Technologies and Costs for Removal of Arsenic From Drinking Water

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2.6.5 Photo-OxidationResearchers at the Australian Nuclear Science and Technology Organisation (ANSTO) havefound that in the presence of light and naturally occurring light-absorbing materials, the oxidation rateof As(III) by oxygen can be increased ten-thousandfold (Cooperative Research Centres for WasteManagement and Pollution Control Limited, 1999). The oxidized arsenic, now As(V), can then beeffectively removed by co-precipitation.ANSTO evaluated both UV lamp reactors and sunlight-assisted-photo-oxidation using acidic,metal-bearing water from an abandoned gold, silver, and lead mine. Air sparging was required forsunlight-assisted oxidation due to the high initial As(III) concentration (12 mg/L). Tests demonstratedthat near complete oxidation of As(III) can be achieved using the photochemical process. Analysisof process waters showed 97% of the arsenic in the process stream was present as As(V).Researchers also concluded that As(III) was preferentially oxidized in the presence of excessdissolved Fe(II) (22:1 iron to arsenic mole ratio). This is a contrast to conventional plants wheredissolved Fe(II) represents an extra chemical oxidant demand which has to be satisfied duringoxidation of As(III) (CRC-WMPC, 1999).Photo-oxidation of the mine water followed by co-precipitation was able to reduce arsenicconcentrations to as low as 17 Fg/L, which meets the current MCL for arsenic. Initial total arsenicconcentrations were unknown, though the As(III) concentration was given as approximately 12 mg/L,which is considerably higher than typical raw water arsenic concentrations. ANSTO reportedresiduals from this process are environmentally stable and passed the Toxicity Characteristic LeachingProcedure (TCLP) test necessary to declare waste non-hazardous and suitable for landfill disposal.Based on the removals achieved and residuals characteristics, it is expected that photooxidationfollowed by co-precipitation would be an effective arsenic removal technology. However,this technology is still largely experimental and should be further evaluated before recommendationas an approved arsenic removal technology for drinking water.2-48
3.0 TECHNOLOGY COSTS3.1 INTRODUCTIONThis chapter presents estimated capital and operations and maintenance (O&M) expendituresfor the following arsenic removal technologies and unit processes:# Pre-oxidation technologies - chlorination;# Precipitative processes, including coagulation assisted microfiltration, enhancedcoagulation/filtration, and enhanced lime softening;# Adsorption processes, specifically activated alumina;# Ion exchange processes, specifically anion exchange;The next sections provide an overview of how the costs of each technology is estimated. Thesections following include a brief description of the technology, design criteria, and capital and O&Mcost curves for systems with design flows ranging from 0.01 to 430 mgd.3.2 BASIS FOR COST ESTIMATES3.2.1 Cost ModelingThree models were used to develop costs: the Very Small Systems Best AvailableTechnology Cost Document (Malcolm Pirnie, 1993), hereafter referred to as the VSS model; theWater Model (Culp/Wesner/Culp, 1984); and the W/W Cost Model (Culp/Wesner/Culp, 1994). Themodels were used for the following flow ranges; linear trends are used in the transition betweenmodels:# VSS - 0.015 to 0.100 mgd# Transition 1 - 0.100 to 0.270 mgd# Water Model - 0.27 to 1.00 mgd# Transition 2 - 1 to 10 mgd# W/W Cost Model - 10 to 200 mgd3-1
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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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Page 23 and 24: ends up as ferric hydroxide. In alu
Page 25 and 26: Optimization Hierarchy for Coagulat
Page 27 and 28: Substantial arsenic removal has bee
Page 29 and 30: Vickers et al. (1997) reported that
Page 31 and 32: 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
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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
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Page 59 and 60: TABLE 2-10Arsenic Removal with RO a
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Page 63 and 64: 2.6 ALTERNATIVE TECHNOLOGIES2.6.1 I
Page 65 and 66: 20 mg As per gram of iron was remov
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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
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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
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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 4-5Coagulation 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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