Technologies and Costs for Removal of Arsenic From Drinking Water

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The costs in both the April 1999 Technology and Cost Document (1) and the November 1999Technology and Cost Document (2) utilize models based on nitrate removal. The Water Model wasone of the cost models used for small systems with design flows less than 1 mgd. Sulfateconcentrations for this model were between 50 and 100 mg/L. The November 1999 Technology andCost Document listed the design criteria for large systems (> 1 mgd) using the W/W model. Thesulfate concentration was 80 mg/L and the nitrate concentration was 100 mg/L. It was not possibleto modify the sulfate concentration in either of these two models. It was determined that the existingcost models could not be used to estimate costs for anion exchange options with sulfate at or below50 mg/L.Design Assumptions: Capital CostsThe following assumptions were made to estimate the capital cost of anion exchange. Thebasis for these assumptions are provided in Appendix E.1. Empty Bed Contact Time (EBCT) = 2.5 minutes per column2. The estimated cost of the anion exchange resin was $125/ft 3 for all system sizes.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.4. The vessel cost has been sized based on 50% bed expansion during backwash. The vesselvolume was calculated as (1.5)(media volume).5. The vessel cost is based on the following equation:Cost = 63.288 * (Vessel Volume in gallons) ^ 0.6793-48
6. The capital costs include a redundant column to allow the system to operate while the mediais being regenerated in the other column.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.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.9. The capital costs have been estimated from the total process costs using a factor of 2.5 forsmall systems and 3.33 for large systems.10. The capital costs estimated in the previous step do not include the cost of a building to housethe process equipment and other add-on costs related to the site. Housing costs were assumedfor all sites. Fence and road were only assumed for those systems that have no treatment.Table 3-13 (above) shows the assumptions made for this analysis regarding the percentage ofsystems with no treatment in place.11. The equation for process area, which is the key variable in estimating the costs for buildings,roads, and fences has been based on the design flow of the system. The equation used forprocess area is:Process Area = 118.7 * Design Flow + 11812. The building cost to house the anion exchange system is $45.38/sq ft for design flows at orbelow 0.65 mgd. The following equation is used for design flows between 0.65 and 1 mgd:Building cost = 54.204 * Process Area + 148873-49
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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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Page 69 and 70: 3.0 TECHNOLOGY COSTS3.1 INTRODUCTIO
Page 71 and 72: included in the estimates presented
Page 73 and 74: Table 3-3Water Model Capital Cost B
Page 75 and 76: 3.2.3 Implementing TDP Recommended
Page 77 and 78: sources. The September 1998 index v
Page 79 and 80: Amortization, or capital recovery,
Page 81 and 82: 3.3 ADDITIONAL CAPITAL COSTSThe cos
Page 83 and 84: PilotingThe Technology Design Panel
Page 85 and 86: The 1993 Technology and Cost Docume
Page 87 and 88: cause disinfection by-product (DBP)
Page 89 and 90: Figure 3-1Pre-oxidation - 1.5 mg/L
Page 91 and 92: 3.6 PRECIPITATIVE PROCESSES3.6.1 Co
Page 93 and 94: enhanced coagulation treatment plan
Page 95 and 96: Figure 3-4Enhanced Coagulation/Filt
Page 97 and 98: Small Systems (Less than 1 mgd)The
Page 99 and 100: Figure 3-6Coagulation Assisted Micr
Page 101 and 102: 3.6.6 Enhanced Lime SofteningEnhanc
Page 103 and 104: Figure 3-8Enhanced Lime SofteningO&
Page 105 and 106: 3. Empty Bed Contact Time (EBCT) is
Page 107 and 108: For design flows greater than 1 mgd
Page 109 and 110: Figure 3-9Activated AluminaCapital
Page 111 and 112: Figure 3-11Activated Alumina (pH 8
Page 113 and 114: Figure 3-13Activated Alumina (pH Ad
Page 115: 3.7.2 Granular Ferric HydroxideGran
Page 119 and 120: Figure 3-15Bed Volumes to Arsenic B
Page 121 and 122: Figure 3-17Anion Exchange (< 20 mg/
Page 123 and 124: Figure 3-19Anion Exchange (20-50 mg
Page 125 and 126: quality feed stream and often requi
Page 127 and 128: Figure 3-20Greensand FiltrationCapi
Page 129 and 130: 3.11 COMPARISON OF COSTSThe April 1
Page 131 and 132: 4.0 RESIDUALS HANDLING AND DISPOSAL
Page 133 and 134: mechanical dewatering processes. Wh
Page 135 and 136: Storage lagoons are best suited for
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Page 139 and 140: 4.3.3 Dewatered Sludge Land Applica
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Page 145 and 146: The solids content of the backwash
Page 147 and 148: carbonate hardness removal produces
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Page 151 and 152: 4.4.10 Reverse OsmosisReverse osmos
Page 153 and 154: Figure 4-1Anion Exchange (< 20 mg/L
Page 155 and 156: Figure 4-3Anion Exchange (20-50 mg/
Page 161 and 162: Figure 4-9Activated Alumina (pH 7 -
Page 163 and 164: Figure 4-11Activated Alumina (pH Ad
Page 165 and 166: 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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Table C10.1 - Base Costs Obtained f
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APPENDIX D: BASIS FOR REVISED ACTIV
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Company case study is 18 minutes (2
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egressed against their respective v
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costs for small systems is as follo
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were based on $40/sq ft). The proce
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Basis. Capital cost components incl
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The source water at Plant D has the
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equation y = (2*10 -8 )x 2 + 0.0002
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The maximum run length is 18,500 be
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Since the available arsenic capacit
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If the first column can be operated
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which includes lighting, ventilatio
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disposal costs, if needed, are cove
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Appendix EBasis for Revised Anion E
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2. The estimated cost of the anion
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9. The capital costs have been esti
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Thus, the cost of a road and fence
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length when sulfate is at or below
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the labor rates for both large and
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2. US EPA. Technologies and Costs f
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Technologies and Costs for Removal of Arsenic From Drinking Water

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