Technologies and Costs for Removal of Arsenic From Drinking Water

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2. The estimated cost of the anion exchange resin was $125/ft 3 for all system sizes.Basis. The November 1999 Technology and Cost Document (2) recommended this cost basedon costs at existing ion exchange facilities and conversations with suppliers. The case studycosts in the AwwaRF Document (4) use a range of $110/ft 3 at 1 mgd to $90/ft 3 at 30 mgd.3. The bed depth assumption ranged from 3 feet to 6 feet depending upon the design flow. Themaximum diameter per column was 12 feet. When the calculated media volume exceeded themaximum, the treatment media was divided into several beds to maintain a realistic beddiameter. Thus, larger designs include multiple anion exchange columns, each treating aportion of the total flow.Basis. The costs for the activated alumina used this approach (6).4. The vessel cost has been sized based on 50% bed expansion during backwash. The vesselvolume was calculated as (1.5)(media volume).Basis. The Water Model used 50% bed expansion to size the vessel (3).5. The vessel cost is based on the following equation:Cost = 63.288 * (Vessel Volume in gallons) ^ 0.679Basis. Quotes were obtained from two manufacturers for glass-lined carbon steel vessels withworking pressure rating between 75 and 150 psi and meeting American Society of MechanicalEngineers (ASME) Code Section VIII requirements. Sizes ranging from 140 gallons to 6764gallons were used to develop the equation. Vessel costs for sixteen different sizes wereregressed against their respective volumes to derive the equation.E-2
6. The capital costs include a redundant column to allow the system to operate while the mediais being regenerated in the other column.Basis. A redundant vessel has been included for each anion exchange column. While the anionexchange column is being regenerated, the other column can produce drinking water.Redundant columns were not included at either of the two full-scale arsenic anion exchangeplants (5).7. The other equipment cost elements are the brine tank, brine pump and mixer. Costs for thebrine tank were based on 30-day storage. Separate costs were prepared for the two sulfateranges based on the number of regenerations per month.Basis. Brine tank costs were based on the salt needed to perform regenerations every 1500bed volumes and 700 bed volumes over a 30 day period. Cost data from RS Means“Environmental Remediation Cost Data” on plastic storage tanks were used to develop thebrine tank costs (7). Data from this source were also used for the brine pump costs. Amanufacturer cost estimate was used for the brine mixer.8. The remaining components of the process equipment include concrete, pipe and valves andelectrical and instrumentation. A cost factor of 25.02% of the manufactured equipment andactivated alumina was used for these other construction cost components.Basis. The Water Model provided construction cost estimates for a variety of conceptualdesigns (3). Construction cost components included process costs such as manufacturedequipment and media, concrete, pipes and valves, electrical and instrumentation as well asconstruction costs such as excavation and sitework. The weighted percentages for concrete,pipe and valves and electrical and instrumentation were expressed as a percentage of themanufactured equipment costs. Resin costs were included in the manufactured equipmentcosts. Concrete was 7.32%, steel was 9.51%, pipe and valves were 3.02%, and electricaland instrumentation were 5.16% of the equipment costs. The total was 25.02%.E-3
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United StatesEnvironmental Protecti
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ACKNOWLEDGMENTSThis document was pr
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2.5.7 Reverse Osmosis .............
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5.0 POINT-OF-ENTRY/POINT-OF-USE TRE
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LIST OF FIGURES2-1 Pressure Driven
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LIST OF ACRONYMSAAAWWAAWWARFBLSBVC/
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POUpoint-of-useppbparts per billion
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# Alternative treatment processes s
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ends up as ferric hydroxide. In alu
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Optimization Hierarchy for Coagulat
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Substantial arsenic removal has bee
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Vickers et al. (1997) reported that
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was reduced to 0.05 mg/L when the i
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Field StudiesSurveys of lime soften
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Effect of pHpH may have significant
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RegenerationRegeneration of AA beds
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een developed provide important inf
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applicability of IX at a particular
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TABLE 2-1Typical IX Resins for Arse
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solution strength. Arsenic elutes r
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2.4.12 Typical Design ParametersThr
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2.5.2 Important Factors for Membran
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arsenic size distribution to correl
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AWWARF (1998) also performed UF pil
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presumably due to changes in electr
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RO performance is adversely affecte
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TABLE 2-10Arsenic Removal with RO a
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eversal is the decreased potential
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2.6 ALTERNATIVE TECHNOLOGIES2.6.1 I
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20 mg As per gram of iron was remov
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The most significant weakness of th
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3.0 TECHNOLOGY COSTS3.1 INTRODUCTIO
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included in the estimates presented
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Table 3-3Water Model Capital Cost B
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3.2.3 Implementing TDP Recommended
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sources. The September 1998 index v
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Amortization, or capital recovery,
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3.3 ADDITIONAL CAPITAL COSTSThe cos
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PilotingThe Technology Design Panel
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The 1993 Technology and Cost Docume
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cause disinfection by-product (DBP)
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Figure 3-1Pre-oxidation - 1.5 mg/L
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3.6 PRECIPITATIVE PROCESSES3.6.1 Co
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enhanced coagulation treatment plan
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Figure 3-4Enhanced Coagulation/Filt
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Small Systems (Less than 1 mgd)The
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Figure 3-6Coagulation Assisted Micr
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3.6.6 Enhanced Lime SofteningEnhanc
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Figure 3-8Enhanced Lime SofteningO&
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3. Empty Bed Contact Time (EBCT) is
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For design flows greater than 1 mgd
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Figure 3-9Activated AluminaCapital
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Figure 3-11Activated Alumina (pH 8
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Figure 3-13Activated Alumina (pH Ad
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3.7.2 Granular Ferric HydroxideGran
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6. The capital costs include a redu
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Figure 3-15Bed Volumes to Arsenic B
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Figure 3-17Anion Exchange (< 20 mg/
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Figure 3-19Anion Exchange (20-50 mg
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quality feed stream and often requi
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Figure 3-20Greensand FiltrationCapi
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3.11 COMPARISON OF COSTSThe April 1
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4.0 RESIDUALS HANDLING AND DISPOSAL
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mechanical dewatering processes. Wh
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Storage lagoons are best suited for
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the current Industrial Pretreatment
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4.3.3 Dewatered Sludge Land Applica
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usually determined by the Paint Fil
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for arsenic toxicity by a substanti
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The solids content of the backwash
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carbonate hardness removal produces
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Domestic sewage means untreated san
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4.4.10 Reverse OsmosisReverse osmos
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Figure 4-1Anion Exchange (< 20 mg/L
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Figure 4-3Anion Exchange (20-50 mg/
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Figure 4-9Activated Alumina (pH 7 -
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Figure 4-11Activated Alumina (pH Ad
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Figure 4-13Greensand FiltrationWast
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5.0 POINT-OF-ENTRY/POINT-OF-USE TRE
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chromatographic peaking, which occu
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5.3.1 Case Study 1: Fairbanks, Alas
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Manufacturer and laboratory data su
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Figure 5-2POU Reverse OsmosisO&M Co
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# Installation time - 1 hour unskil
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Figure 5-3POU Activated AluminaTota
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6.0 REFERENCESAmy, G.L. and P. Bran
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Cooperative Research Centres for Wa
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Fuller, C.C., J.A. Davis, G.W. Zell
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Le, X.C., and M. Ma (1998). “Dete
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Scott, K., J. Green, H.D. Do and S.
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Appendix AVery Small Systems Capita
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Table A4 - VSS Document Capital Cos
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Table B1.1 - Base Costs Obtained fr
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Table B11.1 - Base Costs Obtained f
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Table B13.1 - Base Costs Obtained f
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Appendix CW/W Cost Model Capital Co
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Table C2.1 - Base Costs Obtained fr
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Page 222 and 223: Table C10.1 - Base Costs Obtained f
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Page 243 and 244: APPENDIX D: BASIS FOR REVISED ACTIV
Page 245 and 246: Company case study is 18 minutes (2
Page 247 and 248: egressed against their respective v
Page 249 and 250: costs for small systems is as follo
Page 251 and 252: were based on $40/sq ft). The proce
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Page 255 and 256: The source water at Plant D has the
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Page 263 and 264: If the first column can be operated
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