EPA/600/R-08/008
March 2008
Arsenic Removal from Drinking Water by Adsorptive Media
U.S. EPA Demonstration Project at Rimrock, AZ
Final Performance Evaluation Report
by
Julia Valigore
Abraham S.C. Chen
Lili 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, Ohio 45268
National Risk Management Research Laboratory
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, Ohio 45268
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DISCLAIMER
The work reported in this document was funded by the United States Environmental Protection Agency
(EPA) under Task Order (TO) 0019 of Contract No. 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 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 during and the results obtained from the arsenic removal
treatment technology demonstration project at the Arizona Water Company (AWC) facility in Rimrock,
AZ. The objectives of the project were to evaluate: (1) the effectiveness of AdEdge's Arsenic Package
Unit-100 (APU-100) AD-33™ adsorptive media system in removing arsenic to meet the new arsenic
maximum contaminant level (MCL) of 10 |o,g/L, (2) the reliability of the treatment system for use at small
water facilities, (3) the required system operation and maintenance (O&M) and operator skill levels, and
4) the capital and O&M cost of the technology. The project also characterized water in the distribution
system and residuals produced by the treatment process. The types of data collected included system
operation, water quality, process residuals, and capital and O&M cost.
The APU-100 treatment system consisted of a 25-(im bag filter assembly, two 3-ft * 6-ft composite
fiberglass pressure tanks, a backwash wastewater recycling system, associated piping and Fleck controller
valves, and an instrument/control panel. Each tank contained 22 ft3 of Bay oxide E33 iron-based
adsorptive media, which was developed by Bayer AG and branded under the name of AD-33™ by
AdEdge. Due to the loss of one of AWC's production wells, the system flowrate was reduced from 90 to
30 gal/min (gpm), which prompted a change in system configuration from parallel to series (lead/lag).
The reconfigured APU-100 system had a design capacity of 45 gpm and began operation on June 24,
2004. The actual flowrates through the system averaged 30 gpm, corresponding to an empty bed contact
time (EBCT) of 5.4 min/tank and a hydraulic loading rate of 4.2 gpm/ft2.
Source water contained 43.8 to 81.4 |o,g/L of total arsenic with As(V) as the predominant species.
Prechlorination, although not required for oxidation, was performed to provide disinfection throughout
the treatment train and residuals within the distribution system at AWC's discretion. Concentrations of
iron, manganese, silica, orthophosphate, and other ions in source water did not appear to impact arsenic
removal by the AD-33™ media. The system operated for 12 or 24 hr/day on a timer with 1 to 2%
downtime for repairs and media replacement. After treating 52,150 bed volumes (BV) or 17,164,000 gal
of water during Media Run 1A based on 44 ft3 of media in the lead and lag tanks, the system effluent
reached the 10-jog/L arsenic MCL on August 9, 2006. Because the media in the lag tank still had about
50% of adsorptive capacity remaining, only the lead tank was rebedded. After rebedding, the tank
positions were switched with Tank B containing partially exhausted media in the lead position and Tank
A with virgin media in the lag position. Media Run IB commenced as such on November 27, 2006. To
ensure that normal operations continued following the media changeout, the system was monitored until
March 28, 2007.
Backwashing of the media was initially conducted automatically, but due to initiation of several
unscheduled backwash events and the need to take operational data and backwash wastewater samples,
the programming was changed to manual initiation once every 30 days. The backwash frequency was
eventually decreased to quarterly due to minimal differential pressure (Ap) increase across the tanks
between backwash events. Backwash was performed using source water for 15 min/tank at
approximately 47 gpm, or 6.6 gpm/ft2. Backwash wastewater from the lead tank generally contained
higher concentrations of all analytes than that from the lag tank, most likely because the lead tank
removed the majority of the particulates from source water. A piping loop, a recycle tank, and a metering
pump enabled the system to reclaim nearly 100% of the wastewater produced by blending it with intake
after prechlorination but prior to the adsorption tanks at a rate of 0.5 gpm.
Comparison of the distribution system sampling results from three residences before and after startup of
the APU-100 system showed a decrease in the average arsenic concentration from 48.8 to 19.3 |og/L.
However, samples of the distribution system water exhibited higher arsenic concentrations than those of
IV
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the treatment system effluent due to blending of the treated water with untreated water from other source
wells. pH, alkalinity, iron, manganese, lead, and copper concentrations did not appear to be affected by
the system operation.
Treatment system residuals included spent media and backwash wastewater. Spent media including 620
Ib of AD-33™ passed the Toxicity Characteristic Leaching Procedure (TCLP) test and could be disposed
of as non-hazardous waste at a sanitary landfill. The arsenic loading on the spent media based on
inductively coupled plasma-mass spectrometry (ICP-MS) results was 8.3 mg/g, which was about 80% of
the arsenic mass loaded on the media based on the arsenic breakthrough curves.
The capital investment cost of the system was $88,307, consisting of $63,785 for equipment, $11,372 for
site engineering, and $13,150 for installation. Using the system's rated capacity of 45 gpm (or 64,800
gal/day [gpd]), the capital cost was $l,962/gpm (or $1.36/gpd). The capital cost also was converted to an
annualized cost of $8,335/yr based on a 7% interest rate and a 20-yr return period. During the first year,
the system produced approximately 8,505,000 gal of water, so the unit capital cost increased to
$0.98/1,000 gal. These costs do not include the cost of the system enclosure and backwash recycling
system, which were funded separately by AWC.
The O&M cost for the treatment system included cost for media replacement and disposal, electricity
consumption, and labor. Representing the majority of the O&M cost, the media replacement and disposal
cost depended on the media run length, the number of tanks rebedded, and labor and material cost. With
the long, 2.1-year duration of the media run and the remaining capacity of the lag tank when the system
effluent reached 10 |o,g/L of arsenic, the media of only the lead tank was replaced at a cost of $10,908, or
$0.64/1,000 gal. The combined electricity and labor cost was an additional $0.22/1,000 gal for a total
O&M cost of $0.86/1,000 gal.
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CONTENTS
DISCLAIMER ii
FOREWORD iii
ABSTRACT iv
APPENDICES vii
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 4
3.1 General Project Approach 4
3.2 System O&M and Cost Data Collection 5
3.3 Sample Collection Procedures and Schedules 6
3.3.1 Source Water 6
3.3.2 Treatment Plant Water 6
3.3.3 Backwash Water 6
3.3.4 Distribution System Water 7
3.3.5 Residual Solids 9
3.4 Sampling Logistics 9
3.4.1 Preparation of Arsenic Speciation Kits 9
3.4.2 Preparation of Sampling Coolers 9
3.4.3 Sample Shipping and Handling 9
3.5 Analytical Procedures 10
4.0 DEMONSTRATION SITE AND TECHNOLOGY EVALUATED 11
4.1 Site Description 11
4.1.1 Existing Facility 11
4.1.2 Distribution System 11
4.1.3 Source Water Quality 12
4.2 Treatment Process Description 13
4.3 Treatment System Installation 18
4.3.1 System Engineering and Permitting 18
4.3.2 System Installation, Startup, and Shakedown 18
4.3.3 System Enclosure 19
5.0 RESULTS AND DISCUSSION 20
5.1 System Operation 20
5.1.1 Service Operation 20
5.1.2 Backwash Operation 21
5.1.3 Media Changeout 22
5.1.4 Residual Management 22
5.1.5 System/Operation Reliability and Simplicity 23
VI
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5.1.5.1 Pre- and Post-Treatment Requirements 23
5.1.5.2 System Automation 23
5.1.5.3 Operator Skill Requirements 23
5.1.5.4 Preventative Maintenance Activities 23
5.1.5.5 Chemical/Media Handling and Inventory Requirements 24
5.2 System Performance 24
5.2.1 Treatment Plant Sampling 24
5.2.1.1 Arsenic 25
5.2.1.2 Iron and Manganese 27
5.2.1.3 Onsite Measurements 29
5.2.1.4 Other Water Quality Parameters 30
5.2.2 Backwash Water Sampling 30
5.2.3 Distribution System Water Sampling 30
5.2.4 Spent Media Sampling 33
5.3 Cost Information 34
5.3.1 Facility Cost 34
5.3.2 System Cost 34
5.3.3 O&MCost 35
6.0 REFERENCES 37
APPENDICES
APPENDIX A: OPERATIONAL DATA A-l
APPENDIX B: ANALYTICAL DATA TABLES B-l
FIGURES
Figure 3-1. Process Flow Diagram and Sampling Locations 8
Figure 4-1. Predemonstration Site Photographs 11
Figure 4-2. Schematic of AdEdge's APU-100 Treatment System 15
Figure 4-3. Treatment System Components 17
Figure 4-4. Backwash Recycling System Components 17
Figure 4-5. Gravel Underbedding (Left) and AD-33™ Media (Right) Loading 18
Figure 4-6. System Enclosure 19
Figure 5-1. Flowrate Readings and Ap across Tanks 21
Figure 5-2. Arsenic Species during Media Run 1A at Wellhead, after Tank A, and after Tank B 28
Figure 5-3. Total Arsenic Breakthrough Curves for Media Runs 1A and IB 29
Figure 5-4. Media Replacement (Lead Tank) and Total O&M Cost (Run 1A) 36
TABLES
Table 1-1. Summary of the Round 1 Arsenic Removal Demonstration Sites 2
Table 3-1. Predemonstration Study Activities and Completion Dates 4
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities 5
Table 3-3. Sample Collection Schedule and Analyses 7
Table 4-1. Distribution System Water Quality Data Collected by AWC 12
Table 4-2. Source Water Quality Data 13
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Table 4-3. Physical and Chemical Properties of AD-33™ Media 14
Table 4-4. Design Features for AdEdge's APU-100 Treatment System 16
Table 5-1. Summary of APU-100 System Operations 20
Table 5-2. Recommended Routine Maintenance Activities 24
Table 5-3. Summary of Arsenic, Iron, and Manganese Results 25
Table 5-4. Summary of Other Water Quality Parameter Results 26
Table 5-5. Backwash Water Sampling Results 31
Table 5-6. Distribution System Sampling Results 32
Table 5-7. TCLP Results of a Composite Spent Media Sample 33
Table 5-8. Metals' Analysis of Spent Media 33
Table 5-9. Capital Investment for AdEdge's APU-100 System 34
Table 5-10. O&M Cost for AdEdge's APU-100 System (Run 1A) 36
Vlll
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ABBREVIATIONS AND ACRONYMS
Ap differential pressure
AAL American Analytical Laboratories
ADEQ Arizona Department of Environmental Quality
Al aluminum
AM adsorptive media
APU arsenic package unit
As arsenic
AWC Arizona Water Company
Ba barium
BET Brunauer, Emmett, and Teller
bgs below ground surface
BL baseline
BV bed volume(s)
Ca calcium
CCR Consumer Confidence Report
Cd cadmium
Cl chloride
C/F coagulation/filtration
CRF capital recovery factor
DO dissolved oxygen
EBCT empty bed contact time
EPA U.S. Environmental Protection Agency
F fluoride
Fe iron
FedEx Federal Express
GFO granular ferric oxide
gpd gallons per day
gph gallons per hour
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
IX
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Mn
mV
manganese
millivolts
Na sodium
NaOCl sodium hypochlorite
ND not detected
NS not sampled
NSF NSF International
NTU nephlemetric turbidity units
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
PO4 orthophosphate
psi pounds per square inch
PVC polyvinyl chloride
QA quality assurance
QA/QC quality assurance/quality control
QAPP Quality Assurance Project Plan
RPD relative percent difference
RCRA Resource Conservation and Recovery Act
SDWA Safe Drinking Water Act
SM system modification
SiO2 silica
SO4 sulfate
STMGID South Truckee Meadows General Improvement District
STS Severn Trent Services
TCLP Toxicity Characteristic Leaching Procedure
TDS total dissolved solids
TO Task Order
TOC total organic carbon
TSS total suspended solids
WRWC
White Rock Water Company
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ACKNOWLEDGMENTS
The authors wish to extend their sincere appreciation to the staff of the Arizona Water Company (AWC)
in Phoenix and Sedona, Arizona. The primary operators, John Snickers and Ben Graves, monitored the
treatment system and collected samples from the treatment plant and distribution system on a regular
schedule throughout this reporting period. This performance evaluation would not have been possible
without their support and dedication.
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, onsite 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. The
Arizona Water Company (AWC) water system in Rimrock, AZ, was selected as one of the 17 Round 1
host sites for the demonstration program.
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. AdEdge's adsorptive media process
was selected for the Rimrock facility. Designated as AD-33™ by AdEdge, the process uses the Bayoxide
E33-S media developed by Bayer AG.
1.2 Treatment Technologies for Arsenic Removal
The technologies selected for the 12 Round 1 EPA arsenic removal demonstration host sites included nine
adsorptive media (AM) systems, one anion exchange system, one coagulation/filtration (C/F) 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
(http://www.epa.gov/ORD/NRMRL/wswrd/dw/arsenic/index.html). As of January 2008, all of the
systems were operational, and 10 performance evaluations were completed.
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Table 1-1. Summary of the 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-S)
AM (E33-S)
AM (E33-S)
C/F (Macrolite)
SM
AM (E33-S,E33-P)
AM (E33-S)
AM (E33-S)
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; E33-P = E33 pelletized; E33-S = E33 granular media;
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) 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 12 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 AdEdge system operated at Rimrock, AZ, from June 24,
2004, through March 28, 2007. The types of data collected included system operation, water quality
(both across the treatment train and in the distribution system), residuals, and capital and preliminary
O&M cost.
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2.0 SUMMARY AND CONCLUSIONS
The performance evaluation study of the AdEdge arsenic package unit (APU)-IOO was conducted from
June 24, 2004, through March 28, 2007. Based on the information collected during the 33-months of
system operation, the following was summarized and concluded relating to the overall project objectives.
Performance of the arsenic removal technology for use on small systems:
• AD-33™ media was effective at removing arsenic (existing mostly as As[V]) in source water,
reducing its concentrations from 48.3 to 81.4 |o,g/L to <10 ng/L. Breakthrough at 10 |o,g/L
from the lead tank occurred at 39,180 bed volumes (BV) (1 BV = 22 ft3, the amount in one
tank), which represented only 60% of the vendor-projected media run length. Breakthrough
at 10 |og/L from the lag tank occurred much later at 52,150 BV (1BV = 44 ft3, the amount in
both the lead and lag tanks), twice as long empty bed contact time (EBCT) was believed to
have contributed to the longer run length observed.
• Monthly backwash as recommended by the vendor did not appear to benefit the adsorption
runs. The frequency was later reduced to quarterly.
• The APU-100 system was capable of reducing arsenic concentrations in the distribution
system, although its levels were higher than those in the treated water. This was most likely
due to the contribution of untreated water from other wells, which also contained arsenic.
Required system O&M and operator skill levels:
• The system was easy to operate, requiring minimum operator's attention. Daily demand on
the operator was typically 20 min.
• The O&M issues encountered during the performance period were minor, consisting of only a
malfunctioning chlorine injector and a few broken pressure gauges and flow meters/
totalizers. Unscheduled downtime was <2%.
Characteristics of residuals produced by the technology:
• Each backwash event produced 1,460 gal, on average, of wastewater; nearly 100% of the
wastewater was reclaimed via a backwash recycle system.
• Backwash wastewater contained less arsenic than raw water, indicating removal of arsenic by
the media during backwashing.
• Approximately 10.4 mg of arsenic was loaded on per gram of dry media, equivalent to about
1.04% arsenic loading. The spent media was non-hazardous and could be disposed of at a
sanitary landfill.
Capital and O&M cost of the technology:
• The capital investment for the APU-100 system was $88,307, including $63,785 for
equipment, $11,372 for site engineering, and $13,150 for installation.
• Based on a design capacity of 45 gal/min (gpm), the capital cost was $l,962/gpm, or
$1.36/gpd.
• Media replacement cost represented the majority of the O&M cost. The media in the lead
tank was replaced once at a cost of $10,908 or $0.64/1,000 gal, which accounted for 74% of
the O&M cost. The rest of the O&M cost was incurred by electricity 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 AdEdge treatment system began on June 24, 2004. Table 3-2 summarizes the types of data collected
and/or considered as part of the technology evaluation process. The overall system performance was
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 assessed through quantitative data and qualitative
considerations, including the need for 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 system operation were recorded on an Operator Labor Hour Log Sheet.
The quantity of aqueous and solid residuals generated was estimated by tracking the volume of backwash
water produced during each backwash cycle and the need to replace the media upon arsenic breakthrough.
Backwash water and spent media were sampled and analyzed for chemical characteristics.
Table 3-1. Predemonstration Study Activities and Completion Dates
Activity
Introductory Meeting Held
Request for Quotation Issued to Vendor
Draft Letter of Understanding Issued
Final Letter of Understanding Issued
Vendor Quotation Received
Purchase Order Established
Letter Report Issued
Draft Study Plan Issued
Engineering Package Submitted to ADEQ
Final Study Plan Issued
Approval to Construct Granted by ADEQ
Construction Permit Issued by County
APU-100 Unit Shipped
Initial System Installation and Shakedown Completed
Initial Approval of Construction Granted by ADEQ
Shed Construction Completed
System Re-Configuration Completed
Revised Engineering Package Submitted to ADEQ
Final Approval of Construction Granted by ADEQ
Performance Evaluation Began
Date
July 3 1,2003
August 4, 2003
August 13, 2003
September 9, 2003
September 9, 2003
October 6, 2003
October 17, 2003
November 26, 2003
December 11, 2003
December 19, 2003
February 18, 2004
March 15, 2004
March 30, 2004
April 22, 2004
April 29, 2004
May 2 1,2004
May 27, 2004
June 1, 2004
June 15, 2004
June 24, 2004
ADEQ = Arizona Department of Environmental Quality
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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 gpm (or gal/day [gpd]) of design
capacity and the O&M cost per 1,000 gal of water treated. This task required tracking the capital cost for
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 according to
instructions provided by AdEdge and Battelle. 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
operation on a regular basis. If any problems occurred, the plant operator contacted the Battelle Study
Lead, who determined if the vendor should be contacted for troubleshooting. The plant operator recorded
all relevant information on the Repair and Maintenance Log Sheet. Water quality parameters, including
temperature, pH, dissolved oxygen (DO), oxidation-reduction potential (ORP), and residual chlorine were
measured and recorded on a Weekly Onsite Water Quality Parameters Log Sheet. Backwash data also
were recorded on a Backwash Log Sheet when appropriate.
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 usage, and labor. Consumption of NaOCl was tracked on the Daily System
Operation Log Sheet. Electricity consumption was determined from an electric meter. Labor for various
activities, such as the routine system O&M, troubleshooting and repair, and demonstration-related work,
was tracked using an Operator Labor Hour Log Sheet. The routine O&M included activities such as
completing field logs, replenishing the NaOCl solution, ordering supplies, performing system inspection,
and others as recommended by the vendor. The demonstration-related labor, 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.
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3.3 Sample Collection Procedures and Schedules
To evaluate the system performance, samples were collected from the wellhead, treatment plant, and
distribution system. The sampling schedules and analytes for each sampling event are listed in Table 3-3.
In addition, 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 site visit, 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. Water samples were collected weekly across the treatment train at
the wellhead (IN), after Tank A (TA), and after Tank B (TB) for on- and off-site analyses shown in
Figure 3-1 and Table 3-3. Onsite measurements also were made on samples collected from after
prechlorination (AC) location. Over the course of the demonstration study, several changes were made to
the sampling schedules as listed below and in Table 3-3.
• Beginning on November 3, 2004, regular weekly sampling was reduced from three times per
four week cycle to three times per eight week cycle.
• Speciation sampling was reduced from monthly to bimonthly beginning on October 20, 2004,
and then discontinued after July 12, 2006.
• Since October 12, 2005, orthophosphate analysis was replaced with total phosphorous
analysis due to lack of orthophosphate in raw water and issues related to the short hold time
for orthophosphate.
• Onsite measurements were reduced to monthly beginning April 5, 2006, and to pH,
temperature, and chlorine only beginning June 14, 2006.
• All analyses except for arsenic discontinued on November 28, 2006.
3.3.3 Backwash Water. Grab backwash wastewater samples were initially collected directly from
the sample tap on the backwash wastewater discharge line during the backwash of each tank and filtered
with 0.45-(im disc filters. Grab samples were analyzed for pH and total dissolved solids (TDS), and
filtered samples were analyzed for soluble As, Fe, and Mn. Beginning on November 14, 2005, composite
samples were collected following a modified procedure to allow for more representative characterization
of the wastewater. Connected to the tap on the discharge line, tubing directed a portion of backwash
water from the sample tap at approximately 1 gpm into a clean plastic container of adequate volume over
the duration of the backwash for each tank. After the content in the container was thoroughly mixed,
composite samples were collected and/or filtered onsite with 0.45-(im disc filters. Under this revised
procedure, total As, Fe, and Mn and total suspended solids (TSS) also were measured. Backwash water
sampling was conducted approximately monthly beginning in October 2004, quarterly beginning in
August 2005, and then discontinued after May 2006. Table 3-3 lists the schedule and analytes for the
backwash water samples.
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Table 3-3. Sample Collection Schedule and Analyses
Sample
Type
Source
Water
Treatment
Plant Water
Backwash
Water
Distribution
Water
Residual
Solids
Sample
Location(s)(a)
IN
IN, TA, and
TB
BW
DS (three non-
LCR homes)
Top, middle,
and bottom of
Tank A
No. of
Samples
1
3
2
o
J
o
J
Frequency
Once
Weekly (b)
Monthly(e)
Monthly®
Monthly(h)
Once
Analytes
Off-site: As (III), As(V), total
and soluble Al, As, Fe, and
Mn, Na, Ca, Mg, Cl, F, SO4,
SiO2, PO4, TOC, turbidity,
pH, and alkalinity
Onsite(c): pH, temperature,
DO, ORP, and C12 (free and
total)
Off-site: total As, Fe, and
Mn, SiO2, PO4(d), turbidity,
and alkalinity
Same as above plus the
following off-site: As(III),
As(V), soluble As, Fe, and
Mn, Ca, Mg, F, NO3, and
S04
Off-site: totalfe) and soluble
As, Fe, and Mn, pH, TDS,
TSS(g), and turbidity(g)
Off-site: total As, Fe, Mn,
Cu, and Pb, pH, alkalinity
Off-site: TCLP metals and
total Al, As, Ca, Cd, Cu, Fe,
Mg, Mn, Ni, P, Pb, Si, and
Zn
Collection
Date(s)
10/22/03
See Appendix B
See Appendix B
See Table 5-5
See Table 5-6
11/08/06
(a) Corresponding to sample locations in Figure 3-1, i.e., IN = at wellhead, TA = after Tank A; TB = after
Tank B; BW = at backwash water discharge line from Tanks A and B
(b) Three sets per four-week cycle from 07/07/04 to 10/27/04; three sets per eight-week cycle from 11/03/04 to
09/28/05 and 04/05/06 to 05/17/06; one set per four-week cycle from 11/09/05 to 01/04/06 and 06/14/06 to
08/09/06; and one set per four-week cycle from 11/28/06 to 02/02/07 for total As only.
(c) Performed for samples taken after prechlorination (AC), TA, and TB. Monthly from 04/05/06 to 08/09/06
and DO and ORP discontinued after 06/14/06.
(d) PO4 analysis replaced with total phosphorus analysis since 10/12/05.
(e) One set per eight-week cycle from 10/20/04 to 02/01/06 and 03/08/06 to 07/12/06, and then discontinued.
(f) Quarterly from 08/17/05 to 05/17/06 and then discontinued.
(g) Total As, Fe, and Mn, and TSS analyses performed and turbidity discontinued since 11/14/05.
(h) Four baseline events before system startup from 12/17/03 through 02/05/04. Discontinued after 10/12/05.
3.3.4 Distribution System 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, the arsenic, lead, and copper levels. From December 2003 to February 2004, four sets of
baseline distribution water samples were collected from three locations within the distribution system.
Following system startup, distribution system sampling continued on a monthly basis at the same
locations. Ideally, the sampling locations selected would have been the historical Lead and Copper Rule
(LCR) locations served primarily by the source water well, Well No. 2. However, because the
distribution system was supplied by Well No. 2 and five other wells, such LCR locations did not exist
(Section 4.1.2). Thus, three non-LCR residences supplied in part by Well No. 2 were monitored by the
distribution system sampling.
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INFLUENT
(WELL NO. 2)
RECYCLE PUMP
BAG FILTER
BACKWASH
RECYCLE TANK
(3,000 gal)
BAG FILTER
See Table 3-3 -* ---- LBw
STORAGE TANK
(200,000 gal)
See Table 3-3
DISTRIBUTION
SYSTEM
Footnote
(a) On-site analyses
Rimrock, AZ
AD-33™ Technology
Design Flow: 45 gpm
» See Table 3-3
pH^, temperatureW^O/ORPW,
chlorine1^)
See Table 3-3
See Table 3-3
LEGEND
At Wellhead
After Prechlorination
After Tank A
After Tank B
Backwash Sampling Location
Distribution Water Sampling
Locations
Chlorine Disinfection
Unit Process
Process Flow
Backwash Flow
Figure 3-1. Process Flow Diagram and Sampling Locations
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The samples were taken following an instruction sheet developed according to the Lead and Copper
Monitoring and Reporting Guidance for Public Water Systems (EPA, 2002). The homeowners recorded
the dates and times of last water usage before sampling and of sample collection for calculation of the
stagnation time. All samples were collected from a cold-water faucet that had not been used for at least
6 hr to ensure that stagnant water was sampled.
3.3.5 Residual Solids. Because of the very small quantity of solids in backwash wastewater, only
spent media was collected for residual solids analyses. A total of three spent media samples were
collected from top, middle, and bottom layers of the lead tank (i.e., Tank A) on November 8, 2006. Spent
media were sampled using a 5-gal wet/dry shop vacuum that had been thoroughly cleaned and disinfected
before sampling. The media collected from each target layer were transferred from the shop vacuum,
after mixing with a small garden spade, to a clean 5-gal bucket. A composite sample from each layer was
collected into a wide-mouth, 2-gal plastic container for total metal analyses and a Toxicity Characteristic
Leaching Procedure (TCLP) test. Metal analyses were conducted on air dried and acid digested samples
(see analytes in Table 3-3), and the TCLP test was conducted on an unprocessed sample following the
protocol described in the QAPP (Battelle, 2003).
3.4 Sampling Logistics
3.4.1 Preparation of Arsenic Speciation Kits. The arsenic field speciation method uses 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 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 needed. All sample
bottles were new and contained appropriate preservatives. Each sample bottle was affixed with a pre-
printed, colored-coded 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, the 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 (e.g.,
orange designated TA). The labeled bottles for each sampling location were bagged separately and
packed in the cooler.
In addition, all sampling- and shipping-related materials, such as disposable gloves, sampling instructions,
chain-of-custody forms, prepaid and addressed FedEx air bills, and bubble wrap, were included. The
chain-of-custody forms and FedEx air bills were complete except for the operator's signature and the
sample dates and times. After preparation, the sample cooler was 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 by Battelle's subcontract laboratories,
including American Analytical Laboratories (AAL) in Columbus, OH and TCCI Laboratories in New
-------
Lexington, OH, were packed in coolers at Battelle and picked up by couriers. 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 QAPP (Battelle, 2003) were followed by
Battelle ICP-MS Laboratory, AAL, 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% 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
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 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.
10
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4.1
4.0 DEMONSTRATION SITE AND TECHNOLOGY EVALUATED
Site Description
4.1.1 Existing Facility. Seven wells owned by AWC supplied water to a population of 2,556 in
Rimrock, AZ. Montezuma Haven Wells No. 1 and 2, with a combined capacity of 90 gpm, were selected
for the demonstration study. Figure 4-1 shows photographs taken at the site prior to onset of the
demonstration study.
Wells No. 1 and 2 were 6-in in diameter and 270- and 165-ft deep, respectively, both with an open
borehole extending from 80 ft below ground surface (bgs). The main supply well, Well No. 3, was 1,000-
ft deep and capable of producing a sustainable flow at 315 gpm. Before entering the distribution system,
a 12% NaOCl solution was used to maintain a free chlorine residual of about 0.3 mg/L (as C12).
From Summer 2003 to October 2003, Wells No. 1 and 2 were taken off-line for repairs and
redevelopment. It was later discovered that Well No. 1 had become dry, and that Well No. 2 produced a
sustainable flow of only 31 gpm. This finding prompted a change to the configuration of the two
adsorption tanks of the proposed treatment system from parallel to series (Section 4.2). For the purpose
of the demonstration study, Well No. 2 was operated for 12 hr/day during most of the 33-month study
period.
iran
Figure 4-1. Predemonstration Site Photographs
(Clockwise from Top: Condition in July 2003; Well No. 2 Wellhead after
Redevelopment; and Chlorine Shed and Emergency Shower Station)
4.1.2 Distribution System. The distribution system was supplied by Montezuma Haven Wells
No. 2 and 3, and four other production wells not including Well No. 1, which was out of service. The
transmission main was constructed of 6-in-diameter asbestos cement piping. Service lines to the
11
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individual homes were mostly black high-density polyethylene (HDPE) or polyvinyl chloride (PVC)
piping (including the distribution sampling locations) with some homes having copper or galvanized steel
piping. Well No. 2 water entered the distribution system and blended with Well No. 3 water at the fence
line of the treatment plant. Additional blending with water from other supply wells occurred further
downstream. The blended water was stored in a 200,000-gal tank.
Compliance samples are taken periodically by AWC from the distribution system. Every month, three
samples are collected for bacteria analysis. Under the LCR, samples are collected from customer taps at
14 locations every three years. The monitoring results from AWC's Consumer Confidence Reports
(CCRs) for 2003 to 2005 (AWC, 2004; 2005; 2006) are summarized in Table 4-1.
Table 4-1. Distribution System Water Quality Data
Collected by AWC(a)
Parameter
Alpha Emitters
Arsenic
Barium
Chlorine
Chromium
Copper
Fluoride
Lead
Nitrate (as N)
Selenium
Sodium
Radium-226
Radon(c)
Total Trihalomethanes
Uranium
Unit
pCi/L
Hg/L
mg/L
mg/L
Hg/L
mg/L
mg/L
Hg/L
mg/L
Hg/L
mg/L
pCi/L
pCi/L
Hg/L
Hg/L
2003
ND-3.5
20-54
0.3-0.4
—
11-15
0.4(b)
0.2-0.4
—
ND-0.9
3.2-4.2
38^5
ND-0.2
60
—
1.3-4.5
2004
2.0-7.8
ND-51
—
—
—
—
—
—
ND-1
—
—
—
—
ND-2.5
-
2005
—
ND-48
—
0.3-0.6
—
0.3
—
13
ND-0.6
—
—
—
—
—
-
(a) All other constituents not detected.
(b) Sampled in 2002.
(c) Sampled in 1999.
ND = not detected
4.1.3 Source Water Quality. Samples of Well No. 2 water were collected on October 22, 2003,
for analyses. The results, along with those provided by the facility to EPA for demonstration site
selection and those independently collected and analyzed by EPA, are presented in Table 4-2.
Based on the October 22, 2003, sampling results, Well No. 2 contained 63.6 (ig/L of arsenic existing
solely as As(V). Because As(V) adsorbs better with AD-33™ media, prechlorination upstream of the
treatment process was not required. The source water pH value was 7.1, which was preferred for
effective arsenic adsorption by AD-33™ media. In general, pH values at the lower end of the 6.5 to 8.5
range are preferred.
The adsorption capacity of AD-33™ media can be impacted by high levels of competing ions such as
silica, phosphate, and sulfate. Concentrations of these ions appeared to be low enough not to affect the
media's adsorptive capacity for arsenic. The iron and manganese concentrations (36 and 7.5 (ig/L,
respectively) in Well No. 2 water were sufficiently low; therefore, pretreatment for these metals prior to
adsorption was not required.
12
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Table 4-2. Source Water Quality Data
Parameter
Sampling Date
PH
Alkalinity (as CaCO3)
Hardness (as CaCO3)
Chloride
Fluoride
Nitrate (as N)
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)
Na (total)
Ca (total)
Mg (total)
Unit
-
-
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
HB/L
W?/L
HB/L
W?/L
HB/L
^g/L
W?/L
HB/L
W?/L
HB/L
W?/L
Mg/L
Mg/L
Mg/L
Wells No. 1 & 2
AWC Data(a)
Not specified
7.2
334
300
25.0
NS
NS
13.0
27.8
<0.065(b)
NS
50.0
NS
NS
NS
NS
170(b)
NS
NS
NS
NS
NS
35.0
69.0
31.0
Well No. 3
AWC Data
12/30/02
7.6
444
NS
NS
0.2
0.1
12.2
NS
NS
NS
15.0
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
93
NS
NS
Wells No. 1 & 2
EPA Data
10/03/02
NS
374
330
30.8
NS
NS
11.6
26.3
O.065
NS
52.0
NS
NS
NS
NS
170
NS
<25
NS
<0.4
NS
41.6
80.2
31.6
Well No. 2
Battelle Data
10/22/03
7.1
378
335
32.0
0.5
NS
9.5
24.8
O.10
3.4(c)
63.6
64.8
O.10
0.10
64.8
36
<25
13
<10
7.5
8.1
40.3
82.8
31.0
(a) Provided to EPA for site selection.
(b) Provided by EPA.
(c) Datum questionable.
TOC = total organic carbon; NS = not sampled
4.2
Treatment Process Description
AdEdge's APU-100 system is a fixed-bed downflow adsorption system, which uses Bay oxide® E33-S
granular ferric oxide (GFO) adsorptive media for arsenic removal from drinking water supplies.
Developed by Bayer AG, the media is branded and referred to as AD-33™ by AdEdge. AD-33™ is
delivered in a dry crystalline form and has received NSF International (NSF) approval for use in drinking
water under NSF Standard 61. Table 4-3 presents key physical and chemical properties of the media as
provided by the vendor.
The original design of the APU-100 system was for the two adsorption tanks to operate in parallel to treat
an anticipated flowrate of 90 gpm. However, because Well No. 1 was no longer producing water, the
tanks were reconfigured to operate in series for a design capacity of 45 gpm.
For series operation, the media in the lead tank is generally replaced when it completely exhausts its
capacity or when the effluent from the lag tank reaches 10 |o,g/L of arsenic. After rebedding, the lead tank
with new media, it is switched to the lag position, and the lag tank with the partially exhausted media is
13
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Table 4-3. Physical and Chemical Properties of AD-33™ Media
Physical Properties
Parameter
Matrix
Physical Form
Color
Bulk Density (g/cm3) [lb/ft3]
BET Surface Area (m2/g)
Attrition (%)
Moisture Content (%)
Particle Size Distribution
Crystal Size (A)
Crystal Phase
Value
Iron oxide composite
Dry granular media
Amber
0.45 [28.1]
142
0.3
<15 (by weight)
10 x 35 mesh
70
a -FeOOH
Chemical Analysis
Constituents
FeOOH
CaO
MgO
MnO
S03
Na2O
TiO2
Si02
A12O3
P205
Cl
Weight (%)
90.1
0.27
1.00
0.11
0.13
0.12
0.11
0.06
0.05
0.02
0.01
Source: Bayer AG
BET = Brunauer, Emmett, and Teller
switched to the lead position. In theory, the series operation better utilizes the arsenic removal capacity of
the media when compared to parallel system design and operation.
The APU-100 system included a bag filter assembly for sediment removal from source water, two
pressure tanks arranged in series with hub and lateral underdrains, a backwash recycle system, piping
with an automated valve assembly, and an instrument/control panel with flow meters, pressure and
differential pressure (Ap) gauges, and ball valve sample ports. Skid-mounted on a polyurethane coated,
welded steel frame, the system was equipped with the necessary valves and schedule 80 PVC piping to
allow the adsorption tanks to be switched from lead to lag position and vice versa. Figure 4-2 is a
simplified piping and instrumentation diagram (P&ID) of the treatment system. The system's design
features are summarized in Table 4-4. Figures 4-3 and 4-4 show integral components of the treatment and
backwash recycle processes, respectively. The major process steps included:
• Intake. Source water was supplied by Montezuma Haven Well No. 2 at approximately 31
gpm (Item No. 5 in Figure 4-3).
• Prechlorination. Although not required for oxidation, a 12% NaOCl solution was injected
into raw water prior to the adsorption tanks at AWC's discretion and expense to attain a
target free chlorine residual of 0.3 mg/L (as C12) in the treated water. The feed system
consisted of a 1.5-gal/hr (gph) chemical metering pump with adjustable speed and stroke
settings and a 30-gal day tank. The metering pump was interlocked with the well pump so
14
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that both pumps operated at the same time.
shower station for safety measures.
AWC also provided an emergency eyewash and
• Bag Filter Filtration. After prechlorination, a 25-jam bag filter assembly (FSI model
BFN12) with replaceable polypropylene filter bags was used to remove any sediment from
source water to protect the treatment equipment (Item No. 1 in Figure 4-3).
• Adsorption. The two 3-ft x 6-ft pressure tanks (Structural model 31214) were configured in
series, each containing 22 ft3 of AD-33™ media supported by 4.5 ft3 of gravel underbedding.
Although 27 ft3 of media was originally proposed per tank, less media was loaded to provide
additional freeboard during backwash. The tanks were constructed of composite fiberglass
and rated for a 150-pounds per square inch (psi) working pressure (Item No. 3 in Figure 4-3 ).
Influent, effluent, and backwash piping were connected to a Fleck controller valve
(Performance Water Products model 3150 Downflow) at the 6-in flanged connection on the
top of each tank (Item 2 in Figure 4-3). The influent water entered the tank via the controller
valve, flowed downward through the media bed, collected in the underdrain, and traveled
upward through riser piping to the outlet of the controller valve. A restrictive orifice located
on the effluent piping from each tank provided a safeguard against filter overrun. Based on
22 ft3 of media and 45 gpm of design flowrate, the EBCT through each media bed would be
3.7 min and the hydraulic loading rate would be 6.4 gpm/ft2. Based on the actual flowrate of
30 gpm, the EBCT in each tank was 5.4 min and the hydraulic loading rate was 4.2 gpm/ft2.
Figure 4-2. Schematic of AdEdge's APU-100 Treatment System
Backwash. Backwash was recommended by the vendor to remove participates and/or media
fines accumulating in the media beds. The process might be initiated either manually or
automatically based on a timer (Pentair model 3200NT) or a Ap setting for each tank. After
the system was taken offline, upflow backwash using chlorinated water from the well was
performed on Tank A followed by Tank B.
15
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Backwash Wastewater Recycling. Due to lack of sewer or other onsite wastewater
discharge options, a backwash recycle loop was included in the system to reclaim the
wastewater. The recycling system consisted of a 25-jam bag filter (FSI model BFN12), a
3,000-gal, flat-bottom, HDPE recycle tank with high and low level sensors (Burkert type
8181), and a positive displacement metering pump (ProMinent® Sigma/2 S2BA/S2Ca)
(Figure 4-4). A turbine flow meter and a totalizer also were included to monitor flow.
Wastewater from the recycle tank was metered into the head of the system between the
chlorine injection point and the bag filter assembly at a rate of 0.5 gpm. Relays from the
level sensors in the storage tank prevented the tank from overflowing and enabled automatic
recycling.
Table 4-4. Design Features for AdEdge's APU-100 Treatment System
Parameter
Value(a)
Remarks
Pretreatment
12%NaOCl(mg/L)
Bag Filter (|am)
Not required
25
For providing residuals in
distribution system
For sediment removal
Adsorption
Tank Quantity
Tank Size (ft)
AD-33™ Media Volume (ftVtank)
Underbedding Volume (ftVtank)
Maximum Flowrate (gpm)
Design Flowrate (gpm)
EBCT (min/tank)
Water Production (gpd)
Hydraulic Utilization (%)
Water Production (BV/tank/day)
Media Capacity to 10-|ag/L As Break-
through from Lead Tank (BV)
Estimated throughput to 10 ng/L
As breakthrough from Lead Tank (gal)
Estimated Media Life (month)
2
3D x6H
22
4.5
50
45
3.7
32,400
50
197
66,000
10,860,000
11
Series configuration
7.1 ft2 cross-sectional area
27 ftVtank per original design
Gravel
3 1 gpm typically expected
Based on design flowrate
Based on 45 gpm design flowrate
and 12 hr/day operation
12 hr/day operation
Based on 22 ftVtank media
volume, 45 gpm design flowrate,
and 12 hr/day operation
1 BV = 22 ft3
1 BV = 22 ft3 = 165 gal
Based on media capacity and
utilization
Backwash
Frequency (time/month)
Flowrate (gpm)
Hydraulic Loading Rate (gpm/ft2)
Duration (min/tank)
Wastewater Production (gal/tank)
Recycle Flowrate (gpm)
1
50
7
15
750
0.5
D = diameter; H = height
(a) AdEdge's original design modified from parallel to series reconfiguration.
16
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Figure 4-3. Treatment System Components
([1] Inlet Bag Filter, [2] Fleck Controller Valve, [3] Adsorption Tank;
[4] Instrument/Control Panel; [5] Piping from Wellhead, [6] Piping to
Distribution System, and [7] System Enclosure)
Figure 4-4. Backwash Recycling System Components
(From Left: Backwash Bag Filter; 3,000-gal Storage Tank with Level
Sensors; and Recycle Pump)
17
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4.3
Treatment System Installation
This section summarizes the system engineering, installation, startup, and shakedown activities, which
were carried out by AdEdge and its subcontractor, Fann Environmental, of Prescott, AZ. Installation of
the system was completed in mid-April 2004 and reconfiguration of the system from parallel to series was
completed in mid-May 2004.
4.3.1 System Engineering and Permitting. Engineering plans for the system permit application
were submitted to ADEQ for approval on December 11, 2003. The plans included P&IDs and system
specifications, control panel schematics, equipment cut sheets, and drawings of a site plan, treatment plan,
and piping plan. After the Approval to Construct was granted on February 18, 2004, a construction
permit was applied for and approved by Yavapai County in mid-March 2004. Upon completion of
system installation, as-built drawings were submitted to ADEQ and Approval of Construction was
granted on April 29, 2004. Following the system reconfiguration, updated information was submitted to
ADEQ and a second approval was granted on June 15, 2004.
4.3.2 System Installation, Startup, and Shakedown. Upon arrival of the treatment system on
March 30, 2004, the vendor's subcontractor performed off-loading and installation. The installation
activities including connections to the existing intake and distribution piping, hydraulic testing (with no
media), and media loading were completed on April 20, 2004. Figure 4-5 shows photographs from the
media loading. Due to the loss of Well No. 1, piping from Well No. 3 was installed to allow additional
flow for media backwash. Because some lubricating oil from the pump shaft was found in Well No. 3
water, a decision was made to forgo this supplementary input for backwash. Battelle provided operator
training on data and sample collection from May 6 to 7, 2004.
Figure 4-5. Gravel Underbedding (Left) and AD-33™ Media (Right) Loading
Because of the reduced flowrate from 90 to 31 gpm, the corresponding EBCT across each tank would
have almost tripled from 3.7 to 10.6 min (based on 22 ft3 of media loaded in each tank) if the system
configuration had remained in parallel. To evaluate the system performance near the originally designed
EBCT and to fully utilize the media capacity, the tank configuration was changed to series. The required
modifications were made in mid-May 2004, and shakedown and startup completed in early June 2004.
After the system was sanitized and passed bacteria tests, the performance evaluation began with
commencement of Media Run 1A on June 24, 2004.
18
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4.3.3 System Enclosure. After the treatment system was installed, a sun shed with a base of
12 ft x 15 ft and a height of 9.5 ft was built by AWC over the system in late-May 2004 (Figure 4-6).
Constructed of a galvanized steel frame by Versa-Tube, the sun shed was anchored to the concrete pad
and sheeted with 29-gauge steel with a specially coated surface. The shed was pre-engineered with
loading capacities of 90 mph for wind and 30 lb/ft2 for snow. From late-November to mid-December
2004, the sides and ends of the sun shed were enclosed with metal covering; exposed piping was
insulated; and heat lamps were installed within the building for added protection from below-freezing
temperatures.
Figure 4-6. System Enclosure
(Clockwise from Left: System Installed on Concrete Pad in April 2004;
Sun Shed Built in May 2004; and Enclosure Completed in December 2004)
19
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5.0 RESULTS AND DISCUSSION
5.1
System Operation
5.1.1 Service Operation. The operational data collected during the performance evaluation study
are tabulated and attached as Appendix A. Key parameters are summarized in Table 5-1. The system
operated with Tank A in the lead position from June 24, 2004, through August 9, 2006 (designated as
Run 1A). Starting from August 30, 2006, the system was turned off for well pump maintenance and Tank
A rebedding (Section 5.1.3). System operation resumed for Run IB on November 27, 2006, with Tank B
containing partially exhausted media in the lead position and newly-rebedded Tank A in the lag position.
Sampling was discontinued and the performance evaluation completed on March 28, 2007 after the
results of monitoring confirmed on-spec system operation following the media changeout.
From June 24, 2004 through March 28, 2007, the system operated for a total of 12,024 hr on a 12-hr/day
schedule from 8:00 a.m. to 8:00 p.m., except for the winters when the system operated at night from
11:00 p.m. to 11:00 a.m. to prevent system components from being damaged due to freezing ambient
conditions, and from December 4, 2006, to March 7, 2007, when the system operated 24 hr/day to
compensate for anticipated water shortage due to maintenance on a nearby well. The 12 hr/day run time
was preset on a timer. Meanwhile, an hour meter was installed on November 4, 2004 to track total system
runtime.
Table 5-1. Summary of APU-100 System Operations
Parameter
Evaluation Period
Unit
Date
Value
06/24/04-03/28/07(a)
Treatment Operation
Total Operation Time
Daily Operating Time
Average Flowrate [Range]
Average Hydraulic Loading Rate [Range]
Average EBCT [Range]
Average Ap across Tank [Range]
Media Run Length to 10-|ag/L As following Lead Tank
Media Run Length to 10-|ag/L As following Lag Tank
Media Run Length until Tank A Rebedding
Media Run Length after Tank A Rebedding
hr
hr/day
gpm
gpm/ft2
min/tank
psi/tank
1,000 gal/BV/yr
1,000 gal/BV/yr
1,000 gal/BV/yr
1,000 gal/BV/yr
12,024
12 or 24
30 [16-36]
4.2 [2.3-5.1]
5.4 [4.6-10.3]
4.8 [1.5-6.5]
e^s^iso^/o.s
17,164/52,150(c)/2.1
17,426/52,950(c)/2.2
4,717/14,330(c)/0.3
Backwash Operation
Backwash Count
Time Elapsed between Two Consecutive Backwash Cycles
Average Flowrate [Range]
Average Hydraulic Loading Rate [Range]
Average Backwash Duration [Range]
Wastewater Generated
Total Wastewater Generated
Average Recycle Flowrate [Range]
No
Month
gpm
gpm/ft2
min/tank
gal/tank
gal
gpm
42(d)
1-3
47 [22-54]
6.6 [3.1-7.6]
15 [15-17]
727 [245-996]
33,100
0.5 [0.5-1.5]
(a) System turned off on 08/30/06 and restarted on 11/27/06 after rebedding.
(b) Based on flow meter of lead tank and volume of media in lead tank.
(c) Based on flow meter of lag tank and volume of media in both tanks.
(d) Count for both tanks combined.
20
-------
During Run 1A, the system produced 6,448,000 gal (or 39,180 BV [1 BV = 22 ft3]) and 17,164,000 gal
(or 52,150 BV [1 BV = 44 ft3]) of water at 10 (ig/L of arsenic breakthrough from the lead and lag tanks,
respectively. After media changeout, an additional 4,717,000 gal (or 14,330 BV [1 BV = 44 ft3]) was
produced before sampling was discontinued. System flowrates ranged from 16 to 36 gpm and averaged
30 gpm and the corresponding hydraulic loading rates ranged from 2.3 to 5.1 gpm/ft2 and averaged 4.2
gpm/ft2. Flowrates as low as 16 gpm were measured when decreasing production by Well No. 2 was
observed from June through August 2006 (Figure 5-1). Following the well maintenance, system
flowrates returned to the typical values of around 30 gpm. The resulting EBCTs ranged from 4.6 to 10.3
min/tank and averaged 5.4 min/tank, compared to the design value of 3.7 min/tank (note that the design
EBCT was calculated based on 22 ft3 of media in each tank and 45 gpm of system flowrate).
Ap readings across each tank ranged from 1.5 to 6.5 psi and averaged 4.8 psi (Figure 5-1). As expected,
Ap readings across each tank decreased with decreasing flowrates. Ap readings across Tank A were
generally higher (i.e., about 0.5 psi) than those across Tank B, suggesting removal of some sediment by
Tank A (the lead tank). During system startup, hydraulic testing performed with no media in the tanks
measured a Ap reading of 4.3 psi at 33 gpm. This Ap was thought to have been caused primarily by the
Fleck controller valve installed at the top of each tank, as demonstrated by the hydraulic testing
performed on another APU-100 system at Rollinsford, NH (Oxenham et al., 2005). The Ap readings
across each tank between two consecutive backwash events did not increase significantly, indicating that
few particulates or media fines, if any, were accumulating in the media beds.
40
+ ft+ *iLx x "*" x m- flBF xx
5 --
Tank B Flowrate
x TankAAp
+ Tank B Ap
/
& &
&
/ / 4
Figure 5-1. Flowrate Readings and Ap Across Tanks
/ / /
5.1.2 Backwash Operation. The system was programmed to backwash automatically at 15 psi of
Ap or 27 (for Tank A) or 28 (for Tank B) days of system operation. For the first one and a half months of
operation, the system experienced four unscheduled backwash events, possibly caused by >15 psi pressure
spikes resulting from the operation of the nearby Well No. 3. Because these backwash events took place
unexpectedly, the operator was not onsite to record relevant operational data and take samples. In order
to record backwash data and collect backwash wastewater samples, the Ap relays were disengaged on
21
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August 12, 2004, so that backwash would be controlled solely by the 27/28-day timer. Since then, three
more unscheduled backwash events occurred before the first set of samples could be taken on October 20,
2004, when the tanks were manually backwashed. After another backwash event was missed on
November 15, 2004, the 27/28-day timer setting was changed to 30 days. After November 15, 2004, no
other unscheduled backwashes occurred except on December 6, 2005, possibly due to a power outage.
The vendor checked the backwash settings, tested the process, and ensured normal operation on
December 14,2005.
Backwash was performed with raw water at 47 gpm or 6.6 gpm/ft2 (on average). Initially, a monthly
backwash was performed as recommended by the vendor. After approximately one year of system
operation, the backwash frequency was reduced to quarterly in August 2005. The decrease in backwash
frequency was determined mainly by the minimal Ap increase across the tanks between two consecutive
backwash events. The backwash duration was generally 15 min/tank, producing approximately 730
gal/tank. However, flows as low as 22 gpm or 3.1 gpm/ft2 were used for backwash on August 16, 2006,
due to decreasing well production. Nonetheless, Ap increase following the backwash was not observed.
After media changeout, the system was thoroughly backwashed with anticipated flowrates following the
well maintenance.
Several problems occurred with the backwash recycle pump and a control valve. In mid-August 2004,
after a leak on the backwash recycle line was repaired, the shut-off valve from the backwash recycle
pump was inadvertently left unopened. Consequently, when the recycle pump came on during a
backwash on August 23, 2004, it was dead-headed, causing damages to the diaphragm. The recycle pump
was fixed on September 1, 2004, and a pressure relief valve was installed on the pump discharge to
prevent future problems. A control valve for Tank A began sticking after backwash on June 8, 2005,
causing the tank not to return to service mode after backwash. The valve was repaired by the vendor on
July 26, 2005. Additional problems were experienced with the backwash recycle pump after the media
changeout on November 27, 2006. The system stopped recognizing the programmable logic controller
(PLC) input signal from the level sensor in the recycle tank used to operate the recycle pump. Due to
scheduling conflicts and troubleshooting difficulties, this issue was not resolved by the vendor until
March 28, 2007.
5.1.3 Media Changeout. A media changeout request was made to the vendor and its subcontractor
on August 16, 2006. Due to scheduling conflicts and media disposal and other issues, the changeout did
not take place until almost three months later on November 8, 2006. After the tanks were drained and the
pumps and isolation valves were turned off, the freeboards of Tanks A and B were measured at 17.3 and
19.0 in, respectively, from the flange at the top of each tank to the top of each media bed. The spent
media and underbedding in Tank A were sampled and/or removed as described in Section 3.3.5. The tank
was then half-filled with water before loading of 4.5 ft3 of underbedding gravel and 22 ft3 of virgin media
through a large funnel. The tank was then completely filled with water and the media soaked to eliminate
entrapped air. After the media was thoroughly backwashed, the freeboard of the tank was measured at
16.5 in, which was comparable to the 17.3-in measurement before rebedding. It appeared that minimum
media loss was experienced over the 2.1 yr of system operation.
5.1.4 Residual Management. The backwash wastewater recycling system (Section 4.2) reclaimed
nearly 100% of the backwash wastewater produced. Recycling was accomplished by blending the
supernatant in the recycle tank with the influent water between the chlorine injection point and bag filter
at a rate of 0.5 gpm (see Figure 3.1). Solids and media fines produced during backwash were removed by
a 25 (im bag filter, which required replacement after each backwash. Any remaining solids not removed
by the bag filter were allowed to settle in the recycle tank; accumulation was so negligible that removal
and disposal of these solid were not needed during the course of the 33-month study period. If required,
solid removal from the recycle tank would be a considerable undertaking because the flat-bottom is not
22
-------
conducive to solid collection, and because the only access point to solid is at the top of the approximately
8-ft tall tank. The associated O&M requirements for sites with higher solid loading could easily be
accommodated by using a conical-bottom recycle tank.
Spent media was the only quantifiable residual produced by operation of the treatment system. After
treating 17,500,000 gal of water in 2.2 yr, approximately 620 Ib of spent media and 450 Ib of gravel
underbedding were removed from the lead tank. After they were subjected to and passed the TCLP test
(Section 5.2.4), the media were disposed of by Waste Management, Inc.
5.1.5 System/Operation Reliability and Simplicity. Unscheduled backwashes, problems with the
recycling pump and one control valve (Section 5.1.2), and delays on media changeout (Section 5.1.3)
were the primary source of concerns during this performance evaluation study. Other O&M issues
encountered were problems with the chlorine injector, inlet and outlet pressure gauges, recycle flow
meter, and backwash totalizer. The pressure gauges, flow meter, and totalizer were damaged as a result
of unusually cold weather in late November 2004. The inlet and outlet pressure gauges broke a second
time on December 19, 2005. The unscheduled downtime for system component repairs amounted to
about 1 to 2% of the total system run time.
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.
5.1.5.1 Pre- and Post-Treatment Requirements. Although not required for treatment, chlorine was
injected upstream of the adsorption tanks to provide disinfection throughout the treatment train and a
chlorine residual within the distribution system. A 25-|o,m bag filter following the chlorine injection point
was used to remove sediment from the inlet water. No post-treatments were required.
5.1.5.2 System Automation. The system was equipped with a backwash control to initiate backwash
automatically by a timer and/or a Ap setpoint. Because the system experienced a number of unscheduled
backwashes at the beginning of system operation (Section 5.1.2), the automatic backwash control was
disabled so that the operator could take backwash data and samples during each manual backwash.
Backwash wastewater recycling also was accomplished automatically as operation of the recycle pump
was controlled by the level sensors in the reclaim tank.
5.1.5.3 Operator Skill Requirements. Under normal operating conditions, the daily demand on the
operator was typically 20 min for visual inspection of the system and recording of operational parameters
on the log sheets. During backwash, the operator spent approximately 2 hr onsite to collect operational
data and perform backwash wastewater sampling. Under normal system operation, backwash can be
initiated automatically, as such, the operator's presence would not be necessary.
In Arizona, operator certifications are classified by grade on a scale of 1 (least complex) to 4 (most
complex) according to facility type, size, complexity, and population served (ADEQ, 2005). One AWC
operator had a Level 4 Distribution Grade and a Level 4 Treatment Grade, and the other had a Level 4
Distribution Grade and a Level 3 Treatment Grade. After receiving proper training by the vendor during
the system startup, the operator understood the system and was able to work with the vendor to
troubleshoot and perform minor onsite repairs.
5.1.5.4 Preventative Maintenance Activities. Preventative maintenance tasks recommended by the
vendor are summarized in Table 5-2. The system had few moving parts that required regular maintenance
per the O&M manual. Replacement bag filters were installed without the use of special equipment. With
vendor's concurrence, the frequency for backwash and bag filter replacement was reduced from monthly
23
-------
to quarterly or upon 6 to 7 psi Ap rise (Section 5.1.2). Many of the tasks such as sampling and analysis
and operational data recording including pressure checks were conducted more frequently due to the
nature of the demonstration project.
Because the backwash bag filter assembly was located before the recycle tank, bag filters had to be
replaced after each backwash event. If the backwash bag filter had been located after the recycle tank, its
replacement frequency could be reduced by allowing solids to settle in the recycle tank. To have the bag
filter after the recycle tank, however, could increase the need for solids removal from the recycle tank.
Table 5-2. Recommended Routine Maintenance Activities
Task
Ensure Normal System Operation
Check Site Security
Check for Leaks and Integrity
Read Inlet/Outlet Pressure and Ap Gauges
Check Backwash Recycle Tank Level
Record Totalizer Throughput
Record System Flowrate
Check Effluent Water Clarity
Backwash and Replace Backwash Bag Filter
Check Inlet Bag Filter for Debris/Sediment
Conduct Sampling and Analysis(c)
Perform Equipment Maintenance
Frequency
Daily
A/
V
Weekly
V
V
V
Monthly
V
V
V
V(a)
V
Quarterly
V(b)
V
V
A/
Source: AdEdge, 2004
(a) At beginning of system operation.
(b) or 6 to 7 psi Ap.
(c) Frequency depending on anticipated proximity to arsenic breakthrough.
(d) Per O&M manual.
5.1.5.5 Chemical/Media Handling and Inventory Requirements. Chemical usage was not required
except for disinfection. AWC coordinated the supply of 12% NaOCl supply with Hill Brothers Chemical
Co., refilled the day tank when required, and provided an emergency eyewash and shower station for
safety measures. Rebedding of the lead tank was required when the lag tank effluent reached 10-|o,g/L of
arsenic after 2.1 yr of system operation or 17,146,000 gal of water treated. Media sampling and removal
were labor-intensive, taking 45 labor hr (i.e., 15 hr each for three people). In contrast, media loading took
only 9 labor hr (3 hr each for three people).
5.2 System Performance
5.2.1 Treatment Plant Sampling. The treatment plant water was sampled on 64 occasions
(including five duplicate samples), with field speciation performed on 16 occations. Table 5-3
summarizes the analytical results of arsenic, iron, and manganese at the IN, TA, and TB sampling
locations. Table 5-4 summarizes the results of the other water quality parameters including those
measured onsite at the IN, AC, TA, and TB sampling locations. Appendix B contains a complete set of
analytical results.
24
-------
Table 5-3. Summary of Arsenic, Iron, and Manganese Results
Parameter
(Figure, if any)
As (total) (Figure 5-3)
As (soluble)
As (paniculate)
(Figure 5-2)
As(III)
(Figure 5-2)
As(V) (Figure 5-2)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Sampling
Location
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
Sample
Count
64
64
64
16
16
16
16
16
16
16
16
16
16
16
16
59(a)
60
60
16
16
16
60
60
59(b)
16
16
16
Concentration (ng/L)
Minimum
43.8
0.7
0.2
50.2
0.9
0.3
0.1
0.1
0.1
0.3
0.3
0.2
48.1
0.1
0.1
<25
<25
<25
<25
<25
<25
0.1
0.1
0.1
0.1
0.1
0.1
Maximum
81.4
56.1
31.7
66.7
41.9
7.3
21.7
15.2
1.1
2.2
2.7
1.9
65.5
41.7
7.0
27.2
31.1
55.7
<25
<25
<25
1.6
1.2
0.9
1.1
0.7
0.6
Average
59.7
-
-
57.3
-
-
3.8
3.0
0.3
1.1
1.0
0.8
56.2
-
-
<25
<25
<25
<25
<25
<25
0.3
0.1
0.1
0.3
0.1
0.1
Standard
Deviation
9.5
-
-
5.1
-
-
6.4
4.7
0.3
0.5
0.6
0.5
5.1
-
-
1.9
3.5
7.7
-
-
-
0.3
0.2
0.2
0.3
0.2
0.1
(a) One outlier (i.e., 127 ug/L on 09/22/04) omitted.
(b) One outlier (i.e., 12.4 ug/L on 02/02/05) omitted.
One-half of the detection limit used for nondetect results and duplicates included for calculations.
5.2.1.1 Arsenic. Total arsenic concentrations in source water ranged from 43.8 to 81.4 |o,g/L and
averaged 59.7 |o,g/L, with As(V) as the predominant soluble species at 56.2 |o,g/L (Table 5-3). Figure 5-2
contains bar charts showing the concentrations of particulate arsenic, As(III), and As(V) for each
speciation sampling event. (Note that results for TA and TB in Figure 5-2 were plotted on reduced scales
compared to IN to better show the effluent species.) The arsenic concentrations measured during this
period were consistent with that of source water collected on October 22, 2003 (Table 4-2). Generally,
low levels of particulate arsenic and As(III) existed in raw water at average concentrations of 3.8 and 1.1
Hg/L, respectively. However, highly elevated particulate arsenic concentrations (e.g., up to 21.7 |o,g/L on
March 8, 2006) were observed beginning in February 2006, possibly due to overextraction from the
source well. Most of particulate arsenic was trapped in the media beds (and later removed during
backwash) as evident by the decrease in concentrations from 3.8 to 3.0 and then to 0.3 |o,g/L at IN, TA,
and TB, respectively. As much as 2.2 |o,g/L As(III) was measured in source water and not completely
oxidized with chlorine addition. Because the AD-33™ media had little capacity for As(III), up to 2.7 and
1.9 |o,g/L of As(III) were measured in the tank effluent even in the presence of 0.3 mg/L (as C12) of free
chlorine (Table 5-3).
25
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Table 5-4. Summary of Other Water Quality Parameter Results
Parameter
(Figure, if any)
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Orthophosphate
(asP)
Phosphorus
(asP)
Silica
(as SiO2)
Nitrate
(asN)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
(as C12)
Total Chlorine
(as C12)
Total Hardness
(as CaCO3)
Sampling
Location
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
AC
TA
TB
IN
AC
TA
TB
IN
AC
TA
TB
IN
AC
TA
TB
AC
TA
TB
AC
TA
TB
IN
TA
TB
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
HB/L
^g/L
HB/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
s.u.
s.u.
s.u.
s.u.
°c
°c
°c
°c
mg/L
mg/L
mg/L
mg/L
mV
mV
mV
mV
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
Sample
Count
60
60
60
16
16
16
16
16
16
ll(a)
ll(a)
ll(a)
14
14
14
60
60
60
16
16
16
60
60
60
50
50
50
50
51
51
51
51
48
48
48
48
48
48
48
48
51
51
51
50
50
50
16
16
16
Concentration
Minimum
330
345
351
0.2
0.2
0.2
8.1
7.8
8.1
<0.06
O.06
<0.06
<10
<10
<10
23.6
23.9
23.7
0.2
0.2
0.2
0.1
0.1
0.1
6.8
6.8
6.7
6.8
18.6
19.2
19.4
19.6
3.2
3.0
3.0
3.0
148
365
565
470
0.2
0.2
0.2
0.2
0.2
0.2
287
298
298
Maximum
414
424
410
0.4
0.5
0.4
11
10
11
O.10
O.10
O.10
20.4
21.4
10.9
27.6
27.5
27.4
0.6
0.3
0.3
0.7
1.6
3.4
7.1
7.6
7.1
7.1
26.1
24.5
26.7
24.0
6.0
6.8
6.6
6.9
510
646
688
710
0.5
0.5
0.5
0.7
0.6
0.6
384
397
377
Average
379
380
381
0.3
0.3
0.3
9.7
9.6
9.7
O.06
<0.06
O.06
10.2
11.7
<10
25.6
25.5
25.4
0.2
0.2
0.2
0.2
0.3
0.3
6.9
7.0
7.0
6.9
21.0
20.8
20.9
21.0
3.9
4.2
3.9
3.9
305
597
630
639
0.4
0.3
0.3
0.4
0.4
0.4
327
334
331
Standard
Deviation
14
12
13
0.1
0.1
0.1
0.6
0.6
0.7
0.0
0.0
0.0
5.8
5.9
2.1
0.8
0.9
0.9
0.1
0.0
0.0
0.2
0.3
0.5
0.1
0.2
0.1
0.1
1.3
1.0
1.2
1.1
0.5
0.9
0.6
0.6
125
46
29
39
0.1
0.1
0.1
0.1
0.1
0.1
26
27
22
26
-------
Table 5-4. Summary of Other Water Quality Parameter Results (Continued)
Parameter
(Figure, if any)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Sampling
Location
IN
TA
TB
IN
TA
TB
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
Sample
Count
16
16
16
16
16
16
Concentration
Minimum
171
161
174
110
112
115
Maximum
241
236
235
151
161
149
Average
198
199
199
129
135
132
Standard
Deviation
16
19
14
11
12
11
(a) Data invalid from 01/01/05 to 10/03/05 due to laboratory issue.
One-half of the detection limit used for nondetect results and duplicates included for calculations.
The key parameter for evaluating the effectiveness of the APU-100 system was the arsenic concentration
in the treated water. Shown in Figure 5-3, the arsenic breakthrough curves are presented as gallons of
water treated with the number of bed volumes to arsenic breakthrough at 10 ug/L from the lead and lag
tanks specified. Bed volumes of the lead tank were calculated based on the amount of media in the lead
tank only; however, bed volumes of the lag tank were calculated based on the combined media volume in
both lead and lag tanks since water exiting the lag tank had been treated by this entire media volume.
Initially, the lead tank (TA) removed the majority of arsenic from source water until its capacity gradually
decreased. Afterwards, the lag tank (TB) served as an effective polishing unit, removing arsenic to <10
ug/L throughout most of Run 1A. Both breakthrough curves in Figure 5-3a gradually increased over
time, but effluent concentrations of the lead tank were largely influenced by the fluctuating source water
arsenic concentrations (including elevated levels of particulate arsenic) near the end of Run 1A. The lag
tank, however, was able to dampen the fluctuations observed and produce rather steady arsenic
concentrations in the tank effluent.
Breakthrough of arsenic at 10 ug/L from Tank A occurred at 39,180 BV, which was 60% of the vendor-
estimated working capacity, i.e., 66,000 BV, based on 22 ft3 of media in the lead tank as shown in Table
4-4. In theory, the media should have outperformed the projection, because the system was operating
with a longer EBCT than was originally designed (i.e., 5.4 vs. 3.7 min/tank [based on 22 ft3 of media and
45 gpm of design flowrate]), which potentially could help increase the media run length.
Breakthrough of arsenic at 10 ug/L from Tank B, orthe entire system, occurred at 52,150 BV (1 BV = 44
ft3), which was 33% higher than the 39,180 BV observed following the lead tank. The average EBCT of
the system was 10.8 min, which was twice as long as that of the lead tank only. The longer EBCT
apparently benefited arsenic adsorption, extending the media run length for 33%.
Starting with a partially exhausted Tank B in the lead position and newly rebedded Tank A in the lag
position on November 27, 2006, Media Run IB was carried out to ensure that normal system operations
continued following the media changeout. Results of the initial sampling indicated that the arsenic
concentration in Tank B had dropped from 9.8 (as lag tank on August 9, 2006) to 6.2 ug/L (as lead tank
on November 28, 2006). Because intraparticle mass transport is believed to be a rate-limiting step
(Badruzzaman et al., 2004; Lin and Wu, 2001), the system downtime from August 30 to November 27,
2006, might have temporarily facilitated and improved pore diffusion by allowing additional time for
arsenic on the media surface to move into the pores and provide more easily accessible sites for
adsorption. Total arsenic concentrations continued to be monitored through March 7, 2007, when the
sampling was discontinued and the performance evaluation was completed (Figure 5-3b).
5.2.1.2 Iron and Manganese. Low concentrations of total and soluble iron and manganese existed in
source water and throughout the treatment system. Total iron concentrations were near or below the
27
-------
Arsenic Speciation at Wellhead (IN)
DAs (particulate)
As (III)
DAs(V)
y y y
Arsenic Speciation after Tank A (TA)
Arsenic Speciation after Tank B (TB)
/ / / / s / / / / / / / / / / /
Figure 5-2. Arsenic Species During Media Run 1A at Wellhead, After Tank A, and After Tank B
28
-------
Figure 5-3a. AD-33 Media Run 1A
70-
50-
o 40-
8 30 -
10
2,000 4,000 6,000 8,000 10,000 12,000 14,000 16,000 18,000 20,000
Water Treated (1,000 gal)
Figure 5-3b. AD-33™ Media Run 1B
0 2,000 4,000 6,000 8,000 10,000 12,000 14,000 16,000 18,000 20,000
Water Treated (1,000 gal)
Figure 5-3. Total Arsenic Breakthrough Curves for Media Runs 1A and IB
25-ug/L method reporting limit for all samples with one exception (i.e., 127 ug/L at IN on
September 22, 2004). Soluble iron concentrations were <25 ug/L for all samples. Total manganese
levels ranged from <0.1 to 1.6 ug/L except for one outlier (i.e., 12.4 ug/L at TB on February 2, 2005),
with the majority existing as soluble manganese. Average total and soluble manganese levels in raw
water were reduced from 0.3 ug/L to 0.1 ug/L after the adsorption tanks, indicating some removal by the
media.
5.2.1.3 Onsite Measurements. Average pH values across the treatment train were 6.9 to 7.0, which
were the lowest among the 12 Round 1 demonstration sites (Table 1-1). Near neutral pH is desirable for
29
-------
adsorptive media, which, in general, have greater arsenic removal capacities when treating lower-pH
water. Source water was oxidizing as indicated by the relatively high DO and ORP levels, which
averaged 3.9 mg/L and 305 millivolts (mV), respectively. These measurements might explain the
absence of As(III) in source water. As a result of prechlorination, ORP readings at the AC, TA, and TB
locations increased to the range of 365 to 710 mV. Free and total chlorine residuals measured at the TA
and TB locations were comparable to those measured at the AC location, indicating little or no chlorine
consumption by the AD-33™ media.
5.2.1.4 Other Water Quality Parameters. Alkalinity, fluoride, sulfate, orthophosphate, phosphorus,
silica, nitrate, and turbidity concentrations were relatively low and remained fairly constant throughout
the treatment train. Total hardness ranged from 287 to 397 mg/L (as CaCO3), consisting of approximately
60% of calcium hardness and 40% of magnesium hardness. Hardness was not significantly affected by
the treatment process.
5.2.2 Backwash Water Sampling. Backwash wastewater was sampled in 13 sampling events.
The analytical results are presented in Table 5-5. (Note that Sampling Events 11, 12, and 13 followed a
modified sampling procedure as described in Section 3.3.3.) pH values of the backwash wastewater,
ranging from 7.0 to 7.9, were somewhat higher than those of raw water (Table 5-4). Arsenic
concentrations in the backwash wastewater from Tank A and, especially, Tank B, were lower than those
in raw water used for backwash (except for Event 13), indicating removal of arsenic by the media during
backwash. During Event 13, overextraction of the source well most likely contributed to the elevated
particulate arsenic concentration as discussed in Section 5.2.1.1. The backwash wastewater from Tank A
contained higher amounts of turbidity and particulate iron and manganese than from Tank B, suggesting
filtering of most of particulates by Tank A. Nonetheless, the amounts removed by Tank A were minute,
as reflected by the low levels of TSS, i.e., <1 to 16 mg/L, in the backwash wastewater. The sampling
events did not show significant differences for pH or TDS between the two tanks.
5.2.3 Distribution System Water Sampling. The results of the 20 distribution system water
sampling events (including four baseline [BL] events) are summarized in Table 5-6. Water from the
source well, Well No. 2, blended with water from up to five other wells within the distribution system
would impact the water quality at the three sampling locations as discussed in Section 3.3.4. The most
noticeable change since system startup was the decrease in arsenic concentrations. After system startup,
arsenic concentrations, which ranged from 20.8 to 80.1 |o,g/L and averaged 48.8 |o,g/L during baseline
sampling, were reduced to the range of 2.2 to 45.6 |o,g/L and average of 19.3 |og/L. Water samples from
the distribution system exhibited significantly higher arsenic concentrations than those following the
treatment system due to the contribution of untreated water from other wells which also contained arsenic
(Tables 4-1 and 4-2).
pH, alkalinity, manganese, lead, and copper concentrations after system startup were comparable to
baseline levels except for the pH results for Event BL2 at all locations and the manganese result for Event
BL1 at DS2. Furthermore, lead and copper concentrations were well below the action levels of 15 and
1,300 |og/L, respectively. Although iron levels appeared to decrease somewhat compared to the baseline
levels, the system operation probably did not influence this reduction since Well No. 2 source water
contained little or no iron.
30
-------
Table 5-5. Backwash Water Sampling Results
Sampling
Event
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
Date
10/20/04
12/15/04
01/19/05
02/16/05
03/16/05
04/13/05
05/11/05
06/08/05
07/06/05
08/17/05
11/14/05
02/15/06
05/17/06
Tank A
%
S.U.
7.3
7.1
7.1
7.3
7.2
7.4
7.2
7.3
7.0
7.9
7.3
7.2
7.2
Turbidity
NTU
22
45
19
16
37
19
44(b)
32
52
28
NS
NS
NS
CO
Q
H
mg/L
486
358
462
446
414
564
486
466
440
438
430
420
420
CO
CO
H
mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
<1
5
16
3
£
W
-------
Table 5-6. Distribution System Sampling Results
Sampling
Event
No.
BL1
BL2
BL3
BL4
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
Date
12/17/03(a)
01/06/04
01/21/04
02/05/04
07/28/04(b)
08/26/04(b)
09/22/04(c)
10/20/04
11/17/04
12/15/04(b)
01/12/05(b'd)
02/09/05(b)
03/09/05(b)
04/06/05(b)
05/04/05(b)
06/08/0500
07/07/05(b)
08/09/05(b)
09/14/05
10/12/05fe)
DS1
Non-LCR Residence
1st Draw
e
H
,0
60
3
03
hr
12.0
14.0
34.0
23.0
11.0
20.5
12.0
19.0
7.5
9.0
9.5
9.0
11.0
10.0
6.0
10.0
9.5
7.0
6.0
11.0
K
a
S.U.
7.1
8.9
7.2
7.1
7.2
6.9
7.2
6.7
7.0
7.1
7.1
7.5
7.3
7.6
7.6
7.2
7.0
7.3
6.9
7.2
6
o
C3
u
w
^
.-^
-------
5.2.4 Spent Media Sampling. The treatment system was shut down on August 30, 2006, and
spent media samples were collected from Tank A on November 8, 2006, and analyzed as discussed in
Section 3.3.5. TCLP and total metals results are presented in Tables 5-7 and 5-8, respectively. The
TCLP results indicated that only barium was detected at 1.5 mg/L and that the media was non-hazardous
and could be disposed of in a sanitary landfill.
The ICP-MS results of the spent media indicated that the media, as expected, contained
mostly iron at 569 mg/g (as Fe), or 904 mg/g (as FeOOH), which matches closely with the 90.1% (by
weight) specified by Bayer AG (Table 4-3). The spent media also contained trace levels of Ca, Mg, Mn,
Si, Al, and P at 3.8, 1.4, 2.0, 0.23, 0.33, and 1.5 mg/g, respectively, which, except for Mn and P, also
match closely with Bayer AG's analyses. Trace amounts of Mn and P, both detected in source water,
apparently were removed by the AD-33™ media, increasing the respective loadings from the baseline
levels of 0.11 and 0.02% to 0.52 and 0.34%. The spent media also appeared to have removed some
amounts of Cu and Pb from source water, as evidenced by the decreasing loadings from the top to the
bottom of Tank A.
The arsenic loading on the spent media based on the ICP-MS results was 8.3 mg/g (average across bed
from Table 5-8). For comparison to the spent media results, the adsorptive capacity was calculated by
dividing the arsenic mass represented by the area between the influent and lead tank breakthrough curves,
as shown in Figure 5-3a, by the amount of dry media in each tank. The dry weight of the media, i.e., 527
Ib, was calculated based on a wet weight of 620 Ib (i.e., 22 ft3 of media at 28.1 lb/ft3) and a maximum
moisture content of 15% (Table 4-3). Using this approach, the arsenic loading for the spent media was
10.4 mg/g, of which 80% was recovered via ICP-MS analysis. The arsenic loading on the media in Tank
B was calculated to be 4.9 mg/g, which further supported the decision to rebed only Tank A due to the
remaining capacity of the media in Tank B. This value (4.9 mg/g) was close to that of 5.2 mg/g
calculated for the media in Tank A at the 10-|o,g/L arsenic breakthrough point (as of March 30, 2005).
Table 5-7. TCLP Results of a Composite Spent Media Sample
RCRA Metal
Arsenic
Barium
Cadmium
Chromium
Lead
Mercury
Selenium
Silver
Concentration
mg/L
0.10
1.5
0.010
0.010
0.050
0.0020
0.10
0.010
RCRA = Resource Conservation and Recovery Act
Table 5-8. Metals' Analysis of Spent Media
Tank A
Location
Top
Middle
Bottom
Mg
mg/g
1.4
1.3
1.4
Al
mg/g
0.39
0.29
0.30
Si
mg/g
0.25
0.19
0.26
P
mg/g
1.4
1.4
1.6
Ca
mg/g
4.0
3.8
3.7
Fe
mg/g
579
557
570
Mn
mg/g
2.1
2.0
1.9
Ni
mg/g
0.13
0.13
0.13
Cu
mg/g
0.57
0.36
0.11
Zn
mg/g
1.2
1.2
1.3
As
mg/g
8.7
8.6
7.8
Cd
mg/g
O.0005
0.0005
0.00
Pb
mg/g
0.03
0.01
0.00
As/Fe
Hg/mg
15.0
15.4
13.7
33
-------
5.3
Cost Information
5.3.1 Facility Cost. As part of the facility requirements, AWC provided an enclosure, an eye wash
station, and a backwash wastewater recycling system. The total cost for the sun shed structure was
$13,677, which included $3,500 for materials and $10,177 for labor to assemble the structure. The
backwash recycling system cost $11,546 for material, engineering, and installation. These costs were not
included in the cost analysis because they were funded separately by AWC and not included under the
demonstration project.
5.3.2 System Cost. The system cost 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. The capital investment for the
equipment, site engineering, and installation was $88,307 (Table 5-9). The equipment cost was $63,785
(or 72.2% of the total capital investment), which included the cost for two pressure tanks, 44 ft3 of AD-
33™ media, piping and valves, instrumentation and controls, field services (for operator training, technical
support, and system shakedown), miscellaneous materials and supplies, and a change order for system
reconfiguration from parallel to series operation.
Table 5-9. Capital Investment for AdEdge's APU-100 System
Description
Quantity
Cost
% of Capital
Investment Cost
Equipment
Adsorption Tanks
AD-33™ Media
Piping and Valves
Instrumentation and Controls
O&M Manual, Operator Training, Technical Support
Procurement, Assembly, Labor, Shakedown
Freight
Change Order for System Reconfiguration
Equipment Total
2
44ft3
1
1
1
1
1
1
-
$21,800
$10,690
$7,520
$4,575
$3,800
$12,575
$1,855
$880
$63,785
-
-
-
-
-
-
-
-
72.2%
Engineering
Materials, Submittals, FedEx, Postage, Supplies
Oversight, Specification Preparation
Design, Drawings, Coordination
Review Meeting, Airfare, Lodging, and Meals
Change Order for System Reconfiguration
Engineering Total
1
1
1
1
-
-
$75
$3,420
$4,970
$1,017
$1,890
$11,372
-
-
-
-
-
12.9%
Installation
Subcontractor
Vendor Labor
Vendor Travel
Change Order for System Reconfiguration
Installation Total
Total Capital Investment00
1
4 days
4 days
-
-
-
$6,750
$3,040
$1,290
$2,070
$13,150
$88,307
-
-
-
-
14.9%
100%
$11,546 for backwash recycling system not included.
34
-------
The engineering cost included preparation of the engineering plans, system layout and footprint, drawings
of site and piping plans, and equipment cut sheets for the permit application submittal (Section 4.3.1).
The cost also included resubmission of the redesigned system layout and piping plans following
reconfiguration to ADEQ for approval. The engineering cost of $11,372 was 12.9% of the total capital
investment.
The installation cost included equipment and labor to unload and install the APU-100 system, perform the
piping tie-ins and electrical work, load and backwash the media, and reconfigure the system (Section
4.3.2). The installation cost of $13,150 was 14.9% of the total capital investment.
The capital cost of $88,307 was normalized to $l,962/gpm ($1.36/gpd) of design capacity using the
system's design capacity of 45 gpm (or 64,800 gpd). The capital cost also was converted to an annualized
cost of $8,335/yr by multiplying a capital recovery factor (CRF) of 0.09439 based on a 7% interest rate
and a 20-yr return period. If the system had operated for 24 hr/day, 7 day/week at the 45-gpm design
flowrate to produce 23,652,000 gal/yr, the unit capital cost would have been $0.35/$1,000 gal. During the
first year, the system produced approximately 8,505,000 gal of water (based on flow meter after the lead
tank), so the unit capital cost increased to $0.98/1,000 gal.
5.3.3 O&M Cost. The O&M cost included media replacement and disposal, incremental chemical
supply, electricity, and labor as summarized in Table 5-10. Because the system was under warranty, no
additional cost was incurred for repairs. Due to the long duration of Media Run 1A, it was most cost-
effective to replace the media of the lead tank only when the lag tank effluent reached 10 |o,g/L of arsenic.
The media replacement cost of one tank was $10,908, including $5,830 for 22 ft3 of AD-33 media (or
$265/ft3), $4,240 for labor, and $375 for spent media analysis, and $463 for freight.
By averaging the media replacement cost over the life of the media, the cost per 1,000 gal of water treated
was calculated as shown in Figure 5-4. Note that after the partially exhausted lag tank is switched to the
lead position with the newly rebedded tank in the lag position, the run length for the subsequent run will
be shorter than the initial run, thus resulting in an increased replacement frequency and cost than
presented in Table 5-10.
Chemical usage consisted of NaOCl, which was added to provide disinfection and residual in the
distribution system. Since NaOCl was not required for the treatment process, its usage was not included
in the O&M cost. Electricity consumption was approximately 2.07 kWh/day based on electric meter
readings for one day (or 12 hr) of system operation (including usage from the recycle pump). Therefore,
the electricity cost was $0.008/1,000 gal of water treated. The routine, non-demonstration related labor
activities (Section 5.1.5.4), including preventative maintenance activities and repairs, consumed 15 to 20
min/day. Based on this time commitment and a labor rate of $21/hr, the labor cost was $0.22/1,000 gal of
water treated.
By averaging the total O&M cost over the life of the media, the cost per 1,000 gal of water treated was
plotted as a function of the media run length as shown in Figure 5-4. Note that the bed volumes were
calculated based on the quantity of media in both tanks (i.e., 44 ft3 or 330 gal).
35
-------
Table 5-10. O&M Cost for AdEdge's APU-100 System (Run lA)(a)
Cost Category
Value
Remarks
Media Replacement and Disposal
Media Cost ($)
Labor Cost ($)
Spent Media Analysis ($)
Travel ($)
Freight ($)
Subtotal ($)
Media Replacement and Disposal Cost
($71,000 gal)
$5,830
$4,240
$375
$0
$463
$10,908
$0.64
$265/ft3; 22 ft3 for one tank
Including TCLP test
None
Based on 17,164,000 gal until 10-|ag/L
arsenic breakthrough from lag tank
Chemical Usage
Chemical Cost ($)
$0.000
No additional chemicals required
Electricity
Electricity Cost ($/kWh)
Electricity Usage (kWh/day)
Electricity Cost ($71,000 gal)
$0.089
2.07
$0.008
Rate provided by AWC
Based on 12 hr/day operation
Labor
Labor (hr/week)
Labor Cost ($71,000 gal)
Total O&M cost ($71,000 gal)
1.6
$0.22
$0.86
15 to 20 min/day, 5 day /week
Labor rate = $2 1/hr
Based upon media run length at 10-|ag/L
arsenic breakthrough
(a) O&M cost based upon replacement of lead tank media only.
Total O&M cost
Media replacement cost
66,000 BV: Vendor-
estimated capacity
$0.00
20
30 40 50 60 70
Media Working Capacity (x1,000 BV)
80
90
100
Note: 1 BV = 44 fT = 330 gal
Figure 5-4. Media Replacement (Lead Tank) and Total O&M Cost (Run 1A)
36
-------
6.0 REFERENCES
AdEdge. 2004. Operation and Maintenance Manual, APU Adsorption Package Units for Arsenic and
Heavy Metals Removal, Rimrock,Arizona (Montezuma Haven Wells).
AWC. 2004. 2003 Annual water Quality Report for Rimrock, Arizona PWSID# 13-046.
AWC. 2005. 2004 Annual water Quality Report for Rimrock, Arizona PWSID# 13-046.
AWC. 2006. 2005 Annual water Quality Report for Rimrock, Arizona PWSID# 13-046.
Battelle. 2003. Revised 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.
Badruzzaman, M., P. Westerhoff, and D.R.U. Knappe. 2004. "Intraparticle diffusion and adsorption of
arsenate onto granular ferric hydroxide (GFH)." Water Research, 38(18): 4002-4012.
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.
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): 103-11.
EPA. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic.
Federal Register, 40 CFRPart 141.
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. 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.
Lin, T.F. and J.K. Wu. 2001. "Adsorption of arsenite and arsenate within activated alumina grains:
Equilibrium and kinetics." Water Research, 35(8): 2049-2057.
Oxenham, J.L., A.S.C. Chen, and L. Wang. 2005. Arsenic Removal from Drinking Water by Adsorptive
Media, EPA Demonstration Project at Rollinsford, NH, Six-Month Evaluation Report.
EPA/600/R-05/116. U.S. Environmental Protection Agency, National Risk Management
Research Laboratory, Cincinnati, OH.
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.
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
37
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APPENDIX A
OPERATIONAL DATA
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
06/24/04 12:32
06/25/04 1 1 :30
06/28/0409:17
06/29/0409:19
06/30/04 16:01
07/01/04 13:59
07/02/04 14:56
07/06/04 13:30
07/07/04 09:00
07/08/04 16:32
07/09/04 13:35
07/12/04 13:30
07/13/04 10:00
07/14/0409:30
07/15/04 13:30
07/16/04 14:25
07/19/0409:30
07/20/04 08:57
07/21/04 14:02
07/22/04 16:12
07/23/04 14:48
07/26/0409:16
07/27/04 14:12
07/28/04 09:46
07/29/04 09:01
07/30/04 16:18
08/02/04 10:29
08/03/04 09:27
08/04/04 09:47
08/05/04 08:58
08/06/04 14:25
08/09/04 09:45
08/10/04 16:09
08/11/04 11:09
08/12/0409:19
08/13/04 17:18
08/16/0409:00
08/17/04 12:00
08/18/0409:00
08/19/04 11:30
08/20/04 15:34
08/23/04 10:18
08/24/04 12:31
08/25/0409:12
08/26/04 13:54
08/27/04 15:31
Hour
Meter
hr
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
NA
NA
NA
NA
NA
NA
NA
ON
OFF
NA
NA
NA
NA
NA
ON
ON
NA
ON
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
ON
OFF
OFF
OFF
OFF
ON
OFF
ON
ON
OFF
OFF
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
28
33
32
29
30
31
32
29
32
32
31
32
32
32
30
27
32
28
31
32
32
28
32
33
30
31
32
32
27
32
30
26
31
32
32
30
28
31
28
29
30
32
31
31
31
31
Totalizer
gal
23971
44991
108441
131386
166117
185223
209871
297899
312011
348968
365938
433271
449425
470700
500630
525019
584077
605379
637557
664233
683833
740859
772923
787316
808295
844137
899068
919909
943057
963804
996229
1055151
1089574
1102913
1122569
1160528
1214460
1240824
1259075
1284888
1315490
1375391
1401393
1418118
1449870
1475337
Cum. Flow
gal
NA
21020
84470
107415
142146
161252
185900
273928
288040
324997
341967
409300
425454
446729
476659
501048
560106
581408
613586
640262
659862
716888
748952
763345
784324
820166
875097
895938
919086
939833
972258
1031180
1065603
1078942
1098598
1136557
1190489
1216853
1235104
1260917
1291519
1351420
1377422
1394147
1425899
1451366
Bed
Volume
NA
128
513
653
864
980
1130
1665
1750
1975
2078
2487
2585
2715
2897
3045
3404
3533
3729
3891
4010
4356
4551
4639
4766
4984
5318
5444
5585
5711
5908
6266
6475
6557
6676
6907
7234
7395
7505
7662
7848
8212
8370
8472
8665
8820
Tank B Flow Meter
Flowr
ate
gpm
27
31
32
28
30
30
31
28
33
32
31
31
32
32
31
27
33
27
30
32
31
28
32
32
30
31
31
31
26
30
30
26
30
31
31
30
26
30
26
29
31
31
30
30
30
31
Totalizer
gal
23294
44375
108075
130974
165692
184858
209636
297866
311809
349009
366086
433584
449865
471247
500527
524715
583614
604867
637111
663800
683350
740026
772091
786508
807403
843320
898410
919248
942185
962970
995478
1054232
1087899
1100798
1120172
1157685
1210860
1236957
1255175
1280719
1310625
1369612
1395087
1411570
1442950
1468239
Cum. Flow
gal
NA
21081
84781
107680
142398
161564
186342
274572
288515
325715
342792
410290
426571
447953
477233
501421
560320
581573
613817
640506
660056
716732
748797
763214
784109
820026
875116
895954
918891
939676
972184
1030938
1064605
1077504
1096878
1134391
1187566
1213663
1231881
1257425
1287331
1346318
1371793
1388276
1419656
1444945
Bed
Volume
NA
64
258
327
433
491
566
834
877
990
1042
1247
1296
1361
1450
1524
1702
1767
1865
1946
2006
2178
2275
2319
2382
2492
2659
2722
2792
2855
2954
3132
3235
3274
3333
3447
3608
3688
3743
3821
3911
4091
4168
4218
4313
4390
dP
TA
psi
4.0
5.5
5.5
4.5
5.0
5.5
5.5
4.0
5.5
5.0
5.0
5.0
5.0
5.5
4.5
3.5
5.5
4.0
5.0
5.0
5.0
4.0
5.9
5.5
5.0
5.0
5.0
5.0
4.0
5.0
5.0
3.6
5.0
5.0
5.0
5.0
3.8
5.0
3.9
4.0
5.0
5.0
5.0
5.0
5.0
5.0
TB
psi
3.5
5.0
5.0
4.0
5.0
5.0
5.0
4.0
4.5
5.0
5.0
5.0
5.0
5.0
4.5
3.5
5.0
3.5
4.9
5.0
4.5
4.0
5.0
5.0
5.0
5.0
5.0
4.5
3.6
5.0
5.0
3.6
5.0
5.0
5.0
5.0
3.8
4.8
3.5
3.9
5.0
4.5
4.5
4.5
4.5
4.6
Pressure
Inlet
psig
105
98
100
105
101
100
100
105
100
100
100
100
100
100
101
110
99
102
100
99
100
102
100
100
100
100
100
100
105
100
100
103
100
100
100
100
105
100
105
101
100
100
100
100
100
100
Between
Tanks
psig
104
95
96
103
100
96
96
109
95
97
97
96
95
93
100
110
95
104
97
95
96
102
95
95
96
96
96
96
103
96
98
104
98
97
97
97
103
98
103
101
98
96
96
97
97
97
Outlet
psig
100+
92
93
100+
90
93
94
100+
94
93
94
92
93
92
87
100+
92
104
94
93
94
101
93
92
94
94
90
90
96
90
90
99
90
90
90
90
98
90
97
96
90
90
90
90
89
90
Recycling
Flow
Rate
gpm
0
0
0
1.5
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
1
1
0
0
0
0
0
0
0
0
0
0.5
0.5
0.5
0
0
0
0
0
0
NA
0
0
0
0
Totalizer
gal
0
0
0
287
511
511
511
511
511
511
511
511
511
511
851
1220
1290
1290
1290
1290
1290
1420
1910
2060
2060
2060
2060
2060
2060
2060
2060
2060
2130
2330
2630
2840
2840
2840
2840
2840
2840
NA
2840
2840
2840
2840
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
08/30/0416:13
08/31/0411:17
09/01/0411:00
09/02/0413:54
09/03/0412:42
09/07/0416:52
09/08/0410:57
09/09/0417:29
09/10/0416:45
09/13/0409:43
09/14/0409:30
09/15/0409:30
09/16/0408:22
09/17/0413:30
09/20/0413:00
09/21/0410:00
09/22/0410:00
09/23/04 09:00
09/24/0411:30
09/27/0410:00
09/28/04 1 1 :34
09/29/0415:10
09/30/0411:16
10/01/0413:43
10/05/0410:42
10/06/0417:31
10/07/0410:54
10/08/0411:38
10/12/0417:29
10/13/0417:41
10/14/0418:20
10/18/0414:49
10/19/0415:01
10/20/0410:35
10/22/0412:02
10/25/0410:46
10/26/0415:02
10/27/0410:00
10/28/0410:32
10/29/0414:18
11/01/0415:10
11/02/0411:50
11/03/0409:45
11/04/0414:56
11/05/0412:36
Hour
Meter
hr
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
3.2
12.8
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
ON
ON
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
ON
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
27
31
32
32
30
30
31
31
31
27
32
31
31
31
31
31
31
31
31
32
31
31
31
31
32
29
32
31
27
26
26
31
31
31
32
31
31
31
27
32
31
29
31
32
32
Totalizer
gal
1544210
1557388
1578093
1605790
1625872
1723558
1734996
1769316
1790558
1844869
1867121
1889587
1911446
1944096
201 1 723
2029216
2050996
2074455
2101154
2167484
2192360
2221335
2236812
2264087
2348918
2383918
2394302
2417168
2515357
2538203
2561400
2644969
2667528
2682128
2730730
2796639
2827402
2840201
2864858
2895024
2966104
2982700
3002182
3033540
3052755
Cum. Flow
gal
1520239
1533417
1554122
1581819
1601901
1699587
1711025
1745345
1 766587
1820898
1843150
1865616
1887475
1920125
1987752
2005245
2027025
2050484
2077183
2143513
2168389
2197364
2212841
2240116
2324947
2359947
2370331
2393197
2491386
2514232
2537429
2620998
2643557
2658157
2706759
2772668
2803431
2816230
2840887
2871053
2942133
2958729
2978211
3009569
3028784
Bed
Volume
9238
9318
9444
9612
9734
10328
10398
10606
10735
11065
11200
11337
11470
11668
12079
12185
12318
12460
12623
13026
13177
13353
13447
13613
14128
14341
14404
14543
15140
15279
15419
15927
16064
16153
16448
16849
17036
17114
17264
17447
17879
17980
18098
18289
18405
Tank B Flow Meter
Flowr
ate
gpm
27
30
31
32
30
29
31
31
31
27
31
33
31
31
30
30
30
30
30
32
31
31
32
30
31
30
31
29
27
26
27
31
32
31
28
31
32
30
29
31
32
29
32
32
30
Totalizer
gal
1536384
1549642
1570127
1597517
1617330
1714199
1725572
1759727
1780911
1835049
1857243
1879663
1901462
1933954
2001410
2018904
2040690
2064162
2090817
2156478
2181238
2210018
2225389
2252590
2337120
2372015
2382373
2405125
2502458
2525203
2548271
2631513
2654020
2667888
2716319
2781672
2811839
2824366
2848575
2878185
2948057
2964350
2983630
3014434
3033038
Cum. Flow
gal
1513090
1526348
1546833
1574223
1594036
1690905
1702278
1736433
1757617
1811755
1833949
1856369
1878168
1910660
1978116
1995610
201 7396
2040868
2067523
2133184
2157944
2186724
2202095
2229296
2313826
2348721
2359079
2381831
2479164
2501909
2524977
2608219
2630726
2644594
2693025
2758378
2788545
2801072
2825281
2854891
2924763
2941056
2960336
2991140
3009744
Bed
Volume
4597
4638
4700
4783
4843
5138
5172
5276
5340
5505
5572
5640
5707
5805
6010
6063
6130
6201
6282
6481
6557
6644
6691
6774
7030
7136
7168
7237
7533
7602
7672
7925
7993
8035
8183
8381
8473
8511
8584
8674
8887
8936
8995
9088
9145
dP
TA
psi
4.0
5.0
5.5
5.0
5.0
5.0
5.0
5.0
5.0
3.9
5.1
5.1
5.5
5.1
5.0
5.0
5.0
5.0
4.9
5.0
5.0
5.0
5.0
5.0
5.0
4.9
5.2
5.5
4.0
3.5
4.0
5.0
5.1
5.1
5.0
5.0
5.4
5.0
4.0
4.6
5.5
4.0
5.1
5.0
5.1
TB
psi
4.0
4.7
4.8
5.0
5.0
5.0
5.0
5.0
5.0
3.5
5.0
5.0
5.0
5.0
4.9
4.9
4.9
4.9
4.8
4.8
5.0
5.0
5.0
5.0
5.0
4.9
5.0
5.0
3.5
3.5
4.0
4.6
5.0
4.9
5.0
5.0
5.0
5.0
3.6
4.6
5.1
4.0
5.0
5.0
5.0
Pressure
Inlet
psig
104
100
100
100
100
100
100
100
100
102
100
100
100
100
100
100
100
100
100
100
100
100
100
100
100
102
100
100
102
104
103
100
100
100
100
100
100
100
109
100
100
105
100
100
100
Between
Tanks
psig
101
97
97
96
97
97
97
97
96
103
95
95
96
95
96
96
96
96
97
96
97
96
97
97
96
100
96
96
104
107
105
98
97
97
97
96
97
96
105
98
96
101
98
98
97
Outlet
psig
106
90
90
89
90
90
90
90
90
99
89
90
90
90
91
91
91
91
91
91
91
90
91
90
90
95
89
89
99
104
100
92
91
91
91
100
90
90
100
93
90
96
98
99
98
Recycling
Flow
Rate
gpm
0
0
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0.4
0.5
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
2840
2840
3100
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3630
4010
4452
4690
4849
4849
4849
4849
4849
4849
4849
4849
4849
4849
4870
5621
6323
6323
6323
6323
6323
6327
6327
6327
6327
6327
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
08/30/0416:13
08/31/0411:17
09/01/0411:00
09/02/0413:54
09/03/0412:42
09/07/0416:52
09/08/0410:57
09/09/0417:29
09/10/0416:45
09/13/0409:43
09/14/0409:30
09/15/0409:30
09/16/0408:22
09/17/0413:30
09/20/0413:00
09/21/0410:00
09/22/0410:00
09/23/04 09:00
09/24/0411:30
09/27/0410:00
09/28/04 1 1 :34
09/29/0415:10
09/30/0411:16
10/01/0413:43
10/05/0410:42
10/06/0417:31
10/07/0410:54
10/08/0411:38
10/12/0417:29
10/13/0417:41
10/14/0418:20
10/18/0414:49
10/19/0415:01
10/20/0410:35
10/22/0412:02
10/25/0410:46
10/26/0415:02
10/27/0410:00
10/28/0410:32
10/29/0414:18
11/01/0415:10
11/02/0411:50
11/03/0409:45
11/04/0414:56
11/05/0412:36
11/08/0411:09
Hour
Meter
hr
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
3.2
12.8
47.1
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
ON
ON
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
ON
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
27
31
32
32
30
30
31
31
31
27
32
31
31
31
31
31
31
31
31
32
31
31
31
31
32
29
32
31
27
26
26
31
31
31
32
31
31
31
27
32
31
29
31
32
32
33
Totalizer
gal
1544210
1557388
1578093
1605790
1625872
1723558
1734996
1769316
1790558
1844869
1867121
1889587
1911446
1944096
201 1 723
2029216
2050996
2074455
2101154
2167484
2192360
2221335
2236812
2264087
2348918
2383918
2394302
2417168
2515357
2538203
2561400
2644969
2667528
2682128
2730730
2796639
2827402
2840201
2864858
2895024
2966104
2982700
3002182
3033540
3052755
3120094
Cum. Flow
gal
1520239
1533417
1554122
1581819
1601901
1699587
1711025
1745345
1 766587
1820898
1843150
1865616
1887475
1920125
1987752
2005245
2027025
2050484
2077183
2143513
2168389
2197364
2212841
2240116
2324947
2359947
2370331
2393197
2491386
2514232
2537429
2620998
2643557
2658157
2706759
2772668
2803431
2816230
2840887
2871053
2942133
2958729
2978211
3009569
3028784
3096123
Bed
Volume
9238
9318
9444
9612
9734
10328
10398
10606
10735
11065
11200
11337
11470
11668
12079
12185
12318
12460
12623
13026
13177
13353
13447
13613
14128
14341
14404
14543
15140
15279
15419
15927
16064
16153
16448
16849
17036
17114
17264
17447
17879
17980
18098
18289
18405
18815
Tank B Flow Meter
Flowr
ate
gpm
27
30
31
32
30
29
31
31
31
27
31
33
31
31
30
30
30
30
30
32
31
31
32
30
31
30
31
29
27
26
27
31
32
31
28
31
32
30
29
31
32
29
32
32
30
31
Totalizer
gal
1536384
1549642
1570127
1597517
1617330
1714199
1725572
1759727
1780911
1835049
1857243
1879663
1901462
1933954
2001410
2018904
2040690
2064162
2090817
2156478
2181238
2210018
2225389
2252590
2337120
2372015
2382373
2405125
2502458
2525203
2548271
2631513
2654020
2667888
2716319
2781672
2811839
2824366
2848575
2878185
2948057
2964350
2983630
3014434
3033038
3099099
Cum. Flow
gal
1513090
1526348
1546833
1574223
1594036
1690905
1702278
1736433
1757617
1811755
1833949
1856369
1878168
1910660
1978116
1995610
201 7396
2040868
2067523
2133184
2157944
2186724
2202095
2229296
2313826
2348721
2359079
2381831
2479164
2501909
2524977
2608219
2630726
2644594
2693025
2758378
2788545
2801072
2825281
2854891
2924763
2941056
2960336
2991140
3009744
3075805
Bed
Volume
4597
4638
4700
4783
4843
5138
5172
5276
5340
5505
5572
5640
5707
5805
6010
6063
6130
6201
6282
6481
6557
6644
6691
6774
7030
7136
7168
7237
7533
7602
7672
7925
7993
8035
8183
8381
8473
8511
8584
8674
8887
8936
8995
9088
9145
9346
dP
TA
psi
4.0
5.0
5.5
5.0
5.0
5.0
5.0
5.0
5.0
3.9
5.1
5.1
5.5
5.1
5.0
5.0
5.0
5.0
4.9
5.0
5.0
5.0
5.0
5.0
5.0
4.9
5.2
5.5
4.0
3.5
4.0
5.0
5.1
5.1
5.0
5.0
5.4
5.0
4.0
4.6
5.5
4.0
5.1
5.0
5.1
5.5
TB
psi
4.0
4.7
4.8
5.0
5.0
5.0
5.0
5.0
5.0
3.5
5.0
5.0
5.0
5.0
4.9
4.9
4.9
4.9
4.8
4.8
5.0
5.0
5.0
5.0
5.0
4.9
5.0
5.0
3.5
3.5
4.0
4.6
5.0
4.9
5.0
5.0
5.0
5.0
3.6
4.6
5.1
4.0
5.0
5.0
5.0
5.0
Pressure
Inlet
psig
104
100
100
100
100
100
100
100
100
102
100
100
100
100
100
100
100
100
100
100
100
100
100
100
100
102
100
100
102
104
103
100
100
100
100
100
100
100
109
100
100
105
100
100
100
100
Between
Tanks
psig
101
97
97
96
97
97
97
97
96
103
95
95
96
95
96
96
96
96
97
96
97
96
97
97
96
100
96
96
104
107
105
98
97
97
97
96
97
96
105
98
96
101
98
98
97
98
Outlet
psig
106
90
90
89
90
90
90
90
90
99
89
90
90
90
91
91
91
91
91
91
91
90
91
90
90
95
89
89
99
104
100
92
91
91
91
100
90
90
100
93
90
96
98
99
98
99
Recycling
Flow
Rate
gpm
0
0
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0.4
0.5
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
2840
2840
3100
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3370
3630
4010
4452
4690
4849
4849
4849
4849
4849
4849
4849
4849
4849
4849
4870
5621
6323
6323
6323
6323
6323
6327
6327
6327
6327
6327
6330
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
11/09/0411:19
11/10/0416:57
11/12/0417:15
11/15/0418:03
11/16/0410:12
11/17/0409:46
11/18/0414:49
11/19/0415:40
11/22/0409:38
11/23/0410:00
11/24/0414:11
11/29/0410:14
11/30/0410:47
12/01/0410:58
12/06/0409:35
12/07/0409:15
12/08/0410:04
12/09/0409:32
12/10/0414:00
12/13/0408:15
12/14/0414:00
12/15/0417:00
12/16/0415:13
12/17/0416:39
12/20/0417:14
12/21/0409:24
12/22/0415:02
12/27/0415:15
12/28/0410:05
12/29/0414:33
12/31/0411:01
01/03/0511:07
01/04/05 09:34
01/06/0511:26
01/10/0510:27
01/11/0510:08
01/12/0508:59
01/14/05 16:49
01/17/0511:56
01/18/0509:19
01/19/05 12:45
01/24/05 09:53
01/25/05 08:58
01/26/0511:05
01/27/0510:14
01/28/0515:08
Hour
Meter
hr
59.9
111
102.0
139.1
143.6
154.6
172.0
184.7
215.2
227.7
240.7
299.1
310.1
NA
382.5
394.4
406.7
418.3
432.1
NA
NA
492.2
505.2
517.1
552.8
NA
NA
636.0
NA
659.8
683.1
718.8
729.4
755.4
NA
813.2
823.8
879.6
915.7
925.5
939.7
975.2
986.1
1000.0
1011.1
1028.1
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
Tank A Flow Meter
Flowr
ate
gpm
32
32
31
30
32
32
32
31
32
33
31
30
31
32
33
33
31
33
33
33
33
NA
33
NA
NA
32
NA
NA
32
NA
33
32
33
32
33
34
31
NA
33
34
34
33
34
29
NA
Totalizer
gal
3143725
31 77995
3225113
3296170
3304356
3326877
3359732
338471 1
3443037
3466574
3492632
3605433
3629181
3652572
3766441
3788938
3813731
3835866
3863117
3927415
3957724
3982673
4008571
4032260
4103115
4122253
4149825
4266102
4286326
4312023
4357919
4427087
4447210
4497385
4588277
4590667
4612117
4723345
4795278
4814502
4842508
4914174
4935926
4964184
4986039
5019189
Cum. Flow
gal
3119754
3154024
3201142
3272199
3280385
3302906
3335761
3360740
3419066
3442603
3468661
3581462
3605210
3628601
3742470
3764967
3789760
3811895
3839146
3903444
3933753
3958702
3984600
4008289
4079144
4098282
4125854
4242131
4262355
4288052
4333948
4403116
4423239
4473414
4564306
4566696
4588146
4699374
4771307
4790531
4818537
4890203
4911955
4940213
4962068
4995218
Bed
Volume
18958
19166
19453
19885
19934
20071
20271
20423
20777
20920
21078
21764
21908
22050
22742
22879
23030
23164
23330
23720
23905
24056
24214
24358
24788
24904
25072
25779
25902
26058
26337
26757
26879
27184
27736
27751
27881
28557
28994
29111
29281
29717
29849
30021
30154
30355
Tank B Flow Meter
Flowr
ate
gpm
31
32
33
33
31
28
33
32
30
33
31
30
32
33
33
31
32
33
31
34
33
NA
31
NA
NA
33
NA
NA
31
NA
31
30
30
31
33
33
33
33
NA
31
33
34
33
32
28
NA
Totalizer
gal
3122431
3156140
3202655
3272583
3280723
3303126
3335681
3360410
3418182
3441496
3467298
3579122
3602681
3625889
3738862
3761091
378561 7
3807480
3834341
3897613
3927319
3950999
3976384
3999641
4068989
4087888
4114985
4229848
4249930
4275421
4321069
4389855
4409801
4459637
4549897
4552270
4573178
4681745
4751893
4770599
4797759
4868118
4889629
4917217
4938853
4971767
Cum. Flow
gal
3099137
3132846
3179361
3249289
3257429
3279832
3312387
3337116
3394888
3418202
3444004
3555828
3579387
3602595
3715568
3737797
3762323
3784186
3811047
3874319
3904025
3927705
3953090
3976347
4045695
4064594
4091691
4206554
4226636
4252127
4297775
4366561
4386507
4436343
4526603
4528976
4549884
4658451
4728599
4747305
4774465
4844824
4866335
4893923
4915559
4948473
Bed
Volume
9416
9519
9660
9873
9897
9965
10064
10140
10315
10386
10464
10804
10876
10946
11289
11357
11431
11498
11580
11772
11862
11934
12011
12082
12292
12350
12432
12781
12842
12920
13058
13267
13328
13479
13754
13761
13824
14154
14367
14424
14507
14721
14786
14870
14935
15035
dP
TA
psi
5.5
5.5
5.5
5.0
5.9
5.5
5.9
5.5
5.6
5.5
5.5
6.0
5.5
5.4
5.5
5.5
5.5
5.5
6.5
5.5
5.5
NA
6.0
NA
NA
5.5
NA
NA
5.5
NA
5.5
5.5
5.9
5.9
5.5
6.0
5.9
6.0
NA
5.9
6.0
6.0
6.0
6.0
5.0
NA
TB
psi
5.0
5.0
5.0
5.0
5.1
5.0
5.0
5.0
5.1
5.0
5.0
5.0
5.0
5.0
5.5
5.0
5.0
5.3
5.5
5.0
5.1
NA
5.5
NA
NA
5.0
NA
NA
5.1
NA
5.1
5.1
5.2
5.1
5.0
5.5
5.4
5.5
NA
5.4
5.5
5.4
5.5
5.1
4.4
NA
Pressure
Inlet
psig
100
101
100
101
100
101
101
101
100
101
101
122*
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
104
NA
103
103
104
104
104
107
NA
Between
Tanks
psig
97
96
96
99
97
98
97
99
97
98
97
97
98
97
96
97
97
97
97
98
98
85
97
NA
NA
97
NA
NA
97
NA
97
98
97
97
97
97
97
97
NA
88
94
98
98
96
100
NA
Outlet
psig
98
98
97
100
97
99
97
99
99
98
98
115
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
88
NA
88
88
88
88
88
93
NA
Recycling
Flow
Rate
gpm
0
0
0
0.5
0.5
0.5
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
NA
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0.5
0.5
0.5
0
Totalizer
gal
6330
6330
6330
6451
6565
6913
7406
7784
7905
7905
7905
7908
7908
7908
7908
7908
7908
7908
7908
7908
7908
23
403
751
1610
1610
1610
1610
1610
1610
1610
1612
1615
1615
1615
1615
1615
1615
1615
1615
1668
2704
3036
3440
3764
4055
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
01/31/0509:55
02/01/0516:00
02/02/0511:20
02/03/05 08:45
02/04/0516:16
02/07/05 10:53
02/08/05 10:47
02/09/05 10:05
02/10/0509:00
02/11/0511:08
02/15/05 10:35
02/16/0511:05
02/17/0510:33
02/18/0511:54
02/22/0510:17
02/23/05 10:09
02/24/05 09:06
02/25/0516:46
02/28/05 08:58
03/02/05 09:24
03/03/05 1 1 :05
03/04/0515:05
03/07/05 09:31
03/08/0515:26
03/09/0515:59
03/10/0508:39
03/11/0514:26
03/14/0509:30
03/15/05 10:50
03/16/0508:00
03/17/0508:46
03/18/0517:02
03/21/0510:12
03/22/05 09:40
03/23/0511:21
03/24/0516:40
03/25/0514:06
03/28/0515:35
03/29/05 09:26
03/30/0510:19
03/31/0509:16
04/04/0511:19
04/05/05 10:48
04/06/0515:36
04/07/0516:29
04/08/0514:17
Hour
Meter
hr
1062.3
1075.6
1087.5
1096.8
1111.3
1146.5
1170.2
1181.5
1192.6
1206.2
1254.2
1265.8
1277.8
1290.7
1337.2
1349.1
1359.9
1374.0
1407.3
1431.3
1445.5
1457.7
1491.4
1505.2
1517.1
1526.3
1540.9
1574.9
1588.0
1597.0
1609.4
1623.9
1658.4
1669.7
1683.3
1695.2
1707.1
1742.8
1752.6
1 765.5
1 776.3
1826.0
1837.2
1849.8
1861.7
1868.7
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
ON
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
32
NA
33
29
NA
25
32
32
33
32
32
33
33
32
33
33
33
NA
34
35
33
NA
34
NA
NA
32
NA
32
34
31
33
NA
34
32
33
NA
NA
NA
32
33
31
32
33
NA
NA
33
Totalizer
gal
5086168
5112646
5135971
5153884
5182326
5251055
5297104
5318931
5340324
5367723
546271 7
5486396
5510522
5513120
5606998
5630977
5652469
5681376
5748368
5797131
5825380
5850439
5919211
5947481
5971533
5989742
6020129
6088744
6115750
6133650
6159461
6189230
6259086
6281871
6309100
6333095
6356848
6427387
6446729
6472133
6493593
6592527
6615187
6640145
6663770
6677708
Cum. Flow
gal
5062197
5088675
5112000
5129913
5158355
5227084
5273133
5294960
5316353
5343752
5438746
5462425
5486551
5489149
5583027
5607006
5628498
5657405
5724397
5773160
5801409
5826468
5895240
5923510
5947562
5965771
5996158
6064773
6091779
6109679
6135490
6165259
6235115
6257900
6285129
6309124
6332877
6403416
6422758
6448162
6469622
6568556
6591216
6616174
6639799
6653737
Bed
Volume
30762
30923
31065
31174
31346
31764
32044
32176
32306
32473
33050
33194
33341
33357
33927
34073
34203
34379
34786
35082
35254
35406
35824
35996
36142
36253
36438
36854
37019
37127
37284
37465
37890
38028
38194
38339
38484
38912
39030
39184
39315
39916
40054
40205
40349
40434
Tank B Flow Meter
Flowr
ate
gpm
32
NA
33
29
NA
24
31
32
32
34
32
32
31
32
32
33
29
NA
34
34
35
NA
32
NA
NA
32
NA
33
33
29
32
NA
33
32
31
NA
NA
NA
34
33
30
33
33
NA
NA
33
Totalizer
gal
5038276
5064534
5087715
5105543
5133796
5202212
5248015
5269749
5291091
5318390
5412813
5435484
5459325
5461900
5553239
5576539
5597591
5625653
5690798
5738226
5765640
5789651
5855916
5883084
5906386
5924129
5953383
6019922
6045938
6063495
6087891
6116938
6185027
6207279
6233889
6257541
6280886
6350621
6369758
6394797
6415987
6513805
6536228
6560887
6584247
6598005
Cum. Flow
gal
5014982
5041240
5064421
5082249
5110502
5178918
5224721
5246455
5267797
5295096
5389519
5412190
5436031
5438606
5529945
5553245
5574297
5602359
5667504
5714932
5742346
5766357
5832622
5859790
5883092
5900835
5930089
5996628
6022644
6040201
6064597
6093644
6161733
6183985
6210595
6234247
6257592
6327327
6346464
6371503
6392693
649051 1
6512934
6537593
6560953
657471 1
Bed
Volume
15238
15317
15388
15442
15528
15736
15875
15941
16006
16089
16376
16444
16517
16525
16802
16873
16937
17022
17220
17364
17448
17521
17722
17804
17875
17929
18018
18220
18299
18353
18427
18515
18722
18789
18870
18942
19013
19225
19283
19359
19424
19721
19789
19864
19935
19977
dP
TA
psi
5.5
NA
5.5
4.5
NA
3.2
5.0
5.5
5.5
5.5
5.5
6.0
6.0
5.9
5.5
5.5
5.5
NA
5.8
5.8
5.9
NA
5.9
NA
NA
5.9
NA
5.9
5.9
5.0
6.0
NA
5.6
5.9
5.9
NA
NA
NA
6.0
5.8
4.9
5.9
5.9
NA
NA
5.8
TB
psi
5.2
NA
5.1
4.1
NA
3.5
5.0
5.1
5.3
5.0
5.0
5.1
5.5
5.1
5.0
5.1
5.0
NA
5.3
5.4
5.5
NA
5.5
NA
NA
5.5
NA
5.5
5.5
5.0
5.8
NA
5.2
5.5
5.5
NA
NA
NA
5.5
5.5
4.5
5.2
5.2
NA
NA
5.5
Pressure
Inlet
psig
104
NA
103
107
NA
96
100
104
104
104
104
104
104
104
104
104
104
NA
104
104
104
NA
104
NA
NA
105
NA
105
104
106
104
NA
104
104
104
NA
NA
NA
104
104
108
104
104
NA
NA
105
Between
Tanks
psig
97
NA
97
102
NA
83
99
98
98
98
98
96
96
99
98
96
98
NA
98
99
97
NA
97
NA
NA
89
NA
98
97
98
97
NA
88
89
89
NA
NA
NA
98
98
102
98
97
NA
NA
97
Outlet
psig
88
NA
88
94
NA
86
89
89
90
89
89
89
88
110
88
88
88
NA
88
88
88
NA
88
NA
NA
84
NA
90
90
90
89
NA
89
89
89
NA
NA
NA
88
89
93
89
89
NA
NA
88
Recycling
Flow
Rate
gpm
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
4055
4055
4055
4055
4055
4055
4055
4055
4055
4055
4060
4117
4468
4839
5694
5694
5694
5694
5694
5694
5694
5694
5894
5894
5894
5894
5894
5894
5894
5894
6021
6447
7328
7328
7328
7328
7328
7328
7328
7328
7328
7328
7328
7328
7328
7328
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
04/11/0511:14
04/12/0511:45
04/13/0507:30
04/14/0511:00
04/15/0509:45
04/18/05 14:30
04/20/05 1 1 :31
04/21/05 12:09
04/22/05 14:36
04/25/05 13:45
04/26/05 16:45
04/27/05 10:32
04/28/05 09:36
04/29/05 16:32
05/02/05 13:48
05/03/0513:17
05/04/05 09:30
05/05/05 13:31
05/06/05 14:43
05/09/05 09:29
05/10/05 10:28
05/11/0508:30
05/12/0508:00
05/13/05 13:00
05/16/0509:42
05/17/0509:47
05/18/05 15:07
05/23/05 09:27
05/24/05 09:07
05/25/05 10:30
05/26/05 08:40
05/27/05 16:45
05/31/0509:57
06/01/05 16:43
06/02/0511:35
06/03/0514:10
06/06/05 15:23
06/07/0513:13
06/08/05 10:00
06/09/05 10:00
06/13/05 14:30
06/14/05 14:00
06/15/0509:33
06/16/0511:25
06/17/0515:56
06/20/05 09:24
Hour
Meter
hr
1902.2
1915.1
1922.8
1938.5
1949.2
1990.8
2012.3
2020.1
2034.7
2070.3
2085.7
2091.2
2102.9
2122.1
2155.9
2167.7
2176.0
2191.3
2205.7
2237.0
2250.3
2260.4
2272.2
2289.5
2322.5
2334.8
2348.7
2407.7
2419.6
2433.3
2443.5
2463.8
2505.8
2524.8
2531.9
2546.6
2584.4
2594.5
2603.7
2615.7
2664.1
2675.9
2683.5
2697.7
2714.3
2744.3
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
OFF
OFF
OFF
OFF
OFF
ON
ON
OFF
OFF
OFF
OFF
OFF
OFF
ON
ON
OFF
ON
ON
OFF
ON
OFF
ON
ON
OFF
ON
OFF
ON
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
ON
OFF
OFF
OFF
ON
ON
ON
Tank A Flow Meter
Flowr
ate
gpm
36
35
34
34
34
30
31
33
34
34
33
33
33
30
30
34
30
31
34
31
34
31
31
34
30
32
31
32
34
34
32
34
34
34
33
32
33
33
31
29
33
33
34
30
30
28
Totalizer
gal
6744490
6769857
6785197
6817030
6838395
6921 707
6963999
6979520
7008297
7079621
7110054
7121605
7143856
7182069
7249253
7271983
7288280
7319966
7346749
7408975
7434485
7454512
7478212
7512395
7577780
7601 788
7636716
7747128
7771155
7798620
7819144
7860113
7944635
7983619
7998110
8028056
8103916
8123811
8141844
8166136
8262128
8285731
8301036
8329836
8363080
8422922
Cum. Flow
gal
6720519
6745886
6761226
6793059
6814424
6897736
6940028
6955549
6984326
7055650
7086083
7097634
7119885
7158098
7225282
7248012
7264309
7295995
7322778
7385004
7410514
7430541
7454241
7488424
7553809
7577817
7612745
7723157
7747184
7774649
7795173
7836142
7920664
7959648
7974139
8004085
8079945
8099840
8117873
8142165
8238157
8261760
8277065
8305865
8339109
8398951
Bed
Volume
40839
40993
41087
41280
41410
41916
42173
42268
42442
42876
43061
43131
43266
43498
43907
44045
44144
44336
44499
44877
45032
45154
45298
45506
45903
46049
46261
46932
47078
47245
47370
47619
48132
48369
48457
48639
49100
49221
49331
49478
50062
50205
50298
50473
50675
51039
Tank B Flow Meter
Flowr
ate
gpm
34
34
33
32
33
30
30
33
33
33
32
33
34
30
31
34
30
30
31
30
31
31
31
32
32
32
30
32
33
33
30
34
32
32
33
33
33
31
30
29
32
32
30
28
28
28
Totalizer
gal
6663930
6688978
6704130
6734745
6755800
6837851
6879575
6894870
6923246
6993594
7023634
7035028
7056963
7094744
7160993
7183391
7199462
7230715
7257140
7318530
7343756
7363585
7386221
7419923
7484426
7508093
7542552
7649935
7673116
7699640
7719595
7759187
7841126
7878227
7891957
7920685
7993978
8013258
8030813
8053634
8147515
8170129
8184680
8212046
8244031
8301802
Cum. Flow
gal
6640636
6665684
6680836
6711451
6732506
6814557
6856281
6871576
6899952
6970300
7000340
7011734
7033669
7071450
7137699
7160097
7176168
7207421
7233846
7295236
7320462
7340291
7362927
7396629
7461132
7484799
7519258
7626641
7649822
7676346
7696301
7735893
7817832
7854933
7868663
7897391
7970684
7989964
8007519
8030340
8124221
8146835
8161386
8188752
8220737
8278508
Bed
Volume
20177
20253
20299
20392
20456
20705
20832
20879
20965
21179
21270
21304
21371
21486
21687
21755
21804
21899
21979
22166
22243
22303
22372
22474
22670
22742
22847
23173
23243
23324
23384
23505
23754
23866
23908
23995
24218
24277
24330
24399
24685
24753
24798
24881
24978
25153
dP
TA
psi
5.9
6.0
6.0
6.0
6.0
5.0
5.0
6.0
5.9
5.9
6.0
5.9
5.9
5.0
4.6
6.0
5.0
5.0
6.0
5.0
5.9
5.0
5.0
6.0
5.0
5.9
5.1
5.8
5.9
5.9
4.8
5.9
5.5
5.9
5.9
5.8
5.9
5.5
5.0
4.8
5.5
5.5
5.9
4.6
4.8
4.8
TB
psi
5.5
5.8
5.8
5.5
5.5
5.0
4.9
5.5
5.5
5.5
5.5
5.4
5.2
4.5
4.4
5.6
5.0
4.5
5.5
4.6
5.4
4.8
4.8
5.5
4.5
5.2
5.0
5.5
5.5
5.5
4.5
5.4
5.2
5.2
5.1
5.1
5.4
5.1
4.8
4.2
5.1
5.0
5.2
4.1
4.2
4.2
Pressure
Inlet
psig
104
105
105
105
105
107
107
104
104
105
105
105
105
108
108
104
108
108
104
108
105
108
108
106
109
105
106
105
105
105
108
105
105
105
105
105
105
105
105
109
104
106
106
110
109
109
Between
Tanks
psig
97
97
97
97
98
101
101
97
97
97
97
98
98
101
103
98
102
101
98
102
97
102
102
98
104
99
100
99
99
99
102
97
97
99
98
98
98
97
102
102
98
98
98
103
102
103
Outlet
psig
89
90
90
90
90
93
93
89
89
89
89
89
89
95
95
88
93
93
89
95
90
95
95
90
96
90
92
90
89
90
95
90
90
90
90
90
90
90
94
95
90
90
92
96
96
97
Recycling
Flow
Rate
gpm
0
0
0
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
Totalizer
gal
7328
7328
7328
7710
8022
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
8931
9248
9734
10538
10538
10538
10538
10538
10538
10538
10538
10538
10538
10538
10538
10538
10538
10538
10858
12088
12088
12088
12088
12088
12088
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
06/22/05 10:30
06/23/05 10:07
06/24/05 15:02
06/27/05 13:55
06/28/05 15:24
06/29/05 09:46
06/30/05 09:55
07/01/05 15:48
07/05/0514:11
07/06/05 08:00
07/07/05 08:58
07/08/05 16:05
07/11/0515:07
07/12/05 14:38
07/13/05 10:30
07/14/0509:30
07/18/0509:32
07/19/0509:51
07/20/0517:07
07/21/05 13:24
07/22/05 16:01
07/25/05 09:30
07/26/05 08:30
07/27/05 13:30
07/28/05 10:00
07/29/05 1 1 :00
08/01/05 12:00
08/02/05 14:03
08/03/05 15:32
08/04/05 09:05
08/05/05 16:04
08/08/05 10:45
08/09/05 09:30
08/10/05 12:30
08/11/0511:30
08/12/05 16:44
08/15/0509:33
08/17/0513:15
08/18/0509:49
08/19/05 14:59
08/22/05 10:24
08/23/05 10:28
08/24/0517:07
08/25/05 09:35
08/26/0516:18
08/29/0510:18
Hour
Meter
hr
2769.8
2781.7
2798.8
NA
2847.9
2854.5
2866.8
2884.9
2932.1
2938.3
2951.1
2970.5
3006.1
3017.8
3026.1
3036.9
3085.8
3098.4
3117.8
3126.3
3139.9
3170.2
3181.3
3196.5
3205.3
3218.9
3256.2
3270.2
3283.4
3289.1
3308.2
3339.5
3350.7
3365.6
3376.9
3394.0
3423.4
3449.3
3457.7
3475.0
3507.0
3518.9
3538.1
3542.8
3561.7
3592.1
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
ON
ON
OFF
ON
ON
ON
ON
OFF
OFF
ON
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
ON
OFF
ON
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
29
29
32
30
29
30
30
34
30
30
33
31
28
32
33
33
31
32
32
28
32
32
32
32
31
29
32
29
30
32
33
32
32
32
32
33
32
32
32
32
32
32
31
31
32
32
Totalizer
gal
8472259
8494850
852861 7
8596930
8623299
8636181
8660434
8695429
8786414
8798083
8822760
8859990
8927782
8949528
8965572
8988425
9077394
9100845
9137432
9153108
9179099
9236804
9257866
9286958
9303471
9329436
9400245
942721 1
9452963
9464168
9500919
9561 750
9583390
9612512
9634529
9667841
9724754
9774656
9790540
9823674
9884693
9908120
9944394
9953242
9989501
10047028
Cum. Flow
gal
8448288
8470879
8504646
8572959
8599328
8612210
8636463
8671458
8762443
8774112
8798789
8836019
890381 1
8925557
8941601
8964454
9053423
9076874
9113461
9129137
9155128
9212833
9233895
9262987
9279500
9305465
9376274
9403240
9428992
9440197
9476948
9537779
9559419
9588541
9610558
9643870
9700783
9750685
9766569
9799703
9860722
9884149
9920423
9929271
9965530
10023057
Bed
Volume
51339
51476
51681
52096
52256
52335
52482
52695
53248
53319
53469
53695
54107
54239
54336
54475
55016
55158
55381
55476
55634
55985
56113
56289
56390
56548
56978
57142
57298
57366
57590
57959
58091
58268
58402
58604
58950
59253
59350
59551
59922
60064
60285
60338
60559
60908
Tank B Flow Meter
Flowr
ate
gpm
28
29
32
29
28
30
30
33
30
28
32
30
28
32
32
32
32
30
30
28
30
31
31
31
30
29
31
30
29
29
29
30
31
31
31
32
30
33
27
31
32
32
31
31
32
32
Totalizer
gal
8350099
8372309
8405363
8472476
8498135
8510646
8534051
8567897
8656450
8667915
8691560
8727748
8793516
8814692
8830271
8849575
8939776
8962875
8998883
9014321
9039784
9096171
9116834
9145039
9161253
9186908
9256407
9282369
9307022
9317756
9353436
9411832
9432561
9460748
9481779
9513861
9568794
9617017
9632641
9665271
9725167
9747914
9783282
9791942
9827501
9883968
Cum. Flow
gal
8326805
8349015
8382069
8449182
8474841
8487352
8510757
8544603
8633156
8644621
8668266
8704454
8770222
8791398
8806977
8826281
8916482
8939581
8975589
8991027
9016490
9072877
9093540
9121745
9137959
9163614
9233113
9259075
9283728
9294462
9330142
9388538
9409267
9437454
9458485
9490567
9545500
9593723
9609347
9641977
9701873
9724620
9759988
9768648
9804207
9860674
Bed
Volume
25300
25368
25468
25672
25750
25788
25859
25962
26231
26266
26338
26448
26647
26712
26759
26818
27092
27162
27271
27318
27396
27567
27630
27716
27765
27843
28054
28133
28208
28240
28349
28526
28589
28675
28739
28836
29003
29150
29197
29296
29478
29547
29655
29681
29789
29961
dP
TA
psi
4.7
4.5
5.4
4.4
4.4
4.8
4.9
5.4
5.0
4.9
5.5
5.6
4.5
5.1
5.1
5.1
5.2
5.2
5.2
4.0
5.1
5.1
5.1
5.0
5.1
4.1
5.1
4.4
4.5
5.0
5.0
5.0
5.0
5.1
5.1
5.1
5.0
5.1
5.5
5.4
5.5
5.0
5.2
5.4
5.2
5.4
TB
psi
4.2
4.2
5.0
4.3
4.1
4.2
4.4
5.0
5.0
4.3
5.0
5.0
4.0
4.9
5.0
5.0
4.9
5.0
5.0
4.0
5.0
5.0
5.0
4.9
4.9
4.0
5.0
4.1
4.2
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
4.8
5.0
5.0
4.9
5.0
4.9
Pressure
Inlet
psig
111
109
105
109
110
109
109
105
105
105
105
105
110
105
106
106
105
105
105
110
105
104
105
104
105
109
106
109
109
108
107
106
107
107
107
107
106
107
107
105
108
107
107
108
107
107
Between
Tanks
psig
103
103
98
103
103
102
101
98
97
100
97
97
102
87
98
98
97
97
97
103
97
97
98
97
97
102
97
101
101
97
97
97
97
97
97
97
97
97
97
97
97
97
97
97
97
87
Outlet
psig
100
95
90
96
97
96
95
90
90
90
90
90
96
90
90
90
92
90
90
96
90
90
90
90
90
98
95
96
93
92
91
89
92
90
90
92
89
90
90
90
92
92
90
92
90
90
Recycling
Flow
Rate
gpm
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0.5
0.5
0
0
0
0
0
0
Totalizer
gal
12088
12088
12088
12088
12088
12088
12088
12088
12088
12088
12418
12942
13452
13452
13452
13452
13452
13452
13452
13452
13452
13452
13452
13747
13747
13747
13747
13747
13747
13747
13747
13747
13747
13747
13747
13747
13747
13890
14127
14618
15115
15115
15115
15115
15115
15115
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
08/30/05 14:03
08/31/05 14:00
09/01/0509:56
09/02/0517:31
09/06/0517:34
09/07/05 08:46
09/09/05 14:24
09/12/05 18:04
09/13/0508:57
09/14/0510:15
09/16/05 16:57
09/19/05 16:50
09/20/0509:12
09/21/0509:47
09/22/05 16:29
09/23/05 16:00
09/26/05 15:36
09/27/05 09:23
09/28/05 09:47
09/29/05 1 1 :23
09/30/05 15:09
10/03/0510:08
10/04/0514:35
10/05/0511:00
10/06/0509:12
10/07/0515:35
10/14/0511:00
10/17/0516:18
10/18/0509:30
10/19/0518:17
10/20/0510:12
10/21/0517:26
10/24/0511:00
10/25/0511:00
10/26/0510:19
10/27/0509:24
10/28/0514:04
10/31/0511:06
11/01/0517:01
11/02/0509:43
11/03/0511:47
11/04/0516:39
11/07/0510:24
11/08/0510:57
11/09/0512:00
11/14/0510:40
Hour
Meter
hr
3608.2
3620.8
3628.4
3648.1
3696.9
3700.3
3730.3
3770.4
3773.6
3787.1
3818.1
3854.6
3859.2
3871.9
3890.9
3902.5
3938.8
3944.8
3957.2
3971.2
3987.1
4018.7
4035.3
4043.9
4054.3
4072.9
4155.9
4195.5
4200.9
4221.8
4226.0
4245.4
4275.9
4288.8
4299.3
4310.5
4320.0
4353.6
4371.7
4376.6
4389.7
4406.8
4437 .1
4449.9
NA
4522.7
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
31
32
32
30
30
31
32
32
31
31
31
31
31
28
31
32
31
31
28
32
30
32
31
29
31
31
32
31
31
31
31
29
32
31
31
30
31
31
30
32
31
31
32
28
32
31
Totalizer
gal
10076976
10099296
10115320
10152861
10245525
10252019
10309110
10385368
10391055
10416438
10475134
10543917
10552372
10576374
10612198
10634175
10702288
10713714
10737217
10763271
10793468
10852841
10883701
10899707
10919178
10954110
11106988
11185423
11195564
11234854
11242548
11278815
11336213
11360491
11379945
11401267
11419110
11482442
11516502
11525818
11550593
11584807
11640019
11664539
11688867
11802270
Cum. Flow
gal
10053005
10075325
10091349
10128890
10221554
10228048
10285139
10361397
10367084
10392467
10451163
10519946
10528401
10552403
10588227
10610204
10678317
10689743
10713246
10739300
10769497
10828870
10859730
10875736
10895207
10930139
11083017
11161452
11171593
11210883
11218577
11254844
11312242
11336520
11355974
11377296
11395139
11458471
11492531
11501847
11526622
11560836
11616048
11640568
11664896
1 1 778299
Bed
Volume
61090
61226
61323
61551
62114
62154
62501
62964
62999
63153
63510
63928
63979
64125
64343
64476
64890
64960
65102
65261
65444
65805
65993
66090
66208
66420
67349
67826
67888
68126
68173
68394
68742
68890
69008
69138
69246
69631
69838
69895
70045
70253
70589
70738
70885
71574
Tank B Flow Meter
Flowr
ate
gpm
31
31
31
28
30
30
32
30
30
30
32
32
30
26
30
31
30
30
25
32
31
32
29
25
31
30
30
31
30
29
30
26
31
30
30
30
31
31
30
31
30
31
30
27
31
30
Totalizer
gal
9913251
9934131
9950753
9987510
10078371
10084718
10140652
10215455
10221043
10246065
10303863
10371487
10379847
10403492
10438705
10460351
10527599
10538885
10562096
10587778
10617574
10676208
10706699
10722505
10741755
10776250
10927069
11004554
11014569
11053414
11061031
11096836
11153520
1 1 1 77498
11196745
11217774
11235400
11297916
11331497
11340668
11365192
11396879
11453255
11477493
11501543
11613126
Cum. Flow
gal
9889957
9910837
9927459
9964216
10055077
10061424
10117358
10192161
10197749
10222771
10280569
10348193
10356553
10380198
10415411
10437057
10504305
10515591
10538802
10564484
10594280
10652914
10683405
10699211
10718461
10752956
10903775
10981260
10991275
11030120
11037737
11073542
11130226
11154204
11173451
11194480
11212106
11274622
11308203
11317374
11341898
11373585
11429961
11454199
11478249
11589832
Bed
Volume
30050
30113
30164
30275
30551
30571
30741
30968
30985
31061
31237
31442
31467
31539
31646
31712
31916
31951
32021
32099
32190
32368
32461
32509
32567
32672
33130
33366
33396
33514
33537
33646
33818
33891
33949
34013
34067
34257
34359
34387
34461
34558
34729
34803
34876
35215
dP
TA
psi
5.0
5.0
5.0
4.2
5.0
5.2
5.0
5.0
5.4
5.1
5.2
5.1
5.1
4.2
5.4
5.1
5.0
5.1
4.5
5.2
5.1
5.5
5.3
4.2
5.1
5.0
5.5
5.4
5.0
5.0
5.0
4.5
5.1
5.0
5.0
5.0
5.0
5.5
5.0
5.2
5.2
5.3
6.0
4.0
5.0
5.1
TB
psi
4.6
4.6
4.6
4.0
5.0
4.9
5.0
5.0
5.0
5.0
5.0
4.9
4.9
4.0
5.0
5.0
5.0
5.0
4.0
5.0
4.9
5.0
5.0
4.0
4.8
4.8
4.8
5.0
4.8
4.8
5.0
4.1
5.0
4.9
5.0
4.5
4.6
5.0
4.5
5.0
4.5
4.9
5.5
3.9
4.9
4.9
Pressure
Inlet
psig
106
107
107
109
108
108
107
107
106
106
107
107
108
112
108
108
108
108
111
108
107
107
107
112
108
108
108
108
108
108
108
110
108
108
108
108
108
108
108
107
108
106
110
112
110
108
Between
Tanks
psig
87
87
87
101
97
97
97
97
97
97
97
97
97
103
97
96
97
97
100
97
96
96
97
104
97
97
92
96
97
97
97
102
96
96
97
97
96
96
97
90
87
97
97
103
97
96
Outlet
psig
90
90
92
96
92
90
90
90
90
90
90
90
90
96
90
92
92
92
96
92
92
90
92
98
92
92
90
92
92
92
92
96
92
92
90
92
90
90
92
90
90
90
92
99
92
90
Recycling
Flow
Rate
gpm
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
15115
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
11/15/0517:00
11/16/0516:27
11/17/0510:19
11/21/0509:36
11/22/0513:20
11/28/0510:37
11/29/0509:41
11/30/0510:12
12/01/0514:12
12/02/0514:22
12/05/0517:26
12/06/0511:35
12/07/0509:30
12/08/0511:26
12/09/0512:47
12/12/0513:41
12/13/0515:30
12/14/0510:00
12/15/0510:24
12/19/0509:00
12/20/0510:30
12/21/0510:00
12/22/0516:46
12/27/0511:57
12/28/0510:00
12/29/0509:09
01/03/0617:11
01/04/0610:52
01/05/06 08:30
01/06/0615:10
01/09/06 08:32
01/10/0616:42
01/11/0609:25
01/12/0609:58
01/13/06 15:28
01/16/0609:59
01/17/0612:30
01/18/0617:05
01/19/06 10:00
01/20/0616:14
01/23/06 09:28
01/24/06 16:39
01/25/0616:18
01/26/06 13:24
01/30/06 09:40
01/31/0610:12
Hour
Meter
hr
4536.0
4552.7
4558.7
4606.8
4622.7
4693.1
4704.4
4717.1
4733.3
4745.7
4785.3
4791.7
4801.3
4815.4
4828.9
4865.3
4879.6
4886.1
4898.6
4945.6
4959.0
4970.7
4989.9
5046.0
5056.2
5067.6
5136.6
5142.4
5152.2
5171.1
5201.1
5221.4
5226.3
5239.1
5256.5
5287.6
5302.3
5319.1
5324.3
5342.6
5372.4
5391 .8
5403.6
5412.9
5458.0
5470.0
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
OFF
ON
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
ON
OFF
Tank A Flow Meter
Flowr
ate
gpm
31
27
32
31
31
31
29
32
31
31
32
31
32
31
31
30
31
31
30
31
31
30
31
31
31
32
31
32
30
31
28
32
31
31
32
31
31
30
31
29
28
30
31
31
28
32
Totalizer
gal
11826912
11858080
11869513
11959525
11989320
12121394
12142811
12166165
12196751
12219644
12293908
12305709
12323575
12350329
12375855
12444309
12470869
12483160
12506930
12594669
12619722
12642262
12677448
12782236
12801474
12822799
12951474
12962384
12980720
13016134
13072457
13110211
13119286
13143237
13175833
13234001
13261493
13292885
13302588
13336767
13392515
13428623
13450751
13468232
13552347
13574880
Cum. Flow
gal
11802941
11834109
11845542
11935554
11965349
12097423
12118840
12142194
12172780
12195673
12269937
12281738
12299604
12326358
12351884
12420338
12446898
12459189
12482959
12570698
12595751
12618291
12653477
12758265
12777503
12798828
12927503
12938413
12956749
12992163
13048486
13086240
13095315
13119266
13151862
13210030
13237522
13268914
13278617
13312796
13368544
13404652
13426780
13444261
13528376
13550909
Bed
Volume
71724
71914
71983
72530
72711
73514
73644
73786
73972
74111
74562
74634
74742
74905
75060
75476
75637
75712
75857
76390
76542
76679
76893
77530
77646
77776
78558
78624
78736
78951
79293
79523
79578
79723
79921
80275
80442
80633
80692
80899
81238
81458
81592
81698
82209
82346
Tank B Flow Meter
Flowr
ate
gpm
30
29
33
27
31
31
29
30
30
30
31
31
31
32
32
31
30
30
30
31
31
30
32
30
30
31
30
30
33
32
25
31
28
30
29
30
29
30
30
27
28
30
29
30
30
29
Totalizer
gal
11637458
11668285
11679599
11768503
11797907
11928098
11949244
11972288
12002502
12025126
12098345
12109942
12127187
12153894
12178641
12246261
12272512
12284644
12307967
12394830
12419638
12441925
12475779
12580323
12599304
12620385
12747775
12758551
12776667
12811702
12867467
12904801
12913760
12937427
12969599
13027239
13054497
13085544
13095162
13129051
13184043
13219770
13241694
13259030
13342307
13364371
Cum. Flow
gal
11614164
11644991
11656305
1 1 745209
11774613
11904804
11925950
11948994
11979208
12001832
12075051
12086648
12103893
12130600
12155347
12222967
12249218
12261350
12284673
12371536
12396344
12418631
12452485
12557029
12576010
12597091
12724481
12735257
12753373
12788408
12844173
12881507
12890466
12914133
12946305
13003945
13031203
13062250
13071868
13105757
13160749
13196476
13218400
13235736
13319013
13341077
Bed
Volume
35289
35382
35417
35687
35776
36172
36236
36306
36398
36466
36689
36724
36777
36858
36933
37138
37218
37255
37326
37590
37665
37733
37836
38153
38211
38275
38662
38695
38750
38856
39026
39139
39166
39238
39336
39511
39594
39688
39718
39821
39988
40096
40163
40216
40469
40536
dP
TA
psi
5.1
4.0
5.2
5.0
5.0
5.0
4.5
5.0
5.1
5.0
5.0
5.0
5.1
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.1
5.1
5.0
5.2
5.0
5.0
5.2
4.1
5.1
5.1
5.1
5.5
5.0
5.0
5.0
5.1
4.5
4.2
5.0
5.0
5.0
4.1
5.0
TB
psi
4.9
4.0
5.0
4.5
4.6
4.9
4.0
4.5
5.0
5.0
4.6
4.6
4.8
4.5
4.5
4.6
4.8
4.8
4.8
4.9
4.9
4.9
5.0
4.8
4.9
5.0
4.9
4.9
4.9
5.0
3.8
4.9
5.0
4.9
5.0
4.8
5.0
4.9
5.0
3.9
4.0
4.8
5.0
5.0
3.9
5.0
Pressure
Inlet
psig
108
112
105
108
108
107
110
108
105
108
108
108
108
108
108
108
108
108
108
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
100
103
102
102
102
105
105
102
102
102
107
102
Between
Tanks
psig
96
104
97
97
97
97
102
97
96
97
96
97
97
96
97
98
97
97
97
97
97
97
97
97
97
97
97
96
97
97
103
97
97
97
97
97
97
97
97
100
102
98
97
97
102
97
Outlet
psig
90
96
92
90
90
90
96
92
90
90
92
90
90
92
92
92
92
92
90
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
89
90
90
90
90
95
96
90
90
90
95
90
Recycling
Flow
Rate
gpm
0.5
0.5
0.5
0
0
0
0
0
0
0
0
0
0.5
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
15522
16010
16189
16334
16334
16334
16334
16334
16334
16334
16334
16334
16445
16859
16970
16969
16969
16969
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
02/01/06 10:21
02/02/06 1 1 :26
02/03/06 16:43
02/06/06 09:36
02/07/06 10:39
02/08/06 09:31
02/09/06 09:03
02/10/06 14:24
02/13/0609:57
02/14/06 13:00
02/15/0609:00
02/17/0613:25
02/21/06 10:24
02/22/06 09:39
02/23/06 09:08
02/24/06 13:00
02/27/0610:12
02/28/06 10:03
03/01/0609:46
03/02/06 09:25
03/06/06 08:56
03/07/06 08:36
03/08/06 10:30
03/09/06 14:52
03/10/06 14:38
03/13/0609:24
03/14/0609:07
03/15/0609:09
03/16/06 10:30
03/20/06 10:00
03/21/06 16:26
03/22/06 14:58
03/24/06 16:50
03/27/06 09:02
03/29/06 09:48
03/31/06 16:24
04/03/06 09:04
04/04/06 14:46
04/05/0609:14
04/06/06 10:20
04/07/06 16:25
04/10/06 10:02
04/11/0609:57
04/12/0610:18
04/13/0609:35
04/14/06 14:21
Hour
Meter
hr
5482.4
5495.7
5513.1
5542.6
5555.9
5566.9
5578.7
5596.2
5628.4
5644.1
5651.9
5680.3
5726.2
5737.6
5749.2
5765.7
5799.1
5811.1
5823.1
5834.9
5883.2
5895.1
5909.3
5925.7
5937.7
5969.1
5981.0
5993.2
6006.7
6054.4
6073.7
6084.4
6110.7
6139.5
6164.6
6195.7
6224.9
6242.8
6249.4
6262.7
6281.0
631 1 .2
6323.3
6335.9
6347.3
6364.3
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
Well #3
On/Off
ON
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
28
32
28
31
31
32
31
30
31
31
31
31
30
31
30
31
31
32
31
30
32
32
32
31
31
30
31
27
30
31
31
32
29
31
30
30
31
30
31
30
31
31
31
32
31
30
Totalizer
gal
13597797
13622566
13655366
13710347
13735360
13756133
13777697
13810507
13870469
13899550
13914029
13967257
14052141
14073075
14094513
14124826
14186417
14208458
14230332
14251995
14341511
14363575
14389539
14419956
14442175
14499221
14521661
14544115
14568595
14657330
14693234
14713145
14761852
14815294
14861749
14919782
14974180
15007455
15019762
15044705
15078882
15134563
15157471
15180919
15202283
15234224
Cum. Flow
gal
13573826
13598595
13631395
13686376
13711389
13732162
13753726
13786536
13846498
13875579
13890058
13943286
14028170
14049104
14070542
14100855
14162446
14184487
14206361
14228024
14317540
14339604
14365568
14395985
14418204
14475250
14497690
14520144
14544624
14633359
14669263
14689174
14737881
14791323
14837778
14895811
14950209
14983484
14995791
15020734
15054911
15110592
15133500
15156948
15178312
15210253
Bed
Volume
82486
82636
82835
83170
83322
83448
83579
83778
84143
84319
84407
84731
85247
85374
85504
85688
86063
86196
86329
86461
87005
87139
87297
87482
87617
87963
88100
88236
88385
88924
89142
89263
89559
89884
90166
90519
90850
91052
91127
91278
91486
91824
91963
92106
92236
92430
Tank B Flow Meter
Flowr
ate
gpm
29
30
30
32
31
30
31
29
30
30
30
29
30
30
31
31
31
32
33
31
30
30
30
29
29
32
28
29
29
30
32
32
27
30
28
28
31
29
30
30
28
28
28
33
30
32
Totalizer
gal
13387078
13411577
13444092
13498557
13523375
13543974
13565327
13597829
13657256
13686045
13700395
13752459
13836534
13857251
13878460
13908472
13969479
13991295
14012925
14034347
14122679
14144475
14170139
14200242
14222212
14279124
14300850
14323065
14347291
14435059
14470576
14490217
14538348
14591157
14637115
14694554
14748252
14781152
14793291
14817909
14851638
14906823
14929104
14952248
14973340
15004900
Cum. Flow
gal
13363784
13388283
13420798
13475263
13500081
13520680
13542033
13574535
13633962
13662751
13677101
13729165
13813240
13833957
13855166
13885178
13946185
13968001
13989631
14011053
14099385
14121181
14146845
14176948
14198918
14255830
14277556
14299771
14323997
14411765
14447282
14466923
14515054
14567863
14613821
14671260
14724958
14757858
14769997
14794615
14828344
14883529
14905810
14928954
14950046
14981606
Bed
Volume
40605
40679
40778
40943
41019
41081
41146
41245
41426
41513
41557
41715
41970
42033
42098
42189
42374
42440
42506
42571
42840
42906
42984
43075
43142
43315
43381
43449
43522
43789
43897
43956
44103
44263
44403
44577
44740
44840
44877
44952
45055
45222
45290
45360
45424
45520
dP
TA
psi
4.0
5.0
4.5
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
4.1
5.0
5.0
5.0
5.1
4.2
5.0
5.0
5.0
5.0
5.2
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
TB
psi
3.9
5.0
4.0
5.0
4.9
4.9
4.7
5.0
4.9
4.8
4.8
4.9
4.5
4.8
4.9
4.9
4.5
4.5
4.4
4.5
4.5
4.5
4.4
4.5
4.5
4.5
4.9
3.9
4.9
4.8
5.0
4.9
4.0
4.5
5.0
5.0
4.9
5.0
5.0
4.9
5.0
5.0
5.0
5.0
5.0
5.0
Pressure
Inlet
psig
108
102
105
103
103
103
104
101
103
102
102
103
103
102
103
105
102
102
103
103
103
103
105
103
103
103
103
106
103
104
104
103
105
103
104
103
104
102
104
103
102
103
103
102
102
103
Between
Tanks
psig
104
97
101
97
97
97
97
96
97
97
97
97
97
96
96
96
97
97
97
97
97
97
97
97
97
96
96
103
96
96
96
96
101
97
96
97
97
97
97
97
97
97
97
97
97
98
Outlet
psig
98
90
95
90
90
90
90
90
90
89
89
90
90
90
90
90
90
90
90
91
91
90
90
90
90
90
90
97
90
91
91
90
95
91
90
90
91
90
91
91
90
90
90
90
90
90
Recycling
Flow
Rate
gpm
0
0
0
0
0
0
0
0
0
0
0
0.5
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17046
17871
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
04/17/0609:55
04/18/06 10:30
04/19/0608:00
04/20/0609:15
04/21/06 15:04
04/24/06 08:57
04/26/06 10:17
04/28/06 15:44
05/01/0609:24
05/02/06 10:54
05/03/06 08:56
05/05/06 15:23
05/08/06 09:02
05/09/06 09:24
05/10/06 10:25
05/11/06 10:42
05/12/06 15:01
05/15/06 10:11
05/17/0608:50
05/22/06 09:50
05/24/06 10:00
05/31/06 10:35
06/12/0609:06
06/14/06 14:26
06/19/0609:41
06/21/0609:16
06/28/06 10:06
07/03/06 10:10
07/05/06 09:41
07/10/0609:53
07/12/06 12:15
07/17/0608:30
07/19/06 10:30
07/24/06 10:18
07/31/06 10:13
08/02/06 09:51
08/07/06 09:55
08/09/06 09:46
08/14/06 10:12
08/16/06 10:43
08/23/06 17:20
08/28/06 08:31
11/07/0600:00
11/27/0610:45
11/28/0608:40
12/04/0614:00
Hour
Meter
hr
6396.5
6409.2
6419.0
6432.4
6450.6
6480.8
6491.5
6521.3
6551.6
6565.3
6575.5
6608.4
6636.6
6649.2
6662.4
6674.9
6691.4
6723.2
6746.2
6808.0
6832.6
6918.5
7063.5
7093.1
7149.3
7173.3
7259.5
7320.6
7344.5
7405.4
7432.2
7489.6
7516.1
7576.5
7661.8
7685.9
7746.9
7771.2
7832.6
7857.5
7949.3
8001.5
NA
8052.6
8062.8
8141.2
Lead/L
ag
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
A/B
NA
B/A
B/A
B/A
Well #3
On/Off
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
ON
ON
OFF
ON
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
OFF
NA
OFF
ON
OFF
Tank A Flow Meter
Flowr
ate
gpm
32
31
32
31
31
30
30
31
30
30
31
32
32
28
31
30
31
30
30
29
29
29
27
22
24
22
24
22
23
23
22
22
22
21
20
20
20
20
19
19
18
18
NA
32
26
33
Totalizer
gal
15294114
15317499
15335733
15360560
15393895
15450227
15470207
15526235
15582515
15608029
15626650
15683501
15738939
15761981
15786431
15809513
15839966
15898105
15940100
16052050
16096980
16249404
16493174
16538489
16619819
16654163
16776981
16862233
16894723
16979702
17016599
17089490
17123085
17199655
17306311
17336224
17412012
17441042
17513794
17545866
17647726
17703458
NA
17733317
17752542
17903261
Cum. Flow
gal
15270143
15293528
15311762
15336589
15369924
15426256
15446236
15502264
15558544
15584058
15602679
15659530
15714968
15738010
15762460
15785542
15815995
15874134
15916129
16028079
16073009
16225433
16469203
16514518
16595848
16630192
16753010
16838262
16870752
16955731
16992628
17065519
17099114
17175684
17282340
17312253
17388041
17417071
17489823
17521895
17623755
17679487
NA
0
19225
169944
Bed
Volume
92794
92936
93047
93198
93400
93742
93864
94204
94546
94701
94815
95160
95497
95637
95785
95926
96111
96464
96719
97400
97673
98599
100080
100356
100850
101059
101805
102323
102520
103037
103261
103704
103908
104373
105022
105203
105664
105840
106282
106477
107096
107435
NA
NA
58
516
Tank B Flow Meter
Flowr
ate
gpm
31
31
31
31
30
33
30
30
29
33
30
32
31
26
30
32
31
30
32
27
30
27
26
20
25
22
22
20
22
22
22
22
22
20
20
21
20
19
17
19
16
16
NA
30
25
30
Totalizer
gal
15064081
15087194
15105208
15129713
15162566
15218285
15238095
15293195
15348554
15373668
1539
15447916
15502595
15525303
15549413
15572156
15602128
15659420
15700792
15811485
15854988
16005244
16245932
16290798
16371519
16405587
16527171
16611740
16644007
16728392
16764976
16837581
16871032
16947251
1 7053404
1 7083209
17158558
17187481
1 7260085
17291792
17393291
1 7448958
NA
17479226
1 7496940
1 7634963
Cum. Flow
gal
15040787
15063900
15081914
15106419
15139272
15194991
15214801
15269901
15325260
15350374
NA
15424622
15479301
15502009
15526119
15548862
15578834
15636126
15677498
15788191
15831694
15981950
16222638
16267504
16348225
16382293
16503877
16588446
16620713
16705098
16741682
16814287
16847738
16923957
17030110
17059915
17135264
17164187
17236791
17268498
17369997
17425664
NA
0
17714
155737
Bed
Volume
45700
45770
45825
45899
45999
46169
46229
46396
46564
46641
NA
46866
47032
47101
47175
47244
47335
47509
47635
47971
48103
48560
49291
49427
49673
49776
50145
50402
50500
50757
50868
51089
51190
51422
51744
51835
52064
52152
52372
52469
52777
52946
NA
0
108
946
dP
TA
psi
5.5
5.1
5.1
5.1
5.5
5.0
5.2
5.0
5.0
5.0
5.1
5.0
5.0
4.1
5.0
5.1
5.0
5.0
4.9
5.0
4.6
4.5
4.0
2.9
3.0
2.9
3.0
3.0
3.0
4.0
2.5
2.5
2.5
2.5
2.2
2.2
2.0
2.0
2.0
2.0
1.5
1.5
NA
4.1
3.0
4.0
TB
psi
5.0
5.0
5.0
5.0
5.0
4.9
4.8
4.8
4.9
4.9
4.9
5.0
4.8
3.9
5.0
5.0
4.5
4.9
4.5
4.1
4.2
4.0
3.5
2.5
2.9
2.1
2.8
3.0
2.5
3.5
2.0
2.0
2.0
2.0
2.0
2.0
2.0
1.9
2.0
2.0
1.8
1.5
NA
3.8
3.0
4.0
Pressure
Inlet
psig
102
102
102
102
102
103
102
103
102
101
102
103
102
105
102
101
102
101
103
102
101
100
104
101
96
101
96
96
98
95
94
95
95
92
95
95
94
94
93
93
94
93
NA
103
109
102
Between
Tanks
psig
97
97
97
97
98
98
97
98
98
97
97
97
97
102
97
98
97
97
97
96
97
97
101
96
84
100
94
94
94
95
92
93
93
92
94
93
93
93
93
92
90
93
NA
100
106
101
Outlet
psig
90
90
90
90
90
91
90
91
90
90
90
91
91
96
90
90
90
91
92
91
91
91
96
90
90
93
90
90
92
90
89
90
90
90
90
90
90
90
90
90
91
91
NA
93
102
93
Recycling
Flow
Rate
gpm
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0.5
0
0
NA
0
0
0
Totalizer
gal
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
18147
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19153
19182
19857
19857
NA
19857
19857
19857
-------
EPA Arsenic Demonstration Project at Rimrock, AZ - Daily System Operation Log Sheet
Date and Time
12/11/0610:30
12/18/0609:00
12/27/0610:13
01/03/07 00:00
02/07/07 09:30
03/07/0707:15
03/28/07 1 1 :30
Hour
Meter
hr
8294.1
8460.6
8677.6
8844.2
9684.4
10223
10482
Lead/L
ag
A/B
B/A
B/A
B/A
B/A
B/A
B/A
B/A
Well #3
On/Off
OFF
OFF
OFF
OFF
OFF
OFF
OFF
Tank A Flow Meter
Flowr
ate
gpm
34
33
33
33
32
32
32
Totalizer
gal
18202419
18530106
18956487
19281942
20921512
21958312
22449876
Cum. Flow
gal
469102
796789
1223170
1548625
3188195
4224995
4716559
Bed
Volume
1425
2421
3716
4705
9687
12837
14331
Tank B Flow Meter
Flowr
ate
gpm
30
30
30
30
29
29
28
Totalizer
gal
17912510
18216417
18612813
18915750
20435149
21395094
21849540
Cum. Flow
gal
433284
737191
1133587
1436524
2955923
3915868
4370314
Bed
Volume
2633
4480
6889
8729
17963
23796
26558
dP
TA
psi
4.1
4.1
4.1
4.1
4.1
4.1
3.9
TB
psi
4.0
4.0
4.0
4.0
4.0
4.0
3.9
Pressure
Inlet
psig
102
102
104
104
103
103
103
Between
Tanks
psig
101
101
100
101
100
101
101
Outlet
psig
93
93
93
93
93
94
94
Recycling
Flow
Rate
gpm
0
0
0
0
0
0
0.5
Totalizer
gal
19857
19857
19857
19857
19857
19857
19871
Note: Bed volume calculation based on 22 ft3 of media per vessel.
Highlighted rows indicate backwash; highlighted columns indicated calculated values; NA = data not available.
>
-------
APPENDIX B
ANALYTICAL DATA TABLES
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
mg/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
Hg/L
|xg/L
re/L
re/L
|xg/L
06/30/04
IN
-
355
0.3
9.4
0.3
<0.1
26.0
0.5
7.0
21.5
3.8
475
-
-
287
171
116
59.2
59.1
0.1
0.8
58.3
<25
<25
1.0
1.1
AC
-
-
-
-
-
-
-
-
7.4
21.2
4.9
637
0.4
0.6
-
-
-
-
-
-
-
-
-
-
-
-
TA
0.9
367
0.3
9.4
0.3
<0.1
25.4
0.3
7.0
22.9
3.6
637
0.4
0.6
298
175
123
1.0
0.9
0.1
0.6
0.3
<25
<25
0.4
0.7
TB
0.4
351
0.3
9.4
0.3
<0.1
23.9
0.4
7.0
23.7
3.8
649
0.4
0.6
299
174
124
0.3
0.3
<0.1
0.3
<0.1
<25
<25
0.4
0.6
07/07/04
IN
-
330
-
-
-
<0.1
25.7
0.3
7.0
24.1
4.1
476
-
-
-
-
-
78.5
-
-
-
-
<25
-
0.7
-
AC
-
-
-
-
-
-
-
-
7.2
22.3
5.0
596
0.4
0.7
-
-
-
-
-
-
-
-
-
-
-
-
TA
1.8
382
-
-
-
<0.1
24.4
0.2
7.0
21.9
4.1
596
0.4
0.6
-
-
-
1.2
-
-
-
-
<25
-
<0.1
-
TB
0.9
365
-
-
-
<0.1
24.1
0.6
7.0
22.1
3.7
611
0.4
0.5
-
-
-
0.3
-
-
-
-
<25
-
<0.1
-
07/14/04
IN
-
383
-
-
-
<0.1
24.0
<0.1
7.0
22.4
3.5
488
-
-
-
-
-
79.2
-
-
-
-
<25
-
0.4
-
AC
-
-
-
-
-
-
-
-
7.2
22.4
4.7
607
0.4
0.6
-
-
-
-
-
-
-
-
-
-
-
-
TA
2.7
371
-
-
-
<0.1
24.3
0.2
7.1
22.7
3.7
619
0.4
0.6
-
-
-
0.8
-
-
-
-
<25
-
<0.1
-
TB
1.4
367
-
-
-
<0.1
23.9
0.9
7.1
23.1
3.6
628
0.4
0.6
-
-
-
0.3
-
-
-
-
<25
-
<0.1
-
07/21/04
IN
-
379
-
-
-
<0.1
26.1
0.3
6.9
24.1
4.7
510
-
-
-
-
-
58.8
-
-
-
-
<25
-
1.6
-
AC
-
-
-
-
-
-
-
-
7.2
23.5
6.8
608
0.5
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
3.7
375
-
-
-
<0.1
25.9
0.3
7.0
23.1
6.6
621
0.5
0.5
-
-
-
0.7
-
-
-
-
<25
-
0.4
-
TB
1.9
383
-
-
-
<0.1
25.1
0.4
7.0
23.2
6.9
624
0.4
0.5
-
-
-
0.4
-
-
-
-
47.3
-
0.4
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only);
TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/Lw
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/Lw
mg/Lw
mg/L(a)
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
07/28/04
IN
-
369
0.3
10.0
0.2
<0.1
24.6
0.2
7.0
26.1
4.4
484
-
-
351
208
143
56.0
57.6
<0.1
1.0
56.6
<25
<25
0.3
0.4
AC
-
-
-
-
-
-
-
-
7.2
24.5
5.5
590
0.5
0.6
-
-
-
-
-
-
-
-
-
-
-
-
TA
4.6
381
0.3
10.0
0.2
<0.1
24.5
0.3
7.1
26.7
4.2
599
0.5
0.6
397
236
161
1.0
1.0
<0.1
0.8
0.2
<25
<25
<0.1
<0.1
TB
2.3
377
0.3
10.0
0.2
<0.1
24.3
0.2
7.1
24.0
4.1
613
0.4
0.5
352
207
145
0.3
0.3
<0.1
0.6
<0.1
<25
<25
<0.1
<0.1
08/04/04
IN
-
379
-
-
-
<0.1
25.3
0.3
7.0
22.0
4.2
203
-
-
-
-
-
81.4
-
-
-
-
<25
-
0.5
-
AC
-
-
-
-
-
-
-
-
7.0
21.7
4.1
609
0.5
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
5.6
367
-
-
-
<0.1
25.6
0.3
7.0
21.0
4.0
634
0.4
0.5
-
-
-
1.4
-
-
-
-
<25
-
<0.1
-
TB
2.8
395
-
-
-
<0.1
25.0
0.5
7.0
21.1
3.8
647
0.4
0.5
-
-
-
0.3
-
-
-
-
<25
-
<0.1
-
08/11/04
IN
-
376
-
-
-
<0.1
25.3
0.1
7.0
21.9
4.2
247
-
-
-
-
-
57.0
-
-
-
-
<25
-
0.8
-
AC
-
-
-
-
-
-
-
-
7.2
21.0
5.8
587
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
6.6
376
-
-
-
<0.1
25.2
0.2
7.1
21.2
4.1
627
0.4
0.4
-
-
-
0.7
-
-
-
-
<25
-
0.2
-
TB
3.3
381
-
-
-
<0.1
25.0
0.1
7.0
21.1
4.1
641
0.4
0.4
-
-
-
0.3
-
-
-
-
<25
-
<0.1
-
08/18/04
IN
-
363
-
-
-
<0.1
25.6
0.3
7.0
22.0
4.1
239
-
-
-
-
-
48.3
-
-
-
-
<25
-
0.4
-
AC
-
-
-
-
-
-
-
-
7.4
21.7
4.5
552
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
7.5
375
-
-
-
<0.1
25.6
0.4
7.1
21.3
3.9
614
0.4
0.4
-
-
-
0.7
-
-
-
-
<25
-
<0.1
-
TB
3.7
367
-
-
-
<0.1
25.3
0.7
7.0
22.2
5.1
622
0.4
0.4
-
-
-
0.3
-
-
-
-
<25
-
0.1
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L(a)
mg/L(!l)
Hg/L
|xg/L
|xg/L
re/L
re/L
re/L
re/L
re/L
|xg/L
08/25/04
IN
-
359
0.3
10.0
0.2
<0.1
26.7
0.1
7.0
21.9
3.3
210
-
-
305
183
122
64.6
61.1
3.5
2.1
59.0
<25
<25
1.4
0.5
AC
-
-
-
-
-
-
-
-
7.0
21.2
4.7
610
0.5
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
8.5
363
0.3
9.8
0.2
<0.1
27.2
0.1
7.0
21.2
3.6
649
0.3
0.4
319
182
137
2.7
2.8
<0.1
2.7
0.1
<25
<25
1.2
0.3
TB
4.2
367
0.3
10.0
0.2
<0.1
26.9
<0.1
6.9
21.4
3.4
658
0.3
0.4
328
182
145
1.0
1.2
<0.1
1.1
0.1
<25
<25
0.9
0.1
09/01/04
IN
-
371
-
-
-
<0.1
25.3
0.1
7.1
21.2
4.6
213
-
-
-
-
-
77.5
-
-
-
-
<25
-
0.4
-
AC
-
-
-
-
-
-
-
-
7.6
21.6
4.5
608
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
9.4
375
-
-
-
<0.1
25.2
0.3
7.1
21.2
4.4
637
0.3
0.4
-
-
-
1.1
-
-
-
-
<25
-
<0.1
-
TB
4.7
371
-
-
-
<0.1
25.1
0.2
7.1
21.2
4.6
637
0.3
0.4
-
-
-
0.4
-
-
-
-
<25
-
<0.1
-
09/08/04
IN
-
383
-
-
-
<0.1
25.6
0.1
6.9
22.6
3.5
431
-
-
-
-
-
78.5
-
-
-
-
<25
-
0.3
-
AC
-
-
-
-
-
-
-
-
7.1
22.3
3.4
642
0.4
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
10.4
375
-
-
-
<0.1
25.2
0.1
6.9
21.5
3.6
668
0.4
0.5
-
-
-
1.1
-
-
-
-
<25
-
<0.1
-
TB
5.2
375
-
-
-
<0.1
25.6
0.2
6.9
22.0
3.5
685
0.4
0.5
-
-
-
0.4
-
-
-
-
<25
-
0.1
-
09/15/04
IN
-
372
376
-
-
-
<0.06
<0.06
25.9
25.6
0.6
0.5
7.1
21.5
3.8
226
-
-
-
-
-
55.3
60.2
-
-
-
-
<25
<25
-
0.4
0.3
-
AC
-
-
-
-
-
-
-
-
7.4
21.9
6.1
578
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
11.3
376
372
-
-
-
<0.06
<0.06
25.6
25.0
0.5
0.5
7.1
21.2
4.9
619
0.4
0.4
-
-
-
1.1
1.1
-
-
-
-
<25
<25
-
0.2
0.2
-
TB
5.6
372
384
-
-
-
<0.06
<0.06
25.9
25.5
0.6
0.5
7.1
21.3
4.7
633
0.4
0.4
-
-
-
0.5
0.3
-
-
-
-
<25
<25
-
0.1
<0.1
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/Lw
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
09/22/04
IN
-
369
0.4
8.9
0.2
<0.06
25.9
0.1
7.0
20.1
4.1
214
-
-
332
191
141
65.5
65.0
0.5
1.8
63.2
127
<25
0.8
0.4
AC
-
-
-
-
-
-
-
-
7.4
20.0
6.4
584
0.4
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
12.3
373
0.5
8.8
0.2
<0.06
25.7
<0.1
7.0
20.2
5.7
605
0.4
0.4
340
196
143
2.6
2.4
0.2
1.8
0.6
27
<25
0.3
0.1
TB
6.1
373
0.3
8.7
0.2
<0.06
25.6
0.1
7.0
20.3
4.2
622
0.4
0.4
332
201
131
1.0
0.7
0.3
0.2
0.5
56
<25
0.5
0.1
09/29/04
IN
-
369
-
-
-
<0.06
25.6
<0.1
7.0
20.9
4.1
224
-
-
-
-
-
53.5
-
-
-
-
<25
-
0.3
-
AC
-
-
-
-
-
-
-
-
7.0
21.0
5.2
568
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
13.4
369
-
-
-
<0.06
25.8
<0.1
7.0
21.0
4.4
605
0.3
0.4
-
-
-
1.4
-
-
-
-
<25
-
0.4
-
TB
6.6
369
-
-
-
<0.06
25.8
0.1
7.1
21.0
4.2
617
0.3
0.4
-
-
-
0.9
-
-
-
-
<25
-
0.2
-
10/06/04
IN
-
370
-
-
-
<0.06
25.7
0.3
7.0
20.8
3.9
148
-
-
-
-
-
54.1
-
-
-
-
<25
-
0.1
-
AC
-
-
-
-
-
-
-
-
7.0
20.6
6.3
552
0.2
0.2
-
-
-
-
-
-
-
-
-
-
-
-
TA
14.3
370
-
-
-
<0.06
25.6
0.5
7.0
20.7
3.5
590
0.2
0.2
-
-
-
2.1
-
-
-
-
<25
-
0.2
-
TB
7.1
370
-
-
-
<0.06
25.0
0.2
7.0
20.6
4.0
593
0.2
0.2
-
-
-
0.4
-
-
-
-
<25
-
<0.1
-
10/13/04
IN
-
353
-
-
-
<0.06
24.9
0.2
NA*'
NA*'
NA*'
NA*'
-
-
-
-
-
53.2
-
-
-
-
<25
-
0.4
-
AC
-
-
-
-
-
-
-
-
NA*'
NA*'
NA*'
NA*'
NA*'
NA*'
-
-
-
-
-
-
-
-
-
-
-
-
TA
15.3
345
-
-
-
<0.06
25.2
0.2
NA*'
NA*'
NA*'
NA*'
NA*'
NA*'
-
-
-
1.4
-
-
-
-
<25
-
<0.1
-
TB
7.6
353
-
-
-
<0.06
24.9
0.2
NA*'
NA*'
NA*'
NAW
NA*'
NAW
-
-
-
0.2
-
-
-
-
<25
-
<0.1
-
(a) As CaCO3. (b) Onsite water quality parameter not measured.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B; NA = data not available.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/Lw
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
10/20/04
IN
-
377
0.4
9.8
0.2
<0.06
24.9
0.1
7.0
20.1
4.0
190
-
-
366
214
152
50.8
50.2
0.6
2.2
48.0
<25
<25
0.6
1.0
AC
-
-
-
-
-
-
-
-
7.0
20.1
4.5
637
0.2
0.2
-
-
-
-
-
-
-
-
-
-
-
-
TA
16.2
377
0.3
9.4
0.2
<0.06
25.0
0.1
7.0
20.3
4.1
681
0.2
0.2
365
214
150
1.3
1.1
0.3
1.3
<0.1
<25
<25
<0.1
<0.1
TB
8.0
373
0.4
9.6
0.2
<0.06
24.6
0.2
7.0
20.3
4.1
710
0.2
0.2
361
212
149
1.0
0.7
0.3
1.3
<0.1
<25
<25
0.3
<0.1
10/27/04
IN
-
386
-
-
-
<0.06
25.2
0.1
7.0
19.5
4.2
216
-
-
-
-
-
56.5
-
-
-
-
<25
-
0.2
-
AC
-
-
-
-
-
-
-
-
7.0
19.8
3.6
552
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
17.1
382
-
-
-
<0.06
25.5
0.1
7.0
19.7
3.7
577
0.3
0.4
-
-
-
1.6
-
-
-
-
27.0
-
0.2
-
TB
8.5
390
-
-
-
<0.06
25.3
0.3
7.0
19.7
3.6
590
0.3
0.4
-
-
-
0.8
-
-
-
-
<25
-
<0.1
-
11/03/04
IN
-
369
-
-
-
<0.06
24.7
0.2
6.9
20.4
4.0
180
-
-
-
-
-
56.3
-
-
-
-
<25
-
0.3
-
AC
-
-
-
-
-
-
-
-
6.9
20.6
3.8
491
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
18.1
377
-
-
-
<0.06
25.0
0.2
6.9
20.6
4.1
565
0.3
0.4
-
-
-
1.6
-
-
-
-
31.1
-
0.4
-
TB
9.0
369
-
-
-
<0.06
25.0
0.2
6.9
20.6
3.9
591
0.3
0.4
-
-
-
0.8
-
-
-
-
<25
-
0.2
-
11/17/04
IN
-
390
-
-
-
<0.06
25.6
0.3
6.9®
20.7(b)
3.S®
504*)
-
-
-
-
-
56.5
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
-
6.9
20.7
4.0
619
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
20.1
386
-
-
-
<0.06
25.1
0.3
6.9
21.2
3.5
640
0.3
0.3
-
-
-
1.3
-
-
-
-
<25
-
<0.1
-
TB
10.0
390
-
-
-
<0.06
25.1
0.3
6.8
20.8
4.1
651
0.3
0.3
-
-
-
1.3
-
-
-
-
<25
-
0.9
-
(a) As CaCO3. (b) Measurement possibly taken from incorrect location.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
jjg/L
re/L
re/L
re/L
re/L
re/L
re/L
re/L
|xg/L
12/01/04
IN
-
365
365
-
-
-
<0.06
<0.06
25.5
25.3
0.1
0.1
7.0
20.1
4.3
267
-
-
-
-
-
51.4
52.3
-
-
-
-
<25
<25
-
0.1
0.1
-
AC
-
-
-
-
-
-
-
-
6.9
21.2
3.4
626
0.4
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
22.1
365
365
-
-
-
<0.06
<0.06
25.2
25.4
0.1
0.2
6.9
20.6
3.9
646
0.4
0.5
-
-
-
1.7
1.7
-
-
-
-
<25
<25
-
<0.1
0.4
-
TB
10.9
365
370
-
-
-
<0.06
<0.06
25.3
25.3
0.1
0.3
6.9
21.1
3.5
673
0.4
0.5
-
-
-
0.4
0.4
-
-
-
-
<25
<25
-
<0.1
<0.1
-
12/15/04°°
IN
-
383
0.4
9.7
0.2
<0.06
25.9
0.2
6.9
20.6
4.0
230
-
-
384
241
143
60.3
59.6
0.7
1.2
58.4
<25
<25
0.3
0.1
AC
-
-
-
-
-
-
-
-
6.9
20.1
3.2
618
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
24.1
370
0.4
9.1
0.2
<0.06
26.4
0.2
6.9
20.4
3.5
660
0.3
0.3
374
234
140
3.0
3.0
<0.1
1.3
1.7
<25
<25
<0.1
<0.1
TB
11.9
366
0.3
8.8
0.2
<0.06
26.3
0.1
6.9
20.0
3.4
672
0.3
0.3
377
235
142
0.8
0.6
0.2
0.7
<0.1
<25
<25
0.2
<0.1
01/05/05
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/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
02/02/05
IN
-
414
-
-
-
24.9
0.1
6.8
18.6
4.2
258
-
-
-
-
-
48.8
-
-
-
-
<25
-
1.2
-
AC
-
-
-
-
-
-
-
6.8
19.2
3.9
643
0.5
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
31.1
387
-
-
-
24.5
<0.1
6.8
19.7
3.6
664
0.4
0.5
-
-
-
4.7
-
-
-
-
<25
-
0.2
-
TB
15.4
405
-
-
-
24.8
<0.1
6.8
20.1
4.2
670
0.4
0.5
-
-
-
1.9
-
-
-
-
32.7
-
12.4
-
02/16/05
IN
-
392
0.3
10.0
0.3
27.6
0.1
6.9
20.4
3.6
448
-
-
302
183
119
52.5
51.1
1.4
0.9
50.2
<25
<25
0.3
<0.1
AC
-
-
-
-
-
-
-
6.9
20.0
3.6
643
0.4
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
33.2
374
0.3
10.0
0.3
27.5
<0.1
6.9
20.2
3.6
671
0.3
0.4
311
161
150
6.8
6.6
0.2
0.8
5.8
<25
<25
<0.1
<0.1
TB
16.4
405
0.3
10.0
0.3
27.4
0.2
6.9
20.1
3.7
693
0.3
0.4
305
188
117
0.3
0.3
<0.1
0.7
<0.1
<25
<25
<0.1
<0.1
03/02/05
IN
-
378
378
-
-
-
26.2
26.2
<0.1
<0.1
6.9
20.5
3.4
490
-
-
-
-
-
64.4
67.4
-
-
-
-
<25
<25
-
<0.1
<0.1
-
AC
-
-
-
-
-
-
-
6.9
20.2
3.3
625
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
35.1
369
373
-
-
-
26.4
26.3
0.1
<0.1
6.9
20.2
4.1
654
0.3
0.4
-
-
-
9.1
9.8
-
-
-
-
<25
<25
-
<0.1
<0.1
-
TB
17.4
391
386
-
-
-
26.5
26.1
0.1
0.1
6.8
20.3
4.1
673
0.3
0.4
-
-
-
0.5
0.5
-
-
-
-
<25
<25
-
0.1
<0.1
-
03/16/05
IN
-
388
-
-
-
26.4
<0.1
6.8
18.8
4.8
209
-
-
-
-
-
51.2
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
6.8
19.5
4.4
616
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
37.1
392
-
-
-
26.4
0.1
6.8
19.4
4.5
645
0.3
0.4
-
-
-
8.2
-
-
-
-
<25
-
<0.1
-
TB
18.4
401
-
-
-
25.8
<0.1
6.8
19.6
3.6
656
0.3
0.4
-
-
-
0.4
-
-
-
-
<25
-
<0.1
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(!l)
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(a)
Mg/L
Mg/L
Mg/L
Mg/L
re/L
Mg/L
re/L
Mg/L
Mg/L
03/30/05
IN
-
383
-
-
-
26.1
<0.1
6.9
20.6
6.0
308
-
-
-
-
-
52.7
-
-
-
-
<25
-
0.5
-
AC
-
-
-
-
-
-
-
6.9
20.1
3.4
365
0.4
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
39.2
378
-
-
-
26.1
<0.1
6.9
20.2
3.6
668
0.4
0.5
-
-
-
10.3
-
-
-
-
<25
-
0.4
-
TB
19.4
383
-
-
-
26.0
<0.1
6.8
20.2
3.5
686
0.4
0.5
-
-
-
0.5
-
-
-
-
<25
-
0.4
-
04/13/05
IN
-
401
0.3
8.1
0.2
27.0
0.2
6.9
20.0
3.8
201
-
-
325
199
126
51.9
51.4
0.5
0.8
50.6
27.2
<25
0.2
0.2
AC
-
-
-
-
-
-
-
6.9
20.0
3.9
605
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
41.1
424
0.3
7.8
0.2
27.3
0.4
6.9
20.2
4.1
631
0.4
0.4
322
190
131
8.8
8.9
<0.1
0.7
8.2
<25
<25
<0.1
<0.1
TB
20.3
410
0.3
8.1
0.2
27.0
<0.1
6.9
20.3
3.9
648
0.4
0.4
326
197
129
0.5
0.4
<0.1
0.7
<0.1
<25
<25
<0.1
<0.1
04/27/05
IN
-
405
-
-
-
26.1
0.1
6.8
20.9
4.7
467
-
-
-
-
-
58.7
-
-
-
-
<25
-
0.4
-
AC
-
-
-
-
-
-
-
6.9
20.3
3.3
646
0.5
0.6
-
-
-
-
-
-
-
-
-
-
-
-
TA
43.1
396
-
-
-
26.3
0.1
6.9
20.5
5.4
680
0.5
0.6
-
-
-
13.3
-
-
-
-
<25
-
0.2
-
TB
21.3
396
-
-
-
26.1
<0.1
6.9
20.5
4.3
694
0.5
0.6
-
-
-
0.5
-
-
-
-
<25
-
0.2
-
05/11/05
IN
-
400
-
-
-
26.0
<0.1
6.9
19.8
3.5
217
-
-
-
-
-
50.3
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
6.9
20.0
3.6
580
0.5
0.6
-
-
-
-
-
-
-
-
-
-
-
-
TA
45.2
396
-
-
-
26.2
<0.1
6.9
20.0
3.7
605
0.5
0.6
-
-
-
11.7
-
-
-
-
<25
-
<0.1
-
TB
22.3
400
-
-
-
26.2
<0.1
6.9
20.0
3.7
613
0.5
0.6
-
-
-
0.5
-
-
-
-
25.8
-
<0.1
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/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
05/25/05
IN
-
392
401
-
-
-
25.6
25.3
0.2
0.5
7.0
20.9
4.1
194
-
-
-
-
-
49.7
50.3
-
-
-
-
<25
<25
-
0.1
0.2
-
AC
-
-
-
-
-
-
-
7.0
20.6
3.0
571
0.5
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
47.2
401
401
-
-
-
25.9
25.0
1.3
0.4
7.0
20.6
3.3
608
0.5
0.5
-
-
-
13.3
13.3
-
-
-
-
<25
<25
-
<0.1
<0.1
-
TB
46.6
401
397
-
-
-
25.3
25.9
0.2
0.7
7.0
20.7
3.5
611
0.5
0.5
-
-
-
0.4
0.5
-
-
-
-
<25
<25
-
<0.1
<0.1
-
06/08/05
IN
-
400
0.3
11.0
0.6
26.8
<0.1
6.8
21.4
3.3
447
-
-
323
197
127
57.6
59.8
<0.1
1.2
58.6
<25
<25
0.2
0.2
AC
-
-
-
-
-
-
-
6.8
20.8
3.3
594
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
49.3
387
0.2
10.0
0.3
26.6
<0.1
6.8
21.1
3.5
620
0.3
0.3
323
196
126
17.2
18.8
<0.1
1.2
17.6
<25
<25
<0.1
0.1
TB
24.3
387
0.2
11.0
0.3
26.5
<0.1
6.8
21.1
3.5
627
0.3
0.3
329
204
125
1.2
1.1
<0.1
1.9
<0.1
<25
<25
0.1
<0.1
06/22/05
IN
-
374
-
-
-
25.3
0.7
7.0
21.0
3.2
182
-
-
-
-
-
55.4
-
-
-
-
<25
-
0.3
-
AC
-
-
-
-
-
-
-
7.0
21.1
3.3
600
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
51.3
374
-
-
-
25.3
0.9
7.1
21.0
3.1
628
0.3
0.3
-
-
-
18.3
-
-
-
-
<25
-
0.2
-
TB
25.3
383
-
-
-
25.3
0.2
7.0
21.0
3.0
637
0.3
0.3
-
-
-
0.9
-
-
-
-
<25
-
0.2
-
07/06/05
IN
-
374
-
-
-
26.2
0.2
7.1
21.1
3.5
182
-
-
-
-
-
49.2
-
-
-
-
<25
-
0.2
-
AC
-
-
-
-
-
-
-
7.0
20.7
3.3
580
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
53.3
374
-
-
-
26.1
<0.1
7.0
20.6
3.4
618
0.3
0.3
-
-
-
15.6
-
-
-
-
<25
-
<0.1
-
TB
26.3
374
-
-
-
25.9
0.1
7.0
20.9
3.8
624
0.3
0.3
-
-
-
0.5
-
-
-
-
<25
-
<0.1
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(!l)
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(a)
Mg/L
Mg/L
Mg/L
Mg/L
re/L
Mg/L
re/L
Mg/L
Mg/L
07/21/05
IN
-
374
-
-
-
24.8
0.3
6.9
22.1
3.3
439
-
-
-
-
-
50.8
-
-
-
-
<25
-
0.2
-
AC
-
-
-
-
-
-
-
7.0
21.4
3.1
608
0.2
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
55.5
374
-
-
-
25.0
1.6
7.0
22.5
3.4
628
0.2
0.3
-
-
-
18.9
-
-
-
-
<25
-
<0.1
-
TB
27.3
378
-
-
-
24.8
3.4
6.9
22.8
3.6
636
0.2
0.3
-
-
-
0.9
-
-
-
-
<25
-
0.1
-
08/03/05
IN
-
383
0.3
10.0
0.3
24.4
0.1
7.0
21.7
3.5
434
-
-
296
186
110
50.7
50.8
<0.1
1.5
49.3
<25
<25
<0.1
<0.1
AC
-
-
-
-
-
-
-
6.9
21.2
3.4
611
0.4
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
57.3
378
0.3
10.0
0.2
24.8
0.1
6.9
21.5
3.3
630
0.3
0.4
301
188
112
19.5
19.5
<0.1
1.4
18.1
<25
<25
<0.1
<0.1
TB
28.2
378
0.3
10.0
0.2
25.0
0.1
6.9
22.0
3.7
642
0.3
0.4
306
191
115
0.7
0.7
<0.1
1.5
<0.1
<25
<25
<0.1
<0.1
08/17/05
IN
-
374
-
-
-
25.4
<0.1
6.9
21.3
3.6
399
-
-
-
-
-
51.6
-
-
-
-
<25
-
0.2
-
AC
-
-
-
-
-
-
-
7.0
21.0
4.3
593
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
59.3
383
-
-
-
25.2
<0.1
6.9
21.0
3.9
593
0.2
0.3
-
-
-
19.1
-
-
-
-
<25
-
0.1
-
TB
29.2
387
-
-
-
25.3
0.1
6.9
21.5
3.6
633
0.2
0.3
-
-
-
0.8
-
-
-
-
<25
-
<0.1
-
08/31/05
IN
-
365
-
-
-
26.6
0.3
6.9
22.5
3.3
470
-
-
-
-
-
54.4
-
-
-
-
<25
-
0.3
-
AC
-
-
-
-
-
-
-
7.0
21.4
4.0
612
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
61.2
378
-
-
-
27.3
0.2
6.9
21.8
3.5
610
0.3
0.4
-
-
-
21.7
-
-
-
-
<25
-
<0.1
-
TB
30.1
374
-
-
-
27.1
0.1
6.9
22.7
3.7
608
0.3
0.4
-
-
-
0.7
-
-
-
-
<25
-
<0.1
-
(a) As CaCO3.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Phosphorus (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
Mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(!l)
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
09/14/05
IN
-
374
-
-
-
-
23.6
0.1
7.0
20.7
3.9
199
-
-
-
-
-
49.4
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
-
7.0
20.5
3.8
565
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
63.2
378
-
-
-
-
23.9
0.3
7.0
20.5
4.0
595
0.3
0.4
-
-
-
21.7
-
-
-
-
<25
-
<0.1
-
TB
31.1
374
-
-
-
-
23.7
0.4
7.0
20.4
4.0
603
0.3
0.4
-
-
-
1.0
-
-
-
-
<25
-
<0.1
-
09/28/05
IN
-
383
-
-
-
-
26.7
0.1
7.0
21.0
3.7
469
-
-
-
-
-
55.9
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
-
7.0
20.6
3.7
600
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
65.1
387
-
-
-
-
26.7
<0.1
6.7
20.9
4.1
618
0.2
0.3
-
-
-
25.9
-
-
-
-
<25
-
<0.1
-
TB
32.0
396
-
-
-
-
26.4
0.1
7.0
21.4
3.9
631
0.2
0.3
-
-
-
1.5
-
-
-
-
<25
-
<0.1
-
10/12/05
IN
-
378
0.2
10
0.2
16.8
24.9
<0.1
NA(C)
NA(C)
NA(C)
NA(C)
-
-
322
196
125
66.8
66.7
11.5
1.2
57.0
<25
<25
<0.1
<0.1
AC
-
-
-
-
-
-
-
-
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
-
-
-
-
-
-
-
-
-
TA
NA*'
383
0.2
9.9
0.2
14.8
24.2
<0.1
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
325
198
127
31.7(tl)
25.9
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Phosphorus (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(a)
mg/L
mg/L
mg/L
Mg/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
12/07/05
IN
-
383
0.2
10
0.2
<10
25.2
0.1
6.9
19.9
3.6
205
-
-
325
199
125
61.2
61.6
<0.1
0.7
60.9
<25
<25
0.2
0.2
AC
-
-
-
-
-
-
-
-
7.0
19.5
3.9
595
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
74.7
383
0.2
10
0.2
<10
25.5
<0.1
6.9
19.9
3.8
611
0.2
0.3
337
207
130
35.8
34.6
1.3
0.7
33.8
<25
<25
0.2
0.1
TB
36.8
378
0.2
10
0.2
<10
25.7
<0.1
6.9
19.9
3.9
633
0.2
0.3
341
205
136
3.4
3.1
0.3
0.7
2.4
<25
<25
0.2
0.1
01/04/06
IN
-
396
-
-
-
12.7
25.4
0.2
6.9
19.7
4.0
232
-
-
-
-
-
53.8
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
-
6.8
19.8
4.0
630
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
78.6
396
-
-
-
15.1
25.2
0.4
6.8
19.9
4.3
649
0.3
0.4
-
-
-
33.6
-
-
-
-
<25
-
<0.1
-
TB
38.7
396
-
-
-
<10
25.2
0.1
6.8
20.0
4.2
663
0.3
0.4
-
-
-
2.7
-
-
-
-
<25
-
<0.1
-
02/01/06
IN
-
390
0.2
10
0.2
<10
26.3
0.1
6.8
20.0
4.1
475
-
-
330
202
128
69.4W
54.3(b)
15.1
0.7
53.7
<25
<25
<0.1
<0.1
AC
-
-
-
-
-
-
-
-
6.8
19.9
3.8
634
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
82.5
382
0.2
10
0.2
<10
26.4
<0.1
6.8
20.0
3.8
663
0.3
0.3
339
206
134
43.2
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Phosphorus (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/L(!l)
mg/L
mg/L
mg/L
Mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(!l)
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
04/05/06
IN
-
372
-
-
-
<10
25.3
0.3
6.9
19.3
3.7
211
-
-
-
-
-
63.8
-
-
-
-
<25
-
<0.1
-
AC
-
-
-
-
-
-
-
-
6.9
19.5
3.7
616
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
91.1
376
-
-
-
10.7
24.4
0.5
6.9
19.6
3.8
649
0.4
0.4
-
-
-
45.5
-
-
-
-
<25
-
<0.1
-
TB
44.9
376
-
-
-
<10
25.0
0.6
6.9
19.6
3.5
659
0.4
0.4
-
-
-
6.0
-
-
-
-
<25
-
<0.1
-
04/19/06
IN
-
406
-
-
-
20.4
24.7
0.3
NA*'
NA*'
NA*'
NA*'
-
-
-
-
-
63.7
-
-
-
-
<25
-
0.2
-
AC
-
-
-
-
-
-
-
-
NA*>
NA*'
NA*>
NA*'
NA*'
NA*>
-
-
-
-
-
-
-
-
-
-
-
-
TA
93.0
401
-
-
-
21.4
24.3
0.4
NA*>
NA*'
NA*>
NA*'
NA*'
NA*>
-
-
-
42.2
-
-
-
-
<25
-
0.1
-
TB
45.8
388
-
-
-
10.4
24.4
0.2
NA*>
NA*'
NA*>
NA*'
NA*'
NA*>
-
-
-
5.6
-
-
-
-
<25
-
0.1
-
05/03/06
IN
-
374
0.3
9
0.2
<10
26.0
0.3
7.0
20.5
3.7
217
-
-
342
204
138
66.2
59.1
7.1
0.3
58.7
<25
<25
<0.1
<0.1
AC
-
-
-
-
-
-
-
-
7.0
20.4
3.9
646
0.4
0.4
-
-
-
-
-
-
-
-
-
-
-
-
TA
94.8
386
0.2
9
0.2
13.4
25.6
0.2
6.9
20.9
3.8
666
0.4
0.4
332
198
135
48.7
41.9
6.7
0.3
41.7
<25
<25
<0.1
<0.1
TB
NA
382
0.3
9
0.2
<10
25.9
0.2
6.9
20.7
3.8
685
0.4
0.4
341
202
138
6.5
6.1
0.4
0.3
5.8
<25
<25
<0.1
<0.1
05/17/06
IN
-
380
384
-
-
-
<10
<10
26.8
26.3
0.3
0.3
NA*'
NA*'
NA*'
NA*'
-
-
-
-
-
53.8
54.3
-
-
-
-
<25
<25
-
0.1
<0.1
-
AC
-
-
-
-
-
-
-
-
NA*'
NA*'
NA*>
NA*'
NA*'
NA*>
-
-
-
-
-
-
-
-
-
-
-
-
TA
96.7
388
380
-
-
-
<10
<10
26.7
26.2
0.2
0.4
NA*>
NA*'
NA*>
NA*'
NA*'
NA*>
-
-
-
38.8
39.2
-
-
-
-
<25
<25
-
<0.1
<0.1
-
TB
47.6
384
355
-
-
-
<10
<10
25.7
26.4
0.4
0.2
NA*>
NA*'
NA*>
NA*'
NA*'
NA*>
-
-
-
6.3
6.4
-
-
-
-
<25
<25
-
<0.1
<0.1
-
(a) As CaCO3. (b) Onsite water quality parameter not measured.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B; NA = data not available.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Phosphorus (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine (as C12)
Total Chlorine (as C12)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
103
mg/Lw
mg/L
mg/L
mg/L
Hg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L(a)
mg/L«
re/L
re/L
Hg/L
re/L
|xg/L
|xg/L
|xg/L
|xg/L
|xg/L
06/14/06
IN
-
378
-
-
-
18.0
27.0
0.5
6.9
21.2
NA*>
NA*'
-
-
-
-
-
76.7
-
-
-
-
<25
-
0.1
-
AC
-
-
-
-
-
-
-
-
7.0
20.6
NA*>
NA*'
0.5
0.5
-
-
-
-
-
-
-
-
-
-
-
-
TA
100.4
386
-
-
-
20.0
26.8
0.5
7.0
21.7
NA*>
NA*'
0.5
0.5
-
-
-
56.1
-
-
-
-
<25
-
<0.1
-
TB
49.4
386
-
-
-
10.9
26.5
0.2
7.0
22.4
NA*'
NA*'
0.5
0.5
-
-
-
9.2
-
-
-
-
<25
-
<0.1
-
07/12/06(c)
IN
-
377
0.2
10
0.2
13.4
25.4
0.3
7.0
21.5
NA^
NA*'
-
-
304
185
119
63.9
54.4
9.5
0.4
54.0
<25
<25
0.7
0.2
AC
-
-
-
-
-
-
-
-
7.0
20.7
NA*'
NA*'
0.3
0.3
-
-
-
-
-
-
-
-
-
-
-
-
TA
103.3
390
0.2
10
0.2
14.3
24.8
0.4
7.0
21.1
NA*>
NA*'
0.3
0.3
314
192
122
48.3
40.1
8.2
0.4
39.8
<25
<25
0.6
0.1
TB
50.9
373
0.2
10
0.2
<10
25.5
0.1
7.0
21.1
NA*'
NA*'
0.3
0.3
303
185
118
8.2
7.3
0.9
0.4
7.0
<25
<25
0.6
0.2
08/09/06
NA*'
0.4
0.4
-
-
-
53.7
-
-
-
-
<25
-
<0.1
-
TB
52.2
382
-
-
-
<10
24.2
0.4
7.0
21.7
NA*'
NA*'
0.4
0.4
-
-
-
9.8
-
-
-
-
<25
-
0.1
-
(a) As CaCO3. (b) Onsite water quality parameter not measured, (c) Due to low water levels, well pump throttled from 31 to <25 gpm since 06/16/1
(d) TA and TB sample bottles likely switched and corrected for this event.
IN = at inlet; AC = after prechlorination (field parameters only); TA = after tank A; TB = after tank B; NA = data not available.
-------
Analytical Results from Long-Term Sampling, Rimrock, AZ (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
As (total)
103
|xg/L
ll/28/06(a)
IN
-
64.5
TA
0.1
0.7
TB
0.1
6.2
01/03/07
IN
-
75.0
TA
4.7
0.7
TB
8.7
24.3
02/07/07
IN
-
69.3
TA
9.7
0.7
TB
18.0
31.7
03/07/07
IN
-
58.4
TA
12.8
1.0
TB
23.8
26.0
(a) System offline and well pump pulled for cleaning on 08/30/06. System operation resumed on 11/27/06 after Tank A media replaced and tank positions switched.
Partially exhausted Tank B continues operation in lead position.
IN = at inlet; TA = after tank A; TB = after tank B.
------- |