EPA/600/R-08/140
December 2008
Arsenic Removal from Drinking Water by Adsorptive Media
U.S. EPA Demonstration Project at Desert Sands MDWCA, NM
Final Performance Evaluation Report
by
Abraham S.C. Chen
Christopher T. Coonfare
Lili Wang
Anbo Wang
Battelle
Columbus, OH 43201-2693
Contract No. 68-C-00-185
Task Order No. 0019
for
Thomas J. Sorg
Task Order Manager
Water Supply and Water Resources Division
National Risk Management Research Laboratory
Cincinnati, OH 45268
National Risk Management Research Laboratory
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, OH 45268
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DISCLAIMER
The work reported in this document is funded by the United States Environmental Protection Agency
(EPA) under Task Order 0019 of Contract 68-C-00-185 to Battelle. It has been subjected to the Agency's
peer and administrative reviews and has been approved for publication as an EPA document. Any
opinions and expressed in this paper are those of the author(s) and do not, necessarily, reflect the official
positions and policies of the EPA. Any mention of products or trade names does not constitute
recommendation for use by the EPA.
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FOREWORD
The U.S. Environmental Protection Agency (EPA) is charged by Congress with protecting the Nation's
land, air, and water resources. Under a mandate of national environmental laws, the Agency strives to
formulate and implement actions leading to a compatible balance between human activities and the ability
of natural systems to support and nurture life. To meet this mandate, EPA's research program is
providing data and technical support for solving environmental problems today and building a science
knowledge base necessary to manage our ecological resources wisely, understand how pollutants affect
our health, and prevent or reduce environmental risks in the future.
The National Risk Management Research Laboratory (NRMRL) is the Agency's center for investigation
of technological and management approaches for preventing and reducing risks from pollution that
threaten human health and the environment. The focus of the Laboratory's research program is on
methods and their cost-effectiveness for prevention and control of pollution to air, land, water, and
subsurface resources; protection of water quality in public water systems; remediation of contaminated
sites, sediments and ground water; prevention and control of indoor air pollution; and restoration of
ecosystems. NRMRL collaborates with both public and private sector partners to foster technologies that
reduce the cost of compliance and to anticipate emerging problems. NRMRL's research provides
solutions to environmental problems by: developing and promoting technologies that protect and improve
the environment; advancing scientific and engineering information to support regulatory and policy
decisions; and providing the technical support and information transfer to ensure implementation of
environmental regulations and strategies at the national, state, and community levels.
This publication has been produced as part of the Laboratory's strategic long-term research plan. It is
published and made available by EPA's Office of Research and Development to assist the user
community and to link researchers with their clients.
Sally Gutierrez, Director
National Risk Management Research Laboratory
in
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ABSTRACT
This report documents the activities performed and the results obtained for the arsenic removal treatment
technology demonstration project at the Desert Sands Mutual Domestic Water Consumers Association
(MDWCA) facility in Anthony, NM. The objectives of the project were to evaluate 1) the effectiveness
of Severn Trent Services' (STS) Arsenic Package Unit-300 (APU-300) SORB 33™ media in removing
arsenic to meet the new arsenic maximum contaminant level (MCL) of 10 |o,g/L, 2) the reliability of the
treatment system, 3) the simplicity of required system operation and maintenance (O&M) and operator
skill levels, and 4) the cost-effectiveness of the technology. The project also characterized water in the
distribution system and process residuals produced by the treatment system.
SORB 33™ media is an iron-based adsorptive media developed by Bayer AG and marketed by STS.
Two media runs were conducted in the performance study, with the first utilizing the granular form of the
media (-S) and the second utilizing the pelletized form (-P). According to the vendor, SORB 33™-P is
an improved version of the granular form (SORB 33™-S) and has more robust physical integrity. The
two forms of media have the same composition, but a different bulk density and media particle size
distribution.
The APU-300 system consisted of two 63-in-diameter, 86-in-tall pressure vessels in parallel
configuration. Each pressure vessel initially contained 80 ft3 of SORB 33™-S media or 62 ft3 of
SORB 33™-P media. The adsorptive media were supported by a gravel underbed. Based on a design
flowrate of 320 gal/min (gpm), empty bed contact times (EBCTs) for the system were 3.7 and 2.9 min, for
the SORB 33™ -S and -P media, respectively. Hydraulic loading to each vessel based on the design
flowrate was 7.4 gpm/ft2.
The first media run operated from January 16, 2004 through July 14, 2005, treating approximately
52,645,000 gal of water based on totalizer readings from each vessel. The APU-300 system operated
6.2 hr/day with an average flowrate of 271 gpm. The second media run operated from July 29, 2005
through August 16, 2006, and treated approximately 46,553,000 gal of water based on totalizer readings
from each vessel. The APU-300 system operated 7.8 hr/day with an average flowrate of 251 gpm. The
EBCTs ranged from 3.1 to 7.5 min for the first media run, and from 2.5 to 6.2 min for the second.
Breakthrough of total arsenic at concentration above the 10 (ig/L target MCL occurred at approximately
40,600 bed volumes (BV) during the first media run, representing approximately 62% of the vendor-
estimated working capacity of 66,000 BV. During the second media run, breakthrough of arsenic
occurred at approximately 49,500 BV, representing about 58% of the estimated working capacity of
85,200 BV.
During the study, total arsenic concentrations in source water ranged from 18.6 to 30.1 (ig/L with As(III)
comprising a significant portion of the total soluble arsenic with concentrations ranging from 17.6 to
25.2 (ig/L. Prechlorination was effective in oxidizing As(III) to As(V), as evident by the low As(III)
concentrations (i.e., averaged 2.0 |o,g/L) in water sampled immediately after prechlorination. Total and
free chlorine residuals measured before and after the adsorption vessels were at the equivalent levels of
0.4 to 0.8 mg/L (as C12) and 0.3 to 1.0 mg/L (as C12), respectively, indicating little or no chlorine
consumption by the SORB 33™ media. Concentrations of iron, manganese, silica, orthophosphate, and
other ions in raw water were not high enough to impact arsenic removal by the media.
Backwash wastewater contained soluble arsenic concentrations ranging from 6.4 to 22.2 (ig/L, and
averaging 13.3 (ig/L. The average soluble arsenic concentration was lower than that in raw water,
indicating removal of some soluble arsenic by the media during backwash. Soluble iron and soluble
IV
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manganese concentrations ranged from <25 to 373 and 1.8 to 27.1 (ig/L, respectively. As expected, total
arsenic, iron, and manganese concentrations were considerably higher than soluble concentrations,
indicating the presence of particulate metals in the backwash wastewater. Particulate As might be
associated with either iron particles intercepted by the media beds during the service cycle or the media
fines. Based on the total suspended solid (TSS) values, approximately 9.1 Ib of suspended solid was
produced in 10,000 gal of backwash wastewater from both vessels during each backwash event.
The spent media passed the Toxicity Characteristic Leaching Procedure (TCLP) test for all Resource
Conservation and Recovery Act (RCRA) metals, with only barium showing detectable concentrations
ranging from 0.61 to 0.76 mg/L. The average arsenic loading on the spent media as analyzed by
inductively coupled plasma-mass spectrometry (ICP-MS) was 2.2 mg/g or 0.22% on SORB 33™-S
media and 1.6 mg/g or 0.16% on SORB 33™-P media. These loadings compared well with the average
adsorptive capacities, i.e., 2.1 and 1.7 mg/g, respectively, as calculated by dividing the area between the
influent and effluent breakthrough curves by the amount of dry media in each vessel.
Distribution system water samples were collected to determine any impact of arenic treatment on the lead
and copper levels and water chemistry in the distribution system. Comparison of the distribution system
sampling results before and after the operation of the APU-300 system showed a decrease in arsenic
concentrations (from 22.4 to 28.2 (ig/L to 1.8 to 19.0 (ig/L) at all three sampling locations. However, the
concentrations measured at the distribution system were higher than those in the system effluent. This
likely was due to the blending with untreated water produced by a separate well in the distribution system.
Neither lead nor copper concentrations at the sample sites appear to have been affected by the operation
of the system.
The capital investment cost of $153,000 included $112,000 for equipment, $23,000 for site engineering,
and $18,000 for installation. Using the system's rated capacity of 320 gpm, the capital cost was
$478/gpm of design capacity and the equipment-only cost was $350/gpm of design capacity. These
calculations did not include the cost of a building addition to house the treatment system. The unit
annualized capital cost was $0.09/1,000 gal, assuming the system operated 24 hours a day, 7 days a week,
at the system design flowrate of 320 gpm for 20 years at 7% interest. The system operated only 7 hr/day
on average, producing 40,395,000 gal of water per year. At this reduced usage rate, the unit annualized
capital cost increased to $0.37/1,000 gal.
The O&M cost of the APU-300 system was estimated at $0.74/1,000 gal, which included media
replacement and disposal, chemical supply, electricity consumption, and labor. Because the incremental
costs for chemical supply and electricity were negligible, only media replacement and disposal and O&M
labor would impact O&M costs.
The APU-300 system experienced excessive flow restriction, unbalanced flow, and/or elevated pressure
differential across the adsorption vessels and the entire system during the first four months of system
operation. After extensive on-site and off-site investigations and hydraulic testing, the system was
retrofitted in May 2004 and, thus, able to operate according to the original design specifications.
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CONTENTS
DISCLAIMER ii
FOREWORD iii
ABSTRACT iv
FIGURES vii
TABLES vii
ABBREVIATIONS AND ACRONYMS ix
ACKNOWLEDGMENTS xi
1.0 INTRODUCTION 1
1.1 Background 1
1.2 Treatment Technologies for Arsenic Removal 1
1.3 Project Objectives 2
2.0 SUMMARY AND CONCLUSIONS 3
3.0 MATERIALS AND METHODS 5
3.1 General Project Approach 5
3.2 System O&M and Cost Data Collection 6
3.3 Sample Collection Procedures and Schedules 7
3.3.1 Source Water 7
3.3.2 Treatment Plant Water 7
3.3.3 Backwash Wastewater 7
3.3.4 Residual Solids 9
3.3.5 Distribution System Water 11
3.4 Sampling Logistics 11
3.4.1 Preparation of Arsenic Speciation Kits 12
3.4.2 Preparation of Sampling Coolers 12
3.4.3 Sample Shipping and Handling 12
3.5 Analytical Procedures 12
4.0 RESULTS AND DISCUSSION 14
4.1 Facility Description 14
4.1.1 Pre-existing System 14
4.1.2 Source Water Quality 14
4.1.3 Distribution System 17
4.2 Treatment Process Description 19
4.3 System Installation 23
4.3.1 Permitting 23
4.3.2 Building Construction 24
4.3.3 System Installation, Shakedown, and Startup 24
4.4 System Operation 27
4.4.1 System Retrofit 27
4.4.2 Operational Parameters 30
4.4.3 Media Loss and Breakdown 34
4.4.4 Backwash 35
4.4.5 Media Changeout 37
4.4.6 Residual Management 37
4.4.7 System Operation Reliability and Simplicity 37
4.5 System Performance 38
VI
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4.5.1 Treatment Plant Sampling 38
4.5.2 Backwash Wastewater Sampling 47
4.5.3 Spent Media Sampling 49
4.5.4 Distribution System Water Sampling 50
4.6 System Cost 52
4.6.1 Capital Cost 52
4.6.2 O&MCost 54
5.0 REFERENCES 57
APPENDIX A: OPERATIONAL DATA A-l
APPENDIX B: ANALYTICAL RESULTS B-l
FIGURES
Figure 3-1. Process Flow Diagram and Sampling Locations 10
Figure 3-2. Apparatus Used for Spent Media Sampling 11
Figure 4-1. Map of the Desert Sands MDWCA Service Area 15
Figure 4-2. Well No. 3 (Left) and In-Line Sand Separator (Center) Adjacent to Pump House
(Right) at Desert Sands MDWCA Site 16
Figure 4-3. Piping Inside Pump House at Desert Sands MDWCA Site 16
Figure 4-4. Sodium hypochlorite (NaOCl) Injection System at Desert Sands MDWCA Site 17
Figure 4-5. Schematic Diagram of STS APU-3 00 System after System Retrofit in May 2004 21
Figure 4-6. Treatment Process Components 23
Figure 4-7. Backwash Wastewater Discharge into Pond 24
Figure 4-8. Pump House (right) and System Enclosure 25
Figure 4-9. APU-300 System Being Connected to Distribution System 25
Figure 4-10. APU-300 System before Building Enclosure was Built 26
Figure 4-11. Media Loading to Adsorption Vessels 26
Figure 4-12. Schematic Diagram of STS APU-300 System before System Retrofit 30
Figure 4-13. Flowrate Measurements for First (Left) and Second (Right) Media Runs 33
Figure 4-14. Differential Pressure across Vessels A and B during First (Left) and Second (Right)
Media Runs 33
Figure 4-15. Throughput Between Backwash Events During First (Top) and Second (Bottom)
Media Runs 36
Figure 4-16. Concentrations of Arsenic Species at Wellhead, After Chlorination, and After
Combined Effluent 43
Figure 4-17. Total Arsenic Breakthrough Curves 44
Figure 4-18. Total Manganese Concentrations Over Time 45
Figure 4-19. Media Replacement and O&M Cost for APU-300 System 56
TABLES
Table 1-1. Summary of Round 1 Arsenic Removal Demonstration Sites 2
Table 3-1. Predemonstration Study Activities and Completion Dates 5
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities 6
Table 3-3. Sample Collection Schedule and Analyses 8
Table 4-1. Desert Sands MDWCA Well No. 3 Water Quality Data 18
vn
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Table 4-2. Desert Sands MDWCA Distribution System Water Quality Data 19
Table 4-3. Physical and Chemical Properties of SORB 33™ Media 20
Table 4-4. Design Specifications of APU-300 System 22
Table 4-5. Demonstration Study Activities and Completion Dates 27
Table 4-6. Results of Hydraulic Testing of STS APU-300 Systems 29
Table 4-7. Summary of APU-300 System Operation 31
Table 4-8. Freeboard Measurements and Media Loss 34
Table 4-9. Particle Size Distribution of Granular Media before System Startup and during
First Media Run 35
Table 4-10. Summary of Arsenic, Iron, and Manganese Analytical Results for First and Second
Media Runs 40
Table 4-11. Summary of Water Quality Parameter Measurements 41
Table 4-12. Backwash Wastewater Sampling Results 48
Table 4-13. Backwash Solids Total Metal Analysis 49
Table 4-14. TCLP Results of Spent Media 50
Table 4-15. Spent Media Total Metal Analysis 51
Table 4-16. Summary of SORB 33™ Media Adsorptive Capacities 51
Table 4-17. Distribution System Sampling Results 53
Table 4-18. Capital Investment for APU-300 System 54
Table 4-19. O&M Costs for APU-300 System 55
Vlll
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ABBREVIATIONS AND ACRONYMS
Ap differential pressure
AAL American Analytical Laboratories
Al aluminum
AM adsorptive media
APU arsenic package unit
As arsenic
bgs below ground surface
BV bed volume(s)
C/F coagulation/filtration
Ca calcium
C12 chlorine
CRF capital recovery factor
Cu copper
DO dissolved oxygen
EBCT empty bed contact time
EPA U.S. Environmental Protection Agency
F fluoride
Fe iron
FRP fiberglass reinforced plastic
GFH granular ferric hydroxide
gpd gallons per day
gpm gallons per minute
HOPE high-density polyethylene
ICP-MS inductively coupled plasma-mass spectrometry
ID identification
IX ion exchange
LCR (EPA) Lead and Copper Rule
MCL maximum contaminant level
MDL method detection limit
MDWCA Mutual Domestic Water Consumers Association
Mg magnesium
mg/L milligrams per liter
|o,g/L micrograms per liter
Mn manganese
Mo molybdenum
mV millivolts
IX
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Na sodium
NA not available
NaOCl sodium hypochlorite
NMED New Mexico Environmental Department
NTU nephelometric turbidity unit
O&M operation and maintenance
ORD Office of Research and Development
ORP oxidation-reduction potential
P&ID piping and instrumentation diagram
Pb lead
PLC programmable logic controller
psi pounds per square inch
PO4 orthophosphate
PVC polyvinyl chloride
QA quality assurance
QA/QC quality assurance/quality control
QAPP Quality Assurance Project Plan
RCRA Resource Conservation and Recovery Act
RPD relative percent difference
Sb antimony
SDWA Safe Drinking Water Act
SiO2 silica
SM system modification
SO4 sulfate
SOC synthetic organic compound
STMGID South Truckee Meadows General Improvement District
STS Severn Trent Services
TBD
TCLP
TDS
TOC
TSS
V
voc
to be determined
Toxicity Characteristic Leaching Procedure
total dissolved solids
total organic carbon
total suspended solids
vanadium
volatile organic compound
WRWC
White Rock Water Company
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ACKNOWLEDGMENTS
The authors wish to extend their sincere appreciation to the staff of the Desert Sands Mutual Domestic
Water Consumers Association in Anthony, New Mexico. The Desert Sands staff monitored the treatment
system daily, and collected samples from the treatment system and distribution system on a regular
schedule throughout this study. This performance evaluation would not have been possible without their
efforts.
XI
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1.0 INTRODUCTION
1.1 Background
The Safe Drinking Water Act (SOWA) mandates that U.S. Environmental Protection Agency (EPA)
identify and regulate drinking water contaminants that may have adverse human health effects and that
are known or anticipated to occur in public water supply systems. In 1975 under the SDWA, EPA
established a maximum contaminant level (MCL) for arsenic at 0.05 mg/L. Amended in 1996, the
SDWA required that EPA develop an arsenic research strategy and publish a proposal to revise the
arsenic MCL by January 2000. On January 18, 2001, EPA finalized the arsenic MCL at 0.01 mg/L (EPA,
2001). In order to clarify the implementation of the original rule, EPA revised the rule text on March 25,
2003 to express the MCL as 0.010 mg/L (10 (ig/L) (EPA, 2003). The final rule required all community
and non-transient, non-community water systems to comply with the new standard by January 23, 2006.
In October 2001, EPA announced an initiative for additional research and development of cost-effective
technologies to help small community water systems (<10,000 customers) meet the new arsenic standard,
and to provide technical assistance to operators of small systems in order to reduce compliance costs. As
part of this Arsenic Rule Implementation Research Program, EPA's Office of Research and Development
(ORD) proposed a project to conduct a series of full-scale, on-site demonstrations of arsenic removal
technologies, process modifications, and engineering approaches applicable to small systems. Shortly
thereafter, an announcement was published in the Federal Register requesting water utilities interested in
participating in Round 1 of this EPA-sponsored demonstration program to provide information on their
water systems. In June 2002, EPA selected 17 out of 115 sites to host the demonstration studies,
including the Desert Sands Mutual Domestic Water Consumers Association (MDWCA) water system in
Anthony, NM.
In September 2002, EPA solicited proposals from engineering firms and vendors for cost-effective arsenic
removal treatment technologies for the 17 host sites. EPA received 70 technical proposals for the 17 host
sites, with each site receiving from one to six proposals. In April 2003, an independent technical panel
reviewed the proposals and provided its recommendations to EPA on the technologies that it determined
were acceptable for the demonstration at each site. Because of funding limitations and other technical
reasons, only 12 of the 17 sites were selected for the demonstration project. Using the information
provided by the review panel, EPA, in cooperation with the host sites and the drinking water programs of
the respective states, selected one technical proposal for each site. Severn Trent Services (STS), using the
Bay oxide E33 media developed by Bayer AG, was selected for the Desert Sands MDWCA facility in
Anthony, NM. STS has given the E33 media the designation "SORB 33™".
1.2 Treatment Technologies for Arsenic Removal
The technologies selected for the 12 Round 1 EPA arsenic removal demonstration host sites include nine
adsorptive media systems, one anion exchange system, one coagulation/filtration system, and one process
modification with iron addition. Table 1-1 summarizes the locations, technologies, vendors, and key
source water quality parameters of the 12 demonstration sites. An overview of the technology selection
and system design (Wang et al., 2004) and the associated capital costs for each site (Chen et al., 2004) are
provided on the EPA website at http ://www. epa. gov/ORD/NRMRL/arsenic/ resource .htm. As of
September 2008, all 12 systems were operational, and the performance evaluation of 11 systems was
completed.
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Table 1-1. Summary of Round 1 Arsenic Removal Demonstration Sites
Demonstration Site
WRWC, NH
Rollinsford, NH
Queen Anne's County, MD
Brown City, MI
Climax, MN
Lidgerwood, ND
Desert Sands MDWCA, NM
Nambe Pueblo, NM
Rimrock, AZ
Valley Vista, AZ
Fruitland, ID
STMGID, NV
Technology (Media)
AM(G2)
AM (E33)
AM (E33)
AM (E33)
C/F (Macrolite)
SM
AM (E33)
AM (E33)
AM (E33)
AM (AAFS50/ARM 200)
IX (A300E)
AM (GFH/Kemiron)
Vendor
ADI
AdEdge
STS
STS
Kinetico
Kinetico
STS
AdEdge
AdEdge
Kinetico
Kinetico
Siemens
Design
Flowrate
(gpm)
70(a)
100
300
640
140
250
320
145
90(a)
37
250
350
Source Water Quality
As
(HS/L)
39
36(b)
19(b)
14(b)
39(b)
146(b)
23(b)
33
50
41
44
39
Fe
(HS/L)
<25
46
270(c)
127«o
546(c)
l,325(c)
39
<25
170
<25
<25
<25
PH
7.7
8.2
7.3
7.3
7.4
7.2
7.7
8.5
7.2
7.8
7.4
7.4
AM = adsorptive media; C/F = coagulation/filtration; GFH = granular ferric hydroxide; IX = ion exchange; SM = system
modification
MDWCA = Mutual Domestic Water Consumer's Association; STMGID = South Truckee Meadows General Improvement
District; WRWC = White Rock Water Company; STS = Severn Trent Services
(a) Design flowrate reduced by 50% due to system reconfiguration from parallel to series operation.
(b) Arsenic exists mostly as As(III).
(c) Iron exists mostly as soluble Fe (II).
1.3
Project Objectives
The objective of the Round 1 arsenic demonstration program is to conduct full-scale arsenic treatment
technology demonstration studies on the removal of arsenic from drinking water supplies. The specific
objectives are to:
• Evaluate the performance of the arsenic removal technologies for use on small systems.
• Determine the required system operation and maintenance (O&M) and operator skill levels.
• Characterize process residuals produced by the technologies.
• Determine the capital and O&M cost of the technologies.
This report summarizes the performance of the STS system at the Desert Sands MDWCA facility from
January 16, 2004 through August 17, 2006. The types of data collected included system operation, water
quality (both across the treatment train and in the distribution system), residuals, and capital and O&M
cost.
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2.0 SUMMARY AND CONCLUSIONS
Based on the information collected during the 31 months of system operation, the following conclusions
were made relating to the overall objectives of the treatment technology demonstration study.
Performance of the arsenic removal technology for use on small systems:
• Chlorine was effective in oxidizing As(III) to As(V), reducing soluble As(III) concentrations
from 21.7 (ig/L (on average) in raw water to 2.0 (ig/L (on average).
• SORB33™ media was effective in removing arsenic, but its run length was shorter than
projected by the vendor. For the run with the granular form of the SORB33™ media (-S),
breakthrough of total arsenic at 10 (ig/L occurred at 40,600 bed volumes (BV), representing
62% of the vendor estimated working capacity. For the run with the pelletized form of the
media (-P), breakthrough of total arsenic occurred at 49,500 BV, representing 58% of the
estimated working capacity.
• As much as 45% media loss was observed during the media run using the granular media (-
S). Poor physical integrity of the media might have contributed to the media loss. Sieve
analyses indicated disintegration of the granular media during the run. Media loss reduced to
12% during the second media run using the pelletized media (-P). Sieve analyses were not
performed for the pelletized media.
• The throughput between consecutive backwash events decreased significantly during the
media run using the granular media (-S), from over 2,885 BV after system retrofit to 630 BV
at the end of the run. Media attrition of the granular media (-S) during backwash appeared to
have caused more frequent backwash.
• Arsenic concentrations in the distribution system were reduced from the predemonstration
levels of 22.4-28.2 (ig/L to 1.8-19.0 (ig/L after the sytem became operational. However, the
reduced concentrations were still higher than those in the plant effluent, probably due to the
blending of the treated water with untreated water produced by a separate well in the
distribution system. Neither lead nor copper concentrations appear to have been affected by
operation of the system.
Required system O&M and operator skill levels:
• The APU-300 system experienced excessive flow restriction, imbalanced flow, and/or
elevated pressure differential across the adsorption vessels and the entire system during the
first four months of system operation. After extensive onsite and off-site investigations and
hydraulic testing, the system was retrofitted in May 2004. Since then the system was able to
operate according to the original design specifications through the end of the demonstration
study.
• The skill requirements to operate the treatment system were minimal with a typical daily
demand on the operator of 15 to 20 min. Normal operation of the system did not appear to
require additional skills beyond those necessary to operate the existing water supply
equipment. A Level 3 state-certified operator was required for operation of the water system
at MDWCA.
Characteristics of residuals produced by the technology:
• Each backwash event produced approximately 10,000 gal of wastewater. Backwash
wastewater contained less soluble arsenic than raw water, indicating removal of arsenic by
the media during backwashing.
• Approximately 2.2 and 1.6 mg of arsenic was loaded per gram of dry SORB33™-S and
SORB33™-P media, respectively; equivalent to approximately 0.22 and 0.16%, respectively,
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Capital and O&M cost of the technology:
• The unit annualized capital cost was $0.09/1,000 gal if the system operated at 100%
utilization rate. The system's actual unit annualized capital cost was $0.37/1,000 gal, based
on 7 hr/day of system operation and 40,395,000 gal/year of water production. The unit O&M
cost was $0.74/1,000 gal, based on media replacement and disposal, chemical supply,
electricity consumption, and labor.
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3.0 MATERIALS AND METHODS
3.1
General Project Approach
Following the predemonstration activities summarized in Table 3-1, the performance evaluation study of
the STS treatment system began on January 16, 2004. Table 3-2 summarizes the types of data collected
and/or considered as part of the technology evaluation process. The overall performance of the system
was evaluated based on its ability to consistently remove arsenic to below the target MCL of 10 |o,g/L
through the collection of water samples across the treatment train. The reliability of the system was
evaluated by tracking the unscheduled system downtime and frequency and extent of repair and
replacement. The unscheduled downtime and repair information were recorded by the plant operator on a
Repair and Maintenance Log Sheet.
The O&M and operator skill requirements were evaluated based on a combination of quantitative data
and qualitative considerations, including the need for any pre- and/or post-treatment, level of system
automation, extent of preventative maintenance activities, frequency of chemical and/or media handling
and inventory, and general knowledge needed for relevant chemical processes and related health and
safety practices. The staffing requirements for the system operation were recorded on an Operator Labor
Hour Log Sheet.
Table 3-1. Predemonstration Study Activities and Completion Dates
Activity
Introductory Meeting Held
Request for Quotation Issued to Vendor Issued
Vendor Quotation to Battelle Submitted
Purchase Order Completed and Signed
Letter Report Issued
Concrete Pad Poured
Engineering Package to NMED Submitted
APU-300 Unit Shipped by STS
Draft Study Plan Issued
APU-300 Unit Delivered to Desert Sands MDWCA
System Installation Completed
Approval for Construction Granted by NMED
Building Construction Began
System Shakedown Completed
Performance Evaluation Began
Final Study Plan Issued
Building Construction Completed
Date
August 20, 2003
August 26, 2003
September 17, 2003
October 3, 2003
October 16, 2003
October 30, 2003
November 18, 2003
November 18, 2003
November 26, 2003
December 1, 2003
December 11, 2003
December 22, 2003
December 23, 2003
January 15, 2004
January 16, 2004
January 19, 2004
January 23, 2004
NMED = New Mexico Environmental Department
The quantity of aqueous and solid residuals generated was estimated by tracking the amount of backwash
water produced during each backwash cycle and the need to replace the media upon arsenic breakthrough.
Backwash wastewater and spent media were sampled and analyzed for chemical characteristics.
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Table 3-2. Evaluation Objectives and Supporting Data Collection Activities
Evaluation Objective
Performance
Reliability
System O&M and Operator
Skill Requirements
Residual Management
System Cost
Data Collection
-Ability to consistently meet 10 (o,g/L of arsenic in treated water
-Unscheduled system downtime
-Frequency and extent of repairs including a description of problems,
materials and supplies needed, and associated labor and cost
-Pre- and post-treatment requirements
-Level of system automation for system operation and data collection
-Staffing requirements including number of operators and laborers
-Task analysis of preventative maintenance including number, frequency,
and complexity of tasks
-Chemical handling and inventory requirements
-General knowledge needed for relevant chemical processes and health and
safety practices
-Quantity and characteristics of aqueous and solid residuals generated by
system operation
-Capital cost for equipment, site engineering, and installation
-O&M cost for media, chemical consumption, electricity usage, and labor
The cost of the system was evaluated based on the capital cost per gal/min (gpm) (or gal/day [gpd]) of
design capacity and the O&M cost per 1,000 gal of water treated. This task required tracking of the
capital cost for the equipment, engineering, and installation, as well as the O&M cost for media
replacement and disposal, chemical supply, electricity usage, and labor.
3.2
System O&M and Cost Data Collection
The plant operator performed daily, weekly, and monthly system O&M and data collection following the
instructions provided by STS and Battelle. On a daily basis, the plant operator recorded system
operational data, such as pressure, flowrate, totalizer, and hour meter readings on a Daily System
Operation Log Sheet; checked the sodium hypochlorite (NaOCl) drum level; and conducted visual
inspections to ensure normal system operations. If any problems occurred, the plant operator contacted
the Battelle Study Lead, who determined if STS was contacted for troubleshooting. The plant operator
recorded all relevant information on the Repair and Maintenance Log Sheet. Weekly or bi-weekly, the
plant operator measured water quality parameters, including temperature, pH, dissolved oxygen (DO),
oxidation-reduction potential (ORP), and residual chlorine, and recorded the data on a Weekly Onsite
Water Quality Parameters Log Sheet. Monthly, the plant operator inspected the system control panel to
ensure that moisture had not penetrated into the panel (STS, 2004). A monthly backwash of the media
was originally recommended by STS; however, since it had been retrofitted in May 2004, the system was
backwashed automatically when triggered by an increase in differential pressure (Ap) across each
adsorption vessel. Backwash data were recorded on a Backwash Log Sheet.
The capital cost for the arsenic removal system consisted of the cost for equipment, site engineering, and
system installation. The O&M cost consisted of the cost for media replacement and spent media disposal,
chemical and electricity consumption, replacement parts, and labor. The NaOCl and electricity
consumption was tracked using the Daily System Operation Log Sheet. Labor for various activities, such
as the routine system O&M, troubleshooting and repair, and demonstration-related work, were tracked
using an Operator Labor Hour Log Sheet. The routine O&M included activities such as completing daily
field logs, replenishing the NaOCl solution, ordering inventory, performing regular system inspection, and
others as recommended by the vendor. The demonstration-related work, including activities such as
-------
performing field measurements, collecting and shipping samples, and communicating with the Battelle
Study Lead and the vendor, was recorded, but not used for the cost analysis.
3.3 Sample Collection Procedures and Schedules
To evaluate the system performance, samples were collected from the wellhead, treatment plant, and
distribution system. Table 3-3 provides the sampling schedules and analytes measured during each
sampling event. Figure 3-1 presents a flow diagram of the treatment system along with the analytes and
schedules at each sampling location. Specific sampling requirements for analytical methods, sample
volumes, containers, preservation, and holding times are presented in Table 4-1 of the EPA-endorsed
Quality Assurance Project Plan (QAPP) (Battelle, 2003). The procedure for arsenic speciation is
described in Appendix A of the QAPP.
3.3.1 Source Water. During the initial visit to the site, source water samples were collected and
speciated using an arsenic speciation kit described in Section 3.4.1. The sample tap was flushed for
several minutes before sampling; special care was taken to avoid agitation, which could cause unwanted
oxidation. Analytes for the source water samples are listed in Table 3-3.
3.3.2 Treatment Plant Water. Treatment plant water samples were collected by the plant
operator weekly, on a four-week cycle, for on- and off-site analyses. For the first week of each four-week
cycle, water samples were collected at the wellhead (IN), after chlorination (AC), and from the combined
effluent of Vessels A and B (TT) and analyzed for the monthly treatment plant analyte list shown in
Table 3-3. For the second, third, and fourth week of each four-week cycle, water samples were collected
at four locations across the treatment train, including IN, AC, after Vessel A (TA), and after Vessel B
(TB) and analyzed for the weekly treatment plant analyte list shown in Table 3-3.
Over the course of the demonstration study, several changes were made to the sampling schedule as listed
in Table 3-3 including:
• Sampling at IN, AC, TA, and TB was reduced from three times per month to once per month
from April 30, 2004, to December 14, 2005, and then increased to twice per month from
February 1, to August 2, 2006. No sampling was conducted from December 15, 2005, to
January 31, 2006. Since February 1, 2006, the analysis for SiO2, PO4, alkalinity, and
turbidity was discontinued, and only total As, Fe, and Mn were measured.
• Monthly speciation sampling at IN, AC, and TT was discontinued after January 4, 2006.
• On-site measurements of pH, temperature, DO, ORP, and C12 (free and total) were reduced
from weekly to monthly from March 2, 2005, to January 4, 2006, and discontinued thereafter.
• Total P replaced orthophosphate beginning on October 12, 2005 due to ease of analysis.
3.3.3 Backwash Wastewater. Grab samples were collected periodically from a tap on the
backwash wastewater discharge line by the plant operator from May 2004 through November 2005.
Filtered samples using 0.45-(im filters were analyzed for soluble As, Fe, and Mn and non-filtered samples
analyzed for pH, total dissolved solids (TDS), and turbidity. Since February 2006, composite samples
were collected monthly using a procedure that allowed collection of more representative samples during
backwash. Tubing, connected to the tap on the discharge line, directed a portion of backwash wastewater
at approximately 1 gpm into a clean, 32-gal container over the duration of the backwash for each vessel.
After the content in the container was thoroughly mixed, composite samples were collected and/or filtered
on-site with 0.45-(im disc filters. Filtered and non-filtered samples were analyzed for the analytes
-------
Table 3-3. Sample Collection Schedule and Analyses
Sample
Type
Source
Water
Treatment
Plant
Water
Backwash
Wastewater
Sampling
Locations'3'
IN
IN, AC, TA,
TB
IN, AC, TT
BW
No. of
Samples
1
4
o
6
2
Frequency
Once
(during
initial site
visit)
3
time/month
(01/28/04-
04/07/04);
monthly
(04/30/04 -
12/14/05);
No
sampling
(12/15/05 -
01/31/06);
2
time/month
(02/01/06 -
08/02/06)
Monthly
(01/23/04-
01/04/06)
Eighteen
times
Analytes
On-site: pH
Off-site:
As (total and soluble),
As(III), As(V),
Fe (total and soluble),
Mn (total and soluble),
Al (total and soluble),
V (total and soluble),
Mo (total and soluble),
Sb (total and soluble),
Na, Ca, Mg, Cl, F,
SO4, sulfide, SiO2,
PO4, TOC, and
alkalinity
On-site(b): pH,
temperature, DO,
ORP, C12 (free and
total)
Off-site(c): As (total),
Fe (total), and Mn
(total), SiO2, PO4(d)
alkalinity, and
turbidity
On-site(b): pH,
temperature, DO,
ORP, C12 (free and
total)
Off-site:
As (total and soluble),
As(III), As(V),
Fe (total and soluble),
Mn (total and soluble),
Ca, Mg, F, NO3, SO4,
sulfide, SiO2,
alkalinity, and
turbidity
Before 02/0 1/06 :pH,
TDS, turbidity, soluble
As, Fe, and Mn
After 02/0 1/06 :pH,
TDS, andTSS,
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble)
Collection Date(s)
08/20/03
01/28/04, 02/04/04, 02/11/04,
02/25/04, 03/03/04, 03/10/04,
03/24/04, 03/31/04, 04/07/04,
04/30/04, 05/26/04, 06/23/04,
07/21/04, 08/18/04, 09/15/04,
10/13/04, 11/03/04, 12/01/04,
01/05/05, 02/02/05, 03/02/05,
03/30/05, 04/27/05, 05/25/05,
06/07/05, 07/06/05,08/17/05(e),
09/14/05(e), 10/12/05,11/09/05,
12/14/05, 02/01/06, 02/15/06,
03/01/06, 03/15/06, 03/29/06,
04/12/06, 04/26/06, 05/10/06,
05/24/06, 06/07/06, 06/21/06,
07/05/06, 07/19/06, 08/02/06
01/23/04, 02/18/04, 03/17/04,
04/14/04, 05/12/04, 06/09/04,
07/07/04, 08/04/04, 09/01/04,
09/29/04, 10/28/04, 11/17/04,
12/15/04, 01/20/05, 02/16/05,
03/16/05, 04/13/05, 05/11/05,
06/22/05, 08/03/05, 08/31/05,
09/28/05, 10/26/05, 11/30/05,
01/04/06
05/23/04, 07/13/04, 09/30/04,
11/17/04, 12/06/04, 02/07/05,
06/14/05, 07/07/05, 09/15/05,
10/12/05, 11/09/05, 02/01/06,
03/15/06, 04/11/06, 05/10/06,
06/06/06, 07/18/06, 08/16/06
-------
Table 3-3. Sample Collection Schedule and Analyses (Continued)
Sample
Type
Backwash
Solids
Distribution
Water
Spent
Media
Sampling
Locations*3'
BW
One home
(anLCR
sampling
location)
and two
non-
residences
within area
served by
Well No. 3,
according to
MDWCA
model
From spent
media in
vessels
No. of
Samples
1 per
vessel
5
(3 first
draw and
2
flushed)
2 to 3 per
vessel
Frequency
Three times
Monthly
Two times
(at end of
media runs)
Analytes
Total Al, As, Ca, Cd,
Cu, Fe, Mg, Mn, Ni, P,
Pb, Si, and Zn
pH, alkalinity, total
As, Cu, Fe, Mn, and
Pb
TCLP; total Al, As,
Ca, Cd, Cu, Fe, Mg,
Mn, Ni, P, Pb, Si, and
Zn
Collection Date(s)
06/06/06, 07/18/06, 08/16/06
Baseline sampling®:
12/08/03, 12/11/03, 12/30/03
Monthly sampling: 02/11/04,
03/10/04, 04/07/04, 05/12/04,
06/23/04, 07/21/04, 08/18/04,
09/15/04, 10/13/04, 11/10/04,
12/08/04, 01/20/05, 02/16/05,
03/16/05,04/13/05,05/11/05,
06/22/05, 08/03/05, 09/14/05,
10/12/05, 11/09/05, 12/14/05
07/27/05, 09/11/06 (Vessel B
only)
(a)
Abbreviation corresponding to sample locations in Figure 3-1: IN = at wellhead, AC = after chlorination, TA =
after Vessel A, TB = after Vessel B, TT = comined effluent, and BW = at backwash wastewater discharge line
(b) Onsite chlorine residual measurements not performed at IN; measurements reduced to monthly from March 2,
2005 to January 4, 2006 and discontinued thereafter.
Since February 1, 2006, only total As, Fe, and Mn measured.
Total P replaced PO4 since October 12, 2005.
Samples collected at IN, AC, and TT.
Three baseline sampling events performed before system startup.
(c)
(d)
(e)
(f)
performed for the grab samples plus total suspended solids (TSS) and total As, Fe, and Mn. TDS was
discontinued after February 2006.
3.3.4 Residual Solids. Residual solids included backwash solids and spent media samples.
Backwash solids/water mixtures were collected after solids settled in the 32-gal backwash containers and
the supernatant carefully decanted. Due to low solids in the backwash wastewater, solids were collected
from multiple backwash events during the last few months of system operation and combined for
suffcient sample quantity. The samples were air-dried, acid-digested, and analyzed for Al, As, Ca, Cd,
Cu, Fe, Mg, Mn, Ni, P, Pb, Si, and Zn. Insufficient sample existed for Toxicity Characteristic Leaching
Procedure (TCLP) tests.
Two spent media samples were collected from each vessel during the first media changeout on July 27,
2005. Spent SORB 33™-S media were removed from the top and bottom of each adsorption vessel using
a 5-gal wet/dry shop vacuum that had been thoroughly cleaned and disinfected (Figure 3-2). Using a
garden spade, the media from each layer was well-mixed in a clean 5-gal pail prior to being filled in an
unpreserved 1-gal wide-mouth high-density polyethylene (HDPE) bottle. One aliquot of each sample was
sent for TCLP tests. Another was air dried and acid digested for metal analysis. Three spent media
samples were collected from Vessel B only during the second media changeout on September 11, 2006.
Spent SORB 33™-P media was removed from the top, middle, and bottom of the media bed using the
method similar to that for the previous changeout. A portion of each sample was submitted for TCLP
tests. Another portion of each sample was air dried and acid digested for metal analysis.
-------
INFLUENT
(WELL NO. 3)
\>
IN-LINE SAND
SEPARATION
„
(BWJ-*— POND (AC)
i A |
i
i
i
See Table 3-3
for schedule A A
and analytes ' '
/MEDIA\ /MEDIA
-••{ VESSEL 1 •••••( VESSEI
V A J V B
See Table 3-3 for schedule _ l^,^\
j i ^ ^ 1 i i /
and analytes \_>/
V
See Table 3-3 for schedule^ _ _ (^\ . DISTRIBUTION
and analytes V_-X SYSTEM
Footnote
(a) On-site analyses
Desert Sands MDWCA
Anthony, NM
SORB-33™ Technology
Design Flow: 320 gpm
See Table 3-3 for schedule
and analytes
See Table 3-3 for schedule
and analytes
, 1
See Table 3-3 for schedule
and analytes
LEGEND
(lNj At Wellhead
g (AC) After Chlorination
s1 /* N
•3 (TA) After Vessel A
2 (TB) After VesselB
( TT J After Vessels A & B
fBWj Backwash Sampling Location
Sampling Locations
INFLUENT Unit Process
NaOCl Chlorination
^ .
Figure 3-1. Process Flow Diagram and Sampling Locations
10
-------
Figure 3-2. Apparatus Used for Spent Media Sampling
3.3.5 Distribution System Water. Water samples were collected from the distribution system to
determine the impact of the arsenic treatment system on the water chemistry in the distribution system,
specifically on lead, copper, and arsenic levels. In December 2003, prior to the startup of the treatment
system, three baseline distribution system water samples were collected at three locations within the
distribution system. Following system startup, distribution system sampling continued on a monthly basis
at the same three locations until December 2005. Baseline and monthly distribution system samples were
collected by the plant operator. Samples were collected at his home, which was included in the current
Desert Sands MDWCA Lead and Copper Rule (LCR) sampling schedule, as well as two non-LCR
sampling taps, with all three locations served by water produced from Well No. 3, as indicated by the
Desert Sands MDWCA distribution system model.
The samples were collected at the LCR location following an instruction sheet developed according to the
Lead and Copper Rule Reporting Guidance for Public Water Systems (EPA, 2002). Sampling at the two
non-LCR locations was performed with the first sample taken at the first draw and the second sample
taken after flushing the sample tap for several minutes. First draw samples were collected from cold-
water faucets that had not been used for at least 6 hr to ensure that stagnant water was sampled. The
sampler recorded the date and time of last water use before sampling and the date and time of sample
collection for calculating the stagnation time. Analytes for the baseline samples coincided with the
monthly distribution system water samples as described in Table 3-3. Arsenic speciation was not
performed for the distribution water samples.
3.4
Sampling Logistics
All sampling logistics including arsenic speciation kits preparation, sample cooler preparation, and
sampling shipping and handling are discussed as follows:
11
-------
3.4.1 Preparation of Arsenic Speciation Kits. The arsenic field speciation method used an anion
exchange resin column to separate the soluble arsenic species, As(V) and As(III) (Edwards et al., 1998).
Resin columns were prepared in batches at Battelle laboratories according to the procedures detailed in
Appendix A of the EPA-endorsed QAPP (Battelle, 2003).
3.4.2 Preparation of Sampling Coolers. For each sampling event, a cooler was prepared with the
appropriate number and type of sample bottles, disc filters, and/or speciation kits. All sample bottles
were new and contained appropriate preservatives. Each sample bottle was affixed with a pre-printed,
colored-coded, waterproof label consisting of the sample identification (ID), date and time of sample
collection, collector's name, site location, sample destination, analysis required, and preservative. The
sample ID consisted of a two-letter code for the specific water facility, sampling date, a two-letter code
for a specific sampling location, and a one-letter code designating the arsenic speciation bottle (if
necessary). The sampling locations at the treatment plant were color-coded for easy identification. For
example, red, orange, yellow, and green were used to designate sampling locations for IN, TA, TB, and
TT, respectively. The labeled bottles for each sampling location were placed separately in a ziplock bag
(each corresponding to a specific sample location) and packed in the cooler. On a monthly basis, the
sample cooler also included bottles for the distribution system sampling.
In addition, all sampling- and shipping-related materials, such as disposable gloves, sampling instructions,
chain-of-custody forms, prepaid/pre-addressed FedEx air bills, and bubble wrap, were placed in each
cooler. The chain-of-custody forms and air bills were completed except for the operator's signature and
the sample dates and times. After preparation, sample coolers were sent to the site via FedEx for the
following week's sampling event.
3.4.3 Sample Shipping and Handling. After sample collection, samples for off-site analyses were
packed carefully in the original coolers with wet ice and shipped to Battelle. Upon receipt, the sample
custodian checked sample IDs against the chain-of-custody forms and verified that all samples indicated
on the forms were included and intact. Discrepancies noted by the sample custodian were addressed with
the plant operator by the Battelle Study Lead. The shipment and receipt of all coolers by Battelle were
recorded on a cooler tracking log.
Samples for metal analyses were stored at Battelle's inductively coupled plasma-mass spectrometry (ICP-
MS) laboratory. Samples for other water quality analyses were packed in separate coolers and picked up
by couriers from American Analytical Laboratories (AAL) in Columbus, OH and TCCI Laboratories in
New Lexington, OH, or shipped to DHL Analytical in Round Rock, TX. The chain-of-custody forms
remained with the samples from the time of preparation through analysis and final disposition. All
samples were archived by the appropriate laboratories for the respective duration of the required hold
time and disposed of properly thereafter.
3.5 Analytical Procedures
The analytical procedures described in Section 4.0 of the EPA-endorsed QAPP (Battelle, 2003) were
followed by Battelle ICP-MS, AAL, DHL, and TCCI Laboratories. Laboratory quality assurance/quality
control (QA/QC) of all methods followed the prescribed guidelines. Data quality in terms of precision,
accuracy, method detection limit (MDL), and completeness met the criteria established in the QAPP (i.e.,
20% relative percent difference [RPD], 80 to 120% percent recovery and 80% completeness). The quality
assurance (QA) data associated with each analyte will be presented and evaluated in a QA/QC Summary
Report to be prepared under separate cover upon completion of the Arsenic Demonstration Project.
Field measurements of pH, temperature, DO, and ORP were conducted by the plant operator using a
WTW Multi 340i handheld meter, which was calibrated for pH and DO prior to use following the
12
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procedures provided in the user's manual. The ORP probe also was checked for accuracy by measuring
the ORP of the standard solution and comparing it to the expected value. The plant operator collected a
water sample in a clean, plastic beaker and placed the WTW probe in the beaker until a stable value was
obtained. The plant operator also performed free and total chlorine measurements using Hach chlorine
test kits following the user's manual.
13
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4.0 RESULTS AND DISCUSSION
4.1 Facility Description
Desert Sands MDWCA has been in operation as a non-profit association under the New Mexico Sanitary
Projects Act since December 1978. At the time of this demonstration study, the governing board
consisted of five members, and the staff members consisted of an office manager (Secretary of the
Association), a full-time operator, a part-time customer service clerk, and a part-time contracted operator
intern. Desert Sands MDWCA served its customers through an existing supply, storage, and distribution
network covering an area of approximately four square miles of unincorporated area in Southern Dona
Ana County. The water treatment facility was located approximately 2 miles north of Anthony, NM and
serves an area generally situated between Interstate 10 on the east, NM 478 on the west, O'Hara Road on
the south, and Ernesto Road on the north.
According to the 40 Year Water Plan (Desert Sands MDWCA, 2002a) prepared for the water utility in
2002, Desert Sands MDWCA served 1,886 community members. It was projected that population in the
Desert Sands MDWCA service area would increase by approximately 5,600 over a 40-yr planning period,
assuming a median growth rate of 3.5%. The water production and use have fluctuated over the past
several years with the peak production occurring in 1998 at 63,500,000 gal. In 2002, total water
production and use were approximately 56,100,000 and 51,400,000 gal, respectively. Water loss
percentages ranged from 6.3 to 14.1% during 1998 through 2002, with the lowest and highest loss
occurring in 2002 and 1998, respectively.
4.1.1 Pre-existing System. The pre-existing system consisted of two production wells (Wells No.
2 and 3) with a combined capacity of 420 gpm, one 99,000-gal and one 240,000-gal storage tank, and
approximately 30 miles of distribution piping. Figure 4-1 presents a map of the Desert Sands MDWCA
delivery service area.
Prior to the installation of the STS arsenic removal system, the treatment plant consisted of Well No. 3
(located about 20 ft from the pump house), a pump house, and a drainage pond. Well No. 3 was screened
from 690 to 740 ft below ground surface (bgs) with the static groundwater table at 45 ±1 ft bgs. The well
water was filtered through an in-line sand separator (shown along with Well No. 3 on Figure 4-2) and
then fed into the pump house (see piping in the pump house on Figure 4-3). A pressure of 75 pounds per
square inch (psi) was maintained through the system. The maximum daily production was approximately
259,000 gpd and the average daily production was 158,000 gpd.
Before entering the distribution system, 0.4 to 0.5 mg/L (as C12) of NaOCl was added to the water using a
peristaltic pump (Figure 4-4) for a target chlorine residual level of 0.3 mg/L (as C12). The two storage
tanks are filled with excess water from the distribution system.
4.1.2 Source Water Quality. Source water samples were collected from Well No. 3 on August
20, 2003 and subsequently analyzed for the analytes shown in Table 3-3. The results of the source water
analyses, along with those provided by the facility to EPA for the demonstration site selection and those
independently collected and analyzed by EPA, are presented in Table 4-1.
Total arsenic concentrations in source water ranged from 17.0 to 22.7 |o,g/L. Based on the August 20,
2003 speciation sampling results, arsenic was present primarily as soluble As(III) (i.e., 96.9% at
21.6 (ig/L), with only a small amount existing as soluble As(V) (i.e., 0.7 |o,g/L ) and particulate As (i.e.,
0.4 |og/L). Because As(V) adsorbs better with the SORB 33™ media, it was desirable to oxidize As(III)
to As(V) before adsorption.
14
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DESERT SANDS MUTUAL DOMESTIC
WATER CONSUMERS ASSOCIATION
DONA ANA COUNTY, NEW MEXICO
Figure 4-1. Map of Desert Sands MDWCA Service Area
-------
Figure 4-2. Well No. 3 (Left) and In-Line Sand Separator (Center) Adjacent
to Pump House (Right) at Desert Sands MDWCA Site
Figure 4-3. Piping Inside Pump House at Desert Sands MDWCA Site
16
-------
Figure 4-4. Sodium hypochlorite (NaOCl) Injection System at Desert Sands MDWCA Site
pH values of source water ranged from 7.6 to 7.7, which was within the range recommended by STS.
Therefore, pH adjustment was not recommended.
Iron levels in source water ranged from 38.9 to 73.0 (ig/L; manganese levels ranged from 8.9 to
10.0 (ig/L. At these levels, the vendor recommended not to pretreat iron and manganese prior to
adsorption. Competing anions, such as orthophosphate and silica, were at levels sufficiently low (i.e.,
<0.065 to 0.1 mg/L and 34.6 to 35.1 mg/L, respectively) to not have a significant effect on arsenic
adsorption by SORB 33™ media. Other analytes also were at levels low enough not to exert any impact
on arsenic adsorption.
Although sulfide odor has been observed by the operator and by sampling personnel, sulfide was not
detected at a detection limit of 0.05 mg/L. Additional samples were collected monthly during the
demonstration study and analyzed for sulfide using a detection limit of 0.005 mg/L. The results are
discussed in Section 4.4.1.
4.1.3 Distribution System. The Desert Sands MDWCA distribution system consists of a looped
distribution line supplied by Wells No. 2 and No. 3. After chlorination, water from the two wells was
pumped into the distribution system at two different locations, separated by approximately 2 miles. When
the water production from the two wells exceeded the consumer demand, the excess flowed under
pressure into the two storage tanks (i.e., Tank No. 2 at 75 ft tall by 15 ft in diameter, and Tank No. 3 at 86
ft tall by 22 ft in diameter) connected to the distribution system via 6- and 10-in-diameter polyvinyl
chloride (PVC) pipe, respectively. The distribution system was constructed of PVC pipe, measuring
approximately 30 miles in total length and varying from 2 to 10-in in diameter. The well pumps were
activated by level sensors in the storage tanks, which signaled the pumps to turn on and off when the tank
level reached a pre-set low and high level, respectively.
17
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Table 4-1. Desert Sands MDWCA Well No. 3 Water Quality Data
Parameter
Unit
Sample Date
pH
Alkalinity (as CaCO3)
Hardness (as CaCO3)
Chloride
Fluoride
Sulfide
Sulfate
Silica (as SiO2)
Orthophosphate (as P)
TOC
As (total)
As (soluble)
As (paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Al (total)
Al (soluble)
Mn (total)
Mn (soluble)
V (total)
V (soluble)
Mo (total)
Mo (soluble)
Sb (total)
Sb (soluble)
Na
Ca
Mg
—
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
W?/L
HB/L
W?/L
HB/L
W?/L
^g/L
HB/L
W?/L
HB/L
W?/L
HB/L
W?/L
HB/L
^g/L
W?/L
HB/L
W?/L
mg/L
mg/L
mg/L
Utility
Raw Water
Data
NA
7.6
240
152
253
NA
NA
158
NA
O.065
NA
22.0
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
266
43.0
11.0
EPA
Raw Water
Data
09/24/02
NA
185
NA
161
0.5
NA
180
34.6
0.1
NA
17.0
NA
NS
NA
NA
73.0
NA
<25
NA
8.9
NA
NA
NA
NA
NA
<25
NA
225
26.3
3.4
Battelle
Raw Water
Data
08/20/03
7.7
188
84
180
1.0
O.05
190
35.1
O.10
1.6
22.7
22.3
0.4
21.6
0.7
38.9
<30
27.2
<10
10.0
9.0
0.5
0.5
11.6
11.9
<0.1
0.1
189
27.2
3.9
NA = not available; TOC = total organic carbon
Water from Wells No. 2 and No. 3 blended within the distribution system and the storage tanks. Desert
Sands MDWCA has completed a modeling effort to examine the portions of the system served by the
individual wells. The results of this modeling study were used to select distribution system sampling
locations from areas that appear to be served by Well No. 3.
Desert Sands MDWCA sampled water periodically from the distribution system for several analytes: once
a month for bacteria; once every three years for inorganics (such as heavy metals, cyanide, and F),
volatile organic compounds (VOCs), and synthetic organic compounds (SOCs); and once every four years
for radionuclides. Under the LCR, samples have been collected from customer taps at 20 locations every
three years, with samples most recently collected in 2000. The monitoring results in 2002 (except for the
LCR results that were reported in 2000) are summarized in Table 4-2. Desert Sands MDWCA's
18
-------
Table 4-2. Desert Sands MDWCA Distribution
System Water Quality Data
Parameter
Arsenic
Barium
Cadmium
Chromium
Copper(a)
Nickel
Lead(a)
Selenium
Thallium
Units
HB/L
ug/L
ug/L
HB/L
ug/L
lig/L
W?/L
HB/L
W?/L
Detected Level (Range)
19 (10.4 to 19.3)
52 (34.1 to 55.2)
0.2 (0 to 0.2)
6 (3.3 to 5.5)
93 (2.8 to 103.5)
1(0.54 to 1.2)
6 (0 to 6.9)
2 (1.1 to 1.6)
0.12(0 to 0.12)
(a) Lead and copper data reported based on result of 20
samples collected on August 29, 2000.
Consumer Confidence Report (2002b) also included results for the contaminants that were monitored
every three years for inorganics, VOCs, and SOCs, or four years for radionuclides.
4.2
Treatment Process Description
STS' APU systems are designed for arsenic removal for small systems with flowrates greater than 100
gpm. They use Bayoxide® E33 (branded as SORB 33™ by STS), an iron-based adsorptive media
developed by Bayer AG, for the removal of arsenic from drinking water supplies. Table 4-3 presents
vendor-provided physical and chemical properties of the media. The SORB 33™ media were delivered
in a dry crystalline form and listed by NSF International under Standard 61 for use in drinking water
applications. The media exist in both granular and pelletized forms, which have similar physical and
chemical properties, except that pellets are denser than granules (i.e., 35 vs. 28 lb/ft3). Both granular and
pelletized forms of the media were used at the Desert Sands MDWCA facility, with the granule form used
in Media Run 1 and pelletized form used in Media Run 2.
STS provided an APU-300 system for the Desert Sands MDWCA site. Since the inception of the
performance evaluation study in January 2004, difficulties were encountered in APU-300 system
operation, including excessive flow restriction, imbalanced flow, and elevated Ap across the adsorption
vessels and entire system. The system was retrofitted in May 2004 and details are described in Section
4.4.1.
Figure 4-5 is a simplified piping and instrumentation diagram (P&ID) of the system after the system
retrofit. As shown in Figure 4-5, The APU-300 system consisted of two adsorption vessels, electrically
actuated valve tree, and associated piping and instrumentation. Electrically actuated butterfly valves
diverted raw water downward through the two adsorption vessels operating in parallel. As water passed
through the fixed-bed adsorbers, arsenic concentrations were reduced to below 10 |o,g/L. When reaching
10-|o,g/L arsenic breakthrough, the spent media were removed and disposed of after being subjected to the
EPA TCLP test. The design features of the APU-300 system are summarized in Table 4-4.
Four key process components are discussed as follows:
• Intake and In-Line Sand Separation. Raw water supplied from Well No. 3 passed through
the in-line sand separator before it was chlorinated and fed into the APU-300 system.
19
-------
Table 4-3. Physical and Chemical Properties of SORB 331M Media
Physical Properties
Parameter
Matrix
Physical Form
Color
Bulk Density (lb/ft3)
BET Surface Area (m2/g)
Attrition (%)
Moisture Content (%)
Particle Size Distribution
(U.S. Standard Mesh)
Crystal Size (A)
Crystal Phase
SORB 33™-S
Iron oxide composite
Dry granular media
Amber
28.1
142
0.3
<15% (by weight)
10 x35
70
a -FeOOH
SORB 33™-P
Iron oxide composite
Dry pelletized media
Amber
35.0
-
0.3
<15% (by weight)
14 x 18
70
a -FeOOH
Ch emical An alysis
Constituents
FeOOH
CaO
Si02
MgO
Na20
S03
A12O3
MnO
TiO2
P205
Cl
Weight %
90.1
0.27
0.06
1.00
0.12
0.13
0.05
0.23
0.11
0.02
0.01
Source: STS
Chlorination. The existing chlorination system was used to chlorinate source water with
NaOCl. NaOCl was fed with a peristaltic pump at a location downstream of the in-line sand
separator and upstream of the APU-300 treatment system. The peristaltic pump was
synchronized with the well pump so that it operated only when the well pump was on.
NaOCl dosage was controlled at 0.4 to 0.5 mg/L (as C12) for a target chlorine residual level of
0.3 mg/L (as C12). Actual dosages were monitored directly by measuring solution
consumption rates in the chemical day tank and indirectly by measuring total and free
chlorine residual levels at the AC sampling location, installed on a common feed line to the
adsorption vessels, and at the TA, TB, and/or TT locations after the adsorption vessels.
Arsenic Adsorption. The APU-300 system was a fixed-bed down-flow adsorption system
consisting of two 63-in-diameter, 86-in-tall vertical pressure vessels. The vessels were
fiberglass reinforced plastic (FRP) construction, rated for 75 psi working pressure, skid
mounted, and piped to a valve rack mounted on a polyurethane coated, welded frame. Each
vessel was loaded with approximately 80 ft3 of SORB 33™-S or 62 ft3 of SORB 33™-P media
supported by a gravel underbed. Loading of different volumes of media in the adsorption
vessels were caused by different densities of the granular and pelletized media since the
media were sold by weight rather than by volume. Empty bed contact time (EBCT) for the
system was 3.7 and 2.9 min for the SORB 33™-S and SORB 33™-P media beds, respectively,
based on a design flowrate of 320 gpm. Hydraulic loading to each vessel was approximately
7.4 gpm/ft2.
20
-------
Figure 4-5. Schematic Diagram of STS APU-300 System after System Retrofit in May 2004
As illustrated in Figure 4-5, the two adsorption vessels were interconnected with schedule 80
PVC piping and 10 electrically actuated butterfly valves using a valve tree design (Figure 4-
6). During normal operation, the feed valves (i.e., BF-121 A and B) and effluent valves (i.e.,
BF-122 A and B) were opened and the other six valves were closed to divert water downward
through the two adsorption vessels. Flow through the two vessels was balanced by throttling
the effluent valves, if needed. During backwash, the feed and effluent valves were closed and
the backwash feed valves (i.e., BF-123 A and B) and backwash effluent valves (i.e., BF-124
A and B) were opened to divert water upward through the two adsorption vessels. During
backwash rinse process, the feed valves (i.e., BF-121 A and B) and rinse valves (i.e., BF-125
A and B) were opened and the other six valves were closed to rinse the media with downward
water flow.
21
-------
Table 4-4. Design Specifications of APU-300 System
Parameter
Value
Remarks
Pretreatment
Sand Separator
NaOCl Dosage (mg/L)
NA
0.4-0.5
Gravity separation
-
Adsorption Vessels and Media Beds
Number of Adsorption Vessels
Vessel Size (in)
Type of Media
Media Volume (ftVvessel)
Media Bed Depth (ft)
2
63 D x 86 H
SORB 33™
80 (SORB 33™-S)
62 (SORB 33™-P)
3.7 (SORB 33™-S)
2.9 (SORB 33™-P)
Parallel configuration
21.6 ft2 cross-section
Run 1: SORB 33™-S (granular)
Run 2: SORB 33™-P (pelletized)
-
-
Service
Design Flowrate (gpm/vessel)
EBCT (min)
Hydraulic Loading (gpm/ft2)
Average Use Rate (gpd)
Hydraulic Utilization (%)
Estimated Working Capacity (BV)
Estimated Breakthrough (1,000 gal)
Estimated Media Life (month)
160
3.7 (SORB 33™-S)
2.9 (SORB 33™-P)
7.4
345,600
75%
66,000
85,200
-------
4.3
Figure 4-6. Treatment Process Components
(APU-300 System Valve Tree [top left and middle]; Backside of System
Piping including Vessel Flow Meter Sensors [top right];
Sampling ports [middle]; and Control Panel [bottom])
System Installation
The installation of the APU-300 system, as originally designed with the use of a diaphragm valve, a Fleck
valve controller along with a riser tube, and an orifice plate for each vessel, was completed in December
2003, with shakedown and startup activities continuing into January 2004. The system installation and
building construction activities were carried out by the plant operator as a subcontractor to STS.
4.3.1 Permitting. Engineering plans for the system permit application were prepared by Bohannon
Huston, an STS subcontractor located in Las Cruces, NM. The plans included diagrams and
specifications of the APU-300 system, as well as drawings detailing the connections of the new unit to the
23
-------
Figure 4-7. Backwash Wastewater Discharge into Pond
existing facility. After incorporating comments from Desert Sands MDWCA and Battelle, the plans were
submitted by Desert Sands MDWCA to the New Mexico Environmental Department (NMED) Drinking
Water Bureau for review and approval on November 18, 2003. The NMED issued a letter of approval on
December 22, 2003, requiring that Desert Sands MDWCA flush and disinfect the system and associated
plumbing, and retain negative results from bacteriological sampling prior to sending treated water to the
distribution system.
4.3.2 Building Construction. Desert Sands MDWCA constructed an addition to its existing pump
house at Well No. 3 to house the APU-300 system. The structure measures 15 ft x 15.5 ft at the base
(232.5 ft2) with a total height of 12 ft, and consists of a concrete floor, a steel frame, insulated steel siding
and roofing, and a walk-through door. The structure is just large enough to house the APU-300 system
and the inlet and outlet plumbing. A photograph of the new structure, adjacent to the existing block pump
house, is shown in Figure 4-8.
The building construction began on October 30, 2003, as the concrete pad was poured. After the system
was placed on the pad, work on the frame and roof began on December 23, 2003 and was completed on
January 5, 2004. Installation of the siding and insulation was completed by January 23, 2004.
4.3.3 System Installation, Shakedown, and Startup. The APU-300 system was delivered to the
site on December 1, 2003. The plant operator, subcontracted to STS, performed the off-loading and
installation of the system, including connections to the existing entry and distribution piping (Figure 4-9).
Figure 4-10 shows the APU-300 system before the building enclosure was built around it. Figure 4-11
shows the media loading to the adsorption vessels. The system installation and media loading were
completed and the system shakedown and startup commenced on December 11, 2003.
During system shakedown, it was observed that the system could produce no more than 40 gpm of flow in
either the service or backwash mode, and that under-sized orifice plates had caused the unwanted flow
restriction. The opening of the orifice plates had to be enlarged in an STS shop and repeatedly tested
24
-------
Figure 4-8. Pump House (right) and System Enclosure
Figure 4-9. APU-300 System Being Connected to Distribution System
onsite from 0.5 to 1.5 in (on January 8, 2004) and then to 1.875 in (on January 15, 2004) in order to
achieve the 150-gpm/vessel target flowrate in the service mode and 160 gpm/vessel in the backwash
mode. Moreover, while operating at 320 gpm, the system experienced a pressure loss of 18 psi across the
system, which was significantly higher than the STS specified value of less than 8 psi. The pressure loss
across the adsorption vessels and the associated diaphragm valves, Fleck valve controllers, and orifice
plates also was elevated, exceeding the maximum value of the Ap gauge readouts (i.e., 15 psi). Because
of this elevated pressure loss (which was higher than the would-be set point of about 15 psi for triggering
the automatic backwash), the pressure-actuated automatic backwash feature at the control panel had to be
disabled to avoid the system operating in a constant backwash mode.
25
-------
Figure 4-10. APU-300 System before Building Enclosure was Built
Figure 4-11. Media Loading to Adsorption Vessels
Under the conditions described above, the performance evaluation study officially began on January 16,
2004. Battelle provided operator training on data and sample collection and collected the first set of
samples from the APU-300 system.
26
-------
4.4
System Operation
Table 4-5 presents timelines of key activities/events that occurred during the system performance
evaluations. These demonstration activities are described in more details in the following sections.
4.4.1 System Retrofit. In addition to the problems identified during shakedown and startup,
several operational difficulties were encountered following commencement of the evaluation study,
including one incident on February 3, 2004 when the flow through Vessel A decreased to 40 gpm and the
system inlet pressure increased to 100 psi. At the request of Battelle, STS performed a series of hydraulic
testing on three similar systems: one that was located at STS' Torrance, CA shop and ready to be shipped
to the Queen Anne's County site in Maryland and two that were installed in Brown City, MI, and
experiencing similar operational problems (i.e., restricted and unbalanced flow and elevated pressure
losses).
Table 4-5. Demonstration Study Activities and Completion Dates
Activity/Event
APU-300 System Performance Evaluation Began
Final Study Plan Issued
Building Construction Completed
STS Performed Aggressive Backwash on Both Vessels
to Troubleshoot High Ap Issues
STS Collected Media Samples
STS Installed 3-in-diameter Bypass Line around Fleck
Valve Controllers
System Retrofit with Valve Tree Plumbing Installed
STS onsite to troubleshoot and conduct a backwash
STS on Site to Perform Repairs and Re-program PLC
Media Changeout (switch from granular SORB 33™-S
to pelletized SORB 33™-P)
STS Onsite for Troubleshooting and Media Sampling
APU-300 System Performance Evaluation Completed
APU-300 Property Transfer Completed
Date
January 16, 2004
January 19, 2004
January 23, 2004
February 19, 2004
February 26, 2004
March 8 to 9, 2004
May 16 to 24, 2004
January 6, 2005
April 4 to 5, 2005
July 27, 2005
October 27 to 28, 2005
August 17, 2006
August 25, 2006
APU = arsenic package unit; PLC = programmable logic controller;
STS = Severn Trent Services
Before reaching a decision to perform hydraulic testing, STS suggested that the operational problems
encountered might have been caused by:
(1) Damaged media - media crushed by zero to 300 gpm flow swings after flow restrictors had
been temporarily removed from the system to troubleshoot the flow restriction problem
during the initial startup,
(2) Insufficient backwash flowrates - due to the use of restrictor plates, and
(3) Clogged top distributors and/or bottom laterals.
As part of its investigative work, STS performed more aggressive backwashes on both vessels and
collected media samples for particle size distribution analyses on February 19 and 26, 2004, respectively.
On March 8, 2004, STS installed a 3-in-diameter bypass line around the Fleck valve controller on each
vessel with the intent to decrease the pressure loss and increase backwash flowrate. These efforts,
27
-------
however, did not help resolve the problems, and the results of the particle size distribution analyses did
not appear to support the speculation concerning media damage. These observations led STS to focus its
investigative work on the design and construction of system plumbing.
Hydraulic testing on the two APU-300 systems at Brown City, MI, was conducted on March 19, 2004,
with no media loaded in the vessels. While operating the system at 103 to 115 gpm/vessel (versus the
design value of 160 gpm/vessel), a pressure loss of 7 to 8 psi was observed across each vessel, and 24 to
26 psi across the entire system. These results suggested that the system plumbing most likely was the
source of high pressure losses, and that the media mostly likely was not responsible for the difficulties
encountered at Desert Sands MDWCA. Replacement of the restrictive orifices from 1.25 to 1.875 in (as
was used for the Desert Sands MDWCA system) did not solve the elevated pressure loss problems.
Additional hydraulic testing was therefore conducted at Brown City, MI and STS' Torrance, CA facility
in mid-April 2004. Table 4-6 summarizes the test results collected at Brown City, MI, Torrance, CA, and
Anthony, NM.
Pressure profile data were collected across the systems at Brown City, MI and the Torrance, CA facility.
As listed in Table 4-6 and shown in Figure 4-12, the major system components across each of the two
parallel treatment trains included piping inlet, an automatic variable diaphragm valve (to control flow), a
strainer, a programmable Fleck valve controller (to control flow from a service to backwash mode), an
FRP vessel with atop diffuser and a bottom lateral, a restrictive orifice plate, and outlet piping. Pressure
gauges were across the treatment train so that a complete pressure profile might be established. Ap
readings as measured at Desert Sands MDWCA included those across the strainer, Fleck valve controller,
and vessel, which was equipped with atop diffuser and a bottom lateral and loaded with 80 ft3 of media
supported by 14 ft3 of under bedding.
The results of the Brown City testing on April 6, 2004 showed that, after removing the restrictive orifice
plate, strainer, and top diffuser, pressure losses were observed across the variable diaphragm valve (from
80 to 71 psi) and valve controller and bottom laterals (from 61 to 58 psi). These results were consistent
with those observed during the April 8, 2004 testing at Torrance, CA, except for the 1-psi loss (from 44 to
43 psi) across the variable diaphragm valve. It was not clear what had caused the 11 psi loss across the
variable diaphragm valve at Brown City; one possible explanation was that the valve was partially
throttled during the testing. The pressure loss across the Fleck valve controller, strainer, top diffuser, and
bottom laterals at Torrance, CA was 13 psi (from 43 to 30 psi), identical to that found at Brown City, MI.
Furthermore, the pressure loss across the top diffuser and bottom lateral was 1 psi (from 34 to 33 psi),
indicating little or no loss across these system components.
The test results at Brown City, MI and Torrance, CA were further confirmed during a separate test in
Torrance, CA on April 14, 2004, which showed no loss across the variable diaphragm valve, 1 psi loss
(from 54 to 53 psi) across top diffuser and bottom lateral, 13 psi loss (from 64 to 50 psi and less 1 psi
across the top diffuser and bottom lateral) across the Fleck valve controller, and possibly 20 psi across the
restrictive orifice plate (see the 20 psi increase at the inlet after restrictive orifice was restored to the
system in Table 4-6). It was therefore evident that the main sources of the pressure loss originated from
the Fleck valve controller and restrictive orifice plate.
Upon completion of the hydraulic testing, STS recommended four options to address the problems at
Desert Sands MDWCA (and Brown City):
(1) Replace the submersible pump by the host site,
(2) Install a booster pump,
(3) Run the existing submersible pump for longer periods each day, or
(4) Retrofit the STS system.
28
-------
Table 4-6. Results of Hydraulic Testing of STS APU-300 Systems
Site
Date
Vessel
Flowrate
(gpm)
Pressure (psi)
PI
P2
P3
P4
P5
P6
AP (psi)
Vessel(a)
System
System Components
Variable
Diaphragm
Valvp
Valve Controller
Strainer
Vessel
Top Diffuser
2
•3
15
>15
7
8
8
8
13
13
13
13
14
30
30
24
24
26
26
22
22
14
14
NA
•/
^
^
^
^
^
•/
•/
•/
^
^
•/
^
^
^
^
^
•/
•/
•/
^
^
•/
^
^
^
^
^
•/
^
^
•/
^
^
^
^
^
•/
^
^
•/
^
•/
^
^
^
^
^
^
^
•/
•/
•/
^
^
•/
^
^
^
^
^
^
After System Retrofitting
Torrance, CA
Brown City, MI
Desert Sands
MDWCA, NM
04/20/04
04/29/04
05/24/04
A
B
A
B
A
B
A
B
165
165
170
155
190
190
140
135
23
52
34
34
62
62
66
66
22
51
33
34
19
50
30
33
19
50
30
30
58
58
60
60
o
J
1
o
J
1
0
0
o
J
3
4
2
4
4
4
4
6
6
•/
^
•/
^
•/
^
•/
^
,/
^
^
^
^
^
^
^
PI = at system inlet
P2 = after variable diaphragm valve and before entering strainer, valve controller, and vessel
P3 = at top of vessel
P4 = at bottom of vessel
P5 = after vessel and valve controller and before entering restrictive orifice (if present)
P6 = at system outlet
AP across vessel (including valve controller) = P2 - P5
AP across vessel = P3 - P4 (after retrofitting)
AP across system (treatment train) = PI - P6
(a) Including valve controller before system retrofitting
-------
Figure 4-12. Schematic Diagram of STS APU-300 System before System Retrofit
After reviewing the pros and cons of each option, Battelle recommended and STS agreed to retrofit the
APU-300 systems at both the Desert Sands MDWCA and Brown City sites. The changes included
replacement of the 3-in-diameterpipe with 4-in-diameter pipe; removal of the diaphragm valves,
restrictive orifice plates, and Fleck valve controllers; and installation of a nested network of fully-ported
actuated butterfly valves and a new control panel. A schematic diagram of the new system design is
presented in Figure 4-5.
The test results collected at Torrance, CA, Brown City, MI, and Desert Sands MDWCA, NM after the
system retrofit are presented in Table 4-6. With the Torrance, CA and Brown City, MI systems operating
at 155 to 190 gpm without media or underbedding loaded in the vessels, the pressure losses across the
vessel (along with bottom laterals) and the system were 0 to 3 and 2 to 4 psi, respectively. The system
was returned to service on May 24, 2004 with the modified pipe design, a new upper distributor, and new
control panel in place. STS measured the freeboard as the new upper distributors were being installed,
observing between 16.25 and 16.5-in in each vessel. Startup testing of the retrofitted unit showed a
pressure loss across the media-filled vessels of 3 psi, and a total pressure loss across the system of 6 psi.
4.4.2 Operational Parameters. The operational parameters for the entire performance evaluation
study are tabulated and attached as Appendix A. Key parameters are summarized in Table 4-7. The
APU-300 system was evaluated with two forms of SORB 33™ media, with the first media run using the
granular form and the second media run using the pelletized form. The first media run operated from
January 16, 2004, through July 14, 2005. The second media run operated from July 29, 2005, through
August 16, 2006. Relevant system operational parameters are discussed in detail below.
30
-------
Table 4-7. Summary of APU-300 System Operation
Parameter
Cumulative Operating Time (hr)
Average Daily Operating Time (hr)
Component
Throughput (1,000 gal)
Bed Volumes of Water Treated (BV)
Average Flowrate (gpm)(a)
Range of Flowrate (gpm)(b)
Average EBCT (min)(d)
Range of EBCT (min)(e)
Differential Pressure Across Vessel
(psi)
System Pressure Loss (psi)
Number of Backwashes
Backwash Interval (day)
First Media Run
(SORB 33™-S)
01/16/04-05/16/04
(before Retrofit)
493
4.3
Vessel A
3,442
5,737
116
110-
150^
5.2
4.0-5.4
>20
NA
6
1-49
Vessel B
4,433
7,388
150
140-
18000
4.0
3.3^.3
>20
NA
6
7-35
05/24/04-07/14/05
(after Retrofit)
2,745
6.6
Vessel A
22,803
38,005
138
90-190(b)
4.3
3.1-6.6
2.5-15(f)
NA
60
1-37
Vessel B
21,967
36,612
133
80-175(b)
4.5
3.4-7.5
2.5-15(f)
NA
63
1-20
01/16/04 -
07/14/05
(Combined)
3,238
6.2
System
52,645
43,871
271
205-300(c)
NA
NA
NA
4-30w
NA
NA
Second Media Run
(SORB 33™-P)
07/29/05-08/16/06
3,004
7.8
Vessel A
22,719
48,963
121
75-170(b)
3.8
2.7-6.2
2.0-11
NA
50
1-18
Vessel B
23,834
51,366
130
75-
185(b)
3.6
2.5-6.2
2.0-11
NA
53
1-26
System
46,553
50,165
251
225-275(c)
NA
NA
NA
2-26
NA
NA
(a) Calculated based on cumulative throughput and corresponding operating time.
(b) Based on the instant flowrates measured at Vessels A and B.
(c) Calculated based on the daily operation time and daily throughput measured by the master flowmeter at the wellhead.
(d) Based on the average flowrate; and 80 ft3 and 62 ft3 of media per vessel during the first and second media runs, respectively.
(e) Based on the instant flowrates measured at Vessels A and B; and 80 ft3 and 62 ft3 of media per vessel during the first and second media runs,
respectively
(f) For all measurements, except one outlier measured on July 11, 2005.
NA = not applicable
-------
First Media Run. The first media run began on January 16, 2004. Difficulties were encountered during
the initial four months of operation, and the system was retrofitted (Section 4.4.1) and returned to service
on May 24, 2004. The first media run ended on July 14, 2005. The first media run operated for a total of
3,238 hr based on the well pump hour meter readings collected daily at the wellhead. This operational
time represented a utilization rate of approximately 26%, or 6.2 hr/day. The low utilization rate was due
primarily to relatively low water demand and the concurrent use of another well, Well No. 2, to supply
water to the distribution system.
The first media run treated approximately 52,645,000 gal of water, with 49.9 and 50.1% of water flowing
through Vessels A and B, respectively, based on totalizer readings from both vessels. This amount is 4%
higher than that (50,712,000 gal) recorded from the master flow meter at the wellhead. Significant
imbalance flow was observed between the two vessels before the system retrofit, with 43.7 and 56.3%
flowing through Vessels A and B, respectively. The problems associated with the imbalanced flow were
resolved after system retrofit, with 50.9 and 49.1% flowing through Vessels A and B, respectively,
throughout the remainder of the first media run.
Figure 4-13 (left graph) presents instantaneous flowrates measured at Vessels A and B during the first
media run. The imbalance flow before system retrofit was reflected in Figure 4-13, with flowrates
through Vessel B significantly higher than those through Vessel A. This trend of constantly higher flow
through Vessel B discontinued after system retrofit. The total flow through the APU-300 system
remained relatively constant throughout the first media run at 266 and 271 gpm before and after retrofit,
respectively (or 83.1 and 84.7% of the design value of 320 gpm). Because the imbalanced flow problem
occurred before retrofit, EBCT values varied significantly between the two vessels, averaging at 5.2 min
for Vessel A and 4.0 min for Vessel B. After retrofit, the difference in EBCT reduced significantly, with
EBCT averaged 4.3 min for Vessel A and 4.5 min for Vessel B. The average EBCT was calculated based
on total throughput and total operating hours.
Figure 4-14 (left graph) presents Ap readings measured across Vessels A and B during the first media run.
Before system retrofit, the APU-300 system experienced elevated Ap across both vessels with readings
that pegged the pressure gauges with graduations up to 20 psig. Ap readings across the entire system
based on the difference between the pressure readings at the system inlet and outlet fluctuated from
approximately 18 to more than 30 psig during this period. After system retrofit, Ap readings across each
vessel reduced to as low as 2.5 to 6 psig from most measurements immediately after backwash. Similar
to imbalanced flow problems, the problems associated with high Ap were solved with system retrofit.
Second Media Run. The second media run began on July 29, 2005 and ended on August 16, 2006,
operating for a total of 3,004 hr based on well pump hour meter readings collected daily at the wellhead.
The operational time represented a utilization rate of approximately 32.5%, or 7.8 hr/day.
The second media run treated approximately 46,553,000 gal of water, with 48.8 and 51.2% flowing
through Vessels A and B, respectively, based on totalizer readings from both vessels. This amount was
almost identical to that (i.e., 46,580,000 gal) recorded from the master flow meter at the wellhead. Figure
4-13 (right graph) presents instantaneous flowrates measured at Vessels A and B during the second media
run. The two flowrate curves fluctuated slightly but essentially overlapped each other at 120 to 130 gpm
throughout the run. The averaged total flow through the APU-300 system was 251 gpm, or 78.4% of the
design value. The average EBCT was 3.8 min for Vessel A and 3.6 min for Vessel B, which is 31 to 24%
higher than the design value of 2.9 min.
Figure 4-14 (right graph) presents Ap readings measured across Vessels A and B during the second media
run. In most cases, Ap readings across each vessel immediately after backwash ranged from 2 to 5 psig,
which were slightly lower than those measured during the first media run. The lower readings observed
32
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Flowrates during First Media Run
Flowrates during Second Media Run
01/19/04 03/19/04 05/18/04 07/17/04 09/15/04 11/14/04 01/13/05 03/14/05 05/13/05 07/12/05
07/29/05 09/27/05 11/26/05 01/25/06 03/26/06 05/25/06 07/24/06
Figure 4-13. Flowrate Measurements for First (Left) and Second (Right) Media Runs
OJ
OJ
01/19/04 03/19/04 05/18/04 07/17/04 09/15/04 11/14/04 01/13/05 03/14/05 05/13/05 07/12/05
07/29/05 09/27/05 11/26/05 01/25/06 03/26/06 05/25/06 07/24/06
Figure 4-14. Differential Pressure across Vessels A and B during First (Left) and Second (Right) Media Runs
-------
probably were due the somewhat larger media size and shorter bed depth associated with the use of
pelletized media.
4.4.3 Media Loss and Breakdown. A significant amount of media were lost from the adsorption
vessels during both media runs. The amount of loss was measured based on the freeboard measurements
performed during media changout (Table 4-8). During the first media run, 42.1% and 45% of the
granular media was lost from Vessels A and B, respectively. Apparently, the loss occurred throughout
the run rather than during any specific period, according to the periodic freeboard measurements carried
out on May 24, 2004, January 6, April 5, and July 25, 2005. Some of the other demonstration sites using
SORB 33™-S also experienced media loss, including about 50% during each of two media runs at
Rollinsford, NH (Cumming et al., 2008) and at least 14 to 18% during the first 13 months of operation at
Queen Anne's County, MD (Chen et al., 2008). The media loss problem improved significantly after
switching to the pelletized media, as evidenced by the 12% media loss (with a total throughput of
46,550,000 gal), which was one third of that lost in the first media run (with a total throughput of
52,650,000 gal). This was consistent with the vendor's claim that the pelletized media was somewhat
more robust than the granular media. Because the pelletized media were 25% denser, loading a similar
weight of the pelletized media resulted in 25% less bed depth, thus yielding more freeboard in the vessels.
The less media loss also could have been caused by less wash-away of media or media fines during
backwash (assuming similar backwash flowrates) due to the presence of the 0.8-ft more freeboard in the
adsorption vessels.
Table 4-8. Freeboard Measurements and Media Loss
First Media Run
Granular
Parameter
Volume Loaded (ft3)
Initial Freeboard (in)
(May 24, 2004)
Freeboard (in)
(January 6, 2005)
Freeboard (in)
(April 5, 2005)
Final Freeboard (in)
(July 25, 2005)
Total Media Loss (in)
Total Media Loss (ft3)
Total Media Loss (%)
Vessel A
80.0
16.3
25.3
32.0
35.0
18.7
33.7
42.1
Vessel B
80.0
16.5
24.0
30.5
36.5
20.0
36.0
45.0
Second Media Run
Pelletized
Parameter
Volume Loaded (ft3)
Initial Freeboard (in)
(July 28, 2005)
Freeboard (in)
(October 27, 2005)
Final Freeboard (in)
(September 12, 2006)
NA
Total Media Loss (in)
Total Media Loss (ft3)
Total Media Loss (%)
Vessel A
62.0
24.0
24.0
NM
NA
NM
NM
NM
Vessel B
62.0
24.0
23.5
28.0
NA
4.0
7.2
11.6
NA = not applicable; NM = not measured
Weak physical integrity might have contributed to media loss observed. Sieve analyses conducted by
STS indicated that the granular media was breaking down as the run went by. As shown in Table 4-9, the
samples collected from Vessel B at a depth of 16 in on July 2005 (or 18 months after system startup) had
fewer large particles (i.e., 30% instead of 40% > 1,180 |am) and a larger amount of fines (i.e., 35% instead
of 25% < 550 |am) when compared to the virgin granular media. The media breakdown might be linked
to frequent or improper backwash (such as the use of excessive backwash loading rates), which is further
discussed in Section 4.4.4.
34
-------
Table 4-9. Particle Size Distribution of Granular Media before
System Startup and during First Media Run
Sieve Size
U.S. Standard
Mesh (|J.m)
January 2004
Virgin Media Collected
before System Startup
July 2005
Used Media Collected
from Vessel B(a)
40
30
+30 (>550)
75
65
-30 (<550)
25
(a) Collected at a depth of 16 in.
Note: Sieve analyses conducted by STS.
4.4.4 Backwash. STS recommended the SORB 33™ media be backwashed manually or
automatically approximately once per month to loosen up the media bed. Automatic backwash could be
initiated either by a timer or a Ap setting. However, due to faster than anticipated increase in Ap during
system operation, backwash was conducted far more frequently than was originally anticipated. A brief
description of the backwash events follows:
First Media Run. Due to the high Ap problems encountered, backwash was conducted only manually
before system retrofit in mid-May 2004. During the first 17 weeks of operation leading to system retrofit,
backwash was conducted seven times for Vessel A and eight times for Vessel B. After system retrofit,
backwash took place either automatically based on a 10-psi Ap setting or manually when backwash
wastewater sampling was required.
Backwash was performed 59 times for Vessel A and 62 times for Vessel B during the remaining 14
months of the first media run. The throughput between two consecutive backwash events is presented in
Figure 4-15 (top). After system retrofit, the throughput between backwash events for Vessels A and B
decreased during the first four months from over 1,250,000 (2,090 BV) and 2,200,000 gal (3,680 BV),
respectively, to around 500,000 gal (840 BV) in mid-September 2004. The throughput further reduced to
and then leveled off at an average of around 375,000 gal (630 BV) for both Vessels A and B.
Second Media Run. Backwash was conducted 51 times for both Vessels A and B during the second
media run, which lasted for about 12 months. Similar to the first media run, backwash was conducted
either automatically based on a 10-psi Ap setting or manually when backwash wastewater sampling was
needed. The throughput between two consecutive backwash events for the second media run is presented
in Figure 4-15 (bottom). Throughput values between backwash events fluctuated widely between
1,300,000 and 150,000 gal and showed no noticeable trend of increasing or decreasing throughout the
run. The averaged throughput between backwash events was 454,000 gal (760 BV) for Vessel A and
476,000 gal (800 BV) for Vessel B. These average throughput values were 1.2 to 1.6 times higher than
that recorded in the first media run. The improved physical integrity of the pelletized media might have
contributed to the higher throughput between backwash events observed during the second media run.
35
-------
Throughput between Backwash Events during First Media Run
2,500
2,000
1,500
1,000
500
01/15/04 03/15/04 05/14/04 07/13/04 09/11/04 11/10/04 01/09/05 03/10/05 05/09/05 07/08/05
Throughput between Backwash Events during Second Media Run
2,500
2,000
1,500
£
m
S
1,000
500
07/25/05
09/23/05
11/22/05
01/21/06
03/22/06
05/21/06
07/20/06
Figure 4-15. Throughput Between Backwash Events During First (Top) and
Second (Bottom) Media Runs
36
-------
The backwash was performed at flow rates typically ranging from 200 to 220 gpm. Each backwash event
lasted typically for 20 min, followed by a four-min rinse, producing approximately 4000 to 5000 gal of
water per vessel during each backwash event. Due to the cycles of water demand, automated backwash
events typically took place overnight, when the operator was not present.
4.4.5 Media Changeout. During the performance evaluation study, one media changeout was
performed by STS on July 27, 2005. Before spent media removal, the heights of the freeboard (i.e., from
the flange at the top of the vessels to the media surface) were measured as recorded in Table 4-8. The
spent SORB 33™-S media then was sampled and removed from each vessel as described in Section 3.3.4.
A vacuum truck was used to remove the spent media and the gravel underbedding. Vacuum removal of
the media was paused in each vessel to allow for the collection of spent media samples from the lower
portion of the bed in each vessel. After the spent media and gravel were completely removed, the vessels
were rinsed, new bottom laterals were installed, and the bottom flanges were reconnected. Each vessel
was then half filled with chlorinated water. New gravel was added to each vessel, followed by virgin
media, in the pelletized form. All gravel and media were added to the vessels through the 3-in diameter
top flange. The vessels were then completely filled with chlorinated water with air bled from the top of
each vessel, and the media was allowed to soak overnight. After the media were properly backwashed
and freeboard measurements obtained, the system was returned to service.
Spent SORB 33™-P samples also were collected by Desert Sands MDWCA during media removal on
September 11, 2006, although the media were not replaced at this time due to the completion of the
demonstration study.
4.4.6 Residual Management. Residuals produced by the operation of the APU-300 system
included backwash wastewater and spent media. Above ground piping for backwash wastewater from
both vessels was combined before extending outside the building below the base of the wall. Backwash
wastewater was discharged into an evaporation pond, where water either evaporated to the air or
infiltrated into the ground (Figure 4-7). Particulates carried in the backwash wastewater remained in the
pond.
4.4.7 System Operation Reliability and Simplicity. The overall system reliability and simplicity
were examined both before and after system retrofit in May 2004. Aside from the excessive pressure
losses and imbalanced flow prior to the system retrofit, the only other O&M issue encountered was the
temporary failure of digital flow meters on the vessels on two separate occasions for one to two days at a
time. After approximately two years of system operation after retrofit, two of the actuated valves (121-A
and 123-A) began to stick and had to be replaced with Asahi Type 57 butterfly valves and Asahi Type 94
actuators in September 2006.
Unscheduled downtime during the first media run was caused by the need to address elevated pressure
losses and imbalanced flows (Section 4.4.1). The system was shut down on February 19, 2004 for a
system inspection, February 26, 2004 for media sampling, March 8, 2004 for the installation of a bypass
line around the Fleck valve controller, and May 16 through 24, 2004 for system retrofit. Neither
scheduled nor unscheduled downtime was required after system retrofit until the end of the performance
evaluation study.
The simplicity of system operation and operator skill requirements are discussed according to pre- and
post treatment requirements, levels of system automation, operator skill requirements, preventative
maintenance activities, and frequency of chemical/media handling and inventory requirements.
Pre- and Post-Treatment Requirements. Pretreatment consisted of the injection of NaOCl upstream of
the system for oxidation of As(III), Fe(II), and, perhaps, sulfide. The prechlorination system was already
37
-------
in place to provide chlorine residuals in water before entering the distribution system. Vigilant oversight
of the prechlorination system was necessary to ensure that the residual chlorine levels were maintained
properly. Post-treatment was not required.
System Automation. For the most part, backwash was conducted automatically and triggered by a 10-psi
Ap setting across each vessel. Backwash also was initiated manually when backwash wastewater
sampling was required. Occasionally, only one vessel reached the trigger level and was backwashed, thus
enabling it to receive more flow than the other and producing an imbalanced flow. When this occurred,
the operator initiated a manual backwash on the second vessel, returning the system to a balanced flow.
All other functions of the APU-300 system were automatic.
Operator Skill Requirements. Under normal operating conditions, the skill requirements to operate the
APU-300 system were minimal. The daily demand on the operator was 15 min to allow the operator to
visually inspect the system and record the operating parameters on the log sheets. The operation of the
system did not appear to require additional skills beyond those necessary to operate the existing
production equipment.
Based on the size of the population served and the treatment technology, the State of New Mexico
requires Level 3 Certification for operation of the STS system at MDWCA facility. The State of New
Mexico has five levels of certifications for operations of public water supply systems, based on the
complexity of the treatment and distribution system, such as the size and type of the system, the capacity
of the system in terms of size service area and number of users served, the type and character of the water
to be treated, and the physical conditions affecting the treatment plants. The levels range from Level 1,
the least complex, to Level 5, the most complex.
Preventative Maintenance Activities. Preventative maintenance tasks recommended by STS included
monthly inspection of the control panel, quarterly checking and calibration of the flow meters, biannual
inspection of the actuator housings, fuses, relays, and pressure gauges, and annual inspection of the
butterfly valves. STS recommended checking the actuators at each backwash event to ensure that the
valves were opening and closing in the proper sequence. Further, inspection of the adsorber laterals and
replacement of the gravel underbedding were recommended concurrent with the media replacement. The
operator inspected the valves and wiring monthly, which consumed approximately 15 min/month. The
operator also compared the flow meter and totalizer data from the STS system to his existing meters on a
consistent basis, which did not require any appreciable time expenditure.
Chemical/Media Handling and Inventory Requirements. Chemical use was not required beyond the
prechlorination system already in place. At the water production rate observed during the performance
evaluation study, Desert Sands MDWCA ordered one 53-gal drum of NaOCl per month. The plant
operator switched the metering pump inlet tube from the empty drum to the new drum when necessary.
4.5 System Performance
The performance of the APU systems were evaluated based on analyses of water samples collected from
the treatment plant, system backwash, and distribution system.
4.5.1 Treatment Plant Sampling. Water samples were collected at five locations through the
treatment process: including at the inlet (IN), after prechlorination (AC), after Vessels A and B (TA and
TB, respectively), and at the combined effluent (TT). The treatment plant water was sampled on 75
occasions (including five duplicate events) during the study, with field speciation performed 25 times (19
times during the first media run and six times during the second media run). Field-speciation samples at
IN, AC, and TT were collected once every four weeks from system start-up through January 4, 2006.
38
-------
Field speciation was discontinued from February 1 through the end of the performance evaluation
sampling on August 2, 2006.
Table 4-10 provides a summary of analytical results for arsenic, iron, and manganese during the first
media run from January 16, 2004, through July 14, 2005, and the second media run from July 29, 2005,
through August 16, 2006. Table 4-11 summarizes the results of the other water quality parameters. The
standard deviations for the measurements also are presented in Tables 4-10 and 4-11. Appendix B
contains a complete set of analytical results during the operation of the first and second media runs. The
analytical data were not significantly different throughout the demonstration study whether using
SORB 33™-S for the first media run or SORB 33™-P for the second media run. The results of the water
samples collected throughout the treatment plant are discussed below.
Arsenic. The key parameter for evaluating the effectiveness of the APU-300 system was the
concentration of arsenic in the treated water. As shown in Tables 4-10 and 4-11 as well as Figures 4-16
through 4-18, the adsorptive behavior was very similar between the granular and pelletized media.
Figure 4-16 contains three bar charts showing the concentrations of total As, particulate As, and soluble
As(III) and As(V) at the IN, AC, and TT sampling locations for each speciation sampling event. Total
arsenic concentrations in raw water ranged from 19.9 to 30.1 |o,g/L and averaged 23.9 |o,g/L during the first
media run; and it ranged from 18.6 to 25.9 |o,g/L and averaged 23.4 |o,g/L during the second media run
(Table 4-10). Particulate arsenic concentrations averaged 1.2 and 1.1 ng/L during the first and second
media runs, respectively. Soluble As(III) was the predominating species with its concentrations
averaging 21.8 and 21.6 |o,g/L during the first and second media runs, respectively. The remainder of
soluble arsenic was As(V) with concentrations averaging 1.4 and 0.9 |o,g/L , respectively. The arsenic
concentrations measured during this study were consistent with those in raw water collected on August
20, 2003 (Table 4-1).
Prechlorination oxidized As(III) to As(V) and provided required chlorine residuals to the distribution
system. Samples collected downstream of the chlorine addition point (AC) had average As(III) and
As(V) concentrations of 1.9 and 21.4 |o,g/L, respectively, during the first media run;, and 2.1 and 20.2
Hg/L, respectively, during the second media run. Two exceptions were noted on samples collected on
June 9, 2004, and January 20, 2005, during which arsenic oxidation did not appear to occur. Onsite free
and total chlorine measurements, however, indicated the presence of residual chlorine; therefore,
sampling errors were suspected for these AC samples. Typically at the AC location, free chlorine was
measured at 0.3 to 0.7 mg/L (as C12) during the first media run and 0.6 to 1.0 mg/L during the second
media run. Free chlorine residuals measured were very similar to total chlorine levels, which ranged from
0.4 to 0.8 mg/L during the first and second media runs (Table 4-11). The chlorine residuals measured at
the TA, TB, and TT locations were similar to those at the AC location, indicating little or no chlorine
consumption through the adsorption vessels.
The arsenic breakthrough curves for both media runs are shown in Figure 4-17. The plots clearly
demonstrate the similarity in total arsenic concentrations at the IN and AC locations and significant
decrease in total arsenic concentrations following adsorption vessels at the TA, TB, and TT locations.
Arsenic concentrations at TA and TB were similar, despite the imbalanced flow observed.
As shown in the top of Figure 4-17, during the first media run, concentration spikes exceeding the 10-
|o,g/L As target MCL were observed on December 1, 2004, at both TA and TB locations after treated
21,200 and 23,300 BV of water by Vessels A and B, respectively. These concentration spikes could not
be related to any particular incidents after reviewing the field logs. An STS engineer came to the site on
January 6, 2005, to perform a backwash. Total arsenic concentrations at the effluent locations went down
39
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Table 4-10. Summary of Arsenic, Iron, and Manganese Analytical
Results for First and Second Media Runs
Parameter
(Figure, if any)
As (total)
(see Figure 4-
17)
As (soluble)
As (paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Sampling
Location'3'
IN
AC
TA
TB
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TT
Number of
Samples
Media Run I/
Media Run 2
49/26
49/26
30/18
29/18
19/8
19/6
19/6
19/6
19/6
19/6
19/6
19/6
17(b)/6
19/6
19/6
17(b)/6
19/6
49/25(c)
49/26
30/18
29/18
19/8
19/6
19/6
19/6
49/26
49/26
30/18
29/18
19/8
19/6
19/6
19/6
Concentration (|ig/L)
Minimum
Media Run I/
Media Run 2
19.9/18.6
19.6/21.1
NM
NM
NM
21.2/19.7
20.3/21.0
NM
0.1/0.1
0.1/0.1
NM
17.6/19.1
0.5/0.9
NM
0.1/0.1
18.4/18.1
NM
<25/<25
<25/<25
<25/<25
<25/<25
<25/<25
<25/<25
<25/<25
<25/<25
7.0/6.9
7.1/7.4
0.1/0.1
0.1/0.1
0.1/0.1
6.3/8.7
4.7/6.6
O.l/O.l
Maximum
Media Run I/
Media Run 2
30.1/25.9
30.1/31.5
NM
NM
NM
26.8/24.4
27.2/23.7
NM
4.7/3.3
5.1/9.6
NM
25.2/23.1
4.6/3.8
NM
6.7/2.1
23.6/22.0
NM
154/290
112/112
48.1/<25
43.7/<25
<25/<25
57.1/39.2
49.0/<25
<25/<25
24.8/15.7
22.0/14.2
5.0/1.0
1.4/0.8
0.8/0.6
10.5/10.3
9.2/8.3
0.5/0.5
Average
Media Run I/
Media Run 2
23.9/23.4
24.2/23.8
NM
NM
NM
23.2/22.2
23.2/22.4
NM
1.2/1.1
1.4/2.5
NM
21.8/21.6
1.9/2.1
NM
1.4/0.9
21.4/20.2
NM
59.9/98.6
50.8/53.5
<25/<25
<25/<25
<25/<25
27.5/<25
<25/<25
<25/<25
9.5/9.7
9.7/9.9
0.6/0.4
0.3/0.5
0.3/0.3
8.8/9.4
6.6/7.4
0.2/0.3
Standard
Deviation
Media Run I/
Media Run 2
2.5/1.7
2.6/2.1
NM
NM
NM
1.5/1.6
1.7/0.9
NM
1.5/1.4
1.9/3.7
NM
1.6/1.4
1.1/1.0
NM
1.9/0.7
1.2/1.5
NM
28.8/72.4
24.9/23.4
10.4/0.0
8.7/0.0
0.0/0.0
16.4/10.6
9.0/2.8
0.0/0.0
2.7/1.9
2.8/1.9
1.3/0.3
0.3/0.2
0.2/0.2
1.1/0.7
1.3/0.6
0.2/0.2
(a) See Table 3-3.
(b) Data not included in calculations for 06/09/04 or 01/20/05 due to suspected sampling errors.
(c) One outlier (i.e., 1,151 |ag/L on 07/19/06) not included in calculations.
NM = not meaningful for data related to breakthrough curves; see Figure 4-17 and Appendix B for results.
One-half of detection limit used for non-detect results for calculations.
Duplicate samples included for calculations.
40
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Table 4-11. Summary of Water Quality Parameter Measurements
Parameter
(Figure, if any)
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Orthophosphate
(as PO4)
Total P
(as PO4)
Silica
(as SiO2)
Sulfide
TSS
Nitrate
(asN)
Turbidity
pH
Sampling
Location'"'
IN
AC
TA
TB
TT
IN
AC
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
IN
AC
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
ug/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
NTU
NTU
s.u.
s.u.
s.u.
s.u.
s.u.
Number of
Samples
Media Run I/
Media Run 2
49/9
49/9
30/3
30/3
19/6
19/6
19/6
19/6
19/6
19/6
19/6
48/3
48/3
29/0
29/0
18/3(a)
0/6
0/6
0/3
0/3
0/3
49/9
49/9
30/3
30/3
19/6
22/3 l(b)
0/4
0/2
0/2
17/6
17/6
17/6
48/9
48/9
29/3
29/3
19/6
38/6
38/6
18/0
18/0
19/6
Concentration/Value
Minimum
Media Run I/
Media Run 2
164/180
170180
169/198
169/194
173/185
0.2/0.4
0.2/0.4
0.2/0.4
170/156
160/157
170/158
O.05/O.05
O.05/O.05
O.05/NA
O.05/NA
O.05/O.05
NA /O.03
NA /<0.03
NA /O.03
NA /<0.03
NA /O.03
36.4/36.5
36.4/36.2
35.3/36.1
36.2/35.6
36.6/33.7
<5/<5
NA/<1.0
NA/<1.0
NA/<1.0
O.04/O.04
O.04/O.04
O.04/O.04
0.2/0.2
0.1/0.1
O.l/O.l
<0.1/<0.1
O.l/O.l
7.6/7.7
7.6/7.7
7.6/ NA
7.6/ NA
7.6/7.7
Maximum
Media Run I/
Media Run 2
226/198
216/198
202/198
198/198
201/198
0.7/0.5
0.8/0.5
0.7/0.5
255/201
255/200
255/199
0.20/O.05
0.20/0.2
O.10/NA
O.10/NA
0.20/O.05
NA /O.03
NA /O.03
NA /O.03
NA /O.03
NA /O.03
41.8/39.6
41.7/39.6
39.9/38.1
40.0/38.1
40.6/38.9
5.7/<5
NA/1.0
NA/<1.0
NA/<1.0
O.04/0.2
0.6/0.4
0.1/1.0
3.5/1.5
2.4/1.4
2.7/0.6
0.8/0.8
0.7/0.2
8.1/7.9
8.0/7.9
8.0/ NA
7.9/ NA
8.0/7.9
Average
Media Run I/
Media Run 2
187/188
186/192
185/198
185/197
186/191
0.5/0.4
0.5/0.4
0.5/0.4
190/176
186/176
191/173
O.05/O.05
O.05/O.05
O.05/NA
O.05/NA
O.05/O.05
NA /O.03
NA /O.03
NA /O.03
NA /O.03
NA /O.03
38.3/37.8
38.2/37.8
37.9/37.0
38.0/36.9
38.2/37.6
<5/<5
NA/<1.0
NA/<1.0
NA/<1.0
O.04/0.1
0.06/0.12
O.04/0.2
0.7/0.7
0.5/0.4
0.3/0.2
0.2/0.3
0.2/0.1
7.7/7.8
7.7/7.8
7.8/ NA
7.8/ NA
7.7/7.8
Standard
Deviation
Media Run I/
Media Run 2
12/6
9/7
8/0
8/2
7/5
0.1/0.0
0.1/0.0
0.1/0.0
25/18
26/17
24/18
0.0/0.0
0.0/0.0
0.0/NA
0.0/NA
0.0/0.0
NA /O.O
NA /O.O
NA /O.O
NA /O.O
NA /O.O
1.0/1.0
1.1/1.1
1.0/1.0
1.1/1.3
1.0/2.0
0.0/0.0
NA /0.3
NA /O.O
NA /O.O
0.0/0.1
0.2/0.2
0.0/0.4
0.7/0.4
0.4/0.4
0.5/0.3
0.2/0.4
0.2/0.1
0.2/0.1
0.1/0.1
0.1/NA
0.1/NA
0.1/0.1
41
-------
Table 4-11. Summary of Water Quality Parameter Measurements (Continued)
Parameter
(Figure, if any)
Temperature
DO
ORP
Free Chlorine
(as C12)
Total Chlorine
(as C12)
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Sampling
Location'"'
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
AC
TA
TB
TT
AC
TA
TB
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
Unit
°C
°c
°c
°c
°c
mg/L
mg/L
mg/L
mg/L
mg/L
mV
mV
mV
mV
mV
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
Number of
Samples
Media Run I/
Media Run 2
38/6
38/6
18/0
18/0
19/6
38/6
38/6
18/0
18/0
19/6
26/6
27/6
11/0
11/0
16/6
35/6
17/0
15/0
19/6
33/2
15/0
13/0
18/1
19/6
19/6
19/6
19/6
19/6
19/6
19/6
19/6
19/6
Concentration/Value
Minimum
Media Run I/
Media Run 2
19.9/29.9
28.8/30.8
28.9/NA
29.0/ NA
29.5/30.8
0.1/0.1
0.2/0.1
0.4/ NA
0.4/ NA
0.2/0.2
20/14
454/370
471/NA
485/ NA
392/410
0.3/0.6
0.3/NA
0.3/NA
0.3/0.3
0.4/0.6
0.5/NA
0.5/NA
0.4/0.6
68.9/81.4
68.3/74.5
68.4/75.2
53.1/68.2
53.3/61.1
53.3/61.4
13.2/13.2
12.6/13.4
12.4/13.8
Maximum
Media Run I/
Media Run 2
31.6/31.6
31.6/31.8
31.2/NA
31.1/NA
31.7/31.8
1.9/0.3
2.0/0.3
2.0/ NA
1.9/NA
2.3/0.2
101/52
562/514
566/NA
576/ NA
561/576
0.7/1.0
0.6/ NA
0.6/ NA
0.7/0.7
0.8/0.8
0.7/ NA
0.7/ NA
0.8/0.6
102/90.0
111/87.4
110/88.1
83.7/75.5
91.9/73.1
86.5/74.2
20.0/15.0
19.2/15.1
23.5/15.1
Average
Media Run I/
Media Run 2
29.9/30.8
30.4/31.2
30.3/NA
30.3/NA
30.7/31.3
0.9/0.2
1.0/0.2
1.2/NA
1.2/NA
0.9/0.2
57/32
509/484
521/NA
527/ NA
511/511
0.5/0.8
0.5/NA
0.4/ NA
0.5/0.5
0.6/0.7
0.5/NA
0.5/NA
0.6/0.6
86.6/84.7
87.3/83.6
86.3/84.0
70.7/70.6
71.7/69.3
70.4/69.6
15.9/14.1
15.6/14.2
15.9/14.3
Standard
Deviation
Media Run I/
Media Run 2
1.8/0.7
0.7/0.5
0.7/ NA
0.6/ NA
0.6/0.4
0.5/0.1
0.5/0.1
0.4/ NA
0.4/ NA
0.6/0.0
22/17
30/56
29/NA
29/NA
39/54
0.1/0.2
0.1/NA
0.1/NA
0.1/0.1
0.1/0.1
0.1/NA
0.1/NA
0.1/NA
8.6/3.1
9.7/5.1
11.3/4.7
7.8/2.6
8.5/4.6
9.3/4.4
1.6/0.7
1.9/0.7
2.4/0.5
(a) One outlier (i.e., 1.4 mg/L on 11/29/05) not included in calculations.
(b) Includes 26 duplicate sampling events.
One-half of detection limit used for non-detect results for calculations.
Duplicate samples included for calculations.
to the levels around 5 |o,g/L at all effluent sampling locations thereafter, and increased gradually thereafter
through the end of the first media run. The actual breakthrough of the first media run occurred at
approximately 40,600 BV, representing about 62% of the vendor-estimated working capacity of 66,000
BV.
During the second media run (bottom of Figure 4-17), total arsenic concentrations at the effluent locations
increased gradually. Breakthrough of arsenic above the 10 |o,g/L MCL occurred at approximately 49,500
BV, representing about 58 % of the estimated working capacity of 85,200 BV.
42
-------
Arsenic Species at the Influent (IN)
35 -,
30 -
1 »-|
c
•2 20 -| |
1 15
c
o
0 10 H
{/)
5 1
0
y
35
30
ra 25
| 20
ro
§ 15-
c
o
0 10 -
3.
5
0
Arsenic Species after Chlorination (AC)
, Sampling errors.
suspected \
*•
B
s* <** ^ x y x x
35 -,
30 -
ra 25 -
| 20
£
•E „
" 10
3
5
DAs (particulate)
• As(V)
DAs (III)
Arsenic Species after the Combined Effluent (TT)
First
Media Run
Second
Media Run
Figure 4-16. Concentrations of Arsenic Species at Wellhead,
After Chlorination, and After Combined Effluent
43
-------
First Media Run Using E33-S
-•-At Influent
-*- After Chlorination
-•-After Vessel A
-A-After Vessel B
-*- After Combined Effluent
15 20 25 30 35
Bed Volumes of Water Treated (xlOOO)
Second Media Run Using E33-P
35
30 -
25 -
I20
-•-At Influent
-x- After Chlorination
-•-After Vessel A
-A-After Vessel B
-*- After Combined Effluent
6 15
10 -
5 -
10 15 20 25 30 35
Bed Volumes of Water Treated (xlOOO)
40
45
50
Figure 4-17. Total Arsenic Breakthrough Curves
44
-------
First Media Run Using E33-S
-•-At Influent
-*- After Chlorination
-•-After Vessel A
-A-After Vessel B
-*- After Combined Effluent
15 20 25 30 35
Bed Volumes of Water Treated (xlOOO)
30
Second Media Run Using E33-P
25
-•-At Influent
-x- After Chlorination
-•-After Vessel A
-A-After Vessel B
-*- After Combined Effluent
S> 20
8 15-
o
O
£ 10
o
5
10
15 20 25 30 35
Bed Volumes of Water Treated (xlOOO)
40
45
50
Figure 4-18. Total Manganese Concentrations Over Time
45
-------
Iron. Total iron concentrations in raw water ranged from <25 to 154 |o,g/L and averaged 59.9 |o,g/L during
the first media run, and from <25 to 290 |o,g/L and averaged 98.6 |o,g/L during the second media run
(except for one outlier of 1,151 |o,g/L on July 19, 2006, as shown in Table 4-10). Total iron
concentrations following prechlorination at the AC location ranged from <25 to 112 |o,g/L and averaged
50.8 |o,g/L during the first media run; and from <25 to 112 |o,g/L and averaged 53.5 |o,g/L during the second
media run. Nearly all of the total iron concentrations at the TA, TB, and TT locations were <25 |o,g/L and
with averaged concentrations <25 |o,g/L. Average dissolved iron concentrations were near and/or <25
Hg/L at all locations. These data indicate that the majority of the total iron entering the treatment system
was in particulate form, and that the iron particles were effectively captured by the media beds.
Manganese. Total Mn concentrations at the various sampling locations are plotted over time in Figure 4-
18. Total manganese levels in raw water ranged from 7.0 to 24.8 |o,g/L and averaged 9.5 |o,g/L during the
first media run, and ranged from 6.9 to 15.7 |o,g/L and averaged 9.7 |o,g/L during the second media run
(Table 4-10). Soluble manganese levels in raw water and after the prechlorination process averaged 8.8
and 6.6 |o,g/L, respectively, in the first run; they averaged 9.4 and 7.4 |o,g/L, respectively, in the second
media run. The data indicated that manganese existed primarily in the soluble form in raw water, and
chlorination precipitated only <25% (on average) of soluble manganese before water entered the
adsorption vessels. This observation was consistent with previous findings that free chlorine was
relatively ineffective at oxidizing Mn(II) at pH values less than 8.5 (Knocke et al., 1987 and 1990).
As shown in Table 4-10, total Mn concentrations at the TA, TB, and TT locations were reduced to 0.3 to
0.6 |o,g/L during both media runs, indicating removal of Mn by the SORB 33™ media. Knocke et al.
(1990) reported that the presence office chlorine in the filter promoted Mn(II) removal on MnOx-coated
media, and that in the absence office chlorine, Mn(II) removal was by adsorption only. In the absence of
free chlorine, SORB 33™ media apparently had a limited adsorptive capacity for Mn(II). The presence
of 0.3 to 1.0 mg/L (as C12) office chlorine (Table 4-11) apparently was enough to promote the removal of
manganese by the SORB 33™ media presumably via a mechanism similar to that proposed by Knocke et
al. (1990).
Other Water Quality Parameters. In addition to arsenic analyses, other water quality parameters were
analyzed to provide insight to the chemical processes occurring within the treatment system. The
complete water quality results are attached in Appendix B and summarized in Table 4-11.
Alkalinity (as CaCO3) ranged from 164 to 226 mg/L during the first media run and from 180 to 198 mg/L
during the second media run. Sulfate concentrations ranged from 170 to 255 mg/L during the first media
run and from 156 to 201 mg/L during the second media run. Both alkalinity and sulfate concentrations
remained relatively constant throughout the treatment train, indicating little or no effects by
prechlorination or the adsorptive media. Historically, sulfide odor in raw water had been detected by the
system operator. Sulfide analysis of raw water was conducted on 53 occasions (including 26 duplicate
samples). Sulfide was only detected for two events: 5.2 |o,g/L (5.1 |o,g/L for duplicate) on March 3, 2004
and 5.7 |o,g/L (<5 |o,g/L for duplicate) on March 31, 2004.
Fluoride concentrations ranged from 0.2 to 0.8 mg/L in all samples throughout the study. Fluoride
concentrations did not appear to be affected by the treatment. Orthophosphate (as PO4) concentrations
were below or near the method detection limit of 0.10 mg/L for all samples, with two exceptions (i.e.,
0.20 mg/L at IN, AC, and TT on January 23, 2004, and 1.4 mg/L, most likely an outlier, at TT on
November 17, 2004). Total P (as PO4) concentrations measured during the second media run were under
the method detection limit of 0.03 mg/L for all samples. Silica (as SiO2) concentrations, ranging from
33.7 to 40.6 mg/L in vessel effluent, were similar to the levels in raw water only 19 days after system
startup, indicating little or no adsorptive capacity for silica.
46
-------
Onsite pH measurements throughout the study remained consistent across the treatment train at 7.6 to 8.1.
DO levels ranged from 0.1 to 2.3 mg/L and were not affected by the prechlorination or the media. ORP
readings were collected using a dedicated ORP probe since April 14, 2004. ORP readings at the IN
location varied from 14 to 101 mV, indicating a reducing environment. After prechlorination, ORP
readings at the AC location increased significantly, ranging from 370 to 562 mV. ORP readings at
effluent locations (TA, TB, and TT) ranged from 392 to 576 mV. There did not appear to be a significant
difference in ORP values between the AC and treated water samples (TA, TB, and TT), indicating little or
no effect from the media.
Total hardness (as CaCO3) ranged from 68.9 to 102 mg/L in raw water, consisting predominantly of
calcium hardness (approximately 82%). Hardness was not affected by either prechlorination or the
media.
Sodium hypochlorite was added upstream of the treatment system. In addition to the original purpose of
disinfecting water, chlorine also oxidized As(III) to As(V) to increase the arsenic adsorptive capacity by
the media. Free and total chlorine were monitored at the AC, TA, TB, and TT sampling locations. Free
and total chlorine residuals at the AC location ranged from 0.3 to 1.0 mg/L and 0.4 to 0.8 mg/L,
respectively. Chlorine residuals measured at the TA, TB, and TT locations were similar to those
measured at the AC location, indicating little or no chlorine consumption through the APU-300 system.
4.5.2 Backwash Wastewater Sampling. Backwash wastewater was sampled periodically from
the sample ports located in the backwash effluent discharge lines from each vessel. Backwash was
performed using raw water (non-chlorinated). The unfiltered samples were analyzed for pH, turbidity,
and TDS/TSS. Filtered samples using 0.45-(im disc filters were analyzed for soluble arsenic, iron, and
manganese. For the last seven backwash wastewater sampling events (taking place since February 1,
2006, through the end of the performance evaluation study), TSS and total As, Fe, and Mn concentrations
also were measured. The analytical results are summarized in Table 4-12; results of the sample collected
on May 23, 2004 were not included in the data analysis due to a sampling error that the operator filled
bottles reserved for filtered samples with a portion of an unfiltered sample. Section 3.3.3 describes the
sampling procedures and modifications.
pH values of backwash wastewater ranged from 7.5 to 8.1, similar to those of raw water. Soluble arsenic
concentrations ranged from 6.4 to 25.7 |o,g/L and averaged 13.3 |o,g/L. This average concentration was
lower than that in raw water (i.e., 22.7 |o,g/L [on average]), indicating removal of some soluble arsenic by
the media during backwash. Soluble iron concentrations ranged from <25 to 373 |o,g/L and averaged
133 |og/L; soluble manganese concentrations ranged from 1.8 to 27.1 |o,g/L and averaged 10.5 |og/L.
Soluble Mn concentrations in backwash wastewater were slightly higher than those in raw water
(averaged 9.6 ng/L).
As expected, total arsenic, iron, and manganese concentrations were significantly higher than soluble
concentrations, indicating the presence of particulates in backwash wastewater. Particulate As might be
associated with either iron particles intercepted by the media beds during the service cycle or the media
fines. Assuming the average backwash flowrate was 200 gpm and the backwash duration was 25 min per
vessel (Table 4-4), the total amount of backwash wastewater generated during each backwash event
would be 10,000 gal. Assuming that 109 mg/L of TSS (i.e., the average of TSS values measured on May
10, June 6, July 18, and August 16, 2006) was produced in 10,000 gal of backwash wastewater from the
vessels, approximately 9.1 Ib of solids would be discharged during each backwash event. Based on the
average total metal (or, more correctly, digested metal) data collected during the last seven backwash
events (i.e., 53.3 (ig/L of particulate arsenic, 14,635 (ig/L of particulate iron, and 851 (ig/L of particulate
manganese), the solids discharged would be composed of 0.005, 1.2, and 0.07 Ib of arsenic, iron, and
47
-------
Table 4-12. Backwash Wastewater Sampling Results
Sampling
Event
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
Date
05/23/04(a)
07/13/04
09/30/04
11/17/04
12/06/04
02/07/05
06/14/05
07/07/05
09/15/05
10/12/05
1 1/09/05
02/01/06(c)
03/15/06
04/1 1/06
05/10/06
06/06/06
07/18/06
08/16/06
Vessel A
M
S.U.
7.5
7.9
8.0
7.8
7.6
7.6
7.8
7.8
7.6
8.0
7.9
8.0
8.1
7.9
8.0
7.9
8.0
7.9
Turbidity
NTU
180
220
0.2(b)
260
240
220
119(b)
70(b)
240
220
300
NS
NS
NS
NS
NS
NS
NS
VI
B
mg/L
NS
766
886
772
730
706
780
852
852
794
770
974
802
806
768
784
760
742
VI
ft!
mg/L
203
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
924
2,180
1,080
100
154
132
127
(K
"f,
"3
£
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
143
40.4
72.0
48.8
49.3
111
60.0
uble As
&
Mg/L
3.5
12.1
9.4
9.0
8.0
9.0
25.7
19.6
7.9
9.7
10.4
10.9
13.1
16.1
15.9
13.6
19.8
17.5
"ticulate As
03
a.
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
132
27.3
56.0
32.9
35.7
90.9
42.6
£
"3
£
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
28,818
5,463
30,841
6,915
12,758
16,632
13,187
uble Fe
&
Mg/L
825
69.8
160
136
25.0
140
70.0
50.0
111
26.7
<25
199
255
62.4
194
197
325
164
1
"3
£
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
1,620
453
1,224
443
793
1,381
910
uble Mn
&
Mg/L
89.0
7.6
13.0
7.6
2.1
7.3
6.3
6.9
11.1
3.6
2.7
15.4
17.7
6.8
19.2
16.1
21.7
12.0
Vessel B
W
o.
S.U.
7.9
7.9
8.1
7.9
7.7
7.9
7.9
7.9
7.7
8.0
7.9
8.1
8.1
8.0
8.0
7.9
7.9
7.9
Turbidity
NTU
99
160
0.1(b)
200
180
330
nl(b)
85(b)
170
280
110
NS
NS
NS
NS
NS
NS
NS
VI
B
mg/L
NS
756
780
794
710
742
772
872
798
786
766
782
812
762
758
744
938
786
VI
vi
mg/L
202
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
408
1,850
792
70
122
152
17
(K
"f,
"3
£
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
103
40.7
80.0
45.2
50.6
80.0
33.7
uble As
&
Mg/L
5.6
9.6
11.3
12.2
6.4
10.2
22.2
21.2
9.7
10.3
11.3
16.0
13.1
13.2
14.5
13.6
15.2
15.6
"ticulate As
03
a.
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
86.5
27.6
66.8
30.7
37.0
64.8
18.1
B
"3
£
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
32,793
10,106
18,599
4,317
11,049
13,999
2,229
uble Fe
&
Mg/L
2,166
83.0
176
152
38.0
175
53.0
57.4
106
35.9
<25
163
373
47.7
227
196
307
113
1
"3
£
Mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
1,267
468
1,035
383
707
1,110
266
uble Mn
&
Mg/L
131
8.2
13.5
10.2
2.6
8.8
4.8
7.3
9.7
4.1
1.8
12.5
27.1
5.3
19.9
16.2
19.7
9.2
(a) Operator filled sample bottle with a portion of unfiltered water.
(b) Sample analyzed outside of hold time.
(c) Sampling protocol hereafter revised to include TSS and total As, Fe, and Mn analyses.
NS = not sampled
-------
manganese, respectively (Table 4-12). These amounts, after being converted to the weights of
corresponding metal oxides, apparently were lower than those estimated based on TSS. Challenges
associated with sampling and sample digestion were believed to have contributed to the discrepancies
observed.
Table 4-13 presents the total metal results of backwash solid samples. Backwash solid samples were
collected three times on June 6, July 18, and August 16, 2006, from both Vessels A and B. The samples
collected were combined to obtain sufficient sample quantitative for total metal analysis and the results
are presented in Table 4-13. Iron levels in the solids averaged 329 mg/g (or 33%). Arsenic levels
averaged 1.4 mg/g (or 0.1
The total throughput between the backwash events conducted on June 6, July 18, and August 16, 2006 for
both Vessels A and B was 3,584,000 gal (Figure 4-15). Assuming the average total Fe in source water
was 98.6 (ig/L and all Fe in source water was collected by the media beds and discharged as backwash
solids during backwash events, then there would be approximately 1,338 g of solid Fe was discharged as
a part of TSS in the three backwash events. The average TSS values measured on June 6, July 18, and
August 16, 2006 was 117.3 mg/L (Table 4-12). Assuming 30,000 gal of backwash wastewater were
produced in the three backwash events from both vessels, approximately 13,320 g solids would be
discharged during the three backwash events. Therefore, the iron level in backwash solids can be
calculated as approximately 10%, which is less than one third of that calculated based on backwash solids
metal analysis, indicating the backwash solids contained significant amount of media fine.
Table 4-13. Backwash Solids Total Metal Analysis
Analyte
(Hg/g)
Vessel A
Vessel B
Mg
3,477
2,460
Al
5,855
4,071
Si
772
711
P
376
310
Ca
30,224
17,525
Mn
6,801
3,455
Fe
310,337
347,988
Ni
74.5
88.0
Cu
63.2
38.4
Zn
129
90.1
As
1,331
1,496
Cd
<0.5
0.5
Pb
13.5
3.6
Note: Solids collected from three backwash events (on June 6, July 18, and August 16, 2006)
and combined for sufficient sample quantity.
Average compositions calculated from triplicate analyses.
4.5.3 Spent Media Sampling. Spent media samples were collected for metals and TCLP analysis
(Section 3.3.4) at the end of the first media run on July 27, 2005, and the end of the second media run on
September 11, 2006. The results from TCLP analysis (Table 4-14) indicated that the media was non-
hazardous and could be disposed of in a sanitary landfill. Only barium was detected at 0.61 to 0.64 mg/L
on the spent SORB 33™-S media; and at 0.76 mg/L on the spent SORB 33™-P media. All other
Resources Conservation and Recovery Act (RCRA) metals were at concentrations less than the respective
method detection limits.
The ICP-MS results of spent media are shown in Table 4-15. The spent media contained mostly iron at
595 mg/g (as Fe) or 946 mg/g (as FeOOH) on the granular media, and at 457 mg/g (as Fe) or 727 mg/g
(as FeOOH) on the pelletized media. The FeOOH content of the spent granular media was higher than
the 90.1% (by weight) specified by the Bayer AG for the virgin media (Table 4-3), perhaps indicating
some iron attachment on the spent media during treatment. The FeOOH content of the spent pelletized
media, however, was significantly lower than the 90.1% specified by the Bayer AG for the virgin granular
media. STS indicated that the chemical contents are the same for both the granular and pelletized media.
It is not clear what caused the low iron content on the spent pelletized media. Challenges associated with
49
-------
Table 4-14. TCLP Results of Spent Media
Parameter
Arsenic (mg/L)
Barium (mg/L)
Cadmium (mg/L)
Chromium (mg/L)
Lead (mg/L)
Mercury (mg/L)
Selenium (mg/L)
Silver (mg/L)
Method
EPA 200.7
EPA 200.7
EPA 200.7
EPA 200.7
EPA 200.7
EPA 245.1
EPA 200.7
EPA 200.7
SORB 33™-S
Vessel A
<0.12
0.64
O.018
O.043
O.040
O.00036
<0.15
O.048
Vessel B
<0.12
0.61
<0.018
<0.043
<0.040
<0.00036
<0.15
O.048
SORB 33™-P
Vessel B
<0.10
0.76
<0.010
<0.010
<0.050
<0.0020
<0.10
<0.010
sampling and sample digestion were believed to have contributed to the discrepancies observed. The
spent granular media also contained higher concentrations of Al, Mn, Cu, Zn and As and lower
concentrations of P compared to the spent pelletized media.
The average arsenic loadings on the spent granular and pelletized media were 2.2 and 1.6 mg/g of dry
media based on the analytical results shown on Table 4-15. The adsorptive capacity also was calculated
by dividing the arsenic mass represented by the area between the influent (AC) and effluent (TT) curves,
as shown in Figure 4-17 by the amount of dry media in each vessel. Assuming no media loss, the dry
weight of the granular media, i.e., 1,913 Ib/vessel, was calculated based on a wet weight of 2,250 Ib (i.e.,
80 ft3 of media at 28.1 lb/ft3) and a maximum moisture content of 15% (Table 4-3). Similarly, the dry
weight of the pelletized media was calculated as 1,845 Ib/vessel. Using this approach, the theoretical
arsenic loadings on the media were calculated as 2.1 and 1.7 mg/g of dry media for the granular and
pelletized media, respectively; of which 105 and 94% were recovered via ICP-MS analysis. The
adsorptive capacities and percentages of recovery for both media are summarized in Table 4-16.
4.5.4 Distribution System Water Sampling. Distribution system samples were collected to
investigate if the water treated by the arsenic removal system would impact the lead, copper, and arsenic
levels and other water chemistry in the distribution system. Prior to the installation/operation of the
treatment system, baseline distribution water samples were collected on December 8, 11, and 30, 2003.
Following the installation of the treatment system, distribution water sampling continued on a monthly
basis at the same three locations. The sampling at the distribution system discontinued after December
14, 2005. The samples were analyzed for pH, alkalinity, arsenic, iron, manganese, lead, and copper. First
draw samples were collected at the three sampling locations according to the procedure noted in
Section 3.3.5. In addition, flushed samples also were collected at the DS2 and DS3 locations, which were
non-residences.
The main difference observed between the baseline samples and samples collected after the treatment
system startup was a decrease in arsenic concentrations at each of the sampling locations. Arsenic
concentrations were reduced from the range of 22.4 to 28.2 |o,g/L to 1.8 to 19.0 |og/L. Although the
arsenic concentrations measured during system operation were lower than the baseline values, they were
still higher than the APU-300 system effluent results. This phenomenon was due probably to the
blending of water produced by Well No. 3 in the distribution system with untreated water from Well
No. 2. A sample collected from Well No. 2 on June 2, 2004 contained 14.9 |o,g/L of total arsenic.
Measured pH values ranged from 7.1 to 8.2, and alkalinity levels ranged from 176 to 268 mg/L (as
CaCO3). Iron concentrations in the first draw samples ranged from <25 to 97.7 |og/L, except for two
samples at DS2 (i.e., 783 and 931 |o,g/L), with the majority of the samples <25 |o,g/L. Iron concentrations
50
-------
Table 4-15. Spent Media Total Metal Analysis
Analyte (^g/g)
Mg
Al
Si
P
Ca
Fe
Mn
Ni
Cu
Zn
As
Cd
Pb
Media Run 1: SORB 33™-S Samples Collected on 07/27/05
Vessel A - Top
Vessel A - Bottom
Vessel B - Top
Vessel B - Bottom
1,915
1,928
1,924
1,922
576
596
744
627
1,146
979
1,180
1,254
267
277
297
297
2,551
2,581
2,578
2,735
602,316
579,891
596,164
603,437
3,001
2,720
3,011
3,019
126
125
116
118
37.9
31.7
39.6
38.2
39.2
34.3
42.7
38.9
2,192
2,037
2,289
2,315
<0.2
<0.2
<0.2
<0.2
1.0
0.9
1.0
0.9
Media Run 2: SORB 33™ -P Samples Collected on 09/11/06
Vessel B - Top
Vessel B - Middle
Vessel B - Bottom
1,948
1,814
1,878
457
322
356
618
878
1,212
530
510
522
2,690
2,529
2,489
457,691
466,760
447,598
2,770
2,358
2,280
126
125
122
23.0
15.4
14.7
<50
<50
<50
1,767
1,488
1,483
<0.5
<0.5
<0.5
1.0
0.9
0.9
Note: Average compositions calculated from triplicate analyses.
Table 4-16. Summary of SORB 33 Media Adsorptive Capacities
Period
Source
Unit
Average
Recovery
Media Run 1
(01/16/04-07/14/05)
Breakthrough
Curve
(Figure 4-17)
Spent Media
(Table 4-15)
mg As/g dry SORB 33™-S
2.1(b)
2.2
105%
Media Run 2
(07/29/05-08/16/06)
-------
in the flushed samples from DS2 and DS3 ranged from <25 to 55 |o,g/L. In general, iron concentrations in
the distribution system samples decreased since the system began operating. Manganese concentrations
in the distribution system samples ranged from <0.1 to 94.1 |o,g/L, but the only results greater than
7.7 |og/L were first draw samples at DS2. Manganese levels appear slightly lower since the system began
to operate.
Lead levels ranged from 0.2 to 71.7 |og/L, with eight of the 119 samples exceeding the action level of
15 ng/L. Five of the action level exceedances for lead were from first draw samples at DS2, with the
remaining three exceedances in first draw samples from DS3. Copper concentrations ranged from <0.1 to
393 ng/L, with no samples exceeding the 1,300 |o,g/L action level. Neither lead nor copper concentrations
in the distribution system appeared to have been affected by the operation of the arsenic treatment unit.
The results of the distribution system sampling are summarized in Table 4-17.
4.6 System Cost
The cost of the system was evaluated based on the capital cost per gpm (or gpd) of design capacity and
the O&M cost per 1,000 gal of water treated. This task required tracking capital cost for the equipment,
site engineering, and installation and the O&M cost for media replacement and disposal, replacement
parts, chemical supply, electricity consumption, and labor. The building cost was not included in the
capital cost because it was outside of the scope of this demonstration project and was funded separately
by Desert Sands MDWCA.
4.6.1 Capital Cost. The capital investment for the equipment, site engineering, and installation
was $153,000 (see Table 4-18). The equipment cost was $112,000 (or 73% of the total capital
investment), which included $72,200 for the APU-300 skid-mounted unit, $24,000 for the SORB 33™
media (i.e., $5.34/lb to fill two vessels), and vendor's labor and travel for the system shakedown and
startup.
The engineering cost included preparation of the system layout and footprint, design of the piping
connections up to the distribution tie-in points, design of the electrical connections, and assemblage and
submission of the engineering plans for the permit application (Section 4.3.1). The engineering cost was
$23,000, which was 15% of the total capital investment.
The installation cost included equipment and labor to unload and install the APU-300 system, perform the
piping tie-ins and electrical work, and load and backwash the media (Section 4.3.3). The installation was
performed by STS and the Desert Sands MDWCA plant operator subcontracted to STS. A variety of
elevated pressure and flow restriction issues caused the actual system startup date to be delayed,
eventually prompting STS to redesign the system's piping, valving, and instruments and controls. The
costs for the system retrofitting were not included in this cost analysis. The installation costs were
$18,000, or 12% of the total capital investment.
The capital cost of $153,000 was normalized to $478/gpm ($0.33/gpd) of design capacity using the
system's rated capacity of 320 gpm (or 460,800 gpd). The capital cost also was converted to an
annualized cost of $14,442/yr using a capital recovery factor (CRF) of 0.09439 based on a 7% interest
rate and a 20-yr return period. Assuming that the system operated 24 hr/day, 7 day/wk at the design
flowrate of 320 gpm to produce 168,192,000 gal/yr, the unit capital cost would be $0.09/1,000 gal.
During the first media run, the system operated an average of only 7 hr/day (average of the first and
second media run, Table 4-7), producing 40,395,000 gal of water in one year, so the unit capital cost
increased to $0.37/1,000 gal at this reduced rate of usage.
52
-------
Table 4-17. Distribution System Sampling Results
Sampling
Event
No.
BL1
BL2
BL3
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
Date
12/08/03
12/11/03
12/30/03
02/11/04
03/10/04
04/07/04
05/12/04
06/23/04
07/21/04
08/18/04
09/15/04
10/13/04
11/10/04
12/08/04
01/20/05
02/16/05
03/16/05
04/13/05
05/11/05
06/22/05
08/03/05
09/14/05
10/12/05
1 1/09/05
12/14/05
DS1
LCR
1st Draw
1 Stagnation
Time
hr
8.0
8.5
7.7
8.5
7.8
8.5
8.1
8.1
8.1
8.1
8.1
8.1
8.1
8.8
7.5
7.8
8.0
7.4
8.0
7.5
8.1
8.2
9.0
8.2
7.8
o.
S.U.
7.1
7.8
7.7
7.6
7.8
7.7
7.8
8.0
7.7
7.5
7.8
7.7
7.9
8.0
7.5
7.9
7.9
8.1
7.3
7.6
7.5
7.6
7.8
7.7
7.9
Alkalinity
mg/L
200
178
197
207
230
249
223
183
188
180
226
207
201
211
211
201
201
220
185
189
176
220
194
176
198
•3
Mg/L
23.3
26.0
22.4
10.4
8.1
9.3
9.5
1.8
4.9
5.7
8.0
6.9
4.8
12.3
7.5
6.8
6.6
7.0
7.4
10.8
7.6
5.2
4.6
4.7
7.3
£
Mg/L
48.1
40.1
<25
49.2
<25
<25
<25
<25
<25
29.0
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
•
Mg/L
5.0
4.0
2.0
1.9
1.9
3.5
1.7
1.0
0.2
0.3
1.5
4.2
0.5
1.8
1.2
0.8
0.0
0.5
0.5
1.7
0.6
1.8
0.5
<0.1
0.7
£
Mg/L
0.9
0.6
1.1
0.4
0.7
0.2
1.7
2.0
0.2
1.7
0.3
0.3
1.3
0.2
0.2
0.3
0.1
0.2
0.4
0.3
0.3
0.5
0.3
0.4
0.4
0
Mg/L
9.1
7.1
17.0
14.1
12.5
7.5
156
33.7
4.1
23.7
10.2
6.8
65.1
5.5
8.7
12.1
5.0
5.4
4.4
5.1
3.3
4.9
<0.1
3.6
57.9
DS2
Non-Residence
-------
Desert Sands MDWCA constructed an addition to its existing pump house at Well No. 3 to house the
APU-300 system (Section 4.3.2). The structure was built by the Desert Sands MDWCA plant operator
with the exception of the electrical tie-in. The total cost for the building construction was $3,700,
including $2,700 for materials and $1,000 for approximately 80 hr of labor.
Table 4-18. Capital Investment for APU-300 System
Description
Cost
% of Capital Investment Cost |
Equipment
APU-300 Skid-Mounted System
SORB 33™ Media
Misc. Equipment and Materials
Vendor Labor
Vendor Travel
Equipment Total
$72,200
$24,000
$2,500
$9,500
$3,800
$112,000
—
2,250 Ib for SORB 33™-S;
2,170 Ib for SORB 33™-P
—
—
—
73%
Engineering
Subcontractor
Vendor Labor
Engineering Total
$16,300
$6,700
$23,000
-
-
15%
Installation
Subcontractor
Vendor Labor
Vendor Travel
Installation Total
Total Capital Investment
$9,000
$5,600
$3,400
$18,000
$153,000
-
-
-
12%
100%
4.6.2 O&M Cost. The O&M cost was $0.74/1,000 gal for media replacement and disposal,
replacement parts, chemical supply, electricity, and labor, as summarized in Table 4-19. The media
replacement and disposal cost was calculated based upon the throughput to arsenic breakthrough at the
end of the second media run for actual costs incurred (i.e., $30,900 to rebed both vessels). This media
changeout cost included costs for media, freight, labor, travel expenses, and a media profiling and
disposal fee. Upon arsenic breakthrough at 46,553,000 gal during the second media run, the media
replacement cost was $0.66/1,000 gal (Figure 4-19).
Because the system was under warranty during the first year of operation, no expenses were incurred for
repairs to the system during this time. However, after two years of operation, two actuated valves (121-A
and 123-A) began sticking and required replacement. A local company, Parmeter Power and Control,
was contracted to perform the replacement for $3,036. This cost included $2,625 for the two valves and
$411 for labor and travel costs. The new valves were installed on September 8, 2006.
The only chemical cost was the use NaOCl for prechlorination, which was in place prior to the installation
of the APU-300 system to provide chlorine residual prior to distribution. The APU-300 system did not
change the use rate of the NaOCl solution, so the chemical cost was negligible.
Electricity consumption also was negligible, particularly since the system retrofit in May 2004. After
retrofitting, the electric meter stopped registering power consumption. The operator assumed that the
meter was faulty, and replaced it with a new and factory-tested meter, which also did not register any
power consumption. It was then determined that the APU-300 system did not consume enough electricity
54
-------
to register regular increases on the meter (i.e., less than 1 kWh/week after retrofit compared to 3-4
kWh/week before retrofit).
The routine, non-demonstration related labor activities consumed only 15 min/day (Section 4.4.7). Based
on this time commitment and a labor rate of $18.20/hr, the labor cost was $0.05/1,000 gal of water
treated.
Table 4-19. O&M Costs for APU-300 System
Cost Category
Media Re
Media Cost ($/ft3)
Media Volume (ft3)
Media Replacement Cost ($)
Labor Cost ($)
Media Disposal Fee ($)
Subtotal ($)
Media Replacement and Disposal Cost
($71,000 gal)
Equii
Replacement Valves' Cost ($)
Labor and Travel Cost ($)
Equipment Replacement Cost ($71,000 gal)
Value
Remarks
placement and Disposal
$202
124
$25,080
$4,130
$1,690
$30,900
$0.66
-
SORB 33-P media
-
-
Waste profile included
-
Second media run throughput =
46,553,000 gal, see Figure 4-19
oment Replacement
$2,625
$411
$0.03
Two actuated valves
-
Total system throughput = 99,200,000 gal
Electricity
Electric Utility Charge ($7kWh)
Usage (kWh)
Total Electricity Cost ($)
Electricity Cost ($71,000 gal)
$0.14
126
$17.64
$0.00
Rate provided by DSMDWCA
-
Total system throughput = 99,200,000 gal
$0.01/1,000 gal prior to retrofit
Labor
Average Weekly Labor (hr)
Total Labor (hr)
Labor Cost ($71, 000 gal)
Total O&M Cost ($71,000 gal)
1.75
270
$0.05
$0.74
15 min/day
Total system throughput = 99,200,000 gal
Labor rate = $18.20/hr
See Figure 4-19
55
-------
• Total O&Mcost
Media replacement cost
20
30 40 50 60 70
Media Working Capacity (xlOOO BV)
80
90
100
Figure 4-19. Media Replacement and O&M Cost for APU-300 System
56
-------
5.0 REFERENCES
Battelle. 2003. Quality Assurance Project Plan for Evaluation of Arsenic Removal Technology.
Prepared under Contract No. 68-C-00-185, Task Order No. 0019, for U.S. Environmental
Protection Agency, National Risk Management Research Laboratory, Cincinnati, OH.
Chen, A.S.C., L. Wang, J.L. Oxenham, and W.E. Condit. 2004. Capital Costs of Arsenic Removal
Technologies: U.S. EPA Arsenic Removal Technology Demonstration Program Round 1.
EPA/600/R-04/201. U.S. Environmental Protection Agency, National Risk Management
Research Laboratory, Cincinnati, OH.
Chen, A.S.C., G.M. Lewis, L. Wang, A.Wang 2008. Draft Final Performance Evaluation Report:
Arsenic Removal from Drinking Water by Adsorptive Media EPA Demonstration Project at
Queen Anne's County, Maryland. Prepared under Contract No. 68-C-00-185, Task Order No.
0019 for Environmental Protection Agency, National Risk Management Research Laboratory,
Cincinnati, OH.
Cumming, L.J., A.S.C. Chen, and L. Wang 2008. Draft Final Performance Evaluation Report: Arsenic
Removal from Drinking Water by Adsorptive Media EPA Demonstration Project at Rollinsford,
NH. Prepared under Contract No. 68-C-00-185, Task Order No. 0037 for Environmental
Protection Agency, National Risk Management Research Laboratory, Cincinnati, OH.
Desert Sands MDWCA. 2002a. 40 Year Water Plan 2003-2004. July 18.
Desert Sands MDWCA. 2002b. Consumer Confidence Report for 2002.
Edwards, M., S. Patel, L. McNeill, H. Chen, M. Frey, A.D. Eaton, R.C. Antweiler, and H.E. Taylor. 1998.
"Considerations in As Analysis and Speciation." J. AWWA, 90(3): 103-113.
EPA. 2001. National Primary Drinking Water Regulations: Arsenic and Clarifications to Compliance
and New Source Contaminants Monitoring. Federal Register, 40 CFR Parts 9, 141, and 142.
EPA. 2002. Lead and Copper Monitoring and Reporting Guidance for Public Water Systems.
EPA/816/R-02/009. U.S. Environmental Protection Agency, Office of Water, Washington, D.C.
EPA. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic. Federal
Register, 40 CFR Part 141.
Knocke, W.R., R.C. Hoehn, and R.L. Sinsabaugh. 1987. "Using Alternative Oxidants to Remove
Dissolved Manganese from Waters Laden with Organics." J. AWWA, 79(3):15-19.
Knocke, W.R., J.E. Van Benschoten, M. Kearney, A. Soborski, and D.A. Reckhow. 1990. "Alternative
Oxidants for the Remove of Soluble Iron andMn." AWWA Research Foundation, Denver, CO. .
Severn Trent Services. 2004. Operation and Maintenance Manual, Model APU- 300, Desert Sands
MDWCA (Anthony), NM. June 30.
Wang, L., W.E. Condit, and A.S.C. Chen. 2004. Technology Selection and System Design: U.S. EPA
Arsenic Removal Technology Demonstration Program Round 1. EPA/600/R-05/001. U.S.
57
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Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
58
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APPENDIX A
OPERATIONAL DATA
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet
Week
No.
1
2
3
4
5
6
7
8
9
10
Date
01/23/04
01/24/04
01/25/04
01/26/04
01/27/04
01/28/04
01/29/04
01/30/04
01/31/04
02/01/04
02/02/04
02/03/04
02/04/04
02/05/04
02/09/04
02/10/04
02/11/04
02/12/04
02/13/04
02/16/04
02/17/04
02/18/04
02/19/04
02/20/04
02/23/04
02/24/04
02/25/04
02/26/04
02/27/04
02/28/04
02/29/04
03/01/04
03/02/04
03/03/04
03/04/04
03/05/04
03/06/04
03/07/04
03/08/04
03/09/04
03/10/04
03/11/04
03/12/04
03/13/04
03/14/04
03/15/04
03/16/04
03/17/04
03/18/04
03/19/04
03/20/04
03/21/04
03/22/04
03/23/04
03/24/04
03/25/04
03/26/04
03/27/04
03/28/04
Pump House Instrument Panel
Operation
Hours
hr
0.0
4.9
8.1
5.0
2.0
5.0
4.0
4.0
3.0
4.0
4.0
5.6
1.3
8.0
11.5
0.4
5.7
4.7
4.9
14.1
5.2
5.0
7.5
5.5
11.4
4.3
4.3
3.9
2.9
4.0
4.2
4.1
4.6
4.0
4.6
6.9
5.0
5.9
1.7
2.8
5.0
5.8
3.3
3.4
6.2
3.0
7.6
6.9
1.9
8.4
2.2
3.3
3.2
4.0
5.1
5.8
4.3
3.6
3.5
Cumulative
Operation
Hours
hr
0.0
4.9
13.0
18.0
20.0
25.0
29.0
33.0
36.0
40.0
44.0
49.6
50.9
58.9
70.4
70.8
76.5
81.2
86.1
100.2
105.4
110.4
117.9
123.4
134.8
139.1
143.4
147.3
150.2
154.2
158.4
162.5
167.1
171.1
175.7
182.6
187.6
193.5
195.2
198.0
203.0
208.8
212.1
215.5
221.7
224.7
232.3
239.2
241.1
249.5
251.7
255.0
258.2
262.2
267.3
273.1
277.4
281.0
284.5
Master
Flow Meter
kgal
234,081
234,153
234,282
234,359
234,403
234,476
234,540
234,597
234,658
234,713
234,771
234,845
234,866
234,989
235,167
235,174
235,225
235,333
235,408
235,623
235,701
235,777
235,891
235,976
236,151
236,216
236,282
236,342
236,387
236,448
236,511
236,575
236,644
236,715
236,775
236,801
236,876
236,966
236,994
237,035
237,112
237,201
237,253
237,305
237,377
237,455
237,564
237,671
237,698
237,799
237,864
237,924
237,963
238,025
238,103
238,199
238,258
238,315
238,369
Flow
Totalizer
Vessel A
kgal
221
266
335
375
399
438
471
501
538
568
584
600
615
620
753
756
799
830
863
956
990
1,025
1,074
1,112
1,192
1,221
1,250
1,279
1,298
1,327
1,356
1,384
1,415
1,446
1,475
1,480
1,521
1,563
1,563
1,594
1,631
1,671
1,694
1,717
1,749
1,784
1,839
1,889
1,902
1,949
1,979
2,003
2,025
2,053
2,088
2,138
2,166
2,192
2,217
Flow
Totalizer
Vessel B
kgal
216
259
327
367
391
428
461
491
526
558
603
663
681
757
868
872
926
969
1,015
1,111
1,158
1,207
1,277
1,328
1,436
1,476
1,516
1,555
1,582
1,623
1,660
1,698
1,740
1,782
1,820
1,836
1,883
1,936
1,936
1,977
2,022
2,083
2,105
2,137
2,180
2,227
2,299
2,360
2,377
2,434
2,472
2,502
2,531
2,567
2,613
2,676
2,710
2,743
2,775
Total
Flow
Daily
kgal
NA
88
137
80
48
76
66
60
72
62
61
76
33
81
244
7
97
74
79
189
81
84
119
89
188
69
69
68
46
70
66
66
73
73
67
21
88
95
0
72
82
101
45
55
75
82
127
111
30
104
68
54
51
64
81
113
62
59
57
Cumulative
Flow
Totalizer
kgal
NA
88
225
305
353
429
495
555
627
689
750
826
859
940
1,184
1,191
1,288
1,362
1,441
1,630
1,711
1,795
1,914
2,003
2,191
2,260
2,329
2,397
2,443
2,513
2,579
2,645
2,718
2,791
2,858
2,879
2,967
3,062
3,062
3,134
3,216
3,317
3,362
3,417
3,492
3,574
3,701
3,812
3,842
3,946
4,014
4,068
4,119
4,183
4,264
4,377
4,439
4,498
4,555
Cumulative
Total Bed
Volumes
#of BV
NA
73
188
254
294
358
413
463
523
574
625
688
716
783
987
993
1073
1135
1201
1358
1426
1496
1595
1669
1826
1883
1941
1998
2036
2094
2149
2204
2265
2326
2382
2399
2473
2552
2552
2612
2680
2764
2802
2848
2910
2978
3084
3177
3202
3288
3345
3390
3433
3486
3553
3648
3699
3748
3796
Head Loss
(psi)
Vessel A
>15
off
off
off
off
>15
off
off
off
off
off
off
24
off
off
>15
>15
>15
off
off
off
>15
off
off
off
off
>15
off
off
off
off
off
off
>15
off
off
>15
>15
>15
off
>15
off
off
off
off
>20
off
>20
>20
off
>20
off
>20
off
>20
off
off
off
off
Vessel B
>15
off
off
off
off
>15
off
off
off
off
off
off
24
off
off
>15
>15
>15
off
off
off
>15
off
off
off
off
>15
off
off
off
off
off
off
>15
off
off
>15
>15
>15
off
>15
off
off
off
off
>20
off
>20
>20
off
>20
off
>20
off
>20
off
off
off
off
System Pressure
(psig)
Influent
76
52
56
58
54
78
54
60
60
60
55
60
80
52
NM
84
84
86
56
54
50
82
54
50
50
50
82
52
50
50
50
50
52
82
54
59
82
84
82
off
80
off
off
off
off
80
off
82
off
off
84
54
84
off
84
off
off
off
off
Effluent
56
52
56
58
54
60
54
60
60
60
55
60
56
52
NM
54
56
56
56
54
50
56
54
50
50
50
56
52
50
50
50
50
52
58
54
54
60
60
56
off
56
off
off
off
off
60
off
60
off
off
62
off
62
off
off
off
off
off
off
AP
psig
20
NA
NA
NA
NA
18
NA
NA
NA
NA
NA
NA
24
NA
NA
30
28
30
NA
NA
NA
26
NA
NA
NA
NA
26
NA
NA
NA
NA
NA
NA
24
NA
5
22
24
26
NA
24
NA
NA
NA
NA
20
NA
22
NA
NA
22
NA
22
NA
NA
NA
NA
NA
NA
A-l
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
11
12
13
14
15
16
17
18
19
20
Date
03/29/04
03/30/04
03/31/04
04/01/04
04/02/04
04/03/04
04/04/04
04/05/04
04/06/04
04/07/04
04/08/04
04/09/04
04/10/04
04/11/04
04/12/04
04/13/04
04/14/04
04/15/04
04/16/04
04/17/04
04/18/04
04/19/04
04/20/04
04/21/04
04/22/04
04/23/04
04/24/04
04/25/04
04/26/04
04/27/04
04/28/04
04/29/04
04/30/04
05/01/04
05/02/04
05/03/04
05/04/04
05/05/04
05/06/04
05/07/04
05/08/04
05/09/04
05/10/04
05/11/04
05/12/04
05/13/04
05/14/04
05/15/04
05/16/04
05/1 7/04
05/18/04
05/19/04
05/20/04
05/21/04
05/22/04
05/23/04
05/24/04
05/25/04
05/26/04
05/27/04
05/28/04
05/29/04
05/30/04
05/31/04
06/01/04
06/02/04
06/03/04
06/04/04
06/05/04
06/06/04
Pump House Instrument Panel
Operation
Hours
hr
4.3
3.5
4.3
4.8
2.9
3.0
NA
6.3
2.9
2.0
3.9
2.8
3.5
2.9
3.2
2.9
3.2
4.3
3.4
4.0
3.4
4.0
3.6
4.1
2.9
3.3
3.8
4.4
3.8
4.0
4.0
3.1
3.8
5.4
5.1
2.8
3.9
4.5
6.6
5.7
6.2
6.0
5.7
7.5
4.0
6.9
3.3
5.7
12.9
Cumulative
Operation
Hours
hr
288.8
292.3
296.6
301.4
304.3
307.3
NA
313.6
316.5
318.5
322.4
325.2
328.7
331.6
334.8
337.7
340.9
345.2
348.6
352.6
356.0
360.0
363.6
367.7
370.6
373.9
377.7
382.1
385.9
389.9
393.9
397.0
400.8
406.2
411.3
414.1
418.0
422.5
429.1
434.8
441.0
447.0
452.7
460.2
464.2
471.1
474.4
480.1
493.0
Master
Flow Meter
kgal
238,434
238,494
238,554
238,628
238,674
238,719
238,772
238,816
238,868
238,893
238,952
238,995
239,049
239,093
239,135
239,188
239,235
239,301
239,353
239,413
239,465
239,525
239,580
239,634
239,687
239,737
239,795
239,860
239,919
239,980
240,023
240,101
240,147
240,230
240,291
240,360
240,400
240,478
240,577
240,664
240,759
240,849
240,936
241,034
241,110
241,215
241,266
241,353
241,554
Flow
Totalizer
Vessel A
kgal
2,246
2,273
2,301
2,341
2,363
2,384
2,408
2,428
2,449
2,464
2,497
2,517
2,542
2,562
2,582
2,606
2,627
2,664
2,688
2,715
2,739
2,767
2,791
2,816
2,846
2,870
2,896
2,926
2,953
2,955
2,955
2,955
2,983
3,022
3,030
3,077
3,104
3,136
3,188
3,229
3,274
3,315
3,356
3,402
3,436
3,493
3,517
3,557
3,663
Flow
Totalizer
Vessel B
kgal
2,813
2,848
2,884
2,934
2,960
2,987
3,018
3,043
3,071
3,090
3,130
3,155
3,186
3,212
3,237
3,268
3,296
3,341
3,372
3,407
3,438
3,473
3,505
3,537
3,575
3,604
3,638
3,676
3,711
3,746
3,779
3,817
3,850
3,895
3,953
3,968
4,002
4,042
4,107
4,157
4,210
4,262
4,312
4,368
4,412
4,478
4,507
4,557
4,649
Total
Flow
Daily
kgal
67
62
64
90
48
48
55
45
49
34
73
45
56
46
45
55
49
82
55
62
55
63
56
57
68
53
60
68
62
37
33
38
61
84
66
62
61
72
117
91
98
93
91
102
78
123
53
90
198
Cumulative
Flow
Totalizer
kgal
4,622
4,684
4,748
4,838
4,886
4,934
4,989
5,034
5,083
5,117
5,190
5,235
5,291
5,337
5,382
5,437
5,486
5,568
5,623
5,685
5,740
5,803
5,859
5,916
5,984
6,037
6,097
6,165
6,227
6,264
6,297
6,335
6,396
6,480
6,546
6,608
6,669
6,741
6,858
6,949
7,047
7,140
7,231
7,333
7,411
7,534
7,587
7,677
7,875
Cumulative
Total Bed
Volumes
#of BV
3852
3903
3957
4032
4072
4112
4158
4195
4236
4264
4325
4363
4409
4448
4485
4531
4572
4640
4686
4738
4783
4836
4883
4930
4987
5031
5081
5138
5189
5220
5248
5279
5330
5400
5455
5507
5558
5618
5715
5791
5873
5950
6026
6111
6176
6278
6323
6398
6563
Head Loss
(psi)
Vessel A
off
off
off
off
off
off
off
off
off
>20
off
off
off
off
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
Vessel B
off
off
off
off
off
off
off
off
off
>20
off
off
off
off
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
>20
System Pressure
(psig)
Influent
NM
NM
NM
NM
NM
NM
NM
NM
NM
60
NM
NM
NM
NM
82
82
84
84
82
84
84
84
84
82
82
80
80
80
82
82
82
82
82
82
82
82
82
80
80
82
80
80
82
80
80
80
80
80
80
Effluent
60
60
58
60
58
58
60
60
60
82
62
58
60
60
60
60
60
60
60
60
60
60
60
58
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
58
60
60
60
60
60
AP
psig
NA
NA
NA
NA
NA
NA
NA
NA
NA
22
NA
NA
NA
NA
22
22
24
24
22
24
24
24
24
24
22
20
20
20
22
22
22
22
22
22
22
22
22
20
20
22
20
20
22
22
20
20
20
20
20
System was turned off for repairing
4.6
7.0
6.2
5.8
3.8
8.9
6.4
6.5
8.8
7.8
6.9
5.3
6.8
6.4
497.6
504.6
510.8
516.6
520.4
529.3
535.7
542.2
551.0
558.8
565.7
571.0
577.8
584.2
241,646
241,746
241,846
241,940
242,002
242,146
242,248
242,353
242,498
242,617
242,725
242,810
242,917
243,018
3,663
3,705
3,759
3,809
3,842
3,919
3,972
4,029
4,104
4,166
4,223
4,266
4,321
4,373
4,649
4,752
4,779
4,820
4,852
4,929
4,983
5,040
5,116
5,179
5,231
5,283
5,341
5,396
0
145
81
91
65
154
107
114
151
125
109
95
113
107
7,875
8,020
8,101
8,192
8,257
8,411
8,518
8,632
8,783
8,908
9,017
9,112
9,225
9,332
6563
6683
6751
6827
6881
7009
7098
7193
7319
7423
7514
7593
7688
7777
2.8
3.0
3.0
off
off
3.0
3.0
3.0
2.8
3.0
off
off
4.0
3.0
3.0
3.0
3.0
off
off
3.0
3.0
3.0
3.0
3.0
off
off
4.0
3.0
66
68
64
52
52
56
62
66
68
60
off
off
60
56
60
62
58
52
52
50
56
60
62
54
52
50
52
50
6
6
6
NA
NA
6
6
6
6
6
NA
NA
8
6
A-2
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
21
22
23
24
25
26
27
28
29
30
Date
06/07/04
06/08/04
06/09/04
06/10/04
06/11/04
06/12/04
06/13/04
06/14/04
06/15/04
06/16/04
06/17/04
06/18/04
06/19/04
06/20/04
06/21/04
06/22/04
06/23/04
06/24/04
06/25/04
06/26/04
06/27/04
06/28/04
06/29/04
06/30/04
07/01/04
07/02/04
07/03/04
07/04/04
07/05/04
07/06/04
07/07/04
07/08/04
07/09/04
07/10/04
07/11/04
07/12/04
07/13/04
07/14/04
07/15/04
07/16/04
07/17/04
07/18/04
07/19/04
07/20/04
07/21/04
07/22/04
07/23/04
07/24/04
07/25/04
07/26/04
07/27/04
07/28/04
07/29/04
07/30/04
07/31/04
08/01/04
08/02/04
08/03/04
08/04/04
08/05/04
08/06/04
08/07/04
08/08/04
08/09/04
08/10/04
08/11/04
08/12/04
08/13/04
08/14/04
08/15/04
Pump House Instrument Panel
Operation
Hours
hr
9.2
6.7
10.4
9.2
4.4
9.5
6.1
10.3
9.2
7.5
9.7
8.1
8.9
6.0
15.0
9.1
5.5
9.8
5.8
6.4
6.0
6.4
7.3
5.5
6.8
5.9
10.2
5.3
8.3
9.1
6.1
13.4
8.0
9.9
8.0
8.3
4.7
13.4
8.3
7.0
11.7
9.0
8.7
9.5
6.7
12.1
8.2
9.9
3.8
8.2
5.6
14.8
6.2
7.5
5.4
6.6
4.3
7.8
5.2
9.9
9.0
8.1
8.4
7.7
8.5
8.5
7.1
5.9
4.3
4.0
Cumulative
Operation
Hours
hr
593.4
600.1
610.5
619.7
624.1
633.6
639.7
650.0
659.2
666.7
676.4
684.5
693.4
699.4
714.4
723.5
729.0
738.8
744.6
751.0
757.0
763.4
770.7
776.2
783.0
788.9
799.1
804.4
812.7
821.8
827.9
841.3
849.3
859.2
867.2
875.5
880.2
893.6
901.9
908.9
920.6
929.6
938.3
947.8
954.5
966.6
974.8
984.7
988.5
996.7
1002.3
1017.1
1023.3
1030.8
1036.2
1042.8
1047.1
1054.9
1060.1
1070.0
1079.0
1087.1
1095.5
1103.2
1111.7
1120.2
1127.3
1133.2
1137.5
1141.5
Master
Flow Meter
kgal
243,164
243,270
243,432
243,576
243,645
243,795
243,891
244,054
244,203
244,321
244,477
244,606
244,747
244,843
245,019
245,164
245,251
245,407
245,509
245,602
245,706
245,794
245,911
245,999
246,109
246,205
246,368
246,455
246,588
246,735
246,832
247,046
247,175
247,333
247,468
247,597
247,672
247,886
248,022
248,136
248,328
248,468
248,609
248,763
248,872
249,069
249,197
249,349
249,418
249,549
249,625
249,697
249,798
249,918
250,003
250,112
Flow
Totalizer
Vessel A
kgal
4,446
4,499
4,580
4,652
4,680
4,761
4,808
4,837
4,910
4,972
5,055
5,123
5,198
5,248
5,349
5,415
5,461
5,542
5,589
5,643
5,697
5,742
5,803
5,849
5,907
5,958
6,045
6,090
6,158
6,227
6,277
6,384
6,453
6,535
6,603
6,667
6,703
6,815
6,886
6,947
7,046
7,120
7,194
7,274
7,332
7,456
7,501
7,580
7,651
7,685
7,727
7,765
7,820
7,887
7,934
7,997
250,191 8,041
250,310
250,402
250,554
250,647
250,778
250,915
8,109
8,159
8,246
8,300
8,376
8,446
251,038 8,495
251,177
251,317
251,423
251,528
251,600
251,665
8,572
8,647
8,704
8,760
8,796
8,831
Flow
Totalizer
Vessel B
kgal
5,476
5,534
5,621
5,700
5,739
5,821
5,872
5,970
6,054
6,116
6,197
6,263
6,337
6,387
6,479
6,555
6,600
6,683
6,732
6,786
6,841
6,887
6,948
6,994
7,051
7,101
7,189
7,230
7,301
7,385
7,437
7,554
7,621
7,705
7,777
7,848
7,891
8,006
8,076
8,137
8,237
8,311
8,385
8,466
8,522
8,626
8,694
8,774
8,811
8,882
8,924
8,961
9,013
9,072
9,114
9,166
9,205
9,261
9,308
9,380
9,414
9,486
9,559
9,640
9,708
9,803
9,834
9,888
9,924
9,957
Total
Flow
Daily
kgal
153
111
168
151
67
163
98
127
157
124
164
134
149
100
193
142
91
164
96
108
109
91
122
92
115
101
175
86
139
153
102
224
136
166
140
135
79
227
141
122
199
148
148
161
114
228
113
159
108
105
84
75
107
126
89
115
83
124
97
159
88
148
143
130
145
170
88
110
72
68
Cumulative
Flow
Totalizer
kgal
9,485
9,596
9,764
9,915
9,982
10,145
10,243
10,370
10,527
10,651
10,815
10,949
11,098
11,198
11,391
11,533
11,624
11,788
11,884
11,992
12,101
12,192
12,314
12,406
12,521
12,622
12,797
12,883
13,022
13,175
13,277
13,501
13,637
13,803
13,943
14,078
14,157
14,384
14,525
14,647
14,846
14,994
15,142
15,303
15,417
15,645
15,758
15,917
16,025
16,130
16,214
16,289
16,396
16,522
16,611
16,726
16,809
16,933
17,030
17,189
17,277
17,425
17,568
17,698
17,843
18,013
18,101
18,211
18,283
18,351
Cumulative
Total Bed
Volumes
#of BV
7904
7997
8137
8263
8318
8454
8536
8642
8773
8876
9013
9124
9248
9332
9493
9611
9687
9823
9903
9993
10084
10160
10262
10338
10434
10518
10664
10736
10852
10979
11064
11251
11364
11503
11619
11732
11798
11987
12104
12206
12372
12495
12618
12753
12848
13038
13132
13264
13354
13442
13512
13574
13663
13768
13843
13938
14008
14111
14192
14324
14398
14521
14640
14748
14869
15011
15084
15176
15236
15293
Head Loss
(psi)
Vessel A
off
3.0
5.0
5.0
6.0
off
off
off
3.0
off
4.0
off
off
off
3.0
off
3.0
off
off
6.0
off
8.0
off
10.0
3.0
3.0
off
off
3.5
off
4.0
off
off
off
6.0
3.0
off
off
off
3.0
off
off
off
3.5
4.0
off
off
off
5.5
6.5
3.0
off
off
off
3.5
off
4.0
off
4.5
off
5.6
off
off
9.5
off
off
3.0
off
off
off
Vessel B
off
3.0
5.0
6.0
8.0
off
off
off
3.0
off
4.0
off
off
off
2.5
off
3.0
off
off
6.0
off
8.0
off
10.0
2.8
3.0
off
off
3.0
off
3.0
off
off
off
6.0
3.0
off
off
off
3.0
off
off
off
3.5
4.0
off
off
off
5.5
6.5
3.0
off
off
off
3.5
off
4.0
off
4.5
off
5.6
off
off
3.0
off
off
3.0
off
off
off
System Pressure
(psig)
Influent
off
56
62
67
64
off
off
off
66
off
70
off
off
off
60
off
58
off
off
72
off
76
off
80
62
58
off
off
62
off
63
off
off
off
68
62
off
off
off
62
off
off
off
61
68
off
off
NM
65
65
60
off
off
off
59
off
64
off
61
off
66
off
67
66
off
off
64
off
off
off
Effluent
58
50
52
56
58
52
58
58
60
62
62
58
60
52
56
off
52
58
60
60
58
60
62
60
56
52
60
58
56
52
54
58
60
62
56
56
54
56
56
56
52
52
52
54
60
56
54
NM
54
52
54
56
58
58
52
56
56
54
52
56
56
52
56
52
50
56
58
56
54
53
AP
psig
NA
6
10
11
6
NA
NA
NA
6
NA
8
NA
NA
NA
4
NA
6
NA
NA
12
NA
16
NA
20
6
6
NA
NA
6
NA
9
NA
NA
NA
12
6
NA
NA
NA
6
NA
NA
NA
7
8
NA
NA
NA
11
13
6
NA
NA
NA
7
NA
8
NA
9
NA
10
NA
11
14
NA
NA
6
NA
NA
NA
A-3
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
31
32
33
34
35
36
37
38
39
40
Date
08/16/04
08/17/04
08/18/04
08/19/04
08/20/04
08/21/04
08/22/04
08/23/04
08/24/04
08/25/04
08/26/04
08/27/04
08/28/04
08/29/04
08/30/04
08/31/04
09/01/04
09/02/04
09/03/04
09/04/04
09/05/04
09/06/04
09/07/04
09/08/04
09/09/04
09/10/04
09/11/04
09/12/04
09/13/04
09/14/04
09/15/04
09/16/04
09/17/04
09/18/04
09/19/04
09/20/04
09/21/04
09/22/04
09/23/04
09/24/04
09/25/04
09/26/04
09/27/04
09/28/04
09/29/04
09/30/04
10/01/04
10/02/04
10/03/04
10/04/04
10/05/04
10/06/04
10/07/04
10/08/04
10/09/04
10/10/04
10/11/04
10/12/04
10/13/04
10/14/04
10/15/04
10/16/04
10/17/04
10/18/04
10/19/04
10/20/04
10/21/04
10/22/04
10/23/04
10/24/04
Pump House Instrument Panel
Operation
Hours
hr
3.4
3.2
2.0
4.8
4.3
4.8
4.8
5.9
10.4
3.8
5.2
6.1
4.9
5.6
4.9
5.5
5.9
6.0
5.6
4.6
4.4
4.5
5.5
4.9
5.2
5.5
5.3
6.3
5.8
4.9
5.7
5.5
6.0
5.7
5.2
3.8
3.6
4.3
3.7
4.2
3.9
3.4
4.0
4.3
6.4
5.4
1.6
5.5
4.6
3.5
4.3
3.5
4.0
3.5
4.0
4.1
3.7
3.5
4.8
6.2
3.4
3.1
3.7
3.5
3.7
3.3
5.4
3.3
2.9
4.1
Cumulative
Operation
Hours
hr
1144.9
1148.1
1150.1
1154.9
1159.2
1164.0
1168.8
1174.7
1185.1
1188.9
1194.1
1200.2
1205.1
1210.7
1215.6
1221.1
1227.0
1233.0
1238.6
1243.2
1247.6
1252.1
1257.6
1262.5
1267.7
1273.2
1278.5
1284.8
1290.6
1295.5
1301.2
1306.7
1312.7
1318.4
1323.6
1327.4
1331.0
1335.3
1339.0
1343.2
1347.1
1350.5
1354.5
1358.8
1365.2
1370.6
1372.2
1377.7
1382.3
1385.8
1390.1
1393.6
1397.6
1401.1
1405.1
1409.2
1412.9
1416.4
1421.2
1427.4
1430.8
1433.9
1437.6
1441.1
1444.8
1448.1
1453.5
1456.8
1459.7
1463.8
Master
Flow Meter
kgal
Flow
Totalizer
Vessel A
kgal
251,721 8,864
251,774
251,807
251,885
251,954
252,034
252,112
252,209
252,376
252,437
252,523
252,622
252,703
252,795
252,880
252,965
253,060
253,167
253,250
253,326
253,397
253,472
253,561
253,641
253,725
253,815
253,901
254,007
254,101
254,181
254,275
254,365
254,465
254,556
254,641
254,704
254,767
254,833
254,894
254,965
255,028
255,090
255,150
255,221
255,324
255,411
255,439
255,530
255,606
255,663
255,733
255,793
255,857
255,916
255,982
256,047
256,110
256,176
256,247
256,347
256,403
256,454
256,515
256,573
256,633
256,696
256,776
256,830
256,879
256,946
8,892
8,910
8,948
8,982
9,026
9,069
9,123
9,216
9,249
9,282
9,322
9,365
9,414
9,459
9,504
9,555
9,611
9,656
9,697
9,736
9,777
9,827
9,871
9,918
9,969
10,018
10,071
10,120
10,163
10,212
10,261
10,313
10,361
10,408
10,439
10,477
10,513
10,545
10,582
10,615
10,648
10,680
10,719
10,776
10,823
10,835
10,882
10,922
10,951
10,988
11,020
11,054
11,085
11,120
11,155
11,188
11223
11,261
11,313
11,337
11,358
11,382
11,402
11423
11,445
11,485
11,513
11,538
11,573
Flow
Totalizer
Vessel B
kgal
9,986
10,013
10,030
10,073
10,112
10,152
10,190
10,238
10,319
10,349
10,425
10,470
10,511
10,558
10,602
10,646
10,695
10,750
10,793
10,831
10,867
10,904
10,947
10,986
11,028
11,071
11,112
11,170
11,219
11,261
11,309
11,355
11,407
11,454
11,496
11,526
11,554
11,592
11,624
11,660
11,693
11,737
11,737
11,792
11,842
11,887
11,904
11,952
11,991
12,021
12,057
12,088
12,122
12,152
12,186
12,219
12,251
12285
12,321
12,373
12,408
12,441
12,481
12,520
12561
12,606
12,649
12,673
12,703
12,738
Total
Flow
Daily
kgal
62
55
35
81
73
84
81
102
174
63
109
85
84
96
89
89
100
111
88
79
75
78
93
83
89
94
90
111
98
85
97
95
104
95
89
61
66
74
64
73
66
77
32
94
107
92
29
95
79
59
73
63
68
61
69
68
65
69
74
104
59
54
64
59
62
67
83
52
55
70
Cumulative
Flow
Totalizer
kgal
18,413
18,468
18,503
18584
18657
18741
18822
18924
19098
19161
19270
19355
19439
19535
19624
19713
19813
19924
20012
20091
20166
20244
20337
20420
20509
20603
20693
20804
20902
20987
21084
21179
21283
21378
21467
21528
21594
21668
21732
21805
21871
21948
21980
22074
22181
22273
22302
22397
22476
22535
22608
22671
22739
22800
22869
22937
23002
23071
23145
23249
23308
23362
23426
23485
23547
23614
23697
23749
23804
23874
Cumulative
Total Bed
Volumes
#of BV
15344
15390
15419
15487
15548
15618
15685
15770
15915
15968
16058
16129
16199
16279
16353
16428
16511
16603
16677
16743
16805
16870
16948
17017
17091
17169
17244
17337
17418
17489
17570
17649
17736
17815
17889
17940
17995
18057
18110
18171
18226
18290
18317
18395
18484
18561
18585
18664
18730
18779
18840
18893
18949
19000
19058
19114
19168
19226
19288
19374
19423
19468
19522
19571
19623
19678
19748
19791
19837
19895
Head Loss
(psi)
Vessel A
off
off
6.0
off
off
off
off
5.0
5.0
off
off
off
off
off
off
off
3.5
off
off
off
off
off
4.0
off
off
off
off
off
3.0
3.0
3.5
4.5
4.5
off
off
off
off
off
off
off
off
off
off
4.0
6.0
7.0
off
off
off
off
off
off
off
off
off
off
off
off
5.0
5.0
5.0
off
off
off
off
off
off
off
off
off
Vessel B
off
off
6.0
off
off
off
off
5.0
5.0
off
off
off
off
off
off
off
3.5
off
off
off
off
off
4.0
off
off
off
off
off
3.0
3.0
4.0
5.0
5.0
off
off
off
off
off
off
off
off
off
off
4.0
6.0
7.0
off
off
off
off
off
off
off
off
off
off
off
off
5.0
5.0
5.0
off
off
off
off
off
off
off
off
off
System Pressure
(psig)
Influent
off
off
64
off
off
off
off
64
62
off
off
off
off
off
off
off
64
off
off
off
off
off
off
67
off
off
off
off
off
off
58
off
off
off
off
off
off
off
off
off
off
off
off
64
72
78
off
off
off
off
off
off
off
off
off
off
off
off
66
off
off
off
off
off
off
off
off
off
off
off
Effluent
60
58
52
58
60
58
56
54
52
58
56
54
60
60
58
60
57
60
58
56
54
60
58
58
60
60
58
60
58
60
50
58
58
60
58
58
60
54
58
60
56
60
60
56
60
58
56
58
56
58
60
56
60
60
56
54
60
58
56
58
60
60
56
58
58
56
58
60
60
58
AP
psig
NA
NA
12
NA
NA
NA
NA
10
10
NA
NA
NA
NA
NA
NA
NA
7
NA
NA
NA
NA
NA
NA
9
NA
NA
NA
NA
NA
NA
8
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
8
12
20
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
10
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
A-4
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
41
42
43
44
45
46
47
48
49
50
Date
10/25/04
10/26/04
10/27/04
10/28/04
10/29/04
10/30/04
10/31/04
11/01/04
11/02/04
11/03/04
11/04/04
11/05/04
11/06/04
11/07/04
11/08/04
11/09/04
11/10/04
11/11/04
11/12/04
11/13/04
11/14/04
11/15/04
11/16/04
11/17/04
11/18/04
11/19/04
11/20/04
11/21/04
11/22/04
11/23/04
11/24/04
11/25/04
11/26/04
11/27/04
11/28/04
11/29/04
11/30/04
12/01/04
12/02/04
12/03/04
12/04/04
12/05/04
12/06/04
12/07/04
12/08/04
12/09/04
12/10/04
12/11/04
12/12/04
12/13/04
12/14/04
12/15/04
12/16/04
12/17/04
12/18/04
12/19/04
12/20/04
12/21/04
12/22/04
12/23/04
12/24/04
12/25/04
12/26/04
12/27/04
12/28/04
12/29/04
12/30/04
12/31/04
01/01/05
01/02/05
Pump House Instrument Panel
Operation
Hours
hr
3.9
2.4
9.1
6.4
5.4
6.0
3.3
5.9
2.8
3.6
7.7
5.9
3.0
6.7
6.2
4.1
6.4
5.5
3.2
0.9
8.8
2.9
3.0
3.9
5.6
5.4
3.4
3.2
2.9
2.6
3.0
2.8
2.9
2.5
3.3
2.8
3.0
3.9
7.5
4.9
4.5
3.1
1.2
3.9
2.4
3.6
3.3
3.0
3.4
3.2
3.1
3.2
4.0
4.2
3.0
3.1
3.3
4.0
3.8
3.3
3.3
7.3
2.8
2.9
6.7
6.8
3.3
3.6
6.3
4.1
Cumulative
Operation
Hours
hr
1467.7
1470.1
1479.2
1485.6
1491.0
1497.0
1500.3
1506.2
1509.0
1512.6
1520.3
1526.2
1529.2
1535.9
1542.1
1546.2
1552.6
1558.1
1561.3
1562.2
1571.0
1573.9
1576.9
1580.8
1586.4
1591.8
1595.2
1598.4
1601.3
1603.9
1606.9
1609.7
1612.6
1615.1
1618.4
1621.2
1624.2
1628.1
1635.6
1640.5
1645.0
1648.1
1649.3
1653.2
1655.6
1659.2
1662.5
1665.5
1668.9
1672.1
1675.2
1678.4
1682.4
1686.6
1689.6
1692.7
1696.0
1700.0
1703.8
1707.1
1710.4
1717.7
1720.5
1723.4
1730.1
1736.9
1740.2
1743.8
1750.1
1754.2
Master
Flow Meter
kgal
257,011
257,061
257,199
257,304
257,393
257,490
257,545
257,641
257,687
257,747
257,875
257,969
258,018
258,126
258,227
258,295
258,401
258,490
258,544
258,599
258,702
258,749
258,797
258,859
258,951
259,040
259,096
259,148
259,195
259,239
259,286
259,333
259,377
259,418
259,469
259,517
259,565
259,631
259,756
259,833
259,907
259,957
259,976
260,052
260,082
260,141
260,197
260,246
260,302
260,354
260,403
260,455
260,538
260,589
260,640
260,692
260,796
260,811
260,870
260,927
260,982
261,102
261,163
261,195
261,305
261,417
261,472
261,530
261,634
261,702
Flow
Totalizer
Vessel A
kgal
11,607
11633
11,705
11,761
11,807
11,855
11,877
11,911
11935
11,961
12,019
12,063
12,085
12,133
12,177
12214
12,269
12,315
12,343
12,371
12,423
12,448
12474
12,507
12,555
12,602
12,632
12,659
12,685
12710
12,737
12,765
12,788
12,808
12,832
12,857
12,883
12,917
12,982
13,022
13,063
13,091
13,101
13,142
13,158
13,189
13,218
13,245
13,275
13,305
13,325
13,367
13,412
13,439
13,466
13,493
13,523
13,561
13,595
13,625
13,654
13,719
13,755
13,774
13,832
13,892
13,921
13,953
14,009
14,045
Flow
Totalizer
Vessel B
kgal
12,772
12798
12,878
12,925
12,970
13,024
13,059
13,120
13149
13,186
13,259
13,316
13,344
13,410
13,471
13,506
13,561
13,608
13,636
13,664
13,722
13,748
13772
13,808
13,850
13,897
13,926
13,952
13,976
13996
14,017
14,039
14,062
14,085
14,114
14,138
14,164
14,197
14,262
14,301
14,338
14,362
14,372
14,411
14,426
14,456
14,485
14,510
14,537
14,561
14,583
14,615
14,646
14,672
14,698
14,724
14,751
14,781
14,808
14,837
14,866
14,925
14,953
14,968
15,023
15,080
15,108
15,137
15,189
15,224
Total
Flow
Daily
kgal
68
52
152
103
91
102
57
95
53
63
131
101
50
114
105
72
110
93
56
56
110
51
50
69
90
94
59
53
50
45
48
50
46
43
53
49
52
67
130
79
78
52
20
80
31
61
58
52
57
54
42
74
76
53
53
53
57
68
61
59
58
124
64
34
113
117
57
61
108
71
Cumulative
Flow
Totalizer
kgal
23942
23994
24146
24249
24340
24442
24499
24594
24647
24710
24841
24942
24992
25106
25211
25283
25393
25486
25542
25598
25708
25759
25809
25878
25968
26062
26121
26174
26224
26269
26317
26367
26413
26456
26509
26558
26610
26677
26807
26886
26964
27016
27036
27116
27147
27208
27266
27318
27375
27429
27471
27545
27621
27674
27727
27780
27837
27905
27966
28025
28083
28207
28271
28305
28418
28535
28592
28653
28761
28832
Cumulative
Total Bed
Volumes
#of BV
19952
19995
20122
20208
20283
20368
20416
20495
20539
20592
20701
20785
20827
20922
21009
21069
21161
21238
21285
21332
21423
21466
21508
21565
21640
21718
21768
21812
21853
21891
21931
21973
22011
22047
22091
22132
22175
22231
22339
22405
22470
22513
22530
22597
22623
22673
22722
22765
22813
22858
22893
22954
23018
23062
23106
23150
23198
23254
23305
23354
23403
23506
23559
23588
23682
23779
23827
23878
23968
24027
Head Loss
(psi)
Vessel A
off
off
off
off
off
off
off
off
off
5.0
off
off
5.0
off
2.5
off
off
off
off
off
off
off
off
11.0
off
3.0
off
off
off
off
off
off
off
off
off
off
off
4.0
off
off
off
off
12.0
off
off
off
off
off
off
off
off
10.0
off
off
off
off
off
10.0
off
off
off
off
10.0
12.0
off
5.0
7.0
10.0
3.0
off
Vessel B
off
off
off
off
off
off
off
off
off
4.0
off
off
5.0
off
5.0
off
off
off
off
off
off
off
off
11.0
off
3.0
off
off
off
off
off
off
off
off
off
off
off
4.0
off
off
off
off
12.0
off
off
off
off
off
off
off
off
10.0
off
off
off
off
off
10.0
off
off
off
off
10.0
12.0
off
5.0
7.0
10.0
3.0
off
System Pressure
(psig)
Influent
off
off
off
off
off
off
off
off
off
65
off
off
64
off
63.5
off
off
off
off
off
off
off
off
80
off
70
off
off
off
off
off
off
off
off
off
off
off
66
off
off
off
off
80
off
off
off
off
off
off
off
off
78
off
off
off
off
off
80
off
off
off
off
78
80
off
70
76
82
70
off
Effluent
60
58
54
54
52
56
56
56
58
55
56
58
54
54
56
56
52
56
58
56
56
58
56
58
56
64
60
60
60
56
58
60
60
58
58
56
56
58
54
58
60
60
54
60
54
52
60
58
58
58
56
58
54
56
60
54
52
60
56
56
52
58
58
56
52
60
62
62
64
58
AP
psig
NA
NA
NA
NA
NA
NA
NA
NA
NA
9
NA
NA
9
NA
7.5
NA
NA
NA
NA
NA
NA
NA
NA
22
NA
6
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
26
NA
NA
NA
NA
NA
NA
NA
NA
20
NA
NA
NA
NA
NA
20
NA
NA
NA
NA
20
24
NA
10
14
20
6
NA
A-5
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
51
52
53
54
55
56
57
58
59
60
Date
01/03/05
01/04/05
01/05/05
01/06/05
01/07/05
01/08/05
01/09/05
01/10/05
01/11/05
01/12/05
01/13/05
01/14/05
01/15/05
01/16/05
01/17/05
01/18/05
01/19/05
01/20/05
01/21/05
01/22/05
01/23/05
01/24/05
01/25/05
01/26/05
01/27/05
01/28/05
01/29/05
01/30/05
01/31/05
02/01/05
02/02/05
02/03/05
02/04/05
02/05/05
02/06/05
02/07/05
02/08/05
02/09/05
02/10/05
02/11/05
02/12/05
02/13/05
02/14/05
02/15/05
02/16/05
02/17/05
02/18/05
02/19/05
02/20/05
02/21/05
02/22/05
02/23/05
02/24/05
02/25/05
02/26/05
02/27/05
02/28/05
03/01/05
03/02/05
03/03/05
03/04/05
03/05/05
03/06/05
03/07/05
03/08/05
03/09/05
03/10/05
03/11/05
03/12/05
03/13/05
Pump House Instrument Panel
Operation
Hours
hr
3.2
3.4
0.7
2.3
3.4
4.9
6.8
3.1
3.8
7.8
6.7
3.3
3.4
8.0
3.9
4.0
5.6
2.9
6.9
1.7
4.1
4.0
3.1
3.5
1.1
1.2
3.1
3.0
3.0
3.5
3.6
8.5
3.9
2.6
0.8
0.0
6.3
4.2
2.4
3.1
4.1
4.1
4.4
4.7
0.2
6.6
4.3
3.9
0.0
2.1
5.5
7.2
7.3
6.2
5.2
5.3
2.4
8.4
5.9
7.3
7.5
5.3
7.7
2.8
8.0
9.8
5.5
2.9
5.0
4.8
Cumulative
Operation
Hours
hr
1757.4
1760.8
1761.5
1763.8
1767.2
1772.1
1778.9
1782.0
1785.8
1793.6
1800.3
1803.6
1807.0
1815.0
1818.9
1822.9
1828.5
1831.4
1838.3
1840.0
1844.1
1848.1
1851.2
1854.7
1855.8
1857.0
1860.1
1863.1
1866.1
1869.6
1873.2
1881.7
1885.6
1888.2
1889.0
1889.0
1895.3
1899.5
1901.9
1905.0
1909.1
1913.2
1917.6
1922.3
1922.5
1929.1
1933.4
1937.3
1937.3
1939.4
1944.9
1952.1
1959.4
1965.6
1970.8
1976.1
1978.5
1986.9
1992.8
2000.1
2007.6
2012.9
2020.6
2023.4
2031.4
2041.2
2046.7
2049.6
2054.6
2059.4
Master
Flow Meter
kgal
261,755
261,812
261,823
261,863
261,920
262,001
262,112
262,164
262,227
262,352
262,464
262,518
262,573
262,691
262,738
262,804
262,898
262,944
263,060
263,103
263,155
263,203
263,254
263,311
263,330
263,349
263,399
263,451
263,501
263,559
263,619
263,756
263,820
263,860
263,876
263,876
263,981
264,045
264,089
264,140
264,210
264,277
264,345
264,424
264,427
264,536
264,607
264,671
264,671
264,706
264,797
264,914
265,033
265,135
265,221
265,307
265,346
265,485
265,582
265,700
265,821
265,910
266,039
266,091
266,209
266,369
266,460
266,509
266,591
266,666
Flow
Totalizer
Vessel A
kgal
14,075
14,105
14,112
14,135
14,168
14,212
14,270
14,298
14,331
14,397
14,453
14,483
14,512
14,569
14,591
14,625
14,674
14,699
14,759
14,782
14,809
14,835
14,862
14,893
14,905
14,915
14,941
14,969
14,995
15,026
15,058
15,135
15,171
15,194
15,204
15,204
15,259
15,295
15,324
15,387
15,395
15,480
15,480
15,524
15,525
15,582
15,619
15,655
15,655
15,675
15,727
15,797
15,865
15,919
15,967
16,015
16,039
16,112
16,163
16,227
16,292
16,339
16,409
16,438
16,505
16,591
16,638
16,664
16,706
16,743
Flow
Totalizer
Vessel B
kgal
15,224
15,278
15,283
15,301
15,327
15,368
15,425
15,452
15,484
15,549
15,605
15,634
15,662
15,727
15,755
15,788
15,836
15,861
15,928
15,942
15,969
15,994
16,019
16,046
16,056
16,065
16,090
16,117
16,142
16,171
16,200
16,267
16,297
16,316
16,323
16,323
16,377
16,407
16,425
16,444
16,479
16,538
16,538
16,574
16,576
16,631
16,669
16,703
16,703
16,719
16,762
16,814
16,869
16,919
16,961
17,003
17,021
17,091
17,139
17,198
17,253
17,304
17,368
17,393
17,448
17,528
17,575
17,600
17,642
17,683
Total
Flow
Daily
kgal
30
84
12
41
59
85
115
55
65
131
112
59
57
122
50
67
97
50
127
37
54
51
52
58
22
19
51
55
51
60
61
144
66
42
17
0
109
66
47
82
43
144
0
80
3
112
75
70
0
36
95
122
123
104
90
90
42
143
99
123
120
98
134
54
122
166
94
51
84
78
Cumulative
Flow
Totalizer
kgal
28862
28946
28958
28999
29058
29143
29258
29313
29378
29509
29621
29680
29737
29859
29909
29976
30073
30123
30250
30287
30341
30392
30444
30502
30524
30543
30594
30649
30700
30760
30821
30965
31031
31073
31090
31090
31199
31265
31312
31394
31437
31581
31581
31661
31664
31776
31851
31921
31921
31957
32052
32174
32297
32401
32491
32581
32623
32766
32865
32988
33108
33206
33340
33394
33516
33682
33776
33827
33911
33989
Cumulative
Total Bed
Volumes
#of BV
24052
24122
24132
24166
24215
24286
24382
24428
24482
24591
24684
24733
24781
24883
24924
24980
25061
25103
25208
25239
25284
25327
25370
25418
25437
25453
25495
25541
25583
25633
25684
25804
25859
25894
25908
25908
25999
26054
26093
26162
26198
26318
26318
26384
26387
26480
26543
26601
26601
26631
26710
26812
26914
27001
27076
27151
27186
27305
27388
27490
27590
27672
27783
27828
27930
28068
28147
28189
28259
28324
Head Loss
(psi)
Vessel A
7.0
off
11.0
12.0
10.0
off
off
4.0
off
6.0
off
off
off
8.0
10.0
3.0
off
3.0
off
off
5.0
off
8.0
9.0
off
off
3.0
off
4.0
off
5.0
6.0
off
10.0
off
10.0
5.0
off
5.0
off
off
off
12.0
3.0
3.0
6.0
10.0
off
off
5.0
off
10.0
3.0
off
off
10.0
10.0
3.0
off
off
4.0
off
6.0
7.0
10.0
3.0
off
5.0
off
15.0
Vessel B
7.0
off
11.0
12.0
10.0
off
off
4.0
off
6.0
off
off
8.0
8.0
10.0
3.0
off
3.0
off
off
5.0
5.0
8.0
9.0
off
off
3.0
off
4.0
off
5.0
6.0
off
10.0
off
10.0
5.0
off
5.0
off
off
off
12.0
3.0
3.0
6.0
10.0
off
off
5.0
off
10.0
3.0
off
off
10.0
10.0
3.0
off
off
4.0
off
6.0
7.0
10.0
3.0
off
5.0
off
15.0
System Pressure
(psig)
Influent
74
off
78
76
72
off
off
64
off
70
off
off
off
68
72
62
off
64
off
off
66
off
70
76
off
off
62
off
64
off
66
78
off
82
off
80
70
off
72
off
off
off
90
70
60
68
78
off
off
70
off
74
62
off
off
82
80
68
off
off
68
off
76
74
82
62
off
64
off
90
Effluent
60
62
56
52
52
58
56
56
58
58
62
56
56
52
52
56
58
58
56
58
50
58
56
58
58
56
58
56
56
56
56
66
60
62
58
60
60
56
62
56
56
58
66
64
54
56
58
off
off
60
56
54
56
58
58
62
60
62
58
56
60
58
64
60
62
56
62
54
62
60
iP
psig
14
NA
22
24
20
NA
NA
8
NA
12
NA
NA
NA
16
20
6
NA
6
NA
NA
16
NA
14
18
NA
NA
4
NA
8
NA
10
12
NA
20
NA
20
10
NA
10
NA
NA
NA
24
6
6
12
20
NA
NA
10
NA
20
6
NA
NA
20
20
6
NA
NA
8
NA
12
14
20
6
NA
10
NA
30
A-6
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
61
62
63
64
65
66
67
68
69
70
Date
03/14/05
03/15/05
03/16/05
03/17/05
03/18/05
03/19/05
03/20/05
03/21/05
03/22/05
03/23/05
03/24/05
03/25/05
03/26/05
03/27/05
03/28/05
03/29/05
03/30/05
03/31/05
04/01/05
04/02/05
04/03/05
04/04/05
04/05/05
04/06/05
04/07/05
04/08/05
04/09/05
04/10/05
04/11/05
04/12/05
04/13/05
04/14/05
04/15/05
04/16/05
04/17/05
04/18/05
04/19/05
04/20/05
04/21/05
04/22/05
04/23/05
04/24/05
04/25/05
04/26/05
04/27/05
04/28/05
04/29/05
04/30/05
05/01/05
05/02/05
05/03/05
05/04/05
05/05/05
05/06/05
05/07/05
05/08/05
05/09/05
05/10/05
05/11/05
05/12/05
05/13/05
05/14/05
05/15/05
05/16/05
05/17/05
05/18/05
05/19/05
05/20/05
05/21/05
05/22/05
Pump House Instrument Panel
Operation
Hours
hr
7.1
8.6
5.5
10.5
3.8
6.5
5.3
3.1
4.2
10.4
5.5
6.0
5.2
4.2
6.6
3.1
2.0
9.5
5.9
2.7
0.0
0.0
0.0
7.3
14.2
9.3
10.1
8.8
9.7
10.0
8.4
11.3
12.9
10.0
11.4
10.6
10.4
12.0
10.5
7.2
7.5
9.8
5.0
10.6
7.6
11.5
7.9
6.6
8.2
11.6
6.6
9.2
9.3
8.6
7.6
13.9
8.9
11.0
6.8
10.2
9.3
6.7
9.1
8.2
14.6
10.2
9.4
13.1
11.1
9.0
Cumulative
Operation
Hours
hr
2066.5
2075.1
2080.6
2091.1
2094.9
2101.4
2106.7
2109.8
2114.0
2124.4
2129.9
2135.9
2141.1
2145.3
2151.9
2155.0
2157.0
2166.5
2172.4
2175.1
2175.1
2175.1
2175.1
2182.4
2196.6
2205.9
2216.0
2224.8
2234.5
2244.5
2252.9
2264.2
2277.1
2287.1
2298.5
2309.1
2319.5
2331.5
2342.0
2349.2
2356.7
2366.5
2371.5
2382.1
2389.7
2401.2
2409.1
2415.7
2423.9
2435.5
2442.1
2451.3
2460.6
2469.2
2476.8
2490.7
2499.6
2510.6
2517.4
2527.6
2536.9
2543.6
2552.7
2560.9
2575.5
2585.7
2595.1
2608.2
2619.3
2628.3
Master
Flow Meter
kgal
266,784
266,924
267,015
267,185
267,247
267,355
267,441
267,493
267,561
267,732
267,822
267,921
268,007
268,075
268,184
268,238
268,265
268,420
268,516
268,561
268,561
268,561
268,561
268,607
268,830
268,980
269,143
269,284
269,437
269,594
269,731
269,909
270,114
270,280
270,451
270,619
270,784
270,972
271,137
271,253
271,374
271,528
271,617
271,780
271,893
272,077
272,204
272,311
272,443
272,630
272,735
272,882
273,029
273,161
273,288
273,512
273,666
273,830
273,942
274,106
274,255
274,361
274,507
274,639
274,874
275,039
275,188
275,398
275,572
275,715
Flow
Totalizer
Vessel A
kgal
16,805
16,877
16,924
17,000
17,040
17,099
17,149
17,184
17,232
17,325
17,374
17,427
17,473
17,511
17,571
17,598
17,615
17,703
17,760
17,788
17,788
17,788
17,788
17,813
17,934
18,013
18,101
18,178
18,248
18,320
18,376
18,471
18,586
18,666
18,755
18,831
18,904
19,008
19,111
19,170
19,232
19,313
19,358
19,447
19,510
19,605
19,671
19,722
19,792
19,888
19,946
20,021
20,085
20,142
20,203
20,321
20,402
20,487
20,543
20,631
20,710
20,768
20,830
20,909
21,032
21,120
21,199
21,317
21,419
21,504
Flow
Totalizer
Vessel B
kgal
17,743
17,816
17,865
17,939
17,987
18,040
18,080
18,095
18,121
18,205
18,250
18,299
18,341
18,375
18,428
18,452
18,467
18,540
18,582
18,601
18,601
18,601
18,601
18,628
18,738
18,814
18,895
18,964
19,052
19,142
19,227
19,316
19,413
19,491
19,592
19,689
19,785
19,875
19,943
20,041
20,066
20,144
20,190
20,270
20,323
20,418
20,483
20,541
20,610
20,704
20,755
20,830
20,917
21,001
21,065
21,178
21,254
21,338
21,396
21,478
21,551
21,603
21,690
21,748
21,865
21,948
22,021
22,120
22,199
22,265
Total
Flow
Daily
kgal
122
145
96
150
88
112
90
50
74
177
94
102
88
72
113
51
32
161
99
47
0
0
0
52
231
155
169
146
158
162
141
184
212
158
190
173
169
194
171
157
87
159
91
169
116
190
131
109
139
190
109
150
151
141
125
231
157
169
114
170
152
110
149
137
240
171
152
217
181
151
Cumulative
Flow
Totalizer
kgal
34111
34256
34352
34502
34590
34702
34792
34842
34916
35093
35187
35289
35377
35449
35562
35613
35645
35806
35905
35952
35952
35952
35952
36004
36235
36390
36559
36705
36863
37025
37166
37350
37562
37720
37910
38083
38252
38446
38617
38774
38861
39020
39111
39280
39396
39,586
39,717
39,826
39,965
40,155
40,264
40,414
40,565
40,706
40,831
41,062
41,219
41,388
41,502
41,672
41,824
41,934
42,083
42,220
42,460
42,631
42,783
43,000
43,181
43,332
Cumulative
Total Bed
Volumes
#of BV
28426
28547
28627
28752
28825
28918
28993
29035
29097
29244
29323
29408
29481
29541
29635
29678
29704
29838
29921
29960
29960
29960
29960
30003
30196
30325
30466
30588
30719
30854
30972
31125
31302
31433
31592
31736
31877
32038
32181
32312
32384
32517
32593
32733
32830
32988
33098
33188
33304
33463
33553
33678
33804
33922
34026
34218
34349
34490
34585
34727
34853
34945
35069
35183
35383
35526
35653
35833
35984
36110
Head Loss
(psi)
Vessel A
off
off
5.0
7.0
3.5
off
off
off
10.0
off
4.0
off
5.0
off
6.0
off
6.0
off
9.0
off
off
off
off
3.0
off
off
6.0
off
off
6.0
6.0
off
off
4.0
off
6.0
off
4.0
off
off
off
8.0
3.0
off
4.0
off
off
off
5.0
off
8.0
off
off
5.0
7.0
3.0
3.0
off
6.0
off
off
off
off
off
3.0
off
4.0
5.0
off
6.0
Vessel B
off
off
5.0
7.0
3.5
off
off
off
12.0
off
4.0
off
5.0
off
6.0
off
6.0
off
9.0
off
off
off
off
3.0
off
off
6.0
off
off
6.0
6.0
off
off
4.0
off
6.0
off
4.0
off
off
off
8.0
3.0
off
4.0
off
off
off
5.0
off
8.0
off
off
5.0
7.0
3.0
3.0
off
6.0
off
off
off
off
off
3.0
off
4.0
5.0
off
6.0
System Pressure
(psig)
Influent
off
off
66
66
59
off
off
off
76
off
64
off
72
off
66
off
66
off
72
off
off
off
off
62
off
off
64
off
off
68
66
off
off
62
off
70
off
66
off
off
off
76
64
off
66
off
off
off
70
off
76
off
off
70
70
66
68
off
70
off
off
off
off
off
64
off
62
62
off
68
Effluent
58
54
56
52
52
58
56
56
54
56
56
58
62
58
54
58.0
54
58
54
off
off
off
off
56
58
60
52
56
60
56
54
56
54
54
55
58
56
58
54
60
54
60
58
56
58
56
56
58
60
60
60
58
54
60
56
60
62
58
58
58
56
58
54
54
58
56
54
52
58
56
iP
psig
NA
NA
10
14
7
NA
NA
NA
22
NA
8
NA
10
NA
12
NA
12
NA
18
NA
NA
NA
NA
6
NA
NA
12
NA
NA
12
12
NA
NA
8
NA
12
NA
8
NA
NA
NA
16
6
NA
8
NA
NA
NA
10
NA
16
NA
NA
10
14
6
6
NA
12
NA
NA
NA
NA
NA
6
NA
8
10
NA
12
A-7
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
71
72
73
74
75
76
77
78
79
80
Date
05/23/05
05/24/05
05/25/05
05/26/05
05/27/05
05/28/05
05/29/05
05/30/05
05/31/05
06/01/05
06/02/05
06/03/05
06/04/05
06/05/05
06/06/05
06/07/05
06/08/05
06/09/05
06/10/05
06/11/05
06/12/05
06/13/05
06/14/05
06/15/05
06/16/05
06/17/05
06/18/05
06/19/05
06/20/05
06/21/05
06/22/05
06/23/05
06/24/05
06/25/05
06/26/05
06/27/05
06/28/05
06/29/05
06/30/05
07/01/05
07/02/05
07/03/05
07/04/05
07/05/05
07/06/05
07/07/05
07/08/05
07/09/05
07/10/05
07/11/05
07/12/05
07/13/05
07/14/05
07/15/05
07/16/05
07/17/05
07/18/05
07/19/05
07/20/05
07/21/05
07/22/05
07/23/05
07/24/05
07/25/05
07/26/05
07/27/05
07/28/05
07/29/05
07/30/05
07/31/05
Pump House Instrument Panel
Operation
Hours
hr
15.4
13.4
12.4
12.7
9.1
6.7
5.7
6.0
11.3
9.3
13.7
19.0
10.8
22.9
17.1
8.9
12.1
14.0
10.4
11.3
10.1
10.1
13.7
11.7
13.7
13.3
12.5
9.4
11.3
9.6
7.9
15.0
9.5
10.7
10.2
11.3
12.1
13.2
14.3
20.4
10.2
11.3
12.5
16.0
10.0
10.7
12.0
9.5
10.5
5.7
6.5
7.1
5.1
Cumulative
Operation
Hours
hr
2643.7
2657.1
2669.5
2682.2
2691.3
2698.0
2703.7
2709.7
2721.0
2730.3
2744.0
2763.0
2773.8
2796.7
2813.8
2822.7
2834.8
2848.8
2859.2
2870.5
2880.6
2890.7
2904.4
2916.1
2929.8
2943.1
2955.6
2965.0
2976.3
2985.9
2993.8
3008.8
3018.3
3029.0
3039.2
3050.5
3062.6
3075.8
3090.1
3110.5
3120.7
3132.0
3144.5
3160.5
3170.5
3181.2
3193.2
3202.7
3213.2
3218.9
3225.4
3232.5
3237.6
Master
Flow Meter
kgal
275,956
276,169
276,368
276,569
276,706
276,789
276,881
276,978
277,160
277,309
277,527
277,653
277,826
277,946
278,188
278,324
278,523
278,745
278,907
279,087
279,249
279,409
279,620
279,808
280,026
280,235
280,432
280,581
280,759
280,912
281,038
281,273
281,424
281,593
281,753
281,931
282,122
282,327
282,548
282,859
283,015
283,191
283,383
283,626
283,783
283,947
284,126
284,253
284,407
284,496
284,596
284,710
284,793
Flow
Totalizer
Vessel A
kgal
21,649
21,764
21,869
21,983
22,063
22,102
22,150
22,201
22,297
22,377
22,495
22,565
22,656
22,719
22,847
22,923
23,024
23,143
23,231
23,326
23,412
23,502
23,629
23,727
23,842
23,953
24,058
24,137
24,242
24,327
24,394
24,523
24,604
24,701
24,797
24,893
24,994
25,117
25,237
25,410
25,507
25,602
25,708
25,839
25,922
26,013
26,112
26,183
26,260
26,306
26,364
26,424
26,466
Flow
Totalizer
Vessel B
kgal
22,369
22,472
22,571
22,663
22,733
22,771
22,817
22,865
22,956
23,028
23,133
23,192
23,279
23,339
23,458
23,527
23,624
23,734
23,812
23,902
23,982
24,057
24,147
24,241
24,350
24,454
24,551
24,624
24,701
24,775
24,837
24,949
25,027
25,100
25,168
25,255
25,350
25,439
25,544
25,689
25,754
25,838
25,929
26,047
26,123
26,200
26,285
26,344
26,427
26,478
26,516
26,574
26,616
Total
Flow
Daily
kgal
249
218
204
206
150
77
94
99
187
152
223
129
178
123
247
145
198
229
166
185
166
165
217
192
224
215
202
152
182
159
129
241
159
170
164
183
196
212
225
318
162
179
197
249
159
168
184
130
160
97
96
118
84
Cumulative
Flow
Totalizer
kgal
43,581
43,799
44,003
44,209
44,359
44,436
44,530
44,629
44,816
44,968
45,191
45,320
45,498
45,621
45,868
46,013
46,211
46,440
46,606
46,791
46,957
47,122
47,339
47,531
47,755
47,970
48,172
48,324
48,506
48,665
48,794
49,035
49,194
49,364
49,528
49,711
49,907
50,119
50,344
50,662
50,824
51,003
51,200
51,449
51,608
51,776
51,960
52,090
52,250
52,347
52,443
52,561
52,645
Cumulative
Total Bed
Volumes
#of BV
36318
36499
36669
36841
36966
37030
37108
37191
37347
37473
37659
37767
37915
38018
38223
38344
38509
38700
38838
38993
39131
39268
39449
39609
39796
39975
40143
40270
40422
40554
40662
40863
40995
41137
41273
41426
41589
41766
41953
42218
42353
42503
42667
42874
43007
43147
43300
43408
43542
43623
43703
43801
43871
Head Loss
(psi)
Vessel A
10.0
3.0
4.0
off
off
5.0
6.0
off
3.0
off
off
10.0
3.0
4.0
7.0
10.0
off
off
10.0
off
5.0
6.0
10.0
off
5.0
10.0
off
6.0
10.0
off
5.0
off
3.0
10.0
off
5.0
off
10.0
6.0
off
5.0
off
10.0
off
6.0
10.0
4.0
5.0
off
25.0
15.0
14.0
off
Vessel B
10.0
3.0
4.0
off
off
5.0
6.0
off
3.0
off
off
10.0
3.0
4.0
7.0
10.0
off
off
10.0
off
5.0
6.0
10.0
off
5.0
10.0
off
6.0
10.0
off
5.0
off
3.0
10.0
off
5.0
off
10.0
6.0
off
5.0
off
10.0
off
6.0
10.0
4.0
5.0
off
25.0
15.0
14.0
off
System Pressure
(psig)
Influent
80
62
60
off
off
62
66
off
62
off
off
76
60
62
70
74
off
off
76
off
64
66
76
off
64
76
off
66
76
off
64
off
66
80
off
70
off
74
68
off
68
off
74
off
66
76
64
68
off
110
80
86
off
Effluent
60
56
54
56
54
52
54
54
56
56
58
56
54
54
56
54
58
56
66
54
54
54
56
56
54
56
58
54
56
54
54
60
60
60
60
60
58
54
56
60
58
58
54
58
54
56
58
58
60
60
50
58
off
AP
psig
20
6
6
NA
NA
10
12
NA
6
NA
NA
20
6
8
14
20
NA
NA
10
NA
10
12
20
NA
NA
20
NA
12
20
NA
10
NA
6
20
NA
10
NA
20
12
NA
10
NA
20
NA
12
20
6
10
NA
50
30
28
NA
System was switched off from 07/14/05 through 07/28/05. The bottom laterals, under
bedding, and media were replaced and other system repairs were performed during the down
time.
NA
10.8
7.1
NA
10.8
17.9
285,730
285,903
286,014
26,488
26,576
26,632
26,638
26,724
26,782
NA
174
114
NA
174
288
NA
188
310
3.0
off
6.0
3.0
off
6.0
60
off
64
54
58
52
6
NA
12
A-8
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
81
82
83
84
85
86
87
88
89
90
Date
08/01/05
08/02/05
08/03/05
08/04/05
08/05/05
08/06/05
08/07/05
08/08/05
08/09/05
08/10/05
08/11/05
08/12/05
08/13/05
08/14/05
08/15/05
08/16/05
08/17/05
08/18/05
08/19/05
08/20/05
08/21/05
08/22/05
08/23/05
08/24/05
08/25/05
08/26/05
08/27/05
08/28/05
08/29/05
08/30/05
08/31/05
09/01/05
09/02/05
09/03/05
09/04/05
09/05/05
09/06/05
09/07/05
09/08/05
09/09/05
09/10/05
09/11/05
09/12/05
09/13/05
09/14/05
09/15/05
09/16/05
09/17/05
09/18/05
09/19/05
09/20/05
09/21/05
09/22/05
09/23/05
09/24/05
09/25/05
09/26/05
09/27/05
09/28/05
09/29/05
09/30/05
10/01/05
10/02/05
1 0/03/05
10/04/05
10/05/05
10/06/05
10/07/05
10/08/05
10/09/05
Pump House Instrument Panel
Operation
Hours
hr
8.1
7.7
12.4
11.8
6.2
8.4
9.1
10.9
5.9
9.1
13.9
9.5
8.9
7.7
5.4
5.0
10.2
14.1
6.7
6.9
9.6
8.7
8.1
8.2
9.2
9.6
13.1
9.7
9.5
5.0
8.4
10.2
7.9
7.2
9.0
6.2
7.8
8.0
7.3
9.0
6.9
6.2
5.5
5.5
8.0
7.7
9.6
8.2
8.8
8.6
9.3
9.6
9.6
9.7
9.1
9.9
11.0
10.9
7.8
11.1
7.4
7.5
9.3
9.3
7.7
5.3
10.2
6.3
8.6
7.7
Cumulative
Operation
Hours
hr
26.0
33.7
46.1
57.9
64.1
72.5
81.6
92.5
98.4
107.5
121.4
130.9
139.8
147.5
152.9
157.9
168.1
182.2
188.9
195.8
205.4
214.1
222.2
230.4
239.6
249.2
262.3
272.0
281.5
286.5
294.9
305.1
313.0
320.2
329.2
335.4
343.2
351.2
358.5
367.5
374.4
380.6
386.1
391.6
399.6
407.3
416.9
425.1
433.9
442.5
451.8
461.4
471.0
480.7
489.8
499.7
510.7
521.6
529.4
540.5
547.9
555.4
564.7
574.0
581.7
587.0
597.2
603.5
612.1
619.8
Master
Flow Meter
kgal
286,141
286,261
286,456
286,642
286,742
286,875
287,021
287,194
287,288
287,433
287,653
287,804
287,936
288,058
288,145
288,224
288,387
288,609
288,717
288,826
288,981
289,117
289,245
289,374
289,517
289,668
289,872
290,024
290,174
290,252
290,385
290,549
290,674
290,781
290,922
291,019
291,142
291,266
291,383
291,527
291,638
291,735
291,824
291,911
292,037
292,159
292,314
292,444
292,583
292,723
292,869
293,014
293,168
293,319
293,461
293,618
293,793
293,964
294,087
294,263
294,381
294,500
294,645
294,793
294,916
294,983
295,151
295,252
295,388
295,510
Flow
Totalizer
Vessel A
kgal
26,698
26,760
26,860
26,952
26,997
27,068
27,142
27,229
27,274
27,349
27,459
27,535
27,603
27,662
27,705
27,744
27,825
27,936
27,990
28,043
28,121
28,192
28,259
28,323
28,393
28,468
28,569
28,645
28,718
28,756
28,823
28,905
28,966
29,021
29,091
29,139
29,199
29,261
29,323
29,394
29,447
29,493
29,537
29,580
29,643
29,704
29,781
29,846
29,917
29,990
30,065
30,154
30,244
30,335
30,407
30,498
30,579
30,657
30,714
30,800
30,859
30,918
30,988
31,053
31,114
31,149
31,233
31,282
31,346
31,420
Flow
Totalizer
Vessel B
kgal
26,846
26,906
27,006
27,106
27,161
27,229
27,305
27,395
27,445
27,532
27,648
27,727
27,794
27,868
27,906
27,947
28,033
28,147
28,201
28,260
28,340
28,406
28,470
28,537
28,612
28,690
28,795
28,874
28,953
28,994
29,062
29,146
29,211
29,265
29,336
29,388
29,452
29,515
29,572
29,648
29,707
29,759
29,805
29,850
29,915
29,978
30,058
30,125
30,195
30,264
30,332
30,410
30,475
30,538
30,618
30,679
30,775
30,870
30,938
31,030
31,091
31,152
31,238
31,314
31,378
31,411
31,498
31,551
31,624
31,676
Total
Flow
Daily
kgal
130
122
200
192
100
139
150
177
95
162
226
155
135
133
81
80
167
225
108
112
158
137
131
131
145
153
206
155
152
79
135
166
126
109
141
100
124
125
119
147
112
98
90
88
128
124
157
132
141
142
143
167
155
154
152
152
177
173
125
178
120
120
156
141
125
68
171
102
137
126
Cumulative
Flow
Totalizer
kgal
418
540
740
932
1,032
1,171
1,321
1,498
1,593
1,755
1,981
2,136
2,271
2,404
2,485
2,565
2,732
2,957
3,065
3,177
3,335
3,472
3,603
3,734
3,879
4,032
4,238
4,393
4,545
4,624
4,759
4,925
5,051
5,160
5,301
5,401
5,525
5,650
5,769
5,916
6,028
6,126
6,216
6,304
6,432
6,556
6,713
6,845
6,986
7,128
7,271
7,438
7,593
7,747
7,899
8,051
8,228
8,401
8,526
8,704
8,824
8,944
9,100
9,241
9,366
9,434
9,605
9,707
9,844
9,970
Cumulative
Total Bed
Volumes
#of BV
450
582
797
1004
1112
1262
1423
1614
1717
1891
2135
2302
2447
2591
2678
2764
2944
3186
3303
3423
3594
3741
3883
4024
4180
4345
4567
4734
4898
4983
5128
5307
5443
5560
5712
5820
5954
6088
6217
6375
6496
6601
6698
6793
6931
7065
7234
7376
7528
7681
7835
8015
8182
8348
8512
8676
8866
9053
9188
9379
9509
9638
9806
9958
10093
10166
10350
10460
10608
10744
Head Loss
(psi)
Vessel A
9.0
10.0
3.0
off
9.0
off
3.0
off
off
3.5
3.0
3.0
off
off
9.0
5.0
9.0
2.0
off
off
4.0
5.0
off
7.0
off
8.0
off
off
9.0
9.0
2.0
off
3.0
off
off
6.0
off
8.0
2.0
off
off
6.0
7.0
8.0
8.0
9.0
off
off
6.0
off
8.0
4.0
3.0
off
off
off
6.0
off
9.0
2.0
off
off
9.0
4.0
6.0
3.0
off
5.0
off
3.0
Vessel B
9.0
10.0
3.0
off
9.0
off
3.0
off
off
3.5
3.0
3.0
off
off
9.0
5.0
9.8
2.0
off
off
4.0
5.0
off
7.0
off
8.0
off
off
9.0
9.0
2.0
off
3.0
off
off
6.0
off
8.0
2.0
off
off
6.0
7.0
8.0
8.0
9.0
off
off
6.0
off
8.0
4.0
3.0
off
off
off
6.0
off
9.0
2.0
off
off
9.0
4.0
5.0
3.0
off
5.0
off
3.0
System Pressure
(psig)
Influent
70
76
62
off
78
off
66
off
off
61
64
60
off
off
74
64
74
62
off
off
62
68
off
70
off
74
off
off
74
62
60
off
60
off
off
76
off
70
60
off
off
68
68
70
72
72
off
off
72
off
70
70
62
off
off
off
68
off
72
58
off
off
76
66
65
62
off
66
off
62
Effluent
52
56
56
58
60
58
60
60
56
54
58
54
58
60
56
54
56
58
58
60
54
58
60
56
54
58
56
58
56
54
50
off
54
54
58
64
58
54
56
58
58
56
54
54
56
54
58
60
60
58
54
61
56
58
56
60
56
58
54
54
58
56
58
58
54
56
58
56
58
56
iP
psig
18
20
6
NA
18
NA
6
NA
NA
7
6
6
NA
NA
18
10
18
4
NA
NA
8
10
NA
14
NA
16
NA
NA
18
8
10
NA
6
NA
NA
12
NA
16
4
NA
NA
12
14
16
16
18
NA
NA
12
NA
16
9
6
NA
NA
NA
12
NA
18
4
NA
NA
18
8
11
6
NA
10
NA
6
A-9
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
91
92
93
94
95
96
97
98
99
100
Date
10/10/05
10/11/05
10/12/05
10/13/05
10/14/05
10/15/05
10/16/05
1 0/1 7/05
10/18/05
10/19/05
10/20/05
10/21/05
10/22/05
10/23/05
10/24/05
10/25/05
10/26/05
10/27/05
10/28/05
10/29/05
10/30/05
10/31/05
11/01/05
11/02/05
11/03/05
11/04/05
11/05/05
11/06/05
11/07/05
11/08/05
11/09/05
11/10/05
11/11/05
11/12/05
11/13/05
11/14/05
11/15/05
11/16/05
11/17/05
11/18/05
11/19/05
11/20/05
11/21/05
11/22/05
11/23/05
11/24/05
11/25/05
11/26/05
11/27/05
11/28/05
11/29/05
11/30/05
12/01/05
12/02/05
12/03/05
12/04/05
12/05/05
12/06/05
12/07/05
12/08/05
12/09/05
12/10/05
12/11/05
12/12/05
12/13/05
12/14/05
12/15/05
12/16/05
12/17/05
12/18/05
Pump House Instrument Panel
Operation
Hours
hr
8.2
5.3
6.9
8.1
6.0
5.3
5.7
5.5
6.2
6.9
4.4
6.2
8.7
6.3
4.4
9.6
6.7
6.9
11.0
6.3
8.0
8.1
5.4
4.9
6.1
5.7
7.1
5.9
5.7
6.5
5.6
7.1
9.0
6.0
6.0
6.2
6.3
5.5
7.2
7.6
7.7
5.4
6.0
3.9
8.4
5.3
5.3
5.6
5.4
5.2
5.4
3.2
6.3
5.4
17.5
11.1
7.8
5.1
6.7
7.0
6.9
8.6
5.7
5.8
5.3
3.5
6.9
7.4
5.3
5.7
Cumulative
Operation
Hours
hr
628.0
633.3
640.2
648.3
654.3
659.6
665.3
670.8
677.0
683.9
688.3
694.5
703.2
709.5
713.9
723.5
730.2
737.1
748.1
754.4
762.4
770.5
775.9
780.8
786.9
792.6
799.7
805.6
811.3
817.8
823.4
830.5
839.5
845.5
851.5
857.7
864.0
869.5
876.7
884.3
892.0
897.4
903.4
907.3
915.7
921.0
926.3
931.9
937.3
942.5
947.9
951.1
957.4
962.8
980.3
991.4
999.2
1004.3
1011.0
1018.0
1024.9
1033.5
1039.2
1045.0
1050.3
1053.8
1060.7
1068.1
1073.4
1079.1
Master
Flow Meter
kgal
295,572
295,657
295,767
295,898
295,994
296,079
296,178
296,257
296,357
296,468
296,538
296,638
296,778
296,878
296,947
297,101
297,209
297,318
297,483
297,599
297,728
297,859
297,937
298,024
298,122
298,214
298,327
298,423
298,518
298,616
298,707
298,833
298,968
299,062
299,159
299,258
299,358
299,445
299,561
299,684
299,807
299,894
299,981
300,053
300,188
300,275
300,371
300,450
300,543
300,619
300,704
300,757
300,860
300,945
301,008
301,084
301,177
301,259
301,367
301,477
301,585
301,724
301,816
301,909
302,003
302,051
302,162
302,281
302,365
302,456
Flow
Totalizer
Vessel A
kgal
31,449
31,490
31,541
31,605
31,654
31,697
31,742
31,784
31,835
31,891
31,937
31,978
32,064
32,109
32,145
32,224
32,278
32,333
32,416
32,475
32,540
32,606
32,645
32,695
32,747
32,794
32,853
32,901
32,946
32,996
33,035
33,113
33,164
33,212
33,259
33,306
33,351
33,388
33,443
33,503
33,562
33,603
33,643
33,672
33,740
33,783
33,826
33,870
33,911
33,949
33,986
34,008
34,060
34,103
34,134
34,169
34,211
34,250
34,296
34,338
34,378
34,447
34,493
34,539
34,585
34,616
34,675
34,737
34,780
34,823
Flow
Totalizer
Vessel B
kgal
31,708
31,754
31,814
31,882
31,931
31,973
32,020
32,065
32,117
32,173
32,215
32,259
32,325
32,372
32,405
32,482
32,537
32,592
32,678
32,738
32,803
32,870
32,910
32,964
33,012
33,057
33,113
33,161
33,210
33,262
33,315
33,396
33,448
33,490
33,549
33,603
33,659
33,709
33,772
33,836
33,906
33,949
33,996
34,039
34,110
34,154
34,197
34,244
34,290
34,335
34,384
34,421
34,473
34,516
34,548
34,590
34,642
34,685
34,748
34,817
34,886
34,957
35,003
35,051
35,099
35,132
35,184
35,241
35,283
35,331
Total
Flow
Daily
kgal
61
87
111
132
98
85
92
87
103
112
88
85
152
92
69
156
109
110
169
119
130
133
79
104
100
92
115
96
94
102
92
159
103
90
106
101
101
87
118
124
129
84
87
72
139
87
86
91
87
83
86
59
104
86
63
77
94
82
109
111
109
140
92
94
94
64
111
119
85
91
Cumulative
Flow
Totalizer
kgal
10,031
10,118
10,229
10,361
10,459
10,544
10,636
10,723
10,826
10,938
11,026
11,111
11,263
11,355
11,424
11,580
11,689
11,799
11,968
12,087
12,217
12,350
12,429
12,533
12,633
12,725
12,840
12,936
13,030
13,132
13,224
13,383
13,486
13,576
13,682
13,783
13,884
13,971
14,089
14,213
14,342
14,426
14,513
14,585
14,724
14,811
14,897
14,988
15,075
15,158
15,244
15,303
15,407
15,493
15,556
15,633
15,727
15,809
15,918
16,029
16,138
16,278
16,370
16,464
16,558
16,622
16,733
16,852
16,937
17,028
Cumulative
Total Bed
Volumes
#of BV
10809
10903
11023
11165
11270
11362
11461
11555
11666
11787
11881
11973
12137
12236
12310
12478
12596
12714
12897
13025
13165
13308
13393
13505
13613
13712
13836
13940
14041
14151
14250
14421
14532
14629
14744
14852
14961
15055
15182
15316
15455
15545
15639
15717
15866
15960
16053
16151
16245
16334
16427
16490
16602
16695
16763
16846
16947
17036
17153
17273
17390
17541
17640
17741
17843
17912
18031
18159
18251
18349
Head Loss
(psi)
Vessel A
4.0
off
9.0
2.0
off
off
off
9.0
2.0
off
4.0
6.0
off
9.0
10.0
off
4.0
off
off
off
off
4.0
5.0
off
off
6.0
off
off
6.0
off
10.0
off
off
4.0
off
off
7.0
8.0
off
4.0
off
off
5.0
9.0
off
off
off
5.0
off
5.0
6.0
3.0
off
off
off
off
off
6.0
7.0
10.0
11.0
off
off
off
4.0
4.0
off
off
6.0
off
Vessel B
4.0
off
9.0
2.0
off
off
off
9.0
2.0
off
4.0
6.0
off
9.0
10.0
off
4.0
off
off
off
off
4.0
5.0
off
off
6.0
off
off
6.0
off
10.0
off
off
4.0
off
off
7.0
8.0
off
4.0
off
off
5.0
9.0
off
off
off
5.0
off
5.0
6.0
3.0
off
off
off
off
off
6.0
7.0
10.0
11.0
off
off
off
4.0
4.0
off
off
6.0
off
System Pressure
(psig)
Influent
62
off
76
58
off
off
off
74
58
off
66
70
off
80
78
off
64
off
off
off
off
70
68
off
off
70
off
off
68
off
76
off
off
64
off
off
72
70
off
64
off
off
68
76
off
off
off
66
off
66
70
64
off
off
off
off
off
68
70
78
78
off
off
off
66
64
off
off
70
off
Effluent
54
58
58
54
58
56
54
56
54
60
58
58
56
62
58
58
56
60
60
58
58
62
58
56
56
58
60
60
56
58
56
58
58
56
58
60
58
54
58
56
60
off
58
58
60
62
60
56
60
56
58
58
60
58
58
60
58
56
56
58
56
60
60
58
58
56
56
58
58
56
AP
psig
8
NA
18
4
NA
NA
NA
18
4
NA
8
12
NA
18
20
NA
8
NA
NA
NA
NA
8
10
NA
NA
12
NA
NA
12
NA
20
Na
NA
8
NA
NA
14
16
NA
8
NA
NA
10
18
NA
NA
NA
10
NA
10
12
6
NA
NA
NA
NA
NA
12
14
20
22
NA
NA
NA
8
8
NA
NA
12
NA
A-10
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
101
102
103
104
105
106
107
108
109
110
Date
12/19/05
12/20/05
12/21/05
12/22/05
12/23/05
12/24/05
12/25/05
12/26/05
12/27/05
12/28/05
12/29/05
12/30/05
12/31/05
01/01/06
01/02/06
01/03/06
01/04/06
01/05/06
01/06/06
01/07/06
01/08/06
01/09/06
01/10/06
01/11/06
01/12/06
01/13/06
01/14/06
01/15/06
01/16/06
01/17/06
01/18/06
01/19/06
01/20/06
01/21/06
01/22/06
01/23/06
01/24/06
01/25/06
01/26/06
01/27/06
01/28/06
01/29/06
01/30/06
01/31/06
02/01/06
02/02/06
02/03/06
02/04/06
02/05/06
02/06/06
02/07/06
02/08/06
02/09/06
02/10/06
02/11/06
02/12/06
02/13/06
02/14/06
02/15/06
02/16/06
02/17/06
02/18/06
02/19/06
02/20/06
02/21/06
02/22/06
02/23/06
02/24/06
02/25/06
02/26/06
Pump House Instrument Panel
Operation
Hours
hr
8.2
4.9
7.2
5.7
5.2
5.8
5.5
5.0
5.7
5.2
5.7
5.9
7.7
5.6
5.0
5.8
4.1
8.0
5.3
5.4
5.6
6.2
5.8
5.9
5.9
5.7
5.3
5.8
5.2
4.2
9.5
4.3
3.7
4.6
5.2
5.9
5.5
5.4
5.6
5.7
5.1
5.3
6.4
5.2
3.2
10.0
5.8
5.4
5.5
5.6
5.4
5.3
6.6
4.9
4.5
5.0
8.1
5.4
2.5
7.9
5.4
4.9
5.1
5.0
5.8
5.9
5.9
5.8
5.0
5.4
Cumulative
Operation
Hours
hr
1087.3
1092.2
1099.4
1105.1
1110.3
1116.1
1121.6
1126.6
1132.3
1137.5
1143.2
1149.1
1156.8
1162.4
1167.4
1173.2
1177.3
1185.3
1190.6
1196.0
1201.6
1207.8
1213.6
1219.5
1225.4
1231.1
1236.4
1242.2
1247.4
1251.6
1261.1
1265.4
1269.1
1273.7
1278.9
1284.8
1290.3
1295.7
1301.3
1307.0
1312.1
1317.4
1323.8
1329.0
1332.2
1342.2
1348.0
1353.4
1358.9
1364.5
1369.9
1375.2
1381.8
1386.7
1391.2
1396.2
1404.3
1409.7
1412.2
1420.1
1425.5
1430.4
1435.5
1440.5
1446.3
1452.2
1458.1
1463.9
1468.9
1474.3
Master
Flow Meter
kgal
302,587
302,665
302,780
302,871
302,958
303,043
303,131
303,211
303,302
303,386
303,475
303,570
303,694
303,783
303,862
303,954
304,018
304,148
304,233
304,319
304,408
304,507
304,598
304,693
304,787
304,878
304,963
305,055
305,141
305,206
305,354
305,424
305,483
305,557
305,641
305,734
305,821
305,907
305,996
306,088
306,169
306,254
306,345
306,438
306,488
306,660
306,744
306,829
306,917
307,006
307,072
307,188
307,279
307,356
307,428
307,509
307,638
307,723
307,764
307,889
307,975
308,054
308,135
308,214
308,307
308,398
308,493
308,585
308,665
308,749
Flow
Totalizer
Vessel A
kgal
34,885
34,923
34,978
35,019
35,056
35,092
35,131
35,169
35,211
35,249
35,286
35,335
35,397
35,441
35,480
35,525
35,558
35,623
35,664
35,704
35,748
35,793
35,832
35,865
35,915
35,962
36,005
36,053
36,099
36,133
36,217
36,249
36,277
36,313
36,353
36,397
36,435
36,478
36,526
36,576
36,618
36,662
36,708
36,756
36,780
36,866
36,908
36,950
36,993
37,036
37,077
37,122
37,164
37,199
37,234
37,273
37,335
37,375
37,393
37,455
37,499
37,538
37,579
37,619
37,668
37,721
37,765
37,810
37,850
37,890
Flow
Totalizer
Vessel B
kgal
35,401
35,441
35,502
35,553
35,603
35,652
35,702
35,745
35,795
35,840
35,894
35,942
36,004
36,050
36,090
36,137
36,169
36,236
36,280
36,325
36,372
36,426
36,480
36,542
36,586
36,632
36,674
36,719
36,760
36,790
36,856
36,895
36,926
36,964
37,000
37,050
37,107
37,166
37,207
37,250
37,289
37,376
37,376
37,421
37,447
37,534
37,576
37,620
37,664
37,711
37,756
37,806
37,855
37,898
37,936
37,997
38,043
38,089
38,113
38,176
38,218
38,258
38,298
38,337
38,381
38,419
38,470
38,516
38,557
38,600
Total
Flow
Daily
kgal
132
78
116
92
87
85
89
81
92
83
91
97
124
90
79
92
65
132
85
85
91
99
93
95
94
93
85
93
87
64
150
71
59
74
76
94
95
102
89
93
81
131
46
93
50
173
84
86
87
90
86
95
91
78
73
100
108
86
42
125
86
79
81
79
93
91
95
91
81
83
Cumulative
Flow
Totalizer
kgal
17,160
17,238
17,354
17,446
17,533
17,618
17,707
17,788
17,880
17,963
18,054
18,151
18,275
18,365
18,444
18,536
18,601
18,733
18,818
18,903
18,994
19,093
19,186
19,281
19,375
19,468
19,553
19,646
19,733
19,797
19,947
20,018
20,077
20,151
20,227
20,321
20,416
20,518
20,607
20,700
20,781
20,912
20,958
21,051
21,101
21,274
21,358
21,444
21,531
21,621
21,707
21,802
21,893
21,971
22,044
22,144
22,252
22,338
22,380
22,505
22,591
22,670
22,751
22,830
22,923
23,014
23,109
23,200
23,281
23,364
Cumulative
Total Bed
Volumes
#of BV
18491
18575
18700
18800
18893
18985
19081
19168
19267
19357
19455
19559
19693
19790
19875
19974
20044
20186
20278
20370
20468
20574
20675
20777
20878
20978
21070
21170
21264
21333
21495
21571
21635
21714
21796
21898
22000
22110
22206
22306
22393
22534
22584
22684
22738
22925
23015
23108
23202
23298
23391
23494
23592
23676
23754
23862
23978
24071
24116
24251
24344
24429
24516
24601
24702
24800
24902
25000
25087
25177
Head Loss
(psi)
Vessel A
off
4.0
off
off
6.0
7.0
off
off
5.0
off
7.0
off
off
off
off
5.0
7.0
off
4.0
off
off
off
off
off
off
4.0
off
off
5.0
off
off
3.0
off
off
off
off
6.0
off
off
off
4.0
off
5.0
off
8.0
off
off
off
off
8.0
off
9.0
off
4.0
off
off
off
6.0
7.0
off
off
off
off
off
6.0
off
off
off
6.0
off
Vessel B
off
4.0
off
off
6.0
7.0
off
off
5.0
off
7.0
off
off
off
off
5.0
7.0
off
4.0
off
off
off
off
off
off
4.0
off
off
7.0
off
off
3.0
off
off
off
off
5.0
off
off
off
4.0
off
5.0
off
8.0
off
off
off
off
8.0
off
9.0
off
4.0
off
off
off
6.0
6.0
off
off
off
off
off
6.0
off
off
off
6.0
off
System Pressure
(psig)
Influent
off
64
off
off
60
72
off
off
66
off
72
off
off
off
off
64
70
off
66
off
off
off
off
off
off
66
off
off
68
off
off
62
off
off
off
off
67
off
off
off
66
off
66
off
70
off
off
off
off
72
off
74
off
66
off
off
off
70
67
off
off
off
off
off
70
off
off
off
74
off
Effluent
60
56
56
58
58
58
60
58
56
56
58
56
60
58
60
54
56
56
58
56
56
56
56
58
58
58
56
58
56
56
58
56
56
58
56
56
56
58
56
58
58
56
56
58
54
58
58
56
56
56
60
56
56
58
58
56
58
58
54
58
58
56
56
56
58
56
56
58
62
58
AP
psig
NA
8
NA
NA
2
14
NA
NA
10
NA
14
NA
NA
NA
NA
10
14
NA
8
NA
NA
NA
NA
NA
NA
8
NA
NA
12
NA
NA
6
NA
NA
NA
NA
11
NA
NA
NA
8
NA
10
NA
16
NA
NA
NA
NA
16
NA
18
NA
8
NA
NA
NA
12
13
NA
NA
NA
NA
NA
12
NA
NA
NA
12
NA
A-ll
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
111
112
113
114
115
116
117
118
119
120
Date
02/27/06
02/28/06
03/01/06
03/02/06
03/03/06
03/04/06
03/05/06
03/06/06
03/07/06
03/08/06
03/09/06
03/10/06
03/11/06
03/12/06
03/13/06
03/1 4/06
03/1 5/06
03/16/06
03/17/06
03/18/06
03/19/06
03/20/06
03/21/06
03/22/06
03/23/06
03/24/06
03/25/06
03/26/06
03/27/06
03/28/06
03/29/06
03/30/06
03/31/06
04/01/06
04/02/06
04/03/06
04/04/06
04/05/06
04/06/06
04/07/06
04/08/06
04/09/06
04/1 0/06
04/11/06
04/1 2/06
04/1 3/06
04/14/06
04/15/06
04/16/06
04/17/06
04/18/06
04/19/06
04/20/06
04/21/06
04/22/06
04/23/06
04/24/06
04/25/06
04/26/06
04/27/06
04/28/06
04/29/06
04/30/06
05/01/06
05/02/06
05/03/06
05/04/06
05/05/06
05/06/06
05/07/06
Pump House Instrument Panel
Operation
Hours
hr
5.4
6.6
3.1
18.1
8.4
5.7
6.2
6.5
6.0
6.1
5.0
5.8
5.1
4.4
7.8
8.6
5.1
7.8
6.9
6.4
6.6
5.5
7.2
6.8
7.4
8.5
6.1
6.4
5.8
7.3
3.0
8.9
9.2
7.9
8.6
9.1
8.0
8.2
7.1
7.0
11.1
9.9
9.7
8.1
8.2
8.8
10.0
10.0
8.0
7.4
7.5
7.3
8.8
8.0
6.9
8.1
8.6
8.2
5.4
8.5
6.8
6.2
7.7
8.2
8.7
8.6
8.8
9.6
7.2
8.5
Cumulative
Operation
Hours
hr
1479.7
1486.3
1489.4
1507.5
1515.9
1521.6
1527.8
1534.3
1540.3
1546.4
1551.4
1557.2
1562.3
1566.7
1574.5
1583.1
1588.2
1596.0
1602.9
1609.3
1615.9
1621.4
1628.6
1635.4
1642.8
1651.3
1657.4
1663.8
1669.6
1676.9
1679.9
1688.8
1698.0
1705.9
1714.5
1723.6
1731.6
1739.8
1746.9
1753.9
1765.0
1774.9
1784.6
1792.7
1800.9
1809.7
1819.7
1829.7
1837.7
1845.1
1852.6
1859.9
1868.7
1876.7
1883.6
1891.7
1900.3
1908.5
1913.9
1922.4
1929.2
1935.4
1943.1
1951.3
1960.0
1968.6
1977.4
1987.0
1994.2
2002.7
Master
Flow Meter
kgal
308,833
308,939
308,988
309,082
309,210
309,301
309,400
309,503
309,605
309,694
309,774
309,866
309,947
310,020
310,141
310,276
310,355
310,481
310,589
310,690
310,785
310,880
310,992
311,100
311,216
311,350
311,446
311,545
311,636
311,753
311,800
311,943
312,088
312,213
312,348
312,491
312,614
312,744
312,854
312,963
313,139
313,294
313,446
313,571
313,701
313,843
314,000
314,155
314,279
314,394
314,509
314,625
314,763
314,890
314,998
315,125
315,258
315,388
315,474
315,607
315,714
315,812
315,933
316,061
316,198
316,331
316,467
316,617
316,729
316,861
Flow
Totalizer
Vessel A
kgal
37,925
37,973
37,996
38,039
38,090
38,136
38,186
38,236
38,289
38,339
38,380
38,426
38,468
38,505
38,565
38,634
38,670
38,735
38,789
38,840
38,888
38,935
38,989
39,033
39,089
39,154
39,199
39,242
39,279
39,330
39,352
39,424
39,495
39,555
39,625
39,695
39,759
39,822
39,870
39,919
40,001
40,072
40,141
40,192
40,257
40,325
40,401
40,476
40,536
40,591
40,645
40,706
40,780
40,848
40,903
40,967
41,032
41,092
41,132
41,192
41,240
41,288
41,348
41,411
41,487
41,545
41,614
41,685
41,738
41,801
Flow
Totalizer
Vessel B
kgal
38,648
38,707
38,733
38,784
38,797
38,843
38,893
38,945
38,994
39,045
39,084
39,128
39,168
39,204
39,263
39,328
39,361
39,434
39,487
39,537
39,583
39,630
39,688
39,753
39,812
39,881
39,931
39,986
40,040
40,104
40,129
40,201
40,274
40,338
40,402
40,471
40,532
40,598
40,657
40,717
40,809
40,892
40,973
41,004
41,069
41,184
41,262
41,340
41,405
41,462
41,521
41,593
41,635
41,714
41,765
41,827
41,894
41,962
42,006
42,176
42,135
42,185
42,245
42,308
42,375
42,432
42,505
42,583
42,640
42,708
Total
Flow
Daily
kgal
83
107
49
94
64
92
100
102
102
101
80
90
82
73
119
134
69
138
107
101
94
94
112
109
115
134
95
98
91
115
47
144
144
124
134
139
125
129
107
109
174
154
150
82
130
183
154
153
125
112
113
133
116
147
106
126
132
128
84
NA
NA
98
120
126
143
115
142
149
110
131
Cumulative
Flow
Totalizer
kgal
23,447
23,554
23,603
23,697
23,761
23,853
23,953
24,055
24,157
24,258
24,338
24,428
24,510
24,583
24,702
24,836
24,905
25,043
25,150
25,251
25,345
25,439
25,551
25,660
25,775
25,909
26,004
26,102
26,193
26,308
26,355
26,499
26,643
26,767
26,901
27,040
27,165
27,294
27,401
27,510
27,684
27,838
27,988
28,070
28,200
28,383
28,537
28,690
28,815
28,927
29,040
29,173
29,289
29,436
29,542
29,668
29,800
29,928
30,012
30,242
30,249
30,347
30,467
30,593
30,736
30,851
30,993
31,142
31,252
31,383
Cumulative
Total Bed
Volumes
#of BV
25266
25381
25434
25536
25605
25704
25811
25921
26031
26140
26226
26323
26412
26490
26619
26763
26837
26986
27101
27210
27311
27413
27533
27651
27775
27919
28022
28127
28225
28349
28400
28555
28710
28844
28988
29138
29273
29412
29527
29644
29832
29998
30159
30248
30388
30585
30751
30916
31051
31171
31293
31436
31561
31720
31834
31970
32112
32250
32341
32588
32596
32702
32831
32967
33121
33245
33398
33558
33677
33818
Head Loss
(psi)
Vessel A
off
off
4.0
off
off
off
off
7.0
off
off
4.0
off
off
5.0
off
off
8.0
off
off
off
5.0
off
off
off
4.0
off
off
5.0
6.0
off
4.0
off
off
5.0
off
off
off
7.0
off
3.0
off
off
7.0
9.0
3.0
off
off
off
5.0
off
4.0
5.0
off
5.0
off
8.0
9.0
4.0
5.0
off
8.0
off
off
5.0
off
8.0
9.0
9.0
off
off
Vessel B
off
off
4.0
off
off
off
off
7.0
off
off
4.0
off
off
5.0
off
off
8.0
off
off
off
5.0
off
off
off
4.0
off
off
5.0
6.0
off
4.0
off
off
5.0
off
off
off
7.0
off
3.0
off
off
7.0
9.0
3.0
off
off
off
5.0
off
4.0
5.0
off
5.0
off
8.0
9.0
4.0
5.0
off
8.0
off
off
5.0
off
8.0
9.0
9.0
off
off
System Pressure
(psig)
Influent
off
off
64
off
off
off
off
74
off
off
62
off
off
66
off
off
70
off
off
off
66
off
off
off
62
off
off
66
66
off
62
off
off
66
off
off
off
70
off
66
off
off
72
74
62
off
off
off
66
off
62
66
off
68
off
76
74
64
66
off
72
off
off
64
off
72
76
64
off
off
Effluent
58
56
56
58
60
56
56
60
60
58
54
56
56
56
58
58
54
58
54
56
56
58
56
56
54
56
58
56
54
58
54
56
60
56
56
58
58
56
56
58
58
58
58
56
56
58
58
56
56
58
54
56
58
58
58
60
56
56
56
56
56
56
58
54
56
56
58
56
58
56
AP
psig
NA
NA
8
NA
NA
NA
NA
14
NA
NA
8
NA
NA
10
NA
NA
16
NA
NA
NA
10
NA
NA
NA
8
NA
NA
10
12
NA
8
NA
NA
10
NA
NA
NA
14
NA
8
NA
NA
14
18
6
NA
NA
NA
10
NA
8
10
NA
10
NA
16
18
8
10
NA
16
NA
NA
10
NA
16
18
8
NA
NA
A-12
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
121
122
123
124
125
126
127
128
129
130
Date
05/08/06
05/09/06
05/10/06
05/11/06
05/12/06
05/13/06
05/14/06
05/15/06
05/16/06
05/17/06
05/18/06
05/19/06
05/20/06
05/21/06
05/22/06
05/23/06
05/24/06
05/25/06
05/26/06
05/27/06
05/28/06
05/29/06
05/30/06
05/31/06
06/01/06
06/02/06
06/03/06
06/04/06
06/05/06
06/06/06
06/07/06
06/08/06
06/09/06
06/10/06
06/11/06
06/12/06
06/13/06
06/14/06
06/15/06
06/16/06
06/17/06
06/18/06
06/19/06
06/20/06
06/21/06
06/22/06
06/23/06
06/24/06
06/25/06
06/26/06
06/27/06
06/28/06
06/29/06
06/30/06
07/01/06
07/02/06
07/03/06
07/04/06
07/05/06
07/06/06
07/07/06
07/08/06
07/09/06
07/10/06
07/11/06
07/12/06
07/13/06
07/14/06
07/15/06
07/16/06
Pump House Instrument Panel
Operation
Hours
hr
8.7
9.1
8.5
8.8
6.9
9.6
9.8
8.7
9.6
12.4
13.2
9.4
6.7
14.2
11.0
11.3
8.2
12.4
11.0
12.3
8.9
7.0
13.5
11.7
10.8
11.8
7.3
13.2
10.8
13.0
13.0
11.8
9.4
12.6
15.3
5.3
13.2
12.6
11.9
13.0
9.0
10.2
14.4
10.5
10.2
11.6
11.0
13.0
11.6
7.3
7.7
13.1
9.5
11.6
8.1
7.9
11.1
12.6
8.8
12.4
6.5
5.8
5.6
6.2
11.7
9.8
11.1
9.9
12.0
10.3
Cumulative
Operation
Hours
hr
2011.4
2020.5
2029.0
2037.8
2044.7
2054.3
2064.1
2072.8
2082.4
2094.8
2108.0
2117.4
2124.1
2138.3
2149.3
2160.6
2168.8
2181.2
2192.2
2204.5
2213.4
2220.4
2233.9
2245.6
2256.4
2268.2
2275.5
2288.7
2299.5
2312.5
2325.5
2337.3
2346.7
2359.3
2374.6
2379.9
2393.1
2405.7
2417.6
2430.6
2439.6
2449.8
2464.2
2474.7
2484.9
2496.5
2507.5
2520.5
2532.1
2539.4
2547.1
2560.2
2569.7
2581.3
2589.4
2597.3
2608.4
2621.0
2629.8
2642.2
2648.7
2654.5
2660.1
2666.3
2678.0
2687.8
2698.9
2708.8
2720.8
2731.1
Master
Flow Meter
kgal
316,996
317,136
317,267
317,404
317,514
317,663
317,814
317,948
318,096
318,286
318,492
318,636
318,741
318,959
319,129
319,303
319,430
319,624
319,792
319,984
320,121
320,231
320,438
320,617
320,785
320,965
321,079
321,284
321,448
321,644
321,849
322,027
322,172
322,365
322,508
322,629
322,882
323,072
323,258
323,455
323,597
323,747
323,970
324,131
324,289
324,462
324,637
324,838
325,016
325,128
325,246
325,448
325,596
325,775
325,900
326,027
326,196
326,388
326,524
326,689
326,815
326,904
326,992
327,089
327,270
327,421
327,595
327,746
327,932
328,092
Flow
Totalizer
Vessel A
kgal
41,864
41,928
41,984
42,052
42,105
42,176
42,248
42,310
42,378
42,463
42,568
42,648
42,693
42,805
42,894
42,978
43,038
43,130
43,206
43,301
43,368
43,422
43,525
43,619
43,710
43,800
43,856
43,954
44,028
44,111
44,211
44,298
44,367
44,457
44,522
44,581
44,702
44,796
44,891
44,993
45,066
45,137
45,241
45,318
45,343
45,473
45,562
45,661
45,751
45,808
45,871
45,972
46,041
46,125
46,179
46,230
46,314
46,410
46,476
46,558
46,628
46,679
46,718
46,763
46,846
46,913
47,007
47,081
47,169
47,242
Flow
Totalizer
Vessel B
kgal
42,777
42,852
42,925
42,995
43,050
43,128
43,203
43,272
43,350
43,451
43,550
43,620
43,680
43,773
43,773
43,940
44,004
44,103
44,193
44,288
44,355
44,092
44,509
44,592
44,682
44,700
44,826
44,928
45,015
45,125
45,227
45,315
45,389
45,488
45,564
45,679
45,752
45,844
45,931
46,024
46,089
46,165
46,281
46,362
46,441
46,531
46,615
46,712
46,796
46,849
46,901
47,001
47,075
47,167
47,235
47,308
47,387
47,482
47,548
47,624
47,682
47,718
47,765
47,814
47,904
47,988
48,081
48,155
48,248
48,331
Total
Flow
Daily
kgal
132
139
129
138
108
149
147
131
146
186
204
150
105
205
NA
NA
124
191
166
190
134
NA
NA
177
181
108
182
200
161
193
202
175
143
189
141
174
194
186
182
195
138
147
220
158
104
220
173
196
174
110
115
201
143
176
122
124
163
191
132
158
128
87
86
94
173
151
187
148
181
156
Cumulative
Flow
Totalizer
kgal
31,515
31,654
31,783
31,921
32,029
32,178
32,325
32,456
32,602
32,788
32,992
33,142
33,247
33,452
33,541
33,792
33,916
34,107
34,273
34,463
34,597
34,388
34,908
35,085
35,266
35,374
35,556
35,756
35,917
36,110
36,312
36,487
36,630
36,819
36,960
37,134
37,328
37,514
37,696
37,891
38,029
38,176
38,396
38,554
38,658
38,878
39,051
39,247
39,421
39,531
39,646
39,847
39,990
40,166
40,288
40,412
40,575
40,766
40,898
41,056
41,184
41,271
41,357
41,451
41,624
41,775
41,962
42,110
42,291
42,447
Cumulative
Total Bed
Volumes
#of BV
33960
34110
34249
34398
34514
34675
34833
34974
35131
35332
35552
35713
35827
36047
36143
36414
36547
36753
36932
37137
37281
37056
37616
37807
38002
38119
38315
38530
38704
38912
39129
39318
39472
39676
39828
40015
40224
40425
40621
40831
40980
41138
41375
41545
41657
41894
42081
42292
42480
42598
42722
42939
43093
43282
43414
43547
43723
43929
44071
44241
44379
44473
44566
44667
44853
45016
45218
45377
45572
45740
Head Loss
(psi)
Vessel A
off
8.0
9.0
off
4.0
off
off
off
8.0
10.0
3.0
off
off
off
off
9.0
3.0
off
off
4.0
off
5.0
6.0
off
off
off
off
6.0
off
9.0
4.0
off
off
off
8.0
10.0
3.0
off
off
off
6.0
7.0
3.0
off
5.0
9.0
off
off
off
8.0
off
3.0
off
off
off
10.0
off
off
4.0
off
6.0
off
off
5.0
off
off
off
5.0
off
8.0
Vessel B
off
8.0
9.0
off
4.0
off
off
off
8.0
10.0
3.0
off
off
off
off
10.0
3.0
off
off
4.0
off
5.0
6.0
off
off
off
off
6.0
off
8.0
4.0
off
off
off
8.0
10.0
3.0
off
off
off
6.0
7.0
3.0
off
5.0
9.0
off
off
off
8.0
off
3.0
off
off
off
10.0
off
off
4.0
off
6.0
off
off
5.0
off
off
off
5.0
off
8.0
System Pressure
(psig)
Influent
off
72
74
off
66
off
off
off
NM
78
62
off
off
off
off
77
60
off
off
66
off
64
68
off
off
off
off
68
off
73
66
off
off
off
74
70
62
off
off
off
72
74
60
off
64
72
off
off
off
70
off
62
off
off
off
74
off
off
64
off
68
off
off
66
off
off
off
64
off
80
Effluent
58
56
56
56
58
56
58
56
58
58
56
56
58
58
58
58
54
56
56
58
56
54
56
58
56
58
56
56
58
56
58
56
56
56
58
58
56
58
58
54
60
60
54
56
54
54
56
58
54
54
54
56
58
56
54
54
54
56
56
54
56
58
56
56
58
58
56
54
56
54
AP
psig
NA
16
18
NA
8
NA
NA
NA
NA
20
6
NA
NA
NA
NA
19
6
NA
NA
8
NA
10
12
NA
NA
NA
NA
12
NA
17
8
NA
NA
NA
16
12
6
NA
NA
NA
12
14
6
NA
10
18
NA
NA
NA
16
NA
6
NA
NA
NA
20
NA
NA
8
NA
12
NA
NA
10
NA
NA
NA
10
NA
26
A-13
-------
Table A-l. EPA Arsenic Demonstration Project at Desert Sands MDWCA, NM - Daily System
Operation Log Sheet (Continued)
Week
No.
131
132
133
134
Date
07/17/06
07/18/06
07/19/06
07/20/06
07/21/06
07/22/06
07/23/06
07/24/06
07/25/06
07/26/06
07/27/06
07/28/06
07/29/06
07/30/06
07/31/06
08/01/06
08/02/06
08/03/06
08/04/06
08/05/06
08/06/06
08/07/06
08/08/06
08/09/06
08/10/06
08/11/06
08/12/06
08/13/06
08/14/06
08/15/06
08/16/06
08/17/06
Pump House Instrument Panel
Operation
Hours
hr
10.0
2.7
12.7
16.4
11.5
11.9
10.2
11.2
10.7
10.8
11.5
10.4
8.0
7.8
9.8
5.3
4.2
10.4
4.3
5.5
8.7
8.6
8.0
9.5
6.5
9.1
7.0
7.2
7.2
8.5
3.4
3.9
Cumulative
Operation
Hours
hr
2741.1
2743.8
2756.5
2772.9
2784.4
2796.3
2806.5
2817.7
2828.4
2839.2
2850.7
2861.1
2869.1
2876.9
2886.7
2892.0
2896.2
2906.6
2910.9
2916.4
2925.1
2933.7
2941.7
2951.2
2957.7
2966.8
2973.8
2981.0
2988.2
2996.7
3000.1
3004.0
Master
Flow Meter
kgal
328,243
328,288
328,488
328,739
328,916
329,098
329,254
329,425
329,591
329,758
329,935
330,093
330,216
330,338
330,488
330,568
330,633
330,795
330,863
330,948
331,085
331,215
331,340
331,488
331,590
331,733
331,841
331,954
332,065
332,197
332,251
332,310
Flow
Totalizer
Vessel A
kgal
47,309
47,328
47,425
47,545
47,629
47,713
47,783
47,860
47,937
48,013
48,092
48,159
48,221
48,290
48,353
48,393
48,426
48,505
48,535
48,576
48,635
48,686
48,740
48,814
48,863
48,932
48,984
49,040
49,092
49,154
49,179
49,207
Flow
Totalizer
Vessel B
kgal
48,412
48,436
48,535
48,660
48,750
48,843
48,924
49,016
49,100
49,186
49,280
49,366
49,426
49,485
49,557
49,595
49,617
49,697
49,732
49,775
49,848
49,925
49,992
50,062
50,113
50,183
50,236
50,290
50,347
50,414
50,441
50,472
Total
Flow
Daily
kgal
148
43
196
245
174
177
151
169
161
162
173
153
122
128
135
78
55
159
65
84
132
128
121
144
100
139
105
110
109
129
52
59
Cumulative
Flow
Totalizer
kgal
42,595
42,638
42,834
43,079
43,253
43,430
43,581
43,750
43,911
44,073
44,246
44,399
44,521
44,649
44,784
44,862
44,917
45,076
45,141
45,225
45,357
45,485
45,606
45,750
45,850
45,989
46,094
46,204
46,313
46,442
46,494
46,553
Cumulative
Total Bed
Volumes
#of BV
45900
45946
46157
46421
46609
46800
46962
47144
47318
47492
47679
47844
47975
48113
48259
48343
48402
48573
48643
48734
48876
49014
49144
49300
49407
49557
49670
49789
49906
50045
50101
50165
Head Loss
(psi)
Vessel A
off
9.0
4.0
off
off
off
8.0
off
4.0
off
off
9.0
off
4.0
off
off
5.0
off
4.0
off
6.0
off
4.0
off
off
4.0
off
off
4.0
off
6.0
off
Vessel B
off
9.0
4.0
off
off
off
8.0
off
4.0
off
off
9.0
off
4.0
off
off
6.0
off
4.0
off
6.0
off
4.0
off
off
4.0
off
off
4.0
off
6.0
off
System Pressure
(psig)
Influent
off
72
67
off
off
off
70
off
62
off
off
72
off
66
off
off
65
off
64
off
68
off
62
off
off
66
off
off
64
off
70
off
Effluent
58
54
56
58
56
56
54
58
54
56
56
54
56
58
56
56
54
54
56
58
56
56
54
54
56
58
54
56
56
56
58
off
iP
psig
NA
18
11
NA
NA
NA
16
NA
8
NA
NA
18
NA
8
NA
NA
11
NA
8
NA
12
NA
8
NA
NA
8
NA
NA
8
NA
12
NA
Note: BV calculation for Run 1 (01/23/04-07/14/05) based on 80 ft3 of E33-S media per vessel.
Note: BV calculation for Run 2 (07/29/05-08/16/06) based on 62 ft3 of E33-P media per vessel.
A-14
-------
APPENDIX B
ANALYTICAL DATA
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
NO3-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
mg/L(a)
mg/L
mg/L
mg/LW
mg/L
Mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L(a)
mg/L«
mg/L(a)
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
01/23/04(c)
IN
-
173
0.5
180
0.2
41.8
<5
<5
<0.05
3.5
7.8
28.7
1.0
-
-
81.1
65.5
15.6
26.1
23.2
2.9
17.6
5.6
45
<25
9.1
9.4
AC
-
173
0.5
170
0.2
41.7
-
<0.05
1.2
7.9
29.4
1.4
-
0.5
80.7
67.5
13.2
26.7
23.0
3.7
1.1
21.9
43
<25
8.4
8.1
TT
0
173
0.5
180
0.2
37.2
-
<0.05
0.1
7.9
29.7
2.3
-
0.3
81.5
67.6
13.9
1.5
1.2
0.2
0.9
0.3
<25
<25
0.2
0.1
01/28/04
IN
-
173
-
-
<0.10
40.5
-
-
0.2
8.1
28.4
1.9
-
-
-
-
-
26.0
-
-
-
-
73
-
10.1
-
AC
-
173
-
-
<0.10
40.8
-
-
0.2
8.0
28.8
2.0
-
0.3
-
-
-
25.9
-
-
-
-
70
-
10.3
-
TA
362
169
-
-
<0.10
38.5
-
-
0.1
8.0
28.9
2.0
-
0.3
-
-
-
1.9
-
-
-
-
<25
-
0.3
-
TB
353
169
-
-
<0.10
39.2
-
-
<0.1
7.9
29.0
1.9
-
0.3
-
-
-
1.5
-
-
-
-
<25
-
0.1
-
02/04/04
IN
-
180
-
-
<0.10
36.4
<5
<5
-
0.5
8.1
30.2
1.1
-
-
-
-
-
26.2
-
-
-
-
106
-
9.4
-
AC
-
176
-
-
<0.10
37.3
-
-
0.8
8.0
29.5
1.8
-
-
-
-
-
27.0
-
-
-
-
112
-
9.5
-
TA
657
180
-
-
<0.10
35.3
-
-
0.2
7.9
29.9
1.5
-
0.4
-
-
-
2.0
-
-
-
-
45
-
0.1
-
TB
775
178
-
-
<0.10
36.4
-
-
0.2
7.9
29.8
1.5
-
0.4
-
-
-
1.7
-
-
-
-
35
-
0.1
-
02/11/04
IN
-
186
-
-
<0.10
36.6
-
-
0.4
7.9
29.9
1.0
-
-
-
-
-
25.3
-
-
-
-
98
-
9.6
-
AC
-
190
-
-
<0.10
37.4
-
-
0.5
7.9
30.0
1.6
-
-
-
-
-
27.5
-
-
-
-
97
-
9.0
-
TA
963
186
-
-
<0.10
36.2
-
-
0.2
7.9
30.2
1.5
-
-
-
-
-
2.0
-
-
-
-
46
-
0.1
-
TB
1,183
182
-
-
<0.10
37.0
-
-
0.2
7.9
29.9
1.4
-
-
-
-
-
2.0
-
-
-
-
42
-
0.2
-
(a) As CaCO3. (b) As PO4. (c) Water quality parameters sampled on January 27, 2004.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
NO3-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L
Hg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
02/18/04
IN
-
193
0.6
190
<0.10
38.4
-
<0.08
2.4
7.8
29.8
1.2
-
-
-
89.4
71.9
17.5
28.6
23.9
4.7
22.8
1.1
55
<25
9.9
9.0
AC
-
191
0.6
190
<0.10
39.0
-
<0.08
0.2
7.9
30.1
1.3
-
0.4
0.5
87.4
70.7
16.7
28.7
23.6
5.1
1.1
22.6
36
<25
9.4
6.0
TT
1,496
189
0.6
190
<0.10
38.2
-
<0.08
0.7
7.9
30.2
1.4
-
0.4
0.5
89.2
71.1
18.1
1.5
1.4
0.1
1.1
0.3
<25
<25
0.3
0.1
02/25/04
IN
-
185
-
-
<0.10
39.3
-
-
0.3
7.9
29.7
1.2
-
-
-
-
-
-
27.6
-
-
-
-
35
-
9.7
-
AC
-
185
-
-
<0.10
38.9
-
-
0.3
7.9
28.9
1.2
-
0.4
0.5
-
-
-
27.9
-
-
-
-
31
-
9.5
-
TA
1,715
185
-
-
<0.10
39.0
-
-
0.1
7.9
29.0
1.1
-
0.4
0.5
-
-
-
1.7
-
-
-
-
<25
-
0.1
-
TB
2,167
185
-
-
<0.10
38.5
-
-
0.1
7.9
29.4
1.6
-
0.4
0.5
-
-
-
1.5
-
-
-
-
<25
-
0.1
-
03/03/04
IN
-
177
-
-
<0.10
37.9
<5
<5
-
0.3
7.9
29.9
1.3
-
-
-
-
-
-
29.8
-
-
-
-
39
-
9.5
-
AC
-
179
-
-
<0.10
37.3
-
-
0.1
7.9
29.7
1.3
-
-
-
-
-
-
28.6
-
-
-
-
30
-
9.1
-
TA
2,042
179
-
-
<0.10
37.9
-
-
0.2
-
-
-
-
-
-
-
-
-
1.8
-
-
-
-
<25
-
0.1
-
TB
2,610
181
-
-
<0.10
38.3
-
-
<0.1
-
-
-
-
-
-
-
-
-
1.7
-
-
-
-
<25
-
0.1
-
03/10/04
IN
-
181
-
-
<0.10
36.4
-
-
0.4
8.0
30.4
1.3
-
-
-
-
-
-
23.0
-
-
-
-
53
-
8.3
-
AC
-
189
-
-
<0.10
36.4
-
-
0.3
7.9
30.8
1.2
-
0.4
0.5
-
-
-
23.2
-
-
-
-
47
-
8.2
-
TA
2,350
185
-
-
<0.10
36.0
-
-
0.2
7.8
30.6
1.2
-
0.4
0.5
-
-
-
1.4
-
-
-
-
<25
-
0.2
-
TB
3,010
181
-
-
<0.10
36.3
-
-
0.2
7.8
30.6
1.2
-
0.4
0.5
-
-
-
1.4
-
-
-
-
<25
-
0.3
-
(a) As CaCO3. (b) As PO4.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
mg/L»
mg/L
mg/L
mg/L<»
mg/L
Mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/Lw
mg/Lw
mg/Lw
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
03/17/04
IN
-
182
0.5
190
<0.10
38.7
-
<0.05
0.5
7.9
30.4
1.3
-
-
-
78.4
63.9
14.5
22.6
22.4
0.2
20.7
1.7
49
<25
8.5
7.5
AC
-
182
0.5
180
<0.10
38.4
-
<0.05
0.2
7.9
30.4
1.2
-
0.4
0.5
82.1
67.4
14.7
22.3
22.1
0.2
0.5
21.6
32
<25
7.6
5.3
TT
3,177
178
0.5
190
<0.10
38.6
-
<0.05
0.2
7.9
30.6
1.3
-
0.4
0.5
81.9
66.6
15.3
0.9
0.8
0.1
0.3
0.5
<25
<25
<0.1
<0.1
03/24/04
IN
-
189
-
-
<0.10
38.5
-
-
0.4
7.9
30.4
1.5
-
-
-
-
-
-
25.9
-
-
-
-
33
-
8.4
-
AC
-
189
-
-
<0.10
38.3
-
-
0.3
7.9
31.0
1.2
-
0.4
0.5
-
-
-
25.9
-
-
-
-
30
-
7.9
-
TA
3,112
185
-
-
<0.10
38.0
-
-
0.1
7.9
30.9
1.1
-
0.5
0.5
-
-
-
2.4
-
-
-
-
<25
-
0.1
-
TB
3,995
193
-
-
<0.10
38.4
-
-
0.1
7.8
31.1
1.1
-
0.4
0.5
-
-
-
2.5
-
-
-
-
<25
-
0.1
-
03/31/04
IN
-
183
-
-
<0.10
37.9
<5
<5
-
1.0
7.8
30.2
1.2
-
-
-
-
-
-
20.7
-
-
-
-
71
-
9.0
-
AC
-
181
-
-
<0.10
37.2
-
-
1.5
7.9
30.6
1.2
-
0.5
0.6
-
-
-
21.2
-
-
-
-
69
-
9.4
-
TA
3,467
185
-
-
<0.10
37.6
-
-
0.5
7.9
31.0
1.3
-
0.5
0.6
-
-
-
1.8
-
-
-
-
<25
-
<0.1
-
TB
4,447
181
-
-
<0.10
37.8
-
-
0.2
7.9
31.0
1.1
-
-
-
-
-
-
1.9
-
-
-
-
<25
-
0.1
-
04/07/04
IN
-
180
-
-
<0.10
39.4
-
-
0.9
NA(C)
NA(C)
NA(C)
-
-
-
-
-
-
30.1
-
-
-
-
<25
-
7.5
-
AC
-
180
-
-
<0.10
40.2
-
-
1.0
NA(C)
NA(C)
NA(C)
-
-
-
-
-
-
30.1
-
-
-
-
<25
-
7.3
-
TA
3,738
184
-
-
<0.10
39.9
-
-
0.2
NA(C)
NA(C)
NA(C)
-
-
-
-
-
-
1.9
-
-
-
-
<25
-
0.1
-
TB
4,790
180
-
-
<0.10
40.0
-
-
0.4
NA(C)
NA(C)
NA(C)
-
-
-
-
-
-
1.8
-
-
-
-
<25
-
0.1
-
(a) As CaCO3. (b) As PO4. (c) Operator was not available to take water quality readings.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
mg/L(a)
mg/L
mg/L
mg/L<»
mg/L
Hg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(a)
Mg/L
M8/L
M8/L
M8/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
04/14/04
IN
-
164
0.7
190
<0.10
38.2
-
<0.05
0.6
7.9
29.6
1.3
42
-
-
85.7
71.1
14.6
28.5
24.8
3.7
22.0
2.8
<25
<25
8.3
8.0
AC
-
170
0.7
190
<0.10
38.1
-
<0.05
0.3
7.9
29.5
1.3
550
0.4
0.5
85.3
70.9
14.4
29.6
24.7
4.9
1.1
23.6
<25
<25
8.1
6.2
TT
4,572
178
0.7
180
<0.10
37.6
-
<0.05
0.3
8.0
29.5
1.3
561
0.5
0.6
84.0
69.4
14.6
1.5
1.6
<0.1
0.9
0.7
<25
<25
0.2
0.1
04/30/04
IN
-
199
-
-
NA(C)
38.1
-
-
NA(C)
7.9
30.3
1.2
48
-
-
-
-
-
24.2
-
-
-
-
32
-
9.1
-
AC
-
175
-
-
NA(C)
38.0
-
-
NA(C)
7.9
30.6
1.2
542
0.4
0.5
-
-
-
23.6
-
-
-
-
27
-
7.9
-
TA
4,603
199
-
-
NA(C)
38.0
-
-
NA(C)
7.9
30.1
1.1
521
0.4
0.5
-
-
-
1.7
-
-
-
-
<25
-
0.5
-
TB
6,057
179
-
-
NA(C)
37.9
-
-
NA(C)
7.8
30.5
1.2
525
0.4
0.5
-
-
-
1.6
-
-
-
-
<25
-
0.5
-
05/12/04
IN
-
194
0.6
180
<0.10
37.4
<5
<5
<0.05
0.7
7.8
30.7
1.2
52
-
-
101.1
83.7
17.4
25.8
22.0
3.8
21.2
0.8
<25
<25
7.0
7.1
AC
-
194
0.6
180
<0.10
37.5
-
<0.05
0.6
7.8
30.9
1.1
537
0.4
0.5
111.1
91.9
19.2
25.4
20.3
5.1
0.9
19.4
<25
<25
7.1
5.9
TT
6,176
188
0.6
180
<0.10
37.7
-
<0.05
0.5
7.8
31.2
1.3
541
0.4
0.5
110.1
86.6
23.5
1.6
1.4
0.2
0.8
0.6
<25
<25
<0.1
<0.1
05/26/04
IN
-
226
194
-
-
<0.10
<0.10
38.3
38.1
-
-
2.8
1.5
7.9
31.0
1.2
62
-
-
-
-
-
21.4
21.2
-
-
-
-
64
51
-
9.9
9.1
-
AC
-
190
186
-
-
<0.10
<0.10
37.3
37.1
-
-
0.8
0.5
7.8
31.3
1.1
525
0.5
0.6
-
-
-
21.7
21.7
-
-
-
-
40
38
-
8.6
8.4
-
TA
5,897
194
190
-
-
<0.10
<0.10
37.9
37.1
-
-
0.4
0.7
7.8
31.2
1.6
503
0.5
0.6
-
-
-
1.7
2.0
-
-
-
-
<25
<25
-
0.3
0.3
-
TB
7,605
194
194
-
-
<0.10
<0.10
37.6
37.2
-
-
0.5
0.8
7.7
31.1
1.5
510
0.5
0.6
-
-
-
2.1
2.4
-
-
-
-
<25
<25
-
0.3
0.3
-
(a) As CaCO3. (b) As PO4. (c) Sample out of holding time for laboratory analysis.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L»
mg/L
mg/L
mg/L*'
mg/L
Hg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(a)
Mg/L
Mg/L
M8/L
M8/L
M8/L
Mg/L
Mg/L
Mg/L
Mg/L
06/09/04
IN
-
187
0.6
170
<0.10
37.8
-
<0.04
2.6
7.8
31.6
1.8
55
-
-
89.8
72.5
17.3
25.1
23.1
2.0
22.6
0.5
50
<25
11.0
10.5
AC
-
187
0.6
170
<0.10
37.8
-
<0.04
0.6
7.8
31.5
1.4
488
0.4
0.5
90.1
73.0
17.1
25.4
23.5
1.9
21.1
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
NO3-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(!l)
mg/L
mg/L
mg/L*'
mg/L
|xg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/Lw
re/L
re/L
re/L
re/L
re/L
|xg/L
Hg/L
|xg/L
Hg/L
08/04/04
IN
-
184
0.5
170
<0.10
38.1
<5
<5
<0.04
0.2
7.6
30.4
1.1
92
-
-
98.3
82.0
16.3
21.5
21.5
<0.1
21.0
0.5
49
38
8.7
8.8
AC
-
188
0.5
170
<0.10
38.0
-
<0.04
0.2
7.7
30.8
1.2
454
0.5
0.5
99.2
83.0
16.2
22.0
21.7
0.3
0.8
20.9
61
<25
10.7
5.9
TT
14.2
184
0.5
180
<0.10
37.8
-
<0.04
0.1
7.7
31.2
1.1
468
0.4
0.5
99.3
82.9
16.4
2.8
2.8
<0.1
0.8
2.0
<25
<25
0.2
0.5
08/18/04
IN
-
184
-
-
<0.10
38.8
-
-
0.6
7.6
30.2
0.9
101
-
-
-
-
-
22.4
-
-
-
-
89
-
8.6
-
AC
-
180
-
-
<0.10
38.1
-
-
0.6
7.6
30.5
0.9
476
0.4
0.5
-
-
-
22.8
-
-
-
-
88
-
8.7
-
TA
14.5
176
-
-
<0.10
38.2
-
-
0.1
7.6
30.8
1.3
471
0.4
0.5
-
-
-
4.2
-
-
-
-
<25
-
0.2
-
TB
16.4
180
-
-
<0.10
38.1
-
-
0.1
7.6
30.6
1.4
485
0.4
0.5
-
-
-
4.2
-
-
-
-
<25
-
0.6
-
09/01/04
IN
-
181
0.4
170
<0.10
38.2
<5
<5
<0.04
0.9
7.6
30.1
0.9
NA
-
-
-
-
-
24.9
24.5
0.4
22.2
2.3
68
27
9.0
9.6
AC
-
181
0.4
160
<0.10
38.0
-
<0.04
0.2
7.6
30.4
1.0
495
0.5
0.6
-
-
-
27.2
25.2
5.0
3.3(c)
21.9
56
<25
11.9
6.0
TT
16.5
181
0.4
200
<0.10
38.4
-
<0.04
0.2
7.7
30.4
0.8
515
0.5
0.6
-
-
-
7.4
7.4
<0.1
41(c)
3.3
<25
<25
0.3
0.4
09/15/04
IN
-
182
-
-
<0.06
38.5
-
-
0.7
7.6
29.9
0.8
74
-
-
-
-
-
21.6
-
-
-
-
108
-
10.1
-
AC
-
182
-
-
<0.06
38.3
-
-
0.7
7.6
30.1
1.1
480
0.5
0.6
-
-
-
23.2
-
-
-
-
112
-
14.7
-
TA
16.7
186
-
-
<0.06
38.4
-
-
0.4
7.6
30.3
1.3
490
0.5
0.5
-
-
-
3.1
-
-
-
-
48
-
0.6
-
TB
18.5
182
-
-
<0.06
38.8
-
-
0.4
7.6
30.2
1.2
502
0.5
0.5
-
-
-
3.5
-
-
-
-
44
-
0.7
-
(a) As CaCO3. (b) As PO4. (c) Prechlorination system failed the day before sampling. System repaired and chlorine residual returned to normal prior to collecting samples.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
NO3-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L00
mg/L
mg/L
mg/L*'
mg/L
re/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
re/L
re/L
re/L
re/L
re/L
re/L
re/L
re/L
re/L
09/29/04
IN
-
176
0.3
180
<0.06
37.8
-
<0.04
0.8
7.6
30.2
0.9
90
-
-
101.6
83.4
18.2
24.8
24.5
0.3
23.2
1.3
64
47
9.4
9.2
AC
-
185
0.3
170
<0.06
38.4
-
<0.04
0.3
7.6
30.4
1.1
506
0.5
0.6
101.0
83.1
17.9
25.4
24.7
0.7
3.2(c)
21.5
49
<25
8.3
6.0
TT
18.5
185
0.3
170
<0.06
37.7
-
<0.04
<0.1
7.6
30.5
1.2
520
0.5
0.6
102.4
84.1
18.3
6.8
6.6
0.2
3.4(c)
3.2
<25
<25
0.4
0.3
10/13/04
IN
-
171
171
-
-
<0.06
<0.06
37.5
37.4
<5
<5
-
0.5
0.4
7.6
30.1
0.5
79
-
-
-
-
-
22.1
23.0
-
-
-
-
78
81
-
24.8
9.7
-
AC
-
171
175
-
-
<0.06
<0.06
37.2
37.2
-
-
0.4
0.4
7.6
30.1
1.0
529
0.6
0.6
-
-
-
22.4
22.1
-
-
-
-
85
63
-
10.0
9.2
-
TA
18.4
187
183
-
-
<0.06
<0.06
37.2
37.4
-
-
0.2
0.1
7.6
30.4
1.0
545
0.6
0.6
-
-
-
3.7
3.7
-
-
-
-
<25
<25
-
4.9
3.1
-
TB
20.2
175
175
-
-
<0.06
<0.06
37.8
36.5
-
-
0.4
0.2
7.6
30.4
0.9
552
0.6
0.6
-
-
-
3.5
3.6
-
-
-
-
<25
<25
-
1.4
0.1
-
10/28/04
IN
-
185
0.2
170
<0.06
38.0
-
<0.04
0.3
7.6
30.1
0.3
28
-
-
90.4
70.4
20.0
23.8
25.4
<0.1
25.2
0.2
39
<25
7.9
7.8
AC
-
189
0.2
170
<0.06
38.2
-
<0.04
0.3
7.6
30.3
0.6
502
0.6
0.7
95.0
76.0
19.0
27.9
27.2
0.2
4.6(c)
22.6
26
<25
7.5
5.8
TT
20.2
189
0.2
170
<0.06
37.8
-
<0.04
0.3
7.6
30.4
0.5
392
0.5
0.5
99.6
81.7
17.9
9.3
7.4
1.9
41(c)
3.3
<25
<25
0.3
0.4
11/03/04
IN
-
185
-
-
<0.06
36.8
<5
<5
-
0.2
7.6
29.0
0.5
56
-
-
-
-
-
23.0
-
-
-
-
<25
-
7.7
-
AC
-
185
-
-
<0.06
36.9
-
-
0.2
7.7
29.2
0.7
458
0.5
0.6
-
-
-
23.0
-
-
-
-
<25
-
7.4
-
TA
19.6
181
-
-
<0.06
37.3
-
-
0.1
7.7
29.4
0.7
494
0.5
0.5
-
-
-
6.8
-
-
-
-
<25
-
0.1
-
TB
21.6
185
-
-
<0.06
37.3
-
-
0.2
7.7
29.4
0.6
502
0.5
0.6
-
-
-
7.2
-
-
-
-
<25
-
<0.1
-
(a) As CaCO3. (b) As PO4. (c) Prechlorination system failed the day before sampling. System repaired and
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA
chlorine residual returned to normal prior to collecting samples.
= data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L
re/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(a)
|xg/L
re/L
re/L
re/L
re/L
|xg/L
|xg/L
|xg/L
|xg/L
11/17/04
IN
-
185
0.5
170
<0.06
37.7
-
<0.04
0.5
7.6
29.3
0.4
27
-
-
82.7
67.2
15.5
22.7
22.5
0.2
22.0
0.5
34
<25
9.1
8.9
AC
-
189
0.5
160
<0.06
37.6
-
<0.04
0.3
7.6
30.1
0.6
540
0.7
0.8
83.4
67.7
15.7
23.0
23.1
<0.1
1.4
21.7
<25
<25
8.8
7.3
TT
21.6
189
0.7
170
1.4(c)
37.5
-
<0.04
0.3
7.6
30.1
0.5
502
0.7
0.8
82.7
67.1
15.6
5.8
5.8
<0.1
0.1
5.7
<25
<25
0.3
<0.1
12/01/04
IN
-
183
-
-
<0.06
37.8
<5
<5
-
0.4
7.6
29.6
0.6
78
-
-
-
-
-
26.7
-
-
-
-
64
-
8.2
-
AC
-
183
-
-
<0.06
37.4
-
-
0.3
7.6
30.1
0.7
530
0.6
0.7
-
-
-
27.8
-
-
-
-
58
-
8.3
-
TA
21.2
175
-
-
<0.06
37.6
-
-
0.1
7.7
29.9
0.8
548
0.6
0.7
-
-
-
10.4
-
-
-
-
<25
-
0.4
-
TB
23.3
187
-
-
<0.06
37.5
-
-
0.2
7.7
30.0
0.6
565
0.6
0.7
-
-
-
11.4
-
-
-
-
<25
-
0.3
-
12/15/04
IN
-
183
0.5
190
<0.06
38.9
-
<0.04
1.1
7.6
29.6
0.6
63
-
-
97.0
80.8
16.2
23.9
22.1
1.8
22.0
0.1
154
57
9.7
9.0
AC
-
183
0.5
190
<0.06
38.3
-
<0.04
0.3
7.6
30.1
0.6
562
0.6
0.7
97.4
81.0
16.4
23.7
23.6
0.1
2.2
21.4
73
<25
9.6
5.4
TT
23.0
187
0.5
190
<0.06
38.9
-
<0.04
0.4
7.7
30.3
0.4
520
0.6
0.7
99.3
82.4
16.9
5.3
4.4
1.0
1.9
2.5
<25
<25
0.4
0.2
01/05/05
IN
-
186
186
-
-
<0.06
<0.06
38.7
39.5
<5
<5
-
0.4
0.5
7.8
29.0
0.4
52
-
-
-
-
-
20.6
20.9
-
-
-
-
82
75
-
18.1
10.1
-
AC
-
190
186
-
-
<0.06
<0.06
38.4
38.9
-
-
0.3
0.4
7.8
30.2
0.4
540
0.5
0.5
-
-
-
21.1
21.2
-
-
-
-
68
71
-
11.0
10.3
-
TA
23.2
198
198
-
-
<0.06
<0.06
39.1
38.9
-
-
0.1
0.1
7.7
30.4
0.4
566
0.5
0.5
-
-
-
4.2
4.2
-
-
-
-
<25
<25
-
0.2
<0.1
-
TB
25.1
194
190
-
-
<0.06
<0.06
38.7
39.7
-
-
0.2
0.1
7.7
30.4
0.5
576
0.4
0.5
-
-
-
4.4
4.6
-
-
-
-
<25
<25
-
<0.1
<0.1
-
(a) As CaCO3. (b) As PO4. (c) Data is questionable due to potential sampling or analytical error. All other results from January 28, 2004 through March 2, 2005 have been below reporting limits.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L
re/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
01/20/05
IN
-
181
0.7
251
<0.05
37.3
-
<0.05
0.2
7.6
30.6
0.3
48
-
-
90.3
74.8
15.5
23.0
22.0
1.0
22.1
<0.1
93
30
10.5
9.2
AC
-
172
0.8
249
<0.05
36.8
-
<0.05
0.2
7.6
31.0
0.4
518
0.7
0.7
81.1
67.0
14.1
21.3(c)
22.0(c)
<0.1
21.6(c)
0.4
43
25
10.2
9.1
TT
25.1
189
0.7
250
<0.05
36.6
-
<0.05
<0.1
7.6
31.2
0.4
537
0.6
0.7
80.2
65.8
14.4
5.0
4.3
0.7
2.5
1.8
<25
<25
0.3
0.1
02/02/05
IN
-
200
-
-
<0.05
36.5
<5
<5
-
0.2
7.6
30.8
0.3
28
-
-
-
-
-
19.9
-
-
-
-
54
-
8.7
-
AC
-
200
-
-
<0.05
37.3
-
-
0.1
7.6
31.2
0.3
523
0.6
0.6
-
-
-
19.6
-
-
-
-
49
-
8.1
-
TA
24.7
191
-
-
<0.05
37.1
-
-
<0.1
7.7
30.9
0.4
544
0.5
0.6
-
-
-
3.7
-
-
-
-
<25
-
0.1
-
TB
26.6
195
-
-
<0.05
36.2
-
-
<0.1
7.7
30.8
0.4
546
0.5
0.5
-
-
-
3.8
-
-
-
-
<25
-
0.7
-
02/16/05
IN
-
201
0.5
255
<0.05
39.8
-
<0.05
0.4
7.6
30.6
0.2
20
-
-
76.8
63.6
13.2
20.6
22.1
<0.1
21.7
<0.1
119
55
8.4
9.1
AC
-
201
0.5
255
<0.05
40.2
-
<0.05
0.3
7.6
30.7
0.2
520
0.6
0.6
82.8
70.2
12.6
22.3
22.7
<0.1
1.6
21.1
96
<25
11.2
4.7
TT
26.4
201
0.5
255
<0.05
40.6
-
<0.05
<0.1
7.6
30.7
0.4
522
0.5
0.6
68.3
55.9
12.4
3.5
3.1
0.4
1.6
1.5
<25
<25
0.1
<0.1
03/02/05
IN
-
187
-
-
<0.05
39.1
<5
<5
-
0.3
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
-
-
-
23.2
-
-
-
-
43
-
10.7
-
AC
-
178
-
-
<0.05
39.4
-
-
0.2
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
-
-
-
23.3
-
-
-
-
37
-
8.3
-
TA
26.5
187
-
-
<0.05
39.1
-
-
<0.1
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
-
-
-
5.3
-
-
-
-
<25
-
5.0
-
TB
28.2
182
-
-
<0.05
38.9
-
-
<0.1
NA(d)
NA(d)
NA
NA(d)
NA(d)
NA(d)
-
-
-
4.6
-
-
-
-
<25
-
0.1
-
(a) As CaCO3. (b) As PO4. (c) Data is questionable due to suspected sampling error. It is speculated that the
Confirmatory analysis of sample produced similar values, (d) In order to reduce the work load, the operator w:
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA
AC sample may actually have been collected from the IN sample tap on this date.
ill be taking on-site water quality parameters once every month.
data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
NO3-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L
re/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/Lw
re/L
re/L
re/L
re/L
re/L
|xg/L
Hg/L
|xg/L
Hg/L
03/16/05
IN
-
196
0.5
214
<0.05
39.0
-
<0.05
0.3
7.6
29.9
0.7
31
-
-
82.9
67.0
15.9
20.5
21.7
<0.1
21.7
<0.1
48
29
8.3
8.8
AC
-
196
0.5
199
<0.05
38.9
-
<0.05
0.3
7.6
30.2
0.2
540
0.4
0.4
83.1
67.6
15.5
21.1
22.1
<0.1
2.0
20.1
59
<25
13.9
6.3
TT
28.6
192
0.5
200
<0.05
39.2
-
<0.05
<0.1
7.7
30.4
0.2
558
0.4
0.4
87.1
71.9
15.2
5.3
5.4
<0.1
2.6
2.8
<25
<25
<0.1
<0.1
03/30/05
IN
-
189
-
-
<0.05
38.4
-
-
0.2
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
22.1
-
-
-
-
56
-
9.0
-
AC
-
189
-
-
<0.05
38.3
-
-
0.2
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
22.6
-
-
-
-
48
-
9.3
-
TA
28.9
180
-
-
<0.05
37.5
-
-
<0.1
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
6.5
-
-
-
-
<25
-
0.2
-
TB
30.4
189
-
-
<0.05
38.4
-
-
<0.1
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
6.5
-
-
-
-
<25
-
0.2
-
04/13/05
IN
-
211
0.4
201
<0.05
39.4
-
<0.05
0.5
7.6
30.3
0.2
63
-
-
83.0
68.4
14.6
26.2
26.8
<0.1
20.1
6.7
90
<25
9.6
6.3
AC
-
216
0.5
200
<0.05
39.2
-
<0.05
0.5
7.6
30.5
0.3
505
0.4
0.5
83.1
68.8
14.3
21.1
20.5
0.6
2.1
18.4
72
49
15.8
7.6
TT
31.0
180
0.4
195
<0.05
39.4
-
0.06
0.1
7.6
30.6
0.2
522
0.5
0.5
81.2
66.2
15.0
5.8
5.8
<0.1
2.1
3.7
<25
<25
0.2
0.2
04/27/05
IN
-
220
-
-
<0.05
39.9
<5
<5
-
0.5
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
25.4
-
-
-
-
52
-
8.6
-
AC
-
202
-
-
<0.05
40.5
-
-
0.3
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
25.4
-
-
-
-
47
-
8.5
-
TA
32.1
202
-
-
<0.05
39.7
-
-
<0.1
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
8.1
-
-
-
-
<25
-
0.4
-
TB
33.5
198
-
-
<0.05
40.0
-
-
<0.1
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
9.0
-
-
-
-
<25
-
0.5
-
(a) As CaCO3. (b) As PO4. (c) In order to reduce the work load, the operator will be taking on-site water quality parameters once every month.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L
re/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(!l)
mg/L«
mg/L(a)
re/L
Hg/L
re/L
|xg/L
re/L
re/L
Hg/L
re/L
|xg/L
05/11/05
IN
-
198
0.5
174
<0.05
38.4
<5
<5
<0.05
0.2
7.6
31.2
0.2
50
-
-
82.6
69.0
13.7
21.2
21.2
<0.1
21.2
<0.1
59
37
9.3
10.5
AC
-
198
0.5
178
<0.05
39.0
-
0.6
0.2
7.6
31.4
0.3
476
0.6
0.7
82.3
69.3
13.0
22.1
22.8
<0.1
2.0
20.8
64
<25
22.0
7.5
TT
34.6
198
0.5
186
<0.05
38.9
-
<0.05
<0.1
7.6
31.5
0.3
502
0.5
0.6
80.5
66.5
14.0
7.1
7.2
<0.1
1.6
5.6
<25
<25
0.3
0.4
05/25/05
IN
-
178
-
-
<0.05
37.9
<5
<5
-
0.2
NA(C)
NA
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
21.0
-
-
-
-
32
-
8.4
-
AC
-
201
-
-
<0.05
37.7
-
-
2.4
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
22.1
-
-
-
-
30
-
8.0
-
TA
36.1
187
-
-
<0.05
37.6
-
-
2.7
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
7.5
-
-
-
-
<25
-
0.2
-
TB
37.3
187
-
-
<0.05
37.7
-
-
0.7
NA(C)
NA
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
7.3
-
-
-
-
<25
-
0.1
-
06/07/05
IN
-
194
-
-
<0.05
39.1
-
-
0.8
NA(d)
NA<4»
NA(d)
NA(d)
NA(d)
NA(d)
-
-
-
24.3
-
-
-
-
73
-
9.2
-
AC
-
189
-
-
<0.05
39.0
-
-
1.1
NA(d)
NA
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
Sulfide
N03-N
Turbidity
TSS
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L
re/L
mg/L
NTU
mg/L
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
07/06/05
IN
-
176
-
-
<0.05
38.9
<5
<5
-
0.3
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
22.3
-
-
-
-
51
-
8.4
-
AC
-
198
-
-
<0.05
37.9
-
-
0.4
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
22.9
-
-
-
-
51
-
9.4
-
TA
42.8
176
-
-
<0.05
38.3
-
-
<0.1
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
11.9
-
-
-
-
<25
-
0.6
-
TB
43.2
198
-
-
<0.05
38.2
-
-
<0.1
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
8.9
-
-
-
-
<25
-
0.4
-
08/03/05(d)
IN
-
185
0.5
176
<0.05
37.5
<5
<5
0.06
0.7
-
7.9
31.6
0.2
14
-
-
83.2
69.4
13.8
24.1
21.5
2.6
23.1
<0.1
77
<25
8.9
8.7
AC
-
185
0.5
175
<0.05
36.8
-
<0.05
0.3
-
7.9
31.8
0.2
512
1.0
-
80.7
67.0
13.7
31.5
21.9
9.6
3.8
18.1
41
<25
9.1
7.3
TT
0.8
189
0.5
162
<0.05
33.7
-
<0.05
<0.1
-
7.9
31.6
0.2
520
0.5
-
82.6
68.7
13.9
6.8
2.7
4.1
3.3
<0.1
<25
<25
0.3
0.2
08/17/05(e)
IN
-
-
-
-
-
-
-
-
-
-
7.9
29.9
0.2
52
-
-
-
-
-
24.5
-
-
-
-
290
-
10.6
-
AC
-
-
-
-
-
-
-
-
-
-
7.9
30.9
0.1
370
0.6
-
-
-
-
24.7
-
-
-
-
33
-
8.0
-
TT
2.9
-
-
-
-
-
-
-
-
-
7.8
31.2
0.2
410
0.3
-
-
-
-
7.6
-
-
-
-
<25
-
0.4
-
08/31/05
IN
-
185
0.5
194
<0.05
39.6
<5
0.2
1.5
1
7.8
31.4
0.1
65
-
-
83.1
69.2
13.9
25.7
22.5
3.3
21.3
1.2
186
30
10.6
10.3
AC
-
180
0.5
192
<0.05
39.6
-
0.3
0.2
-
7.8
31.7
0.2
502
0.6
-
85.0
70.5
14.6
27.1
23.7
3.4
1.7
22.0
47
18
9.7
8.3
TT
5.1
185
0.5
194
<0.05
38.7
-
1.0
0.2
-
7.7
31.9
0.3
518
0.4
-
85.5
70.9
14.5
2.2
1.8
0.5
1.6
0.2
<25
<25
0.4
0.5
(a) As CaCO3. (b) As PO4. (c) In order to reduce the work load, the operator will be taking on-site water quality parameters once every month, (d) System v
and placed back online July 29, 2005. The bottom laterals, under bedding, and media were replaced and other system repairs were performed during the dow
schedule has been modified to reduce the number of analytes starting August 17, 2005.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
was switched off July 14, 2005
/ntime. (e) The sampling
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Sulfide
NO3-N
Turbidity
TSS
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L*'
mg/L
re/L
mg/L
NTU
mg/L
-
°C
mg/L
mV
mg/L
mg/L
mg/L(!l)
mg/L(a)
mg/L(!l)
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
09/14/05
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Sulfide
N03-N
Turbidity
TSS
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
mg/L*'
mg/L
re/L
mg/L
NTU
mg/L
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
11/09/05
IN
-
189
-
-
-
<0.03
36.5
<5
<5
-
0.2
-
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
-
-
24.7
-
-
-
-
32
-
7.9
-
AC
-
189
-
-
-
<0.03
37.0
-
-
0.1
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
24.1
-
-
-
-
26
-
7.4
-
TA
14.1
198
-
-
-
<0.03
36.7
-
-
<0.1
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
3.7
-
-
-
-
<25
-
<0.1
-
TB
14.4
194
-
-
-
<0.03
36.9
-
-
<0.1
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
3.7
-
-
-
-
<25
-
<0.1
-
11/30/05
IN
-
185
0.4
161
-
<0.03
38.2
<5
<5
<0.05
0.2
1
7.7
31.0
0.3
33
-
-
90.2
75.5
14.8
18.6
19.7
<0.1
19.1
0.5
46
27
8.8
9.0
AC
-
189
0.4
162
-
<0.03
38.4
-
<0.05
0.1
<1
7.7
31.3
0.3
505
0.8
NA
87.1
73.1
14.0
21.8
21.0
0.8
2.0
19.0
27
<25
8.9
7.8
TT
16.5
189
0.4
161
-
<0.03
38.5
-
<0.05
<0.1
<1
7.7
31.4
0.2
524
0.6
NA
88.1
74.2
13.9
5.0
4.9
<0.1
2.2
2.7
<25
<25
0.6
0.4
12/14/05
IN
-
185
-
-
-
<0.03
37.4
-
-
1.0
-
NA
NA(C)
NA(C)
NA(C)
-
-
-
-
-
21.4
-
-
-
-
42
-
8.9
-
AC
-
194
-
-
-
<0.03
37.9
-
-
1.4
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
21.1
-
-
-
-
36
-
8.6
-
TA
17.5
198
-
-
-
<0.03
38.1
-
-
0.6
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
4.3
-
-
-
-
<25
-
0.8
-
TB
18.3
198
-
-
-
<0.03
38.1
-
-
0.8
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
4.3
-
-
-
-
<25
-
0.6
-
01/04/06
IN
-
189
0.4
165
-
<0.03
38.2
<5
<5
<0.05
0.5
<1
7.7
30.6
0.1
18
-
-
86.3
71.3
15.0
21.5
22.2
<0.1
21.8
0.4
65
29
9.1
9.0
AC
-
198
0.4
170
-
<0.03
36.9
-
<0.05
0.5
-
7.7
30.8
0.2
495
0.8
NA
86.7
72.0
14.7
21.8
22.6
<0.1
0.9
21.6
53
<25
9.5
7.6
TT
20.1
194
0.4
165
-
<0.03
37.6
-
<0.05
0.2
-
7.8
30.8
0.2
512
0.7
NA
86.1
71.3
14.8
3.9
3.9
<0.1
1.0
2.9
<25
<25
0.4
0.3
(a) As CaCO3. (b) As PO4. (c) In order to reduce work load, the operator will be taking on-site water quality parameters once every month.
IN = inlet; AC = after prechlorination; TA = after tank A; TB = after tank B; TT = after tanks combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Desert Sands MDWCA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
As (total)
Fe (total)
Mn (total)
103
re/L
re/L
re/L
02/01/06
------- |