Technologies and Costs for Removal of Arsenic From Drinking Water

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For design flows greater than 1 mgd, the building cost varied based on flow from $100 to $90per square foot.Basis. The data from both the Very Small Systems Document and the Water Model wereexamined to develop housing costs for the activated alumina system. The housing rate listedin the Very Small Systems Document was $40/sq ft (10). This rate includes the following:basic storage building, foundation, electrical wiring, HVAC, and plumbing. The rate is fora pre-fabricated building installed on a concrete slab. The rate is based on data from prefabricatedbuilding manufacturers and the 1993 Means Building Construction Cost Data forstorage buildings multiplied by a conversion factor for small-sized buildings. The housingcosts in the Water Model vary based on size with rates ranging from $87/sq ft for the smallestconceptual design and $50/sq ft for a facility treating approximately 1 mgd (6). The onlydocumentation on the costs in the Water Model states that in lieu of segregating building costsinto several components, the housing category represents all material and labor costsassociated with the building, including heating, ventilating, lighting, and normal convenienceoutlets. However, the fabrication and building type are unknown and, most critically, thesources used to derive the building costs are unknown. The costs in the Water Model weredeveloped in 1983. The ENR Building Cost Index was used to update both sets of costs toSeptember 1998. The housing rate from the Very Small Systems Document was selectedbased on better documentation and the use of more recent data for design flows up to 0.65mgd. For design flows between 0.65 and 1 mgd, a linear regression of housing cost againstprocess area was used to derive the equation listed above. For design flows greater than1mgd, the building cost rate assumptions were the same as those used in the for AlbuquerqueReport (7) and for the case studies in the AwwaRF Report (4).D.2.1Capital Costs - pH Adjustment15. For two options, pH adjustment to the optimal pH 6 is utilized. The capital cost equation forthe pH adjustment module is:Capital cost = 40517 * Design Flow + 31889D-10
Basis. Capital cost components include piping, acid and caustic metering pumps, and storagetanks for the acid and caustic. For the metering pumps, pH controllers, pH sensors, and levelsensors are included in the costs. Cost data for each of the components were obtained frommanufacturers for design flows ranging from 0.1 to 3 mgd. Capital costs were estimated bymultiplying the total process cost by 2.5 or 3.33 depending upon size(8). The Phoenix casestudy in the AwwaRF report provides the only realistic comparison for disposable activatedalumina at optimal pH (4). The other case studies are based regeneration and would use acidand caustic for those purposes. A design flow of 0.2 mgd was evaluated in both the Phoenixcase study and the process cost estimate used to derive the above equation. The process costestimate of $16,200 is very similar to the process cost from the Phoenix case study of $16,750.D.2.1Operation and Maintenance CostsThere are three major components to the operation and maintenance (O&M) costs -replacement media, energy and labor.16. The critical variable in calculating the replacement media costs is the run length - the numberof bed volumes until the effluent concentration exceeds a specific concentration. The runlength for the natural pH range of 7 # pH < 8 is 10,000 bed volumes (BV). The run length forthe natural pH range of 8 # pH # 8.3 is 5,200 BV. These run lengths are used to estimate thereplacement of the activated alumina in half of the active columns.Basis. The full-scale systems in New Hampshire serve as the basis for the run lengths for thenatural pH options (3). Plant C data were used for the range of 7 # pH < 8 and data from PlantD were used for the range of 8 # pH # 8.3.D-11
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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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Table B1.1 - Base Costs Obtained fr
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Table B3.1 - Base Costs Obtained fr
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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: were based on $40/sq ft). The proce
Page 255 and 256: The source water at Plant D has the
Page 257 and 258: equation y = (2*10 -8 )x 2 + 0.0002
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
Page 265 and 266: which includes lighting, ventilatio
Page 267 and 268: disposal costs, if needed, are cove
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Page 272 and 273: 2. The estimated cost of the anion
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Page 280 and 281: the labor rates for both large and
Page 282 and 283: 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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