Technologies and Costs for Removal of Arsenic From Drinking Water

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Table B8.1 - Base Costs Obtained from the Water Model for Package Lime SofteningCost ComponentDesign Capacity (gpd)Capital Cost15,000 150,000 430,000 750,000 1,000,000 CategoryExcavation & Sitework $3,500 $5,800 $6,700 $8,400 $9,800 cManufactured Equipment $33,200 $49,800 $66,300 $86,200 $103,800 pConcrete $1,100 $2,500 $3,200 $5,900 $7,000 pLabor $14,000 $18,200 $28,000 $36,400 $43,800 cPipes and Valves $5,200 $10,400 $14,100 $16,700 $45,900 pElectrical $8,500 $12,200 $17,000 $18,900 $26,700 pHousing $8,800 $16,400 $19,800 $30,000 $33,000 pSubtotal $74,300 $115,300 $155,100 $202,500 $270,000Contingencies $11,100 $17,300 $23,300 $30,400 $40,500 cTotal $85,400 $132,600 $178,400 $232,900 $310,500Table B8.2 - Water Model Base Construction Cost Analysis for Package Lime SofteningCost Component15,000 150,000Design Capacity (gpd)Average430,000 750,000 1,000,000 PercentExcavation & Sitework 4.10% 4.37% 3.76% 3.61% 3.16% 3.80%Manufactured Equipment 38.88% 37.56% 37.16% 37.01% 33.43% 36.81%Concrete 1.29% 1.89% 1.79% 2.53% 2.25% 1.95%Labor 16.39% 13.73% 15.70% 15.63% 14.11% 15.11%Pipes and Valves 6.09% 7.84% 7.90% 7.17% 14.78% 8.76%Electrical 9.95% 9.20% 9.53% 8.12% 8.60% 9.08%Housing 10.30% 12.37% 11.10% 12.88% 10.63% 11.46%Contingencies 13.00% 13.05% 13.06% 13.05% 13.04% 13.04%Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%International Consultants, Inc.Contract 68-C6-0039 B-8February 1999Water Model Capital Cost Breakdown
Table B9.1 - Base Costs Obtained from the Water Model for Permanganate FeedCost ComponentMaximum Feed Rate (lb/day)Capital Cost0.5-5 12.5 25 50 125 250 CategoryDissolving Tank $290 $430 $640 $910 $1,830 $2,200 pMixer $180 $200 $200 $240 $410 $620 pMetering Pump $430 $700 $750 $1,230 $1,600 $1,670 pPipes and Valves $180 $180 $220 $220 $280 $280 pLabor $180 $180 $240 $260 $300 $330 cElectrical $80 $100 $150 $200 $250 $300 pSubtotal $1,340 $1,790 $2,200 $3,060 $4,670 $5,400Contingencies $200 $270 $330 $460 $700 $810 cTotal $1,540 $2,060 $2,530 $3,520 $5,370 $6,210Table B9.2 - Water Model Base Construction Cost Analysis for Permanganate FeedCost Component0.5-5 12.5Maximum Feed Rate (lb/day)Average25 50 125 250 PercentExcavation & Sitework 18.83% 20.87% 25.30% 25.85% 34.08% 35.43% 26.73%Manufactured Equipment 11.69% 9.71% 7.91% 6.82% 7.64% 9.98% 8.96%Concrete 27.92% 33.98% 29.64% 34.94% 29.80% 26.89% 30.53%Labor 11.69% 8.74% 8.70% 6.25% 5.21% 4.51% 7.52%Pipes and Valves 11.69% 8.74% 9.49% 7.39% 5.59% 5.31% 8.03%Electrical 5.19% 4.85% 5.93% 5.68% 4.66% 4.83% 5.19%Contingencies 12.99% 13.11% 13.04% 13.07% 13.04% 13.04% 13.05%Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%International Consultants, Inc.Contract 68-C6-0039 B-9February 1999Water Model Capital Cost Breakdown
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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
Page 153 and 154: Figure 4-1Anion Exchange (< 20 mg/L
Page 155 and 156: Figure 4-3Anion Exchange (20-50 mg/
Page 157 and 158: Figure 4-5Coagulation Assisted Micr
Page 159 and 160: Figure 4-7Coagulation Assisted Micr
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
Page 167 and 168: 5.0 POINT-OF-ENTRY/POINT-OF-USE TRE
Page 169 and 170: chromatographic peaking, which occu
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Page 173 and 174: Manufacturer and laboratory data su
Page 175 and 176: Figure 5-2POU Reverse OsmosisO&M Co
Page 177 and 178: # Installation time - 1 hour unskil
Page 179 and 180: Figure 5-3POU Activated AluminaTota
Page 181 and 182: 6.0 REFERENCESAmy, G.L. and P. Bran
Page 183 and 184: Cooperative Research Centres for Wa
Page 185 and 186: Fuller, C.C., J.A. Davis, G.W. Zell
Page 187 and 188: Le, X.C., and M. Ma (1998). “Dete
Page 189 and 190: Scott, K., J. Green, H.D. Do and S.
Page 191: Appendix AVery Small Systems Capita
Page 194 and 195: Table A4 - VSS Document Capital Cos
Page 197 and 198: Table B1.1 - Base Costs Obtained fr
Page 203: Table B7.1 - Base Costs Obtained fr
Page 207 and 208: Table B11.1 - Base Costs Obtained f
Page 209 and 210: Table B13.1 - Base Costs Obtained f
Page 211: Appendix CW/W Cost Model Capital Co
Page 214 and 215: Table C2.1 - Base Costs Obtained fr
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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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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