six 8-inch droplegs will branch off of the pass header and penetrate through the aeration tank 

cover. For Passes A, B and C, both switch zones at the head of the pass will have a dropleg and 

connected diffuser grid. The remaining four droplegs will service the oxic zone. In Pass D, the 

three switch zones will each have one dropleg with the three remaining droplegs servicing the 

oxic zone. Each dropleg will be provided with a butterfly valve. A flow schematic of the air 

distribution system can be seen in Drawing 14. 

Although the Advanced Basic Step Feed BNR design level includes new baffle walls and switch 

zones, the original baffles present within the tank will remain in place, as discussed in Section 

6.3.2. 

Concrete pipe cradles will be necessary to support both the main air header and aeration tank 

headers under the influent channel. The addition of more aeration piping above the aeration 

tanks and the related support structures may restrict movement and access to other equipment on 

top of the aeration tank covers. Taking aeration tanks offline will be required to install all piping 

and to ensure that the new penetrations are tightly sealed. Sway braces will be installed into the 

aeration tank walls to provide support for the droplegs. The existing main air header, pass 

headers and droplegs will be demolished, as shown in Drawing 13. Pipe supports will be 

demolished also due to prolonged exposure to the weather. Penetrations into the aeration tank 

cover and Pass B wall will require filling and sealing. 

The motorized valves will need to be tied into the DO control system to regulate air distribution. 

The pass header flow meters will provide accurate measurements of the air distribution between 

the passes and aeration tanks. The system will have the capability to be controlled by DO level, 

airflow, or a combination of the two. These will be tied into the plant-wide SCADA system. 


With the increase in the aeration capacity under the new design upgrades, the diffuser grids will 

be redesigned to provide a distribution of air throughout the aeration tank oxic zones and switch 

zones. 

Currently, North River has approximately 18,300 diffusers or 3,660 diffusers per aeration tank. 

The diffusers are 7” diameter ceramic dome types. Each dropleg services 24 diffuser manifold 

6-7



DRAFT 

laterals with a centerline configuration allowing for 12 laterals on both sides of the dropleg. The 

entire aeration tank bottom area has diffuser coverage under this configuration. 

Under the Contract NR-35 upgrade, the diffuser quantity will be increased by 25%. The total 

number of diffusers will be 22,900. 


nitrification and to optimize the control of DO levels. These objectives, as identified in the BNR 

guidance documents, include: 


• Provide flexibility for different process operating conditions, including the implementation 

of switch zones 


The quantity of diffusers required for each design level was based on the calculated air 

requirements. The selected diffuser type was the 9” diameter fine bubble membrane disc 

diffuser with a manufacturer recommended air flow range of 1 to 3 scfm per diffuser. An 

average flow of 1.5 scfm per diffuser was initially assumed under average loading conditions. 

Anticipated variations in loads were evaluated to ensure sufficient capacity was available and 

that the diffusers operated within their appropriate manufacturer-suggested typical range. Table 

6-7 shows the required diffusers. 




(scfm) 


Required (1) 



In order to ensure sufficient diffusers could be installed at the facility, the available floor area 

was evaluated and compared to the diffuser requirements. It appears that there is sufficient space 


proper design of the diffuser grid. 




new air requirements associated with BNR and allow the facility to fully utilize the new 

technologies, the process air blower system will need to be enhanced. 


nitrification and to optimize the control of DO levels. These objectives, as identified in the BNR 

guidance documents, include: 

6-8



DRAFT 






conditions 


levels based on the projected flows and loads and the projected mass balance for 2045. The 

calculated air requirements were compared against the existing process aeration system to 

determine the necessary increase in aeration capacity that must be provided. Table 10-8 presents 

the calculated air requirements. 

Level of 

Treatment 

Table 6-8: Projected 2045 Air Requirements for Advanced Basic BNR 

Nitrogen 

Oxidized (2) 

BOD 

Oxidized (3) 

Oxygen 

Required (4) 

Aeration 

Tank 

Loading 

Condition (1) lb/d lb/d lb/d scfm 

Air 

Required (5) 

Advanced Average 22,500 177,800 298,900 66,000 

Basic BNR Peak Daily 29,900 263,500 427,500 94,400 

(1) Secondary influent includes primary effluent, gravity thickener overflow and elutriation effluent 

(2) All secondary influent nitrogen assumed oxidized or assimilated, except 2 mg/L in effluent; credit for PST 

removals was taken 

(3) All secondary influent BOD assumed oxidized; no BOD credit for denitrification was taken; credit for PST 


(4) Oxygen required = (N oxidized * 4.57 lb O 2 /lb TKN) + BOD oxidized * 1.1 lbO 2 /lb BOD 

(5) Air required = 0.04*O 2 required / Overall Efficiency; Overall Efficiency = 18% for Advanced Basic BNR 

For Advanced Basic BNR level of treatment, the air requirements were determined at both the 

average and peak daily loading conditions, where influent BOD was completely oxidized and 

influent TKN was reduced to 2 mg/L in the final effluent. Since the aeration tanks at North 

River are deeper than most of the aeration tanks at other NYCDEP WPCPs (29.6 feet versus 15 

feet, typically), the overall oxygen transfer efficiency is greater than typically observed. Higher 

mixed liquor concentrations result in a lower alpha factor, which impacts oxygen transfer 

efficiency. 


using the existing blowers. With the addition of the sixth blower under Contract NR-35, the 

average loading conditions could theoretically be met for the Step Feed BNR technologies, but 

the facility would be operating with all blowers and not provide the spare and standby 

requirements identified in the BNR design guidance documents (N+2) for average conditions. 

Max month loading conditions would not be met at all. Figure 6-1 shows this comparison. A 

new process air blower system is required as part of the Advanced Basic BNR proposed upgrade 

designs. 

6-9



DRAFT 

160,000 

Figure 6-1: Existing Blower Capacity and Air Requirement Comparison 

140,000 

120,000 

Peak Daily 

100,000 

scfm 

80,000 

6 Blowers (N) 

Peak Daily 

Average 

60,000 

40,000 

5 Blowers (N) 

4 Blowers (N + 1) 



Average 

20,000 


0 

Existing Blower 

Capacity 


Capacity 

(NR-35 Completed) 

Step Feed BNR 

Technology 

Membrane 

BioReactor 

Technology 

Many factors figure into the selection of the blowers, including required air, available footprint, 

power requirements, discharge pressure, and design guidance constraints. Based on these 

parameters, one blower type was selected for application to all the design levels. The Roots- 

Dresser HT-series blower will provide sufficient air at the required discharge pressure. The HTseries 

is also a multistage, horizontally split, centrifugal unit that can provide up to 43,000-scfm 

(approx.) at 14 psig, 100F and 2,500 hp. The number of blowers was selected to satisfy the 

capacity requirement of N + 2 blowers operating during average conditions and N + 1 blowers 

operating during peak day conditions. The new 2,500 hp engines for the blowers can be electric 

driven. Table 6-9 shows the blower selection for the Advanced Basic BNR level of treatment. 

Table 6-9: Blower Selection at the Advanced Basic BNR Level of Treatment 

Air Blower Required Air Required 

Level of 

Required (5) Capacity Blower Provided Design 

Treatment 

Quantity 

Quantity 

scfm scfm 

scfm 

Advanced 66,000 43,000 2 84,000 N+2 

Basic BNR 94,400 43,000 3 129,000 N+1 

Total 

Blowers 

for 

Design 

Level 

4 

6-10



DRAFT 

The dimensions of the HT-series blowers are not much greater than the existing HR-series 

blowers and will fit within the available footprint for all alternatives. Figure 6-2 shows the 

comparison in blower dimensions. 

Figure 6-2: Blower Sizing Comparison 

225” – Existing (HR-series) 

271” – Proposed (HT-series) 

120” – Existing (HR-series) 

138” – Proposed (HT-series) 

The existing blowers will be replaced with the new blowers in the existing blower and engine 

room within the main building with a minimum of 10 feet between each unit. The lube system 

will be integrated into the blower base. All alternatives will require demolition of virtually all 

the blower related equipment as shown on Drawing 16. 

With a greater air capacity flowing through the blower room, the inlet air filtration system will 

be upgraded. The existing baghouse collectors will be replaced by four 43,000-scfm collectors 

to provide similar operational redundancy as the blowers. Due to the increased blower size, the 

inlet flanges on the new blowers must be replaced. This includes valves, silencers and pitot 

tubes. The 66-inch diameter inlet air header will also be modified. The segments that include 

the wye connection to each blower must be increased and segment that is directed to the current 

fifth blower can be demolished. 

After the blowers, two 50-inch diameter headers will replace the 42-inch diameter air main 

header leaving the main building. Each header will be supplied by two blowers and will connect 

via a motorized butterfly valve into a new 70-inch air main header. To accommodate the new 

50-inch headers, one will run beneath the blower room (similar to the existing system) while the 

other header will be directed just outside of the main building and will run parallel to the new 

header, below the inlet header. The 70-inch air main header will start where the current 42-inch 

air main header exits the main building and run along the same path to the aeration tanks. The 

startup bypass piping and valves will be replaced, but will still connect to the raw air plenum for 

atmospheric blowoff. Drawing 17 shows the process schematic for this design. 

An increase in electrical demand is anticipated with the installation of at least four 2,500 hp 

blower engines, which is significantly higher than the existing blowers. Additional power will 

be required for the associated valves and equipment within the system. 

6-11



DRAFT 

Each blower will come equipped with a new blower control panel that will be connected to the 

associated valves and lube oil system. A new blower system control panel will be installed that 

will oversee all the new blowers as well as the related appurtenances, including the motorized 

butterfly valve connecting the two blower headers. The blower will be controlled based on 

maintaining a pressure setpoint and air flow will be controlled by the DO/airflow control system 

installed on the header to each pass. 



technology. 





Objectives: 






Parameters: 



• Operating Range: 23.5 to 102 mgd 


The required RAS capacity of 85 mgd total can be achieved with the existing 22.6 mgd pumps (4 

operating and 2 standby). The installation of magnetic flow meters in lieu of the existing 

ultrasonic flow meters is recommended. 



Objectives: 




Aeration Tank 



6-12



DRAFT 


Parameters: 



• WAS Design flow operating range: 1.7 – 6.8 mgd 

While design guidance seeks WAS flexibility that allows for 20% AT effluent, a combination of 

draw from RAS and AEMLSS is assumed. Based on pump sizing, waste sludge wet well and 

gravity thickener surface overflow limits, the capability to pump all 20% of AT effluent flow is 

not recommended. WAS normal operating range shall be maintained at 1.7 – 6.8 mgd (per 

design guidance), but AT effluent will not approach 34 mgd. The existing pumping arrangement 

will allow for pumping capacity to address the range of MCRTs and solids concentrations 

envisioned. Pumps will be able to handle anticipated flow with two pumps running, one standby 

and one spare (N+1+1). 

By increasing WAS draw from RAS distribution box weir to 6.8 mgd (per design guidance), 

flow through the existing 12” line between the RAS box and WAS wet well more than doubles. 

At this flow level, the velocity within the 12” pipe exceeds recommended maximum sludge flow 

velocities and can lead to chipping and erosion of the pipe. Therefore, the existing pipe will be 

replaced by a single 18” line (see Drawings 21 and 22); thereby lowering the maximum velocity 

created in each WAS pipe. The minimum recommended velocity is also maintained in order to 

prevent sludge settling in the piping. 

Proposed improvements include an upgrade of the WAS flow metering being used at the North 

River WPCP. The existing ultrasonic meters being used to monitor the WAS flowrates will be 

removed and replaced by magnetic flow meters that can transmit flow information to the central 

control system. These flow meters will be installed on all three influent lines entering the WAS 

Wet Well. 







Once at the surface, the froth tends to stay there causing the operational problems. 






6-13



DRAFT 





follows: 


pass length 








Each AT at North River is covered and can utilize that cover as part of an FCH. A typical FCH 

includes chemical storage and feed, dilution water pumping, distribution system, nozzles to spray 

the chlorine solution onto the water surface and protective enclosures to avoid personnel contact 

with the chlorinated spray. The chemical storage and feed facility will be described in the RAS 

Chlorination section. 

As indicated above, a total of four FCHs will be required per tank. Penetrations will be cut-out 

of the AT roof slab at the required locations (locations seen in Drawings 6 and 8). These 

penetrations will be large enough to construct a FCH structure. This structure will allow 

personnel access to nozzles and nozzle piping (on the upstream end), and retractable baffle 

segments (on the downstream end). An FCH will be constructed with adjacent, removable air 

tight hatches installed above the penetrations. 

The upstream hatches will provide personnel access to spray headers that will be installed 

approximately 2 feet above the existing roof with connectors, nozzle pipe leads, nozzle fittings 

and nozzles to apply the chlorinated spray. Removable nozzle pipe segments will extend from 

the header, through the roof penetration, and into the enclosed treatment area within the tank. 

The distance between nozzle connections will be determined by the nozzle type and dose 

requirements. It can be assumed that approximately six nozzle connections will be installed per 

hood. The spray nozzles will be installed at approximately 3 feet above the water surface to 

provide enough elevation for sufficient spray coverage. Each individual spray nozzle pipe lead 

will be provided with individual quick disconnects or unions to facilitate removal for 



main. There will be distribution piping extended from the main to the side of each of the FCH 

structures. From there it will be divided into each of the nozzle pipes. A schematic of the froth 

system piping is shown in Drawing 23. 

6-14



DRAFT 

The downstream hatches will provide personnel access to the sliding retractable baffle segments. 

These segments will be lifted in unison by an actuated mechanism located atop the FCH 

structure. These adjacent flaps will span the width of the pass and extend below the water 

surface to trap the foam within the enclosed hood area. The flaps will facilitate the trapping of 

the froth to ensure effective chlorination. They shall be retractable by mechanically sliding them 

up to allow any trapped material to flow freely on the surface of the water when the FCH is not 

in use. A mechanism will be included to lock the flaps into place when raised by personnel. 

Detail drawings of the FCH can be seen in Drawings 24 and 25. 

Chlorine storage, feed and distribution throughout the plant is included in Section 6.8.2. Piping 

will be used to bring the chlorine solution from the distribution main to each hood. A dual 

strainer will be installed for each aeration tank with an interconnection that will allow it to serve 

two tanks, providing sufficient redundancy. 

The proposed froth control hoods including the retractable baffle and spraying apparatus will 

increase the weight on the structural support system for the ATs. This increase will be minimal 

compared to the current loading, but the structural system should be verified in future design 

phases and additional support provided where necessary. 



formation and poor settling secondary solids. 






The chemical feed system is being coordinated with the froth control hoods. The maximum 

sodium hypochlorite usage rate for BNR upgrades estimated by this conceptual design indicates 

that approximately 42,000 gallons of hypochlorite storage will be needed in order to meet the 5- 

day storage requirements for both RAS chlorination and froth control. It is assumed that the 

existing five 10,000 gallon tanks cannot handle this additional storage, and therefore, a new 

system, dedicated to BNR hypochlorite uses, will be provided. The system will contain six 

double walled fiberglass storage tanks within a containment area, 2 active and 2 standby 

chemical feed metering pumps, and double-walled chemical piping to each point of use. Level 

sensing will be provided and an indication panel will be provided for both the storage tanks and 

fill connection point. The hypochlorite will be delivered via a chemical fill station, complete 

with spill containment provisions, by way of the existing south road. 

The existing chlorination building does not have room for additional storage tanks. It is 

proposed that a new structure be constructed within the unassigned areas below the secondary 

6-15



DRAFT 

settling tanks. The new structure will house the storage tanks and chemical feed metering pumps 

in a containment area. Drawing 26 shows a schematic of the hypochlorite storage and 

distribution system for BNR uses. Drawing 27 shows a part plan of the hypochlorite storage 

area. 

A new chlorine room will be constructed and will be coordinated with the supplemental carbon 

(methanol) storage facilities. The creation of a chlorine room is included in the supplemental 

carbon (methanol) section. There will also be six sodium hypochlorite tanks with a combined 

load of 50,000 pounds. 

Level sensing will be provided at the new storage tanks with level indication at the point of fill 

connection. A Programmable Logic Controller (PLC) panel for feed control shall also be 

provided. 


Surface wasting from the aeration tanks is one of the required applications to effectively control 

froth and contribute to MCRT control. Currently there is no surface wasting capabilities at the 

North River WPCP. 


froth formation and provide MCRT control. Implementation of surface wasting to control the 

secondary treatment process reduces the potential for froth formation. The design objectives as 

described in the BNR design guidance document include: 






• Allow for the wasted solids to be accounted for within the MCRT calculations 

A new surface wasting pump station will be constructed in the Pass A oxic zone of each of the 

aeration tanks. A downward-opening sluice gate will allow the froth to flow into the wasting pit. 

The gate will be automatically controlled to rise and fall with the aeration tank water elevation or 

manually controlled for simplicity of operation. Froth will also be wasted through a floating 

weir device. Attached to the pump station via a slide gate, the weir will move along with the 

water elevation within the tank and collect froth. A neutral buoyancy flexible hose will allow the 

weir to be relocated within aeration tank to where frothing is observed. 

In the wasting pit, a submersible 100-gpm pump will remove the surface wasting and direct it 

towards the WAS wet well. Each line will be provided with valves for increased control and a 

connection for hypochlorite addition. The pump station will be located near the second froth 

control hood within Pass A to utilize a common access hatch and for connection to the 

hypochlorite dosage lines. The submersible pump will be attached to a rail system allowing 

6-16



DRAFT 

removal of the pump through the access hatch. A level sensor will be installed within the 

wasting pit for level control of the pump operation. The discharge lines will also be equipped 

with a meter for individual flow measurement. The flow will be totalized and TSS 

concentrations will be monitored via sampling to aid in the SRT control. Drawings 28 and 29 

show the flow schematic, and detail and section views of the surface wasting system. 



Alkalinity addition is not provided at the Advanced Basic BNR level of technology. 

6.9.2 Carbon 

Carbon addition is not provided at the Advanced Basic BNR level of technology. 

6.9.3 Polymer 

The addition of polymer will be provided to enhance the settling of solids in the secondary 

settling tanks and reduce the development of froth in the secondary system. 

The design objectives and features as described in the BNR design guidance for polymer 

addition include: 

• Polymer addition must allow for sufficient mixing to optimize polymer efficiency. 

• Polymer feed rate must provide for 0.5 to 3.0 mg/L in the mixed liquor stream. 

• Polymer addition should be flow paced. 

Polymer addition capabilities will be provided through the use of two 550-gallon bulk polymer 

polyethylene storage tanks with spill containment provisions, one active and one standby 

polymer mix feed systems, and a channel diffusing device to introduce and mix the polymer into 

the mixed liquor stream immediately upstream of the final settling tank influent channels. The 

polymer will be delivered via a chemical fill station, complete with spill containment provisions, 

by way of service road “B”. The proposed location for the system is within the unassigned areas 

below the final settling tanks. The polymer feed system will require plant effluent water to carry 

the polymer to the dose point. At this conceptual design level, the plant effluent water demand 

will be approximately 4,220 gph. 

Drawing 30 shows a schematic of the polymer mix feed system for BNR uses. Drawing 31 

shows a part plan of the polymer storage area. Drawing 32 shows a part plan of the polymer 

distribution to the final settling tank influent channel and a section detailing the diffuser 

distribution piping. 

The two polymer storage tanks will need to be housed within a containment area and will create 

a new load of 15,000 pounds. A foundation may be required to distribute the load to the existing 

caisson system. 

6-17



DRAFT 

The majority of the power requirements are due to the polymer mix/feed system. The two sets of 

motors consist of a 1-hp 90 VDC mixer motor and a 0.5-hp 90 VDC metering pump motor. 

Level sensing will be provided at the new storage tank with level indication at the point of fill 

connection. The guidance calls for polymer addition to be flow paced. Therefore, the polymer 

mix feed system will include a flow signal (4-20 mA) for polymer pump pacing. The flow signal 

sends a discrete output to the plant SCADA system, and should have little to no effect on plantwide 

systems. 











Due to the proximity of the facility to the public, all new facilities will be provided with odor 

control equipment. The objective of the odor control facilities is to treat the air from new or 

modified facilities that have the potential for odors. 

There are currently three separate odor control facilities operating at the North River WPCP to 

treat the air collected from the primary, secondary and sludge processing areas. Each system 

consists of wet scrubbers and activated carbon adsorption units. 

The system will consist of chemical wet scrubbers followed by carbon adsorption. The size of 

the system is based on the size of the proposed facilities and the necessary air exchanges for each 

facility. The odor control system will collect and treat the air from all new facilities to remove 

odorous compounds prior to discharging the air to the atmosphere. 

In order to facilitate the newly constructed facilities for the various alternatives, it will be 

necessary to construct a new structure in the Hudson River on the South end of the North River 

WPCP. Space will be allocated for the odor control equipment as well. A flow conduit structure 

will also be required for several alternatives and will require structural support as well. 

6-18



DRAFT 



The principal function of the primary settling tanks is to removal particulate material to reduce 

the load on the secondary system. In addition, the PSTs contribute to the overall hydraulic 

profile of the facility. In order to implement improvements in downstream facilities (flow 

distribution in aeration tanks), additional head will be required. 

A major source of head loss will be the new flow distribution and control chambers that are 

described in a later section. To gain a portion of that head loss, it is proposed to increase the 

water surface level of the primary tanks by approximately 1 foot. Additional head beyond that 

gained in the PSTs can be gained by downstream processes and is described in the Aeration 

Tanks Flow Distribution section. Detailed hydraulic design will refine the necessary water 

surface level. 

In order to increase the water surface level in the primary settling tanks, the primary settling tank 

effluent weirs must be removed and replaced by new weirs at a higher elevation. There currently 

exists almost 3 feet of available space above the primary settling tanks water surface level and a 

reduction by 1 foot will still allow sufficient freeboard in the primary tanks. This will impact the 

scum collection system, which must be modified. Modification of the sludge collection 

mechanism to return the scum collecting flights at the higher water surface elevation will be 

required to facilitate scum removal. Scum collection troughs will also be updated. The proposed 

modifications can be seen on Drawing 1. 











Full Step BNR 10% 40% 30% 20% 


distribution and gate setting. The proposed design for Full Step Feed BNR includes relocation of 

the motorized gate currently located at the head of Pass D (in tanks 3201-3204) and installation 

7-1



DRAFT 

of a new automated gate at the head of said pass. This relocation includes the demolition of the 

existing 42” x 42” sluice gate and the construction of a new 42” x 42” sluice gate downstream of 

the newly built baffle between Passes C and D. 

This proposed design requires modification of the existing influent sluice gates at the head of all 

passes to improve flow distribution. At each gate location, the existing gate will be demolished 

(see Drawing 7) and an influent flow distribution and control chamber will be installed (see 

Drawing 8 for location of control structures and Drawing 9 for details and sections). This will 

require penetrations through the roof of the AT at the required locations to allow access to the 

gates. The flow will enter the chamber from a new 60” x 60” sluice gate and flow upward to a 

set of downward opening flow distribution gates. Flow will continue over the gates and drop to 

the free surface water of the aeration tanks. This will require additional head, but will allow for 

positive flow control at each pass without being impacted by the water level in the aeration tank. 

Pass D will include an actuated gate that will allow for rapid response to high flows. A gate 

controller will be connected into the plant SCADA control system to allow for either flow paced 

or manual control. Flow monitoring will be accomplished by measuring the water surface 

elevation over the weir compared against the setting of the sluice gates. 

In order to implement flow distribution improvements in the aeration tanks, additional head will 

be required. To gain a portion of that head loss, it is proposed to raise the water surface level of 

the primary tanks by approximately 1 foot (see primary settling tanks section). It is anticipated 

that more than one foot will be required. In addition to the primary settling tanks it is proposed 

to lower the aeration tank effluent troughs to reduce the downstream head within the tank. 

Detailed hydraulic design will refine the necessary water surface level. 




are seen below in Table 7-2 and a sketch of these locations is seen in Drawings 6, 8 and 10. 



(between (between (between (between (between Preanoxic 

Pass 

zones 

successive successive Anoxic/ Oxic and 

Anoxic/Switch Anoxic/Switch Switch and Pre-anoxic and subsequent 

zones) 

zones) Oxic zone) zones) Pass) 

A 1/6 length of pass N/A 


pass of pass 

N/A 

B 1/6 length of pass N/A 


N/A 

C 1/6 length of pass N/A 

D 1/6 length of pass 1/3 length of pass 

pass 

1/3 length of 

pass 

1/2 length of 

pass 

of pass 

10% of end 

of pass 

N/A 

N/A 

N/A 

7-2



DRAFT 

The design locations of the Full Step BNR baffle walls will be optimized to stay consistent with 

the design guidance. This upgrade requires a total of 15 baffle walls per tank; fourteen similar to 

those described in Section 6.3.2 and in Drawing 11 and one to accommodate Pass B/C structural 

requirements. Penetrations will be cut in the existing roof slab at each installation location and 

the roof will be replaced with a removable air tight hatch to allow access by plant personnel. For 

ATs 3201-3204, this option requires the demolition of the existing inter-pass baffle walls 

between Passes A/B, B/C and C/D. These baffle walls will be replaced with new, 18” thick 

inter-pass baffle walls located to remain consistent with design criteria and maintain equal 

volume in each pass. The existing wall that separates passes B and C currently extends the full 

height of the tank except for a 10’x 12’ opening in the bottom that facilitates flow between 

passes. These B/C walls will be fixed and non-modular in nature but will allow a free surface of 

water to overflow the baffle to avoid froth trapping and still have openings in the bottom to 

facilitate drainage and filling of the tank. 

In tank 3205, the existing inter-pass walls between A/B and C/D are located consistent with the 

guidance and can be modified rather than replaced to match the other baffle walls. A 

modification similar to those in ATs 3201-3204 will be made to the inter-pass wall between B/C. 











Full Step BNR 6,558 3,810 2,899 2,500 



varying process temperatures; thereby possibly changing mixer requirements. Based on the 

anticipated mixed liquor concentrations and the zone sizing, the required horsepower was 

estimated as shown in Table 7-5. 

7-3



DRAFT 

Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 23,543 23,543 87,109 7,063 

Pass B 23,543 23,543 87,109 7,063 

Pass C 23,543 23,543 80,047 14,126 

Pass D 23,543 23,543 23,543 70,629 

Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

Pass A 8.7 8.7 N/A 2.6 

Pass B 7.4 7.4 N/A 2.2 

Pass C 6.8 6.8 N/A 4.1 

Pass D 6.5 6.5 6.5 N/A 






Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 









7-4



DRAFT 

A description of the air distribution and control design needed for the Full Step BNR level of 














(scfm) 


Required (1) 

Full Step BNR 66,000 44,100 












Level of 

Treatment 


Nitrogen BOD 

Oxidized (2) Oxidized (3) 

Aeration 

Oxygen 

Tank 

Required (4) 

Loading 


Air 

Required (5) 

Full Step Average 22,500 177,800 298,900 66,000 

BNR Peak Daily 29,900 263,500 427,500 94,400 







7-5



DRAFT 

(5) Air required = 0.04*O 2 required / Overall Efficiency; Overall Efficiency = 18% for Advanced Basic BNR 

For the Full Step BNR level of treatment, the air requirements were determined at both the 

average and peak daily loading conditions, where influent BOD was completely oxidized and 

influent TKN was reduced to 2 mg/L in the final effluent. Since the aeration tanks at North 

River are deeper than most of the aeration tanks at other NYCDEP WPCPs (29.6 feet versus 15 

feet, typically), the overall oxygen transfer efficiency is greater than typically observed. Higher 

mixed liquor concentrations result in a lower alpha factor, which impacts oxygen transfer 

efficiency. 

As discussed in Section 6.4 and shown in Figure 6-1, the average loading conditions could 

theoretically be met for the Step Feed BNR technologies, but the facility would be operating with 

all blowers and not provide the spare and standby requirements identified in the BNR design 

guidance documents (N+2) for average conditions. A new process air blower system is required 

as part of the proposed Full Step BNR upgrade designs. A description of the new blower system 

is provided in Section 6.4. 

Table 7-9 shows the blower selection for the Advanced Basic BNR level of treatment. 

Table 7-9: Blower Selection at the Full Step BNR Level of Treatment 


Level of 


Treatment 

Quantity 

Quantity 

scfm scfm 

scfm 

Full Step 66,000 43,000 2 84,000 N+2 

BNR 94,400 43,000 2 129,000 N+1 

Total 

Blowers 

for 

Design 

Level 

4 



technology. 





Objectives 





Parameters 

7-6



DRAFT 



• Operating Range: 23.5 – 170 MGD 



To achieve desired flow capacity with the same number of units in operation and standby as the 

existing operational scheme, larger pumps are required. The existing pumps cannot be retrofitted 

or modified as-is to increase their capacity from the current 22.6 mgd to the required 42.5 mgd 

(170 mgd total). Respective suction and discharge piping for each pump must also be replaced. 

Furthermore, the existing 54” suction and 42” discharge headers are insufficient to handle the 

proposed flow and must be replaced by larger piping and valves. The demolition of existing 

facilities can be seen in Drawing 19. The proposed RAS system is shown in Drawing 20. 


A description of the modifications to the Waste Activated Sludge System needed for the Full 

Step BNR level of technology was provided in Section 6.7 for the Advanced Basic BNR 














New York wastewaters are typically low in alkalinity and the nitrification process can consume 

significant amounts of alkalinity. Consumption of alkalinity can decrease pH and the rate of 

nitrification. Therefore, alkalinity addition is an important component of BNR strategies. The 

design objectives and features include the following: 


7-7



DRAFT 

• Maintain 50 to 100 mg/L CaCO 3 in all passes. 




The proposed conceptual design provides a liquid chemical system based on caustic soda (50 

percent sodium hydroxide). The system includes six-6,000 gallon fiberglass reinforced plastic 

(FRP) liquid chemical storage tanks (total storage 36,000 gallons). The storage tanks will be 

insulated and heat traced to avoid crystallization of the caustic. The storage tanks will be located 

inside what is currently known as “Unassigned Area No. 1.” Delivery will be accessible through 

a chemical delivery station located on “Existing Service Road B.” Two-2 hp metering pumps 

will distribute the chemical to the RAS distribution box. Dosing rate will be controlled by pH 

that is monitored in the aeration effluent channel as recommended by the BNR design guidance 

documents. The capability for flow-paced control will also be incorporated into the control 

logic. The system will be connected to the plant wide SCADA system. 

Drawing 33 shows a schematic of the alkalinity feed system. Drawing 31 shows a part plan of 

the alkalinity storage area. Drawing 32 shows a part plan of the alkalinity discharge to the final 

settling tank influent channel and a section detailing the diffuser distribution piping. 

Power supply to the storage tanks will be required. The tanks will include level sensors. Power 

supply, instrumentation and control wiring will be required at the metering pumps. The chemical 

storage area will require potable water connections for drench showers and eyewash, wash down 

water supply and connection to the plant drain system. Level sensing will be required in each 

storage tank. pH will be monitored at the Aeration Effluent Channel and tied into the control of 

the metering pumps and the plant SCADA system. The capability for flow-paced control will be 

incorporated to the control system. 

7.9.2 Carbon 


available in the wastewater may be insufficient to promote sufficient denitrification to meet low 

levels of nitrogen. Supplemental carbon addition will be required for the nitrogen removal 

design alternatives. 

The design objectives and features include the following: 

• Provide supplemental carbon to enhance denitrification 

• Provide capability to feed to the head of all anoxic zones 


BOD, and TKN with a feedback bias based on residual nitrate measurement 

• Provide mixing at dosage points 


7-8



DRAFT 




systems are subject to the regulations of several entities including the Department of 


guidelines provided by independent associations such as the National Fire Protection Association 

and the Manufacturing Chemists Association; and precautions and requirements imposed by 

insurance providers. It is important to recognize that, in addition to basic system requirements 

identified by the conceptual design needs, a methanol system will have ancillary requirements, 

such as the need for explosion proof equipment and lighting, which will contribute significantly 

to the cost of the installation. 




chemical in the process stream. A separate chemical mixing device will not be provided. Tanks 

will be designed for a unit volume of 22,440 gallons with the number of tanks varying based on 

the design technology. Pump capacities vary based on the technology. Schematics for Full Step 

BNR are shown in Drawing 34. 

The storage tanks will be located in what is currently known as “Unassigned Area No. 2.” This 

area must be entirely enclosed as a separate room since methanol is highly flammable. 

Construction of this room will be coordinated with the new RAS chlorination facility. Chemical 

unloading will be available through a chemical delivery station located on the “South Road.” 

Drawing 37 shows the plan views of the methanol storage area for the Full Step BNR. 

The storage tanks will need appropriate foundations. A new storage room will be constructed 

within the existing facility. Lightweight concrete will be used to minimize the loading on the 

existing support structure. 

Power supply to the new systems will be required. All equipment and systems associated with 

the methanol unloading, storage, and feeding must be explosion-proof and rated for Class 1, 

Group D, Division 1 or 2 uses. This includes the structures, doorways and lighting. 

The chemical storage area will require potable water connections for drench showers and 

eyewash, wash down water supply and connection to the plant drain system. Due to the 

flammable nature of methanol, fire protection such as sprinklers should be provided. 

Level sensing will be required in each storage tank. Additional lower explosive limit and other 

fire protection instruments and controls may be required based on code and final design 

requirements for storage of a flammable liquid. 

7.9.3 Polymer 

7-9



DRAFT 

A description of the Polymer addition design needed for the Full Step BNR level of technology 












A description of the odor control system needed for the Full Step BNR level of technology was 

provided in Section 7.12 for the Advanced Basic BNR treatment option. 

7-10



DRAFT 



A description of the modifications to the Primary Settling Tanks needed for the Full Step BNR 

with Solids Filtration level of technology was provided in Section 7.1 for the Full Step BNR 

















BNR with Solids Filtration level of technology was provided in Section 6.3.4 for the Advanced 

Basic BNR treatment option. 









8-11



DRAFT 









A description of the Waste Activated Sludge System design needed for the Full Step BNR with 

Solids Filtration level of technology was provided in Section 6.7 for the Advanced Basic BNR 

Design. 













option. 




Filtration level of technology was provided in Section 7.9.1 for the Full Step BNR treatment 

option. 

8-12



DRAFT 

8.9.2 Carbon 



8.9.3 Polymer 

A description of the Polymer addition design needed for the Full Step BNR with Solids Filtration 


option. 








technology. 



technology. 



technology. 


A description of the odor control system needed for the Full Step BNR with Solids Filtration 

level of technology was provided in Section 6.12 for the Advanced Basic BNR treatment option. 

8-13



DRAFT 




with Microfiltration/Ultrafiltration level of technology was provided in Section 7.1 for the Full 



No fine screens are needed for the Full Step BNR with Microfiltration/Ultrafiltration level of 

technology. 

















the Advanced Basic BNR treatment option. 






9-1



DRAFT 













Microfiltration/Ultrafiltration level of technology was provided in Section 6.7 for the Advanced 

















9-2



DRAFT 




9.9.2 Carbon 




9.9.3 Polymer 

A description of the Polymer addition design needed for the Full Step BNR with 






technology. 




Conditions with Microfiltration/Ultrafiltration treatment option. 








A description of the odor control system needed for the Full Step BNR with 

Microfiltration/Ultrafiltration level of technology was provided in Section 6.12 for the Advanced 


9-3



DRAFT 




with Denitrification Filters level of technology was provided in Section 7.1 for the Full Step 



Filter and membrane technologies require more-advanced removal of influent solids than is 

typically achieved by conventional settling. Fine screens can be used to remove solids from 

process effluent that may cause clogging of the filters or membranes reducing their treatment 

efficiency and increasing maintenance requirements. 

The design objectives of the fine screening process for Full Step BNR with Denitrification Filters 

include: 

• Remove particles larger than 2 mm from secondary effluent for Full Step Feed BNR with 

Denitrification Filter alternative 



• Provide odor control for fine screening process area 

The proposed design for the fine screening process at the North River WPCP consists of a new 

facility to house the screening units and to facilitate the removal of the screens solids. For the 

Full Step Feed BNR with Denitrification Filters alternative, secondary effluent will be diverted 

from the Final Settling Tank effluent channel and the screened effluent discharged to the new 

Denitrification Filters. 

The screening facility will be designed to process 281 MGD (1.5 x DDWF plus recycles). The 

proposed screening facility will consist of ten (10) rotating disc screens with a capacity of 32 

mgd each. Nine (9) units will be required during peak flow with one (1) unit available on 

standby. Each screening unit will feature a 2-mm screen perforation and will be connected to a 

spray water system to remove the collected screenings from the screen panels. The spray water 

system will be connected to the plant’s existing effluent water system or will utilize the 

screening effluent to wash the screen panels. The screenings residuals and washwater will be 

discharged to a collection trough and will flow by gravity to a wet well from where it will be 

pumped to the sludge thickeners. Each of the ten (10) screening channels will be approximately 

8 feet wide by 20 feet deep. A sluice gate at both ends of each channel will be installed to isolate 

the channel for maintenance. 

There is no space within the existing footprint of the plant that will accommodate the 

construction of these channels and the existing platform must be extended. This will require the 

installation of new caissons to support the platform extension. The platform extension will also 

10-1



DRAFT 

support the electrical, HVAC, and odor control systems associated with the fine screening 

facility. The extension will be enclosed to facilitate odor control of the fine screening facility. 

Under the Full Step Feed BNR with Denitrification Filter alternative, the screening facility will 

be located to the south of the existing Digester Tanks adjacent to the existing structure and the 

new Denitrification Filters. The proposed upgrades can be seen in Drawings 2, 3, 4 and 5. 

Odor control will be provided for the screening area and coordinated with the other new facilities 

installed for each option. This system will consist of chemical wet scrubbers followed by carbon 

adsorption. The odor control system will collect and treat the air from within the screening 

facility to remove odorous compounds prior to discharging the air to the atmosphere. 

Dedicated HVAC systems will be incorporated into the design of the new screening facility and 

no additional load will be placed on the plant’s existing HVAC systems. No impact is 

anticipated. 

Plumbing requirements for the new screening facility will be coordinated with the plumbing 

requirements for the new platform extension and will be connected to the plant’s existing 

plumbing system. In addition to general plumbing requirements, emergency eyewash and 

shower facilities will be required in the vicinity of the chemical storage and feed equipment for 

the odor control system. 

Instrumentation and controls requirements for the new screening facility will be coordinated with 

the instrumentation and controls requirements for the new platform extension and will be 

connected to the plant’s existing controls system. Spare equipment will require storage. 













10-2



DRAFT 


BNR with Denitrification Filters level of technology was provided in Section 6.3.4 for the 



















Denitrification Filters level of technology was provided in Section 6.7 for the Advanced Basic 

BNR Design. 









option. 

10-3



DRAFT 




option. 





10.9.2 Carbon 



The carbon addition system for the Full Step BNR with Denitrification Filters level of 

technology will consist of storage tanks with appropriate unloading and spill containment 

provisions, metering pumps, and chemical piping, as shown in Drawing 35. Drawing 38 shows 

the plan views of the methanol storage area for the Full Step Feed BNR with Denitrification 

Filters design level. 

10.9.3 Polymer 

A description of the Polymer addition design needed for the Full Step BNR with Denitrification 


option. 




technology. 



technology. 


Serving as an enhancement to the Full Step Feed BNR design, Denitrification Filters can be 

added downstream of the final settling tanks to treat nitrified secondary effluent. 

10-4



DRAFT 

The addition of Denitrification Filters to the Full Step Feed BNR design level will achieve lower 

levels of nitrogen and provide filtration to remove additional particulate matter from the waste 

stream. The addition of denitrification filters allows the step feed process tanks to operate with 

additional aerated zone volume to enhance the nitrification process. Enhanced levels of 

denitrification can be achieved in the denitrification filters. The objectives include: 





The Denitrification Filters will be located downstream of the FSTs and upstream of disinfection 

at North River. A new structure will be constructed on the south end of the plant to house the 

new equipment. The design of the Full Step Feed BNR upgrades includes switch zones that 

allow the activated sludge process to operate with additional oxic volume to enhance the 

nitrification capability. No additional facilities will be required for the aeration tanks. 

Nitrified settled secondary effluent will be directed to a new pump station by gravity flow 

through a new conduit. The pump station will then direct the secondary effluent through the fine 

screens facility and then the denitrification filters. Denitrification filter effluent will flow by 

gravity to the existing disinfection system. Methanol will be added as a supplemental carbon 

source downstream of the final settling tanks. Drawing 55 shows the process flow diagram. 

Drawing 56 shows a process flow schematic. Plans and sections of the facilities are shown in 

Drawings 57 through 60. 


secondary effluent and supplemental carbon flow through the biomass-enriched media, 

denitrification will occur, as well as removals of particulate matter. The denitrification process 

will be supported by maintaining an anoxic state within the filters and by having a supplemental 

carbon addition point upstream of the filters. The biomass responsible for denitrification will 

utilize the supplemental carbon and any inherent carbon in the secondary effluent. 

To maintain the efficiency of the Denitrification filters, periodic backwashing must be performed 

to remove the accumulated solids from between the media particles. Equipment will be provided 

that will flush the media by recycling the treated effluent to serve as washwater. A blower 

system will also be provided for air scouring of the media when the filter units are not operating 

in a denitrification mode. The reused effluent and released solids will then be directed to the 

gravity thickeners. 

Odor control will be provided as part of the odor control system for the new structure that also 

houses the new fine screens facility. This system will consist of chemical wet scrubbers 

followed by carbon adsorption. The odor control system will collect and treat the air from within 

the facility to remove odorous compounds prior to discharging the air to the atmosphere. 

10-5



DRAFT 

In order to facilitate the required facilities for the denitrification alternative, it will be necessary 

to construct a new structure in the Hudson River on the South end of the North River WPCP. A 

flow conduit structure will also be required to be built to provide a path for certain process flows 

to and from this structure. This conduit will run along the West side of the building, also in the 

Hudson River. This will be a substantial undertaking that will require a new structural support 

system. 






of the building footprint, height, and width of flow conduit are shown in Table 10-1. 

Table 10-1: Approximate Denitrification Filters Structure Dimensions 






technology. 


A description of the odor control system needed for the Full Step BNR with Denitrification 

Filters level of technology was provided in Section 6.12 for the Advanced Basic BNR treatment 

option. 

10-6



DRAFT 



The construction of the Membrane Bioreactor alternative calls for the complete demolition of 

primary settling tanks. 


Fine screens are included in the Membrane Bioreactor alternative. The design objectives of the 

fine screening process include: 

• Remove particles larger than 2 mm from primary effluent 



• Provide odor control for fine screening process area 

The proposed design for the fine screening process at the North River WPCP consists of a new 

facility to house the screening units and to facilitate the removal of the screens solids. For the 

Membrane Bioreactor Tanks alternative, primary effluent will be diverted from the Primary 

Settling Tank effluent channel to the screening facility and the screened effluent will be 

discharged to the new Pre-Anoxic Tanks influent channel. 

A description of the screening facility is provided in Section 10.2. For the Membrane Bioreactor 

Tank alternative, the screening facility will be located to the south of the existing Digester Tanks 

adjacent to the existing structure and the new Pre-Anoxic Tanks. The proposed upgrades can 

be seen in Drawings 2, 3, 4 and 5. Odor control, HVAC systems, plumbing requirements, and 

instrumentation and controls requirements for the new screening facility are described in Section 

10.2. 



Flow distribution and control is an important factor that can affect nitrogen removal performance 

of any BNR process. The constraints for flow distribution at North River WPCP include the 

existing hydraulic profile, tank size, channel internal structure, and flow requirements. The 

following are the major design objectives and parameters for MBR treatment. 

Objectives: 

• Provide capability to direct 100% of influent flow into Aeration Tank influent channel 

Parameters: 

• Design flow: 90 mgd (1.5 x DDWF) 

11-1



DRAFT 





below. 





The entire flow distribution of the aeration tanks will change. To implement the MBR process, 

primary settled flow will be directed off site to a screening facility. Screened effluent will be 

combined with aeration tank effluent (internal recycle) and pass through new pre-anoxic tanks 

for partial denitrification. Flow will continue to a new wet well where it will meet the MBR 

RAS flow. The combined flow will be pumped by a new intermittent pumping station to the 

head of the existing aeration tanks for subsequent nitrification. A portion of the aerated effluent 

will be returned by a gravity channel back to the new pre-anoxic tanks and the remainder will 

continue to the post anoxic tanks and then the membrane filtration facilities (both constructed 

within the existing final settling tanks). 

The existing aeration tanks will be modified to include new influent and effluent channels, and a 

pre-anoxic zone. Each aeration tank will be modified such that all of the flow moves in the same 

direction. All of the existing AT inter-zone baffles will be demolished in order to provide oxic 

zone capacity for the flow. The existing common influent channel does not have sufficient 

capacity to handle the expected increase in flow required for the MBR process. Furthermore, the 

existing channel must be maintained and isolated so that primary effluent flow can be drawn and 

moved by gravity to the off-site treatment area. Therefore, a new influent channel for the ATs 

must be constructed within the existing tankage. To achieve required capacity and allow for the 

incoming piping, a 20’ wide by 20’ tall influent channel must be constructed. The existing ATs 

will be converted into ten separate passes to be fed by the common influent channel. Each pass 

will be fed through four 48” x 48” sluice gates and will consist of an oxic zone (95% of pass 

volume) followed by a pre-anoxic zone (5% of pass volume). The effluent end of the ATs will 

also be modified to allow the aerated effluent to travel over weirs and into the effluent channel. 

The effluent channel must also be expanded to allow free flow over each weir segment. 

Demolition of the existing step-feed influent channel is not recommended due to its structural 

use. A Plan of the influent distribution and effluent weirs is shown in Drawing 10. 





locations is seen in Drawings 6, 8 and 10. 

11-2



DRAFT 


Baffle 1 

(between Oxic and Pre-anoxic zones) 


A description of the baffle walls is given in Section 6.3.2, and an example of a typical baffle 

wall can be seen in Drawing 11. 

To accommodate the required tank modification and oxic capacity for this alternative, all 

existing baffle walls must be demolished. In order to provide the pre-anoxic capacity at the end 

of each pass (5% of pass volume), one baffle wall must be installed in each AT pass, as indicated 

in Table 11-3. 

Table 11-3: Membrane Bioreactor Baffle Walls 

Number of Baffle Walls 

Tanks Demolition New Modification 

3201-3204 (each) 3 2 0 

3205 2 2 0 

It is anticipated that the permanent section of the new baffle walls will be a minimum of 18” 

thick lightweight concrete. The permanent section of the inter-pass walls will match the 

thickness of the existing Y-walls. The new baffle walls are thicker than the existing inter-pass 

walls in AT 3205 because of the use of lightweight concrete to minimize the additional weight 

on the existing pile foundation system. 














varying process temperatures; thereby possibly changing mixer requirements. Based on the 

anticipated mixed liquor concentrations and the zone sizing, the required horsepower was 

estimated as shown in Table 11-6. 

11-3



DRAFT 

Pass 


Zone Volume (Cubic Feet) 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

All Passes 250,497 13,184 

Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Pre-anoxic 

All Passes N/A 5.2 






Pass 



Anoxic/ 

Switch 

Anoxic/ 

Switch 

Anoxic/ 

Switch 

Oxic 

Preanoxic 

Total 

Mixers 

All Passes N/A 1 10 





The existing air distribution and control systems will be demolished as shown on Drawing 13. 



BNR designs. The most significant difference will be the pipe diameters since more air must be 


the consequential reduction in the oxygen transfer efficiency. The anticipated air velocities 

within the pipes are still within the typical ranges identified in the Step Feed BNR design 

description. 

Another difference between the design levels will be in the positioning of the droplegs. With the 

installation of membrane bioreactor technology at the North River WPCP, the existing aeration 

11-4



DRAFT 

tanks will be completely converted into oxic zones. Therefore, each pass will still receive six 

droplegs, which will be evenly spaced along the pass length. A process flow schematic for the 

aeration system under the MBR design level can is shown in Drawing 15. 

Concrete pipe cradles will be necessary to support both the main air header and aeration tank 

headers under the influent channel. The addition of more aeration piping above the aeration 

tanks and the related support structures may restrict movement and access to other equipment on 

top of the aeration tank covers. Taking aeration tanks offline will be required to install all piping 

and to ensure that the new penetrations are tightly sealed. Sway braces will be installed into the 

aeration tank walls to provide support for the droplegs. The existing main air header, pass 

headers and droplegs will be demolished, as shown in Drawing 13. Pipe supports will be 

demolished also due to prolonged exposure to the weather. Penetrations into the aeration tank 

cover and Pass B wall will require filling and sealing. 

The motorized valves will need to be tied into the DO control system to regulate air distribution. 

The pass header flow meters will provide accurate measurements of the air distribution between 

the passes and aeration tanks. The system will have the capability to be controlled by DO level, 

airflow, or a combination of the two. These will be tied into the plant-wide SCADA system. 


With the increase in the aeration capacity under the MBR level of treatment, the diffuser grids 

will be redesigned to provide a distribution of air throughout the aeration tank oxic zones and 

switch zones. 











(scfm) 


Required (1) 



In order to ensure sufficient diffusers could be installed at the facility, the available floor area 

was evaluated and compared to the diffuser requirements. It appears that there is sufficient space 


proper design of the diffuser grid. 

11-5



DRAFT 







Level of 

Treatment 


Nitrogen BOD 

Oxidized (2) Oxidized (3) 

Aeration 

Oxygen 

Tank 

Required (4) 

Loading 


Air 

Required (5) 

Membrane Average 22,500 177,800 298,900 94,300 

Bioreactor Peak Daily 29,900 263,500 427,500 134,900 







(5) Air required = 0.04*O 2 required / Overall Efficiency; Overall Efficiency = 13% for MBR 

For each design level, the air requirements were determined at both the average and peak daily 

loading conditions, where influent BOD was completely oxidized and influent TKN was reduced 

to 2 mg/L in the final effluent. Since the aeration tanks at North River are deeper than most of 

the aeration tanks at other NYCDEP WPCPs (29.6 feet versus 15 feet, typically), the overall 

oxygen transfer efficiency is greater than typically observed. The Membrane Bioreactor 

technology has a lower overall oxygen transfer efficiency because it operates at greater mixed 

liquor concentrations than the Step Feed BNR technologies. Higher mixed liquor concentrations 

result in a lower alpha factor, which impacts oxygen transfer efficiency. 


using the existing blowers. Figure 11-1 shows this comparison. Two new process air blowers 

are required as part of the proposed Membrane Bioreactor upgrade designs. 

11-6



DRAFT 

160,000 

140,000 

120,000 

Peak Daily 

100,000 

scfm 

80,000 

6 Blowers (N) 

Peak Daily 

Average 

60,000 

40,000 

5 Blowers (N) 




Average 

20,000 


0 


Capacity 


Capacity 

(NR-35 Completed) 

Step Feed BNR 

Technology 

Membrane 

BioReactor 

Technology 

Figure 11-1: Existing Blower Capacity and Air Requirement Comparison 

The Roots-Dresser HT-series blower was selected for use in the MBR design, and is described in 

detail in Section 6.4. Table 11-10 shows the blower selection for each design level. 

Table 11-10: Blower Selection at the Membrane Bioreactor Level of Treatment 


Level of 


Treatment 

Quantity 

Quantity 

scfm scfm 

scfm 

Membrane 94,300 43,000 3 129,000 N+2 

Bioreactor 134,900 43,000 4 172,000 N+1 

Total 

Blowers 

for 

Design 

Level 

The existing blowers will be replaced with the new blowers in the existing blower and engine 

room within the main building with a minimum of 10 feet between each unit. The lube system 

will be integrated into the blower base. All alternatives will require demolition of virtually all 

the blower related equipment as shown on Drawing 16. 

The process air blower system for the Membrane Bioreactor design level is very similar to the 

Step Feed technology system, described in Section 6.4, except with an additional blower. 

5 

11-7



DRAFT 

The inlet air filtration system will be increased to five 43,000-scfm collectors to provide similar 

operational redundancy as the blowers. Due to the increased blower size, the inlet flanges on the 

new blowers are larger than the current inlet aeration piping can connect to and must be replaced. 

This includes valves, silencers and pitot tubes. The 66-inch diameter inlet air header will also 

require upgrades. The segments that include the wye connection to each blower must be 

increased. The segment that is directed to the current fifth blower can be kept although the 

connecting inlet piping will be increased in size. 

A 56-inch diameter header will run under the blower room and will be supplied by three of the 

blowers. The two remaining blowers will connect to a 50-inch diameter header that will be 

directed just outside of the main building and will run parallel to the 56-inch diameter header, 

below the inlet header. The two headers will connect via a motorized butterfly valve into a new 

82-inch air main header that will start where the current 42-inch air main header exits the main 

building and run along the same path to the aeration tanks. The startup bypass piping and valves 

will be replaced, but will still connect to the raw air plenum for atmospheric blowoff. Drawing 

18 shows the process schematic for the MBR alternative. 

The new blowers will fit within the existing infrastructure, although the new headers will require 

some demolition. There is space for the second blower header to run along the main building, 

but concrete pipe cradles will be necessary for support. The new air main header will also need 

larger cradles for support for its approach to the aeration tanks. The existing support for the inlet 

header should be sufficient, although under the Step Feed BNR design levels it could be reduced 

due to the partial demolition of the header. 

An increase in electrical demand is anticipated with the installation of at least four 2,500 hp 

blower engines, which is significantly higher than the existing blowers. Additional power will 

be required for the associated valves and equipment within the system. 

Each blower will come equipped with a new blower control panel that will be connected to the 

associated valves and lube oil system. A new blower system control panel will be installed that 

will oversee all the new blowers as well as the related appurtenances, including the motorized 

butterfly valve connecting the two blower headers. The blower will be controlled based on 

maintaining a pressure setpoint and air flow will be controlled by the DO/airflow control system 

installed on the header to each pass. 



will be demolished. 


Objectives for the RAS system in the MBR level of technology include: 

11-8



DRAFT 


• Internal Recycle: Recycle nitrified effluent to the pre-anoxic zones to facilitate denitrification 

Parameters 

• RAS concentration: 8,000 – 10,000 mg/L 

• RAS capacity: 4 times DDWF (680 MGD) 

• Internal Recycle concentration : 8,000 – 10,000 mg/L 

• Internal Recycle capacity: 2 times DDWF (340 MGD) 


RAS facilities and aeration tanks can not be used to meet the RAS and internal recycling flow 

requirements. New facilities must be constructed off site. The design of new RAS and internal 

recycling can be coordinated with the other new off-site facilities required for the MBR system 

(fine screens and pre-anoxic tanks). 


Flow will be directed from the MBR process tanks through three new 8’ x 10’ conduits 

constructed on the West End of the facility and travel South to a wet well located in the new 

facilities building. Each conduit will have a motorized sluice gate at its influent and effluent 

ends. At the wet well, the RAS will meet flow from the Pre-anoxic zone. All of the flow will be 

pumped by the intermittent pumping station to the reconstructed aeration tank influent 

distribution channel. 

Internal recycle flow will be collected from the reconstructed aeration tank effluent channel and 

travel through two new 8’ x 10’ conduits constructed on the West End of the facility and travel 

South to the head of the new pre-anoxic zone where it will meet screened aeration tank influent 

waste stream. Flow will continue through the pre-anoxic tanks and subsequently to the 

intermittent pumping station wet well. All combined flow will be pumped to the aeration tanks 

by the intermittent pumping station that is more fully described in the MBR section. 


The Membrane Bioreactor process will not require a significantly different sludge wasting rate 

compared to the Step Feed BNR processes. The RAS distribution box from which the current 

WAS is wasted will not be required, but the capability to waste from the aeration tank effluent 

will be maintained. The MBR process operates at a higher mixed liquor (8,000 mg/L), which is 

consistent with the concentration anticipated from the WAS in the step feed BNR alternatives. 

The capacity of the aerated effluent wasting system is greater than the WAS system and 

therefore can handle the entire secondary waste load. In addition the surface wasting system can 

supplement the aerated effluent wasting system if necessary. 

The existing WAS system will be demolished under this alternative. Proposed improvements 

include an upgrade of the WAS flow metering on the aerated effluent and the primary sludge 

wasting system. Metering of surface wasting is included in the froth control section, but will 

also be included. The existing ultrasonic meters will be removed and replaced by magnetic flow 

11-9



DRAFT 

meters that can transmit flow information to the central control system. These flow meters will 

be installed on all three influent lines entering the WAS Wet Well. 



Froth Hoods are not recommended for the Membrane Bioreactor level of technology. 


Froth Hoods are not recommended for the Membrane Bioreactor level of technology. 



technology is provided in Section 11.11.4. 





11.9.2 Carbon 


technology was provided in Section 7.9.2 for the Full Step BNR treatment option. Schematics 

for the MBR level of technology is shown on Drawing 36, and Drawing 39 shows the plan 

views of the methanol storage area. 


No Polymer addition is recommended for the Membrane Bioreactor level of technology. 







11-10



DRAFT 



The Membrane Bioreactor (MBR) process is used to achieve low levels of nitrogen, solids and 


but will replace the secondary clarifiers with a membrane filtration process. Because this is a 

filtration process that doesn’t depend on the capability of solids to settle, the membrane process 








The MBR process is a combination of activated sludge reactors and membrane filtration 

facilities. The process configuration consists of a series of four activated sludge process zones 

that cycle between aerobic and anoxic conditions to achieve nitrification and denitrification. The 

first and third zones are anoxic (un-aerated) and the second and fourth are aerobic (aerated). The 

fourth aerated zone is also considered the membrane reactor. Return pumps remove excess 

solids from the membrane reactor tanks and return them to the process tanks. Based on the site 

conditions and the process requirements to meet low levels of nitrogen, RAS is directed from the 

fourth to the second zone. In order to maximize the use of primary effluent as a carbon source 

for denitrification, recirculation is also provided from the second zone (nitrification reactor) to 

the first zone (pre-anoxic reactor). A process flow diagram is shown in Drawing 40. 

The MBR process will require new fine screening facilities, new pre-anoxic tanks, a new 

intermittent pumping station, modification of the existing aeration tanks, new post-anoxic 

process volume located in a portion of the existing secondary clarifiers, new MBR facilities and 

other supporting equipment. The facilities will be constructed in a new building and in the 

existing secondary clarifiers. An overall plant process flow schematic is shown in Drawing 41. 

In order to construct the new facilities and the flow distribution channels a new structure and 

supporting caisson foundation will be required. These are shown on Drawings 42, 43 and 44. 

Odor control will be required for the new facilities and the existing secondary clarifiers 

(addressed in a later section). Modification of the aeration tanks has been addressed in the 

aeration tanks section. This section will present the pre-anoxic tanks, the post-anoxic tanks, the 

membrane bioreactors, the intermittent pumping station and associated structural requirements. 

Surface wasting for froth control will also be described here. 

11.11.1Pre-Anoxic Tanks 

An evaluation of the process tank sizing was performed using the BioWin process model and 

other engineering calculations. The evaluation showed that additional process volume beyond 

the existing tank volume would be required to meet the low effluent nitrogen discharge goals for 

11-11



DRAFT 

the MBR process. In considering the existing facility conditions and the process requirements 

for screening and pumping, a new pre-anoxic facility located at the South end of the plant was 

considered most appropriate. 

The new pre-anoxic facility will be located adjacent to the fine screens. The fine-screened 

primary effluent and nitrified internal recycle flow will mix in the influent recycle channel prior 

to it entering into the pre-anoxic tanks influent channel. The influent recycle channel will be 

approximately 350 feet long, 40 feet wide, and 12 feet deep whereas the pre-anoxic tanks 

influent channel will be approximately 474 feet long, 10 feet wide, and 12 feet deep. Flow from 

the influent recycle channel passes through one 120” x 72” sluice gate into the pre-anoxic tanks 

influent channel. From there, it is distributed equally through 72” x 72” gates into the pre-anoxic 

tanks. The internal recycle and pre-anoxic tanks influent channels will be covered for odor 

control. 

A total of eight new pre-anoxic tanks with a total process volume of 8.7 MG will be provided 

(Drawings 45, 46 and 47). Each tank will be split into two passes with one 72” x 72” sluice gate 

serving each pass. This will allow each pass and tank to be isolated for maintenance. Each tank 

will be 216 feet long, 56 feet wide and 12 feet deep. A drain will be installed in each pass train 

to allow for maintenance. Flow will continue to the end of the tank where it will pass over weirs 

to the pre-anoxic tanks effluent channel and into the intermittent pumping station wet well. The 

entire facility will be constructed on a new platform. All facilities will be covered for odor 

control. 

11.11.2Post-Anoxic Tanks 

The post-anoxic tanks will be located in the existing final settling tanks. All final settling tank 

equipment will be removed (Drawing 48) and new baffle walls installed to create the postanoxic 

zone, post-anoxic effluent channel, membrane reactors, RAS channel and membrane 

equipment gallery. Baffle walls will be located at 90 feet from the head of the existing final 

settling tank passes to provide the necessary anoxic process volume. There will be 16 trains. 

Each train will be 90 feet long, 74 feet wide and 10.9 feet deep. Flow will enter the post-anoxic 

tanks through the existing influent channel gates. New mixers will be installed to keep the solids 

in suspension. Flow will pass through new isolation gates to the post-anoxic effluent channel 

prior to entering the membrane process tanks. 

11.11.3Membrane Bioreactor 

The MBR will be located in the existing final settling tanks. The existing final settling tanks will 

be divided into a post-anoxic zone, membrane bioreactor zone, equipment gallery to locate the 

permeate pumping and air scour blower systems, and some free space for other miscellaneous 

equipment. The plan view of the post-anoxic tanks and membrane tanks can be seen in Drawing 

49. The MBR zone will be divided into 16 process tanks to allow each tank to be isolated for 

chemical cleaning. Each process tank will have three membrane units for a total of 48 units. 

Each tank will be fed from the post-anoxic effluent channel by an individual 36” x 36” sluice 

gate. The tanks will also require new baffle walls located at 174 feet from the head of the pass. 

11-12



DRAFT 

Flow from the MBR tanks will continue to two RAS channels (one per side). A new WAS 

collection box will be installed in one of the empty locations not being used by the MBR process. 

The WAS collection box will collect WAS from the surface through a downward opening gate to 

facilitate surface wasting. A floating type telescoping valve will also be installed as described 

later. 

This conceptual design will be based on the Zenon MBR Reactor system, but other vendors 

should be considered during subsequent design phases. The MBR system consists of membrane 

units, permeate pumping system, and air scour system. There will be 16 process tanks with three 

membrane units per tank (48 units total). Each membrane unit is 68 feet long, 18.5 feet wide, 

and 12 feet deep. The membrane unit consists of cassettes, support frames and support beams. 

The Zenon process connects ZeeWeed membrane cassettes to the support frame. Permeate will 

be pulled from each ZeeWeed cassette into a common permeate header. Connected to the header 

is a back pulse header that provides intermittent cleaning of the membranes. Permeate will be 

pulled by the permeate pump system provided by the vendor and discharged to either the back 

pulse storage tank or the disinfection tanks. Below each membrane cassette are air scour 

diffusers that are supplied with air from an air header that extends along the top of the tank. The 

air supply originates at a new process scour air blower area in the existing final settling tanks. 

Drawings 50 and 51 show section views of the membrane tank. 

11.11.4Surface Wasting 

For the Membrane Bioreactor, the surface wasting pits will be located in the existing final 

settling tanks along the downstream (Northern) end of Return Activated Sludge channel. The 

wasting box will be constructed within an existing portion of the final settling tanks that is not 

required for process. Foam from the aeration tanks will flow downstream along the water 

surface to the MBR tanks. Foam accumulated in the MBR tanks will flow with the RAS 

downstream to the common RAS channel (one channel on each side). Flow will continue 

Northerly where it will meet a new baffle wall that extends from above the water surface to a 

point just below. This will trap the foam in that channel. Located in that area will be a 

“Megator” type floating telescoping weir connected by a neutral buoyancy hose to the Wasting 

Pit. In addition, the common wall between the RAS channel and the wasting pit will have four 

downward opening gates that will allow additional surface wasting. Flow will continue by 

gravity to the existing waste sludge wet well. This source of wasting will supplement wasting 

from the aeration tank effluent channel. Drawings 52 and 53 show section views of the surface 

wasting system. 

11.11.5Intermittent Pumping Station 

The two RAS collection channels will meet and flow to the west side of the plant. A new 

conduit will carry the flow to the new off-site wet-well located in a new intermittent pumping 

station. There it will meet effluent flow from pre-anoxic tanks before being pumped back to the 

aeration tanks. The pumping station will consist of a wet well and pump room containing twelve 

centrifugal-type pumps. Each pump has a flow capacity of 120 mgd at a head of 40 feet. During 

peak flow conditions (1,200 mgd), ten pumps will be in service while maintaining two on 

11-13



DRAFT 

standby. The pumps will provide suction from the wet well through individual 54” suction lines. 

The pumps will be divided into groups of three and each group will discharge into one 96” force 

mains (four force mains in total). These force mains will be linked downstream of the pumping 

station to allow flow to travel from any pump group into any force main in case of pump 

malfunction or maintenance. The force mains will carry the flow away from the off-site facility 

and discharge into the modified aeration tank influent channel. A schematic of the intermittent 

pumping station is shown in Drawing 54. 

11.11.6Miscellaneous 

In order to facilitate the required additions for the Membrane Bioreactor alternative, it will be 

necessary to construct a new structure in the Hudson River on the South end of the North River 

WPCP. A flow conduit structure will also be required to be built to provide a path for certain 

process flows to and from this structure. This conduit will run along the West side of the 

building, also in the Hudson River. This will be a substantial undertaking that will require a new 

structural support system. 



approximately 18’x32’. 

Since the building platform will be constructed in place of an existing dock, the construction will 

also include a new dock on the South end of the new building. The approximate dimensions of 

the building footprint, height, and width of flow conduit are shown in Table 11-11. 

Table 11-11: Approximate Membrane Bioreactor Structure Dimensions 




The Membrane Bioreactor will have significant electrical requirements to support the anoxic 

mixing system, the Membrane permeate pumping system, the scour air system the intermittent 

pumping station and other miscellaneous support facilities 

The Membrane Bioreactors, post anoxic tanks and the new facility must be developed with a new 

HVAC system including Odor Control. 

The Membrane Bioreactor will come supplied with a control system. The system will be linked 

to the plant wide SCADA control system. 


A description of the odor control system needed for the Membrane Bioreactor level of 

technology was provided in Section 6.12 for the Advanced Basic BNR treatment option. 

11-14



DRAFT 




Flow CBOD TSS 



TN 

(mg/L) 

Base Case 60 30 25 13.1 

Existing Conditions 32.8 7.8 11.9 13.1 




Full Step BNR 38.1 10 – 15 12 – 15 6 – 10 





Table 12-2 provides a summary of anticipated capital construction costs for each level of 

technology at the North River WPCP. The project executive summary provides details into the 

contingencies used, key cost assumptions, and overall approach to cost estimation. The detailed 

cost estimates for eight technologies at each of the four WPCPs in question can be found in their 

entirety after the four plant-specific conceptual design reports and drawing sets. 

Table 12-2: Capital Construction Costs for Levels of Treatment, North River WPCP 








Full Step BNR with Solids Filtration $1,334 

Full Step BNR with Microfiltration/Ultrafiltration $1,568 

Full Step BNR with Denitrification Filtration $1,501 


12-1



DRAFT 

APPENDIX A 

Evaluation of Plant 

Influent Flows and Loads 

I



DRAFT 

APPENDIX B 

Equipment Lists 

II



DRAFT 

Equipment Lists 

I. Primary Settling Tanks Equipment List 

II. 

Fine Screens Equipment List 

III. Aeration Tank Flow Distribution and Control 

IV. Aeration Tank Baffle Equipment List 

V. Aeration Tank Mixer Equipment List 

VI. Air Distribution System Demolition List 

VII. Air Distribution System Equipment List 

VIII. Diffuser Grid Demolition List 

IX. Diffuser Grid Equipment List 

X. Process Air System Demolition List 

XI. Process Air System Equipment List 

XII. Return Activated Sludge Equipment List 

XIII. Waste Activated Sludge Equipment List 

XIV. Froth Control Equipment List 

XV. Hypochlorite System Equipment List 

XVI. Surface Wasting Equipment List 

XVII. Polymer Feed System Equipment List 

XVIII. Alkalinity System Equipment List 

XIX. Methanol System Equipment List 

XX. MBR Structural Equipment List 

XXI. MBR Pre-Anoxic Tank Equipment List 

XXII. FST Retrofit for MBR System Equipment List 

XXIII. MBR Intermittent Pumping Station Equipment List 

XXIV. MBR System Equipment List 

XXV. Denitrification Filter Structural Equipment List 

XXVI. Denitrification Filter Equipment List 

XXVII. Denitrification Filter Pump Station Equipment List 

XXVIII. Odor Control System Equipment List 

XXIX. Effluent Filter Structural Equipment List 

XXX. Effluent Filter Equipment List 

XXXI. Effluent Filter Pump Station Equipment List 

XXXII. Microfiltration/Ultrafiltration Structural Equipment List 

XXXIII. Microfiltration/Ultrafiltration Equipment List 

XXXIV. Microfiltration/Ultrafiltration Membrane Tank Equipment List 

III



DRAFT 

APPENDIX C 


IV



DRAFT 



1. Primary Settling Tanks – Section – Effluent Weir and Scum Trough 

Fine Screening Facility 

2. Fine Screening Facility – Process Schematic 

3. Fine Screening Facility – Plan - Bottom Level 

4. Fine Screening Facility – Plan - Top Level 

5. Fine Screening Facility – Section 


6. Aeration Tanks – Plan – Advanced Basic Step Feed BNR 

7. Aeration Tanks – Plan – Demolition – Full Step Feed BNR 

8. Aeration Tanks – Plan – Full Step Feed BNR 

9. Aeration Tanks – Detail and Section – Flow Distribution Box – Full Step Feed BNR 

10. Aeration Tanks – Plan – MBR 

11. Aeration Tanks – Section and Elevation – Baffles 

12. Aeration Tanks – Section - Mixing 

Aeration System 

13. Aeration Tank Process Air Distribution - Schematic – Demolition 

14. Aeration Tank Process Air Distribution - Schematic – Advanced Basic & Full Step Feed 

BNR 

15. Aeration Tank Process Air Distribution - Schematic – Membrane Bioreactor 

16. Process Air Blowers - Schematic – Demolition 

17. Process Air Blowers - Schematic – Advanced Basic & Full Step Feed BNR 

18. Process Air Blowers - Schematic – Membrane Bioreactor 

Return Activated Sludge System 

19. RAS System – Schematic – Demolition 

20. RAS System – Schematic – Full Step Feed BNR 

Waste Activated Sludge System 

21. WAS System – Schematic – Demolition 

22. WAS System – Schematic – Advanced Basic & Full Step Feed BNR 

Froth Control System 

23. Froth Control System Piping – Schematic 

24. Froth Control Hood – Plan and Section – Advanced Basic & Full Step BNR 

25. Froth Control Hood – Elevation – Advanced Basic & Full Step BNR 

26. Hypochlorite System – Schematic - Storage and Distribution 

27. Chemical Systems – Plan – Hypochlorite Storage Area – Advanced Basic & Full Step 

Feed BNR 

28. Froth Control - Schematic - Surface Wasting – Advanced Basic & Full Step Feed BNR 

V



DRAFT 

29. Froth Control - Plan and Section - Surface Wasting – Advanced Basic & Full Step Feed 

BNR 

Chemical Facilities 

30. Polymer System – Schematic – Storage and Feed System 

31. Chemical Systems – Plan – Storage Area – Alkalinity and Polymer 

32. Chemical Systems – Part Plan – Polymer, Alkalinity, and RAS Chlorination Distribution 

– Advanced Basic & Full Step Feed BNR 

33. Alkalinity System – Schematic – Storage and Feed System 

34. Methanol System – Schematic – Storage and Feed System – Full Step Feed BNR 

35. Methanol System – Schematic – Storage and Feed System – Full Step Feed BNR with 


36. Methanol System – Schematic – Storage and Feed System – Membrane Bioreactor 

37. Chemical Systems – Plan – Storage Area – Methanol and Hypochlorite - Full Step Feed 

BNR 

38. Chemical Systems – Plan – Storage Area – Methanol and Hypochlorite – Full Step BNR 

with Denitrification Filters 

39. Chemical Systems – Plan – Storage Area – Methanol and Hypochlorite – Membrane 

Bioreactor 

Membrane Bioreactors 

40. Membrane Bioreactor – Process Flow Diagram 

41. Membrane Bioreactor – Process Flow Schematic 

42. Membrane Bioreactor – Plan – Flow Conduit Platform 

43. Membrane Bioreactor – Section – Flow Conduit Platform 

44. Membrane Bioreactor – Plan – Cassion Layout 

45. Membrane Bioreactor – Plan – Pre-anoxic Tanks 

46. Membrane Bioreactor – Section A – Pre-anoxic Tanks 

47. Membrane Bioreactor – Section B – Pre-anoxic Tanks 

48. Membrane Bioreactor – Plan – Demolition – Final Settling Tanks 

49. Membrane Bioreactor – Plan – Post-anoxic Tanks and Membrane Tank 

50. Membrane Bioreactor – Section A – Membrane Tank 

51. Membrane Bioreactor – Section B – Membrane Tank 

52. Froth Control – Section C – Surface Wasting – Membrane Bioreactor 

53. Froth Control – Section D – Surface Wasting – Membrane Bioreactor 

54. Membrane Bioreactor – Intermittent Pumping Station Flow Schematic 


55. Denitrification Filters – Process Flow Diagram 

56. Denitrification Filters – Process Flow Schematic 

57. Denitrification Filters – Plan – Denitrification Filter, Pump Station and Fine Screen 

58. Denitrification Filters – Plan - Facility and Flow Conduit 

59. Denitrification Filters – Section – Flow Conduit Platform 

60. Denitrification Filters – Plan - Facility and Flow Conduit Cassion Layout 

VI



DRAFT 

Effluent Filters 

61. Effluent Filters – Plan – Process Flow Schematic 

62. Effluent Filters – Plan – Effluent Filter and Pump Building 

63. Effluent Filters – Facility and Flow Conduit Layout 

64. Effluent Filters – Section – Flow Conduit Platform 

65. Effluent Filters – Facility and Flow Conduit Cassion Layoutnd Pump Building 

Microfiltration/ultrafiltration 

66. Microfiltration/Ultrafiltration – Process Flow Schematic 

67. Microfiltration/Ultrafiltration – Plan – Filter Tanks and Equipment Gallery 

68. Microfiltration/Ultrafiltration – Section A – Filter Tanks and Equipment Gallery 

69. Microfiltration/Ultrafiltration – Section B – Filter Tanks and Equipment Gallery 

70. Microfiltration/Ultrafiltration – Plan – Facility and Flow Conduit Platform 

71. Microfiltration/Ultrafiltration – Section – Flow Conduit Platform 

72. Microfiltration/Ultrafiltration – Plan – Facility and Flow Conduit Caisson Layout 

VII

EFFLUENT FILTER 

PLAN 

FACILITY AND FLOW CONDUIT PLATFORM 

G:\SavinAutocad\2101.01(NorthRiver)\FINAL REPORT (3-5-07)\EFFLUENT FILTER\EFFLUENT FILTER -PLAN-FACILITY AND FLOW CONDUIT PLAT..dwg, Layout1


PLAN - PROCESS FLOW SCHEMATICS 

G:\SavinAutocad\2101.01(NorthRiver)\FINAL REPORT (3-5-07)\EFFLUENT FILTER\EFFLUENT FILTER -PLAN-PROCESS FLOW SCHEMATICS.dwg, Layout1


SECTION 

FLOW CONDUIT PLATFORM 

G:\SavinAutocad\2101.01(NorthRiver)\FINAL REPORT (3-5-07)\EFFLUENT FILTER\EFFLUENT FILTER SECTION-FLOW CONDUIT PLATFORM .dwg, Layout2


PLAN 

EFFLUENT FILER, MUDWELL, BLOWER AND 

PUMP BUILDING 

G:\SavinAutocad\2101.01(NorthRiver)\FINAL REPORT (3-5-07)\EFFLUENT FILTER\EFFLUENT FILTER- PLAN-EFFL. FILTER, MUDWELL,BLOWER&PUMP BLDG..dwg, Layout1


PLAN 

FACILITY AND FLOW CONDUIT CASSION LAYOUT 

G:\SavinAutocad\2101.01(NorthRiver)\FINAL REPORT (3-5-07)\EFFLUENT FILTER\EFFLUENT FILTER-PLAN-FACILITY & FLOW CONDUIT-CASSION LAYOUT.dwg, Layout1

MICRO FILTER 

PLAN 

FACILITY AND FLOW CONDUIT PLATFORM

MICRO FILTER 

PLAN - PROCESS FLOW SCHEMATICS

MICRO FILTER PLAN 

FILTER TANKS AND EQUIPMENT GALLERY


FILTER TANKS AND EQUIPMENT GALLERY 

SECTION A

MICRO FILTER 

SECTION 

FLOW CONDUIT PLATFORM

MICRO FILTER 

PLAN 

FACILITY AND FLOW CONDUIT CASSION LAYOUT


FILTER TANKS AND EQUIPMENT GALLERY 

SECTION B

PRIMARY SETTLING TANKS SECTION 

EFFLUENT WEIR AND SCUM TROUGH

FINE SCREENING FACILITY 

PROCESS SCHEMATIC

NORTH 


BOTTOM LEVEL

NORTH 


TOP LEVEL


SECTION



AERATION TANK PLAN 

ADVANCED BASIC STEP FEED BNR



AERATION TANK 

DEMOLITION PLAN 

FULL STEP FEED BNR



AERATION TANK PLAN 

FULL STEP FEED BNR

SECTION 

DETAIL 

SECTION 

SECTION 

AERATION TANK FLOW DISTRIBUTION BOX 

FULL STEP FEED BNR 

DETAIL AND SECTIONS

AERATION TANKS - 

PLAN - MBR

SECTION 

ELEVATION

AERATON TANKS - 

SECTION - MIXING

AERATION TANK PROCESS AIR DISTRIBUTION 

SCHEMATIC 

DEMOLITION

AERATION TANK PROCESS AIR DISTRIBUTION SCHEMATIC 

ADVANCED BASIC STEP FEED BNR & FULL STEP FEED BNR

AERATION TANK PROCESS AIR 

DISTRIBUTION SCHEMATIC 

MEMBRANE BIO REACTOR

PROCESS AIR BLOWERS - SCHEMATIC - 

ADVANCED BASIC BNR AND FULL STEP FEED BNR

PROCESS AIR BLOWERS - SCHEMATIC - 

MEMBRANE BIO REACTOR

RAS SYSTEM 

SCHEMATIC 

DEMOLITION

RAS SYSTEM 

SCHEMATIC 

FULL STEP BNR

WAS SYSTEM 

SCHEMATIC 

DEMOLITION

WAS SYSTEM 

SCHEMATIC 

PROPOSED

DETAIL 

FROTH CONTROL SYSTEM PIPING 

SCHEMATIC

SECTION 

PLAN 

FROTH CONTROL HOOD - PLAN AND SECTION - 

ADVANCED BASIC BNR AND FULL STEP BNR

SECTION (DOWNSTREAM VIEW) 

SECTION (UPSTREAM VIEW) 

FROTH CONTROL HOOD - 

ELEVATIONS - ADVANCED BASIC 

BNR AND FULL STEP BNR

FROTH CONTROL 

SURFACE WASTING SYSTEM 

STEP FEED BNR

PLAN 

SECTION 

FROTH CONTROL 

SURFACE WASTING- STEP FEED BNR 

PUMP STATION - PLAN & SECTION

FROTH CONTROL 

SURFACE WASTING 

MEMBRANE BIO REACTOR 

SECTION C

FROTH CONTROL 

SURFACE WASTING 


SECTION D

CHEMICAL SYSTEMS - PLAN - STORAGE AREA 

METHANOL AND HYPOCHLORITE 

FULL STEP FEED BNR ALTERNATIVE

CHEMICAL SYSTEMS - PLAN - STORAGE AREA - 

METHANOL AND HYPOCHLORITE - FULL STEP 

BNR WITH DN ALTERNATIVE

CHEMICAL SYSTEMS - PLAN - STORAGE AREA - 

METHANOL AND HYPOCHLORITE 

MEMBRANE BIO REACTOR ALTERNATIVE

PLAN 

CHEMICAL SYSTEMS - PLAN - 

STORAGE AREA - ALKALINITY AND 

POLYMER - ALL ALTERNATIVES

METHANOL FEED SYSTEM - PART PLAN 

METHANOL DISTRIBUTION

METHANOL FEED SYSTEM - SCHEMATIC - 

FULL STEP FEED BNR ALTERNATIVE


FULL STEP BNR WITH DN FILTERS ALTERNATIVE


MEMBRANE BIO REACTOR ALTERNATIVE

ALKALINITY FEED SYSTEM - SCHEMATIC - 

STORAGE AND FEED SYSTEM

DETAIL 

SECTION 

CHEMICAL SYSTEMS - PART PLAN 

POLYMER, ALKALINITY AND 

RAS CHLORINATION DISTRIBUTION

FIG. 

POLYMER FEED SYSTEM - SCHEMATIC - 

STORAGE AND FEED SYSTEM

HYPOCHLORITE SYSTEM - SCHEMATIC - 

STORAGE AND DISTRIBUTION

ELUTRIATION EFFLUENT 

ELUTRIATION 

RETHICKENERS 

ELUTRIATION 

WATER 

THICKENER OVERFLOW 

WASTEWATER INFLUENT 

GRIT 

TO 

LANDFILL 

BAR 

SCREENS 

WET 

WELL 

MAIN 

SEWAGE 

PUMPS 

GRIT 

CLASSIFIERS 

CYCLONE 

DEGRITTERS 

PRIMARY 

SETTLING 

TANKS 

SCUM 

CONCENTRATOR 

ALKALINITY 

FEED 

OXIC 

TANKS 

SCUM TO 

LANDFILL 

DEGRITTED 

PRIMARY SLUDGE 

AERATION TANK INFLUENT 

(7Q) 

METHANOL 

FEED 

SECONDARY INFLUENT 

(GRAVITY FEED) (1Q) 

POST-ANOXIC 

TANK 

MBR 

TANK 

WAS 

PLANT 

WATER 

CHLORINE 

CONTACT 

TANKS 

BALANCE 

WATER 

TOTAL 

WASTED 

SLUDGE 

PLANT 

EFFLUENT 

GRAVITY 

THICKENERS 

PRIMARY 

DIGESTERS 

SECONDARY 

DIGESTERS 

SLUDGE 

STORAGE 

TANKS 

DIGESTED 

SLUDGE TO 

OFFSITE 

DEWATERING 

FACILITY 

PLANT 

DRAIN 

WASTE 

SLUDGE 

WET WELL 

NEW OFFSITE FACILITY 

FINE 

SCREENS 

(2 mm) 

PRE-ANOXIC 

TANK 

PUMPING 

WET WELL STATION 

INTERNAL RECYCLE 


RAS 


MEMBRANE BIO REACTORS 

PROCESS FLOW DIAGRAM 

SAVIN ENGINEERS, P.C.

MEMBRANE BIO REACTOR - PLAN 

FACILITY AND FLOW CONDUIT- 

CASSION LAYOUT

MEMBRANE BIO REACTOR - PLAN 



SECTION 



PLAN 

PROCESS FLOW SCHEMATICS


PLAN 

PRE-ANOXIC TANKS


PRE-ANOXIC TANKS 

SECTION A


PRE-ANOXIC TANKS 

SECTION B

FINAL SETTLING TANKS - 

PLAN - DEMO


PLAN 

POST ANOXIC TANKS AND MEMBRANE TANK


MEMBRANE TANK 

SECTION A


INTERMEDIATE PUMPING STATION 

PROCESS FLOW SCHEMATIC


MEMBRANE TANK 

SECTION B

ELUTRIATION EFFLUENT 

ELUTRIATION 

RETHICKENERS 

ELUTRIATION 

WATER 

THICKENER OVERFLOW 

WASTEWATER INFLUENT 

GRIT 

TO 

LANDFILL 

BAR 

SCREENS 

WET 

WELL 

MAIN 

SEWAGE 

PUMPS 

GRIT 

CLASSIFIERS 

CYCLONE 

DEGRITTERS 

PRIMARY 

SETTLING 

TANKS 

SCUM 

CONCENTRATOR 

AERATION 

TANKS 

RAS 

SCUM TO 

LANDFILL 

DEGRITTED 

PRIMARY SLUDGE 

FINAL SETTLING 

TANKS 

WAS 

FINAL TANK 

EFFLUENT 

DENITRIFIED 

EFFLUENT 

CHLORINE 

CONTACT 

TANKS 

TOTAL 

WASTED 

SLUDGE 

PLANT 

EFFLUENT 

GRAVITY 

THICKENERS 

PRIMARY 

DIGESTERS 

SECONDARY 

DIGESTERS 

SLUDGE 

STORAGE 

TANKS 

DIGESTED 

SLUDGE TO 

OFFSITE 

DEWATERING 

FACILITY 

PLANT 

DRAIN 

WASTE 

SLUDGE 

WET WELL 

NEW OFFSITE FACILITY 

PUMPING 

STATION 

FINE 

SCREENS 

(2 mm) DN FILTER 

FILTER 

BACKWASH 

RETURN 


PROCESS FLOW DIAGRAM 

SAVIN ENGINEERS, P.C.

DENITRIFICATION FILTERS-PLAN 

FACILITY AND FLOW CONDUIT 

CASSION LAYOUT

DENITRIFICATION FILTER 

PROCESS FLOW SCHEMATICS

DENITRIFICATION FILTER 

FACILITY AND FLOW CONDUIT-PLAN


FLOW CONDUIT PLATFORM 

SECTION A


DENITRIFICATION FILTER, PUMP 

STATION AND FINE SCREEN


PLAN 

FACILITY AND FLOW CONDUIT CASSION LAYOUT


PLAN - PROCESS FLOW SCHEMATICS


PLAN 

FACILITY AND FLOW CONDUIT PLATFORM


SECTION 



PLAN 

EFFLUENT FILER, MUDWELL, BLOWER AND 

PUMP BUILDING


MEMBRANE TANK 

SECTION A


Owls Head 



June 2007 

DRAFT


Owls Head Water Pollution Control Plant 

DRAFT 



1 OWLS HEAD WATER POLLUTION CONTROL PLANT 1-1 



1.3 SUMMARY OF PLANT OPERATIONS 1-6 

1.4 NORMAL AND WET WEATHER OPERATIONS 1-7 

1.5 LIMITATIONS AND BOTTLENECKS OF EXISTING FACILITIES 1-8 

1.6 POTENTIAL SITES FOR ADDITIONAL FACILITIES 1-8 

2 MASS BALANCES 2-1 

2.1 TSS BALANCE 2-1 

2.2 BOD BALANCE 2-3 

2.3 TKN BALANCE 2-4 

2.4 PROJECTED 2045 TSS BALANCE 2-5 

2.5 PROJECTED 2045 BOD BALANCE 2-7 

2.6 PROJECTED 2045 TKN BALANCE 2-8 






4.3.1 Baffles 4-1 

4.3.2 Mixers 4-1 

4.3.3 Aeration Requirements 4-1 

4.3.4 Blowers 4-1 



4.5 RETURN AND WASTE ACTIVATED SLUDGE SYSTEM 4-1 







4.7.2 Carbon 4-2 

4.7.3 Sodium Hypochlorite 4-2 

4.7.4 Polymer 4-2 





TOC-1



DRAFT 



4.11 INSTRUMENTATION AND CONTROL 4-6 

4.12 SITE PLAN 4-6 





5.3.1 Baffles 5-2 

5.3.2 Mixers 5-2 


5.3.4 Blowers 5-2 










5.7.2 Carbon 5-3 


5.7.4 Polymer 5-3 













6.3.1 Baffles 6-1 

6.3.2 Mixers 6-2 


6.3.4 Blowers 6-5 





TOC-2



DRAFT 






6.7.2 Carbon 6-9 


6.7.4 Polymer 6-10 













7.3.1 Baffles 7-1 

7.3.2 Mixers 7-1 


7.3.4 Blowers 7-2 







7.7.2 Carbon 7-5 


7.7.4 Polymer 7-6 












TOC-3



DRAFT 


8.3.1 Baffles 8-1 

8.3.2 Mixers 8-1 


8.3.4 Blowers 8-1 







8.7.2 Carbon 8-2 


8.7.4 Polymer 8-2 













9.3.1 Baffles 9-1 

9.3.2 Mixers 9-1 


9.3.4 Blowers 9-1 










9.7.2 Carbon 9-2 


9.7.4 Polymer 9-3 




TOC-4



DRAFT 










10.3.1 Baffles 10-1 

10.3.2 Mixers 10-1 


10.3.4 Blowers 10-1 







10.7.2 Carbon 10-2 


10.7.4 Polymer 10-3 








10.12 SITE PLAN 10-6 





11.3.1 Baffles 11-4 

11.3.2 Mixers 11-4 


11.3.4 Blowers 11-5 


11.5 RETURN AND WASTE ACTIVATED SLUDGE SYSTEM/INTERNAL RECYCLE 11-8 

11.5.1 Mixed Liquor Recycle 11-8 

11.5.2 Return Activated Sludge (RAS) 11-8 

11.5.3 Waste Activated Sludge (WAS) 11-9 


TOC-5



DRAFT 






11.7.2 Carbon 11-12 


11.7.4 Polymer 11-13 








11.12 SITE PLAN 11-15 

FIGURE 2-11: MBR AERATION TANK PART PLAN DETAILSUMMARY OF COST 

AND PERFORMANCE 11-18 

SUMMARY OF COST AND PERFORMANCE 12-19 

APPENDIX A 

I 

TOC-6



DRAFT 



Figure 1-1: NYCDEP WPCPs in the New York Harbor ............................................................. 1-1 

Figure 1-2: Schematic Flow Diagram of Existing Treatment Process ........................................ 1-3 

Figure 1-3: Existing Plant Site Plan............................................................................................. 1-4 

Figure 1-4: Owls Head WPCP Hydraulic Profile ........................................................................ 1-5 

Figure 2-1: TSS Balance.............................................................................................................. 2-2 

Figure 2-2: BOD Balance ............................................................................................................ 2-4 

Figure 2-3: TKN Balance............................................................................................................. 2-5 

Figure 2-4: TSS Balance for 2045 Projected Flow and Loading................................................. 2-7 

Figure 2-5: BOD Balance for 2045 Projected Flow and Loading ............................................... 2-8 

Figure 2-6: TKN Balance for 2045 Projected Flow and Loading ............................................... 2-9 

Figure 4-1: Tertiary Filter Section ............................................................................................... 4-4 

Figure 4-2: Site Plan with Location of Existing Conditions with Solids Filtration Upgrades .... 4-7 

Figure 5-1: Membrane Filter Modularity..................................................................................... 5-4 

Figure 5-2: Site Plan with Location of Existing Conditions with Microfiltration/Ultrafiltration 

Upgrade........................................................................................................................................ 5-8 

Figure 6-1: Owls Head Aeration Tank Conceptual Configuration.............................................. 6-1 

Figure 6-2: Typical Installation of Hyperboloid Mixers.............................................................. 6-2 

Figure 6-3: Existing Blower Process Flow Diagram ................................................................... 6-6 

Figure 6-4: Location of Froth Hoods for Advanced Basic BNR................................................. 6-8 

Figure 6-5: New Froth Control Process Flow Diagram for Advanced Basic BNR................... 6-10 

Figure 6-6: Site Plan with Location of Advanced Basic BNR Upgrades .................................. 6-12 

Figure 7-1: RAS/WAS Process Flow Diagram for Full Step BNR ............................................. 7-4 

Figure 7-2: Site Plan with Locations of Full Step BNR Upgrades .............................................. 7-8 

Figure 8-1: Site Plan with Locations of Full Step BNR with Solids Filtration Upgrades ........... 8-4 

Figure 9-1: Site Plan with Locations of Full Step BNR with Solids Filtration Upgrades ........... 9-4 

Figure 10-1: Denitrification Filter ............................................................................................. 10-5 

Figure 10-2: Site Plan with Locations of Full Step BNR with Denitrification Filtration Upgrades 

.................................................................................................................................................... 10-7 

Figure 11-1: Primary Effluent Flow through 2mm Screens ...................................................... 11-3 

Figure 11-2: Final Settling Tank Demolition Plan for MBR Option......................................... 11-7 

TOC-7



DRAFT 

Figure 11-3: Site Plan with Locations of MBR Upgrades....................................................... 11-16 

Figure 11-4: Schematic flow diagram of the MBR system ..................................................... 11-17 

Figure 11-5: MBR Aeration Tank Part Plan Detail ................................................................. 11-18 



Table 1-1: Summary of the Owls Head WPCP ........................................................................... 1-6 

Table 2-1: Values used for TSS Mass Balance............................................................................ 2-1 

Table 2-2: Values used for BOD mass balance ........................................................................... 2-3 

Table 2-3: Values used for TKN Mass Balance .......................................................................... 2-4 

Table 2-4: Projected Flows and Loads for 2045.......................................................................... 2-6 

Table 4-1: Tertiary Pump Station specifications ......................................................................... 4-3 

Table 4-2: Solids Filter Operating Parameters for DCWASA..................................................... 4-3 

Table 4-3: Tertiary Filter Area Sizing ......................................................................................... 4-4 

Table 4-4: Tertiary Filter Component Section............................................................................. 4-5 

Table 4-5: Tertiary Filter Backwash System Components .......................................................... 4-5 

Table 4-6: Tertiary Filter Air Scour Blower specifications ......................................................... 4-6 

Table 5-1: Fine Screen Specifications ......................................................................................... 5-1 

Table 5-2: Existing Conditions with Microfiltration/Ultrafiltration Filter Specifications........... 5-4 

Table 5-3: Existing Conditions with Microfiltration/Ultrafiltration Membrane Filter Sizing..... 5-5 

Table 5-4: Second Stage Reject Bleed Membrane Sizing ........................................................... 5-7 

Table 6-1: Location of Baffles for Advanced Basic BNR........................................................... 6-2 

Table 6-2: Values of α, β and θ.................................................................................................... 6-4 

Table 6-3: Advanced Basic BNR Air Requirements Calculated per Design Guidance .............. 6-4 

Table 6-4: Advanced Basic BNR Air Requirements derived from BioWin Modeling................ 6-5 

Table 6-5: Advanced Basic BNR Diffuser Information .............................................................. 6-5 

Table 6-6: Instrumentation and Control for Advanced Basic BNR........................................... 6-11 

Table 7-1: Full Step BNR Air Requirements derived from BioWin Modeling ........................... 7-2 

Table 7-2: Full Step BNR Diffuser Information.......................................................................... 7-2 

Table 7-3: Instrumentation and Control for Full Step BNR ........................................................ 7-7 

Table 10-1: Denitrification Filter Supplemental Carbon System specifications ....................... 10-3 

Table 10-2: Denitrification Filter Specifications ....................................................................... 10-4 

TOC-8



DRAFT 

Table 10-3: Denitrification Filter Backwash Specifications...................................................... 10-4 

Table 11-1: Existing Primary Clarifier Specifications............................................................... 11-1 

Table 11-2: Fine Screen Specifications ..................................................................................... 11-2 

Table 11-3: Aeration Tank Specifications for MBR Treatment ................................................ 11-3 

Table 11-4: Mixer Specifications for MBR Treatment.............................................................. 11-5 

Table 11-5: Blower Specifications for MBR Treatment............................................................ 11-6 

Table 11-6: Overview of MLSS recycling, RAS, and WAS systems for MBR Treatment ...... 11-8 

Table 11-7: Specifications for MLSS recycling system for MBR Treatment ........................... 11-8 

Table 11-8: Specifications for the RAS system for MBR Treatment........................................ 11-9 

Table 11-9: Specifications for WAS systems for MBR Treatment ......................................... 11-10 

Table 11-10: Froth Control Hoods Specifications for MBR Treatment .................................. 11-10 

Table 11-11: RAS Chlorination System Specifications for MBR Treatment.......................... 11-10 

Table 11-12: Sodium Hydroxide Supply Specifications for MBR Treatment ........................ 11-11 

Table 11-13: Sodium Hydroxide Storage and Piping Requirements for MBR Treatment...... 11-11 

Table 11-14: Supplemental Carbon System Specifications for MBR Treatment.................... 11-12 

Table 11-15: Supplemental Carbon Storage and Piping Requirements for MBR Treatment.. 11-12 

Table 11-16: Membrane Module Specifications for MBR Treatment..................................... 11-14 

Table 11-17: Membrane Tank Specifications for MBR Treatment......................................... 11-14 

Table 11-18: Instrumentation and Control for MBR Treatment.............................................. 11-15 

Table 12-1: Treatment Goals for Nine Treatment Considerations .......................................... 12-19 

Table 12-2: Capital Construction Costs for Levels of Treatment............................................ 12-20 

TOC-9



DRAFT 

1 OWLS HEAD WATER POLLUTION CONTROL PLANT 


The Owls Head WPCP is one of 14 WPCPs operated by the NYCDEP, and located in the 

vicinity of Bay Ridge section of Brooklyn, New York (see Figure 1-1). In this chapter, a 

historical development of the Owls Head WPCP and a detailed description of the existing (as of 

year 2007) facility are presented. 


Figure 1-1: NYCDEP WPCPs in the New York Harbor 

The existing Owls Head WPCP consists of screening, primary settling, cyclone degritting of 

primary sludge, step-feed activated sludge, final settling, and sodium hypochlorite disinfection. 

The screening facilities, main wastewater pump station, and primary settling tanks are designed 

for an average dry weather flow of 120 mgd and a peak hydraulic flow of 240 mgd. The 

activated sludge process is designed for a peak flow of 180 mgd. Primary effluent in excess of 

180 mgd is by-passed to the head of the chlorine contact tanks where it is mixed with secondary 

effluent. Primary sludge is degritted by cyclone degritters and co-thickened with waste activated 

sludge in gravity thickeners. Thickened mixture of primary and waste activated sludge is then 

anaerobically digested. Digested sludge is transported by sludge vessels to be further processed 

at the Wards Island WPCP or to the 26 th Ward WPCP. Supernatant from the gravity thickeners 

is sent back to the pump house and combined with incoming raw wastewater. A summary of the 

existing facility is reported in Table 1-1, and a simplified flow diagram is shown in Figure 1-2. 

The site plan is shown in Figure 1-3. 

1-1



DRAFT 

The hydraulic profile for the plant is shown in Figure 1-4. All elevations indicated are based on 

Brooklyn Highway Datum which is 2.56 feet above mean sea level as established by the U.S. 

Coast and Geodetic Survey at Sandy Hook, New Jersey. 

About 80 percent of the wastewater reaching the Owls Head WPCP is from combined sewers. 

The rest (20 percent) is from sanitary sewers. All are primarily domestic in nature. Raw sewage 

reaching the plant flows through the four screening channels into the main pump station wet 

well. Each screening channel is equipped with two mechanically cleaned screens. The first is a 

coarse screen with a clear bar spacing of 1.25 inches. The second is a fine screen with a clear bar 

spacing of 0.75 inches. 

Two identical mechanically cleaned bar screens are installed in series in each of the screening 

channels. A belt conveyor carries the screenings from the screens to a 6 cu-yd container located 

in the building at ground level. Portable chutes are provided to divert the screenings to smaller 

containers in the event the conveyor is out of service. Screenings are trucked to a landfill for 

disposal. 

Degritted primary sludge flows by gravity to the sludge thickeners where it is thickened by 

gravity settling. Overflow from the thickeners flows back to the wet well by gravity. Thickened 

sludge is pumped to the four primary digesters where anaerobic digestion renders the sludge 

relatively harmless. The by-product of anaerobic digestion, methane gas, is stored in a gas 

holder and used to power the dual fuel generators which supply a portion of the plants electrical 

energy requirements. Digested sludge from the primary digesters is piped to the two gas 

extractors for further digestion and gas extraction. Digested sludge from the gas extractors is 

pumped to the two sludge storage tanks for eventual disposal, via sludge boats, at sea. 

After primary settling, the sewage enters four aeration tanks for step-feed activated sludge 

process. Four step-feed activated sludge tanks, located symmetrically, receive primary effluent 

at a default flow split of 0, 33, 33, and 33 percent for Pass A, B, C, and D, respectively. Four 

centrifugal compressors provide process air through diffusers, located systemically throughout 

the floor of the aeration tanks, to provide oxygen to speed up growth of microorganisms. 

Return sludge from the final settling tanks is introduced at the influent of each aeration tank. 

Foam control of aeration tank is by means of water sprays from spray heads located at both sides 

of the aeration tanks. Activated sludge (mixed liquor) flows by gravity to the final settling tanks 

where scum is removed and disposed of by the same method as the primary tank scum. The 

sludge can be diverted to the thickeners in the form of waste sludge. 

Final tank effluent flows by gravity to the chlorination tanks. Hypochlorite is mixed with the 

final effluent for the purpose of disinfection. Treated effluent is discharged into Upper New 

York Bay through a multiport diffuser outfall pipe. 

1-2



DRAFT 

Figure 1-2: Schematic Flow Diagram of Existing Treatment Process 

1-3



DRAFT 

Figure 1-3: Existing Plant Site Plan 

1-4



DRAFT 

Figure 1-4: Owls Head WPCP Hydraulic Profile 

1-5



DRAFT 

1.3 Summary of Plant Operations 

Table 1-1 shows a summary of the existing facilities and equipment at the Owls Head WPCP. 

Table 1-1: Summary of the Owls Head WPCP 


General 

Tributary area acres 13,664 

Interceptors 

Discharge location 

Flows 

Average design dry weather 

flow 

12’6”×8’0” (north), 9’0”×9’0” (south) 

Upper New York Bay 

mgd 120 

Maximum primary treatment mgd 240 

Maximum secondary treatment mgd 180 

Screening 

Type - Mechanical bar screens 

Number - 

8 [2 per channel (coarse and fine), 4 

channels] 

Screen size inch coarse: 1 1/4, fine: 3/4 

Sewage Pumps 

Number - 5 



Type 

Rectangular with chain and flight 

mechanism 

Number of tanks - 4 

Dimensions ft x ft x ft 63 x 242.7 x 13 

Surface area ft 2 15,290 

Total overflow rate – at 120 

mgd (at 240 mgd) 


gal/ft 2 /day 1,962 (3,924) 

Type - four-pass, step-feed 

Number of tanks - 4 

Dimensions ft × ft ×ft 100 × 392.75 × 17.3 

Total volume ft 3 (Mgal) 2,720,000 (20.3) 

1-6



DRAFT 


HRT at 180 mgd hrs 2.7 

Process Blowers 

Number - 4 

Capacity (each) scfm 27,000 



Type 

Rectangular with chain and flight 

mechanism 

Number of tanks 16 

Dimensions ft × ft × ft 170.5L × 55W × 12.25D 

Surface area (each) ft 2 9,377 

Total overflow rate – at 120 

mgd (at 180 mgd) 

RAS Pumps 

Type 

gal/ft 2 /day 800 (1200) 

centrifugal, non-clog, vertically mounted, 

variable speed 

Number 4 

Capacity (each) gpm 20833 at 444 RPM at 25 ft head 


Type 

Circular 

Number 4 

Diameter (inside) ft 80 

Side wall depth ft 10 

Total surface area ft 2 20,107 

Anaerobic Digesters 

Number - 6 


Side water depth ft 32 

Total sludge volume ft 3 965,400 

1.4 Normal and Wet Weather Operations 

During dry weather, the plant will provide secondary treatment and disinfection for an average 

dry weather flow of 120 mgd and a peak hydraulic flow of 180 mgd (1.5 peaking factor). 

1-7



DRAFT 

During wet weather the plant will treat up to 240 mgd (2.0 peaking factor) through primary 

treatment. The primary effluent flow in excess of the hydraulic capacity of the secondary 

treatment facilities (180 mgd) bypasses the secondary facilities is combined with the secondary 

effluent and disinfected. 

1.5 Limitations and Bottlenecks of Existing Facilities 

In terms of wastewater treatment operations, currently no limitations or bottlenecks are 

recognized to the extent of existing treatment goals at the Owls Head WPCP. Rather tight 

spacing of the plant and limited vacant space may pose potential limitations when plant 

modifications are considered. 

1.6 Potential Sites for Additional Facilities 

The Owls Head WPCP has tight spacing and additional facilities with large footprints will 

require expanding the site out into the river. The most suitable location for expansion into the 

river is west side of the plant, adjacent to the chorine contact tank, aeration basins, and final 

settling tanks. 

Facilities with small footprint, e.g., caustic and carbon storage facilities, may be located within 

the existing vacant space. The size of these facilities must be determined first to evaluate the 

feasibility of locating additional facilities with small sizes in the vacant spaces of existing plant 

boundary. 

1-8



DRAFT 

2 MASS BALANCES 

A mass balance for the existing operating condition was evaluated for TSS, BOD 5 , and TKN, 

using the plant operation data from fiscal years 2003 through 2005. A statistical outlier 

determination analysis was made for the data sets provided by the NYC DEP. Using these three 

years of data, the average and standard deviation values were first determined. Data points that 

ranged within two standards deviations of the average were considered acceptable; all other data 

points were considered outliers and were rejected. The average values for the remaining 

accepted data were used to evaluate the mass balance. The Owls Head WPCP ships digested 

sludge to other WPCP for dewatering, and thus the flow after the sludge digester is not included 

in the mass balance. 

2.1 TSS Balance 

The values obtained from the operations datasheets are shown in Table 2-1. The calculations 

and assumptions applied to develop the mass balance are presented below. The TSS balance for 

the existing operating condition is illustrated on Figure 2-1. 

Unit 

Raw 

sewage 

Table 2-1: Values used for TSS Mass Balance 

(obtained from the operations datasheet) 

FST 

Prim. 

eff. 

Aer. 

eff. 

Sec. 

eff. 

2-1 

RAS 

UF 

WAS GTO PS Digester 

Flow mgd 98.3 97.0 - - 25.8 - - - - 0.498 

TSS mg/L 173 82.4 781 16.7 3392 3392 3392 134 - - 

Loading lb/d - - - - - - - - 80.2 - 

Raw sewage: 

TSS (mg/L) and flow (mgd) were obtained from the operation data. Loading (lb/d) was 

calculated from the TSS and flow. 

Primary effluent (PE): 



Aerator effluent (AE): 

TSS (mg/L) was obtained from the operation data. Flow was calculated from the balance of PE 

and RAS. Loading (lb/d) was calculated from the TSS and flow. 

Secondary effluent (SE): 

TSS (mg/L) was obtained from the operation data. Flow was calculated from the incoming flow 

and outgoing flow to the digester. Loading (lb/d) was calculated from the TSS and flow. 

Return activated sludge (RAS): 


calculated from the TSS and flow.



DRAFT 

Final settling tank (FST) underflow: 

TSS (mg/L) was obtained from the operation data. Loading was calculated as a balance from AE 

and SE. Flow was calculated using the TSS and calculated loading. 

Waste activated sludge (WAS): 

TSS (mg/L) was obtained from the operation data. Flow and loading were calculated as a 

balance from final settling tank underflow and RAS. 

Gravity thickener overflow (GTO): 

TSS (mg/L) was obtained from the operation data. Flow was estimated using a typical overflow 

rate of 250 gal/ft 2 /d and the total surface area of the gravity thickener, 20,107 ft 2 (= 5.0 mgd). 

Loading was calculated using the TSS and estimated flow. 

Primary sludge (PS): 

Loading was obtained from the operation data. Flow was calculated from the WAS flow and the 

flow to the thickener. TSS was calculated using the loading and the calculated flow. 

Flow to the thickener: 

Flow was calculated from the balance of GTO and the flow to the digester. Loading was 

calculated from the balance of PS and WAS. TSS was calculated using the calculated flow and 

loading. 

Flow to the digester: 

Flow was obtained from the operation data. Loading was calculated from the balance of GTO 

and the flow to the thickener. TSS was calculated using the flow and the calculated loading. 

Figure 2-1: TSS Balance 

2-2



DRAFT 

2.2 BOD Balance 

The values obtained from the operations datasheet are shown in Table 2-2. The focus of the 

BOD balance is to determine the BOD mass removed in the activated sludge. BOD balance in 

the RAS flow, including flow through the activated sludge, was assumed to be constant. 

Therefore, the BOD in returned/waste activated sludge was not measured or estimated. The 

calculations and assumptions applied to develop the mass balance are presented below. The 

BOD balance for the existing operating condition is illustrated on Figure 2-2. 

Table 2-2: Values used for BOD mass balance 

(BOD 5 obtained from the operations datasheet. Flow data include estimated flow rate from Figure 4-1) 

Unit 

Raw 

sewage 

Prim. 

eff. 

Aer. 

eff. 

Sec. 

eff. 

RAS 

FST 

UF 

WAS GTO PS Digester 

Flow mgd 98.3 97.0 123 97.8 25.8 27.8 2.0 5.0 3.5 0.498 

BOD 5 mg/L 171 137 - 12.1 - - - 43.6 - - 

Raw sewage: 

BOD (mg/L) and flow (mgd) were obtained from the operation data. Loading (lb/d) was 

obtained from the operation data, and also calculated from the concentration and flow. 


BOD (mg/L) and flow (mgd) were obtained from the operation data. Loading (lb/d) was 

calculated from the concentration and flow. 


BOD (mg/L) was obtained from the operation data. The same flow estimate in the TSS balance 

was used. BOD loading from GTO was estimated using the concentration and the estimated 

flow. 


Flow was estimated by the TSS balance. Assuming no biological activity, the BOD loading 

removed at primary settling was estimated as the reduction of BOD mass from raw sewage and 

GTO to the primary effluent. 


BOD (mg/L) was obtained from the operation data. Flow was calculated from the incoming flow 

and outgoing flow to the digester. Loading (lb/d) was obtained from the operation data, and also 


2-3



DRAFT 

2.3 TKN Balance 

Figure 2-2: BOD Balance 

The values obtained from the operations datasheet are shown in Table 2-3. The calculations and 

assumptions applied to develop the mass balance are presented below. The Owls Head WPCP is 

currently operating for BOD removal, and thus no nitrification and denitrification is assumed in 

the treatment process. The reduction of TKN is assumed to be due to assimilation to biomass. 

The TKN balance for the existing operating condition is illustrated on Figure 2-3. 

Unit 

Raw 

sewage 

Table 2-3: Values used for TKN Mass Balance 

(obtained from the operations datasheet) 

Prim. 

eff. 

Aer. 

eff. 

Sec. 

eff. 

RAS 

FST 

UF WAS GTO PS Digester 

Flow mgd 98.3 97.0 123 97.8 25.8 27.8 2.0 5.0 3.5 0.498 

TKN 

mg- 

N/L 

29.5 26.6 19.2 - 1819 

Raw sewage: 

TKN (mg/L) and flow (mgd) were obtained from the operation data. Loading (lb/d) was 



TKN (mg/L) and flow (mgd) were obtained from the operation data. Loading (lb/d) was 



TKN (mg/L) were obtained from the operation data. Flow was calculated from the incoming 

flow and outgoing flow to the digester. Loading (lb/d) was calculated from the TSS and flow. 

2-4



DRAFT 

The difference between TKN mass in PE and SE represents the mass of nitrogen removed during 

activated sludge process. 


Assume 2.5 percent of TSS (mg/L) is nitrogen [typical value from Metcalf & Eddy (2003)], i.e., 

68.7 mg/L. Flow (mgd) was obtained from solids balance. Loading (lb/d) was calculated from 

the TSS and flow. 

Waste activated sludge (WAS): 

Assuming TSS in secondary effluent is all biomass, VSS/TSS fraction of 0.85 (typical value), 

VSS/COD ratio of 1.42, and COD/N ratio of 0.07, the TKN in SE from biomass was estimated at 

16.7×0.85×1.42×0.07 = 1.4 mg-N/L. Therefore soluble TKN is 17.8 mg-N/L. Assume the 

soluble TKN in WAS is the same as SE, and the same nitrogen fraction in biomass, the nitrogen 

in WAS was estimated as: 

TKN WAS ~ 3392×0.85×1.42×0.07 +17.8 = 304 mg-N/L. 

Loading was calculated using the above estimation and the flow, derived in the solids balance. 


Flow was assumed to be 5.0 mgd based on the thickener surface area and typical overflow rate, 

as described in the solids balance. From the loading at the raw sewage, PE, and PS, TKN from 

GTO was estimated negligible (Raw sewage TKN < TKN PE + TKN PS , and the difference is 

small). The same estimation (negligible TKN in GTO) was made from the balance between 

primary sludge, WAS, and the nitrogen to the digester. 

Figure 2-3: TKN Balance 

2.4 Projected 2045 TSS Balance 

Mass balance for the projected 2045 conditions was estimated using the mass balance from 

existing conditions (Sections 2.1 through 2.3) and the BEPA 2045 projections for influent flow 

2-5



DRAFT 

and loading provided in Table 2-4. The mass balance for TSS is shown in Figure 2-4; the basis 

for calculations and assumptions are described below. 


Flow rate, 

CBOD TSS TN 

MGD 


104.6 

Loading, lb/d 

134,400 150,000 27,100 

Raw sewage: 

Values in Table 2-4 are used. 


Percent solids removal in terms of loading was assumed to be the same as the existing condition 

(=55%) to obtain estimated loading. Solids concentration was assumed to be the same as the 

existing condition (=2747 mg/L). Flow was estimated from the loading and concentration. 

Return activated sludge (RAS): 

Concentration, flow and loading were assumed to be the same as the existing condition. The 

same concentration was used for the FST underflow and WAS. 

Flows to and from the gravity thickener: 

Percent removal of the solids was assumed to be the same as the existing condition (95%). 


From the existing sludge flow to the digester (0.498 mgd), the flow to the digester in 2045 was 

assumed to be 0.5 mgd. 

Solids loading balance: 

Using the above assumptions, the loadings from GTO, PS, and WAS were calculated to balance 

each other. 

2-6



DRAFT 

Figure 2-4: TSS Balance for 2045 Projected Flow and Loading 

2.5 Projected 2045 BOD Balance 

The flows calculated for the TSS balance were used to calculate the BOD balance. BOD balance 

in the RAS flow, including flow through the activated sludge, was assumed to be constant. 

Therefore, the BOD in returned/waste activated sludge was not measured or estimated. The 

mass balance for BOD is shown in Figure 2-5, and the basis for calculations and assumptions 

are described below. 

Raw sewage: 



Percent BOD removal in terms of loading was assumed to be the same as the existing condition 

(=22.7%) to obtain estimated loading. 


The BOD concentration in the GTO was assumed to be the same as the existing condition (43.6 

mg/L). 


Effluent concentration of the existing condition was used. 

2-7



DRAFT 

Figure 2-5: BOD Balance for 2045 Projected Flow and Loading 

2.6 Projected 2045 TKN Balance 

The flows calculated for the TSS balance were used to calculate the TKN balance. No 

nitrification and denitrification is assumed in the treatment process. The reduction of TKN is 

assumed to be due to assimilation to biomass. The mass balance is shown in Figure 2-6, and the 

basis for calculations and assumptions are described below. 

Raw sewage: 



Percent TKN removal in terms of loading was assumed to be the same as the existing condition 

(=11.2%) to obtain estimated loading. 


The TKN contribution from the GTO was assumed to be negligible, as estimated in the existing 

condition. 


Effluent concentration of the existing condition was used. 


The same concentration as the existing condition was assumed. 

2-8



DRAFT 

Figure 2-6: TKN Balance for 2045 Projected Flow and Loading 

2-9



DRAFT 




technology. 




• Screening 


Baffles 

Mixers 

Aeration Requirements 

Blowers 

Diffusers 


• Return and Waste Activated Sludge System 






Alkalinity 

Carbon 

Sodium Hypochlorite 

Polymer 







• Instrumentation and Control 

3-1



DRAFT 




Solids Filtration level of technology. 


No fine screens are needed for the Existing Conditions with Solids Filtration level of technology. 


4.3.1 Baffles 


treatment. 

4.3.2 Mixers 

No mixers will be installed for the Existing Conditions with Solids Filtration level of treatment. 

4.3.3 Aeration Requirements 

There are no changes in the aeration requirements for the Existing Conditions with Solids 

Filtration level of treatment. 

4.3.4 Blowers 

There are no modifications for the blower system necessary for the Existing Conditions with 






No modifications to the Final Settling Tanks are needed for the Existing Conditions with Solids 


4.5 Return and Waste Activated Sludge System 

No modifications to the Return and Waste Activated Sludge Systems are needed for the Existing 

Conditions with Solids Filtration level of technology. 

4-1



DRAFT 



Froth Control Hoods are not recommended for the Existing Conditions with Solids Filtration 



No RAS chlorination measures are recommended for the Existing Conditions with Solids 



Surface wasting is not recommended for the Existing Conditions with Solids Filtration level of 

technology. 





4.7.2 Carbon 


technology. 

4.7.3 Sodium Hypochlorite 

Sodium Hypochlorite addition is not recommended for the Existing Conditions with Solids 


4.7.4 Polymer 

Polymer addition is not recommended for the Existing Conditions with Solids Filtration level of 

technology. 


Filtration of the process stream will induce a head loss that the plant's hydraulic profile cannot 

accommodate, and will therefore require installation of tertiary pumping. 

Neither of the two locations of apparent hydraulic surplus can safely be credited towards the 

filters. Upstream, the present 1.59 foot drop from the aeration tank effluent channel to the final 

settling tank influent channel may already be claimed to offset losses due to baffles and 

substantially increased recycle flows of Full Step BNR. Downstream, the chlorine contact tank's 

4-2



DRAFT 

effluent launder weir is set just 4.18 feet above the design tide, so cannot be lowered. (See 

Figure 1-4) This means that a dedicated pump station must balance the head loss of solids 

filtration. Table 4-1 details the pump station specifications. Archimedes screw pumps are very 

efficient for high-flow, low-head applications. 

Table 4-1: Tertiary Pump Station specifications 

Item 

Specification 

Pump type 

Number of pumps 

Pump screw diameter 

Archimedes screw pump 

8 (N+1+1) 

96-inch 

Angle of inclination 30° 

Design capacity 

Lift (surface-to-surface) 

Motor size 

Cover 



30 mgd/pump 

10.0 feet 

100 HP 

Fiberglass grating 

A downflow dual-media sand/anthracite filter system will meet Owls Head's TSS reduction 

goals. Such filters are a commonplace, conventional means of achieving tertiary TSS reduction. 

Owls Head's conceptual design can be largely scaled-down from the long-serving tertiary filter 

installation at DC Water and Sewer Authority's (DCWASA) Blue Plains Advanced Wastewater 

Treatment Plant (AWTP) and shown in Table 4-2. 

Important design criteria for the proposed Owls Head's WPCP filter fall within operating 

parameters for the DCWASA Blue Plains AWTP filter. 

Table 4-2: Solids Filter Operating Parameters for DCWASA 

Operating Parameter 

Filter run duration Avg. 24 Min. 6 hrs 

Unit 

Backwash rate High 25 Low 10 gpm/ft 2 

Filter loading rate Avg. 3.4 Peak 7.4 gpm/ft 2 

The Owls Head's filter design accommodates DCWASA's minimum filter run duration 

(productive operation between backwashing) of 6 hours. The design targets a filter loading rate 

of 5 gpm/ft 2 in compliance with "Recommended Standards for Wastewater Facilities" by the 

Great Lakes - Upper Mississippi River Board of State and Provincial Public Health and 

Environmental Managers is available (commonly referred to as The Ten-State Standards) 

§112.31. Table 4-3 sizes the required filter area. Figure 4-1 depicts one possible configuration 

of the layout tabulated above. 

4-3



DRAFT 

Table 4-3: Tertiary Filter Area Sizing 

Parameter Value Unit Source 

Peak flow 180 125,000 mgd | gpm [Section 2.2] 

Filter run duration 6 hrs Blue Plains 

Backwash rate 25 gpm/ft 2 Blue Plains 

Backwash duration 15 min Blue Plains 

Backwash flow 47 32,895 mgd | gpm calc. 

Peak flow + Backwash flow 227 157,895 mgd | gpm calc. 

Filter loading rate 5.0 gpm/ft 2 Ten-States 

Required filter area in service 31,579 ft 2 calc. 

Filter dimensions 52 20 L | W, ft Blue Plains 

Filter pair dimensions 52 51 L | W, ft Blue Plains 

Area per filter pair 2,080 ft 2 calc. 

No. of filter pairs in service 15.2 15 calc | whole calc. 

No. of filter pairs 

backwashing 

0.6 1 calc | whole calc. 

Total filter pairs 16 ea calc. 

Filter process footprint 95 816 L | W, ft Blue Plains | calc. 

Figure 4-1 shows the tertiary filter section at the Owls Head WPCP. 

Filter 

Influent 

Channel 

Figure 4-1: Tertiary Filter Section 

Filter 

Gallery 

Spent Washwater 

Conduit 

Washwater 

Filtered Water 

Conduit 

Table 4-4 sizes the section above in Figure 4-1. 

4-4



DRAFT 

Table 4-4: Tertiary Filter Component Section 

Item 

Specification 

Filter Depth 20' 

Media 1, Upper - Anthrecite; Depth 24" 

Media 2, Lower - Sand; Depth 12" 

Influent channel dimensions 

10'W x 20'H 

Central gullet width 10' 

Washwater conduit 

Spent washwater conduit 

Filtered water conduit 

Pipe gallery dimensions 

Underdrain system 

20'W x 7.0'H 

20'W x 7.0'H 

25'W x 7.0'H 

20'W x 20'H 

Porous tile 

The Owls Head's filter design accommodates DCWASA's Blue Plains AWTP high backwash 

rate of 25 gpm/ft 2 (from Table 4-2) Because there are only 16 filter pairs, it is possible to 

backwash them one at a time even at the shortest filter run duration. Table 4-5 lists the backwash 

system components. Table 4-6 specifies the air scour blowers. 

Table 4-5: Tertiary Filter Backwash System Components 

Item 

Specification 

Backwash rate 25 gpm/ft 2 

Area per filter pair 2,080 ft 2 

Backwash flow 

No. of Backwash pumps 

Pump capacity 

Pump type 

Pump motor HP 

No. of Backwash jockey pump 

Jockey pump capacity 

Jockey pump type 

Jockey pump motor HP 

52,000 gpm 

6 (N+1+1) 

13,000 gpm 

Vertical turbine 

100 HP 

3 (N+1+1) 

3,000 gpm 

Vertical turbine 

25 HP 

Washwater troughs per filter 6 

4-5



DRAFT 

Table 4-6: Tertiary Filter Air Scour Blower specifications 

Item 

Specification 

Scour air pressure 

10.0 psi 

Scour air rate 3 scfm/ft 2 

Area per filter pair 2,080 ft 2 

Scour air requirement 

No. of Blowers 

Blower capacity 

Blower HP 

6,240 scfm 

5 (N+1+1) 

2,100 scfm 

200 HP 



technology. 



technology. 



technology. 

4.11 Instrumentation and Control 

No Instrumentation and Control measures are needed for the Existing Conditions with Solids 


4.12 Site Plan 

The site plan with locations of Existing Conditions with Solids Filtration upgrades is shown in 

Figure 4-2. 

4-6



DRAFT 

Figure 4-2: Site Plan with Location of Existing Conditions with Solids Filtration Upgrades 

4-7



DRAFT 







Screens are key components of the Microfiltration/Ultrafiltration process as large particulate 

matters can adversely affect the performance and lifetime of membranes significantly. 

The existing screens at the Owls Head WPCP include 1-¼ inch and ¾ inch bar screens, installed 

prior to the primary settling tanks. In the proposed design for Microfiltration/Ultrafiltration, the 

existing screens are utilized without modification. 

For the Microfiltration/Ultrafiltration system, it is prudent to remove larger particles from the 

secondary effluent. A 2 mm fine screen is recommended by the vendor. The assumptions used 

for the design of the fine screens are: 

• The fine screen is a band screen with a 2mm screen size 

• A band screen with a design capacity of 15 mgd 

• A discharge velocity of 0.87 ft/s 

• Screens will be housed indoors as an odor control measure (if feasible) 

• Anticipated solids removal rate of 15 cubic feet per hour 

• Preferred location is downstream of the secondary settling, upstream of the 

Microfiltration/Ultrafiltration process 

• The 2 mm screen is expected to result in approximately 2 ft of headloss 

Solids removed by the 2 mm screens would be pumped to the existing primary sludge line, and 

sent with the primary sludge and wasted activated sludge to the gravity thickeners. 

Specifications for the fine screens are summarized in Table 5-1. 

Item 

Screen opening size 

Location 


Sludge production (120mgd) 

Number of screens 

Screen reject treatment 

Wash water requirement: 

Table 5-1: Fine Screen Specifications 

Specification 

2mm 

after secondary clarifiers within the channel 

15 mgd/screen 

120 cf/hr 

14 (N+1+1) 

Sludge pump, pipe connected to the existing primary sludge line 

250 gpm 

5-1



DRAFT 

The type of screen used in this conceptual design is a dual flow band screen with 2 mm opening. 

Each screen has a design capacity of 15 mgd, and 12 screens are installed to treat up to 180 mgd. 

The flow exceeding maximum design treatment flow of 180 mgd will be diverted upstream of 

the fine screen, thus the screens will not receive the flow excess of 180 mgd. 

The screens would be installed in the channel downstream of the secondary clarifier, upstream of 

the Microfiltration/Ultrafiltration process. 


5.3.1 Baffles 



5.3.2 Mixers 

No mixers will be installed for the Existing Conditions with Microfiltration/Ultrafiltration level 

of treatment. 


There are no changes in the aeration requirements for the Existing Conditions with 


5.3.4 Blowers 

There are no modifications for the blower system necessary for the Existing Conditions with 












5-2



DRAFT 





No RAS chlorination measures are recommended for the Existing Conditions with 









5.7.2 Carbon 




Additional Sodium Hypochlorite is not recommended for the Existing Conditions with 


5.7.4 Polymer 

Polymer addition is not recommended for the Existing Conditions with 



A description of the Intermediate Pump Station needed for the Existing Conditions with 


Conditions with Solids Filtration treatment option. 



5-3



DRAFT 




Filtration is achieved by drawing water to the inside of the membrane fiber under low vacuum 

pressure. Table 5-2 lists defining features of the membrane filters specified for tertiary treatment 

downstream of a conventional activated sludge process. 

Table 5-2: Existing Conditions with Microfiltration/Ultrafiltration Filter Specifications 

Feature 

Specification 

Pore size 

Pressure 

Flow direction 

Membrane type 

Nominal 0.02µm; absolute 0.1µm 

Low-pressure, immersed (open tank) 

Outside-in flow (suction) 

Hollow, non-reinforced fiber membranes 

The membrane filters considered herein have pore sizes at the small end of the microfiltration 

range or the large end of the ultrafiltration range. At this range, colloidal and suspended particles 

and microorganisms/pathogens including certain viruses are removed. 

Each membrane module consists of hollow fiber ultrafiltration membranes mounted in cassettes. 

Figure 5-1 shows that the system is modular on two tiers: 

• Membrane modules combine into cassettes 

• Cassettes combine into process trains (tanks) 

Figure 5-1: Membrane Filter Modularity 

Module Cassette Process train 

The membrane filtration system would replace the final settling effluent channel that spans the 

plant's western shore. Table 5-3 sizes the membrane filter system. The elongated Layout #2 

minimizes fill. 

5-4



DRAFT 

Table 5-3: Existing Conditions with Microfiltration/Ultrafiltration Membrane Filter Sizing 

Parameter Value Unit 

Flow- average 98 67,917 mgd|gpm 

Flow- design 120 83,333 mgd|gpm 

Flow- peak (sustained) 180 125,000 mgd|gpm 

Layout #1 

No. of trains (tanks) 22 

No. of cassettes per train 12 

Total no. of cassettes 264 

No. of modules per cassettes 81 

No. of module spaces per cassettes 96 

Train (tank) dimensions 32.3 14.0 11.8 L | W | D, ft 

Filter process footprint 540 120 L|W,ft 

Layout #2 (more oblong) 

No. of trains (tanks) 32 

No. of cassettes per train 8 

Total no. of cassettes 256 

No. of modules per cassettes 84 

No. of module spaces per cassettes 96 

Filter process footprint 650 80 L|W,ft 

Aside from the membrane modules and their support framing, the tanks contain: 

• Level transmitters 

• Level switches 

• Inlet and drain valves 

Permeate pumps impart all energy required to move the process stream through the tertiary 

membrane filtration system. They produce the low vacuum that draws water through the 

membrane fiber, and propel the treated water (permeate) through the main permeate collection 

manifold piping with sufficient energy so that the effluent head matches the influent head. 

Aside from the permeate pumps themselves, the system includes: 

• Permeate collection piping, grade 316 stainless steel 

• Permeate air removal system 

• Trans-membrane pressure transmitters 

• Permeate pump pressure gauges 

• Permeate flowmeters 

• Turbidimeters 

Filter operation entails a recurring, intermittent process by which the filters are cleaned while in 

service in order to sustain peak performance. This in-service cleaning consists of 2 simultaneous 

processes: 

• Backpulsing 

• Air scouring 

5-5



DRAFT 

At pre-set time intervals, backpulse pumps are engaged to momentarily reverse the flow of 

permeate through the membranes. This back-pulsing removes any particles that may have 

obstructed the pores during membrane operation, and thereby. 

Aside from the backpulse pumps, this system includes: 

• Backpulse water storage tanks 

• Backpulse water storage tanks level transmitters 

• Backpulse tank inlet fill valves 

• Backpulse flowmeter 

Simultaneously with the back-pulsing, diffused air is introduced at the base of the membrane by 

coarse bubble diffusers. The bubbles travel along the surface of the membrane creating 

turbulence that agitates the membrane and scours solids away from its surface. 

The membrane air scour system includes: 

• Scour air distribution piping, grade 304 stainless steel 

• Blowers 

• Blower flow switches 

• Blower pressure gauges 

In membranes must periodically be switched off-line and chemically cleaned in-situ. Routine 

cleanings use sodium hypochlorite, while less frequent cleanings to alleviate persistent fouling 

require citric acid or sodium hydroxide. Spent sodium hypochlorite cleaning solution is 

neutralized with sodium bisulfite then sent to the head of the plant. Components of the chemical 

in-place cleaning system are: 

• Cleaning solutions storage tanks 

• Cleaning solutions distribution system 

• Cleaning solutions neutralization tanks 

• Level transmitters 

• Fill valves 

• Discharge isolation valves 

• Flowmeter 

• Chemical feed systems comprised of storage tank and metering pumps for: 

Sodium hypochlorite 

Sodium bisulfite 

Citric acid 

Sodium hydroxide 

In order to limit the concentration of solids on the filters, tertiary system reject flow must be 

continually bled off. Table 5-4 quantifies filter reject bleed flow as equivalent to 10% of the 

filter influent. This reject flow cannot simply be recycled back to the head of the plant because 

the consequent build-up of colloidal particles within system would increase fouling of the 

membrane and inhibit settling. Instead, the reject bleed enters a second stage solid/liquid 

separator which concentrates the solids into a waste flow less than 1% of tertiary inflow; a flow 

small enough to be blended with the primary and secondary waste sludge. 

5-6



DRAFT 

Table 5-4: Second Stage Reject Bleed Membrane Sizing 

Parameter Value Unit 

Reject bleed flow- design 12 8,333 mgd | gpm 

Reject bleed flow- peak (sustained) 18 12,500 mgd | gpm 

Second stage membrane footprint 163 80 L | W, ft 

The membrane filtration system discharges all solids as waste sludge via this second stage 

solid/liquid separator. For conceptual design purposes, this system is assumed to be 25% the cost 

and size of the membrane filters. This portion is a product of the relative flow second stage 

system must treat (10%) multiplied by 2.5 to account for greater complexity and inverse 

economy of scale. A second stage membrane system could achieve the described solid/liquid 

separation. 

The membrane tanks, second stage membrane tanks, and all ancillary equipment will be 

sheltered in a building. For maintenance and replacement of membrane modules, a bridge crane 

grid will be configured to serve membrane zones. The entire membrane filtration system and its 

building would require extension of the western shore of the plant be means of bay fill. 








No Instrumentation and Control measures are needed for the Existing Conditions with 



The site plan with locations of Existing Conditions with Microfiltration/Ultrafiltration upgrades 

is shown in Figure 5-2. 

5-7



DRAFT 

Figure 5-2: Site Plan with Location of Existing Conditions with 

Microfiltration/Ultrafiltration Upgrade 

5-8



DRAFT 



No modifications to the preliminary or primary treatment systems are required for the Advanced 

Basic BNR level of technology. 




Advanced Basic BNR utilizes the existing step-feed aeration tanks at the Owls Head WPCP. 

The design includes the implementation of baffles, mixers, membrane diffusers, and froth control 

measures. To ensure that the anoxic and switch zones are well-mixed, Invent mixers are 

mounted in each anoxic and switch zone. Because switch zones are sometimes used as aerobic 

zones, membrane fine bubble diffusers will also be mounted in these zones alongside the Invent 

mixer. Aerobic zones will be fitted with membrane fine bubble diffusers. Three levels of froth 

control measures will also be implemented. Figure 6-1 shows the Owls Head aeration tank 

configuration. 

Figure 6-1: Owls Head Aeration Tank Conceptual Configuration 

6.3.1 Baffles 

6-1



DRAFT 

New baffles will be installed in all four passes of each tank to separate potential anoxic and deoxygenation 

zones from the aerobic zones. The new baffles will be “full width” (23 ft 6 inches 

wide) and submerged with flow both over and under the baffles. The submerged baffles will 

allow the froth to move along the surface from zone to zone without physical traps. The 

underflow will allow the wastewater to drain freely from zone to zone. This will also minimize 

the structural requirements and cost of the baffles. The baffle over/under flow split will be 

approximately 85/15. For cost estimating purposes, the baffles are assumed to be made of 

fiberglass panels mounted on steel beams. 

The tanks are retrofitted with baffles to create anoxic (including swing zones), aerobic, and preanoxic 

zones. Table 6-1 presents the design guidance for the location of new baffles. Figure 6- 

1 shows the baffle locations at the Owls Head WPCP. 

Pass 

Table 6-1: Location of Baffles for Advanced Basic BNR 

Baffle2 

(between switch zone 

and aerobic zone) 

Baffle 1 

(between first anoxic zone 

and switch zone) 

Baffle 3 

(between aerobic zone 

and pre-anoxic zone) 

A 1/6 length of pass 1/3 length of pass 5% from end of pass 

B 1/6 length of pass 1/3 length of pass 5% from end of pass 

C 1/6 length of pass 1/3 length of pass 10% from end of pass 

D 1/6 length of pass 1/2 length of pass N/A 

6.3.2 Mixers 

Hyperboloid mixers (Invent mixers) are proposed for this conceptual design. A typical 

installation of the mixers is shown in Figure 6-2. 

Figure 6-2: Typical Installation of Hyperboloid Mixers 

Similar mixers will be installed at the Wards Island WPCP full scale BNR demonstration at 

Battery E. Each mixer is 8 ft in diameter, and is placed approximately 1 ft above the bottom of 

the reactor. Each mixer is mounted from the top of the reactor with a supporting structure as 

suggested by the vendor. 

Invent HyperClassic mixers are low speed (20–50rpm), non-corrosive, and the motor energy 

required can be up to 50% less than a conventional mixer. Because of this, standard geared 

6-2



DRAFT 

motors are used, as there are no side or upward forces on the mixer shaft. Details of the mixers 

are presented below: 

Type: 

Horsepower: 

Propeller Speed: 

Motor Speed: 

Number of Mixers: 

Vertical Hyperboloid 

1.5 hp 

22 rpm 

1800 rpm 

20 per tank (80 total) 

Pass A 2 in anoxic zone 

2 in switch zone 

1 in deoxygenation zone 

Pass B 2 in anoxic zone 



Pass C 2 in anoxic zone 



Pass D 2 in anoxic zone 


Mixers are typically mounted in the middle of the tank and the mixer shaft is mounted on the 

side of a platform, directly over the center of the zone. Mounting the mixer shafts off the edge of 

the platform allows easier removal of the mixer for maintenance purposes. Because some zones 

have a greater than 2:1 ratio (65 feet long by 25 feet wide), two mixers will be installed in each 

anoxic and switch zone, as well as the deoxygenation zone in Pass C. The hyperboloid mixers 

create a “virtual wall”, which will essentially create two continuously stirred tank reactors 

(CSTRs) in each of these zones. The mixers will be mounted off the edge of the platform, 

approximately 25% and 75% along the length of the zone. Mixers will be mounted in the middle 

of each deoxygenation zone in Passes A and B. Partial platforms are required over each anoxic 

zone, switch zone, and deoxygenation zone. 


Sufficient aeration to satisfy process oxygen requirements is a prerequisite for BNR process 

performance. Air must be available to meet both carbonaceous and nitrogenous oxygen demands. 

As suggested by the Design Guidance, no oxygen demand credit was accounted due to 

denitrification. The total oxygen demand (TOD) was estimated using the following equation: 

TOD = 1.1 (BOD pe ) + 4.6 (TKN pe – TKN assim – TKN unox ) 

Where: 

TOD = Total oxygen demand (lbs/day) 

BOD pe = Primary effluent BOD (lbs/day) 

TKN pe = Primary effluent TKN (lbs/day) 

6-3



DRAFT 

TKN assim = TKN assimilated in the WAS (lbs/day) 

TKN unox = Unoxidized final effluent TKN (lbs/day) 

At average conditions and assuming the TKN assimilated in the WAS is negligible, total oxygen 

demand is estimated to be 187,110 lb/day. Likewise, at peak conditions, the total oxygen 

demand is 282,618 lb/day. 

The air requirement estimate depends on the values of , , , and SOTE of diffuser. The 

factor is the ratio of the K L a of wastewater to the K L a of clean water, and varies with the 

physical features of the diffuser system, the geometry of the reactor, and the characteristics of 

wastewater. The factor is the ratio of the dissolved oxygen saturation concentration in 

wastewater to the corresponding value in clean water. The factor is used to employ temperature 

correction for K L a. SOTE is the standard oxygen transfers efficiency of diffuser. The SOTE 

value per foot submergence of the diffuser varies with diffuser type, airflow per diffuser, basin 

geometry, and diffuser placement and density. 

For estimating the air requirements, the values of , and were selected as shown in Table 6- 

2. The recommended values from two different sources are shown in Table 6-2. 

Table 6-2: Values of α, β and θ 

Parameter Selected Value 

Recommended Value 

Range 

Typical 

, diffused air 0.5 0.4 - 0.8 (1) 

0.95 

0.7 – 0.98 (1) 0.95 (1) 

0.8 – 1.0 (2) 

1.024 

1.015 - 1.04 (1) 1.024 (1) 

1.008 - 1.047 (2) 1.024 (2) 

(1) Wastewater Engineering – Treatment and Reuse, 2003 by Metcalf & Eddy 

(2) EPA Design Manual - Fine Pore Aeration System (EPA/625/1-89/023) 

The SOTE value was assumed to be 1.75% per foot of diffuser submergence for the fine bubble 

diffuser. The OTR f /SOTR (ratio of oxygen transfer rate at field condition to standard condition) 

was estimated as 0.3, which appeared conservative. The calculated air requirements for average 

and peak loadings are shown in Table 6-3. 

Table 6-3: Advanced Basic BNR Air Requirements Calculated per Design Guidance 

Condition 

Total Oxygen Demand 

(lb/day) 

Air Requirement 

(SCFM) 

Average Day (SCFM) 187,110 98,000 

Peak Day (SCFM) 282,618 148,000 

(1) Based on the estimated maximum concentrations of BOD and TKN in the primary effluent 

Table 6-2 shows the calculated total oxygen demand for an average day and a peak day, based 

on stoichiometry and taking no credit for denitrification. Because the Advanced Basic BNR 

Design Guidance calls for maximizing use of existing facilities, these air requirements were 

compared to the air requirements determined using the BioWin model. All modeling was 

performed at the average design dry weather flow of 120 mgd. Average loads were determined 

6-4



DRAFT 

by the AWT Team using NYC DEP BEPA 2045 population projections. Three operating cases 

were evaluated using the BioWin model: 

1. Average: 120 mgd (ADDW flow) and 2045 projected loads at 20°C 

2. Peak: 120 mgd and peak loads at 20°C 

3. Winter: 120 mgd (ADDW flow) and 2045 projected loads at 12°C 

The modeling targeted an AEMLSS of 2,000 mg/L and effluent quality goals as described in 

Table EX-1. The air requirements as determined by the BioWin modeling are shown in Table 6- 

4. 

Table 6-4: Advanced Basic BNR Air Requirements derived from BioWin Modeling 

Condition 


(SCFM) 

Peak Day (1) 53,000 

Average Day 50,000 

Winter Average Day 46,000 

(1) Based on the estimated maximum concentrations of BOD and TKN in the primary effluent 

6.3.4 Blowers 

Owls Head WPCP currently has four 27,000 cfm blowers. For Advanced Basic BNR operation, 

two of these blowers can be utilized with two blowers designated for standby and peak demand 

requirements. The existing air piping is sufficient for the anticipated air requirements. The 

existing blower process flow diagram is shown in Figure 6-3. 


The sustained operating range for membrane disk diffusers is 0.5 to 4.0 SCFM per diffuser. The 

maximum allowable airflow is 7 SCFM for short periods of time. The typical design airflow 

range is 1 to 2 SCFM per diffuser. 

For conceptual design purposes, the approximate number of diffusers was determined by taking 

the average air demand specifying that each diffuser supply 1.5 cfm/diffuser. The peak and low 

air demands are then compared to the required number of diffusers to check that peak demands 

do not require greater than 3.0 cfm/diffuser and winter demands do not require less than 1.0 cfm 

diffuser. The Advanced Basic BNR operating mode requires 35,500 membrane diffusers. 

Specifications for the diffuser system are shown in Table 6-5. 

Table 6-5: Advanced Basic BNR Diffuser Information 

Item 

Specification 

Diffuser Type 

9-inch fine bubble membrane 

Capacity 

0.5 to 4.0 cfm/diffuser (typical) 

7 cfm/diffuser (max) 

Number of diffusers 35,500 

6-5



DRAFT 

Figure 6-3: Existing Blower Process Flow Diagram 

6-6



DRAFT 


The Final Settling Tanks at Owls Head WPCP are adequately sized for Advanced Basic BNR 

operation. The overflow rate at peak flow rate of 180 mgd (1.5 times DDWF) is 1,200 gallons 

per day per square foot. The loading rate at peak flow with 50 percent RAS flow (240 mgd) is 

27 pounds suspended solids per day per square foot. These two criteria are consistent with Ten 

State Standards. 


The RAS/WAS system at Owls Head WPCP is adequately sized for Advanced Basic BNR 

operation. The existing RAS system consists of four 30 mgd pumps; 50 percent DDWF RAS 

flow can be achieved using two of these pumps while having two pumps as standby. The 

existing WAS system is designed for 15 percent DDWF capacity, which is more than adequate 

for Advance Basic BNR operation. 


The older sludge that is required for nitrification also promotes the growth of filaments. The 

filaments create froth on the surface of aeration tanks, and the froth can deteriorate the effluent 

quality, cause odors, upset anaerobic digesters, and create slipping hazards on walkways. The 

primary cause of froth is excessive filaments such as Nocardia and Microthrix. Older sludge does 

not compete as well with the filaments for the limited food and nutrients. As the filament 

population increases in the older activated sludge, the hydrophobic filaments (Nocardia and 

Microthrix) tend to rise with the air bubbles to the surface of aeration tanks. 

Three methods of froth control are planned for Owls Head WPCP under the Advanced Basic 

BNR level of treatment: 

1. Froth hoods (surface chlorination) 

2. RAS chlorination 

3. Surface wasting 


Surface chlorination preferentially targets surface foaming filaments and proved to be an 

effective froth control technique in pilot demonstrations. The BNR Design Guidance document 

recommended design criteria for the surface chlorination system including the chlorine dosage 

and locations of the chlorine spray hoods. Sixteen full-width froth control hoods have been 

recommended for surface chlorination. Their locations will be at approximately the 16% and 

66% positions along passes A and B per the Design Guidance. Figure 6-4 shows the location of 

the froth hoods. The chlorine dosage would be 0.5 to 2.0 mg/L based on wastewater flow for 

maintenance and 4.0 to 8.0 mg/L for emergency dosages. The sodium hypochlorite usage would 

be about 1,800 gallons per day at maintenance concentrations and 13% chlorine. Five day 

storage of sodium hypochlorite would amount to 9,000 gallons. 

6-7



DRAFT 

Each froth control hood will contain one or more spray bars. Each spray bar will be connected to 

the froth hood with quick disconnects. Spray bars will be interchangeable to test various nozzles 

and orifices. The disinfected plant effluent used for chlorine dilution water will be strained 

through automatic backwash duplex strainers with mesh openings of 1/32 inch or less to 

minimize plugging of the nozzles. The spray bars will have individual shut-off valves and will be 

accessible for maintenance and/or replacement. Flushing water for the spray bars will be 

provided. Each froth hood will have adjustable gates upstream and downstream to allow froth to 

enter, to periodically allow accumulated floatable solids to escape, and to minimize the chlorine 

odors from escaping the hood. The froth control hoods will be accessible for maintenance. 

For each tank, there will be six metering pumps, four online and two standby. The metering 

pumps will be manually operated or paced on primary effluent flow. The source of chlorine for 

surface chlorination will be sodium hypochlorite at concentrations of approximately 13% to 15% 

sodium hypochlorite. The sodium hypochlorite will be diluted with disinfected plant effluent to 

approximately 1,000 to 3,000 mg/L as chlorine. The disinfected plant effluent used for dilution 

will be strained through automatic backwash duplex strainers with mesh openings of 1/32 inch or 

less to minimize plugging of the nozzles. 

Figure 6-4: Location of Froth Hoods for Advanced Basic BNR 


RAS chlorination is generally used to control sludge bulking but it has also had limited success 

in reducing froth. It is less effective than surface chlorination for froth control, and it can create a 

turbid effluent and inhibit nitrification if overdosed. Its primary advantage is that it has fewer of 

6-8



DRAFT 

the practical problems: no spray nozzles to clog, no spray hoods to access and maintain. It is 

recommended that RAS chlorination be implemented as the third line of defense for froth control 

in the Step-feed BNR facilities. The RAS chlorination design objectives include: 

• Design dose should range from 1 to 10 lbs Cl 2 per 1000 lbs MLSS inventory in the secondary 

system per day (based on bulking control). 

• Typical dose for froth control ranges from 3 to 5 lbs Cl 2 per 1000 lbs MLSS inventory in the 

secondary system per day. 

For RAS chlorination, diluted sodium hypochlorite will be added downstream of the RAS 

pumps. There will be two metering pumps, one online and one standby. The metering pumps 

will be paced on RAS flow or manually operated. The source of chlorine for RAS chlorination 

will be sodium hypochlorite at concentrations of approximately 13% to 15% sodium 

hypochlorite. The sodium hypochlorite will be diluted with disinfected plant effluent to 

approximately 5,000 to 15,000 mg/L of chlorine before addition to the RAS. 

RAS chlorination demand is approximately 8,800 gallons per day of sodium hypochlorite. 

Because RAS chlorination is to be used intermittently, two days of storage should be sufficient to 

meet RAS chlorination needs. Additional storage of sodium hypochlorite for RAS chlorination 

is 17,600 gallons. 

The total additional sodium hypochlorite storage requirement for surface chlorination and RAS 

chlorination is approximately 27,000 gallons, consisting of three 9,000-gallon tanks. 


Surface wasting removes the floating nuisance organisms that contribute to froth. Adjustable 

downward opening gates are recommended for surface wasting for Owls Head WPCP. The 

downward opening gates will be mounted on two new surface wasting pump sumps built at the 

end of each pass A. Lowering a gate(s) will allow the froth and/or MLSS to overflow the weir 

into the surface wasting pump station(s). The surface waste will be pumped to the existing waste 

activated sludge wet well near the Final Settling Tanks for further delivery to sludge processing. 

The flow and TSS concentration of the surface waste will be measured and totalized. The flow 

and TSS data will dictate time based operation of the pumps preventing overwasting. The 

elevation of the downward opening gates will be operated either automatically or manually based 

on the aeration tank wastewater elevation. 



Alkalinity addition is not recommended for the Advanced Basic BNR level of technology. 

6.7.2 Carbon 


6-9



DRAFT 


As described in Section 6.6.1, it is anticipated that sodium hypochlorite usage for froth hoods 

would be about 1,800 gallons per day at maintenance concentrations and 13% chlorine. Five day 

storage of sodium hypochlorite would amount to 9,000 gallons. In addition, RAS chlorination 

demand is approximately 8,800 gallons per day of sodium hypochlorite. Because RAS 

chlorination is to be used intermittently, two days of storage should be sufficient to meet RAS 

chlorination needs. Additional storage of sodium hypochlorite for RAS chlorination is 17,600 

gallons. The total additional sodium hypochlorite storage requirement for surface chlorination 

and RAS chlorination is approximately 27,000 gallons, consisting of three 9,000-gallon tanks. 

These three new tanks will be located in a new Sodium Hypochlorite Storage Building, located 

south of the Primary Settling Tanks. The new building will be single story and have a footprint 

of approximately 24 feet by 120 feet, or 2,880 sq. ft. Figure 6-5 shows the new froth control 

process. 

Figure 6-5: New Froth Control Process Flow Diagram for Advanced Basic BNR 

6.7.4 Polymer 

Polymer addition is not recommended for the Advanced Basic BNR level of technology. 


6-10



DRAFT 













Monitoring equipments for the system control would be the essential part of the Advanced Basic 

BNR system. A summary of required instrumentations are shown in Table 6-6. 

Table 6-6: Instrumentation and Control for Advanced Basic BNR 

Instrumentation and 

Location(s) 

Number of instruments 

Control 

Flow meter 

Plant influent (existing) 

RAS (existing) 

WAS (existing) 

Surface wasting (new) 

Primary sludge (existing) 

Plant effluent (existing) 

Sodium hydroxide (new) 

1 for each metering location 

DO Probes Passes B and C 2 in each tank (Passes B and C), 

8 total 


The site plan along with the location of the potential Advanced Basic BNR upgrades is shown in 

Figure 6-6. 

6-11



DRAFT 

Figure 6-6: Site Plan with Location of Advanced Basic BNR Upgrades 

6-12



DRAFT 



No modifications to the preliminary or primary treatment systems are required for Full Step BNR 

operation. 




Full Step BNR utilizes the existing step-feed aeration tanks at the Owls Head WPCP. The 

design includes the implementation of baffles, mixers, chemical addition, and froth control 

measures. To ensure that the anoxic and switch zones are well-mixed, Invent mixers are 

mounted in each zone anoxic and switch zone. Because switch zones are sometimes used as 

aerobic zones, membrane fine bubble diffusers will also be mounted in these zones alongside the 

Invent mixer. Aerobic zones will be fitted with membrane fine bubble diffusers. Carbon 

addition, alkalinity addition and three levels of froth control measures will also be implemented. 

7.3.1 Baffles 

The baffle design for Full Step BNR is the same as the design for Advanced Basic BNR as 

described in Section 6.3.1 and shown in Figure 6-1. 

7.3.2 Mixers 

The mixer design for Full Step BNR is the same as for Advanced Basic BNR. Hyperboloid 

mixers (Invent mixers) are proposed for the Full Step BNR conceptual design. See Section 

6.3.2 for a description of these mixers. 


Sufficient aeration to satisfy process oxygen requirements is a prerequisite for BNR process 

performance. Full Step BNR operates at higher RAS rates (up to 100% DDWF), which leads to 

higher mixed liquor concentrations in the aeration tanks than under Advanced Basic BNR 

operation. Full Step BNR operation requires higher air requirements and improves effluent 

quality. Air must be available to meet both carbonaceous and nitrogenous oxygen demands. As 

suggested by the Design Guidance, no oxygen demand credit was accounted due to 

denitrification. Total oxygen demand was calculated in Section 6.3.3. 

As described in Section 6.3.3, the air requirements were also calculated using the BioWin model. 

All modeling was performed at the average design dry weather flow of 120 mgd. Average loads 

were determined by the AWT Team using NYC DEP BEPA 2045 population projections. Three 

operating cases were evaluated using the BioWin model: 

7-1



DRAFT 

1. Average: 120 mgd (ADDW flow) and 2045 projected loads at 20°C 

2. Peak: 120 mgd and peak loads at 20°C 

3. Winter: 120 mgd (ADDW flow) and 2045 projected loads at 12°C 

The modeling targeted an AEMLSS of 2,500 mg/L and effluent quality goals as described in 

Table EX-1. Table 7-1 shows air requirements as determined from the modeling. 

Table 7-1: Full Step BNR Air Requirements derived from BioWin Modeling 

Condition 


(SCFM) 

Peak Day (1) 79,000 

Average Day 64,000 

Winter Average Day 55,000 

(1) Based on the estimated maximum concentrations of BOD and TKN in the primary effluent. 

7.3.4 Blowers 

Owls Head WPCP currently has four 27,000 cfm blowers. For Full Step BNR operation, three of 

these blowers can be utilized with one blower designated for standby and peak demand 

requirements. The existing air piping is sufficient for the anticipated air requirements. 


The sustained operating range for membrane disk diffusers is 0.5 to 4.0 SCFM per diffuser. The 

maximum allowable airflow is 7 SCFM for short periods of time. The typical design airflow 

range is 1 to 2 SCFM per diffuser. 

As with the Advanced Basic BNR design, the approximate number of diffusers was determined 

by taking the average air demand specifying that each diffuser supply 1.5 cfm/diffuser. The peak 

and low air demands are then compared to the required number of diffusers to check that peak 

demands do not require greater than 3.0 cfm/diffuser and winter demands do not require less than 

1.0 cfm diffuser. The Full Step BNR operating mode requires 42,700 membrane diffusers. 

Specifications for the diffuser system are shown in Table 7-2. 

Item 

Table 7-2: Full Step BNR Diffuser Information 

Specification 

Diffuser Type 

9-inch fine bubble membrane 

Capacity 

0.5 to 4.0 cfm/diffuser (typical), 7 cfm/diffuser (max) 

Number of diffusers 42,700 


The Final Settling Tank overflow rate at peak flow rate of 180 mgd (1.5 times DDWF) is 1,200 

gallons per day per square foot. The loading rate at peak flow with 50 percent RAS flow (240 

mgd) is 41.81 pounds suspended solids per day per square foot. These two criteria are consistent 

with Ten State Standards. 

7-2



DRAFT 

Although the Final Settling Tanks at Owls Head WPCP are adequately sized for Full Step BNR 

operation, polymer addition is recommended as a precautionary measure. The guidance 

documents identify the ability to add polymer as a method of assuring solids removal during 

periods of unstable operation. The design objectives and features for polymer addition as 

indicated in the BNR guidance document include: 

• Polymer addition must allow for sufficient mixing to optimize polymer efficiency. 

• Polymer feed rate must provide for 0.5 to 3.0 mg/L in the mixed liquor stream. 

• Polymer addition should be flow paced. 

See Section 7.7.4 for Polymer storage requirements. 


The existing RAS system consists of four 30 mgd pumps, which provides 100 percent DDWF 

RAS flow if all four pumps are operating. However, there is not sufficient floor space in the 

existing RAS pump area to add a standby unit. To avoid major structural modifications, four 

new 40 mgd RAS will replace the existing RAS pumps. Three of these pumps will provide 

100% DDWF RAS capacity while providing one standby unit. 

The existing WAS system is designed for 15% DDWF capacity, which is more than adequate for 

Advance Basic BNR operation. The RAS/WAS flow diagram is shown in Figure 7-1. 

7-3



DRAFT 

Figure 7-1: RAS/WAS Process Flow Diagram for Full Step BNR 

7-4



DRAFT 


Froth control measures are the same for Full Step BNR and Advanced Basic BNR. See Section 

6.6 for a discussion of the three methods of froth control planned for Owls Head WPCP under 

the Full Step BNR level of treatment. 



Alkalinity addition is required to maintain a favorable pH for nitrification. Sodium hydroxide is 

selected as the source of alkalinity for the BNR based on cost and ease of handling. Based on the 

BNR Design Guidance, alkalinity requirement is estimated assuming no credit for alkalinity 

produced by denitrification. An average of 110 mg/L of alkalinity, as calcium carbonate, is 

present in the wastewater. Although alkalinity is also contributed during the denitrification 

process by returning about 3.57 lbs to the mixed liquor per every pound denitrified, for this 

analysis no credit is going to be taken for denitrification. During the nitrification process, 7.14 

lbs are consumed per pound nitrified and it is also necessary to provide an alkalinity residual of 

50 mg/L to keep the pH at desirable levels. Given that there is approximately 24,000 lbs of TKN 

in the primary effluent, approximately 5,460 gallons of sodium hydroxide (25% solution) are 

required per day. Two 15,000 gallon tanks will provide a little more than a 5-day supply. These 

two tanks will be located in a new Sodium Hydroxide Storage Building, located to the east of the 

Aeration Tanks and just south of the Grit and Scum Building. The new building will be singlestory 

and have a footprint of approximately 60 feet by 120 feet, or 7,200 sq. ft. 

7.7.2 Carbon 


available in the wastewater may be insufficient to promote denitrification. Carbon addition will 

be incorporated at the Full Step BNR level of treatment. The design objectives and features as 

described in the BNR design guidance include: 

• Provide supplemental carbon to enhance denitrification. 

• Provide capability to feed to the head of all anoxic zones. 


BOD, and TKN with a feedback bias based on residual nitrate measurement. 

• Provide mixing at dosage points. 

• Provide seven days of chemical storage under average conditions. 

If full nitrification is followed by full denitrification, the addition of an external carbon source to 

the wastewater in the head of Pass B and Pass D of each Aeration Tank pass will be required. 

The carbon source is a BOD load that will consume any available oxygen, in this case the 

oxygen bound in the nitrate form (NO 3 ). Once this occurs, the free unbound nitrogen (N) comes 

out of solution as a gas and is released to the atmosphere. 

7-5



DRAFT 

Methanol is the supplemental carbon source currently proposed for Full BNR operation. 

Methanol requirements were determined using the BioWin model. The methanol facility will 

consist of five 50 gph feed pumps (one per aeration tank, one standby), and two 18,000 gallon 

underground storage tanks, which provide seven days of storage capacity under average 

conditions. The feed pumps and controls will be housed in a new Methanol Storage Building to 

be installed on the deck of the aeration tanks. 

The tanks will be double-walled, with a 304L stainless steel interior and a carbon steel exterior. 

The carbon steel exterior will be coated with urethane coating for corrosion protection. 

Piping for methanol system will be installed underground. The segment of piping from the 

methanol storage system to the aeration tanks will be 2-inch double walled CPVC. Underground 

piping will conform to UL-971 (nonmetallic Underground Piping for Flammable Liquids). 

Where above ground piping is necessary, 316 stainless steel pipe would be used. 

Methanol will be supplied via truck delivery and unloading will be gravity-driven through 

flexible hoses into an internal drop tube to the tank. The entire containment area and fill station 

will be protected by a foam fire suppression system designed to meet NFPA requirements. 


The sodium hypochlorite storage requirements are the same for Full Step BNR and Advanced 

Basic BNR and are described in Section 6.7.3. The total additional sodium hypochlorite storage 

requirement for surface chlorination and RAS chlorination is approximately 27,000 gallons, 

consisting of three 9,000-gallon tanks. 

These three new tanks will be located in a new Sodium Hypochlorite Storage Building, located 

south of the Primary Settling Tanks. The new building will be single story and have a footprint 

of approximately 24 feet by 120 feet, or 2,880 sq. ft. 

7.7.4 Polymer 

Polymer storage requirements are relatively small: two 2,000-gallon tanks will provide five days 

storage capacity. Polymer feed facilities will include 4 (2 duty, 2 standby) hydraulic diaphragm 

pumps, each with a capacity of 10 to 75 gph. The feed will be flow paced based on the influent 

flow to the settling tanks, at a rate equivalent to 0.5 – 3.0 mg/L in accordance with the guidance 

documents. 



technology. 



7-6



DRAFT 









Monitoring equipments for the system control would be the essential part of the Full Step BNR 

system. A summary of required instrumentations are shown in Table 7-3. 

Table 7-3: Instrumentation and Control for Full Step BNR 


Control 

Location(s) 


Flow meter 

DO Probes 

pH meter 


Plant influent (existing) 

RAS (existing) 

WAS (existing) 

Surface wasting (new) 

Primary sludge (existing) 

Plant effluent (existing) 

Sodium hydroxide (new) 

2 in each pass of each 

aeration tank 

1 probe in Pass D of each 

tank 


8 per tank, 32 total 

1 per tank, 4 total 

The site plan along with the location of the potential Full Step BNR upgrade is shown in Figure 

7-2. 

7-7



DRAFT 

Figure 7-2: Site Plan with Locations of Full Step BNR Upgrades 

7-8



DRAFT 








8.3.1 Baffles 



8.3.2 Mixers 

A description of the mixers needed for the Full Step BNR with Solids Filtration level of 



A description of the aeration requirements for the Full Step BNR with Solids Filtration level of 


8.3.4 Blowers 

A description of the modifications to the blowers needed for the Full Step BNR with Solids 


option. 






A description of the modifications to the final setline tanks needed for the Full Step BNR with 



8-1



DRAFT 


A description of the Return and Waste Activated Sludge System design needed for the Full Step 

BNR with Solids Filtration level of technology was provided in Section 7.5 for the Full Step 



Froth control measures are the same for Full Step BNR with Solids Filtration and Advanced 

Basic BNR. See Section 6.6 for a discussion of the three methods of froth control planned for 

Owls Head WPCP under the Full Step BNR with Solids Filtration level of treatment. 





option. 

8.7.2 Carbon 




A description of the Sodium Hypochlorite addition design needed for the Full Step BNR with 



8.7.4 Polymer 

A description of the Polymer addition design needed for the Full Step BNR with Solids Filtration 



A description of the Intermediate Pump Station needed for the Full Step BNR with Solids 

Filtration level of technology was provided in Section 4.8 for the Existing Conditions with 

Solids Filtration treatment option. 



8-2



DRAFT 






technology. 



technology. 



technology. 


A description of the Instrumentation and Control needed for the Full Step BNR with Solids 

Filtration level of technology was provided in Section 7.11 for the Full Step BNR treatment 

option. 


Figure 8-1 lays out tertiary filters and a supporting pump station. 

8-3



DRAFT 

Figure 8-1: Site Plan with Locations of Full Step BNR with Solids Filtration Upgrades 

8-4



DRAFT 










9.3.1 Baffles 




9.3.2 Mixers 

A description of the mixers needed for the Full Step BNR with Microfiltration/Ultrafiltration 



A description of the aeration requirements needed for the Full Step BNR with 



9.3.4 Blowers 

A description of the modifications to the blower system needed for the Full Step BNR with 








9-1



DRAFT 

























9.7.2 Carbon 








9-2



DRAFT 

9.7.4 Polymer 

A description of the Polymer addition design needed for the Full Step BNR with 




A description of the Intermediate Pump Station needed for the Full Step BNR with 






technology. 












A description of the Instrumentation and Control needed for the Full Step BNR with 




Figure 9-1 lays out membrane filters and a supporting pump station. 

9-3



DRAFT 

Figure 9-1: Site Plan with Locations of Full Step BNR with Solids Filtration Upgrades 

9-4



DRAFT 







technology. 


10.3.1 Baffles 



10.3.2 Mixers 

A description of the mixers needed for the Full Step BNR with Denitrification Filters level of 



A description of the aeration requirements for the Full Step BNR with Denitrification Filters 


10.3.4 Blowers 

A description of the modifications to the blower system needed for the Full Step BNR with 








A description of the modifications to the final setline tanks needed for the Full Step BNR with 



10-1



DRAFT 


A description of the Return and Waste Activated Sludge System design needed for the Full Step 

BNR with Denitrification Filters level of technology was provided in Section 7.5 for the Full 



Froth control measures are the same for Full Step BNR with Denitrification Filters and 

Advanced Basic BNR. See Section 6.6 for a discussion of the three methods of froth control 

planned for Owls Head WPCP under the Full Step BNR with Denitrification Filters level of 

treatment. 





10.7.2 Carbon 

A description of the Carbon addition design needed for the secondary treatment in the Full Step 



In addition, supplemental denitrification requires addition of more external carbon to the anoxic 

filter. As with BNR, methanol is the supplemental carbon source currently proposed for 

denitrification filter operation. 

Methanol will be stored together with methanol for the denitrification process in a third 18,000 

gallon underground storage tank. The feed pumps and controls will be housed in the same new 

Methanol Storage Building to be installed on the deck of the aeration tanks for the BNR process. 

Its delivery, storage and distribution piping will conform to the requirements presented in 

Section 7.7.2 of this report. Table 10-1 shows the specifications for supplemental carbon for 

denitrification filters. 

10-2



DRAFT 

Carbon source 

Concentration 

Table 10-1: Denitrification Filter Supplemental Carbon System specifications 

Item 

Specification 

Requirement: Average | Max month 

Required on-site storage 

Storage tanks / capacity 

Type of feed pumps 

Pump capacity 



Methanol 

100% (1,188,000 mg-COD/L) 

1.75 | 2.288 gpm 

7 days @ Avg. = 17,640 gal 

1 tank @ 18,000 gal 

Metering 

0.5 gpm 

8 (1 per filter) 





A description of the Polymer addition design needed for the Full Step BNR with Denitrification 



A description of the Intermediate Pump Station needed for the Full Step BNR with 

Denitrification Filters level of technology was provided in Section 4.8 for the Existing 





technology. 



technology. 


The following is the process sequence through one typical modular up-flow submerged fixedfilm 

filter. The intermediate pumps feed process water into a common inlet channel above the 

10-3



DRAFT 

denitrification filters. From here, process water flows down to feed the individual cells from 

beneath. The head in the channel forces process water upwards through the filter media. The 

media contained in the cells is composed of specially manufactured high density polystyrene 

beads covered by active biomass. In the absence of air but in the presence of added methanol, 

this active biomass converts nitrate to nitrogen gas. Ceiling plates with regularly spaced nozzles 

are used to retain the filter media against the upflow. The nozzles collect treated water into a 

common water reservoir above the filters. The specifications for denitrification filter and 

backwash are shown in Tables 10-2 and 10-3 respectively. 

Item 

Denitrification filter type 

Table 10-2: Denitrification Filter Specifications 

Specification 

Modular up-flow submerged fixed-film 

(Krüger BIOSTYR) 

Number of filters modules 8 

Filter Area of module 2,582 ft 2 

Size of media 

Depth of media 

4.5mm 

8.2 feet 

Filter loading rate, Peak 7.44 gpm/ft 2 


Methanol requirement, Max month 

Head loss through filter 

22.5 mgd/module 

21,780 lb/d = 3,295 gal/d 

8 feet 

Table 10-3: Denitrification Filter Backwash Specifications 

Item 

Specification 

Sludge Production, Max. month 

Process air (for backwash only) 

Backwash mud well capacity 

Sludge production, Max month 

17,780 lb/d 

1,700 scfm per module 

476,000 gallons 

17,780 lb/d 

Figure 10-1 shows a denitrification filter. 

10-4



DRAFT 

Figure 10-1: Denitrification Filter 

Growth of biomass and the retention of suspended solids in the filter media make periodic 

backwashing necessary. Water from the common treated water reservoir flows down through the 

filter by gravity, thereby expanding the media bed and flushing solids from the bottom of the 

filter. (This does not require additional pumping.) An air grid located below the media composed 

of perforated stainless steel piping injects scouring air during the backwash sequence. Finally, 

used backwash water is collected in drainpipes at the bottom of the filters. 

Backwashing is required every 24 hours or more. The backwash sequence is performed 

automatically and is triggered either when a preset time limit has expired or when the head loss 

across the filter exceeds a predetermined set-point. 

Treated water is collected in an effluent channel for use during backwash. A typical backwash 

for these filters will produce around 396,000 gallons. For design purposes we estimate that 

3,168,000 gallons of waste backwash water the will be generated per day during maximum 

month conditions. During backwash, the used backwash water is detained in a waste backwash 

mud well and then pumped over a period of about 60 to 120 minutes to the primary clarifiers. 

Backwash air can be supplied with a centralized blower system. The discharge pressure typically 

ranges from 8 to 10 psig. 



technology. 


A description of the Instrumentation and Control needed for the Full Step BNR with 



10-5



DRAFT 


Figure 10-2 shows the site plan with the locations of Full Step BNR with Denitrification Filters 

upgrade. 

10-6



DRAFT 

Figure 10-2: Site Plan with Locations of Full Step BNR with Denitrification Filtration 

Upgrades 

10-7



DRAFT 



The existing primary clarification tanks are utilized without modification. The specifications for 

the primary clarification tanks are shown in Table 11-1. 

Table 11-1: Existing Primary Clarifier Specifications 

Primary Tanks – 

Specification 

grease/oil removal mechanisms 

Type of tanks 

11-1 

Rectangular with chain and flight mechanism 


Dimensions (W x L x D) 63’ x 242.7’ x 13’ 

Surface area 15,290 ft 2 

Total overflow rate (at 120 mgd) 

Provide equal and uniform flow distribution to 

each tank 

Provide removal of grease and floatables 

Maximize solids removal within existing 

tankage 


2,616 gal/ft 2 /day 

Screens are key components of the MBR process as large particulate matters can adversely affect 

the performance and lifetime of membranes significantly. A typical MBR process includes a 6 

mm fine screen upstream of the primary clarifiers, and a 2 mm fine screen downstream of the 

primary clarifiers to further remove larger particles. 

The existing screens at the Owls Head WPCP include 1-¼ inch and ¾ inch bar screens, installed 

prior to the primary settling tanks. In the proposed design for MBR, the existing screens are 

utilized without modification. 

Even though the design guidance suggested that the conceptual design include 6 mm fine screens 

upstream of primary settling tanks, it was deemed unnecessary to install 6 mm screens upstream 

of the primary clarifiers at the Owls Head WPCP, and existing coarse screens could be used. It 

was suggested by Zenon that existing coarse screens upstream of the primary settling tank should 

be sufficient as long as the 2 mm fine screens are installed downstream of the primary settling 

tanks. 

For the MBR system, it is prudent to remove larger particles prior to the biological treatment 

process as they affect the efficacy and life-time of the membrane modules. A 2 mm fine screen 

is recommended by the vendor. G.P. Jager & Associates, which locally represents both JWC's 

2mm fine screens a competing MBR design by Seimens reiterated that it is not uncommon to 

Yes 

Yes 

Yes



DRAFT 

install fine screening downstream of the primary settling tanks. The assumptions used for the 

design of the fine screens are: 

• The second fine screen is a band screen with a 2mm screen size 

• A band screen with a design capacity of 15 mgd 

• A discharge velocity of 0.87 ft/s 

• Screens will be housed indoors as an odor control measure (if feasible) 

• Anticipated solids removal rate of 15 cubic feet per hour 

• Preferred location is downstream of the primary settling, upstream of the aeration basins 

• The 2 mm screen is expected to result in approximately 2 ft of headloss 

Solids removed by the 2 mm screens would be pumped to the existing primary sludge line, and 

sent with the primary sludge and wasted activated sludge to the gravity thickeners. 

Specifications for the fine screens are summarized in Table 11-2. 

Item 

Screen opening size 

Location 


Sludge production (120mgd) 


Screen reject treatment 

Wash water requirement: 

Table 11-2: Fine Screen Specifications 

Specification 

2mm 

after primary clarifiers within the channel 

15 mgd/screen 

120 cf/hr 

14 (N+1+1) 

Sludge pump, pipe connected to the existing primary sludge line 

250 gpm 

The type of screen used in this conceptual design is a dual flow band screen with 2 mm opening. 

Each screen has a design capacity of 15 mgd, and 12 screens are installed to treat up to 180 mgd. 

The flow exceeding maximum design treatment flow of 180 mgd will be diverted upstream of 

the fine screen, thus the screens will not receive the flow excess of 180 mgd. 

The screens would be installed in the channel downstream of the primary clarifier, upstream of 

the bioreactors. The 14 screens are installed in parallel in sideways (see Figure 11-1). To 

accommodate the screens, the final segment of the primary effluent channel between the primary 

sedimentation tanks and the chlorine contact tanks would be divided into 3 regions. The first 

region will retain its structure and function as overflow weir accommodating secondary bypass 

of flows in excess of 180 mgd to the chlorine contact basin. Diversion gates will be added if 

insufficient weir length remains in the first region after the second region is extended to 

accommodate the screens. The third region will retain its structure and function as the primary 

effluent pipe discharging into the aerator influent channel. 

11-2



DRAFT 

Figure 11-1: Primary Effluent Flow through 2mm Screens 


Configurations of the existing aeration tanks are presented in Section 1.0. In summary, there are 

four step-feed activated sludge reactors; each consists of four passes: A, B, C and D. Each pass 

is approximately 25 ft wide and 398 ft long. For the MBR option, each zone will be used as a 

reactor, and the total of 16 reactors will be operated in parallel. 

Each reactor is configured as a four-stage Bardenpho reactor, with the last aeration zone utilized 

as a membrane tank. A simplified schematic of the reactor is shown in Figure 11-5, and the 

proposed tank sizes are summarized in Table 11-3. Detailed descriptions of the process are 

presented below. 

Table 11-3: Aeration Tank Specifications for MBR Treatment 

Item 

Specification 


Tank dimensions per reactor (L x W x 

SWD) 

25’ W x 392.75’ L x 17.3’ SWD 

Total tank volume 2,720,000 ft 3 

Average water depth 

13 ft 

Average MLSS volume 2,042,300 ft 3 

Number of baffles 

Location of Baffles 

Number of Mixers 

Diffuser Type 

Number of Diffusers 


Deox: first 5% of tank 

Anox1: next 10% 

Aero: next 55% 

Anox 2: next 10% 

Membrane tank: last 20% 

5 per tank (80 Total) 

Fine bubble, flexible membrane discs 

(aerobic zone) 

Coarse diffusers (membrane zone) 

87,000 per oxic tank, coarse bubble 

diffusers to be supplied with the membrane 

module by the vendor 

11-3



DRAFT 

The existing reactors have an opening at the end of each pass to send mixed liquor to the next 

pass. To modify the existing aeration tank into 16 parallel four-stage Bardenpho reactors, the 

openings to the adjacent passes would be filled by concrete. Effluent launders in Pass D would 

be demolished to accommodate the membrane modules. 

The existing reactors receive Primary Effluent from the head of each zone, i.e., two of the 

Primary Effluent feeds are located on the other side of the reactor from the primary clarifiers. In 

the proposed design, all Primary Effluent feeds would be located on the primary clarifier side. 

The existing Passes A and C will require a new opening to introduce Primary Effluent to the 

reactor on the primary clarifier side. The existing influent channel would be modified to receive 

all flows on one side of the reactor by lowering the floor of the channel by 2 ft. This would also 

allow the flow from the 2 mm fine screen to the reactor influent after 2 ft headloss. 

11.3.1 Baffles 

As illustrated in Figure 11-5, each reactor consists of (1) deoxygenation (deox), (2) pre-anoxic, 

(3) aerobic, (4) post-anoxic, and (5) membrane zones. Each zone is separated by a baffle to 

prevent back-mixing of the mixed liquor. 

The new baffles will be “full width” (23 ft 6 inches wide) and submerged with flow both over 

and under the baffles. The submerged baffles will allow the froth to move along the surface from 

zone to zone without physical traps. The underflow will allow the wastewater to drain freely 

from zone to zone. This will also minimize the structural requirements and cost of the baffles. 

The baffle over/under flow split will be approximately 85/15. For cost estimating purposes, the 

baffles are assumed to be made of fiberglass panels mounted on steel beams. 

11.3.2 Mixers 

Mixers are installed in the deoxygenation, pre-anoxic, and post-anoxic zones. The aerobic zone 

and the membrane zone will not be equipped with mixers. 

Similar to Advanced Basic BNR and Full Step BNR, the MBR system will utilize hyperboloid 

mixers. The number of Invent mixers installed in each reactor is: 

• Deoxygenation zone: 1 mixer 

• Pre-anoxic zone: 2 mixers 

• Post anoxic zone: 2 mixers 

• Total = 5 mixers/reactor 

The reasoning for the number of mixers is based on the vendor’s recommendation of about 1 

mixer per each 25-40 ft of reactor length. Because the mixed liquor in the reactor is higher than 

normal activated sludge process, a conservative estimation was made for the anoxic zones. The 

specifications for the mixers are summarized in Table 11-4. 

11-4



DRAFT 

Item 

Number of Mixers 

Criteria 

Horsepower 

Mixer diameter 


Table 11-4: Mixer Specifications for MBR Treatment 

Specification 

5 per tank (80 Total) 

N determined by per-mixer coverage as suggested by the vendor 

1.5 per mixer 

Aeration is required for (1) aerobic zone, and (2) membrane tank of the reactor. For the aerobic 

zone, fine bubble membrane diffusers are used. Coarse bubble diffusers are used for the 

membrane reactors to continuously scour the membranes. BioWin modeling was used to 

estimate process air requirements. 

Air requirements for aerobic zones were estimated using BioWin modeling. Under normal 

conditions, total air requirements for aerobic zone would be approximately 92,000 scfm, which 

would be declined to approximately 84,000 scfm under cold weather conditions. Under highloading 

condition, however, the air requirements could go up to approximately 130,000 scfm. 

Design guidance specifies the following air requirements for the membrane tank, which were 

followed when feasible. Otherwise the estimates from the modeling and suggestions from the 

vendor were adopted: 

• Add sufficient number of 30,000 scfm blowers for scourge air 

• Provide 1.4 scfm (average) of scourge air per 100 ft 2 of membrane surface area 

• Blowers will be housed in existing plant blower building if sufficient footprint exists 

Based on the BioWin modeling, the air requirements under normal condition was estimated at 

approximately 185,000 scfm, which would be reduced to 167,000 sfcm under cold weather. The 

highest air requirement under high loading conditions would be approximately 233,000 scfm. 

11.3.4 Blowers 

In the proposed design, a new facility will be constructed at the site of existing final settling 

tanks. The total air requirement for the aerobic zone and membrane tank at the peak condition 

(high loading, 20°C) is approximately 360,000 scfm. The existing blowers are housed in the 

gallery on the downstream side of the activated sludge reactors, but there is not sufficient space 

to accommodate blowers for nearly four times the existing blower capacity. Specifications for 

the blowers are shown in Table 11-5. 

8 ft 

11-5



DRAFT 

Table 11-5: Blower Specifications for MBR Treatment 

Item 

Specification 

Total blower capacity 

Number of blowers 

Capacity, each blower 

Estimated amount of piping required 

400,000 scfm 

12 (10 operating, 2 stand-by) 

40,000 scfm 

(2,000 HP) 

1,000 ft of 60” pipe 

6,400 ft of 30” pipe 

Estimated dimensions of blower facility 150’ x 250’ 


Because the membranes will remove the particulate matters effectively, final clarifiers are not 

necessary for the MBR system. Existing final settling tanks would be demolished and ancillary 

facilities would be constructed at the site. Figure 11-2 shows the demolition plan for the Final 

Settling Tanks for the MBR option. 

11-6



DRAFT 

Figure 11-2: Final Settling Tank Demolition Plan for MBR Option 

11-7



DRAFT 

11.5 Return and Waste Activated Sludge System/Internal Recycle 

The recycle flow and sludge wasting systems proposed for the MBR system are shown in Table 

11-6. Each of these systems is described below. 

Table 11-6: Overview of MLSS recycling, RAS, and WAS systems for MBR Treatment 

System Location: from Location: to Numbers required 

MLSS recycling The end of aeration tank Head of the reactor 8 

Return activated sludge Membrane tank Head of aeration tank 8 

Waste activated sludge RAS line Gravity thickeners 8 

11.5.1 Mixed Liquor Recycle 

Mixed liquor will be recycled from the end of the aeration zone of each MBR at a rate of 4Q 

where Q is the design dry weather flow to each of the MBR reactors (7.5 mgd). There will be 

two dedicated submersible pumps located at the end of each aeration zone that will feed into one 

36 inch diameter pipe for the MLSS recycle. The 36 inch diameter pipe will direct the mixed 

liquor back to the deox zone of each MBR. Specifications for the MLSS recycling system are 

summarized in Table 11-7, and the plan for the MLSS recycling system is depicted in Figure 

11-4. 

Table 11-7: Specifications for MLSS recycling system for MBR Treatment 

Item 

Specification 

Location 

Capacity 

the end of the aeration zone to the head of each reactor, 

running along the side of the reactor with a supporting 

structure 

400% of DDWF 

Number of pumps 32 

Pump type 

Pump capacity 

Pipe size 

Pipe length per 

reactor 

11.5.2 Return Activated Sludge (RAS) 

Submersible 

15 mgd 

36” diameter 

Approximately 300 ft x 16 = 4,800 ft 

Unlike the conventional 4-stage Bardenpho where the RAS is introduced at the head of each 

reactor, the MBR option for the Owls Head WPCP will send the RAS flow back to the aeration 

zone because the dissolved oxygen in the membrane tank is high (set to 4 mg/L) and would 

likely be detrimental to the deox zone in the head of the reactor. The RAS system for each 

reactor will be designed to handle up to two times the design dry weather flow (2Q) for each 

11-8



DRAFT 

reactor (7.5 mgd). Each RAS system will handle the mixed liquor from two reactors, and the 

return line will split the flow into two reactors. Part of the RAS flow will also be wasted (see 

Section 11.5.3 for a description of the waste activated sludge (WAS) system). 

The existing aeration effluent channel will be extended to connect to the end of each MBR 

system. An opening and sluice gate will be constructed in the end of each reactor and will 

connect each reactor to the effluent channel. The effluent channel will convey flows to a 

common RAS wet well located where the existing splitter box for the final settling tanks is 

located. 

The RAS pumps will be placed in a new facility to be constructed adjacent to the proposed 

membrane tanks, where the current final settling tanks are located. The RAS pumps will pull 

flows from the RAS wet well and direct them back to the head of the aeration zones, as described 

above. Specifications for the RAS system are summarized in Table 11-8, and the plan is 

depicted in Figure 11-5. 

Table 11-8: Specifications for the RAS system for MBR Treatment 

Item 

Specification 

Location 

Capacity 

the end of the membrane tanks to the head of the aeration tanks and a 

RAS wet well and pump station located above the splitter box and 

existing final settling tanks, extension of the existing aeration effluent 

channel and piping placed above the MBRs with supporting structures 

200% of DDWF 

Number of pumps 8 

Pump type 

Pump capacity 

Pipe size 

Pipe length 

11.5.3 Waste Activated Sludge (WAS) 

Vertical centrifugal variable speed pump 

30 mgd 

36” diameter 

Approximately 300 ft x 8 = 2,400 ft 

Waste activated sludge will be drawn from each of the eight RAS lines, as depicted in Figure 

11-1. These eight WAS lines will be combined into one line, where a centrifugal, horizontalmounted 

pump will send the sludge to the gravity thickeners. An additional pump will be 

installed as a stand-by to meet the N+1 redundancy. Specifications for the WAS system are 

summarized in Table 11-9. 

11-9



DRAFT 

Table 11-9: Specifications for WAS systems for MBR Treatment 

Item 

Specification 

Capacity of WAS System 

Number of WAS Pumps 

Pump type 

Capacity, each Pump 


15% of DDWF 

3 (2 operating, 1 stand-by) 

Centrifugal/horizontal mounted/variable speed 

9 mgd 

Three methods of froth control are planned for Owls Head WPCP under the MBR level of 

treatment: 

1. Froth hoods (surface chlorination) 

2. RAS chlorination 

3. Surface wasting 


One froth control hood will be installed near the end of the aerobic zone at each reactor. Detail 

of the hood was described in Section 6.6.1, and specifications for the MBR option are shown in 

Table 11-10. 

Table 11-10: Froth Control Hoods Specifications for MBR Treatment 

Item 

Specification 

Number of hoods 

Locations of hoods 



Downstream end of aerobic zone 

A return activated sludge chlorination system would be installed for the returned mixed liquor 

from the membrane tank. The MLSS recycling system will not be equipped with the 

chlorination system. When in operation, sodium hypochlorite solution would be added to the 

wet well where RAS is collected, before it is pumped back to the head of the aeration tanks. 

Specifications for the MBR option are shown in Table 11-11. 

Table 11-11: RAS Chlorination System Specifications for MBR Treatment 

Item 

Specification 

Chlorination Requirement per 1000 lb 

MLSS 

Estimate of additional piping required to 

chlorinate RAS 

3 to 5 lbs per day 

From sodium hypochlorite storage tank to the wet 

well: approximately 500 ft 

11-10



DRAFT 


Surface wasting for the MBR level of treatment is the same as with the Advanced Basic BNR 

level of treatment and is detailed in Section 6.6.3. 



The reactors will be equipped with alkalinity addition at the head of each reactor. Sodium 

hydroxide would be added to screened primary effluent in the conduit for the reactor influent 

using a metering pump. According to the design guidance, sodium hydroxide should be added to 

achieve 50 mg/L alkalinity in the treated effluent, assuming 100% nitrification and no credit 

from MLSS recycling or RAS flows which would contribute to alkalinity due to denitrification. 

As described in Section 7.7.1, the sodium hydroxide requirement was estimated based on 

approximate TKN loading of 24,000 lb/d, resulted in daily flow of approximately 5,460 gallons 

of 25% solution per day (or 3.8 gal/min). Specifications for the sodium hydroxide supply are 

shown in Table 11-12. Caustic will be added downstream of the 2 mm screen at the entrance to 

the reactor influent conduit. 

Table 11-12: Sodium Hydroxide Supply Specifications for MBR Treatment 

Item 

Specification 

Target residual alkalinity 

Design daily loading 

1.3 mmol/L 

11,336 lb/d as NaOH 

Stock solution concentration 25% 

Required flow rate 

Type of pumps 

Pump capacity 


3.8 gal/min 

Metering 

8 gal/min 

2 (1 operational, 1 standby) 

Two 15,000 gallon tanks will provide a little more than a 5-day supply. These two tanks will be 

located in a new Sodium Hydroxide Storage Building, located to the east of the Aeration Tanks 

and just south of the Grit and Scum Building. The new building will be single-story and have a 

footprint of approximately 60 feet by 120 feet, or 7,200 sq. ft. Caustic storage and piping 

requirements are summarized in Table 11-13. 

Table 11-13: Sodium Hydroxide Storage and Piping Requirements for MBR Treatment 

Item 

Specifications 

Number of Days of Storage Required 5 

Number of tanks required 2 

Tank volume 

Estimate of Piping Required 

15,000 gal/tank 

400 ft 

11-11



DRAFT 

11.7.2 Carbon 

Supplemental carbon is added to post-anaerobic zone in each reactor to enhance denitrification. 

BioWin version 2.2 was used to estimate methanol feed rate. It was estimated that under normal 

condition, approximately 2,100 gal/d of 100 percent methanol would be required to maintain the 

TN treatment goal. The requirement would be 5,600 gal/d under the peak loading condition. 

This dosing is translated to the methanol requirement of up to 250 mL/min for each tank. 

Specifications for the supplemental carbon system are shown in Table 11-14. 

Table 11-14: Supplemental Carbon System Specifications for MBR Treatment 

Item 

Specification 

Carbon source 

Concentration 

Requirement (normal/peak condition) 

Methanol peak flow rate (per tank) 

Type of pumps 

Pump capacity 


Methanol 

100% (1,188,000 mg-COD/L) 

2,100/5,600 gal/d 

243 mL/min per tank 

Metering 

0.5 gal/min 

32 (16 operational, 16 standby) 

Methanol will be stored underground in a carbon steel, double-walled tank with an intermediate 

sump and leak detection systems. The storage tank will be constructed at the existing final 

settling tank area after demolition of the settling tanks. 

According to the BioWin version 2.2 modeling, the daily methanol requirement under normal 

conditions would be 2,100 gal/d, with a peak flow of 5,600 gal/d. In accordance of the design 

guideline, 5 days of storage is required. Considering normal carbon requirement of 10,500 

gal/5days and peak demand of 28,000 gal/5days, 24,000 gal is deemed sufficient for the total 

storage tank size (this size provides N+1 redundancy under normal condition). Specifications for 

supplemental carbon storage are shown in Table 11-15. 

Table 11-15: Supplemental Carbon Storage and Piping Requirements for MBR Treatment 

Item 

Specification 

Carbon source 

Type of the tank 

Methanol 

Underground 

Number of tanks required 2 

Volume required 

Estimate of piping required 

12,000 gal/tank 

Number of days of storage required 5 


11-12



DRAFT 

A description of the Sodium Hypochlorite addition design needed for the Membrane Bioreactor 

level of technology in Sections 11.6.1 and 11.6.2. 


No polymer is needed for the Membrane Bioreactor level of technology. 












Membrane modules are installed in the final aeration tank of the 4-stage Bardenpho 

configuration. In accordance with the design guidance, following specifications were assumed to 

determine the required tank volume and air requirements: 

• MBR modules will be placed in the aeration tanks 

• Assume membranes of the hollow fiber configuration (Zenon) 

• Assume a nominal pore size of 0.04 µm 

• Assume 340 ft 2 of contact surface area per cassette 

• Assume 48 cassettes per MBR module 

• Assume an MBR module has dimensions of 69”×83”×100” 

• Design to an average flux rate of 10-12 gallons per sq-ft per day and a peak flux rate of 28 

gal/d/ft 2 for 2 hours only; 20-24 gal/d/ft 2 for up to 24 hours 

• Membrane cleaning solution to be sent to head of plant or to a storage tank for equalization 

Each membrane module consists of hollow fiber ultrafiltration membranes mounted in cassettes. 

Specifications of the membrane module are shown in Table 11-16. 

11-13



DRAFT 

Table 11-16: Membrane Module Specifications for MBR Treatment 

Item 

Specification 

Contact surface area 

340 ft 2 /cassette 

Number of cassettes per module 48 

Design average flux rate 11.5 gal/d/sf 2 

The membrane tank in each of 16 parallel reactors will hold 40 membrane modules, resulting in 

a total of 640 modules for the entire system. Membrane tank specifications are shown in Table 

11-17. 

Table 11-17: Membrane Tank Specifications for MBR Treatment 

Item 

Specification 

Tank volume 

3.5 Mgal 

Tank surface area 36,000 ft 2 

Tank water depth 

Number of modules 

13 ft 

40 per reactor, 640 total 

Size of module 69” × 83” × 100” 

Diffuser type 

Number of diffusers 

Coarse bubble 

2,500 per tank 

Permeate from each membrane module would be collected into collection manifold by vacuum 

pumps. The collection manifold from all modules are connected to one main collection pipe, 

where a vacuum is applied to collect permeate. Each vacuum pump has a capacity of 15 mgd. 

Automatic valves would be installed to the collection manifold, so that the membrane could be 

operated intermittently to minimize biological fouling. Because there would be 16 MBR tanks 

operated in parallel, and at average flow, at least one or two reactor could be taken off the 

operation for maintenance; no additional pump would be installed for redundancy. 

The membranes need to be cleaned periodically in situ with cleaning solution. Sodium 

hypochlorite solution would be used for the regular membrane cleaning. The cleaning process 

also involves filter backwash with the permeate. The permeate pump and valves are installed to 

allow filter backwash. The vendor’s recommendations would be followed for the detailed 

configurations of the cleaning system. 

For regular cleaning of membranes, sodium hypochlorite will be used. The cleaning solution 

provided by the vendor would also be used for persistent fouling. Storage tank for the cleaning 

solution provided by the vendor would be constructed adjacent to the pump/blower housing, as 

indicated in Figure 11-3. The size would be specified by the vendor. 

The sodium hypochlorite used for cleaning will be distributed from the storage tank to the head 

of membrane tanks. The cleaning solution would be distributed to each reactor independently. 

During the cleaning, the cleaned reactor is temporarily taken off from the regular operation. 

11-14



DRAFT 

For maintenance and replacement of membrane modules, a crane supporting structure will be 

constructed on top of the membrane zones. The structure will have following specifications: 

• The structure is to be built on the membrane tanks 

• The structure covers the entire 78ft × 400ft area where membranes are installed 

• The crane mounted on a monorail is capable of lifting one module at a time 

• The crane can be moved across the covered area 


Monitoring equipments for the system control would be the essential part of the MBR system. A 

summary of required instrumentations are shown in Table 11-18. 

Table 11-18: Instrumentation and Control for MBR Treatment 


Location(s) 


Control 

Flow meter 

DO Probes 

Plant influent 

Primary effluent 

RAS 

WAS 

Surface wasting 

Primary sludge 

Secondary by-pass 

(overflow) 

Plant effluent 

Methanol 

Sodium hydroxide 

Aeration tanks 

Membrane tanks 


1 in each tank, 32 total 

pH Meter/Locations Aeration tanks 1 in each tank,16 probes total 

MBR, membrane module 

control 


Membrane tanks 

16, to be centralized 

The site plan with locations of MBR upgrades is shown in Figure 11-3. A simplified schematic 

flow diagram proposed for the modification at the Owls Head WPCP is shown in Figure 11-4, 

and the proposed design plan is presented in Figure 11-5. 

11-15



DRAFT 

Figure 11-3: Site Plan with Locations of MBR Upgrades 

11-16



DRAFT 

Figure 11-4: Schematic flow diagram of the MBR system 

11-17



DRAFT 

Figure 0-1: MBR Aeration Tank Part Plan Detail 

11-18



DRAFT 



Table 12-1: Treatment Goals for Nine Treatment Considerations 

TSS 

CBOD 5 

Alternative 

mg/L 

mg/L 

TN 

mg/L 

1. Base Case (85% removal) (85% removal) 24-30 

2. Existing Conditions 11-16 10-15 24-30 

3. Existing Conditions with Solids 

Filtration 

4. Existing Conditions with 


5. Advanced Basic BNR 

6. Full Step BNR 12-15 

4-5 3-5 24-30 

~1 1-2 24-30 

12-15 10-15 

(60-70 mg/L COD) 

10-15 

(60-70 mg/L COD) 

10-12 

7. Full Step BNR with Solids Filtration 4-5 3-5 6-10 

8. Full Step BNR with 


9. Full Step BNR with Denitrification 

Filters 

6-10 

~1 1-2 6-10 

4-5 

10. MBR ~1 

3-5 

(60-70 mg/L COD) 

1-2 

(25-30 mg/L COD) 

Table 12-2 provides a summary of anticipated capital construction costs for each level of 

technology at the Owls Head WPCP. The project executive summary provides details into the 

contingencies used, key cost assumptions, and overall approach to cost estimation. The detailed 

cost estimates for nine technologies at each of the four WPCPs in question can be found in their 

entirety after the four plant-specific conceptual design reports and drawing sets. 

4-5 

3-4 

12-19



DRAFT 










Full Step BNR with Denitrification Filtration $1,051 

Full Step BNR with Microfiltration/Ultrafiltration $1,096 


12-20



DRAFT 

APPENDIX A 

Major Equipment Lists 

I



DRAFT 

OWLS HEAD WPCP HEP MAJOR EQUIPMENT LIST 

Plant Average Design Capacity = 120 mgd 

Maximum Plant Capacity = 240 mgd 

Secondary System Maximum Capacity = 180 mgd 

Process Category 

Primary Tanks – 

Grease/Oil Removal 

Mechanisms 

Type of Tanks 

Number of Tanks 

Dimensions 

(W x L x D) 

Surface Area 

Total Overflow Rate 

(at 120 mgd) 

Provide equal and 

uniform flow 

distribution to each 

tank 

Provide Removal of 

Grease and Floatables 

Maximize Solids 

Removal Within 

Existing Tankage 

Aeration Tank 

Influent Flow 

Distribution and 

Splitting 

Balance Flow to Each 

Aeration Tank/Pass 

Control Flow with 

Good Accuracy Over 

the Anticipated Flow 

Existing 

Conditions 

Rectangular with 

chain and flight 

mechanism 

Existing 

Conditions with 




mechanism 

Existing 






mechanism 


Step Feed BNR 



mechanism 

Full Step Feed 

BNR 



mechanism 


BNR with 

Filtration 



mechanism 


BNR with Denit 

Filtration 



mechanism 

MBR 



mechanism 

4 4 4 4 4 4 4 4 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

63’ x 242.7’ x 

13’ 

15,290 ft 2 15,290 ft 2 15,290 ft 2 15,290 ft 2 15,290 ft 2 15,290 ft 2 15,290 ft 2 15,290 ft 2 

1,962 gal/ ft 2 /day 1,962 gal/ ft 2 /day 1,962 gal/ ft 2 /day 1,962 gal/ ft 2 /day 

1,962 gal/ 

ft 2 /day` 

1,962 gal/ ft 2 /day 1,962 gal/ ft 2 /day 1,962 gal/ ft 2 /day 

Yes Yes Yes Yes Yes Yes Yes Yes 

Exists Yes Yes Yes Yes Yes Yes Yes 



No No No No Yes Yes Yes Yes 

II



DRAFT 


Ranges 

Existing 

Conditions 

Existing 



Existing 





Step Feed BNR 


BNR 


BNR with 

Filtration 



Filtration 

MBR 

Provide Automated 

Response to Excess 

Storm Flows in Pass D 

Fine Screens 

Pre-treatment 

Fine Screens Design 

Capacity 

Fine Screens Sludge 

production (120mgd) 



No No No 

Pass D influent 

gate will be 

provided with 

electric actuators 

for a manual 

response to 

excess storm 

flow 

Yes Yes Yes 

No No No No No No No 

8 parallel 

Bardenpho 

reactors to 

receive only up 

to 180 mgd: the 

excess flow will 

be diverted to 

disinfection 

following 

primary settling, 

before 2mm 

screen 

Yes 

2mm fine screen 

after primary 

settling 

15 mgd/screen 

120 cf/hr 

Sludge pump, 

pipe to be 

connected to 

primary sludge 

line (primary 

sludge line may 

need expansion) 

14 (N+1+1) 


4 4 4 4 4 4 4 16 

Tank Dimensions per 

Pass (L x W x SWD) 

100’ W x 392.75’ 

L x 17.3’ D 

100’ W x 392.75’ 

L x 17.3’ D 

100’ W x 392.75’ 

L x 17.3’ D 

100’ W x 392.75’ 

L x 17.3’ D 

100’ W x 392.75’ 

L x 17.3’ D 

100’ W x 392.75’ 

L x 17.3’ D 

100’ W x 392.75’ 

L x 17.3’ D 

4 stage 

Bardenpho 

25’ W x 392.75’ 

L x 17.3’ D 

Total Volume 2,720,000 ft 3 2,720,000 ft 3 2,720,000 ft 3 2,720,000 ft 3 2,720,000 ft 3 2,720,000 ft 3 2,720,000 ft 3 2,720,000 ft 3 

III



DRAFT 


Existing 

Conditions 

Existing 



Existing 





Step Feed BNR 


BNR 


BNR with 

Filtration 



Filtration 

MBR 

New Tank Needed? 

N/A 

No No No No No No No 

Estimated New Tank 

Dimensions N/A N/A N/A N/A N/A N/A N/A N/A 

Number of Baffles 

N/A N/A N/A 

Location of Baffles N/A N/A N/A 

Number of Mixers N/A N/A N/A 

Diffuser Type 

Number of Diffusers 

Fine bubble, 9” 

ceramic discs 

28,000 

Plus 7,000 

Blanks 

N/A 

N/A 

28,000 28,000 

11 per tank (44 

Total) 

Pass A: 1/6,1/3 

and 5% between 

oxic/pre-anoxic 

zone 

Pass B: 1/6,1/3 



zone 

Pass C: 1/6,1/3 



zone 

Pass D: 1/3 and 

1/2 between 


zone 


Total) 


membrane discs 


Total) 

Pass A: 1/6,1/3 



zone 

Pass B: 1/6,1/3 



zone 

Pass C: 1/6,1/3 



zone 


1/2 between 


zone 


Total) 




Total) 

Pass A: 1/6,1/3 



zone 

Pass B: 1/6,1/3 



zone 

Pass C: 1/6,1/3 



zone 


1/2 between 


zone 


Total) 




Total) 

Pass A: 1/6,1/3 



zone 

Pass B: 1/6,1/3 



zone 

Pass C: 1/6,1/3 



zone 


1/2 between 


zone 


Total) 



35,500 42,700 42,700 42,700 


total) 

Deox: 5% of tank 

Anox1: next 10% 

Aero: next 72% 

Anox 2: next 

10% 

Membrane tank: 

last 3% 


Total) 

Fine bubble, 

flexible 


Coarse diffusers 

87,000 

per oxic tank, 

Membrane tank 

Diffuser type N/A N/A N/A N/A N/A N/A N/A coarse bubble 

Number of diffusers N/A N/A N/A N/A N/A N/A N/A 2,500 per tank 

IV



DRAFT 


Existing 

Conditions 

Existing 



Existing 





Step Feed BNR 


BNR 


BNR with 

Filtration 



Filtration 

Process Air System 

Total Blower Capacity 81,000 scfm 81,000 scfm 81,000 scfm 81,000 scfm 81,000 scfm 81,000 scfm 81,000 scfm 400,000 scfm 

Air Requirement 53,000 scfm 79,000 scfm 79,000 scfm 79,000 scfm 

233,000 MBR 

(scourge) 

126,500 

(aeration) 

Number of Blowers 

Capacity, Each Blower 

4 

(3 operating, 1 

stand-by) 

4 


stand-by) 

4 


stand-by) 

4 


stand-by) 

4 


stand-by) 

4 


stand-by) 

4 


stand-by) 

27,000 scfm 27,000 scfm 27,000 scfm 27,000 scfm 27,000 scfm 27,000 scfm 27,000 scfm 

Estimated Amount of 

New Piping Required N/A N/A N/A N/A N/A N/A N/A 

New Facility 

Required? 

Estimated Dimensions 

of New Facility 

Final Settling Tank 

Improvements – 

Optimize Settling to 

Allow for Higher 

Solids Loading Rates 

Type of Tanks 

MBR 

12 


stand-by) 

40,000 scfm 

(2,000 HP) 

1,000 ft of 60” 

pipe 

6,400 ft of 30” 

pipe 

N/A No No No No No No Yes 

N/A N/A N/A N/A N/A N/A N/A 150’ x 250’ 



mechanism 



mechanism 



mechanism 



mechanism 



mechanism 



mechanism 



mechanism 

FINAL 

SETTLING 

TANKS TO BE 

DEMOLISHED 

Number of Tanks 16 16 16 16 16 N/A 

Dimensions 

(W x L x D) 

N/A 

Total Overflow Rate 

(at 180 mgd) 

Additional Final 

Tank(s) Required? 

Volume? 

Equally distribute flow 

to each Final Settling 

170.5’ x 55’ x 

12.25’ 

170.5’ x 55’ x 

12.25’ 

170.5’ x 55’ x 

12.25’ 

170.5’ x 55’ x 

12.25’ 

170.5’ x 55’ x 

12.25’ 

170.5’ x 55’ x 

12.25’ 

170.5’ x 55’ x 

12.25’ 

1200 gal/ ft 2 /day 1200 gal/ ft 2 /day 1200 gal/ ft 2 /day 1200 gal/ ft 2 /day 1200 gal/ ft 2 /day 1200 gal/ ft 2 /day 1200 gal/ ft 2 /day N/A 

No No No No No No No N/A 

No No No No 

Improvement of 

flow distribution 





N/A 

N/A 

V



DRAFT 


Existing 

Conditions 

Existing 



Existing 





Step Feed BNR 


BNR 


BNR with 

Filtration 



Filtration 

Tank may be necessary may be necessary may be necessary 

Evaluate sludge 

removal system for 

increased solids 

withdrawal and RAS 

rates 

Provide automated 

scum removal 

No No No No Yes Yes Yes N/A 

No No No No Yes Yes Yes N/A 

RAS System 

(membrane tank 

to aeration tank) 

200% of DDWF 

Capacity of RAS 

RAS 

50 % of DDWF 50 % of DDWF 50 % of DDWF 50 % of DDWF 100 % of DDWF 100 % of DDWF 100 % of DDWF 

System 

400% of DDWF 

ML 

New Pumps Required? No No No No Yes Yes Yes Yes 

Number of RAS 

Pumps 

2 operating 

2 stand-by 

2 operating 

2 stand-by 

2 operating 

2 stand-by 

2 operating 

2 stand-by 

3 operating 

1 stand-by 

3 operating 

1 stand-by 

3 operating 

1 stand-by 

RAS (8 operating 

1 stand-by) 

ML (16 operating 

1 stand-by) 

Capacity, Each Pump 


New RAS Piping 

Required 


Required? 



Centrifugal / 

vertically 

mounted / 

Variable Speed: 

30 mgd 

Centrifugal / 

vertically 

mounted / 


30 mgd 

Centrifugal / 

vertically 

mounted / 


30 mgd 

Centrifugal / 

vertically 

mounted / 


30 mgd 

N/A N/A N/A N/A 

Centrifugal / 

vertically 

mounted / 


40 mgd 

Centrifugal / 

vertically 

mounted / 


40 mgd 

Centrifugal / 

vertically 

mounted / 


40 mgd 

MBR 

Centrifugal / 

vertically 

mounted / 


30 mgd 

No No No No No No No Yes 

N/A N/A N/A N/A N/A N/A N/A 150’ x 250’ 

WAS System 

Capacity of WAS 

System 

Number of WAS 

Pumps 

15% of DDWF 15% of DDWF 15% of DDWF 15% of DDWF 15% of DDWF 15% of DDWF 15% of DDWF 15% of DDWF 

3 – 2 operating 

1 stand-by 


1 stand-by 


1 stand-by 


1 stand-by 


1 stand-by 


1 stand-by 


1 stand-by 


1 stand-by 

VI



DRAFT 


Capacity, Each Pump 


New WAS Piping 

Required 


Required? 



Froth Control 


Number of Hoods 

Locations of Hoods 

Chlorination 

Requirement (13% 

solution) 


Estimate of Additional 

Piping Required to 

Chlorinate RAS 

Existing 

Conditions 

Centrifugal / 

horizontal 

mounted / 


9 mgd 

Existing 



Centrifugal / 

horizontal 

mounted / 


9 mgd 

Existing 




Centrifugal / 

horizontal 

mounted / 


9 mgd 


Step Feed BNR 

Centrifugal / 

horizontal 

mounted / 


9 mgd 


BNR 

Centrifugal / 

horizontal 

mounted / 


9 mgd 


BNR with 

Filtration 

Centrifugal / 

horizontal 

mounted / 


9 mgd 



Filtration 

Centrifugal / 

horizontal 

mounted / 


9 mgd 

MBR 

Centrifugal / 

horizontal 

mounted / 


9 mgd 

N/A N/A N/A N/A N/A N/A N/A N/A 

No No No No No No No No 

N/A N/A N/A N/A N/A N/A N/A N/A 

123 nozzles per 

pass w NaOCl 

N/A 


pass w NaOCl 

N/A 


pass w NaOCl 

N/A 

4 per tank 

(16 total) 

One in oxic zone, 

one in anoxic 

zone in Passes A 

and B 

4 per tank 

(16 total) 


one in anoxic 


and B 

4 per tank 

(16 total) 


one in anoxic 


and B 

4 per tank 

(16 total) 


one in anoxic 


and B 


total) 

Locations TBD 

N/A N/A N/A 5.1 gpm max 5.1 gpm max 5.1 gpm max 5.1 gpm max 5.1 gpm max 

N/A 

Chlorination 

Requirement 

N/A 

N/A 

N/A 

3 to 5 lbs of 

chlorine per day 

per 1000 lbs of 

MLSS 

3 to 5 lbs of 



MLSS 

3 to 5 lbs of 



MLSS 

3 to 5 lbs of 



MLSS 

3 to 5 lbs of 



MLSS 

Polymer System 

(Feed to FSTs) 

New Facilities 

Needed? 

N/A N/A N/A N/A Yes Yes Yes N/A 

VII



DRAFT 


Existing 

Conditions 

Existing 



Existing 





Step Feed BNR 

New Equipment N/A N/A N/A N/A 


New Piping Required 

Volume of Tankage 

Required 




BNR 

Yes, 3 Polymer 

blending units 

and 2 storage 

tanks 

800 ft of 3-inch 

pipe 

4,000 gallons 

2 tanks 


BNR with 

Filtration 



and 2 storage 

tanks 


pipe 

4,000 gallons 

2 tanks 



Filtration 



and 2 storage 

tanks 


pipe 

4,000 gallons 

2 tanks 

MBR 

N/A 

N/A 

N/A 



Mechanism 

Additional Facilities 

Required? 

No No No Yes Yes Yes Yes Yes 

N/A N/A N/A Yes Yes Yes Yes Yes 

TBD 

TBD 


of Additional 

Infrastructure for 

Surface Wasting (If 

Needed) 

N/A N/A N/A TBD 

TBD 

TBD 


Piping Required 

Chlorination 

Required? Amount/day 

required. 

N/A N/A N/A 


pipe 


pipe 


pipe 


pipe 


pipe 


Filters 

Number of Filters N/A 8 32 N/A N/A 8 8 N/A 

Additional Facilities 

N/A Yes Yes N/A N/A Yes Yes N/A 

Required? 




Piping, etc. Required 

Size of Pump Station 

Required? 

N/A 

815’ x 95’ 

(off site) 

540’ x 120’ 

(off-site) 

N/A 

N/A 

815’ x 95’ 

(off site) 

340’ x 105’ 

(off site) 

N/A Yes Yes N/A N/A Yes Yes N/A 

N/A 

30 mgd (6 

operating, 2 

30 mgd (6 

operating, 2 

N/A 

N/A 

30 mgd (6 

operating, 2 

30 mgd (6 

operating, 2 

N/A 

N/A 

VIII



DRAFT 


Existing 

Conditions 

Existing 



stand-by) 

75’ x 45’ 

Existing 




stand-by) 

75’ x 45’ 


Step Feed BNR 


BNR 


BNR with 

Filtration 

stand-by) 

75’ x 45’ 



Filtration 

stand-by) 

75’ x 45’ 

MBR 

Chemical Systems 

Sodium Hypochlorite 

for Froth Control/ 


Number of Tanks 3 3 3 3 3 3 3 3 

Storage Volume, Total 7,835 gall/tank 7,835 gall/tank 7,835 gall/tank 7,835 gall/tank 7,835 gall/tank 7,835 gall/tank 7,835 gall/tank 7,835 gall/tank 

Additional Tank 

Required? 

Number of Additional 

Tanks Required 

Additional Volume 

Required 


Piping Required 

Number of Days of 

Storage Provided 

Sodium Hydroxide 

Additional Tank 

Required? 

N/A No No Yes Yes Yes Yes Yes 

N/A N/A N/A 3 3 3 3 3 

N/A N/A N/A 9,000 gal/tank 9,000 gal/tank 9,000 gal/tank 9,000 gal/tank 9,000 gal/tank 

N/A 

14 days 14 days 14 days 4-5 days 4-5 days 4-5 days 4-5 days 4-5 days 

N/A No No Yes Yes Yes Yes Yes 


Required 

N/A N/A N/A 3 3 3 3 3 

Volume Required N/A N/A N/A 9,000 gall/tank 9,000 gall/tank 9,000 gall/tank 9,000 gall/tank 9,000 gall/tank 

Estimate of Piping 

Required 

N/A 


Storage Required 

N/A N/A N/A 4-5 days 4-5 days 4-5 days 4-5 days 4-5 days 

Carbon Source 

Selected Source? No No No No Yes Yes Yes Yes 


Required 

N/A N/A N/A N/A 2 2 3 2 

Volume Required N/A N/A N/A N/A 18,000 gal/tank 18,000 gal/tank 18,000 gal/tank 18,000 gal/tank 

IX



DRAFT 


Estimate of Piping 

Required 


Storage Required 

Existing 

Conditions 

N/A 

Existing 



Existing 





Step Feed BNR 

N/A 


BNR 


BNR with 

Filtration 



Filtration 

N/A N/A N/A N/A 7 7 7 7 

MBR 


Control 

DO Probes/Locations 

Alkalinity 

Meter/Locations 

Yes, one portable 

probe 


probe 


probe 

Yes, 8 probes 

total, 2 in Passes 

B and C of each 

tank 

Yes, 32 probes 

total, 2 in each 

pass of each 

Aeration Tank 



pass of each 

Aeration Tank 



pass of each 

Aeration Tank 



pass of each tank 


pH Meter/Locations No No No No 

Ammonia 

Probes/Locations 

Nitrate 

Probes/Locations 

Anaerobic Digesters 

Digester Modifications 

for Froth Control? 

Yes, 4 probes 

total, 1 probe in 

Pass D of each 

Aeration Tank 

Yes, 4 probes 



Aeration Tank 

Yes, 4 probes 



Aeration Tank 

Yes, 4 probes 



Aeration Tank 



Flow Metering 

Plant Influent Meter 

Provided? 

Primary Effluent Flow 

Meter Provided? 

Flow Meter to each 

Aeration Tank 

Provided? 

Flow to Meter to each 

Aeration Tank Pass 

Provided? 

Flow to Meter each 

Secondary Clarifier 


No No No No No No No Yes 




X



DRAFT 


Provided? 

RAS Flow Meter 

Provided? 

WAS Flow Meter 

Provided? 

Surface Wasting Flow 


Primary Sludge Flow 


Gravity Thickener 

Overflow Meter 

Provided? 

Secondary ByPass 

Flow Meter Provided? 

Plant Effluent Flow 


Existing 

Conditions 

Existing 



Existing 





Step Feed BNR 


BNR 


BNR with 

Filtration 



Filtration 







No No No No Yes Yes Yes Yes 

MBR 

XI


Conceptual Cost Estimate 

June 2007 

DRAFT

Harbor Estuary Plan 

Conceptual Design Evaluation of Advanced Wastewater Treatment Alternatives 

North River, Owls Head, Red Hook & Port Richmond WPCP 

Construction Cost Summary - no land acquisition costs 

Date: April, 2007 

Water Pollution Control 

Plant 


Full Step BNR 






Microfiltration 



Membrane 

Bioreactor 

North River $ 433,668,132 $ 499,198,529 $ 1,334,306,591 $ 1,501,014,921 $ 1,568,166,081 $ 586,725,210 $ 812,535,784 $ 3,209,501,702 

Owls Head $ 256,600,862 $ 318,868,815 $ 931,119,283 $ 1,050,599,882 $ 1,095,940,198 $ 485,334,212 $ 650,155,127 $ 2,344,996,703 

Red Hook $ 225,465,027 $ 296,173,869 $ 632,038,946 $ 681,648,113 $ 704,171,402 $ 306,823,202 $ 378,967,622 $ 1,572,477,663 

Port Richmond $ 215,691,247 $ 269,630,877 $ 500,535,647 $ 577,698,728 $ 601,108,401 $ 273,782,392 $ 374,355,147 $ 1,398,415,594 

Subtotal: $ 1,131,425,268 $ 1,383,872,092 $ 3,398,000,467 $ 3,810,961,645 $ 3,969,386,082 $ 1,652,665,015 $ 2,216,013,680 $ 8,525,391,663

Water 

Pollution 

Control 

Plant 

Advanced 

Basic BNR 

Full Step 

BNR 

Full Step 

BNR with 

Solids 

Filtration 

Full Step Full Step 

BNR with BNR with 

Denitrificatio Microfiltrati 

n 

on 

Membrane 

Bioreactor 

136.7 North River $ 3.17 $ 3.65 $ 9.76 $ 10.98 $ 11.47 $ 23.48 

104.6 Owls Head $ 2.45 $ 3.05 $ 8.90 $ 10.04 $ 10.48 $ 22.42 

32.9 Red Hook $ 6.85 $ 9.00 $ 19.21 $ 20.72 $ 21.40 $ 47.80 

38.1 

Port 

Richmond 

$ 5.66 $ 7.08 $ 13.14 $ 15.16 $ 15.78 $ 36.70 

Average: $ 4.53 $ 5.69 $ 12.75 $ 14.23 $ 14.78 $ 32.60




Estimated Cost of Land Acquisition 



Plant 


BNR 

Full Step BNR 









Membrane 

Bioreactor 

North River $ - $ - $ 396,332,724 $ 396,332,724 $ 396,332,724 $ 396,332,724 $ 396,332,724 $ 452,951,685 

Owls Head $ - $ - $ 265,702,223 $ 265,702,223 $ 265,702,223 $ 265,702,223 $ 265,702,223 $ 303,659,683 

Red Hook $ - $ - $ 135,071,722 $ 135,071,722 $ 135,071,722 $ 135,071,722 $ 135,071,722 $ 154,367,682 

Port Richmond $ - $ - $ - $ 69,756,471 $ 69,756,471 $ - $ 69,756,471 $ - 

Subtotal: $ - $ - $ 797,106,668 $ 866,863,139 $ 866,863,139 $ 797,106,668 $ 866,863,139 $ 910,979,050




Construction Cost Summary 



Plant 


Full Step BNR 









Membrane 

Bioreactor 

North River $ 433,668,132 $ 499,198,529 $ 1,730,639,315 $ 1,897,347,645 $ 1,964,498,805 $ 983,057,934 $ 1,208,868,508 $ 3,662,453,386 

Owls Head $ 256,600,862 $ 318,868,815 $ 1,196,821,506 $ 1,316,302,105 $ 1,361,642,421 $ 751,036,434 $ 915,857,349 $ 2,648,656,386 

Red Hook $ 225,465,027 $ 296,173,869 $ 767,110,667 $ 816,719,834 $ 839,243,123 $ 441,894,923 $ 514,039,344 $ 1,726,845,345 

Port Richmond $ 215,691,247 $ 269,630,877 $ 500,535,647 $ 647,455,199 $ 670,864,872 $ 273,782,392 $ 444,111,618 $ 1,398,415,594 

Subtotal: $ 1,131,425,268 $ 1,383,872,092 $ 4,195,107,136 $ 4,677,824,784 $ 4,836,249,221 $ 2,449,771,683 $ 3,082,876,819 $ 9,436,370,712



North River WPCP 

Summary 


Item 

Description 


BNR 

Full Step BNR 

Full Step BNR 

with Solids 

Filtration 

Full Step BNR 

with 


Full Step BNR 

with 




Membrane 

Bioreactor 

1 General Requirements $ 10,757,740 $ 12,741,380 $ 19,042,300 $ 19,292,300 $ 19,392,300 $ 19,042,300 $ 19,392,300 $ 23,213,300 

2 Demolition and Site Construction $ 1,649,013 $ 1,649,013 $ 52,462,021 $ 52,462,021 $ 52,462,021 $ 52,462,021 $ 52,462,021 $ 52,462,021 

3 Aeration Tank Modifications, Baffles and Mixers $ 16,394,634 $ 16,394,634 $ 16,536,585 $ 16,536,585 $ 16,536,585 $ - $ - $ 16,536,585 

4 Process Air System $ 22,007,500 $ 22,547,500 $ 53,510,909 $ 53,510,909 $ 53,510,909 $ - $ - $ 53,510,909 

5 RAS and WAS Pumping System $ - $ 1,940,160 $ 2,028,320 $ 2,909,920 $ 2,909,920 $ - $ - $ 2,909,920 

6 Aeration Tank Froth Hood System $ 1,594,800 $ 1,594,800 $ 1,250,840 $ 1,250,840 $ 1,250,840 $ - $ - $ 1,250,840 

7 Chemical Handling Facility with Carbon Tanks $ 5,390,000 $ 7,027,670 $ 8,936,830 $ 8,936,830 $ 8,936,830 $ - $ - $ 8,936,830 

8 Deep Sand Filtration $ - $ - $ 40,320,081 $ - $ - $ 40,320,081 $ - $ - 

9 Denitrification Filtration $ - $ - $ - $ 57,543,362 $ - $ - $ - $ - 

10 Microfiltration Tanks $ - $ - $ - $ - $ 64,768,666 $ - $ 64,768,666 $ - 

11 Membrane Bio Reactor Tanks $ - $ - $ - $ - $ - $ - $ - $ 173,854,181 

12 Fine Screens $ - $ - $ - $ - $ - $ - $ - $ 21,700,000 

13 Grit Classifier and Washer $ - $ - $ - $ - $ - $ - $ - $ 1,600,000 

14 Plantwide Electrical Work $ 4,408,000 $ 4,779,000 $ 15,256,000 $ 16,953,000 $ 17,682,000 $ 7,615,000 $ 9,956,000 $ 30,530,000 

15 Instrumentation and Controls $ 2,204,000 $ 2,389,500 $ 7,628,000 $ 8,476,500 $ 8,841,000 $ 3,807,500 $ 4,978,000 $ 15,265,000 

Subtotal: $ 64,405,687 $ 71,063,657 $ 216,971,886 $ 237,872,267 $ 246,291,071 $ 123,246,902 $ 151,556,987 $ 401,769,586 

21% Overhead and Profit $ 13,525,194 $ 14,923,368 $ 45,564,096 $ 49,953,176 $ 51,721,125 $ 25,881,849 $ 31,826,967 $ 84,371,613 

Subtotal: $ 77,930,881 $ 85,987,025 $ 262,535,982 $ 287,825,443 $ 298,012,196 $ 149,128,751 $ 183,383,954 $ 486,141,199 

40% Design Contingency (60% MBR) $ 31,172,352 $ 34,394,810 $ 105,014,393 $ 115,130,177 $ 119,204,878 $ 59,651,500 $ 73,353,582 $ 291,684,719 

Subtotal: $ 109,103,233 $ 120,381,835 $ 367,550,375 $ 402,955,620 $ 417,217,074 $ 208,780,252 $ 256,737,536 $ 777,825,918 

6% Bond and Insurance $ 6,546,194 $ 7,222,910 $ 22,053,022 $ 24,177,337 $ 25,033,024 $ 12,526,815 $ 15,404,252 $ 46,669,555 

Subtotal: $ 115,649,427 $ 127,604,745 $ 389,603,397 $ 427,132,957 $ 442,250,099 $ 221,307,067 $ 272,141,788 $ 824,495,473 

6% Contract Allowance and Unit Price Items 

8.5% Escalation to Mid-point of Construction 

$ 6,938,966 $ 7,656,285 $ 23,376,204 $ 25,627,977 $ 26,535,006 $ 13,278,424 $ 16,328,507 $ 49,469,728 

Subtotal: $ 122,588,393 $ 135,261,029 $ 412,979,601 $ 452,760,934 $ 468,785,104 $ 234,585,491 $ 288,470,295 $ 873,965,201 

$ 311,079,738 $ 363,937,500 $ 1,317,659,715 $ 1,444,586,711 $ 1,495,713,700 $ 748,472,443 $ 920,398,213 $ 2,788,488,185 

Total: 

$ 433,668,132 $ 499,198,529 $ 1,730,639,315 $ 1,897,347,645 $ 1,964,498,805 $ 983,057,934 $ 1,208,868,508 $ 3,662,453,386



Owl's Head WPCP 

Summary 


Item 

Description 


BNR 

Full Step BNR 

Full Step BNR 

with Solids 

Filtration 

Full Step BNR 

with 


Full Step BNR 

with 




Membrane 

Bioreactor 


2 Demolition and Site Construction $ 1,649,013 $ 1,649,013 $ 35,806,652 $ 35,806,652 $ 35,806,652 $ 35,806,652 $ 35,806,652 $ 41,454,652 

3 Aeration Tank Modifications, Baffles and Mixers $ 14,322,167 $ 14,322,167 $ 14,423,561 $ 14,423,561 $ 14,423,561 $ 2,100,000 $ 2,100,000 $ 14,423,561 


5 RAS and WAS Pumping System $ - $ 1,940,160 $ 1,940,160 $ 1,940,160 $ 1,940,160 $ - $ - $ 2,425,040 







12 Fine Screens $ - $ - $ - $ - $ - $ - $ - $ 21,700,000 




Subtotal: $ 38,108,760 $ 45,392,730 $ 150,046,643 $ 165,026,038 $ 170,710,397 $ 94,158,147 $ 114,821,901 $ 290,556,484 


Subtotal: $ 46,111,600 $ 54,925,203 $ 181,556,438 $ 199,681,506 $ 206,559,580 $ 113,931,358 $ 138,934,500 $ 351,573,346 


Subtotal: $ 64,556,239 $ 76,895,285 $ 254,179,013 $ 279,554,109 $ 289,183,412 $ 159,503,901 $ 194,508,300 $ 562,517,353 


Subtotal: $ 68,429,614 $ 81,509,002 $ 269,429,754 $ 296,327,356 $ 306,534,417 $ 169,074,136 $ 206,178,798 $ 596,268,394 



$ 4,105,777 $ 4,890,540 $ 16,165,785 $ 17,779,641 $ 18,392,065 $ 10,144,448 $ 12,370,728 $ 35,776,104 

Subtotal: $ 72,535,391 $ 86,399,542 $ 285,595,539 $ 314,106,997 $ 324,926,482 $ 179,218,584 $ 218,549,526 $ 632,044,498 

$ 184,065,471 $ 232,469,274 $ 911,225,967 $ 1,002,195,108 $ 1,036,715,939 $ 571,817,851 $ 697,307,823 $ 2,016,611,888 

Total: 

$ 256,600,862 $ 318,868,815 $ 1,196,821,506 $ 1,316,302,105 $ 1,361,642,421 $ 751,036,434 $ 915,857,349 $ 2,648,656,386



Red Hook WPCP 

Summary 


Item 

Description 


BNR 

Full Step BNR 

Full Step BNR 

with Solids 

Filtration 

Full Step BNR 

with 


Full Step BNR 

with 




Membrane 

Bioreactor 


2 Demolition and Site Construction $ 820,107 $ 820,107 $ 18,322,376 $ 18,322,376 $ 18,322,376 $ 18,322,376 $ 18,322,376 $ 23,970,376 

3 Aeration Tank Modifications, Baffles and Mixers $ 13,210,334 $ 13,210,334 $ 13,261,031 $ 13,261,031 $ 13,261,031 $ 1,050,000 $ 1,050,000 $ 13,261,031 


5 RAS and WAS Pumping System $ 1,874,040 $ 1,874,040 $ 1,962,200 $ 1,962,200 $ 1,962,200 $ - $ - $ 1,962,200 







12 Fine Screens $ - $ - $ - $ - $ - $ - $ - $ 15,120,000 




Subtotal: $ 33,484,660 $ 42,161,980 $ 96,173,389 $ 102,392,937 $ 105,216,703 $ 55,400,784 $ 64,445,598 $ 189,434,203 


Subtotal: $ 40,516,439 $ 51,015,995 $ 116,369,801 $ 123,895,454 $ 127,312,211 $ 67,034,949 $ 77,979,174 $ 229,215,386 


Subtotal: $ 56,723,014 $ 71,422,393 $ 162,917,721 $ 173,453,636 $ 178,237,095 $ 93,848,928 $ 109,170,843 $ 366,744,617 


Subtotal: $ 60,126,395 $ 75,707,737 $ 172,692,784 $ 183,860,854 $ 188,931,321 $ 99,479,864 $ 115,721,094 $ 388,749,294 



$ 3,607,584 $ 4,542,464 $ 10,361,567 $ 11,031,651 $ 11,335,879 $ 5,968,792 $ 6,943,266 $ 23,324,958 

Subtotal: $ 63,733,979 $ 80,250,201 $ 183,054,351 $ 194,892,505 $ 200,267,200 $ 105,448,656 $ 122,664,359 $ 412,074,252 

$ 161,731,049 $ 215,923,668 $ 584,056,316 $ 621,827,330 $ 638,975,923 $ 336,446,268 $ 391,374,984 $ 1,314,771,093 

Total: 

$ 225,465,027 $ 296,173,869 $ 767,110,667 $ 816,719,834 $ 839,243,123 $ 441,894,923 $ 514,039,344 $ 1,726,845,345




Summary 


Item 

Description 


BNR 

Full Step BNR 









Membrane 

Bioreactor 


2 Demolition and Site Construction $ 820,107 $ 820,107 $ 820,107 $ 9,565,541 $ 9,565,541 $ 820,107 $ 9,565,541 $ 6,468,107 

3 Aeration Tank Modifications, Baffles and Mixers $ 12,319,753 $ 12,319,753 $ 12,399,460 $ 12,399,460 $ 12,399,460 $ - $ - $ 12,399,460 


5 RAS and WAS Pumping System $ 1,896,080 $ 1,896,080 $ 1,962,200 $ 1,962,200 $ 1,962,200 $ - $ - $ 1,962,200 







12 Fine Screens $ - $ - $ - $ - $ - $ - $ - $ 12,600,000 



15 Instrumentation and Controls $ 955,500 $ 1,129,500 $ 1,906,000 $ 2,580,500 $ 2,697,000 $ 740,500 $ 1,531,500 $ 5,572,500 

Subtotal: $ 32,033,119 $ 38,383,439 $ 62,752,627 $ 81,172,070 $ 84,106,963 $ 34,324,357 $ 55,678,693 $ 153,405,599 


Subtotal: $ 38,760,074 $ 46,443,961 $ 75,930,679 $ 98,218,205 $ 101,769,425 $ 41,532,472 $ 67,371,219 $ 185,620,774 


Subtotal: $ 54,264,104 $ 65,021,545 $ 106,302,950 $ 137,505,487 $ 142,477,195 $ 58,145,461 $ 94,319,706 $ 296,993,239 


Subtotal: $ 57,519,950 $ 68,922,838 $ 112,681,127 $ 145,755,816 $ 151,025,827 $ 61,634,189 $ 99,978,888 $ 314,812,833 


$ 3,451,197 $ 4,135,370 $ 6,760,868 $ 8,745,349 $ 9,061,550 $ 3,698,051 $ 5,998,733 $ 18,888,770 

Subtotal: $ 60,971,147 $ 73,058,208 $ 119,441,995 $ 154,501,165 $ 160,087,376 $ 65,332,240 $ 105,977,622 $ 333,701,603 


$ 154,720,100 $ 196,572,669 $ 381,093,652 $ 492,954,035 $ 510,777,496 $ 208,450,152 $ 338,133,996 $ 1,064,713,991 

Total: $ 215,691,247 $ 269,630,877 $ 500,535,647 $ 647,455,199 $ 670,864,872 $ 273,782,392 $ 444,111,618 $ 1,398,415,594

Item Item Description Qty Unit 

1 General Requirements 

SUPERVISION & LABOR 



North River WPCP Advanced Basic BNR 

Unit Price 

Total Cost 

Labor Material Equip Total Labor Material Equip Total 

Project manager 48.0 mnth $ - $ 12,500.0 $ - $ 12,500 $ - $ 600,000 $ - $ 600,000 

Superintendent 48.0 mnth $ - $ 10,000.0 $ - $ 10,000 $ - $ 480,000 $ - $ 480,000 

Deputy project manager 48.0 mnth $ - $ 10,000.0 $ - $ 10,000 $ - $ 480,000 $ - $ 480,000 

Project engineer (4) 48.0 mnth $ - $ 26,000.0 $ - $ 26,000 $ - $ 1,248,000 $ - $ 1,248,000 

Cost engineer (2) 48.0 mnth $ - $ 13,000.0 $ - $ 13,000 $ - $ 624,000 $ - $ 624,000 

Safety Engineer 48.0 mnth $ - $ 6,000.0 $ - $ 6,000 $ - $ 288,000 $ - $ 288,000 

Clerical (2) 48.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 240,000 $ - $ 240,000 

Master mechanic 42.0 mnth $ - $ 10,300.0 $ - $ 10,300 $ - $ 432,600 $ - $ 432,600 

Maintenance forman 42.0 mnth $ - $ 10,300.0 $ - $ 10,300 $ - $ 432,600 $ - $ 432,600 

Labor forman 42.0 mnth $ - $ 10,300.0 $ - $ 10,300 $ - $ 432,600 $ - $ 432,600 

SUPPORT 

Contractor vans and equipment 42.0 mnth $ - $ 1,000.0 $ - $ 1,000 $ - $ 42,000 $ - $ 42,000 

Contractor trailer 48.0 mnth $ - $ 600.0 $ - $ 600 $ - $ 28,800 $ - $ 28,800 

Cell phone usage 48.0 mnth $ - $ 1,000.0 $ - $ 1,000 $ - $ 48,000 $ - $ 48,000 

Small tools and equipment 42.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 210,000 $ - $ 210,000 

Mobilize and demobilize trailers 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 

Field Office maint. & janitorial service 48.0 mnth $ - $ 1,500.0 $ - $ 1,500 $ - $ 72,000 $ - $ 72,000 

Temp heat and ventilation 42.0 mnth $ - $ 500.0 $ - $ 500 $ - $ 21,000 $ - $ 21,000 

Temp water and sanitary facilities 42.0 mnth $ - $ 1,440.0 $ - $ 1,440 $ - $ 60,480 $ - $ 60,480 

Daily cleaning and site maintenance 42.0 mnth $ - $ 7,000.0 $ - $ 7,000 $ - $ 294,000 $ - $ 294,000 

Rubbish container / carting 42.0 mnth $ - $ 1,500.0 $ - $ 1,500 $ - $ 63,000 $ - $ 63,000 

Safety 1.0 LS $ - $ 650,000.0 $ - $ 650,000 $ - $ 650,000 $ - $ 650,000 

SHOP DRAWINGS & TESTING 

Shop drawings 1.0 LS $ - $ 400,000.0 $ - $ 400,000 $ - $ 400,000 $ - $ 400,000 

As-built drawings 1.0 LS $ - $ 250,000.0 $ - $ 250,000 $ - $ 250,000 $ - $ 250,000 

O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 

Start-up and testing 1.0 LS $ - $ 200,000.0 $ - $ 200,000 $ - $ 200,000 $ - $ 200,000 

Page 9 of 264





Unit Price 

Total Cost 


MISC ITEMS 

RE field office 48.0 mnth $ - $ 8,000.0 $ - $ 8,000 $ - $ 384,000 $ - $ 384,000 

Dust, noise and rodent control 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 

Traffic maintenance requirements 1.0 LS $ - $ 400,000.0 $ - $ 400,000 $ - $ 400,000 $ - $ 400,000 

ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 

Progress schedule 48.0 mnth $ - $ 6,400.0 $ - $ 6,400 $ - $ 307,200 $ - $ 307,200 

Safe and healthful working conditions 42.0 mnth $ - $ 7,630.0 $ - $ 7,630 $ - $ 320,460 $ - $ 320,460 

Quality of life req. / low sulfur fuel 42.0 mnth $ - $ 2,000.0 $ - $ 2,000 $ - $ 84,000 $ - $ 84,000 

Incidental project requirements 1.0 LS $ - $ 1,000,000.0 $ - $ 1,000,000 $ - $ 1,000,000 $ - $ 1,000,000 

Project closeout 1.0 LS $ - $ 500,000.0 $ - $ 500,000 $ - $ 500,000 $ - $ 500,000 

General Requirements Total $ - $ 10,757,740 $ - $ 10,757,740 

2 Demolition and Site Construction 

DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 

In-situ soil sampling 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 

Steel sheeting for excavation 10,000.0 sf $ 5.5 $ 7.0 $ 6.0 $ 18 $ 54,500 $ 70,000 $ 59,500 $ 184,000 

Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 

Crushed stone base 1,000.0 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 12,580 $ 19,800 $ 5,000 $ 37,380 

Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 

SITEWORK 

Temporary fencing 1,000.0 lf $ 1.6 $ 47.0 $ 0.4 $ 49 $ 1,640 $ 47,000 $ 360 $ 49,000 

Sawcut pavement 1,000.0 lf $ 1.9 $ 1.3 $ 1.0 $ 4 $ 1,890 $ 1,260 $ 990 $ 4,140 

Remove pavement 400.0 sy $ 5.8 $ - $ 3.5 $ 9 $ 2,320 $ - $ 1,412 $ 3,732 

Concrete curbs 400.0 lf $ 18.0 $ 19.7 $ 4.0 $ 42 $ 7,200 $ 7,880 $ 1,600 $ 16,680 

New pavement 400.0 sy $ 3.2 $ 29.4 $ 2.8 $ 35 $ 1,260 $ 11,740 $ 1,100 $ 14,100 

New concrete pads 100.0 sy $ 28.4 $ 36.9 $ 1.9 $ 67 $ 2,844 $ 3,690 $ 189 $ 6,723 

Catch basins 28.0 each $ 3,006.0 $ 1,117.0 $ 73.0 $ 4,196 $ 84,168 $ 31,276 $ 2,044 $ 117,488 

Electric manholes 8.0 each $ 3,000.0 $ 3,069.0 $ 220.0 $ 6,289 $ 24,000 $ 24,552 $ 1,760 $ 50,312 

Page 10 of 264





Unit Price 

Total Cost 


Lightpoles 6.0 each $ 2,640.0 $ 5,175.0 $ 318.0 $ 8,133 $ 15,840 $ 31,050 $ 1,908 $ 48,798 

Sheeting for misc trench excavation 2,400.0 sf $ 5.5 $ 7.0 $ 6.0 $ 18 $ 13,080 $ 16,800 $ 14,280 $ 44,160 

Trench excavation for pipe/cable reloc. 2,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 20,000 $ - $ 19,440 $ 39,440 

Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 

Fine grading and seeding 2,000.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 5,200 $ 840 $ 640 $ 6,680 

Concrete thrust blocks 400.0 cy $ 400.0 $ 300.0 $ 100.0 $ 800 $ 160,000 $ 120,000 $ 40,000 $ 320,000 

Concrete ductbanks 400.0 cy $ 140.0 $ 150.0 $ 25.0 $ 315 $ 56,000 $ 60,000 $ 10,000 $ 126,000 

Demolition and Site Construction Total $ 712,122 $ 639,288 $ 297,603 $ 1,649,013 

3 Aeration Tank Modifications, Baffles and 

Mixers 

Aeration Tank Modifications 

Scaffolding 63,000.0 sqft $ 2.7 $ - $ 0.3 $ 3 $ 170,100 $ - $ 18,900 $ 189,000 

Demo tank walls 4,200.0 cf $ 26.3 $ - $ 4.4 $ 31 $ 110,460 $ - $ 18,480 $ 128,940 

Tank dewatering 1.0 LS $ 40,000.0 $ - $ 15,000.0 $ 55,000 $ 40,000 $ - $ 15,000 $ 55,000 

Misc. removal and disposal 7,000.0 cy $ 30.0 $ - $ 30.0 $ 60 $ 210,000 $ - $ 210,000 $ 420,000 

Drill dowels 8,400.0 each $ 70.0 $ 6.0 $ 10.0 $ 86 $ 588,000 $ 50,400 $ 84,000 $ 722,400 

Concrete walls and channels 5,600.0 cy $ 600.0 $ 260.0 $ 63.0 $ 923 $ 3,360,000 $ 1,456,000 $ 352,800 $ 5,168,800 

Waterproof lining 434,000.0 sf $ 7.0 $ 1.0 $ - $ 8 $ 3,038,000 $ 434,000 $ - $ 3,472,000 

Handrails 21,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 420,000 $ 3,150,000 $ 42,000 $ 3,612,000 

Baffles 

FRP baffle walls 34,650.0 sqft $ 8.8 $ 9.8 $ 0.5 $ 19 $ 304,920 $ 339,570 $ 17,325 $ 661,815 

FRP beams 10,164.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 53,869 $ 65,050 $ - $ 118,919 

Mixers 

FRP grating at mixer platform 3,920.0 sf $ 3.0 $ 25.0 $ - $ 28 $ 11,760 $ 98,000 $ - $ 109,760 

Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 

Aeration Tank Modifications, Baffles and 

Mixers Total 

$ 8,547,109 $ 7,073,020 $ 774,505 $ 16,394,634 

4 Process Air System 

Demo existing process air system 1.0 LS $ 150,000.0 $ - $ 70,000.0 $ 220,000 $ 150,000 $ - $ 70,000 $ 220,000 

Page 11 of 264





Unit Price 

Total Cost 


Demo existing pipe support 1.0 LS $ 250,000.0 $ - $ 100,000.0 $ 350,000 $ 250,000 $ - $ 100,000 $ 350,000 

Process air blowers, silencers, etc. 4.0 each $ 500,000.0 $ 1,300,000.0 $ 50,000.0 $ 1,850,000 $ 2,000,000 $ 5,200,000 $ 200,000 $ 7,400,000 

Process air piping 20,000.0 lnft $ 100.0 $ 300.0 $ 50.0 $ 450 $ 2,000,000 $ 6,000,000 $ 1,000,000 $ 9,000,000 

Diffusers 500.0 each $ 50.0 $ 25.0 $ - $ 75 $ 25,000 $ 12,500 $ - $ 37,500 

PA gates and valves 1.0 LS $ 1,000,000.0 $ 1,500,000.0 $ 50,000.0 $ 2,550,000 $ 1,000,000 $ 1,500,000 $ 50,000 $ 2,550,000 

Metal pipe support 1.0 LS $ 750,000.0 $ 1,000,000.0 $ 50,000.0 $ 1,800,000 $ 750,000 $ 1,000,000 $ 50,000 $ 1,800,000 

Temp access bridge or crane 1.0 LS $ 500,000.0 $ 100,000.0 $ 50,000.0 $ 650,000 $ 500,000 $ 100,000 $ 50,000 $ 650,000 

Process Air System Total $ 6,675,000 $ 13,812,500 $ 1,520,000 $ 22,007,500 

5 RAS and WAS Pumping System 

RAS and WAS Pumping System Total $ - $ - $ - $ - 

6 Aeration Tank Froth Hood System 

Misc. removal 1.0 LS $ 40,000.0 $ - $ 10,000.0 $ 50,000 $ 40,000 $ - $ 10,000 $ 50,000 

Froth Control Hoods 20.0 each $ 4,500.0 $ 25,000.0 $ 240.0 $ 29,740 $ 90,000 $ 500,000 $ 4,800 $ 594,800 

Piping and supports 1.0 LS $ 600,000.0 $ 300,000.0 $ 50,000.0 $ 950,000 $ 600,000 $ 300,000 $ 50,000 $ 950,000 

Aeration Tank Froth Hood System Total $ 730,000 $ 800,000 $ 64,800 $ 1,594,800 

7 Chemical Handling Facility with Carbon 

Tanks 

Hypochlorite storage tanks 3.0 each $ 75,000.0 $ 75,000.0 $ 20,000.0 $ 170,000 $ 225,000 $ 225,000 $ 60,000 $ 510,000 

Alkalinity storage tanks 3.0 each $ 125,000.0 $ 125,000.0 $ 40,000.0 $ 290,000 $ 375,000 $ 375,000 $ 120,000 $ 870,000 

Misc. pumps and piping 1.0 LS $ 1,200,000.0 $ 1,200,000.0 $ 60,000.0 $ 2,460,000 $ 1,200,000 $ 1,200,000 $ 60,000 $ 2,460,000 

RAS chlorination 1.0 LS $ 750,000.0 $ 750,000.0 $ 50,000.0 $ 1,550,000 $ 750,000 $ 750,000 $ 50,000 $ 1,550,000 

Chemical Handling Facility with Carbon 

Tanks Total 

$ 2,550,000 $ 2,550,000 $ 290,000 $ 5,390,000 

8 Deep Sand Filtration 

Deep Sand Filtration Total $ - $ - $ - $ - 

Page 12 of 264





Unit Price 

Total Cost 


9 Denitrification Filtration 

Denitrification Filtration Total $ - $ - $ - $ - 

10 Microfiltration Tanks 

Microfiltration Tanks Total $ - $ - $ - $ - 

11 Membrane Bio Reactor Tanks 

Membrane Bio Reactor Tanks Total $ - $ - $ - $ - 

12 Fine Screens 

Fine Screens Total $ - $ - $ - $ - 

13 Grit Classifier and Washer 

Grit Classifier and Washer Total $ - $ - $ - $ - 

14 Plantwide Electrical Work 

Plantwide Electrical 1.0 LS $ 1,921,000.0 $ 2,487,000.0 $ - $ 4,408,000 $ 1,921,000 $ 2,487,000 $ - $ 4,408,000 

Plantwide Electrical Work Total $ 1,921,000 $ 2,487,000 $ - $ 4,408,000 

15 Instrumentation and Controls 

Instrumentation 1.0 LS $ 960,500.0 $ 1,243,500.0 $ - $ 2,204,000 $ 960,500 $ 1,243,500 $ - $ 2,204,000 

Instrumentation and Controls Total $ 960,500 $ 1,243,500 $ - $ 2,204,000 

Grand Total $ 22,095,731 $ 39,363,048 $ 2,946,908 $ 64,405,687 

Page 13 of 264





Unit Price 

Total Cost 


Contractor Overhead and Profit 21.0% $ 13,525,194 

Subtotal: $ 77,930,881 

Design Contingency 40.0% $ 31,172,352 

Subtotal: $ 109,103,233 

Bond and Insurance 6.0% $ 6,546,194 

Subtotal: $ 115,649,427 

Contract Allowance and Unit Price Items 6.0% $ 6,938,966 

Subtotal: $ 122,588,393 

Escalation to Mid-point of construction: 8.5% $ 311,079,738 

Grand Total: $ 433,668,132 

Page 14 of 264

CSI 

Div. 


Item Description Qty Unit 




North River WPCP Full Step BNR 

Unit Price 

Total Cost 








Clerical (2) 60.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 300,000 $ - $ 300,000 




SUPPORT 











Safety 1.0 LS $ - $ 750,000.0 $ - $ 750,000 $ - $ 750,000 $ - $ 750,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 



Page 15 of 263




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 

SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 



Page 16 of 263




CSI 

Div. 


Unit Price 

Total Cost 




3 Aeration Tank Modification, Baffles and 

Mixers 









Handrails 21,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 420,000 $ 3,150,000 $ 42,000 $ 3,612,000 

Baffles 


FRP beams 10,164.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 53,869 $ 65,050 $ - $ 118,919 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 8,547,109 $ 7,073,020 $ 774,505 $ 16,394,634 






Diffusers 7,700.0 each $ 50.0 $ 25.0 $ - $ 75 $ 385,000 $ 192,500 $ - $ 577,500 





Page 17 of 263




CSI 

Div. 


Unit Price 

Total Cost 



Misc. modifications 1.0 LS $ 500,000.0 $ 200,000.0 $ 50,000.0 $ 750,000 $ 500,000 $ 200,000 $ 50,000 $ 750,000 

RAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 

Interim RAS pumping system 1.0 LS $ 20,000.0 $ 30,000.0 $ 2,000.0 $ 52,000 $ 20,000 $ 30,000 $ 2,000 $ 52,000 

Piping, valves and pipe support 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

RAS and WAS Pumping System Total $ 1,025,760 $ 810,000 $ 104,400 $ 1,940,160 

6 Aeration Tank Froth Hood Systen 




Aeration Tank Froth Hood Systen Total $ 730,000 $ 800,000 $ 64,800 $ 1,594,800 


Tanks 

Chemical Handling Facility 

In-situ soil sampling 1.0 each $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 

Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 

Crushed stone 177.0 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 2,230 $ 3,505 $ 885 $ 6,620 

Mobilize and demob pile drivers 2.0 each $ 18,650.0 $ - $ 13,750.0 $ 32,400 $ 37,300 $ - $ 27,500 $ 64,800 

Test piles 10.0 each $ - $ 50,000.0 $ - $ 50,000 $ - $ 500,000 $ - $ 500,000 

Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 

Form pile cap 864.0 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 3,456 $ 1,814 $ 1,901 $ 7,171 

Form slab on grade 644.0 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 2,576 $ 1,352 $ 1,417 $ 5,345 

Form pipe pits 756.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 6,350 $ 2,722 $ 2,268 $ 11,340 

Form columns 3,348.0 sf $ 14.8 $ 5.8 $ 4.0 $ 25 $ 49,550 $ 19,418 $ 13,392 $ 82,361 

Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 

Form roof slab 4,236.0 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 16,944 $ 8,896 $ 9,319 $ 35,159 

Form parapet 1,932.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 16,229 $ 6,955 $ 5,796 $ 28,980 

Form equipment pads 608.0 sf $ 14.0 $ 2.1 $ 2.2 $ 18 $ 8,512 $ 1,277 $ 1,338 $ 11,126 

Form concrete containment walls 468.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 3,931 $ 1,685 $ 1,404 $ 7,020 

Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 

Page 18 of 263




CSI 

Div. 


Unit Price 

Total Cost 


Concrete pile caps 64.0 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 14,400 $ 6,144 $ 640 $ 21,184 

Concrete slab on grade 353.0 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 79,425 $ 33,888 $ 3,530 $ 116,843 

Concrete pipe pits 14.0 cy $ 300.0 $ 96.0 $ 10.0 $ 406 $ 4,200 $ 1,344 $ 140 $ 5,684 

Concrete columns 31.0 cy $ 380.0 $ 96.0 $ 20.0 $ 496 $ 11,780 $ 2,976 $ 620 $ 15,376 

Concrete beams 20.0 cy $ 360.0 $ 96.0 $ 20.0 $ 476 $ 7,200 $ 1,920 $ 400 $ 9,520 

Concrete roof slab 79.0 cy $ 380.0 $ 96.0 $ 20.0 $ 496 $ 30,020 $ 7,584 $ 1,580 $ 39,184 

Concrete parapet 18.0 cy $ 300.0 $ 96.0 $ 10.0 $ 406 $ 5,400 $ 1,728 $ 180 $ 7,308 

Concrete equipment pads 35.0 cy $ 275.0 $ 96.0 $ 10.0 $ 381 $ 9,625 $ 3,360 $ 350 $ 13,335 

Concrete containment walls 9.0 cy $ 325.0 $ 96.0 $ 20.0 $ 441 $ 2,925 $ 864 $ 180 $ 3,969 

Scaffolding 10,948.0 sf $ 10.9 $ 2.7 $ - $ 14 $ 119,333 $ 29,560 $ - $ 148,893 

GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 

Brick veneer 10,948.0 sf $ 16.1 $ 9.1 $ - $ 25 $ 176,263 $ 99,627 $ - $ 275,890 

Misc. masonry 1.0 LS $ 50,000.0 $ 25,000.0 $ - $ 75,000 $ 50,000 $ 25,000 $ - $ 75,000 

Fiberglass grating 966.0 sf $ 7.6 $ 52.0 $ - $ 60 $ 7,361 $ 50,232 $ - $ 57,593 

Fiberglass stair 4.0 each $ 2,000.0 $ 5,000.0 $ - $ 7,000 $ 8,000 $ 20,000 $ - $ 28,000 

Fiberglass handrail 507.0 lf $ 75.0 $ 97.0 $ - $ 172 $ 38,025 $ 49,179 $ - $ 87,204 

Firestopping 1.0 each $ 20,000.0 $ 10,000.0 $ - $ 30,000 $ 20,000 $ 10,000 $ - $ 30,000 

Wall insulation 9,982.0 sf $ 4.4 $ 16.1 $ - $ 21 $ 43,921 $ 160,710 $ - $ 204,631 

Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 

Roof insulation 4,236.0 sf $ 1.0 $ 5.0 $ - $ 6 $ 4,236 $ 21,180 $ - $ 25,416 

SST drainage trough / leader 322.0 lf $ 6.0 $ 51.0 $ - $ 57 $ 1,932 $ 16,422 $ - $ 18,354 

Door frames, double 2.0 each $ 562.4 $ 499.5 $ 38.1 $ 1,100 $ 1,125 $ 999 $ 76 $ 2,200 

3 x 7 doors, SST 4.0 each $ 133.0 $ 325.0 $ 20.0 $ 478 $ 532 $ 1,300 $ 80 $ 1,912 

Door hardware, SST 2.0 each $ 203.8 $ 246.2 $ - $ 450 $ 408 $ 492 $ - $ 900 

Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 

Fire extinguisher 8.0 each $ 60.0 $ 250.0 $ - $ 310 $ 480 $ 2,000 $ - $ 2,480 



Polymer storage tanks 2.0 each $ 40,000.0 $ 50,000.0 $ 15,000.0 $ 105,000 $ 80,000 $ 100,000 $ 30,000 $ 210,000 

Polymer blending tanks 3.0 each $ 40,000.0 $ 50,000.0 $ 15,000.0 $ 105,000 $ 120,000 $ 150,000 $ 45,000 $ 315,000 

Misc. pumps and piping 1.0 LS $ 300,000.0 $ 200,000.0 $ 10,000.0 $ 510,000 $ 300,000 $ 200,000 $ 10,000 $ 510,000 

Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Page 19 of 263




CSI 

Div. 


Unit Price 

Total Cost 


Carbon tanks 

Excavation, carbon tanks 1,810.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 18,100 $ - $ 17,557 $ 35,657 

Backfill, carbon tanks 1,072.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,971 $ 23,584 $ 10,398 $ 46,954 

Crushed stone, carbon tanks 22.0 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 277 $ 436 $ 110 $ 823 

Form foundation slab 278.0 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 1,112 $ 584 $ 612 $ 2,307 

Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 

Concrete foundation slab 85.0 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 19,125 $ 8,160 $ 850 $ 28,135 

Concrete walls 120.0 cy $ 325.0 $ 96.0 $ 20.0 $ 441 $ 39,000 $ 11,520 $ 2,400 $ 52,920 

Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 

Removable covers 1,140.0 sf $ 27.8 $ 12.3 $ 9.9 $ 50 $ 31,658 $ 14,033 $ 11,320 $ 57,011 

Carbon tanks 2.0 each $ 84,218.0 $ 162,000.0 $ 64,690.0 $ 310,908 $ 168,436 $ 324,000 $ 129,380 $ 621,816 

Explosion proofing, fire suppression 1.0 LS $ 26,528.0 $ 75,000.0 $ - $ 101,528 $ 26,528 $ 75,000 $ - $ 101,528 

Pumps, piping and associated equip 1.0 LS $ 150,000.0 $ 200,000.0 $ 5,000.0 $ 355,000 $ 150,000 $ 200,000 $ 5,000 $ 355,000 


Tanks Total 

$ 2,991,172 $ 3,430,964 $ 605,534 $ 7,027,670 










Page 20 of 263




CSI 

Div. 


Unit Price 

Total Cost 









Instrumentation 1.0 LS $ 1,052,000.0 $ 1,337,500.0 $ - $ 2,389,500 $ 1,052,000 $ 1,337,500 $ - $ 2,389,500 

Instrumentation and Controls Total $ 1,052,000 $ 1,337,500 $ - $ 2,389,500 

Grand Total $ 24,197,163 $ 43,499,652 $ 3,366,842 $ 71,063,657 


Subtotal: $ 85,987,025 


Subtotal: $ 120,381,835 


Subtotal: $ 127,604,745 


Subtotal: $ 135,261,029 


Page 21 of 263 

Grand Total: $ 499,198,529

CSI 

Div. 






North River WPCP Full Step BNR with Solids Filtration 

Unit Price 

Total Cost 


Project manager 96.0 mnth $ - $ 12,500.0 $ - $ 12,500 $ - $ 1,200,000 $ - $ 1,200,000 




Cost engineer (2) 96.0 mnth $ - $ 13,000.0 $ - $ 13,000 $ - $ 1,248,000 $ - $ 1,248,000 


Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,400,000.0 $ - $ 1,400,000 $ - $ 1,400,000 $ - $ 1,400,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 22 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 

LAND RECLAMATION 

Soil testing and monitoring 1.0 LS $ - $ 500,000.0 $ - $ 500,000 $ - $ 500,000 $ - $ 500,000 

Barge mobilization and demobilization 1.0 each $ 26,100.0 $ - $ 30,700.0 $ 56,800 $ 26,100 $ - $ 30,700 $ 56,800 

Barge driven cofferdam 48,000.0 sf $ 5.5 $ 20.0 $ 6.3 $ 32 $ 261,600 $ 960,000 $ 302,400 $ 1,524,000 

Dredging 341,333.3 cy $ 8.3 $ - $ 7.0 $ 15 $ 2,833,067 $ - $ 2,372,267 $ 5,205,333 

Excavation 341,333.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 3,413,333 $ - $ 3,317,760 $ 6,731,093 

Soil disposal 341,333.3 cy $ 38.3 $ 14.0 $ 52 $ 13,073,067 $ - $ 4,778,667 $ 17,851,733 

Stone base 68,266.7 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 858,795 $ 1,351,680 $ 341,333 $ 2,551,808 

Select fill 341,333.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,123,307 $ 7,509,333 $ 3,297,280 $ 14,929,920 

Grade site 102,400.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 266,240 $ 40,960 $ 30,720 $ 337,920 

DEWATERING 

Mobilize / Demobilize dewatering pumps 1.0 LS $ 5,000.0 $ 5,000.0 $ 1,000.0 $ 11,000 $ 5,000 $ 5,000 $ 1,000 $ 11,000 

Page 23 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Operating engineer, 24/7 12.0 mnth $ 65,700.0 $ - $ - $ 65,700 $ 788,400 $ - $ - $ 788,400 

Standby generator 12.0 mnth $ - $ 10,000.0 $ - $ 10,000 $ - $ 120,000 $ - $ 120,000 

Pump rental 12.0 mnth $ - $ - $ 8,000.0 $ 8,000 $ - $ - $ 96,000 $ 96,000 

Electrical consumption 12.0 mnth $ - $ 9,000.0 $ - $ 9,000 $ - $ 108,000 $ - $ 108,000 

SPDES permit 1.0 LS $ - $ 1,000.0 $ - $ 1,000 $ - $ 1,000 $ - $ 1,000 

SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 




Demolition and Site Construction Total $ 26,361,030 $ 11,235,261 $ 14,865,730 $ 52,462,021 


Mixers 









Page 24 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 21,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 420,000 $ 3,150,000 $ 42,000 $ 3,612,000 

Baffles 


FRP beams 12,012.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 63,664 $ 76,877 $ - $ 140,540 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 8,612,344 $ 7,146,587 $ 777,655 $ 16,536,585 


Blower and Backwash Pump Building 

Excavation 4,230.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 42,300 $ - $ 41,031 $ 83,331 

Backfill 2,116.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 25,604 $ 46,552 $ 20,525 $ 92,681 

Crushed stone 1,058.0 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 13,331 $ 20,948 $ 5,290 $ 39,569 


Test piles 20.0 each $ - $ 50,000.0 $ - $ 50,000 $ - $ 1,000,000 $ - $ 1,000,000 

Piles 150,000.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,830,000 $ 3,600,000 $ 1,350,000 $ 6,780,000 

Form pile cap 2,304.0 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 9,216 $ 4,838 $ 5,069 $ 19,123 

Form slab on grade 2,040.0 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 8,160 $ 4,284 $ 4,488 $ 16,932 

Form column encasement 15,766.0 sf $ 14.8 $ 5.8 $ 4.0 $ 25 $ 233,337 $ 91,443 $ 63,064 $ 387,844 

Form beam encasement 20,016.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 298,238 $ 56,045 $ 68,054 $ 422,338 



Form equipment pads 1,216.0 sf $ 14.0 $ 2.1 $ 2.2 $ 18 $ 17,024 $ 2,554 $ 2,675 $ 22,253 

Rebars 341.2 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 703,334 $ 416,235 $ 13,988 $ 1,133,557 

Concrete pile caps 172.0 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 38,700 $ 16,512 $ 1,720 $ 56,932 

Concrete slab on grade 2,116.0 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 476,100 $ 203,136 $ 21,160 $ 700,396 

Concrete columns 146.0 cy $ 380.0 $ 96.0 $ 20.0 $ 496 $ 55,480 $ 14,016 $ 2,920 $ 72,416 

Concrete beam encasement 248.0 cy $ 360.0 $ 96.0 $ 20.0 $ 476 $ 89,280 $ 23,808 $ 4,960 $ 118,048 



Page 25 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Structural steel 450.0 tons $ 935.0 $ 2,925.0 $ 375.0 $ 4,235 $ 420,750 $ 1,316,250 $ 168,750 $ 1,905,750 

Metal deck 57,768.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 60,079 $ 207,965 $ 5,777 $ 273,820 

Stairs 8.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 120,000 $ 40,000 $ 8,000 $ 168,000 


GFB 73,648.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 1,141,544 $ 692,291 $ 176,755 $ 2,010,590 





Roofing 28,552.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 102,787 $ 148,470 $ 17,131 $ 268,389 


SST drainage trough / leader 1,020.0 lf $ 6.0 $ 51.0 $ - $ 57 $ 6,120 $ 52,020 $ - $ 58,140 

Door frames, double 22.0 each $ 562.4 $ 499.5 $ 38.1 $ 1,100 $ 12,373 $ 10,989 $ 838 $ 24,200 

Door frames, single 42.0 each $ 507.6 $ 357.9 $ 34.5 $ 900 $ 21,319 $ 15,032 $ 1,449 $ 37,800 

Single doors, SST 86.0 each $ 133.0 $ 325.0 $ 20.0 $ 478 $ 11,438 $ 27,950 $ 1,720 $ 41,108 

Door hardware, SST 64.0 each $ 203.8 $ 246.2 $ - $ 450 $ 13,043 $ 15,757 $ - $ 28,800 

Finishes 2.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 500,000 $ 500,000 $ 10,000 $ 1,010,000 

Toilet 4.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 20,000 $ 20,000 $ - $ 40,000 

Windows 2,866.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 42,417 $ 100,883 $ - $ 143,300 

Louvers 5,448.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 223,368 $ 196,128 $ - $ 419,496 

Fire extinguisher 30.0 each $ 60.0 $ 250.0 $ - $ 310 $ 1,800 $ 7,500 $ - $ 9,300 

Elevator 2.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 100,800 $ 320,000 $ 40,000 $ 460,800 

Bridge crane, 15 ton 2.0 each $ 20,000.0 $ 135,000.0 $ 2,000.0 $ 157,000 $ 40,000 $ 270,000 $ 4,000 $ 314,000 







Metal pipe support 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Temp access bridge or crane at Aera Tnk 1.0 LS $ 500,000.0 $ 100,000.0 $ 50,000.0 $ 650,000 $ 500,000 $ 100,000 $ 50,000 $ 650,000 

Plumbing 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 

HVAC 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Page 26 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 1.0 LS $ 2,000,000.0 $ 2,000,000.0 $ 500,000.0 $ 4,500,000 $ 2,000,000 $ 2,000,000 $ 500,000 $ 4,500,000 




RAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 

WAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 

Interim RAS / WAS pumping system 1.0 LS $ 20,000.0 $ 30,000.0 $ 2,000.0 $ 52,000 $ 20,000 $ 30,000 $ 2,000 $ 52,000 









Tanks 



Excavation 1,481.2 cy $ 10.0 $ - $ 9.7 $ 20 $ 14,812 $ - $ 14,368 $ 29,180 

Backfill 494.2 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 5,980 $ 10,872 $ 4,794 $ 21,646 

Crushed stone 247.8 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 3,122 $ 4,906 $ 1,239 $ 9,268 



Piles 18,480.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 225,456 $ 443,520 $ 166,320 $ 835,296 



Form pipe pits 1,058.4 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 8,891 $ 3,810 $ 3,175 $ 15,876 


Form beams 2,192.4 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 32,667 $ 6,139 $ 7,454 $ 46,260 



Page 27 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Rebars 69.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 143,822 $ 85,114 $ 2,860 $ 231,796 









Concrete containment walls 12.6 cy $ 325.0 $ 96.0 $ 20.0 $ 441 $ 4,095 $ 1,210 $ 252 $ 5,557 


GFB 13,974.8 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 216,609 $ 131,363 $ 33,540 $ 381,512 



Fiberglass grating 1,352.4 sf $ 7.6 $ 52.0 $ - $ 60 $ 10,305 $ 70,325 $ - $ 80,630 





Roofing 5,930.4 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 21,349 $ 30,838 $ 3,558 $ 55,746 





Door hardware, SST 3.0 each $ 203.8 $ 246.2 $ - $ 450 $ 611 $ 739 $ - $ 1,350 

Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Page 28 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 



Crushed stone, carbon tanks 30.8 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 388 $ 610 $ 154 $ 1,152 


Form walls 6,032.6 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 50,674 $ 21,717 $ 18,098 $ 90,489 

Rebars 21.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 44,446 $ 26,303 $ 884 $ 71,633 

Concrete foundation slab 119.0 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 26,775 $ 11,424 $ 1,190 $ 39,389 


Waterstop 194.6 lf $ 3.1 $ 11.6 $ - $ 15 $ 599 $ 2,253 $ - $ 2,853 






Tanks Total 

$ 3,737,790 $ 4,401,029 $ 798,011 $ 8,936,830 


Excavation 7,813.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 78,138 $ - $ 75,794 $ 153,932 

Backfill 3,679.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 44,520 $ 80,945 $ 35,689 $ 161,154 




Piles 54,350.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 663,070 $ 1,304,400 $ 489,150 $ 2,456,620 


Form foundation 3,793.1 sf $ 4.0 $ 2.1 $ 2.2 $ 8 $ 15,172 $ 7,966 $ 8,345 $ 31,483 

Form walls 38,689.7 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 324,993 $ 139,283 $ 116,069 $ 580,345 

Rebars 132.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 272,978 $ 161,549 $ 5,429 $ 439,956 


Concrete foundation 948.3 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 213,362 $ 91,034 $ 9,483 $ 313,879 

Page 29 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Aluminum cover 21,734.5 sf $ 43.0 $ 55.0 $ 2.1 $ 100 $ 934,583 $ 1,195,397 $ 45,642 $ 2,175,622 

Aluminum member 46.2 tons $ 3,800.0 $ 4,880.0 $ 2,520.0 $ 11,200 $ 175,586 $ 225,490 $ 116,441 $ 517,517 

Waterproof membrane 41,079.3 sf $ 7.0 $ 1.0 $ - $ 8 $ 287,555 $ 41,079 $ - $ 328,634 

Waterstop 3,224.1 lf $ 5.0 $ 5.0 $ - $ 10 $ 16,121 $ 16,121 $ - $ 32,241 

Filters 1.0 LS $ 1,500,000.0 $ 1,500,000.0 $ 200,000.0 $ 3,200,000 $ 1,500,000 $ 1,500,000 $ 200,000 $ 3,200,000 

Pumps, intermediate pump station 19.0 each $ 500,000.0 $ 700,000.0 $ 20,000.0 $ 1,220,000 $ 9,500,000 $ 13,300,000 $ 380,000 $ 23,180,000 

Piping and misc. equipment 1.0 LS $ 2,000,000.0 $ 2,000,000.0 $ 200,000.0 $ 4,200,000 $ 2,000,000 $ 2,000,000 $ 200,000 $ 4,200,000 

Deep Sand Filtration Total $ 16,536,188 $ 22,019,547 $ 1,764,345 $ 40,320,081 














Page 30 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 89,052,783 $ 105,428,966 $ 22,490,137 $ 216,971,886 


Subtotal: $ 262,535,982 


Subtotal: $ 367,550,375 


Subtotal: $ 389,603,397 


Subtotal: $ 412,979,601 

Escalation to Mid-point of construction: 8.5% ############ 

Grand Total: ############ 

Page 31 of 264

CSI 

Div. 






North River WPCP Full Step BNR with Denitrification 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,650,000.0 $ - $ 1,650,000 $ - $ 1,650,000 $ - $ 1,650,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 



Page 32 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 341,333.3 cy $ 8.3 $ - $ 7.0 $ 15 $ 2,833,067 $ - $ 2,372,267 $ 5,205,333 

Excavation 341,333.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 3,413,333 $ - $ 3,317,760 $ 6,731,093 


Stone base 68,266.7 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 858,795 $ 1,351,680 $ 341,333 $ 2,551,808 

Select fill 341,333.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,123,307 $ 7,509,333 $ 3,297,280 $ 14,929,920 

Grade site 102,400.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 266,240 $ 40,960 $ 30,720 $ 337,920 

DEWATERING 




Page 33 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 









Handrails 21,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 420,000 $ 3,150,000 $ 42,000 $ 3,612,000 

Baffles 

Page 34 of 264




CSI 

Div. 


Unit Price 

Total Cost 



FRP beams 12,012.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 63,664 $ 76,877 $ - $ 140,540 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 8,612,344 $ 7,146,587 $ 777,655 $ 16,536,585 



Excavation 4,230.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 42,300 $ - $ 41,031 $ 83,331 

Backfill 2,116.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 25,604 $ 46,552 $ 20,525 $ 92,681 




Piles 150,000.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,830,000 $ 3,600,000 $ 1,350,000 $ 6,780,000 








Rebars 341.2 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 703,334 $ 416,235 $ 13,988 $ 1,133,557 









Metal deck 57,768.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 60,079 $ 207,965 $ 5,777 $ 273,820 

Stairs 8.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 120,000 $ 40,000 $ 8,000 $ 168,000 

Page 35 of 264




CSI 

Div. 


Unit Price 

Total Cost 



GFB 73,648.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 1,141,544 $ 692,291 $ 176,755 $ 2,010,590 





Roofing 28,552.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 102,787 $ 148,470 $ 17,131 $ 268,389 







Finishes 2.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 500,000 $ 500,000 $ 10,000 $ 1,010,000 

Toilet 4.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 20,000 $ 20,000 $ - $ 40,000 

Windows 2,866.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 42,417 $ 100,883 $ - $ 143,300 

Louvers 5,448.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 223,368 $ 196,128 $ - $ 419,496 


Elevator 2.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 100,800 $ 320,000 $ 40,000 $ 460,800 










Plumbing 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 

HVAC 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Electrical 1.0 LS $ 2,000,000.0 $ 2,000,000.0 $ 500,000.0 $ 4,500,000 $ 2,000,000 $ 2,000,000 $ 500,000 $ 4,500,000 




Page 36 of 264




CSI 

Div. 


Unit Price 

Total Cost 


RAS pumps 24.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 34,560 $ 480,000 $ 14,400 $ 528,960 

WAS pumps 24.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 34,560 $ 480,000 $ 14,400 $ 528,960 



RAS and WAS Pumping System Total $ 1,089,120 $ 1,690,000 $ 130,800 $ 2,909,920 







Tanks 



Excavation 1,481.2 cy $ 10.0 $ - $ 9.7 $ 20 $ 14,812 $ - $ 14,368 $ 29,180 

Backfill 494.2 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 5,980 $ 10,872 $ 4,794 $ 21,646 




Piles 18,480.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 225,456 $ 443,520 $ 166,320 $ 835,296 





Form beams 2,192.4 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 32,667 $ 6,139 $ 7,454 $ 46,260 





Rebars 69.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 143,822 $ 85,114 $ 2,860 $ 231,796 




Page 37 of 264




CSI 

Div. 


Unit Price 

Total Cost 









GFB 13,974.8 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 216,609 $ 131,363 $ 33,540 $ 381,512 








Roofing 5,930.4 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 21,349 $ 30,838 $ 3,558 $ 55,746 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 



Page 38 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Form walls 6,032.6 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 50,674 $ 21,717 $ 18,098 $ 90,489 

Rebars 21.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 44,446 $ 26,303 $ 884 $ 71,633 



Waterstop 194.6 lf $ 3.1 $ 11.6 $ - $ 15 $ 599 $ 2,253 $ - $ 2,853 






Tanks Total 

$ 3,737,790 $ 4,401,029 $ 798,011 $ 8,936,830 




Excavation 15,627.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 156,276 $ - $ 151,588 $ 307,863 

Backfill 7,358.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 89,039 $ 161,890 $ 71,379 $ 322,308 




Piles 108,700.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,326,140 $ 2,608,800 $ 978,300 $ 4,913,240 



Form walls 77,379.3 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 649,986 $ 278,566 $ 232,138 $ 1,160,690 

Rebars 264.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 545,956 $ 323,098 $ 10,858 $ 879,913 

Concrete pile caps 1,593.1 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 358,448 $ 152,938 $ 15,931 $ 527,317 

Concrete foundation 1,896.6 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 426,724 $ 182,069 $ 18,966 $ 627,759 

Concrete walls 1,441.4 cy $ 300.0 $ 96.0 $ 10.0 $ 406 $ 432,414 $ 138,372 $ 14,414 $ 585,200 

Aluminum cover 43,469.0 sf $ 43.0 $ 55.0 $ 2.1 $ 100 $ 1,869,166 $ 2,390,793 $ 91,285 $ 4,351,243 

Aluminum member 92.4 tons $ 3,800.0 $ 4,880.0 $ 2,520.0 $ 11,200 $ 351,172 $ 450,979 $ 232,883 $ 1,035,034 


Page 39 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Waterstop 6,448.3 lf $ 5.0 $ 5.0 $ - $ 10 $ 32,241 $ 32,241 $ - $ 64,483 

Filters 8.0 each $ 100,000.00 $ 100,000.00 $ 5,000.00 $ 205,000 $ 800,000 $ 800,000 $ 40,000 $ 1,640,000 

Denite pumps 8.0 each $ 50,000.0 $ 50,000.0 $ 1,000.0 $ 101,000 $ 400,000 $ 400,000 $ 8,000 $ 808,000 



Denitrification Filtration Total $ 23,735,077 $ 30,939,094 $ 2,869,191 $ 57,543,362 















Grand Total $ 97,396,771 $ 116,856,513 $ 23,618,982 $ 237,872,267 

Page 40 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Subtotal: $ 287,825,443 


Subtotal: $ 402,955,620 


Subtotal: $ 427,132,957 


Subtotal: $ 452,760,934 

Escalation to Mid-point of construction: 8.5% $ 1,444,586,711 

Grand Total: $ 1,897,347,645 

Page 41 of 264

CSI 

Div. 






North River WPCP Full Step BNR with Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,750,000.0 $ - $ 1,750,000 $ - $ 1,750,000 $ - $ 1,750,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 42 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 341,333.3 cy $ 8.3 $ - $ 7.0 $ 15 $ 2,833,067 $ - $ 2,372,267 $ 5,205,333 

Excavation 341,333.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 3,413,333 $ - $ 3,317,760 $ 6,731,093 


Stone base 68,266.7 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 858,795 $ 1,351,680 $ 341,333 $ 2,551,808 

Select fill 341,333.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,123,307 $ 7,509,333 $ 3,297,280 $ 14,929,920 

Grade site 102,400.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 266,240 $ 40,960 $ 30,720 $ 337,920 

DEWATERING 


Page 43 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 









Page 44 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 21,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 420,000 $ 3,150,000 $ 42,000 $ 3,612,000 

Baffles 


FRP beams 12,012.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 63,664 $ 76,877 $ - $ 140,540 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 8,612,344 $ 7,146,587 $ 777,655 $ 16,536,585 



Excavation 4,230.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 42,300 $ - $ 41,031 $ 83,331 

Backfill 2,116.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 25,604 $ 46,552 $ 20,525 $ 92,681 




Piles 150,000.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,830,000 $ 3,600,000 $ 1,350,000 $ 6,780,000 








Rebars 341.2 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 703,334 $ 416,235 $ 13,988 $ 1,133,557 







Page 45 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Metal deck 57,768.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 60,079 $ 207,965 $ 5,777 $ 273,820 

Stairs 8.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 120,000 $ 40,000 $ 8,000 $ 168,000 


GFB 73,648.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 1,141,544 $ 692,291 $ 176,755 $ 2,010,590 





Roofing 28,552.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 102,787 $ 148,470 $ 17,131 $ 268,389 







Finishes 2.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 500,000 $ 500,000 $ 10,000 $ 1,010,000 

Toilet 4.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 20,000 $ 20,000 $ - $ 40,000 

Windows 2,866.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 42,417 $ 100,883 $ - $ 143,300 

Louvers 5,448.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 223,368 $ 196,128 $ - $ 419,496 


Elevator 2.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 100,800 $ 320,000 $ 40,000 $ 460,800 










Plumbing 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 

HVAC 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Page 46 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 1.0 LS $ 2,000,000.0 $ 2,000,000.0 $ 500,000.0 $ 4,500,000 $ 2,000,000 $ 2,000,000 $ 500,000 $ 4,500,000 




RAS pumps 24.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 34,560 $ 480,000 $ 14,400 $ 528,960 

WAS pumps 24.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 34,560 $ 480,000 $ 14,400 $ 528,960 










Tanks 



Excavation 1,481.2 cy $ 10.0 $ - $ 9.7 $ 20 $ 14,812 $ - $ 14,368 $ 29,180 

Backfill 494.2 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 5,980 $ 10,872 $ 4,794 $ 21,646 




Piles 18,480.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 225,456 $ 443,520 $ 166,320 $ 835,296 





Form beams 2,192.4 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 32,667 $ 6,139 $ 7,454 $ 46,260 



Page 47 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Rebars 69.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 143,822 $ 85,114 $ 2,860 $ 231,796 











GFB 13,974.8 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 216,609 $ 131,363 $ 33,540 $ 381,512 








Roofing 5,930.4 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 21,349 $ 30,838 $ 3,558 $ 55,746 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Page 48 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 6,032.6 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 50,674 $ 21,717 $ 18,098 $ 90,489 

Rebars 21.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 44,446 $ 26,303 $ 884 $ 71,633 



Waterstop 194.6 lf $ 3.1 $ 11.6 $ - $ 15 $ 599 $ 2,253 $ - $ 2,853 






Tanks Total 

$ 3,737,790 $ 4,401,029 $ 798,011 $ 8,936,830 






Excavation 18,753.1 cy $ 10.0 $ - $ 9.7 $ 20 $ 187,531 $ - $ 181,905 $ 369,436 

Backfill 8,830.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 106,847 $ 194,268 $ 85,654 $ 386,769 



Page 49 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Piles 130,400.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,590,880 $ 3,129,600 $ 1,173,600 $ 5,894,080 



Form walls 92,855.2 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 779,983 $ 334,279 $ 278,566 $ 1,392,828 

Rebars 317.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 655,148 $ 387,718 $ 13,030 $ 1,055,895 







Waterstop 7,737.9 lf $ 5.0 $ 5.0 $ - $ 10 $ 38,690 $ 38,690 $ - $ 77,379 

Microfilters 11.0 each $ 200,000.0 $ 200,000.0 $ 5,000.0 $ 405,000 $ 2,200,000 $ 2,200,000 $ 55,000 $ 4,455,000 



Microfiltration Tanks Total $ 27,134,144 $ 34,825,953 $ 2,808,569 $ 64,768,666 










Page 50 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 101,305,839 $ 121,426,872 $ 23,558,360 $ 246,291,071 


Subtotal: $ 298,012,196 


Subtotal: $ 417,217,074 


Subtotal: $ 442,250,099 


Subtotal: $ 468,785,104 


Grand Total: $ 1,964,498,805 

Page 51 of 264

CSI 

Div. 






North River WPCP Solids Filtration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,400,000.0 $ - $ 1,400,000 $ - $ 1,400,000 $ - $ 1,400,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 52 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 341,333.3 cy $ 8.3 $ - $ 7.0 $ 15 $ 2,833,067 $ - $ 2,372,267 $ 5,205,333 

Excavation 341,333.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 3,413,333 $ - $ 3,317,760 $ 6,731,093 


Stone base 68,266.7 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 858,795 $ 1,351,680 $ 341,333 $ 2,551,808 

Select fill 341,333.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,123,307 $ 7,509,333 $ 3,297,280 $ 14,929,920 

Grade site 102,400.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 266,240 $ 40,960 $ 30,720 $ 337,920 

DEWATERING 


Page 53 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 


Page 54 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Mixers Total 

$ - $ - $ - $ - 



Page 55 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Page 56 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Process Air System Total $ - $ - $ - $ - 




Aeration Tank Froth Hood System Total $ - $ - $ - $ - 


Tanks 


Page 57 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Page 58 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Tanks Total 

$ - $ - $ - $ - 


Excavation 7,813.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 78,138 $ - $ 75,794 $ 153,932 

Backfill 3,679.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 44,520 $ 80,945 $ 35,689 $ 161,154 




Piles 54,350.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 663,070 $ 1,304,400 $ 489,150 $ 2,456,620 



Form walls 38,689.7 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 324,993 $ 139,283 $ 116,069 $ 580,345 

Rebars 132.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 272,978 $ 161,549 $ 5,429 $ 439,956 



Page 59 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Aluminum cover 21,734.5 sf $ 43.0 $ 55.0 $ 2.1 $ 100 $ 934,583 $ 1,195,397 $ 45,642 $ 2,175,622 



Waterstop 3,224.1 lf $ 5.0 $ 5.0 $ - $ 10 $ 16,121 $ 16,121 $ - $ 32,241 

Filters 1.0 LS $ 1,500,000.0 $ 1,500,000.0 $ 200,000.0 $ 3,200,000 $ 1,500,000 $ 1,500,000 $ 200,000 $ 3,200,000 

















Page 60 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 49,332,218 $ 57,284,608 $ 16,630,075 $ 123,246,902 


Subtotal: $ 149,128,751 


Subtotal: $ 208,780,252 


Subtotal: $ 221,307,067 


Subtotal: $ 234,585,491 


Grand Total: $ 983,057,934 

Page 61 of 264

CSI 

Div. 






North River WPCP Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,750,000.0 $ - $ 1,750,000 $ - $ 1,750,000 $ - $ 1,750,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 62 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 341,333.3 cy $ 8.3 $ - $ 7.0 $ 15 $ 2,833,067 $ - $ 2,372,267 $ 5,205,333 

Excavation 341,333.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 3,413,333 $ - $ 3,317,760 $ 6,731,093 


Stone base 68,266.7 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 858,795 $ 1,351,680 $ 341,333 $ 2,551,808 

Select fill 341,333.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,123,307 $ 7,509,333 $ 3,297,280 $ 14,929,920 

Grade site 102,400.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 266,240 $ 40,960 $ 30,720 $ 337,920 

DEWATERING 


Page 63 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 


Page 64 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Mixers Total 

$ - $ - $ - $ - 



Page 65 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Page 66 of 264




CSI 

Div. 


Unit Price 

Total Cost 








Tanks 


Page 67 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Page 68 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Tanks Total 

$ - $ - $ - $ - 






Excavation 18,753.1 cy $ 10.0 $ - $ 9.7 $ 20 $ 187,531 $ - $ 181,905 $ 369,436 

Backfill 8,830.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 106,847 $ 194,268 $ 85,654 $ 386,769 



Page 69 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Piles 130,400.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,590,880 $ 3,129,600 $ 1,173,600 $ 5,894,080 



Form walls 92,855.2 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 779,983 $ 334,279 $ 278,566 $ 1,392,828 

Rebars 317.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 655,148 $ 387,718 $ 13,030 $ 1,055,895 







Waterstop 7,737.9 lf $ 5.0 $ 5.0 $ - $ 10 $ 38,690 $ 38,690 $ - $ 77,379 














Page 70 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 61,520,174 $ 72,362,514 $ 17,674,298 $ 151,556,987 


Subtotal: $ 183,383,954 


Subtotal: $ 256,737,536 


Subtotal: $ 272,141,788 


Subtotal: $ 288,470,295 


Grand Total: $ 1,208,868,508 

Page 71 of 264

CSI 

Div. 






North River WPCP Membrane Bioreactor 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 3,500,000.0 $ - $ 3,500,000 $ - $ 3,500,000 $ - $ 3,500,000 




O&M Manuals 1.0 LS $ - $ 188,000.0 $ - $ 188,000 $ - $ 188,000 $ - $ 188,000 


MISC ITEMS 


Page 72 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 19,000.0 $ - $ 19,000 $ - $ 19,000 $ - $ 19,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 341,333.3 cy $ 8.3 $ - $ 7.0 $ 15 $ 2,833,067 $ - $ 2,372,267 $ 5,205,333 

Excavation 341,333.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 3,413,333 $ - $ 3,317,760 $ 6,731,093 


Stone base 68,266.7 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 858,795 $ 1,351,680 $ 341,333 $ 2,551,808 

Select fill 341,333.3 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,123,307 $ 7,509,333 $ 3,297,280 $ 14,929,920 

Grade site 102,400.0 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 266,240 $ 40,960 $ 30,720 $ 337,920 

DEWATERING 


Page 73 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 









Page 74 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 21,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 420,000 $ 3,150,000 $ 42,000 $ 3,612,000 

Baffles 


FRP beams 12,012.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 63,664 $ 76,877 $ - $ 140,540 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 8,612,344 $ 7,146,587 $ 777,655 $ 16,536,585 



Excavation 4,230.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 42,300 $ - $ 41,031 $ 83,331 

Backfill 2,116.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 25,604 $ 46,552 $ 20,525 $ 92,681 




Piles 150,000.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,830,000 $ 3,600,000 $ 1,350,000 $ 6,780,000 








Rebars 341.2 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 703,334 $ 416,235 $ 13,988 $ 1,133,557 








Page 75 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Metal deck 57,768.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 60,079 $ 207,965 $ 5,777 $ 273,820 

Stairs 8.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 120,000 $ 40,000 $ 8,000 $ 168,000 


GFB 73,648.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 1,141,544 $ 692,291 $ 176,755 $ 2,010,590 





Roofing 28,552.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 102,787 $ 148,470 $ 17,131 $ 268,389 







Finishes 2.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 500,000 $ 500,000 $ 10,000 $ 1,010,000 

Toilet 4.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 20,000 $ 20,000 $ - $ 40,000 

Windows 2,866.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 42,417 $ 100,883 $ - $ 143,300 

Louvers 5,448.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 223,368 $ 196,128 $ - $ 419,496 


Elevator 2.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 100,800 $ 320,000 $ 40,000 $ 460,800 










Plumbing 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 

HVAC 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Electrical 1.0 LS $ 2,000,000.0 $ 2,000,000.0 $ 500,000.0 $ 4,500,000 $ 2,000,000 $ 2,000,000 $ 500,000 $ 4,500,000 

Page 76 of 264




CSI 

Div. 


Unit Price 

Total Cost 





RAS pumps 24.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 34,560 $ 480,000 $ 14,400 $ 528,960 

WAS pumps 24.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 34,560 $ 480,000 $ 14,400 $ 528,960 










Tanks 



Excavation 1,481.2 cy $ 10.0 $ - $ 9.7 $ 20 $ 14,812 $ - $ 14,368 $ 29,180 

Backfill 494.2 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 5,980 $ 10,872 $ 4,794 $ 21,646 




Piles 18,480.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 225,456 $ 443,520 $ 166,320 $ 835,296 





Form beams 2,192.4 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 32,667 $ 6,139 $ 7,454 $ 46,260 




Page 77 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Rebars 69.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 143,822 $ 85,114 $ 2,860 $ 231,796 











GFB 13,974.8 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 216,609 $ 131,363 $ 33,540 $ 381,512 








Roofing 5,930.4 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 21,349 $ 30,838 $ 3,558 $ 55,746 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

Page 78 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 6,032.6 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 50,674 $ 21,717 $ 18,098 $ 90,489 

Rebars 21.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 44,446 $ 26,303 $ 884 $ 71,633 



Waterstop 194.6 lf $ 3.1 $ 11.6 $ - $ 15 $ 599 $ 2,253 $ - $ 2,853 






Tanks Total 

$ 3,737,790 $ 4,401,029 $ 798,011 $ 8,936,830 


Finishes Total $ - $ - $ - $ - 






Excavation 79,968.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 799,680 $ - $ 775,690 $ 1,575,370 

Backfill 26,657.2 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 322,552 $ 586,458 $ 258,575 $ 1,167,585 

Page 79 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Piles 112,450.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,371,890 $ 2,698,800 $ 1,012,050 $ 5,082,740 



Form walls 331,753.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 2,786,725 $ 1,194,311 $ 995,259 $ 4,976,294 

Rebars 740.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 1,526,372 $ 903,310 $ 30,357 $ 2,460,039 


Concrete foundation 6,665.2 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 1,499,668 $ 639,858 $ 66,652 $ 2,206,178 

Concrete walls 6,144.0 cy $ 300.0 $ 96.0 $ 10.0 $ 406 $ 1,843,191 $ 589,821 $ 61,440 $ 2,494,452 


Aluminum member 337.4 tons $ 3,800.0 $ 4,880.0 $ 2,520.0 $ 11,200 $ 1,281,987 $ 1,646,341 $ 850,160 $ 3,778,488 

Waterproof membrane 255,840.5 sf $ 7.0 $ 1.0 $ - $ 8 $ 1,790,883 $ 255,840 $ - $ 2,046,724 

Waterstop 10,367.3 lf $ 5.0 $ 5.0 $ - $ 10 $ 51,836 $ 51,836 $ - $ 103,673 

Membrane bio reactors 20.0 each $ 2,000,000.00 $ 4,000,000.00 $ 50,000.00 $ 6,050,000 $ 40,000,000 $ 80,000,000 $ 1,000,000 $ 121,000,000 

Air scour blower 5.0 each $ 600,000.00 $ 1,200,000.00 $ 50,000.00 $ 1,850,000 $ 3,000,000 $ 6,000,000 $ 250,000 $ 9,250,000 


Odor control system 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Methanol tanks 2.0 each $ 300,000.0 $ 500,000.0 $ 25,000.0 $ 825,000 $ 600,000 $ 1,000,000 $ 50,000 $ 1,650,000 

Membrane Bio Reactor Tanks Total $ 63,397,417 $ 104,645,726 $ 5,811,038 $ 173,854,181 


Fine screens 14.0 each $ 500,000.0 $ 1,000,000.0 $ 50,000.0 $ 1,550,000 $ 7,000,000 $ 14,000,000 $ 700,000 $ 21,700,000 

Fine Screens Total $ 7,000,000 $ 14,000,000 $ 700,000 $ 21,700,000 


Grit classifier and washer 1.0 LS $ 700,000.0 $ 700,000.0 $ 200,000.0 $ 1,600,000 $ 700,000 $ 700,000 $ 200,000 $ 1,600,000 

Grit Classifier and Washer Total $ 700,000 $ 700,000 $ 200,000 $ 1,600,000 




Page 80 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 151,864,612 $ 222,444,145 $ 27,460,829 $ 401,769,586 


Subtotal: $ 486,141,199 


Subtotal: $ 777,825,918 


Subtotal: $ 824,495,473 


Subtotal: $ 873,965,201 


Grand Total: $ 3,662,453,386 

Page 81 of 264

CSI 

Div. 






Owl's Head WPCP Advanced Basic BNR 

Unit Price 

Total Cost 








Clerical (2) 48.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 240,000 $ - $ 240,000 




SUPPORT 











Safety 1.0 LS $ - $ 400,000.0 $ - $ 400,000 $ - $ 400,000 $ - $ 400,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 82 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 

SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 

Page 83 of 264




CSI 

Div. 


Unit Price 

Total Cost 







Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Odor Control tank covers 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 100,000.0 $ 2,100,000 $ 1,000,000 $ 1,000,000 $ 100,000 $ 2,100,000 

Baffles 


FRP beams 7,260.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 38,478 $ 46,464 $ - $ 84,942 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 7,185,078 $ 6,475,014 $ 662,075 $ 14,322,167 




Process air piping 2,000.0 lnft $ 100.0 $ 300.0 $ 50.0 $ 450 $ 200,000 $ 600,000 $ 100,000 $ 900,000 


PA gates and valves 1.0 LS $ 100,000.0 $ 150,000.0 $ 5,000.0 $ 255,000 $ 100,000 $ 150,000 $ 5,000 $ 255,000 

Page 84 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Metal pipe support 1.0 LS $ 75,000.0 $ 100,000.0 $ 5,000.0 $ 180,000 $ 75,000 $ 100,000 $ 5,000 $ 180,000 


Process Air System Total $ 1,660,000 $ 1,142,500 $ 330,000 $ 3,132,500 









Tanks 



Misc. pumps and piping 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

RAS chlorination 1.0 LS $ 500,000.0 $ 500,000.0 $ 25,000.0 $ 1,025,000 $ 500,000 $ 500,000 $ 25,000 $ 1,025,000 


Tanks Total 

$ 1,950,000 $ 1,950,000 $ 210,000 $ 4,110,000 







Page 85 of 264




CSI 

Div. 


Unit Price 

Total Cost 












Instrumentation 1.0 LS $ 605,000.0 $ 540,500.0 $ - $ 1,145,500 $ 605,000 $ 540,500 $ - $ 1,145,500 

Instrumentation and Controls Total $ 605,000 $ 540,500 $ - $ 1,145,500 

Grand Total $ 13,914,200 $ 22,636,042 $ 1,558,518 $ 38,108,760 


Subtotal: $ 46,111,600 


Subtotal: $ 64,556,239 


Page 86 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Subtotal: $ 68,429,614 


Subtotal: $ 72,535,391 


Grand Total: $ 256,600,862 

Page 87 of 264

CSI 

Div. 






Owl's Head WPCP Full Step BNR 

Unit Price 

Total Cost 








Clerical (2) 60.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 300,000 $ - $ 300,000 




SUPPORT 











Safety 1.0 LS $ - $ 450,000.0 $ - $ 450,000 $ - $ 450,000 $ - $ 450,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 



Page 88 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 

SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 



Page 89 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Baffles 


FRP beams 7,260.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 38,478 $ 46,464 $ - $ 84,942 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 7,185,078 $ 6,475,014 $ 662,075 $ 14,322,167 










Page 90 of 264




CSI 

Div. 


Unit Price 

Total Cost 




RAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 

Page 91 of 264




CSI 

Div. 


Unit Price 

Total Cost 












GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 




Polymer storage tank 2.0 each $ 40,000.0 $ 50,000.0 $ 15,000.0 $ 105,000 $ 80,000 $ 100,000 $ 30,000 $ 210,000 

Polymer blending unit 3.0 each $ 40,000.0 $ 50,000.0 $ 15,000.0 $ 105,000 $ 120,000 $ 150,000 $ 45,000 $ 315,000 


Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Page 92 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,946,172 $ 3,353,964 $ 585,534 $ 6,885,670 










Page 93 of 264




CSI 

Div. 


Unit Price 

Total Cost 











Grand Total $ 16,239,132 $ 27,115,146 $ 2,038,452 $ 45,392,730 


Subtotal: $ 54,925,203 


Subtotal: $ 76,895,285 


Subtotal: $ 81,509,002 


Subtotal: $ 86,399,542 


Page 94 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Grand Total: $ 318,868,815 

Page 95 of 264

CSI 

Div. 






Owl's Head WPCP Full Step BNR with Solids Filtration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,000,000.0 $ - $ 1,000,000 $ - $ 1,000,000 $ - $ 1,000,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 96 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 227,555.6 cy $ 8.3 $ - $ 7.0 $ 15 $ 1,888,711 $ - $ 1,581,511 $ 3,470,222 

Excavation 227,555.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 2,275,556 $ - $ 2,211,840 $ 4,487,396 


Stone base 45,511.1 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 572,530 $ 901,120 $ 227,556 $ 1,701,205 

Select fill 227,555.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 2,748,871 $ 5,006,222 $ 2,198,187 $ 9,953,280 

Grade site 68,266.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 177,493 $ 27,307 $ 20,480 $ 225,280 

DEWATERING 


Page 97 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 









Page 98 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Baffles 


FRP beams 8,580.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 45,474 $ 54,912 $ - $ 100,386 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 7,231,674 $ 6,527,562 $ 664,325 $ 14,423,561 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 






Page 99 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Structural steel 225.0 tons $ 935.0 $ 2,925.0 $ 375.0 $ 4,235 $ 210,375 $ 658,125 $ 84,375 $ 952,875 

Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 




Door frames, single 21.0 each $ 507.6 $ 357.9 $ 34.5 $ 900 $ 10,660 $ 7,516 $ 725 $ 18,900 

Single doors, SST 43.0 each $ 133.0 $ 325.0 $ 20.0 $ 478 $ 5,719 $ 13,975 $ 860 $ 20,554 


Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 









Plumbing 1.0 LS $ 200,000.0 $ 150,000.0 $ - $ 350,000 $ 200,000 $ 150,000 $ - $ 350,000 

HVAC 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Page 100 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ - $ 2,000,000 $ 1,000,000 $ 1,000,000 $ - $ 2,000,000 




RAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 




Page 101 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

Page 102 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,946,172 $ 3,353,964 $ 585,534 $ 6,885,670 


Excavation 5,860.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 58,603 $ - $ 56,845 $ 115,449 

Backfill 2,759.5 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 33,390 $ 60,709 $ 26,767 $ 120,865 




Piles 40,750.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 497,150 $ 978,000 $ 366,750 $ 1,841,900 



Form walls 29,017.2 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 243,745 $ 104,462 $ 87,052 $ 435,259 

Rebars 99.3 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 204,734 $ 121,162 $ 4,072 $ 329,967 




Page 103 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Aluminum cover 16,300.9 sf $ 43.0 $ 55.0 $ 2.1 $ 100 $ 700,937 $ 896,547 $ 34,232 $ 1,631,716 



Waterstop 2,418.1 lf $ 5.0 $ 5.0 $ - $ 10 $ 12,091 $ 12,091 $ - $ 24,181 

Filters 1.0 LS $ 1,250,000.0 $ 1,250,000.0 $ 50,000.0 $ 2,550,000 $ 1,250,000 $ 1,250,000 $ 50,000 $ 2,550,000 

















Page 104 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 59,854,746 $ 75,615,194 $ 14,576,702 $ 150,046,643 


Subtotal: $ 181,556,438 


Subtotal: $ 254,179,013 


Subtotal: $ 269,429,754 


Subtotal: $ 285,595,539 


Grand Total: ############ 

Page 105 of 264

CSI 

Div. 






Owl's Head WPCP Full Step BNR with Denitrification 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,100,000.0 $ - $ 1,100,000 $ - $ 1,100,000 $ - $ 1,100,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 



Page 106 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 227,555.6 cy $ 8.3 $ - $ 7.0 $ 15 $ 1,888,711 $ - $ 1,581,511 $ 3,470,222 

Excavation 227,555.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 2,275,556 $ - $ 2,211,840 $ 4,487,396 


Stone base 45,511.1 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 572,530 $ 901,120 $ 227,556 $ 1,701,205 

Select fill 227,555.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 2,748,871 $ 5,006,222 $ 2,198,187 $ 9,953,280 

Grade site 68,266.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 177,493 $ 27,307 $ 20,480 $ 225,280 

DEWATERING 




Page 107 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Page 108 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Baffles 


FRP beams 8,580.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 45,474 $ 54,912 $ - $ 100,386 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 7,231,674 $ 6,527,562 $ 664,325 $ 14,423,561 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 









Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Page 109 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 









Plumbing 1.0 LS $ 200,000.0 $ 150,000.0 $ - $ 350,000 $ 200,000 $ 150,000 $ - $ 350,000 

HVAC 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Electrical 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ - $ 2,000,000 $ 1,000,000 $ 1,000,000 $ - $ 2,000,000 




Page 110 of 264




CSI 

Div. 


Unit Price 

Total Cost 


RAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 





Page 111 of 264




CSI 

Div. 


Unit Price 

Total Cost 








GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 




Page 112 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,946,172 $ 3,353,964 $ 585,534 $ 6,885,670 




Excavation 11,720.7 cy $ 10.0 $ - $ 9.7 $ 20 $ 117,207 $ - $ 113,691 $ 230,898 

Backfill 5,519.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 66,779 $ 121,417 $ 53,534 $ 241,731 




Piles 81,500.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 994,300 $ 1,956,000 $ 733,500 $ 3,683,800 



Form walls 58,034.5 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 487,490 $ 208,924 $ 174,103 $ 870,517 

Rebars 198.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 409,467 $ 242,324 $ 8,144 $ 659,934 







Waterstop 4,836.2 lf $ 5.0 $ 5.0 $ - $ 10 $ 24,181 $ 24,181 $ - $ 48,362 

Page 113 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Filters 8.0 each $ 100,000.00 $ 100,000.00 $ 5,000.00 $ 205,000 $ 800,000 $ 800,000 $ 40,000 $ 1,640,000 




Denitrification Filtration Total $ 17,485,328 $ 22,803,720 $ 2,290,543 $ 42,579,591 















Grand Total $ 65,976,760 $ 83,307,055 $ 15,742,224 $ 165,026,038 

Page 114 of 264 

Contractor Overhead and Profit 21.0% $ 34,655,468




CSI 

Div. 


Unit Price 

Total Cost 


Subtotal: $ 199,681,506 


Subtotal: $ 279,554,109 


Subtotal: $ 296,327,356 


Subtotal: $ 314,106,997 


Grand Total: $ 1,316,302,105 

Page 115 of 264

CSI 

Div. 






Owl's Head WPCP Full Step BNR Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,200,000.0 $ - $ 1,200,000 $ - $ 1,200,000 $ - $ 1,200,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 



Page 116 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 227,555.6 cy $ 8.3 $ - $ 7.0 $ 15 $ 1,888,711 $ - $ 1,581,511 $ 3,470,222 

Excavation 227,555.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 2,275,556 $ - $ 2,211,840 $ 4,487,396 


Stone base 45,511.1 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 572,530 $ 901,120 $ 227,556 $ 1,701,205 

Select fill 227,555.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 2,748,871 $ 5,006,222 $ 2,198,187 $ 9,953,280 

Grade site 68,266.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 177,493 $ 27,307 $ 20,480 $ 225,280 

DEWATERING 




Page 117 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Page 118 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Baffles 


FRP beams 8,580.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 45,474 $ 54,912 $ - $ 100,386 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 7,231,674 $ 6,527,562 $ 664,325 $ 14,423,561 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 









Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Page 119 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 









Plumbing 1.0 LS $ 200,000.0 $ 150,000.0 $ - $ 350,000 $ 200,000 $ 150,000 $ - $ 350,000 

HVAC 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Electrical 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ - $ 2,000,000 $ 1,000,000 $ 1,000,000 $ - $ 2,000,000 




Page 120 of 264




CSI 

Div. 


Unit Price 

Total Cost 


RAS pumps 4.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 5,760 $ 80,000 $ 2,400 $ 88,160 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 





Page 121 of 264




CSI 

Div. 


Unit Price 

Total Cost 








GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 







Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 




Page 122 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,946,172 $ 3,353,964 $ 585,534 $ 6,885,670 






Excavation 14,064.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 140,648 $ - $ 136,429 $ 277,077 

Backfill 6,622.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 80,135 $ 145,701 $ 64,241 $ 290,077 




Piles 97,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,193,160 $ 2,347,200 $ 880,200 $ 4,420,560 



Form walls 69,641.4 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 584,988 $ 250,709 $ 208,924 $ 1,044,621 

Rebars 238.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 491,361 $ 290,788 $ 9,772 $ 791,921 




Page 123 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Waterstop 5,803.4 lf $ 5.0 $ 5.0 $ - $ 10 $ 29,017 $ 29,017 $ - $ 58,034 

















Grand Total $ 69,483,866 $ 85,640,299 $ 15,586,232 $ 170,710,397 


Page 124 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Subtotal: $ 206,559,580 


Subtotal: $ 289,183,412 


Subtotal: $ 306,534,417 


Subtotal: $ 324,926,482 


Grand Total: $ 1,361,642,421 

Page 125 of 264

CSI 

Div. 






Owl's Head WPCP Solids Filtration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,000,000.0 $ - $ 1,000,000 $ - $ 1,000,000 $ - $ 1,000,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 126 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 227,555.6 cy $ 8.3 $ - $ 7.0 $ 15 $ 1,888,711 $ - $ 1,581,511 $ 3,470,222 

Excavation 227,555.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 2,275,556 $ - $ 2,211,840 $ 4,487,396 


Stone base 45,511.1 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 572,530 $ 901,120 $ 227,556 $ 1,701,205 

Select fill 227,555.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 2,748,871 $ 5,006,222 $ 2,198,187 $ 9,953,280 

Grade site 68,266.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 177,493 $ 27,307 $ 20,480 $ 225,280 

DEWATERING 


Page 127 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 


Scaffolding 

Demo tank walls 

Tank dewatering 

Misc. removal and disposal 

Drill dowels 

Concrete walls and channels 

Waterproof lining 

Page 128 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 


Baffles 

FRP baffle walls 

FRP beams 

Mixers 

FRP grating at mixer platform 

Mixers 


Mixers Total 

$ 1,000,000 $ 1,000,000 $ 100,000 $ 2,100,000 



Excavation 

Backfill 

Crushed stone 

Mobilize and demob pile drivers 

Test piles 

Piles 

Form pile cap 

Form slab on grade 

Form column encasement 

Form beam encasement 

Form roof slab 

Form parapet 

Form equipment pads 

Rebars 

Concrete pile caps 

Concrete slab on grade 

Concrete columns 

Concrete beam encasement 

Concrete roof slab 

Page 129 of 264




CSI 

Div. 


Concrete parapet 

Concrete equipment pads 

Structural steel 

Metal deck 

Stairs 

Scaffolding 

GFB 

Brick veneer 

Misc. masonry 

Firestopping 

Wall insulation 

Roofing 

Roof insulation 

SST drainage trough / leader 

Door frames, double 

Door frames, single 

Single doors, SST 

Door hardware, SST 

Finishes 

Toilet 

Windows 

Louvers 

Fire extinguisher 

Elevator 

Bridge crane, 15 ton 

Demo existing process air system 

Demo existing pipe support 

Process air piping 

Diffusers 

PA gates and valves 

Metal pipe support 

Temp access bridge or crane at Aera Tnk 

Plumbing 

HVAC 

Unit Price 

Total Cost 


Page 130 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 



Misc. modifications 

RAS pumps 

Interim RAS pumping system 

Piping, valves and pipe support 



Misc. removal 


Piping and supports 



Tanks 


In-situ soil sampling 

Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 


Form pipe pits 

Form columns 

Form beams 


Form parapet 


Page 131 of 264




CSI 

Div. 


Form concrete containment walls 

Rebars 



Concrete pipe pits 


Concrete beams 




Concrete containment walls 

Scaffolding 

GFB 

Brick veneer 

Misc. masonry 


Fiberglass stair 

Fiberglass handrail 

Firestopping 


Roofing 




3 x 7 doors, SST 


Finishes 


Hypochlorite storage tanks 

Alkalinity storage tanks 

Polymer storage tank 

Polymer blending unit 

Misc. pumps and piping 

Plumbing 

Unit Price 

Total Cost 


Page 132 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 

Electrical 

Carbon tanks 

Excavation, carbon tanks 

Backfill, carbon tanks 

Crushed stone, carbon tanks 

Form foundation slab 

Form walls 

Rebars 

Concrete foundation slab 

Concrete walls 

Waterstop 

Removable covers 

Carbon tanks 

Explosion proofing, fire suppression 

Pumps, piping and associated equip 


Tanks Total 

$ - $ - $ - $ - 


Excavation 5,860.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 58,603 $ - $ 56,845 $ 115,449 

Backfill 2,759.5 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 33,390 $ 60,709 $ 26,767 $ 120,865 




Piles 40,750.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 497,150 $ 978,000 $ 366,750 $ 1,841,900 



Form walls 29,017.2 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 243,745 $ 104,462 $ 87,052 $ 435,259 

Rebars 99.3 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 204,734 $ 121,162 $ 4,072 $ 329,967 




Page 133 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Waterstop 2,418.1 lf $ 5.0 $ 5.0 $ - $ 10 $ 12,091 $ 12,091 $ - $ 24,181 

Filters 1.0 LS $ 1,250,000.0 $ 1,250,000.0 $ 50,000.0 $ 2,550,000 $ 1,250,000 $ 1,250,000 $ 50,000 $ 2,550,000 

















Page 134 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Grand Total $ 35,706,275 $ 47,198,597 $ 11,253,276 $ 94,158,147 


Subtotal: $ 113,931,358 


Subtotal: $ 159,503,901 


Subtotal: $ 169,074,136 


Subtotal: $ 179,218,584 


Grand Total: $ 751,036,434 

Page 135 of 264

CSI 

Div. 






Owl's Head WPCP Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,200,000.0 $ - $ 1,200,000 $ - $ 1,200,000 $ - $ 1,200,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 



Page 136 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 227,555.6 cy $ 8.3 $ - $ 7.0 $ 15 $ 1,888,711 $ - $ 1,581,511 $ 3,470,222 

Excavation 227,555.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 2,275,556 $ - $ 2,211,840 $ 4,487,396 


Stone base 45,511.1 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 572,530 $ 901,120 $ 227,556 $ 1,701,205 

Select fill 227,555.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 2,748,871 $ 5,006,222 $ 2,198,187 $ 9,953,280 

Grade site 68,266.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 177,493 $ 27,307 $ 20,480 $ 225,280 

DEWATERING 




Page 137 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 


Scaffolding 




Drill dowels 



Handrails 


Page 138 of 264




CSI 

Div. 


Baffles 


FRP beams 

Unit Price 

Total Cost 


Mixers 


Mixers 


Mixers Total 

$ 1,000,000 $ 1,000,000 $ 100,000 $ 2,100,000 



Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 





Form parapet 


Rebars 









Metal deck 

Page 139 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Stairs 

Scaffolding 

GFB 

Brick veneer 

Misc. masonry 

Firestopping 


Roofing 







Finishes 

Toilet 

Windows 

Louvers 


Elevator 





Diffusers 




Plumbing 

HVAC 

Electrical 




Page 140 of 264




CSI 

Div. 


Unit Price 

Total Cost 


RAS pumps 





Misc. removal 





Tanks 



Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 



Form columns 

Form beams 


Form parapet 



Rebars 





Page 141 of 264




CSI 

Div. 







Scaffolding 

GFB 

Brick veneer 

Misc. masonry 




Firestopping 


Roofing 






Finishes 




Polymer storage tank 

Polymer blending unit 


Plumbing 

HVAC 

Electrical 

Unit Price 

Total Cost 


Carbon tanks 




Page 142 of 264




CSI 

Div. 


Form walls 

Rebars 




Waterstop 


Carbon tanks 




Tanks Total 

Unit Price 

Total Cost 


$ - $ - $ - $ - 






Excavation 14,064.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 140,648 $ - $ 136,429 $ 277,077 

Backfill 6,622.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 80,135 $ 145,701 $ 64,241 $ 290,077 




Piles 97,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 1,193,160 $ 2,347,200 $ 880,200 $ 4,420,560 



Form walls 69,641.4 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 584,988 $ 250,709 $ 208,924 $ 1,044,621 

Rebars 238.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 491,361 $ 290,788 $ 9,772 $ 791,921 




Page 143 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Waterstop 5,803.4 lf $ 5.0 $ 5.0 $ - $ 10 $ 29,017 $ 29,017 $ - $ 58,034 

















Grand Total $ 45,335,394 $ 57,223,701 $ 12,262,806 $ 114,821,901 


Page 144 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Subtotal: $ 138,934,500 


Subtotal: $ 194,508,300 


Subtotal: $ 206,178,798 


Subtotal: $ 218,549,526 


Grand Total: $ 915,857,349 

Page 145 of 264

CSI 

Div. 






Owl's Head WPCP Membrane Bioreactor 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 2,550,000.0 $ - $ 2,550,000 $ - $ 2,550,000 $ - $ 2,550,000 




O&M Manuals 1.0 LS $ - $ 188,000.0 $ - $ 188,000 $ - $ 188,000 $ - $ 188,000 


MISC ITEMS 


Page 146 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 19,000.0 $ - $ 19,000 $ - $ 19,000 $ - $ 19,000 








DEMOLITION 

Misc. demo 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

Demo FST 1.0 LS $ 3,648,000.0 $ - $ 2,000,000.0 $ 5,648,000 $ 3,648,000 $ - $ 2,000,000 $ 5,648,000 

EARTHWORK 



Excavation 5,000.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 50,000 $ - $ 48,600 $ 98,600 


Backfill 4,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 48,320 $ 88,000 $ 38,640 $ 174,960 





Dredging 227,555.6 cy $ 8.3 $ - $ 7.0 $ 15 $ 1,888,711 $ - $ 1,581,511 $ 3,470,222 

Excavation 227,555.6 cy $ 10.0 $ - $ 9.7 $ 20 $ 2,275,556 $ - $ 2,211,840 $ 4,487,396 


Stone base 45,511.1 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 572,530 $ 901,120 $ 227,556 $ 1,701,205 

Select fill 227,555.6 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 2,748,871 $ 5,006,222 $ 2,198,187 $ 9,953,280 

Grade site 68,266.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 177,493 $ 27,307 $ 20,480 $ 225,280 

DEWATERING 

Page 147 of 264




CSI 

Div. 


Unit Price 

Total Cost 








SITEWORK 












Sodding 2,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 1,280 $ 5,400 $ 140 $ 6,820 






Mixers 








Page 148 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Baffles 


FRP beams 8,580.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 45,474 $ 54,912 $ - $ 100,386 

Mixers 


Mixers 80.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 240,000 $ 1,480,000 $ 16,000 $ 1,736,000 


Mixers Total 

$ 7,231,674 $ 6,527,562 $ 664,325 $ 14,423,561 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 






Page 149 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 


Process air blowers, silencers, etc. 8.0 each $ 25,000.0 $ 1,300,000.0 $ 5,000.0 $ 1,330,000 $ 200,000 $ 10,400,000 $ 40,000 $ 10,640,000 




Diffusers 52,000.0 each $ 50.0 $ 25.0 $ - $ 75 $ 2,600,000 $ 1,300,000 $ - $ 3,900,000 




Plumbing 1.0 LS $ 200,000.0 $ 150,000.0 $ - $ 350,000 $ 200,000 $ 150,000 $ - $ 350,000 

Page 150 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Electrical 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ - $ 2,000,000 $ 1,000,000 $ 1,000,000 $ - $ 2,000,000 




RAS pumps 26.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 37,440 $ 520,000 $ 15,600 $ 573,040 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 



Page 151 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Page 152 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,746,172 $ 3,103,964 $ 510,534 $ 6,360,670 








Excavation 47,040.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 470,400 $ - $ 456,288 $ 926,688 

Backfill 15,680.7 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 189,736 $ 344,975 $ 152,103 $ 686,815 


Page 153 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Piles 66,150.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 807,030 $ 1,587,600 $ 595,350 $ 2,989,980 



Form walls 195,148.8 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 1,639,250 $ 702,536 $ 585,446 $ 2,927,232 

Rebars 435.5 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 897,866 $ 531,359 $ 17,857 $ 1,447,082 


Concrete foundation 3,920.7 cy $ 225.0 $ 96.0 $ 10.0 $ 331 $ 882,158 $ 376,387 $ 39,207 $ 1,297,752 

Concrete walls 3,614.1 cy $ 300.0 $ 96.0 $ 10.0 $ 406 $ 1,084,230 $ 346,954 $ 36,141 $ 1,467,325 



Waterproof membrane 150,494.4 sf $ 7.0 $ 1.0 $ - $ 8 $ 1,053,461 $ 150,494 $ - $ 1,203,955 

Waterstop 6,098.4 lf $ 5.0 $ 5.0 $ - $ 10 $ 30,492 $ 30,492 $ - $ 60,984 

Membrane bio reactors 12.0 each $ 2,000,000.00 $ 4,000,000.00 $ 50,000.00 $ 6,050,000 $ 24,000,000 $ 48,000,000 $ 600,000 $ 72,600,000 

Air scour blower 3.0 each $ 600,000.00 $ 1,200,000.00 $ 50,000.00 $ 1,850,000 $ 1,800,000 $ 3,600,000 $ 150,000 $ 5,550,000 


Odor control system 1.0 LS $ 1,000,000.0 $ 1,000,000.0 $ 50,000.0 $ 2,050,000 $ 1,000,000 $ 1,000,000 $ 50,000 $ 2,050,000 

Methanol tanks 2.0 each $ 300,000.0 $ 500,000.0 $ 25,000.0 $ 825,000 $ 600,000 $ 1,000,000 $ 50,000 $ 1,650,000 



Fine screens 14.0 each $ 500,000.0 $ 1,000,000.0 $ 50,000.0 $ 1,550,000 $ 7,000,000 $ 14,000,000 $ 700,000 $ 21,700,000 









Page 154 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Grand Total $ 106,220,576 $ 164,499,949 $ 19,835,959 $ 290,556,484 


Subtotal: $ 351,573,346 


Subtotal: $ 562,517,353 


Subtotal: $ 596,268,394 


Subtotal: $ 632,044,498 


Grand Total: $ 2,648,656,386 

Page 155 of 264

CSI 

Div. 






Red Hook WPCP Advanced Basic BNR 

Unit Price 

Total Cost 








Clerical (2) 48.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 240,000 $ - $ 240,000 




SUPPORT 











Safety 1.0 LS $ - $ 300,000.0 $ - $ 300,000 $ - $ 300,000 $ - $ 300,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 156 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 




Incidental project requirements 1.0 LS $ - $ 500,000.0 $ - $ 500,000 $ - $ 500,000 $ - $ 500,000 




DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 

Crushed stone base 500.0 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 6,290 $ 9,900 $ 2,500 $ 18,690 

Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 

SITEWORK 

Temporary fencing 500.0 lf $ 1.6 $ 47.0 $ 0.4 $ 49 $ 820 $ 23,500 $ 180 $ 24,500 

Sawcut pavement 500.0 lf $ 1.9 $ 1.3 $ 1.0 $ 4 $ 945 $ 630 $ 495 $ 2,070 

Remove pavement 200.0 sy $ 5.8 $ - $ 3.5 $ 9 $ 1,160 $ - $ 706 $ 1,866 

Concrete curbs 200.0 lf $ 18.0 $ 19.7 $ 4.0 $ 42 $ 3,600 $ 3,940 $ 800 $ 8,340 

New pavement 200.0 sy $ 3.2 $ 29.4 $ 2.8 $ 35 $ 630 $ 5,870 $ 550 $ 7,050 



Electric manholes 4.0 each $ 3,000.0 $ 3,069.0 $ 220.0 $ 6,289 $ 12,000 $ 12,276 $ 880 $ 25,156 

Lightpoles 3.0 each $ 2,640.0 $ 5,175.0 $ 318.0 $ 8,133 $ 7,920 $ 15,525 $ 954 $ 24,399 



Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 



Page 157 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Demolition and Site Construction Total $ 326,661 $ 319,644 $ 173,802 $ 820,107 


Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Odor Control tank covers 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Baffles 


FRP beams 3,630.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 19,239 $ 23,232 $ - $ 42,471 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,586,939 $ 6,015,507 $ 607,888 $ 13,210,334 




Process air blowers, silencers, etc. 1.0 each $ 50,000.0 $ 750,000.0 $ 5,000.0 $ 805,000 $ 50,000 $ 750,000 $ 5,000 $ 805,000 


Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Page 158 of 264




CSI 

Div. 


Unit Price 

Total Cost 





RAS pumps 1.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 1,440 $ 20,000 $ 600 $ 22,040 










Tanks 





Tanks Total 

$ 560,000 $ 608,000 $ 120,000 $ 1,288,000 







Page 159 of 264




CSI 

Div. 


Unit Price 

Total Cost 









Plantwide Electrical 1.0 LS $ 1,047,000.0 $ 976,000.0 $ - $ 2,023,000 $ 1,047,000 $ 976,000 $ - $ 2,023,000 

Plantwide Electrical Work Total $ 1,047,000 $ 976,000 $ - $ 2,023,000 




Grand Total $ 12,041,940 $ 20,049,591 $ 1,393,129 $ 33,484,660 


Subtotal: $ 40,516,439 


Subtotal: $ 56,723,014 


Subtotal: $ 60,126,395 

Page 160 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Subtotal: $ 63,733,979 


Grand Total: $ 225,465,027 

Page 161 of 264

CSI 

Div. 






Red Hook WPCP Full Step BNR 

Unit Price 

Total Cost 








Clerical (2) 60.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 300,000 $ - $ 300,000 




SUPPORT 











Safety 1.0 LS $ - $ 400,000.0 $ - $ 400,000 $ - $ 400,000 $ - $ 400,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 162 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 

SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 



Page 163 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Baffles 


FRP beams 3,630.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 19,239 $ 23,232 $ - $ 42,471 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,586,939 $ 6,015,507 $ 607,888 $ 13,210,334 




Process air blowers, silencers, etc. 2.0 each $ 50,000.0 $ 750,000.0 $ 5,000.0 $ 805,000 $ 100,000 $ 1,500,000 $ 10,000 $ 1,610,000 


Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Page 164 of 264




CSI 

Div. 


Unit Price 

Total Cost 





RAS pumps 1.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 1,440 $ 20,000 $ 600 $ 22,040 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Page 165 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 


Tanks Total 

$ 2,335,594 $ 2,587,737 $ 369,348 $ 5,292,680 

Page 166 of 264




CSI 

Div. 


Unit Price 

Total Cost 




















Page 167 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Grand Total $ 14,602,034 $ 25,862,468 $ 1,697,477 $ 42,161,980 


Subtotal: $ 51,015,995 


Subtotal: $ 71,422,393 


Subtotal: $ 75,707,737 


Subtotal: $ 80,250,201 


Grand Total: $ 296,173,869 

Page 168 of 264

CSI 

Div. 






Red Hook WPCP Full Step BNR with Solids Filtration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 700,000.0 $ - $ 700,000 $ - $ 700,000 $ - $ 700,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 


Page 169 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 




Barge driven cofferdam 16,000.0 sf $ 5.5 $ 20.0 $ 6.3 $ 32 $ 87,200 $ 320,000 $ 100,800 $ 508,000 

Dredging 113,777.8 cy $ 8.3 $ - $ 7.0 $ 15 $ 944,356 $ - $ 790,756 $ 1,735,111 

Excavation 113,777.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 1,137,778 $ - $ 1,105,920 $ 2,243,698 


Stone base 22,755.6 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 286,265 $ 450,560 $ 113,778 $ 850,603 

Select fill 113,777.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 1,374,436 $ 2,503,111 $ 1,099,093 $ 4,976,640 

Grade site 34,133.3 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 88,747 $ 13,653 $ 10,240 $ 112,640 

DEWATERING 


Page 170 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 









Page 171 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Baffles 


FRP beams 4,290.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 22,737 $ 27,456 $ - $ 50,193 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,610,237 $ 6,041,781 $ 609,013 $ 13,261,031 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 






Page 172 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 


Scour air blower 2.0 each $ 25,000.0 $ 500,000.0 $ 5,000.0 $ 530,000 $ 50,000 $ 1,000,000 $ 10,000 $ 1,060,000 




Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Plumbing 1.0 LS $ 100,000.0 $ 100,000.0 $ - $ 200,000 $ 100,000 $ 100,000 $ - $ 200,000 

Page 173 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 1.0 LS $ 200,000.0 $ 200,000.0 $ 50,000.0 $ 450,000 $ 200,000 $ 200,000 $ 50,000 $ 450,000 

Electrical 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 




RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 



Page 174 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Page 175 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 


Excavation 2,461.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 24,613 $ - $ 23,875 $ 48,488 

Backfill 1,159.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 14,024 $ 25,498 $ 11,242 $ 50,763 




Piles 17,150.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 209,230 $ 411,600 $ 154,350 $ 775,180 



Form walls 12,187.2 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 102,373 $ 43,874 $ 36,562 $ 182,809 

Rebars 41.7 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 85,988 $ 50,888 $ 1,710 $ 138,586 




Aluminum cover 6,846.4 sf $ 43.0 $ 55.0 $ 2.1 $ 100 $ 294,394 $ 376,550 $ 14,377 $ 685,321 

Page 176 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Waterstop 1,015.6 lf $ 5.0 $ 5.0 $ - $ 10 $ 5,078 $ 5,078 $ - $ 10,156 

Filters 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 


Piping and misc. equipment 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Deep Sand Filtration Total $ 6,139,813 $ 8,243,621 $ 589,174 $ 14,972,608 















Page 177 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Grand Total $ 36,594,118 $ 51,509,406 $ 8,069,865 $ 96,173,389 


Subtotal: $ 116,369,801 


Subtotal: $ 162,917,721 


Subtotal: $ 172,692,784 


Subtotal: $ 183,054,351 


Grand Total: $ 767,110,667 

Page 178 of 264

CSI 

Div. 






Red Hook WPCP Full Step BNR with Denitrification 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 750,000.0 $ - $ 750,000 $ - $ 750,000 $ - $ 750,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 179 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 113,777.8 cy $ 8.3 $ - $ 7.0 $ 15 $ 944,356 $ - $ 790,756 $ 1,735,111 

Excavation 113,777.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 1,137,778 $ - $ 1,105,920 $ 2,243,698 


Stone base 22,755.6 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 286,265 $ 450,560 $ 113,778 $ 850,603 

Select fill 113,777.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 1,374,436 $ 2,503,111 $ 1,099,093 $ 4,976,640 

Grade site 34,133.3 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 88,747 $ 13,653 $ 10,240 $ 112,640 

DEWATERING 




Page 180 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Page 181 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Baffles 


FRP beams 4,290.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 22,737 $ 27,456 $ - $ 50,193 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,610,237 $ 6,041,781 $ 609,013 $ 13,261,031 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 









Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Page 182 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 






Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Plumbing 1.0 LS $ 100,000.0 $ 100,000.0 $ - $ 200,000 $ 100,000 $ 100,000 $ - $ 200,000 

HVAC 1.0 LS $ 200,000.0 $ 200,000.0 $ 50,000.0 $ 450,000 $ 200,000 $ 200,000 $ 50,000 $ 450,000 

Electrical 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 



Page 183 of 264




CSI 

Div. 


Unit Price 

Total Cost 



RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 




Page 184 of 264




CSI 

Div. 


Unit Price 

Total Cost 









GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Page 185 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 




Excavation 4,922.7 cy $ 10.0 $ - $ 9.7 $ 20 $ 49,227 $ - $ 47,750 $ 96,977 

Backfill 2,318.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 28,047 $ 50,995 $ 22,484 $ 101,527 




Piles 34,250.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 417,850 $ 822,000 $ 308,250 $ 1,548,100 



Form walls 24,374.5 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 204,746 $ 87,748 $ 73,123 $ 365,617 

Rebars 83.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 171,976 $ 101,776 $ 3,420 $ 277,172 







Waterstop 2,031.2 lf $ 5.0 $ 5.0 $ - $ 10 $ 10,156 $ 10,156 $ - $ 20,312 

Filters 8.0 each $ 100,000.00 $ 100,000.00 $ 5,000.00 $ 205,000 $ 800,000 $ 800,000 $ 40,000 $ 1,640,000 

Page 186 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Denitrification Filtration Total $ 8,441,716 $ 11,086,043 $ 843,398 $ 20,371,156 















Grand Total $ 39,241,021 $ 54,827,827 $ 8,324,089 $ 102,392,937 


Page 187 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Subtotal: $ 123,895,454 


Subtotal: $ 173,453,636 


Subtotal: $ 183,860,854 


Subtotal: $ 194,892,505 


Grand Total: $ 816,719,834 

Page 188 of 264

CSI 

Div. 






Red Hook WPCP Full Step BNR with Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 800,000.0 $ - $ 800,000 $ - $ 800,000 $ - $ 800,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 189 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 113,777.8 cy $ 8.3 $ - $ 7.0 $ 15 $ 944,356 $ - $ 790,756 $ 1,735,111 

Excavation 113,777.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 1,137,778 $ - $ 1,105,920 $ 2,243,698 


Stone base 22,755.6 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 286,265 $ 450,560 $ 113,778 $ 850,603 

Select fill 113,777.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 1,374,436 $ 2,503,111 $ 1,099,093 $ 4,976,640 

Grade site 34,133.3 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 88,747 $ 13,653 $ 10,240 $ 112,640 

DEWATERING 




Page 190 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Page 191 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Baffles 


FRP beams 4,290.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 22,737 $ 27,456 $ - $ 50,193 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,610,237 $ 6,041,781 $ 609,013 $ 13,261,031 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 









Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Page 192 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 






Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Plumbing 1.0 LS $ 100,000.0 $ 100,000.0 $ - $ 200,000 $ 100,000 $ 100,000 $ - $ 200,000 

HVAC 1.0 LS $ 200,000.0 $ 200,000.0 $ 50,000.0 $ 450,000 $ 200,000 $ 200,000 $ 50,000 $ 450,000 

Electrical 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 



Page 193 of 264




CSI 

Div. 


Unit Price 

Total Cost 



RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 




Page 194 of 264




CSI 

Div. 


Unit Price 

Total Cost 









GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Page 195 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 






Excavation 22,400.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 224,000 $ - $ 217,280 $ 441,280 

Backfill 7,467.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 90,351 $ 164,274 $ 72,430 $ 327,055 




Piles 31,500.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 384,300 $ 756,000 $ 283,500 $ 1,423,800 



Form walls 92,928.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 780,595 $ 334,541 $ 278,784 $ 1,393,920 

Rebars 207.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 427,555 $ 253,028 $ 8,503 $ 689,087 





Page 196 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Waterstop 2,904.0 lf $ 5.0 $ 5.0 $ - $ 10 $ 14,520 $ 14,520 $ - $ 29,040 

Microfilter equipment 11.0 each $ 100,000.0 $ 100,000.0 $ 5,000.0 $ 205,000 $ 1,100,000 $ 1,100,000 $ 55,000 $ 2,255,000 


Piping and misc. equipment 1.0 LS $ 100,000.0 $ 100,000.0 $ 5,000.0 $ 205,000 $ 100,000 $ 100,000 $ 5,000 $ 205,000 














Grand Total $ 41,276,945 $ 54,983,673 $ 8,956,085 $ 105,216,703 

Page 197 of 264 


Subtotal: $ 127,312,211




CSI 

Div. 


Unit Price 

Total Cost 



Subtotal: $ 178,237,095 


Subtotal: $ 188,931,321 


Subtotal: $ 200,267,200 


Grand Total: $ 839,243,123 

Page 198 of 264

CSI 

Div. 






Red Hook WPCP Solids Filtration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 700,000.0 $ - $ 700,000 $ - $ 700,000 $ - $ 700,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 


Page 199 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 113,777.8 cy $ 8.3 $ - $ 7.0 $ 15 $ 944,356 $ - $ 790,756 $ 1,735,111 

Excavation 113,777.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 1,137,778 $ - $ 1,105,920 $ 2,243,698 


Stone base 22,755.6 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 286,265 $ 450,560 $ 113,778 $ 850,603 

Select fill 113,777.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 1,374,436 $ 2,503,111 $ 1,099,093 $ 4,976,640 

Grade site 34,133.3 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 88,747 $ 13,653 $ 10,240 $ 112,640 

DEWATERING 


Page 200 of 264




CSI 

Div. 


Unit Price 

Total Cost 







SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 


Scaffolding 




Drill dowels 



Page 201 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Handrails 


Baffles 


FRP beams 

Mixers 


Mixers 


Mixers Total 

$ 500,000 $ 500,000 $ 50,000 $ 1,050,000 



Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 





Form parapet 


Rebars 






Page 202 of 264




CSI 

Div. 





Metal deck 

Stairs 

Scaffolding 

GFB 

Brick veneer 

Misc. masonry 

Firestopping 


Roofing 







Finishes 

Toilet 

Windows 

Louvers 


Elevator 


Scour air blower 




Nozzles 




Plumbing 

Unit Price 

Total Cost 


Page 203 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 

Electrical 




RAS pumps 





Misc. removal 





Tanks 



Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 



Form columns 

Form beams 


Form parapet 

Page 204 of 264




CSI 

Div. 




Rebars 










Scaffolding 

GFB 

Brick veneer 

Misc. masonry 




Firestopping 


Roofing 






Finishes 





Plumbing 

HVAC 

Unit Price 

Total Cost 


Page 205 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Electrical 

Carbon tanks 





Form walls 

Rebars 



Waterstop 


Carbon tanks 




Tanks Total 

$ - $ - $ - $ - 


Excavation 2,461.3 cy $ 10.0 $ - $ 9.7 $ 20 $ 24,613 $ - $ 23,875 $ 48,488 

Backfill 1,159.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 14,024 $ 25,498 $ 11,242 $ 50,763 




Piles 17,150.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 209,230 $ 411,600 $ 154,350 $ 775,180 



Form walls 12,187.2 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 102,373 $ 43,874 $ 36,562 $ 182,809 

Rebars 41.7 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 85,988 $ 50,888 $ 1,710 $ 138,586 





Page 206 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Waterstop 1,015.6 lf $ 5.0 $ 5.0 $ - $ 10 $ 5,078 $ 5,078 $ - $ 10,156 

Filters 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 


















Page 207 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Grand Total $ 18,018,743 $ 31,675,890 $ 5,706,151 $ 55,400,784 


Subtotal: $ 67,034,949 


Subtotal: $ 93,848,928 


Subtotal: $ 99,479,864 


Subtotal: $ 105,448,656 


Grand Total: $ 441,894,923 

Page 208 of 264

CSI 

Div. 






Red Hook WPCP Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 800,000.0 $ - $ 800,000 $ - $ 800,000 $ - $ 800,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 209 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 113,777.8 cy $ 8.3 $ - $ 7.0 $ 15 $ 944,356 $ - $ 790,756 $ 1,735,111 

Excavation 113,777.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 1,137,778 $ - $ 1,105,920 $ 2,243,698 


Stone base 22,755.6 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 286,265 $ 450,560 $ 113,778 $ 850,603 

Select fill 113,777.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 1,374,436 $ 2,503,111 $ 1,099,093 $ 4,976,640 

Grade site 34,133.3 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 88,747 $ 13,653 $ 10,240 $ 112,640 

DEWATERING 




Page 210 of 264




CSI 

Div. 


Unit Price 

Total Cost 





SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 


Scaffolding 




Drill dowels 



Handrails 


Page 211 of 264




CSI 

Div. 


Baffles 


FRP beams 

Unit Price 

Total Cost 


Mixers 


Mixers 


Mixers Total 

$ 500,000 $ 500,000 $ 50,000 $ 1,050,000 



Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 





Form parapet 


Rebars 









Metal deck 

Page 212 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Stairs 

Scaffolding 

GFB 

Brick veneer 

Misc. masonry 

Firestopping 


Roofing 







Finishes 

Toilet 

Windows 

Louvers 


Elevator 


Scour air blower 




Nozzles 




Plumbing 

HVAC 

Electrical 



Page 213 of 264




CSI 

Div. 


Unit Price 

Total Cost 



RAS pumps 





Misc. removal 





Tanks 



Excavation 

Backfill 

Crushed stone 


Test piles 

Piles 

Form pile cap 



Form columns 

Form beams 


Form parapet 



Rebars 




Page 214 of 264




CSI 

Div. 








Scaffolding 

GFB 

Brick veneer 

Misc. masonry 




Firestopping 


Roofing 






Finishes 





Plumbing 

HVAC 

Electrical 

Unit Price 

Total Cost 


Carbon tanks 





Page 215 of 264




CSI 

Div. 

Form walls 

Rebars 




Waterstop 


Carbon tanks 




Tanks Total 

Unit Price 

Total Cost 


$ - $ - $ - $ - 






Excavation 22,400.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 224,000 $ - $ 217,280 $ 441,280 

Backfill 7,467.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 90,351 $ 164,274 $ 72,430 $ 327,055 




Piles 31,500.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 384,300 $ 756,000 $ 283,500 $ 1,423,800 



Form walls 92,928.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 780,595 $ 334,541 $ 278,784 $ 1,393,920 

Rebars 207.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 427,555 $ 253,028 $ 8,503 $ 689,087 





Page 216 of 264




CSI 

Div. 


Unit Price 

Total Cost 




Waterstop 2,904.0 lf $ 5.0 $ 5.0 $ - $ 10 $ 14,520 $ 14,520 $ - $ 29,040 

Microfilter equipment 11.0 each $ 100,000.0 $ 100,000.0 $ 5,000.0 $ 205,000 $ 1,100,000 $ 1,100,000 $ 55,000 $ 2,255,000 


Piping and misc. equipment 1.0 LS $ 100,000.0 $ 100,000.0 $ 5,000.0 $ 205,000 $ 100,000 $ 100,000 $ 5,000 $ 205,000 














Grand Total $ 22,701,570 $ 35,151,657 $ 6,592,371 $ 64,445,598 

Page 217 of 264 


Subtotal: $ 77,979,174




CSI 

Div. 


Unit Price 

Total Cost 



Subtotal: $ 109,170,843 


Subtotal: $ 115,721,094 


Subtotal: $ 122,664,359 


Grand Total: $ 514,039,344 

Page 218 of 264

CSI 

Div. 






Red Hook WPCP Membrane Bioreactor 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 1,750,000.0 $ - $ 1,750,000 $ - $ 1,750,000 $ - $ 1,750,000 




O&M Manuals 1.0 LS $ - $ 100,000.0 $ - $ 100,000 $ - $ 100,000 $ - $ 100,000 


MISC ITEMS 


Page 219 of 264




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 10,000.0 $ - $ 10,000 $ - $ 10,000 $ - $ 10,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

Demo FST 1.0 LS $ 3,648,000.0 $ - $ 2,000,000.0 $ 5,648,000 $ 3,648,000 $ - $ 2,000,000 $ 5,648,000 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 113,777.8 cy $ 8.3 $ - $ 7.0 $ 15 $ 944,356 $ - $ 790,756 $ 1,735,111 

Excavation 113,777.8 cy $ 10.0 $ - $ 9.7 $ 20 $ 1,137,778 $ - $ 1,105,920 $ 2,243,698 


Stone base 22,755.6 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 286,265 $ 450,560 $ 113,778 $ 850,603 

Select fill 113,777.8 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 1,374,436 $ 2,503,111 $ 1,099,093 $ 4,976,640 

Grade site 34,133.3 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 88,747 $ 13,653 $ 10,240 $ 112,640 

DEWATERING 

Page 220 of 264




CSI 

Div. 


Unit Price 

Total Cost 








SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 








Page 221 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 


Baffles 


FRP beams 4,290.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 22,737 $ 27,456 $ - $ 50,193 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,610,237 $ 6,041,781 $ 609,013 $ 13,261,031 



Excavation 2,115.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 21,150 $ - $ 20,516 $ 41,666 

Backfill 1,058.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,802 $ 23,276 $ 10,263 $ 46,340 




Piles 20,800.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 253,760 $ 499,200 $ 187,200 $ 940,160 








Rebars 170.6 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 351,667 $ 208,117 $ 6,994 $ 566,779 





Page 222 of 264




CSI 

Div. 


Unit Price 

Total Cost 






Metal deck 28,884.0 sf $ 1.0 $ 3.6 $ 0.1 $ 5 $ 30,039 $ 103,982 $ 2,888 $ 136,910 

Stairs 4.0 flgt $ 15,000.0 $ 5,000.0 $ 1,000.0 $ 21,000 $ 60,000 $ 20,000 $ 4,000 $ 84,000 


GFB 36,824.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 570,772 $ 346,146 $ 88,378 $ 1,005,295 





Roofing 14,276.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 51,394 $ 74,235 $ 8,566 $ 134,194 







Finishes 1.0 LS $ 250,000.0 $ 250,000.0 $ 5,000.0 $ 505,000 $ 250,000 $ 250,000 $ 5,000 $ 505,000 

Toilet 2.0 each $ 5,000.0 $ 5,000.0 $ - $ 10,000 $ 10,000 $ 10,000 $ - $ 20,000 

Windows 1,433.0 sf $ 14.8 $ 35.2 $ - $ 50 $ 21,208 $ 50,442 $ - $ 71,650 

Louvers 2,724.0 sf $ 41.0 $ 36.0 $ - $ 77 $ 111,684 $ 98,064 $ - $ 209,748 


Elevator 1.0 each $ 50,400.0 $ 160,000.0 $ 20,000.0 $ 230,400 $ 50,400 $ 160,000 $ 20,000 $ 230,400 


Process air blowers, silencers, etc. 2.0 each $ 25,000.0 $ 500,000.0 $ 5,000.0 $ 530,000 $ 50,000 $ 1,000,000 $ 10,000 $ 1,060,000 




Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Page 223 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Plumbing 1.0 LS $ 100,000.0 $ 100,000.0 $ - $ 200,000 $ 100,000 $ 100,000 $ - $ 200,000 

HVAC 1.0 LS $ 200,000.0 $ 200,000.0 $ 50,000.0 $ 450,000 $ 200,000 $ 200,000 $ 50,000 $ 450,000 

Electrical 1.0 LS $ 500,000.0 $ 500,000.0 $ - $ 1,000,000 $ 500,000 $ 500,000 $ - $ 1,000,000 




RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 


Page 224 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

Page 225 of 264




CSI 

Div. 


Unit Price 

Total Cost 


HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 








Excavation 22,400.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 224,000 $ - $ 217,280 $ 441,280 

Page 226 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Backfill 7,467.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 90,351 $ 164,274 $ 72,430 $ 327,055 




Piles 31,500.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 384,300 $ 756,000 $ 283,500 $ 1,423,800 



Form walls 92,928.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 780,595 $ 334,541 $ 278,784 $ 1,393,920 

Rebars 207.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 427,555 $ 253,028 $ 8,503 $ 689,087 







Waterstop 2,904.0 lf $ 5.0 $ 5.0 $ - $ 10 $ 14,520 $ 14,520 $ - $ 29,040 

Membrane bio reactors 12.0 each $ 500,000.00 $ 4,000,000.00 $ 50,000.00 $ 4,550,000 $ 6,000,000 $ 48,000,000 $ 600,000 $ 54,600,000 

Air scour blower 3.0 each $ 300,000.00 $ 1,200,000.00 $ 50,000.00 $ 1,550,000 $ 900,000 $ 3,600,000 $ 150,000 $ 4,650,000 


Odor control system 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 

Methanol tanks 2.0 each $ 125,000.0 $ 150,000.0 $ 25,000.0 $ 300,000 $ 250,000 $ 300,000 $ 50,000 $ 600,000 



Fine screens 24.0 each $ 120,000.0 $ 500,000.0 $ 10,000.0 $ 630,000 $ 2,880,000 $ 12,000,000 $ 240,000 $ 15,120,000 







Page 227 of 264




CSI 

Div. 


Unit Price 

Total Cost 






Grand Total $ 52,981,945 $ 124,376,173 $ 12,076,085 $ 189,434,203 


Subtotal: $ 229,215,386 


Subtotal: $ 366,744,617 


Subtotal: $ 388,749,294 


Subtotal: $ 412,074,252 


Grand Total: $ 1,726,845,345 

Page 228 of 264

CSI 

Div. 






Port Richmond WPCP Advanced Basic BNR 

Unit Price 

Total Cost 








Clerical (2) 48.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 240,000 $ - $ 240,000 




SUPPORT 











Safety 1.0 LS $ - $ 300,000.0 $ - $ 300,000 $ - $ 300,000 $ - $ 300,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 229 of 264




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 

SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 



Page 230 of 264




CSI 

Div. 


Unit Price 

Total Cost 





Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Baffles 


FRP beams 4,963.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 26,304 $ 31,763 $ - $ 58,067 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,160,268 $ 5,597,832 $ 561,653 $ 12,319,753 


Misc. demo PA pipe / equipment 1.0 LS $ 150,000.0 $ - $ 50,000.0 $ 200,000 $ 150,000 $ - $ 50,000 $ 200,000 

Misc. modifications to PA system 2,000.0 lnft $ 100.0 $ 300.0 $ 50.0 $ 450 $ 200,000 $ 600,000 $ 100,000 $ 900,000 

Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 






Page 231 of 264




CSI 

Div. 


Unit Price 

Total Cost 



RAS pumps 2.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 2,880 $ 40,000 $ 1,200 $ 44,080 










Tanks 





Tanks Total 

$ 560,000 $ 608,000 $ 120,000 $ 1,288,000 









Page 232 of 264




CSI 

Div. 


Unit Price 

Total Cost 







Plantwide Electrical 1.0 LS $ 1,000,000.0 $ 911,000.0 $ - $ 1,911,000 $ 1,000,000 $ 911,000 $ - $ 1,911,000 

Plantwide Electrical Work Total $ 1,000,000 $ 911,000 $ - $ 1,911,000 


Instrumentation 1.0 LS $ 500,000.0 $ 455,500.0 $ - $ 955,500 $ 500,000 $ 455,500 $ - $ 955,500 

Instrumentation and Controls Total $ 500,000 $ 455,500 $ - $ 955,500 

Grand Total $ 11,496,209 $ 19,304,416 $ 1,232,494 $ 32,033,119 


Subtotal: $ 38,760,074 


Subtotal: $ 54,264,104 


Subtotal: $ 57,519,950 


Subtotal: $ 60,971,147 

Page 233 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Grand Total: $ 215,691,247 

Page 234 of 264

CSI 

Div. 






Port Richmond WPCP Full Step BNR 

Unit Price 

Total Cost 








Clerical (2) 60.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 300,000 $ - $ 300,000 




SUPPORT 











Safety 1.0 LS $ - $ 400,000.0 $ - $ 400,000 $ - $ 400,000 $ - $ 400,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 




Page 235 of 264




CSI 

Div. 


Unit Price 

Total Cost 


ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 

SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 





Page 236 of 264




CSI 

Div. 


Unit Price 

Total Cost 



Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Baffles 


FRP beams 4,963.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 26,304 $ 31,763 $ - $ 58,067 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,160,268 $ 5,597,832 $ 561,653 $ 12,319,753 





Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 




Process Air System Total $ 1,309,400 $ 967,200 $ 330,000 $ 2,606,600 



RAS pumps 2.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 2,880 $ 40,000 $ 1,200 $ 44,080 


Page 237 of 264




CSI 

Div. 


Unit Price 

Total Cost 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 








Page 238 of 264




CSI 

Div. 


Unit Price 

Total Cost 





GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 


Tanks Total 

$ 2,335,594 $ 2,587,737 $ 369,348 $ 5,292,680 






Page 239 of 264




CSI 

Div. 


Unit Price 

Total Cost 















Grand Total $ 13,509,303 $ 23,277,293 $ 1,596,842 $ 38,383,439 


Subtotal: $ 46,443,961 


Subtotal: $ 65,021,545 


Page 240 of 264




CSI 

Div. 


Unit Price 

Total Cost 


Subtotal: $ 68,922,838 


Subtotal: $ 73,058,208 


Grand Total: $ 269,630,877 

Page 241 of 264

CSI 

Div. 






Port Richmond WPCP Full Step BNR with Solids Filtration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 500,000.0 $ - $ 500,000 $ - $ 500,000 $ - $ 500,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 


Page 242 of 263




CSI 

Div. 


Unit Price 

Total Cost 




ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 

SITEWORK 












Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 

Page 243 of 263




CSI 

Div. 


Unit Price 

Total Cost 







Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Baffles 


FRP beams 5,866.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 31,090 $ 37,542 $ - $ 68,632 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,196,910 $ 5,639,087 $ 563,463 $ 12,399,460 





Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 



Page 244 of 263




CSI 

Div. 


Unit Price 

Total Cost 






RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 




Page 245 of 263




CSI 

Div. 


Unit Price 

Total Cost 



Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Page 246 of 263




CSI 

Div. 


Unit Price 

Total Cost 


Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 


Excavation 2,266.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 22,660 $ - $ 21,980 $ 44,640 

Backfill 1,067.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 12,911 $ 23,474 $ 10,350 $ 46,735 




Piles 15,757.5 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 192,242 $ 378,180 $ 141,818 $ 712,239 



Form walls 11,220.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 94,248 $ 40,392 $ 33,660 $ 168,300 

Rebars 38.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 79,164 $ 46,849 $ 1,574 $ 127,587 






Page 247 of 263




CSI 

Div. 


Unit Price 

Total Cost 



Waterstop 935.0 lf $ 5.0 $ 5.0 $ - $ 10 $ 4,675 $ 4,675 $ - $ 9,350 

Filters 1.0 LS $ 500,000.0 $ 500,000.0 $ 50,000.0 $ 1,050,000 $ 500,000 $ 500,000 $ 50,000 $ 1,050,000 



















Page 248 of 263




CSI 

Div. 


Unit Price 

Total Cost 



Grand Total $ 21,132,272 $ 39,263,768 $ 2,356,587 $ 62,752,627 


Subtotal: $ 75,930,679 


Subtotal: $ 106,302,950 


Subtotal: $ 112,681,127 


Subtotal: $ 119,441,995 


Grand Total: $ 500,535,647 

Page 249 of 263

CSI 

Div. 






Port Richmond WPCP Full Step BNR with Denitrification 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 600,000.0 $ - $ 600,000 $ - $ 600,000 $ - $ 600,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 250 of 263




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 56,888.9 cy $ 8.3 $ - $ 7.0 $ 15 $ 472,178 $ - $ 395,378 $ 867,556 

Excavation 56,888.9 cy $ 10.0 $ - $ 9.7 $ 20 $ 568,889 $ - $ 552,960 $ 1,121,849 

Soil disposal 56,888.9 cy $ 38.3 $ 14.0 $ 52 $ 2,178,844 $ - $ 796,444 $ 2,975,289 

Stone base 11,377.8 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 143,132 $ 225,280 $ 56,889 $ 425,301 

Select fill 56,888.9 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 687,218 $ 1,251,556 $ 549,547 $ 2,488,320 

Grade site 17,066.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 44,373 $ 6,827 $ 5,120 $ 56,320 

SITEWORK 




Page 251 of 263




CSI 

Div. 


Unit Price 

Total Cost 










Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Baffles 


FRP beams 5,866.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 31,090 $ 37,542 $ - $ 68,632 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,196,910 $ 5,639,087 $ 563,463 $ 12,399,460 

Page 252 of 263




CSI 

Div. 


Unit Price 

Total Cost 






Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 







RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 


Page 253 of 263




CSI 

Div. 


Unit Price 

Total Cost 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 


Page 254 of 263




CSI 

Div. 


Unit Price 

Total Cost 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 




Excavation 5,665.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 56,650 $ - $ 54,951 $ 111,601 

Backfill 2,667.5 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 32,277 $ 58,685 $ 25,875 $ 116,837 




Piles 39,400.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 480,680 $ 945,600 $ 354,600 $ 1,780,880 

Page 255 of 263




CSI 

Div. 


Unit Price 

Total Cost 




Form walls 28,050.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 235,620 $ 100,980 $ 84,150 $ 420,750 

Rebars 96.0 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 197,909 $ 117,123 $ 3,936 $ 318,968 







Waterstop 2,337.5 lf $ 5.0 $ 5.0 $ - $ 10 $ 11,688 $ 11,688 $ - $ 23,375 

Filters 8.0 each $ 100,000.0 $ 100,000.0 $ 5,000.0 $ 205,000 $ 800,000 $ 800,000 $ 40,000 $ 1,640,000 




Denitrification Filtration Total $ 9,273,948 $ 12,065,332 $ 934,179 $ 22,273,459 










Page 256 of 263




CSI 

Div. 


Unit Price 

Total Cost 







Grand Total $ 29,625,626 $ 46,383,189 $ 5,163,255 $ 81,172,070 


Subtotal: $ 98,218,205 


Subtotal: $ 137,505,487 


Subtotal: $ 145,755,816 


Subtotal: $ 154,501,165 


Grand Total: $ 647,455,199 

Page 257 of 263

CSI 

Div. 






Port Richmond WPCP Full Step BNR with Microfiltration 

Unit Price 

Total Cost 








Clerical (2) 96.0 mnth $ - $ 5,000.0 $ - $ 5,000 $ - $ 480,000 $ - $ 480,000 




SUPPORT 











Safety 1.0 LS $ - $ 650,000.0 $ - $ 650,000 $ - $ 650,000 $ - $ 650,000 




O&M Manuals 1.0 LS $ - $ 50,000.0 $ - $ 50,000 $ - $ 50,000 $ - $ 50,000 


MISC ITEMS 



Page 258 of 263




CSI 

Div. 


Unit Price 

Total Cost 



ID badges 1.0 LS $ - $ 5,000.0 $ - $ 5,000 $ - $ 5,000 $ - $ 5,000 








DEMOLITION 

Misc. demo 1.0 LS $ 45,600.0 $ - $ 50,000.0 $ 95,600 $ 45,600 $ - $ 50,000 $ 95,600 

EARTHWORK 



Excavation 2,500.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 25,000 $ - $ 24,300 $ 49,300 


Backfill 2,000.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 24,160 $ 44,000 $ 19,320 $ 87,480 





Dredging 56,888.9 cy $ 8.3 $ - $ 7.0 $ 15 $ 472,178 $ - $ 395,378 $ 867,556 

Excavation 56,888.9 cy $ 10.0 $ - $ 9.7 $ 20 $ 568,889 $ - $ 552,960 $ 1,121,849 

Soil disposal 56,888.9 cy $ 38.3 $ 14.0 $ 52 $ 2,178,844 $ - $ 796,444 $ 2,975,289 

Stone base 11,377.8 cy $ 12.6 $ 19.8 $ 5.0 $ 37 $ 143,132 $ 225,280 $ 56,889 $ 425,301 

Select fill 56,888.9 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 687,218 $ 1,251,556 $ 549,547 $ 2,488,320 

Grade site 17,066.7 sy $ 2.6 $ 0.4 $ 0.3 $ 3 $ 44,373 $ 6,827 $ 5,120 $ 56,320 

SITEWORK 




Page 259 of 263




CSI 

Div. 


Unit Price 

Total Cost 










Sodding 1,000.0 sy $ 0.6 $ 2.7 $ 0.1 $ 3 $ 640 $ 2,700 $ 70 $ 3,410 






Mixers 









Handrails 15,000.0 lf $ 20.0 $ 150.0 $ 2.0 $ 172 $ 300,000 $ 2,250,000 $ 30,000 $ 2,580,000 

Baffles 


FRP beams 5,866.0 lf $ 5.3 $ 6.4 $ - $ 12 $ 31,090 $ 37,542 $ - $ 68,632 

Mixers 


Mixers 90.0 each $ 3,000.0 $ 18,500.0 $ 200.0 $ 21,700 $ 270,000 $ 1,665,000 $ 18,000 $ 1,953,000 


Mixers Total 

$ 6,196,910 $ 5,639,087 $ 563,463 $ 12,399,460 

Page 260 of 263




CSI 

Div. 


Unit Price 

Total Cost 






Nozzles 688.0 each $ 50.0 $ 25.0 $ - $ 75 $ 34,400 $ 17,200 $ - $ 51,600 







RAS pumps 5.0 each $ 1,440.0 $ 20,000.0 $ 600.0 $ 22,040 $ 7,200 $ 100,000 $ 3,000 $ 110,200 










Tanks 



Excavation 1,058.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 10,580 $ - $ 10,263 $ 20,843 

Backfill 353.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 4,271 $ 7,766 $ 3,424 $ 15,461 




Piles 13,200.0 lf $ 12.2 $ 24.0 $ 9.0 $ 45 $ 161,040 $ 316,800 $ 118,800 $ 596,640 


Page 261 of 263




CSI 

Div. 


Unit Price 

Total Cost 





Form beams 1,566.0 sf $ 14.9 $ 2.8 $ 3.4 $ 21 $ 23,333 $ 4,385 $ 5,324 $ 33,043 





Rebars 49.8 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 102,730 $ 60,796 $ 2,043 $ 165,568 











GFB 9,982.0 sf $ 15.5 $ 9.4 $ 2.4 $ 27 $ 154,721 $ 93,831 $ 23,957 $ 272,509 








Roofing 4,236.0 sf $ 3.6 $ 5.2 $ 0.6 $ 9 $ 15,250 $ 22,027 $ 2,542 $ 39,818 






Finishes 1.0 LS $ 250,000.0 $ 75,000.0 $ 5,000.0 $ 330,000 $ 250,000 $ 75,000 $ 5,000 $ 330,000 


Page 262 of 263




CSI 

Div. 


Unit Price 

Total Cost 





Plumbing 1.0 LS $ 15,000.0 $ 15,000.0 $ - $ 30,000 $ 15,000 $ 15,000 $ - $ 30,000 

HVAC 1.0 LS $ 125,000.0 $ 120,000.0 $ 5,000.0 $ 250,000 $ 125,000 $ 120,000 $ 5,000 $ 250,000 

Electrical 1.0 LS $ 130,000.0 $ 120,000.0 $ - $ 250,000 $ 130,000 $ 120,000 $ - $ 250,000 

Carbon tanks 





Form walls 4,309.0 sf $ 8.4 $ 3.6 $ 3.0 $ 15 $ 36,196 $ 15,512 $ 12,927 $ 64,635 

Rebars 15.4 tons $ 2,061.5 $ 1,220.0 $ 41.0 $ 3,323 $ 31,747 $ 18,788 $ 631 $ 51,167 



Waterstop 139.0 lf $ 3.1 $ 11.6 $ - $ 15 $ 428 $ 1,610 $ - $ 2,038 






Tanks Total 

$ 2,871,172 $ 3,280,964 $ 560,534 $ 6,712,670 






Excavation 6,798.0 cy $ 10.0 $ - $ 9.7 $ 20 $ 67,980 $ - $ 65,941 $ 133,921 

Backfill 3,201.0 cy $ 12.1 $ 22.0 $ 9.7 $ 44 $ 38,732 $ 70,422 $ 31,050 $ 140,204 

Page 263 of 263

MWH/Hazen & Sawyer 

A Joint Venture

NYCDEPCostAnalys isReport-0607 .pdf - New York-New Jersey ...

Create successful ePaper yourself

Delete template?

Save as template?