Technologies and Costs for Removal of Arsenic From Drinking Water

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11. 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 shows the assumptions made for this analysis regarding the percentage of systemswith no treatment in place. (See Appendix D for further information on these percentages.)Table 3-13Assumed Percentage of Ground Water Systems with No TreatmentPopulation CategoryPercentage of GWS w/o any Treatment25 - 100 43%101 - 500 19%501 - 1,000 16%1,001 - 3,300 18%3,301 - 10,000 18%10,001 - 50,000 18%50,001 - 100,000 18%100,001 - 1 MIL 18%12. 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 = 726.6 * Design Flow + 5913. The building cost to house the activated alumina 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 + 148873-38
For design flows greater than 1 mgd, the building cost varied based on flow from $100 to $90per square foot.Design Assumptions: Capital Costs with pH AdjustmentFor two options, the water pH is adjusted to the optimal pH of 6. The capital cost equationfor the pH adjustment module, which includes post-treatment corrosion control is given by thefollowing equation (Appendix D provides additional information):Capital cost = 40517 * Design Flow + 31889Design Assumptions: O&M Costs with and without pH AdjustmentThere are three major components to the operation and maintenance (O&M) costs -replacement media, energy and labor.1. The critical variable in calculating the replacement media costs is the run length - the numberof bed volumes until the effluent concentration exceeds a specific concentration. The runlength for the natural pH range of 7 # pH < 8 is 10,000 bed volumes (BV). The run length forthe natural pH range of 8 # pH # 8.3 is 5,200 BV. These run lengths are used to estimate thereplacement of the activated alumina in half of the active columns.2. The O&M costs were calculated at 2 run lengths when pH is adjusted to pH of 6. The two runlengths that were selected for the optimal pH of 6 are 15,400 and 23,100 BV.3. Chemical costs also are incurred to adjust the pH. The following equation was used forchemical costs for pH adjustment:Chemical cost (pH adjustment) = 81361* Average Flow + 151.74. The second major component in the O&M costs is incremental labor cost. Incremental laboris the labor associated with the additional maintenance that comes with a new process.3-39
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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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Page 59 and 60: TABLE 2-10Arsenic Removal with RO a
Page 61 and 62: eversal is the decreased potential
Page 63 and 64: 2.6 ALTERNATIVE TECHNOLOGIES2.6.1 I
Page 65 and 66: 20 mg As per gram of iron was remov
Page 67 and 68: The most significant weakness of th
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: 3. Empty Bed Contact Time (EBCT) is
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 and 116: 3.7.2 Granular Ferric HydroxideGran
Page 117 and 118: 6. The capital costs include a redu
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
Page 141 and 142: usually determined by the Paint Fil
Page 143 and 144: for arsenic toxicity by a substanti
Page 145 and 146: The solids content of the backwash
Page 147 and 148: carbonate hardness removal produces
Page 149 and 150: Domestic sewage means untreated san
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/
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Figure 4-5Coagulation Assisted Micr
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Figure 4-7Coagulation Assisted Micr
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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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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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