Technologies and Costs for Removal of Arsenic From Drinking Water

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Basis. The Water Model provided construction cost estimates for a variety of conceptualdesigns (6). 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 conceptual designs are based on anEBCT of 7.5 minutes. Since this design is using a total EBCT of 10 minutes (two 5-minEBCTs in series), the activated alumina costs were adjusted to estimate the contribution ofeach component to the construction cost. The weighted percentage of each component wascalculated for both EBCT values. The weighted percentages for concrete, pipe and valves andelectrical and instrumentation were then expressed as a percentage of the manufacturedequipment and activated alumina costs. This was done for the data with an EBCT of 10minutes. Concrete was 3.17%, pipe and valves were 15.18%, and electrical andinstrumentation were 11.12% of the equipment and media costs. However, the designs in theWater Model include pipes, valves, and instrumentation for the sulfuric acid and sodiumhydroxide feed systems in the regeneration process. Those are not needed in this design.Therefore, the pipe and valves percentage has been reduced by a factor of 2. The electricaland instrumentation were reduced by a factor of 3 because pH sensors and alarms are notneeded and the electrical needs are drastically reduced. The main electrical components ofthe activated alumina process in the Water Model are day tank mixers and pumps used forregeneration and the electrical immersion heater for the sodium hydroxide tank. None of thesecomponents are needed in this design. The adjusted cost factor is 14.43%. The other processcosts were calculated by multiplying the adjusted factor by the sum of the manufacturedequipment and activated alumina costs. The sum of the other process costs and themanufactured equipment and activated alumina costs is the total process costs. For the designswith pH adjustment, a separate module has been developed including pipes and valves forthose chemical feed systems.11. 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.Basis. The capital costs have been estimated from the process equipment costs using the ratioin the Guide for Implementing Phase I Water Treatment Cost Upgrades (8). The process costswere assumed to be 40% of the capital costs for small systems. The breakdown of capitalD-6
costs for small systems is as follows: 40% process costs, 40% construction costs, and 20%engineering costs. For large systems, the breakdown of capital cost is: 30% process costs,40% construction, and 30% engineering.12. 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.Basis. Data from the 1995 Community Water Systems Survey were used to identify thepercentage of systems without treatment (9). The data from ground water systems is asfollows:Table D-1Percentage of Ground Water Systems with No Treatment: Systems Serving # 3,300 PeoplePopulation Category25 - 100 101 - 500 501 - 1,000 1,001 - 3,30043% 19% 16% 18%Table D-2Percentage of Ground Water Systems with No Treatment: Systems Serving > 3,300 PeoplePopulation Category3,301 - 10,000 10,001 - 50,000 50,001 - 100,000 100,001 - 1 MIL13% 1% 11% 0%Larger ground water systems rely on multiple entry points to supply ground water rather thanone well. Thus, treatment may be present in the system, but only at one of the wells. Since theanalysis is based on no treatment throughout the system, using the percentages for largerD-7
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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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Page 209 and 210: Table B13.1 - Base Costs Obtained f
Page 211: Appendix CW/W Cost Model Capital Co
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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: egressed against their respective v
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 261 and 262: Since the available arsenic capacit
Page 263 and 264: If the first column can be operated
Page 265 and 266: which includes lighting, ventilatio
Page 267 and 268: disposal costs, if needed, are cove
Page 269: Appendix EBasis for Revised Anion E
Page 272 and 273: 2. The estimated cost of the anion
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Page 276 and 277: Thus, the cost of a road and fence
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Page 280 and 281: the labor rates for both large and
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