Technologies and Costs for Removal of Arsenic From Drinking Water

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Table C4.1 - Base Costs Obtained from the WATERCO$T Model for Chemical Sludge PumpingCost ComponentCapacity (gpm)Capital Cost20 100 500 1,000 5,000 10,000 CategoryExcavation & Sitework $470 $600 $810 $970 $1,840 $2,220 cManufactured Equipment $4,370 $6,230 $8,210 $10,390 $23,320 $38,440 pConcrete $1,500 $2,210 $3,220 $4,100 $9,270 $12,310 pSteel $1,510 $2,130 $3,120 $3,940 $8,640 $11,070 pLabor $5,280 $8,060 $12,880 $17,400 $47,850 $64,720 cPipes and Valves $2,560 $4,570 $10,870 $18,190 $42,810 $79,060 pElectrical $6,290 $7,390 $7,880 $9,380 $10,380 $12,510 pHousing $5,880 $5,880 $5,880 $8,100 $8,100 $11,700 pContingencies $4,180 $5,560 $7,930 $10,870 $22,830 $34,800 cTotal $32,040 $42,630 $60,800 $83,340 $175,040 $266,830Table C4.2 - WATERCO$T Model Base Construction Cost Analysis for Chemical Sludge PumpingCost ComponentCapacity (gpm)Average20 100 500 1,000 5,000 10,000 PercentExcavation & Sitework 1.47% 1.41% 1.33% 1.16% 1.05% 0.83% 1.21%Manufactured Equipment 13.64% 14.61% 13.50% 12.47% 13.32% 14.41% 13.66%Concrete 4.68% 5.18% 5.30% 4.92% 5.30% 4.61% 5.00%Steel 4.71% 5.00% 5.13% 4.73% 4.94% 4.15% 4.78%Labor 16.48% 18.91% 21.18% 20.88% 27.34% 24.26% 21.51%Pipes and Valves 7.99% 10.72% 17.88% 21.83% 24.46% 29.63% 18.75%Electrical 19.63% 17.34% 12.96% 11.26% 5.93% 4.69% 11.97%Housing 18.35% 13.79% 9.67% 9.72% 4.63% 4.38% 10.09%Contingencies 13.05% 13.04% 13.04% 13.04% 13.04% 13.04% 13.04%Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%International Consultants, Inc.Contract 68-C6-0039 C-4February 1999W/W Cost Model Capital Cost Breakdown
Table C5.1 - Base Costs Obtained from the WATERCO$T Model for ChlorinationCost ComponentChlorine Feed Capacity (lb/day)Capital Cost10 500 1,000 2,000 5,000 10,000 CategoryManufactured Equipment $6,760 $21,630 $41,630 $65,950 $76,780 $114,360 pLabor $820 $2,610 $5,030 $7,960 $9,270 $13,810 cPipes and Valves $540 $1,710 $3,300 $5,230 $6,080 $9,060 pElectrical $770 $2,450 $4,710 $7,460 $8,690 $12,940 pHousing $2,430 $18,360 $27,760 $46,550 $100,440 $186,490 pContingencies $1,700 $7,010 $12,360 $19,970 $30,190 $50,500 cTotal $13,020 $53,770 $94,790 $153,120 $231,450 $387,160Table C5.2 - WATERCO$T Model Base Construction Cost Analysis for ChlorinationCost ComponentChlorine Feed Capacity (lb/day)Average10 500 1,000 2,000 5,000 10,000 PercentManufactured Equipment 51.92% 40.23% 43.92% 43.07% 33.17% 29.54% 40.31%Labor 6.30% 4.85% 5.31% 5.20% 4.01% 3.57% 4.87%Pipes and Valves 4.15% 3.18% 3.48% 3.42% 2.63% 2.34% 3.20%Electrical 5.91% 4.56% 4.97% 4.87% 3.75% 3.34% 4.57%Housing 18.66% 34.15% 29.29% 30.40% 43.40% 48.17% 34.01%Contingencies 13.06% 13.04% 13.04% 13.04% 13.04% 13.04% 13.04%Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%International Consultants, Inc.Contract 68-C6-0039 C-5February 1999W/W Cost 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
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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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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 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
Page 253 and 254: Basis. Capital cost components incl
Page 255 and 256: The source water at Plant D has the
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Page 259 and 260: The maximum run length is 18,500 be
Page 261 and 262: Since the available arsenic capacit
Page 263 and 264: If the first column can be operated
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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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