Technologies and Costs for Removal of Arsenic From Drinking Water

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two technologies. Redundancy for the lower cost components would be covered by the conservativeassumptions used in deriving the capital costs.Recommended Standards for Water Works (Great Lakes Upper Mississippi River Board ofState Public Health and Environmental Managers, 1997), often referred to as the Ten State Standards,presents a comprehensive discussion of redundancy and recommended redundant items for watertreatment facilities in those States. Systems may incur additional costs if additional redundant itemsare required by the State.3.4 COSTS FOR MULTIPLE REMOVAL PERCENTAGESCapital and O&M cost estimates are presented for the maximum achievable removal in thisdocument. Table 3-12 presents a removal technology matrix which identifies maximum removalpercentages for the technologies for which costs have been estimated. Costs for facilities requiringless than the maximum removal to meet the arsenic MCL target, can be estimated using the blendingapproach discussed in Section 3.4.2.3.4.1 Removal and Accessory CostsBoth the April 1999 and the November 1999 drafts of the Technology and Cost Documentincluded costs for accessories in Appendix D. Accessory costs included raw and finished waterpumping, and clearwell storage. Removal costs include any process item directly associated with theremoval of a particular contaminant, e.g., the ion exchange bed in ion exchange processes. Inclusionof accessory costs was not based on a recommendation of the Technical Design Panel. A detailedexamination of Section 3.11 of the November 1999 Technology and Cost Document revealed theapparent source of the accessory costs. Section 3.11 compared the costs in the November 1999Technology and Cost Document with the costs from the 1993 Technology and Cost Document(Malcolm Pirnie, 1993a) and Evaluation of Central Treatment Options as Small System ComplianceTechnologies (SAIC, 1999). There is a statement in bold at the end of Section 3.11.1 that states thatthe 1993 estimates are greater than the 1999 estimates for many technologies. It further states that thisis because the 1993 estimates included accessory costs; i.e., raw and finished water pumping andclearwell storage.3-16
The 1993 Technology and Cost Document was examined to determine why the accessory costswere included for each technology. After examining the costs in this document, accessory costs, suchas clearwell storage, were only included for one technology - coagulation/filtration. This isunderstandable because coagulation/filtration would not be installed solely for arsenic removal. Thistechnology would likely be selected by surface water systems, especially since the surface watertreatment rule (SWTR) had only promulgated only recently before the 1993 Technology and CostDocument was prepared. Surface water systems would need the clearwell storage for disinfectioncredit under the SWTR. The costs for lime softening in the 1993 Technology and Cost Documentspecifically state that clearwell storage is not included. Costs were also not included for anionexchange or activated alumina. Therefore, cost estimates presented in this document do notinclude accessory capital and O&M.Table 3-12Treatment Technology Maximum Achievable Removal PercentagesTreatment TechnologyMaximum PercentRemovalCoagulation/Filtration 95Enhanced Coagulation/Filtration 1 95Coagulation Assisted Microfiltration 90Lime Softening (pH > 10.5) 90Enhanced Lime Softening 1 (pH > 10.5) 90Ion Exchange (sulfate < 50 mg/L) 95Activated Alumina 95Reverse Osmosis >95Greensand Filtration (20:1 iron:arsenic) 80POU Activated Alumina 90POU Ion Exchange 901 - Enhanced processes assume the existing plant can achieve 50 percent removal without modification. Processenhancements result in the balance to achieve the maximum removal. For example, an existingcoagulation/filtration facility can achieve 50 percent removal. Process enhancements result in an additional 45percent removal, for a total removal of 95 percent.3-17
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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
Page 33 and 34: Field StudiesSurveys of lime soften
Page 35 and 36: Effect of pHpH may have significant
Page 37 and 38: RegenerationRegeneration of AA beds
Page 39 and 40: een developed provide important inf
Page 41 and 42: applicability of IX at a particular
Page 43 and 44: TABLE 2-1Typical IX Resins for Arse
Page 45 and 46: solution strength. Arsenic elutes r
Page 47 and 48: 2.4.12 Typical Design ParametersThr
Page 49 and 50: 2.5.2 Important Factors for Membran
Page 51 and 52: arsenic size distribution to correl
Page 53 and 54: AWWARF (1998) also performed UF pil
Page 55 and 56: presumably due to changes in electr
Page 57 and 58: RO performance is adversely affecte
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: PilotingThe Technology Design Panel
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 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
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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 4-5Coagulation 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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