EPA/600/R-08/141
December 2008
Arsenic Removal from Drinking Water by Adsorptive Media
U.S. EPA Demonstration Project at Queen Anne's County, Maryland
Final Performance Evaluation Report
by
Abraham S.C. Chen
Gary M. Lewis
Lili Wang
Anbo Wang
Battelle
Columbus, OH 43201-2693
Contract No. 68-C-00-185
Task Order No. 0019
for
Thomas J. Sorg
Task Order Manager
Water Supply and Water Resources Division
National Risk Management Research Laboratory
Cincinnati, 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 0019 of Contract 68-C-00-185 to Battelle. It has been subjected to the Agency's
peer and administrative reviews and has been approved for publication as an EPA document. Any
opinions 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 sub-
surface resources; protection of water quality in public water systems; remediation of contaminated sites,
sediments and groundwater; 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 envi-
ronmental problems by developing and promoting technologies that protect and improve the environment;
advancing scientific and engineering information to support regulatory and policy decisions; and provid-
ing the technical support and information transfer to ensure implementation of environmental regulations
and strategies at the national, state, and community levels.
This publication has been produced as part of the Laboratory's strategic long-term research plan.
It is published and made available by EPA's Office of Research and Development to assist the user
community and to link researchers with their clients.
Sally Gutierrez, Director
National Risk Management Research Laboratory
in
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ABSTRACT
This report documents the activities performed and the results obtained from the arsenic removal
treatment technology demonstration project at the community of Prospect Bay at Grasonville in Queen
Anne's County, MD. The main objective of the project was to evaluate the effectiveness of Severn Trent
Services (STS) SORB 33™ media in removing arsenic to meet the new arsenic maximum contaminant
level (MCL) of 10 |o,g/L. Additionally, this project evaluated 1) the reliability of the treatment system
(Arsenic Package Unit [APU]-300) for use at small water facilities, 2) the required system operation and
maintenance (O&M) and operator skill levels, and 3) the capital and O&M cost of the technology. The
project also characterized water in the distribution system and residuals generated by the treatment
process. The types of data collected included system operation, water quality (both across the treatment
train and in the distribution system), process residuals, and capital and O&M cost.
The STS system consisted of two 63-in-diameter, 86-in-tall fiberglass reinforced plastic (FRP) vessels in
parallel configuration, each containing approximately 80 ft3 of SORB 33™ media. The media is an iron-
based adsorptive media developed by Bayer AG and packaged under the name SORB 33™ by STS. The
system was designed for a flowrate of 300 gal/min (gpm) (150 gpm to each vessel), corresponding to a
design empty bed contact time (EBCT) of about 4.0 min per vessel and a hydraulic loading rate of 6.9
gpm/ft2. Actual flowrates through the system averaged 207 gpm, corresponding to an EBCT of 5.6 min in
Vessel A and 6.0 min in Vessel B.
Upon review and approval of the engineering plan by the State, the APU-300 treatment system was
installed and became operational on June 30, 2004. From June 30, 2004, through April 2, 2007, the APU-
300 system operated an average of 6.2 hr/day for a total operating time of 5,890 hr. The system treated
approximately 71,533,000 gal of water, or 59,800 bed volumes (BV), which was approximately 52% of
the vendor-estimated working capacity for the SORB 33™ media. Several problems were encountered
during the performance evaluation study, including the need to implement prechlorination, shortened run
times between backwashes, and equipment malfunctions. The corrective actions taken to address the
problems are detailed in the report.
Total arsenic concentrations in raw water ranged from 16.0 to 25.8 |o,g/L with soluble As(III) being the
predominating species, averaging 18.9 |o,g/L. After treating only 7,400 BV of water, the arsenic
concentration in the treated water exceeded the target concentration of 10 |og/L. To improve arsenic
removal by the media, prechlorination was implemented in early November 2004. (Prior to this, chlorine
was added at the end of the treatment train.) Arsenic in samples collected following prechlorination
existed primarily as As(V) and particulate As, indicating effective As(III) oxidation. Since then, arsenic
removal improved significantly, with its concentrations in the treated water decreasing from over 10 to
0.9 |og/L within two weeks following the switch to prechlorination. Total arsenic concentrations in the
treated water remained at levels less than 10 |o,g/L (averaged at 2.1 |o,g/L) during the remainder of the
performance evaluation study.
The APU-300 system was designed and programmed with an automatic backwash feature that would
trigger backwash by either a differential pressure (Ap) setting of 10 pounds per square inch (psi) or a
timer. However, backwash of the system was initiated manually by the system operator because there
was no onsite disposal facility to receive the backwash wastewater, which had to be discharged into a
tanker truck and transported to the Stevensville Wastewater Treatment Plant (WWTP) for disposal.
When post-chlorination was performed during the first four months of system operation, the adsorption
vessels were not backwashed because there were little or no changes in pressure across both vessels. The
IV
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pressure readings began to rise once the switch to prechlorination had been implemented. The run times
between backwashes shortened significantly from the initial 2,359 BV to less than 800 BV (or 2
month/backwash to less than 2 week/backwash). Media attrition appears to be the main reason for the
shortened run times and more frequent backwash.
During the 33-month performance evaluation study, the adsorption system was backwashed a total of 50
times, generating 229,646 gal of wastewater. The backwash wastewater contained 100 to 430 mg/L of
total dissolved solids (TDS) and 12 to 130 mg/L of total suspended solids (TSS). The backwash solids
generated by each backwash cycle contained approximately 1.3 Ib of iron, 0.003 Ib of manganese, and
0.02 Ib of arsenic.
Results of the distribution system sampling showed a distinct effect of the treatment system on arsenic
concentrations in the treated water. The treatment system decreased arsenic levels in the distribution
system from an average of 19.0 to 8.4 (ig/L prior to the switch to prechlorination and to 3.6 (ig/L after the
switch to prechlorination. The results from the distribution system sampling mirrored those seen from the
treatment system sampling, with As concentrations dropped once the system was put into service, rose
gradually as As(III) began to break through during the first four months of system operation, and then
went down again once the switch to prechlorination was made. The APU-300 did not appear to have an
effect on the Pb or Cu levels in the distribution system.
The capital investment cost of $211,000 included $129,500 for equipment, $36,700 for site engineering,
and $44,800 for installation. Using the system's rated capacity of 300 gpm (or 432,000 gal per day
[gpd]), the unit capital cost was $703/gpm (or $0.49/gpd). This calculation does not include the cost of
the building to house the treatment system. O&M cost, estimated at $0.31/1,000 gal, included only the
incremental cost for electricity, replacement parts, and labor. The estimated media changeout cost was
$27,728, which would represent the majority of the O&M cost. Media changeout did not occur during
the performance evaluation period.
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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 5
3.1 General Project Approach 5
3.2 System O&M and Cost Data Collection 6
3.3 Sample Collection Procedures and Schedules 7
3.3.1 Source Water 7
3.3.2 Treatment Plant Water 7
3.3.3 Backwash Wastewater 7
3.3.4 Backwash Solids Sample Collection 10
3.3.5 Media Sample Collection 10
3.3.6 Distribution System 10
3.4 Sampling Logistics 10
3.4.1 Preparation of Arsenic Speciation Kits 10
3.4.2 Preparation of Sampling Coolers 10
3.4.3 Sample Shipping and Handling 11
3.5 Analytical Procedures 11
4.0 RESULTS AND DISCUSSION 12
4.1 Facility Description 12
4.1.1 Source Water Quality 12
4.1.2 Pre-Demonstration Treated Water Quality 13
4.1.3 Distribution System 14
4.2 Treatment Process Description 15
4.3 System Installation 20
4.3.1 Permitting 20
4.3.2 Building Construction 20
4.3.3 System Installation, Shakedown, and Startup 20
4.4 System Operation 21
4.4.1 Operational Parameters 21
4.4.2 Previous System Design Changes 27
4.4.3 Backwash Operation 27
4.4.4 Residual Management 27
4.4.5 System/Operation Reliability and Simplicity 27
4.5 System Performance 29
VI
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4.6
4.5.1 Treatment Plant Sampling 29
4.5.2 Backwash Wastewater Sampling 38
4.5.3 Adsorptive Media Sampling 41
4.5.4 Distribution System Water Sampling 41
System Costs 41
4.6.1 Capital Costs 43
4.6.2 Operation and Maintenance Cost 44
5.0 REFERENCES 47
APPENDICES
APPENDIX A: Operational Data
APPENDIX B: Analytical Data
FIGURES
Figure 3-1. Process Flow Diagram and Sampling Locations 9
Figure 4-1. Existing Well House No. 1 12
Figure 4-2. Chlorine Gas System at Well No. 1 13
Figure 4-3. APU-300 Treatment System Prior to Shipment 17
Figure 4-4. Schematic of APU-300 System 17
Figure 4-5 Treatment Process Components 19
Figure 4-6. New Treatment Building Addition with Two Access Hatches on Roof 20
Figure 4-7. Unloading of APU Skid into Partially Completed Treatment Building Addition 21
Figure 4-8. APU-300 Treatment System Daily Operating Time 22
Figure 4-9. APU-300 Treatment System Daily Average Flowrates 24
Figure 4-10. APU-300 Treatment System Inlet and Outlet Pressure 24
Figure 4-11. Differential Pressure Readings across Adsorption Vessels 25
Figure 4-12. Water Production between Two Consecutive Backwash Events 26
Figure 4-13. Concentration of Arsenic Species at IN, AC, and TT Sample Locations 34
Figure 4-14. Total Arsenic Breakthrough Curve 35
Figure 4-15. Average Concentrations of Arsenic Species at IN and AC Sampling Locations 35
Figure 4-16. Total Iron Concentrations Versus Amount of Water Treated 36
Figure 4-17. Total Manganese Concentrations Versus Bed Volumes 37
Figure 4-18. Media Replacement and Operation and Maintenance Costs 46
TABLES
Table 1-1. Summary of Round 1 Arsenic Removal Demonstration Sites 2
Table 3-1. Predemonstration Study Activities and Completion Dates 5
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities 6
Table 3-3. Sampling Schedule and Analyses 8
Table 4-1. Prospect Bay Water Quality Data 14
Table 4-2. Physical and Chemical Properties of SORB 33™ Media 15
Table 4-3. Design Specifications of the APU-300 System 18
Table 4-4. Summary of APU-300 System Operation 22
Table 4-5. Classification of Water Treatment Plants in State of Maryland 28
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Table 4-6. Summary of Arsenic, Iron, and Manganese Analytical Results Prior to Switch to
Prechlorination (July 7 to November 3, 2004) 30
Table 4-7. Summary of Arsenic, Iron, and Manganese Analytical Results After Switch to
Prechlorination (November 9, 2004 to December 30, 2004) 31
Table 4-8. Summary of Water Quality Parameter Results 32
Table 4-9. Backwash Water Sampling Results 39
Table 4-10. Backwash Solids Sampling Results 40
Table 4-11. Media Sampling Results 40
Table 4-12. Distribution System Sampling Results 42
Table 4-13. Capital Investment for Prospect Bay Treatment System 43
Table 4-14. O&M Cost for Prospect Bay Treatment System 44
Vlll
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ABBREVIATIONS AND ACRONYMS
Ap differential pressure
AAL American Analytical Laboratories
Al aluminum
AM adsorptive media
APU arsenic package unit
As arsenic
BET Brunauer, Emmett, and Teller
BV bed volume(s)
Ca calcium
C/F coagulation/filtration
C12 chlorine
CRF capital recovery factor
Cu copper
DO dissolved oxygen
EBCT empty bed contact time
EPA United States Environmental Protection Agency
Fe iron
FRP fiberglass reinforced plastic
GFH granular ferric hydroxide
gpd gallons per day
gpm gallons per minute
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
MDE Maryland Department of the Environment
MDWCA Mutual Domestic Water Consumers Association
Mg magnesium
Mn manganese
Mo molybdenum
mV millivolts
Na sodium
NS not sampled
NSF NSF International
NTU nephelometric turbidity units
IX
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O&M operation and maintenance
ORD Office of Research and Development
ORP oxidation-reduction potential
P&ID piping and instrumentation diagram
psi pounds per square inch
PVC polyvinyl chloride
QAC Queen Anne's County
QAPP Quality Assurance Project Plan
QA/QC quality assurance/quality control
QA quality assurance
RPD relative percent difference
Sb antimony
SDWA Safe Drinking Water Act
SM system modification
STMGID South Truckee Meadows General Improvement District
STS Severn Trent Services
TBD to be determined
TCLP Toxicity Characteristic Leaching Procedure
TDS total dissolved solids
TOC total organic carbon
TSS total suspended solids
V vanadium
VOC volatile organic compounds
WRWC White Rock Water Company
WWTP wastewater treatment plant
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ACKNOWLEDGMENTS
The authors wish to extend their sincere appreciation to the staff of the Queen Anne's County (QAC)
Department of Public Works in Stevensville, Maryland. The QAC staff monitored the treatment system
daily and collected samples from the treatment system 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 (SDWA) mandates that the 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
community of Prospect Bay at Grasonville in Queen Anne's County (QAC), MD 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. Severn Trent Services (STS), using the
Bayoxide E33 media developed by Bayer AG, was selected for the Prospect Bay facility. STS has given
the E33 media the designation "SORB 33™."
1.2 Treatment Technologies for Arsenic Removal
The technologies selected for the 12 Round 1 EPA arsenic removal demonstration host sites include nine
adsorptive media systems, one anion exchange system, one coagulation/filtration system, and one process
modification with iron addition. Table 1-1 summarizes the locations, technologies, vendors, and key
source water quality parameters of the 12 demonstration sites. An overview of the technology selection
and system design (Wang et al., 2004) and the associated capital costs for each site (Chen et al., 2004) are
provided on the EPA website (http://www.epa.gov/ORD/NRMRL/wswrd/dw/arsenic/index.html). As of
March 2008, all 12 systems were operational, and the performance evaluation of 11 systems was
completed.
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Table 1-1. Summary of Round 1 Arsenic Removal Demonstration Sites
Demonstration Site
WRWC, NH
Rollinsford, NH
Queen Anne's County, MD
Brown City, MI
Climax, MN
Lidgerwood, ND
Desert Sands MDWCA, NM
Nambe Pueblo Tribe, NM
Rimrock, AZ
Valley Vista, AZ
Fruitland, ID
STMGID, NV
Technology (Media)
AM(G2)
AM (E33)
AM (E33)
AM (E33)
C/F (Macrolite)
SM
AM (E33)
AM (E33)
AM (E33)
AM (AAFS50/ARM 200)
IX (A300E)
AM (GFH/Kemiron)
Vendor
ADI
AdEdge
STS
STS
Kinetico
Kinetico
STS
AdEdge
AdEdge
Kinetico
Kinetico
Siemens
Design
Flowrate
(gpm)
70(a)
100
300
640
140
250
320
145
90(a)
37
250
350
Source Water Quality
As
(ug/L)
39
36(b)
19(b)
14(b)
39(b)
146(b)
23(b)
33
50
41
44
39
Fe
(Ug/L)
<25
46
270(c)
127(c)
546(c)
l,325(c)
39
<25
170
<25
<25
<25
PH
7.7
8.2
7.3
7.3
7.4
7.2
7.7
8.5
7.2
7.8
7.4
7.4
AM = adsorptive media; C/F = coagulation/filtration; GFH = granular ferric hydroxide; IX = ion exchange; SM =
system modification; MDWCA = Mutual Domestic Water Consumer's Association; STMGID = South Truckee
Meadows General Improvement District; STS = Severn Trent Services; WRWC = White Rock Water Company
(a) Design flowrate reduced by 50% due to system reconfiguration from parallel to series operation.
(b) Arsenic exists mostly as As(III).
(c) Iron exists mostly as soluble Fe(II).
1.3
Project Objectives
The objective of the Round 1 arsenic demonstration program is to conduct full-scale arsenic treatment
technology demonstration studies on the removal of arsenic from drinking water supplies. The specific
objectives are to:
• Evaluate the performance of the arsenic removal technologies for use on small
systems.
• Determine the required system operation and maintenance (O&M) and operator skill
levels.
• Characterize process residuals produced by the technologies.
• Determine the capital and O&M cost of the technologies.
This report summarizes the performance of the STS treatment system operation from June 30, 2004,
through April 2, 2007. The types of data collected include 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
Based on the information collected from operation of STS's APU-300 arsenic removal system at Queen
Anne's County, MD from June 30, 2004, to April 2, 2007, the following summary and conclusions were
made relating to the overall objectives of the treatment technology demonstration study.
Performance of the arsenic removal technology for use on small systems:
• The SORB 33™ media was not effective at removing As(III), as demonstrated by
arsenic breakthrough at 10 |o,g/L after only treating 7,400 bed volumes (BV) of water.
• Chlorine was effective at oxidizing As(III).
• Implementation of prechlorination reversed the trend of arsenic breakthrough,
reducing total arsenic concentrations in the treated water from over 10 |o,g/L to 0.9
within two weeks.
• The use of chlorine significantly increased SORB 33™ media adsorptive capacity for
arsenic. After the switch to prechlorination at approximately 10,200 BV on
November 9, 2004, total arsenic concentrations in treated water remained at levels
less than 10 |o,g/L (averaged at 2. 1 |o,g/L) during the remainder of the performance
evaluation study.
• During the 33 months of the performance evaluation study, the APU-300 system treated
approximately 59,800 BV (or 71,533,000 gal) of water, which is about half of the vendor-
estimated working capacity.
• Run times between backwashes shortened significantly from the initial 2,359 BV/backwash
to less than 800 BV/backwash (or 2 month/backwash to less than 2 week/backwash) at the
end of the performance study. Media attrition during backwash appeared to have caused
more frequent backwash.
• The treatment system had a distinct effect on arsenic concentrations in the
distribution system. The average arsenic concentration in the distribution system
decreased from the original 19 (ig/L (baseline) to 3.6 (ig/L when the treatment system
was in operation. Results from samples collected from within the distribution system
mirrored those from the treatment system.
• The treatment did not appear to have an effect on Pb or Cu levels in the distribution
system.
Simplicity of required system O&M and operator skill levels:
• The treatment system operated as expected during the demonstration study and did
not experience any issues related to flow restriction or pressure drop.
• The skill requirements to operate the treatment system were minimal with a typical
daily demand on the operator of 15 to 20 min. Normal operation of the system did
not appear to require additional skills beyond those necessary to operate the existing
water supply equipment. A Class I state-certified operator was required for operation
of the water system at Prospect Bay.
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Process residuals produced by the technology:
• Backwash wastewater was the only treated residual from APU-300 system
operations.
• Soluble arsenic concentrations in the backwash wastewater averaged 10.1 |og/L,
significantly lower than that in raw water used for backwash, indicating some soluble
arsenic removal during backwash.
Cost-effectiveness of the technology:
• The capital investment for the system was $211,000, consisting of $129,500 for
equipment, $36,700 for site engineering, and $44,800 for installation, shakedown,
and startup.
• The unit capital cost was $703/gpm (or $0.49/gpd) based on a 300-gpm design
capacity. This calculation does not reflect the building cost as it was funded by
QAC.
• The vendor estimated media changeout cost was $27,728. Because media changeout
did not occur during the performance evaluation, the O&M cost, estimated at
$0.31/1,000 gal of water treated, included only the incremental cost for electricity,
replacement parts, and labor.
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3.0 MATERIALS AND METHODS
3.1
General Project Approach
Following the predemonstration activities summarized in Table 3-1, the performance evaluation study
of the STS treatment system began on June 30, 2004. Table 3-2 summarizes the types of data collected
and/or considered as part of the technology evaluation process. The overall performance of the system
was determined based on its ability to consistently remove arsenic to 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.
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 Submitted to Battelle
Purchase Order Completed and Signed
Letter Report Issued
Draft Study Plan Issued
Final Study Plan Issued
Engineering Package Submitted to MDE
Building Construction Began
APU-300 Shipped by STS
APU-300 Delivered to Site and System Installation Began
Permit for Treatment System Issued by MDE
System Installation Completed
Building Construction Completed
System Shakedown Completed
Performance Evaluation Began
Date
August 7, 2003
August 11, 2003
August 13, 2003
September 5, 2003
September 8, 2003
October 3, 2003
October 17, 2003
February 6, 2004
February 23, 2004
March 12, 2004
May 17, 2004
May 26, 2004
June 1, 2004
June 15, 2004
June 17, 2004
June 24, 2004
June 29, 2004
June 30, 2004
MDE = Maryland Department of the Environment
The O&M and operator skill requirements were evaluated based on a combination of quantitative data
and qualitative considerations, including the need for pre- and/or post-treatment, levels of system
automation, extent of preventative maintenance activities, frequency of chemical and/or media handling
and inventory, and general knowledge needed for relevant chemical processes and related health and
safety practices. The staffing requirements for the system operation were recorded on an Operator Labor
Hour Log Sheet.
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 wastewater was sampled and analyzed for chemical characteristics.
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Table 3-2. Evaluation Objectives and Supporting Data Collection Activities
Evaluation Objective
Performance
Reliability
System O&M and Operator
Skill Requirements
Residual Management
System Cost
Data Collection
-Ability to consistently meet 10 (o,g/L of arsenic in treated water
-Unscheduled system downtime
-Frequency and extent of repairs including a description of problems,
materials and supplies needed, and associated labor and cost
-Pre- and post-treatment requirements
-Level of system automation for system operation and data collection
-Staffing requirements including number of operators and laborers
-Task analysis of preventative maintenance including number, frequency,
and complexity of tasks
-Chemical handling and inventory requirements
-General knowledge needed for relevant chemical processes and health and
safety practices
-Quantity and characteristics of aqueous and solid residuals generated by
system operation
-Capital cost for equipment, site engineering, and installation
-O&M cost for media, chemical consumption, electricity usage, and labor
The cost of the system was evaluated based on the capital cost per gpm (or gpd) of design capacity and
the O&M cost per 1,000 gal of water treated. This task required tracking of the capital cost for
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
instruction provided by STS and Battelle. On a daily basis, the plant operator recorded system
operational data, such as pressure, flowrate, totalizer, and hour meter readings on a Daily System
Operation Log Sheet; checked the chlorine gas injection system; and conducted visual inspections to
ensure normal system operations. 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 chlorine
residuals, were measured and recorded on a Weekly Onsite Water Quality Parameters Log Sheet.
Backwash data also were recorded on a Backwash Log Sheet.
The capital cost for the arsenic removal system consisted of the cost for equipment, site engineering, and
system installation. The O&M cost consisted of the cost for media replacement and spent media disposal,
chemical and electricity consumption, replacement parts, and labor. Chlorine gas application and
electricity consumption were tracked using the Daily System Operation Log Sheet. Labor for various
activities, such as the routine system O&M, troubleshooting and repair, and demonstration-related work,
were tracked using an Operator Labor Hour Log Sheet. The routine O&M included activities such as
completing daily field logs, performing regular system inspections, and others as recommended by the
vendor. The demonstration-related work, including activities such as performing field measurements,
collecting and shipping samples, and communicating with the Battelle Study Lead and the vendor, was
recorded, but not used for the cost analysis.
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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 visit to the site, source water samples were collected and
speciated using an arsenic speciation kit described in Section 3.4.1. The sample tap was flushed for
several minutes before sampling; special care was taken to avoid agitation, which could cause unwanted
oxidation. Analytes for the source water samples are listed in Table 3-3.
3.3.2 Treatment Plant Water. During the system performance evaluation study, water samples
were collected biweekly across the treatment train at the wellhead (IN), after chlorination (AC), after
Vessel A (TA), and after Vessel B (TB), and analyzed for the analytes listed in Table 3-3. When
speciation was performed, water samples were collected at IN, AC, and after effluent from Vessels A and
B combined (TT) and analyzed for the analytes also listed in Table 3-3.
Over the course of the demonstration study, the sampling schedules were changed several times as
presented below:
• During the first month of system operation, water samples were taken weekly. The sampling
frequency was reduced to biweekly after the first month due to low water demand and
resulting low volume throughput.
• The AC sampling location was added after the switch to prechlorination on November 9,
2004, approximately four months after system startup. Weekly sampling was conducted
immediately after the switch to better monitor the conversion and breakthrough of As(III) and
to better observe the effects of this change on system performance. The biweekly sampling
schedule was resumed on February 1, 2005.
• Beginning on December 13, 2005, the biweekly sampling schedule was reduced to monthly.
On July 23, 2006, the analytes for monthly sampling were reduced from those listed in Table
3-3 to As speciation, total and soluble Fe and Mn, and total P, Ca, and Mg. The analytes
were further reduced to As speciation and total and soluble Fe and Mn on October 17, 2006.
• Since October 13, 2005, the orthophosphate analysis was replaced with total phosphorus, due
to lack of orthophosphate in raw water and issues related to the short hold time for
orthophosphate.
3.3.3 Backwash Wastewater. From November 17, 2004, (after the switch to prechlorination)
through September 5, 2006, backwash wastewater was sampled and analyzed at 27 backwash events.
Backwash water sampling was discontinued in September 2006 after almost two years of data collection.
Grab backwash wastewater samples were initially collected directly from the sample tap on the backwash
wastewater discharge line during the backwash of each vessel and filtered with 0.45-(im disc filters.
Beginning on December 16, 2005, composite samples also were collected following a modified procedure
to allow for more representative characterization of the wastewater. Tubing directed a portion of
backwash water from the sample tap at approximately 1 gpm into a clean plastic container of adequate
-------
Table 3-3. Sampling Schedule and Analyses
Sample Type
Source Water
Treatment
Plant Water
Distribution
Water
Backwash
Wastewater
Backwash
Solids
Spent Media
Sample Locations'3'
IN
IN, AC(b), TA, TB
IN, AC, TT
Three LCR
Residences
BW
BW
At top of Vessels A
and Vessel B
No. of
Samples
1
4
3
3
2
2-3
12®
Frequency
Once during
initial site
visit
Weekly,
bi-weekly,
or
monthly
(non-
speciation
sampling)
Weekly,
bi-weekly,
or
monthly
(speciation
sampling)
Monthly
Per
backwash
event(e)
(27 times)
3 times("
1 time
Analytes
As(total and soluble), As(III),
As(V),
Fe (total and soluble),
Mn (total and soluble),
Al (total and soluble),
V (total and soluble),
Mo (total and soluble),
Sb (total and soluble),
Na, Ca, Mg, Cl, F, SO4, SiO2,
PO4, TOC, and alkalinity
Onsite: pH, temperature, DO,
ORP, and C12 (free and total)03'
Offsite: As (total), Fe (total),
Mn (total), Si02, PO4(c',
turbidity, and alkalinity
Onsite: pH, temperature,
DO/ORP, and C12 (free and
total) (b)
Offsite: As(III), As(V),
As( total and soluble),
Fe (total and soluble),
Mn (total and soluble),
Ca, Mg, F, NO3, SO4, SiO2,
PO4(c), turbidity, and alkalinity
pH, alkalinity, total As, Fe,
Mn, Pb, Cu, and PO4
Total and/or soluble As, Fe,
and Mn, pH, TDS, TSS,
and/or turbidity
Total Al, As, Ca, Cd, Cu, Fe,
Mg, Mn, Ni, P, Pb, Si, and Zn
Total Al, As, Ca, Cd, Cu, Fe,
Mg, Mn, Ni, P, Pb, Si, and Zn
Date(s) Samples
Collected
08/07/03
See Appendix B
See Appendix B
Baseline sampling1-01':
See Table 4- 11
Monthly sampling:
See Table 4- 11
See Table 4-8
05/12/05,05/31/05,
06/21/05
08/04/05
(a)
Corresponding to sample locations in Figure 3-1: IN = at wellhead; AC = after chlorination; TA = after Vessel A; TB =
after Vessel B; TT = combined effluent; and BW = at backwash water discharge line.
Samples taken only after prechlorination at AC sampling location starting after November 9,2004.
PO4 analysis replaced with total phosphorus analysis starting from October 13, 2005.
Baseline sampling performed before system startup.
Backwash wastewater sampling discontinued after September 5,2006.
Backwash solids were analyzed at three selected backwash events were three samples collected from each vessel both
before and after backwash on August 4, 2005 when STS technicians were onsite to investigate cause of shortened run
length between backwashes.
DO = dissolved oxygen; LCR = Lead and Copper Rule; ORP = oxidation-reduction potential; TDS = total dissolved solids; and
TSS = total suspended solids
(b)
(c)
(d)
(e)
(f)
-------
INFLUENT
(WELL HOUSE
#1)
Speciation Sampling (Once a Month)
pH(a), temperature^3),
DO/ORPW, As (total and
soluble), As (III), As (V),
Fe (total and soluble), -^
Mn (total and soluble),
Ca, Mg, F, N03, S04, SiO2,
PO4, turbidity, alkalinity
pH(a), temperature^),
DO/ORPW, C12 (free and total),
As (total and soluble), As (III),
As (V), Fe (total and soluble), -
Mn (total and soluble), Ca, Mg,
F, NO3, SO4, SiO2, PO4,
turbidity, alkalinity
Stevensville, MD
SORB-3 3® Technology
Design Flow: 300 gpm
BACKWASH
STORAGE TANK/
DISPOSAL TRUCK
Grab Samples:
pH, IDS, turbidity,
As (soluble),
Fe (soluble),
Mn (soluble)
Composite Samples:
pH, TDS/TSS, turbidity,
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble)
Non-Speciation Sampling (Once a Month)
pH(a), temperature^,
DO/ORPW, As (total),
Fe (total), Mn (total), SiO2, PO4,
turbidity, alkalinity
pR(a), temperature^),
DO/ORPW, C12 (free and total),
As (total), Fe (total), Mn (total),
SiO2, PO4, turbidity, alkalinity
HW, temperature^, DO/ORPW,
As (total and soluble), As (III),
As (V), Fe (total and soluble),
Mn (total and soluble), Ca, Mg,
F, N03, S04, Si02, P04,
turbidity, alkalinity
Footnote
(a) On-site analyses
POLYPHOSPHATE
ADDITION
DISTRIBUTION
SYSTEM
m
1
6°
"En
m
S3
1
(IN)
(AC)
(TA)
CTB)
(TT)
rewj
Css)
INFLUENT
DA: C12
LEGEND
Influent
After Chlorination
After Vessel A
After Vessel B
After Vessels A and B
Backwash Wastewater
Sampling Location
Backwash Solids
Sampling Location
Unit Process
Chlorine Disinfection
Process Flow
Backwash Flow
pH(a), temperature^3),
DO/ORPW, As (total), Fe (total),
Mn (total), SiO2, PO4, turbidity,
alkalinity
Figure 3-1. Process Flow Diagram and Sampling Locations
-------
volume over the duration of the backwash for each vessel. After the content in the container was
thoroughly mixed, composite samples were collected and/or filtered onsite with 0.45-(im disc filters.
Analytes for the backwash samples are listed in Table 3-3. Only soluble As, Fe, and Mn, pH, turbidity,
and total dissolved solids (TDS) were analyzed for grab samples. For composite samples, total As, Fe,
Mn, and total suspended solids (TSS) also were analyzed.
3.3.4 Backwash Solids Sample Collection. Backwash solid samples were collected from 1-gal
plastic jars containing backwash water/solids collected during backwash events on May 12, May 31, and
June 21, 2005. After solids in the jar were settled and the supernatant was carefully decanted, residual
solids samples were collected for processing and analysis by Battelle. A portion of each solids sample
was air-dried, acid-digested, and analyzed for Al, As, Ca, Cd, Cu, Fe, Mg, Mn, Ni, P, Pb, Si, and Zn.
3.3.5 Media Sample Collection. Media samples were collected on August 4, 2005, by STS while
its technicians were onsite to investigate the cause of shortened run times between backwashes. As part
of the inspection, media samples were collected at the top and 14 in below the top of the media beds
before and after backwash. Media samples were extracted from the media beds via a clean heavy-walled
garden hose under vacuum-induced siphon. The media samples were collected separately into 5-gal
buckets. A portion of each sample was air-dried and analyzed for Al, As, Ca, Cd, Cu, Fe, Mg, Mn, Ni, P,
Pb, Si, and Zn.
3.3.6 Distribution System. Water samples were collected from the distribution system to
determine the impact of the arsenic treatment system on water chemistry in the distribution system,
specifically, the lead and copper level. From December 2003 through March 2004, four sets of baseline
distribution system water samples were collected monthly by the plant operator at three homes that had
been included in the Prospect Bay Lead and Copper Rule (LCR) sampling in the past. Following system
startup, distribution system sampling continued on a monthly basis at the same three locations.
The samples collected at the LCR locations were taken following an instruction sheet developed
according to the Lead and Copper Monitoring and Reporting Guidance for Public Water Systems
(EPA, 2002). The first draw sample was collected from a cold-water faucet that had not been used for at
least six hours to ensure that stagnant water was sampled. The sampler recorded the date and time of last
water use before sampling and the date and time of sample collection for calculation of the stagnation
time. Analytes for the baseline samples coincided with the monthly distribution system water samples as
described in Table 3-3. Arsenic speciation was not performed for the distribution water samples.
3.4 Sampling Logistics
All sampling logistics including arsenic speciation kits preparation, sample cooler preparation, and
sample shipping and handling are discussed below.
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 EPA-endorsed QAPP (Battelle, 2003).
3.4.2 Preparation of Sampling Coolers. For each sampling event, a cooler was prepared with the
appropriate number and type of sample bottles, disc filters, and /or speciation kits 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), data 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
10
-------
code for a specific sampling location, and a one-letter code designating the arsenic speciation bottle (if
necessary). The sampling locations at the treatment plant were color-coded for easy identification. For
example, red, orange, yellow, and green were used to designate sampling locations for IN, TA, TB, and
TT, respectively. The labeled bottles for each sampling location were placed separately in one of the
plastic bags (each corresponding to a specific sampling location) and packed in the cooler. When arsenic
speciation samples were to be collected, an appropriate number of arsenic speciation kits also were
included in the cooler. When appropriate, the sample cooler was packed with bottles for the three
distribution system sampling locations and/or the two backwash sampling locations (one for each vessel).
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
sampling 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 offsite 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 sample cooler tracking log.
Samples for metal analyses were stored at Battelle's Inductively Coupled Plasma-Mass Spectrometery
(ICP-MS) Laboratory. Samples for other water quality analyses were packed in coolers at Battelle and
picked up by couriers from Battelie's subcontract laboratories, including American Analytical
Laboratories (AAL) in Columbus, OH and TCCI Laboratories in New Lexington, OH. 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.
11
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4.0 RESULTS AND DISCUSSION
4.1
Facility Description
The water system supplied drinking water to approximately 300 connections in the community of
Prospect Bay at Grasonville in Queen Anne's County, MD. Source water was extracted from two wells,
i.e., Wells No. 1 and No. 2, which alternated in operation on a daily basis to supply roughly half of the
total production by each well. Well No. 1, located off Prospect Bay Road near the Prospect Bay Golf
Course and Country Club, was chosen for treatment in the arsenic adsorption system as part of this
demonstration study. Figure 4-1 shows Well House No. 1.
Well No. 1 was drilled to a depth of approximately 360 ft and estimated, prior to the beginning of the
demonstration study, to operate for about 3 to 4 hr/day, every other day, at a rate of about 300 gpm. Prior
to entering the distribution system, water was disinfected using chlorine gas (Figure 4-2) and treated for
corrosion inhibition with polyphosphate. Historical operational data from QAC indicated that chlorine
residuals in the treated water typically were about 0.5 mg/L (as C12) or less and that the target
polyphosphate concentration was 0.8 mg/L.
Figure 4-1. Existing Well House No. 1
4.1.1 Source Water Quality. Source water samples were collected at a sampling tap located
outside Well House No. 1 on August 7, 2003, and analyzed as shown in Table 3-3. The results of the
source water analyses, along with those provided by the facility to EPA for the demonstration site
selection and those independently collected and analyzed by EPA, are presented in Table 4-1.
12
-------
Figure 4-2. Chlorine Gas System at Well No. 1
Total arsenic concentrations in source water ranged from 17.0 to 19.0 |o,g/L. Based on the August 7,
2003, speciation sampling results, arsenic was present primarily as soluble As(III) (i.e., 98% of
18.8 |og/L) with only a small amount existing as particulate As (i.e., 0.1 |og/L) and soluble As(V) (i.e.,
0.3 ng/L).
pH values of source water samples varied between 6.0 and 8.3, which was within the range recommended
by STS. Therefore, pH adjustment was not recommended.
Source water iron levels ranged from <50 to 1,660 |o,g/L; however, more recent data indicated that iron
levels were around 300 |o,g/L or less and that iron existed primarily in the soluble form. Manganese
concentrations ranged from 0.4 to 8 (ig/L. Because iron and manganese concentrations were sufficiently
low, pretreatment prior to the adsorption process was not recommended. Concentrations of
orthophosphate ranged from <0.1 to 0.4 mg/L and silica from 13.3 to 14.5 mg/L (as SiO2). SORB 33™
media were reported to be affected by silica at levels greater than 40 mg/L (Meng et al., 2000 and 2002)
and phosphate at levels greater than 1 mg/L. Neither of these compounds is expected to affect arsenic
adsorption onto the media.
4.1.2 Pre-Demonstration Treated Water Quality. Treated water samples after post-chlorination
were collected by QAC and EPA prior to the demonstration study and analyzed for a number of analytes
shown in Table 4-1. As expected, because the treatment process prior to distribution included only
chlorination and the addition of polyphosphate, concentrations of these constituents in the
13
-------
Table 4-1. Prospect Bay Water Quality Data
Parameter
Unit
Sampling Date
PH
Total Alkalinity
Hardness (as CaCO3)
Turbidity
Chloride
Fluoride
Sulfate
Silica (as SiO2)
Orthophosphate (as P)
TOC
As (total)
As (total soluble)
As (paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Al (total)
Al (soluble)
Mn (total)
Mn (soluble)
V (total)
V (soluble)
Mo (total)
Mo (soluble)
Sb (total)
Sb (soluble)
Na
Ca
Mg
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
HB/L
^g/L
^g/L
HB/L
^g/L
HB/L
^g/L
HB/L
^g/L
^g/L
HB/L
^g/L
HB/L
^g/L
HB/L
^g/L
HB/L
mg/L
mg/L
mg/L
Utility
Raw
Water
Data
NA
8.3
150
91.0
NS
1.5
NS
5.8
14.5
0.4
0.5
17.0
NS
NS
NS
NS
300
NS
NS
NS
8.0
NS
NS
NS
NS
NS
NS
NS
27.0
20.0
9.7
EPA
Raw
Water
Data
10/04/02
NS
137
98.0
NS
16.7
NS
4.3
13.4
NS
NS
19.0
NS
NS
NS
NS
95.0
NS
<25
NS
0.4
NS
NS
NS
NS
NS
<25
NS
24.1
23.3
9.7
EPA
Treated
Water
Data
10/04/02
NS
NA
NA
NS
NA
NS
4.2
13.3
NS
NS
18.0
NS
NS
NS
NS
91.0
NS
<25
NS
0.8
NS
NS
NS
NS
NS
<25
NS
23.6
23.0
9.5
Battelle
Raw
Water
Data
08/07/03
7.3
168
102
NS
1.4
1.0
4.3
14.1
0.1
NA
18.8
18.7
0.1
18.4
0.3
270
254
<10
<10
1.5
1.4
0.
O.
0.
O.
0.
0.
26.2
23.5
10.4
QAC
Raw
Water
Data
2002-
2003
6.0-8.2
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
<50-1,660
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
QAC
Treated
Water
Data
2002-
2003
6.7-8.2
150
91
NS
1.6
NS
5.3
NS
0.038
0.50
17.0-18.0
NS
NS
NS
NS
<50-1,100
NS
NS
NS
<5.0-9.0
NS
NS
NS
NS
NS
NS
NS
24.0
21.0
9.4
NA = Not Available
NS = Not Sampled
TOC = total organic carbon
treated water were very similar to those of raw water. Total arsenic concentrations in the treated water
ranged from 17 to 18 |o,g/L. Iron concentration ranged from <50 to 1,100 |o,g/L and manganese from 0.8
to 9 (ig/L. pH values of the treated water ranged from 6.7 to 8.2 based on historical data from the years
2000 to 2003.
4.1.3 Distribution System. The Prospect Bay distribution system consists of a looped drinking
water distribution line supplied by two production wells (Well No. 1 and Well No. 2). Prior to the
demonstration study, the two wells alternated operation on a daily basis, such that each well supplied
roughly half of the total production to the community. The water is sent to a 300,000-gal storage tank,
14
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which serves to supply the distribution system constructed primarily of poly vinyl chloride (PVC) pipe.
The connections to the distribution system and piping within the residences are primarily PVC and some
copper pipe. It is estimated that a few homes may have pipe with lead solder and that no homes have lead
pipe.
The QAC Department of Public Works samples water from the distribution system for various
parameters. Each month, five locations within the distribution system are sampled for bacterial analysis.
The water also is sampled for volatile organic compounds (VOCs) on a regular basis. Under the EPA
LCR, samples are collected from customer taps at five residences every three years.
4.2
Treatment Process Description
The STS arsenic package unit (APU) is designed for arsenic removal for small systems with flowrates
greater than 100 gpm. It uses Bayoxide® E33 (branded as SORB 33™ by STS), an iron-based adsorptive
media developed by Bayer AG, for the removal of arsenic from drinking water supplies. Table 4-2
presents vendor-provided physical and chemical properties of the media.
Table 4-2. Physical and Chemical Properties of SORB 33™ Media
(a)
Parameter
SORB 33™ Media
Physical Properties
Matrix
Physical Form
Color
Bulk Density Qb/ft3)
BET Area (m2/g)
Attrition (%)
Moisture Content (%)
Particle Size Distribution (U.S. Standard Mesh)
Crystal Size (A)
Crystal Phase
Iron oxide composite
Dry granules
Amber
28.1
142
<15% (by weight)
10
70
A - FeOOH
Ch emical An alysis
Constituents
FeOOH
CaO
MgO
MnO
S03
Na20
Ti02
Si02
A1203
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
(a) Provided by STS.
BET = Brunauer, Emmett, and Teller
15
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The SORB 33™ media are delivered in a dry crystalline form and listed by NSF International (NSF)
under Standard 61 for use in drinking water applications. The media exist in both granular and pelletized
forms, which have similar physical and chemical properties, except that pellets are denser than granules
(i.e., 35 vs. 28 lb/ft3). The granular form of the media was used for the Prospect Bay facility.
The STS APU-300 arsenic removal treatment system consisted of two adsorption vessels, an electrically
actuated valve tree, and associated piping and instrumentation. Electrically actuated butterfly valves
diverted raw water downward through the two adsorption vessels operating in parallel. As water passed
through the fixed-bed adsorbers, arsenic concentrations were reduced to below 10 |o,g/L. When reaching
10-|o,g/L arsenic breakthrough, the spent media would be removed and disposed of after being subjected
to the EPA Toxicity Characteristic Leaching Procedure (TCLP) test. Figure 4-3 shows the APU-300
system at the manufacturing facility prior to shipment to the site. Figure 4-4 is a simplified piping and
instrumentation diagram (P&ID) of the system. The design features of the APU-300 system are
summarized in Table 4-3. Key process components are discussed as follows:
• Intake. Raw water from Well No. 1 was fed from the wellhead via 4-in ductile iron pipe to
the system via 4-in Schedule 80 PVC pipe. The amount of water pumped was tracked with a
flow totalizer (Data Industrial Corp.) installed at the wellhead (Figure 4-5).
• Chlorination. During the first four months of system operation, chlorine was added at the
end of the treatment train following the APU-300 adsorption vessels. In late September
2004, total arsenic levels in the treated water rose to above 10 |o,g/L after treating only 7,400
BV of water, much earlier than projected (see Table 4-3). The speciation results showed that
the majority of arsenic passing through the SORB 33™ media was As(III). To improve
performance, the chlorine injection point was relocated upstream of the adsorption vessels on
November 9, 2004. With this prechlorination step in place, As(III) was oxidized to As(V)
before coming in contact with the media.
The chlorine gas feed rate was controlled by a panel-mounted automatic switchover rotameter
at 12 Ib/day. The chlorine gas was injected to a side stream where it was mixed with carrier
water prior to being drawn into the main line. The chlorinated water then flowed into the two
adsorption vessels. A sample tap at the AC location was installed on a common feed line to
the adsorption vessels to collect samples of chlorinated water prior to treatment by the APU-
300 system.
• Adsorption System. The APU-300 system was a fixed-bed down-flow adsorption system
consisting of two 63-in-diameter, 86-in-tall vertical pressure vessels, constructed of fiberglass
reinforced plastic (FRP). Each vessel contained approximately 80 ft3 of SORB 33™ media
supported by a gravel underbed. The skid-mounted vessels operated in parallel and were
rated for 75 pounds per square inch (psi) working pressure. Empty bed contact time (EBCT)
for the system was 4.0 min based on a design flowrate of 300 gpm. Hydraulic loading to
each vessel was approximately 6.9 gpm/ft2.
As illustrated in Figure 4-5, the two adsorption vessels were interconnected with schedule 80
PVC piping and 10 electrically actuated butterfly valves using a valve tree design (Figure 4-
5). During normal operation, the feed valves (i.e., BF-121 A and B) and effluent valves (i.e.,
BF-122 A and B) were opened and the other six valves were closed to divert water downward
through the two adsorption vessels. Flow through the two vessels was balanced by throttling
the effluent valves, if needed. During backwash, the feed and effluent valves were closed and
the backwash feed valves (i.e., BF-123 A and B) and backwash effluent valves (i.e., BF-124
16
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Figure 4-3. APU-300 Treatment System Prior to Shipment
Figure 4-4. Schematic of APU-300 System
17
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Table 4-3. Design Specifications of APU-300 System
Parameter
Value
Remarks
Pretreatment
Chlorine Dosage (Ib/day as C12)
12(a)
-
Adsorption
Number of Adsorption Vessels
Vessel Configuration
Vessel Size (in)
Type of Media
Media Volume (ft3/vessel)
Media Bed Depth (in)
Freeboard Depth (in)
Design Flowrate (gpm/vessel)
Hydraulic Loading Rate (gpm/ft2)
EBCT (min)
2
Parallel
63 x86
SORB 33™
80
44
22
150
6.9
4.0
-
-
-
-
160 ft3 total
-
-
300 gpm total
Based on vessel cross sectional area of
21.6 ft2 given an inner diameter of 63 in
Based on design flow
Backwash
Frequency (day)
Flowrate (gpm)
Hydraulic Loading Rate (gpm/ft2)
Duration (mm/vessel)
Fast Rinse Duration (mm/vessel)
Wastewater Produced (gal/vessel)
45
200
9.2
20
4
4,800
-
-
-
-
-
-
System Operation
Average Use Rate (gal/day)
Estimated Working Capacity (BV)
Throughput (BV/day)
Estimated Throughput to 10 (o,g/L As
Breakthrough (gal)
Estimated Media Life (month)
72,000
114,000(b)
60
136,400,000
63
Based on 4 hr/day operation at 300 gpm
BV to 10 (o,g/L total arsenic breakthrough
based on an influent arsenic concentration
of 19 (o,g/L and a BV of 160 ft3
Based on 4 hr/day operation at 300 gpm
Based on a bed volume of 160 ft3
Estimated frequency of changeout at 17%
utilization
(a) Switched from post-chlorination
(b) Based on STS provided estimate
to prechlorination on November 9, 2004.
with an influent As concentration of 19 |J.g/L.
A and B) were opened to divert water upward through the two adsorption vessels. During the
backwash rinse process, the feed valves (i.e., BF-121 A and B) and rinse valves (i.e., BF-125
A and B) were opened and the other six valves were closed to rinse the media with downward
water flow.
The flow meters (i.e., FI-151 A and B, +GF+SIGNET 8550 ProcessPro™ Flow Transmitter)
installed in the supply line of each adsorption vessel monitored instantaneous flowrates
through the vessels. The flow meters also tracked the volume of water treated in each vessel.
The differential pressure (Ap) across each vessel was monitored by differential pressure
gauges (i.e., PDI-173 A & B, WIKA Differential Pressure Gauge). The adsorption vessels
were backwashed sequentially whenever the Ap across one vessel reached 10 psi.
Backwash. STS recommended that the SORB 33™ media be backwashed using raw water
approximately once every 45 days to loosen up the media bed and remove media fines and/or
particles accumulated in the beds. The APU-300 system was designed and programmed with
18
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an automatic backwash feature that would place the vessels into backwash based on a set
timer or when the (Ap) across a vessel reached 10 psi. However, backwash of the APU-300
system installed at QAC was initiated manually by the system operator because there was no
onsite disposal facility to receive the backwash wastewater. Backwash was initiated
whenever the differential pressure of Vessels A and B approached 10 psi. The backwash
wastewater was discharged into a tanker truck and transported to a local wastewater treatment
plant.
Figure 4-5 Treatment Process Components
(Clockwise from Top: Well No. 1 Totalizer; APU-300 System Valve Tree;
APU-300 Control Panel; and FI-151A and B Flow Meter Sensors)
19
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4.3
System Installation
The construction of the treatment building and the installation of the STS APU-300 system were
completed on June 24, 2004, by Stearns and Wheler, LLC, a local engineering subcontractor hired by
QACandSTS.
4.3.1 Permitting. Prepared by Stearns and Wheler, LLC, the engineering plans for the system
permit application included a site plan, construction drawings of the new treatment building, and process
and mechanical drawings of the APU-300 treatment system. The plans, along with a construction permit
application, were submitted to the Maryland Department of the Environment (MDE) for review on March
12, 2004. The MDE replied with comments on the engineering package on April 23, 2004, and issued a
letter of approval for operation of the treatment system on June 15, 2004.
4.3.2 Building Construction. QAC constructed an addition to its existing pump house (Well
House No. 1) to contain the APU-300 treatment system. The addition included a 16-ft * 23-ft treatment
area onto the existing 8-ft x 16-ft well house. The building was constructed using concrete block with
brick siding and included a 10-ft-wide rollup door on the end of the building and access hatches in the
roof to facilitate future media replacement. A photograph of the building housing the equipment is shown
in Figure 4-6. Building construction began on May 17, 2004, and was completed on June 24, 2004,
including placement and setting of the vessels within the building, which were put into place before the
roof was installed.
Figure 4-6. New Treatment Building Addition with Two Access Hatches on Roof
4.3.3 System Installation, Shakedown, and Startup. The APU-300 system was shipped on May
26, 2004, and arrived at the site on June 1, 2004. Stearns and Wheler, LLC performed the off-loading and
installation of the system, including all plumbing, mechanical, and electrical work and connections of the
treatment system to the existing entry and distribution piping. A photograph of the system being
20
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unloaded and set in place with a crane is shown in Figure 4-7. The system mechanical equipment
installation was completed by June 11, 2004. Gravel underbedding was placed in the vessels on June 15,
2004, and the adsorption media were loaded in both vessels on June 16, 2004. A bacteria test sample,
required by the state, was collected on June 16, 2004 from the system, which had previously been treated
with chlorine for disinfection. Once the media were loaded, Stearns and Wheler conducted a pressure test
of the system piping. The system was backwashed for media conditioning prior to service on June 17,
2004. The results from the bacteria test, received on June 17, were negative.
Figure 4-7. Unloading of APU Skid into Partially Completed
Treatment Building Addition
Battelle, STS, Stearns and Wheler, LLC, and representatives from QAC were on site to complete system
shakedown and startup procedures on June 29, 2004. All backwashing and system shakedown procedures
were completed prior to this date, so that the system was ready to go into regular service operation.
Battelle provided operator training on data and sample collection and conducted a review of the P&ID
and system checklist with the vendor. The system was put into regular service mode on June 30, 2004.
4.4
System Operation
4.4.1 Operational Parameters. The system operational parameters are tabulated and attached as
Appendix A with the key parameters summarized in Table 4-4. The plant operation data were recorded
from the beginning of the performance evaluation study on June 30, 2004, through April 2, 2007, which
marked the end of the study.
21
-------
Table 4-4. Summary of APU-300 System Operation
Operational Parameter
Duration
Cumulative Operating Time (hr)
Range of Daily Operation Time (hr/day)
Average Daily Operating Time (hr/day)
Adsorption Vessel
Throughput (kgal)
Average Flowrate (gpm)
Range of Flowrate (gpm)
Average EBCT (min)(b)
Range of EBCT (min)(b)
Differential Pressure across Bed (psi)
System Pressure Loss (psi)
Value/Condition
06/30/04-04/02/07
(Weeks 1 through 144)
5,890
0-23.4
6.2
A
36,984
107
30-198
5.6
3.0-20.0
0.8-13.2
NA
B
34,549
100
32-207
6.0
2.9-18.7
1.2-16.6
NA
Total
71,533
207
NA
NA
NA
NA
1-32
(a) System down between 11/03/05 and 12/12/05 due to drilling of a new well in well
house No. 1 and back online on 12/13/05.
(b) Calculated based on 80 ft3 of media in each vessel.
NA = not applicable
Between June 30, 2004, and April 2, 2007, Well No. 1 operated for a total of 5,890 hr based on the well
pump hour meter readings. As shown in Figure 4-8, daily operating times fluctuated significantly from 0
to 23.4 hr and averaged 6.2 hr. Seasonal variations were observed with relatively longer operating time
starting from late spring through early autumn. During that period, the operating time often exceeded
12 hr/day. In the remainder of the year, the operating time was usually less than 12 hr/day.
24 -,
20 -.r
e
E. 16
I 12
•g
oi
Q.
O
4 •_
^
.^
* * "
.•
*
*»
CN CXI
^ ^ £N
O T- CM
LO LO LO LO LO LO LO
O O O O O O O
o o ^ o o o o
CN CN LO CN CN CN CN
CD T- LO CO CN LO CO
CXI CXI CXI CXI
o o o o o o o
CN CN CO
CN CN CN
^ CO CD
O CO CD
Measurement Date
Figure 4-8. APU-300 Treatment System Daily Operating Time
22
-------
Throughputs based on the totalizers installed on the adsorption vessels were 36,984,000 gal for Vessel A
and 34,549,000 gal for Vessel B. Therefore, the total system throughput was 71,533,000 gal, or 59,800
BV, assuming 80 ft3 of media in each vessel. Note that the totalizers were not functioning correctly
during January 13 through March 7, 2006, and July 23 through December 5, 2006, for Vessel A and from
August 14 through October 2, 2006, for Vessel B, as evidenced by uncharacteristically low throughput
and flowrate readings recorded. During these periods, daily throughputs were estimated by multiplying
the average flowrate (i.e., 107 gpm for Vessel A and 100 gpm for Vessel B) by daily operation time. The
Vessel A totalizer was replaced on March 7 and December 7, 2006, and the Vessel B totalizer was
replaced on October 2, 2006. The problems associated with the totalizers are further discussed in Section
4.4.5.
Figure 4-9 compares the daily average flowrate at the wellhead with the flowrate through each vessel.
The daily average flowrate at the wellhead was calculated by dividing the daily volume recorded by the
wellhead totalizer by the daily operating time. Tthe flowrates through each vessel fluctuated significantly
but around 100 gpm most of the time. The exceptions occurred during the periods when the vessel
totalizers were not operating correctly. Excluding the data collected during these periods, an average
flowrate of 107 gpm was calculated for Vessel A and 100 gpm for Vessel B. The average flowrate
through Vessel A was 7% higher than that through Vessel B, indicating slightly imbalanced flows (i.e.,
51.7% through Vessel A vs. 48.3% through Vessel B). The flowrates calculated based on the totalizer at
the wellhead averaged 234 gpm, which was about 13.6% higher than the 207 gpm measured at Vessels A
and B. The average EBCTs in Vessels A and B based on the respective average flowrates were 5.6 and
6.0 min, respectively, which were 40 to 50% higher than the design value of 4.0 min as shown in Table 4-
3.
Figure 4-10 presents measured pressures of the APU-300 treatment system. Prior to the switch to
prechlorination, inlet pressure readings remained relatively constant between 60 to 65 psig for most
measurements. Immediately after the switch, inlet pressure levels increased significantly to between 65 to
75 psig, and then to between 70 to 80 psig for the remainder of the performance evaluation study. Outlet
pressure maintained relatively constant between 54 to 60 psig throughout the entire study duration. The
increase in inlet pressure was caused primarily by the accumulation of iron solids in the adsorption
vessels.
Figure 4-11 presents differential pressure (Ap) readings across the media beds. Prior to the switch to
prechlorination, Ap readings were low, ranging from 2 to 3 psi. Following the switch on November 9,
2004, Ap readings began to rise from about 2.0 to 4.5 psi with 455 BV of water treated. A backwash was
performed on November 17, 2004, at 10,579 BV and the Ap reading returned to the original level around
2 psi. Prior to this, no backwash had been performed. Soon after the backwash, Ap readings began to rise
steadily and approached 10 psi after treating approximately 2,359 BV of water. Backwashing was
performed again on January 12, 2005, at 12,938 BV. It was believed that this Ap rise was caused by the
accumulation of iron solids in the media beds due to the addition of chlorine before the adsorption
vessels.
As presented in Figure 4-12, over the course of the performance evaluation study, the run times between
two consecutive backwash cycles shortened significantly from 2,359 BV per backwash initially to less
than 800 BV per backwash by the end of the study (or once every two months to less than two weeks).
After being contacted by Battelle for the shortened run times, a representative from STS was onsite to
inspect the system on August 3 to 4, 2005. The inspection included internal of the tanks, backwash
process, and media (including performing media sampling before and after backwash using the method
23
-------
a
s
o
u.
a>
O>
5
-------
Figure 4-11. Differential Pressure Readings across Adsorption Vessels
-------
3000000 -,
2750000 -
2500000 -
2250000 -
2000000 -
1750000 -
1500000 -
1250000 -
1000000 -
750000 -
500000 -
250000 -
-Gallon of Water Treated
-BV of Water Treated
-r 3000
2500
2000
1500
1000
500
Backwash Date
Figure 4-12. Water Production between Two Consecutive Backwash Events
described in Section 3.3.5). Measurements of vessel freeboard revealed that about 6 to 8 in of media had
been lost. Because no freeboard measurements were conducted since August 5, 2005, it was not clear if
the vessels continued to lose media in the remainder of the evaluation study. Sampling of the media at the
bed surface and 14 in below immediately after backwash showed that media fines sized roughly 1/10 to %
of virgin granules constituted the top 2 to 3 in of the beds. The reduced media size suggested that media
fines were produced during adsorption/backwash cycles and not completely removed during backwash.
Although mostly at the top of the beds, some media fines might be accumulating in the media beds,
thereby reducing bed porosity. This, along with the iron particles removed during adsorption cycles,
caused Ap to rise more rapidly, thus shortening the run times between backwashes. Some iron particles
also might be accumulating in the media beds, which also could reduce bed porosity and cause shortened
run times.
Media attrition during backwash appeared to be the main reason for the increasingly frequent backwashes
observed. During the initial four months of operation without prechlorination, Ap across the media beds
was low at 2 to 3 psi even with no backwash. After the switch to prechlorination, backwashes were
conducted to remove iron particles generated following prechlorination. The more backwashes that were
performed, the more media fines were generated, causing run times to shorten. Similar deteriorating
media integrity also was observed at other EPA arsenic demonstration sites, including Rollinsford
(Cumming et al., 2008), Desert Sands (Chen et al., 2008b), and Brown City (Chen et al., 2008a). It was
not clear, however, if chlorine would cause any adverse effects on media integrity. All of the
demonstration sites referenced have been using chlorine prior to the adsorption vessels.
26
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4.4.2 Previous System Design Changes. Prior to shipment of the system to Prospect Bay, it was
modified from its original design with revised plumbing that included replacement of the 3-in-diameter
system piping with 4-in-diameter; removal of the diaphragm valves, restrictive orifices, and valve
controllers; and installation of a nested system of fully ported actuated butterfly valves, and a new control
panel. A diagram of the APU-300 system as installed at Prospect Bay is shown in Figure 4-4. These
modifications were made due to operational problems experienced by APU-300 systems previously
installed at the Desert Sands Mutual Domestic Water Consumers Association (MDWCA) in Anthony,
NM, and Brown City, MI, as part of the arsenic demonstration studies. Both of these systems
experienced operational issues related to flow restriction, flow imbalance, and excessive pressure losses
(Chen et al, 2008a and 2008b). To troubleshoot these operational problems, STS performed a series of
systematic hydraulic testing at its Torrance, CA fabrication shop and at the Brown City, MI site. The
results of this testing indicated that the flow restrictions and elevated pressure drop issues were caused
primarily by the programmable Fleck valve controller and the restrictive orifices included in the original
systems. After considering several options, STS retrofitted the systems as described above with larger
diameter pipe and removed certain system components determined to have caused excessive flow
restrictions and pressure loss.
All such system modifications were completed on the APU-300 system for Prospect Bay prior to
shipment from the manufacturing facility in Torrance to the site in Maryland. With these modifications
already in place, the Prospect Bay system operated as expected during the performance evaluation study
and did not experience any issues observed previously at the other two locations.
4.4.3 Backwash Operation. The APU-300 system was designed and programmed with an
automatic backwash feature that would trigger either vessel into backwash by a set Ap (i.e., 10 psi) or a
set time. However, backwash of the APU-300 system at QAC was initiated manually by the system
operator because there was no onsite disposal facility to receive the backwash water. The backwash
water was discharged into a tanker truck and transported to a local wastewater treatment plant.
The APU-300 system was not backwashed during the first four months of system operation because Ap
readings across both adsorption vessels remained low and because the backwash wastewater produced
would require offsite disposal. Following the switch to prechlorination, Ap readings began to rise from
about 2.0 to 4.5 psi. A backwash was performed on November 17, 2004, with each vessel backwashed
separately at a flowrate of 200 gpm for 20 to 25 min. A total amount of 9,500 gal backwash wastewater
was generated during the initial backwash event. During the performance evaluation study, the system
was backwashed a total of 50 times. The backwash duration of each vessel was programmed on the
programmable logic controller (PLC) and averaged 24 min including a 4-min rinse step. The amount of
wastewater produced averaged 9,985 gal/backwash and totaled 499,231 gal for both vessels combined.
4.4.4 Residual Management. Residuals typically produced by the operation of the APU-300
system include spent media and backwash wastewater. The media were not exhausted during the
performance evaluation study; therefore, the only residual produced was backwash wastewater. Because
there was no onsite disposal facility, the backwash water was discharged into a tanker truck and
transported to the Stevensville Wastewater Treatment Plant (WWTP) for disposal. The Stevensville
WWTP also is owned and operated by QAC.
4.4.5 System/Operation Reliability and Simplicity. Because all relevant system modifications
related to operational issues were completed prior to shipment of the system, no major operational
problems were encountered. The primary source of concerns during the study was the shortened run times
between backwash cycles. Other O&M issues encountered included problems with the flow meters
installed on Vessels A and B and a butterfly valve assembly necessary for backwash. The flow meter for
Vessel A was out of order and was replaced on March 7, 2006, and December 5, 2006. The flow meter
27
-------
for Vessel B also was replaced October 2, 2006. On May 18, 2006, the butterfly valve that initiated
automatic backwash on Vessel B was not opening/closing properly. Backwash had to be initiated by
manually turning the valve. A new butterfly valve was ordered and installed on September 29, 2006.
The simplicity of system operation and operator skill requirements are discussed below in relation to pre-
and post-treatment requirements, levels of system automation, operator skill requirements, preventive
maintenance activities, and frequency of chemical/media handling and inventory requirements.
Pre- and Post-Treatment Requirements. During the first four months of operation, no pretreatment was
implemented at the site. In early November 2004, the treatment system was modified to include a new
chlorine addition point upstream of the adsorption vessels to oxidize As(III) to As(V) and improve the
adsorption capacity of the media. Post-treatment consisted only of the addition of polyphosphate as a
corrosion inhibitor using the preexisting polyphosphate feed system.
System Automation. All major functions of the APU-300 system can be automated and require only
minimal operator oversight and intervention. Automated processes include system startup in the forward
feed mode when the well energizes, backwash cycling based on time or pressure triggers, fast rinse
cycling, and system shutdown when the well pump shuts down.
Operator Skill Requirements. Under normal operating conditions, skills required to operate the system
were basic and limited to observation of equipment integrity and recording of operating parameters, such
as pressure, flow, and system run time. The operational setup was intuitive and all major system
operations were automated as described above. The daily demand on the operator was typically only 10
to 15 min to allow the operator to visually inspect the system and record the operating parameters on the
daily log sheets. The time requirement does not include travel time to and from the site.
Based on the treatment technology, the State of Maryland requires Category T-Class 5 certification for the
operation of the STS treatment system at the Queen Anne's County, MD. Five categories of certificates
are issued by the State of Maryland, i.e. water distribution (Category D), water treatment (Category T),
wastewater treatment (Category W), wastewater collection (Category C), and industrial wastewater
treatment (Category I). Under the Category T (water treatment) there are five levels of certificates, which
are classified according to the treatment technology (as presented in Table 4-5). Each certificate is
process-specific, which ensures that operators are technically-qualified for the processes they are certified
to operate.
Table 4-5. Classification of Water Treatment Plants in State of Maryland
Class
1
2
o
J
4
5
Type of
Treatment Systems
Disinfection
Chemical Treatment
Simple Iron Removal
Complete Treatment
Site Specific
Typical Processes Included
Chlorination
Chlorination, pH control, and fluoridation
Chlorination, pH control, fluoridation, filtration, and iron
removal utilizing ion exchange or contact oxidation processes
Chlorination, pH control, fluoridation, aeration, coagulation,
sedimentation, filtration, and complex iron removal
Any alternative technology plants not covered under the
classification system
28
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Preventive Maintenance Activities. Preventive maintenance tasks recommended by STS included
monthly inspection of the control panel, quarterly checking and calibration of the flow meters, biannual
inspection of the actuator housings, fuses, relays, and pressure gauges, and annual inspection of the
butterfly valves. Further, inspection of the adsorber laterals and replacement of the underbedding gravel
were recommended concurrently with the media replacement. During the performance evaluation study,
maintenance activities performed by the operator included cleaning and repair of the flow meter paddle
wheels on the flow meter for Vessel B, replacing flow meters on both Vessels A and B, and replacing an
automatic butterfly valve necessary to backwash Vessel B.
Chemical/Media Handling and Inventory Requirements. The chemicals required for system operation
included the chlorine gas injection system and the polyphosphate addition system which were both
already in use at the site. Media changeout was not required during the performance evaluation study;
however, replacement media were purchased and stored at the facility to facilitate timely media
changeout once arsenic breakthrough is detected at 10 (ig/L.
4.5 System Performance
The system performance was evaluated based on analyses of water samples collected from the treatment
plant, backwash, and distribution system.
4.5.1 Treatment Plant Sampling. Water samples were collected at four locations throughout the
treatment train: at the inlet (IN), after Vessels A and B (TA and TB), and after the combined effluent
(TT). Following the switch to prechlorination on November 9, 2004, a fifth sampling location was added
after the prechlorination injection point (AC). Overall, during the performance evaluation study, water
samples were collected on 58 occasions with field speciation performed on 39 occasions. Table 4-6
summarizes the minimum, maximum, and average concentrations of As, Fe, and Mn measured prior to
the switch to prechlorination; Table 4-7 summarizes concentrations after the switch to prechlorination on
November 9, 2004. Standard deviations also are included in Tables 4-6 and 4-7. Table 4-8 summarizes
the results of other water quality parameters collected during performance evaluation study. Appendix B
contains a complete set of analytical results collected during this period. The results of the water samples
collected throughout the treatment plant are discussed below.
Arsenic Removal. Figure 4-13 contains three bar charts showing the concentrations of total As,
particulate As, and soluble As(III) and As(V) at the IN, AC, and TT locations for each speciation
sampling event. Total As concentrations in source water ranged from 16.0 to 25.8 |o,g/L and averaged
20.6 |o,g/L (Tables 4-6 and 4-7). Soluble As(III) was the predominating species (about 91% of total As),
ranging from 12.8 to 22.7 |o,g/L and averaging 18.9 |og/L. Particulate As concentrations were low,
averaging 0.5 (ig/L. Soluble As(V) concentrations were typically below the detection limit of 0.1 |o,g/L.
Arsenic concentrations measured in source water during this performance evaluation study were
consistent with those of the source water sample collected on August 7, 2003 (Table 4-1).
The key parameter for evaluating the effectiveness of the SORB 33™ system was the concentration of
arsenic in the treated water. The arsenic breakthrough curve is presented in Figure 4-14 with total arsenic
concentration plotted against the volume of water treated in BV. As shown in the figure, before the
switch to prechlorination (at about 10,200 BV), total arsenic concentrations in the treated water increased
steadily and exceeded, in late September 2004, the target level of 10 (ig/L at 7,400 BV, which was
significantly lower than the vendor-provided working capacity of 114,000 BV (Table 4-3). Because
arsenic existed primarily as As(III) in source water and because As(V) has much higher adsorptive
affinity than As(III), prechlorination was implemented on November 9, 2004. Chlorine gas was applied
at a rate of 12 Ib/day, equivalent to a dosage of 3.6 mg/L (as C12) assuming complete dissolution of
chlorine gas in water. The chlorine residual measured at the plant tap just prior to entering the
29
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Table 4-6. Summary of Arsenic, Iron, and Manganese Analytical Results Prior to Switch to
Prechlorination (July 7 to November 3, 2004)
Parameter
As
(total)
As
(soluble)
As
(paniculate)
As(III)
As(V)
Fe
(total)
Fe
(soluble)
Mn
(total)
Mn
(soluble)
Sampling
Location
IN
TA
TB
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TA
TB
TT
IN
TT
IN
TA
TB
TT
IN
TT
Unit
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
^ig/L
Number
of
Samples
12
7
7
6
5
4
5
4
6
6
5
4
12
7
7
6
5
4
12
6(b)
7
6
5
4
Minimum
Concentration
18.4
0.7
0.3
0.3
19.0
0.2
<0.1
<0.1
12.8
0.2
0.1
<0.1
193
<25
<25
<25
161
<25
1.4
1.2
0.8
1.5
1.5
1.5
Maximum
Concentration
25.8
14.8
12.9
13.3
22.0
13.1
0.8
0.2
22.4
13.2
8.1
0.3
315
77
38
116
222
80
6.0
6.8
9.6
6.7
3.1
5.9
Average
Concentration
21.0
_(a)
-
-
20.6
-
0.3
-
18.7
-
1.7
-
241
-
-
-
195
-
2.4
4.4
4.9
4.4
2.0
3.5
Standard
Deviation
2.2
-
-
-
1.3
-
0.3
-
4.0
-
3.6
-
36
-
-
-
24
-
1.4
2.1
2.9
2.0
0.7
1.9
(a) Not meaningful for data related to breakthrough curves; see Figures 4-13 and 4-15 and Appendix B for
results.
(b) One outlier (i.e., 17.9 ug/L on 10/07/07) omitted.
One-half detection limit used for samples with concentrations less than detection limit; duplicate samples included
for calculations.
distribution system increased from 0.1 to 0.5 mg/L (as C12) approximately 12 hr after the relocation of the
chlorine addition point. Measurements collected over the next two days showed 0.5 to 0.9 mg/L (as C12)
following the treatment system.
The day after the switch to prechlorination, a treated water sample was collected from the TT location and
speciated for arsenic. This sample had a total arsenic concentration of 14.7 (ig/L with arsenic present as
As(III). One week later on November 16, 2004 (or after approximately 220 BV of water had been treated
since the switch to prechlorination), samples were collected from the IN, AC, and TT locations and
speciated for arsenic. As shown in Figure 4-13, As(III) in source water was converted almost completely
to As(V) and particulate As (i.e., 12.0 and 7.7 (ig/L, respectively) after chlorination at the AC location;
however, about 87% of the 12.0 (ig/L of total arsenic in the combined effluent at the TT location
remained as As(III). It was likely that chlorine added to the water was consumed by the As(III) and
ferrous ions previously removed by the media and some As(III) adsorbed by the media were displaced by
As(V) into the treated water. Two weeks later on November 23, 2004 (or after approximately 440 BV of
water had been treated since the switch to prechlorination), total arsenic concentration in the treated water
30
-------
Table 4-7. Summary of Arsenic, Iron, and Manganese Analytical Results after
Switch to Prechlorination (November 9, 2004 to April 2, 2007)
Parameter
As
(total)
As
(soluble)
As
(paniculate)
As(III)
As(V)
Fe
(total)
Fe
(soluble)
Mn
(total)
Mn
(soluble)
Sampling
Location
IN
AC
TA
TB
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TT
Unit
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Number
of
Samples
44
45(a)
16
16
33
28
31
33
28
31
33
28
31
33
28
31
33
4400
45
16(d)
16
33(e)
29«
31
33(g)
44
45
16
16
33
26(h)
31
33
Minimum
Concentration
16.0
16.8
0.3
0.1
0.3
17.4
11.2
0.2
0.1
0.1
0.1
15.2
0.1
0.1
0.1
0.1
0.1
194
<25
<25
<25
<25
44.9
<25
<25
1.2
0.1
0.1
0.1
0.1
1.5
O.I
O.I
Maximum
Concentration
25.2
23.2
6.8
3.8
14.7
26.0
21.1
14.6
3.0
10.1
6.2
22.7
20.9
14.8
10.3
14.0
6.0
473
376
<25
<25
25.4
495
363
<25
14.1
3.8
0.1
3.0
11.5
5.7
3.8
11.5
Average
Concentration
20.1
20.2
.(b)
-
-
20.1
15.4
-
0.7
4.9
-
19.1
6.8
-
1.3
8.7
-
269
230
<25
<25
<25
244
86.1
<25
2.9
1.8
2.1
0.8
1.5
2.5
0.9
1.5
Standard
Deviation
2.0
1.8
-
-
-
1.8
3.3
-
0.8
3.7
-
1.8
8.9
-
2.1
5.8
-
80
63
-
-
-
101
102
-
2.6
0.6
0.7
1.1
2.9
1.3
0.9
2.9
(a) One outlier (i.e., 0.4 ug/L on 12/01/04) omitted.
(b) Not meaningful for data related to breakthrough curves; see Figure 4-13 and Appendix B for results.
(c) Two outliers (i.e., 802 ug/L on 1 1/16/04 and 888 ug/L 01/21/07) omitted.
(d) One outlier (i.e., 30.4 ug/L on 04/25/05) omitted.
(e) Two outliers (i.e., 108 ug/L on 1 1/9/04 and 361 ug/L on 05/1 1/05) omitted.
(f) Two outliers (i.e., 777 ug/L on 1 1/16/04 and 733 ug/L on 01/21/07) omitted.
(g) One outlier (i.e., 61.4 ug/L on 11/9/04) omitted.
(h) Two outliers (i.e., 14.3 ug/L on 11/16/04 and 14.0 ug/L on 01/21/07) omitted.
See Appendix B for complete analytical results.
One-half detection limit used for samples with concentrations less than detection limit; duplicate samples
included for calculations.
31
-------
Table 4-8. Summary of Water Quality Parameter Results
Parameter
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Orthophosphate
(asP)
P (total)
(asP)
Silica
(as SiO2)
Nitrate
(asN)
Turbidity
pH
Temperature
Sampling
Location
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
ug/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
NTU
NTU
s.u.
s.u.
s.u.
s.u.
s.u.
°c
°c
°c
°c
°c
Number
of
Samples
48
36
23
23
30
48
36
23
23
30
31
23
5
5
30
39
2?(a)
22
22
22
13
13
2
48
36
23
23
30
26(b)
21(0
5
4
-------
Table 4-8. Summary of Water Quality Parameter Results (Continued)
Parameter
Dissolved
Oxygen
ORP
Free Chlorine
Total Chlorine
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Sampling
Location
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
AC
PT
AC
PT
IN
AC
TT
IN
AC
TT
IN
AC
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mV
mV
mV
mV
mV
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
Number
of
Samples
41
29
18
17
29
43
29
19
19
30
37
41
37
41
28
25
33
28
25
33
28
25
33
Minimum
Concentration
0.9
1.1
0.8
0.7
2.1
-148
-144
-112
-94.0
-110
0.0
0.0
0.0
0.0
90.9
90.2
90.0
45.6
44.6
44.3
34.9
36.4
36.2
Maximum
Concentration
7.7
6.4
4.8
5.1
6.1
220
603
592
614
612
1.1
1.9
2.2
2.1
117
113
160
67.3
66.7
90.0
54.5
47.4
75.2
Average
Concentration
4.4
3.4
2.4
2.1
4.2
-23
177
86.1
96.3
141
0.3
0.3
0.7
0.7
101
99.3
103
57.9
57.1
58.6
43.4
42.2
44.6
Standard
Deviation
.7
.4
.3
.3
.3
114
204
196
197
196
0.3
0.3
0.6
0.5
6.8
4.7
13.1
5.0
4.1
7.4
4.5
2.9
8.1
(a) Two outliers (i.e., 1.6 and 1.3 mg/L on 12/01/04) omitted.
(b) Three outliers (i.e., 0. 1 mg/L on 02/15/05 and 08/16/05 and 0.2 mg/L on 10/05/05) omitted.
(c) Two outliers (i.e., 0.4 mg/L on 08/16/05 and 0.2 mg/L on 10/05/05) omitted.
(d) One outlier (i.e., 0.1 mg/L on 07/13/04) omitted.
(e) Four outliers (i.e., 0.4 mg/L on 01/26/05, 0.1 mg/L on 02/15/05 and 07/19/05, and 0.6 mg/L on 04/13/05)
omitted
NTU = nephelometric turbidity units
See Appendix B for complete analytical results.
One-half detection limit used for samples with concentrations less than detection limit; duplicate samples included
for calculations.
decreased sharply to 0.9 (ig/L, of which only 0.4 (ig/L existed as As(III) (soluble). Since then, total
arsenic concentrations in treated water were maintained at a level of less than 10 (ig/L.
As shown in Figure 4-13, most samples collected after prechlorination at the AC location contained
mostly soluble As(V) and particulate arsenic, indicating effective oxidation of As(III) with chlorine. The
exceptions were the 10 samples collected on May 11, July 19, August 15, September 21, and December
13, 2005; May 17, August 16, October 17, and November 12, 2006; and March 7, 2007. The results of
speciation sampling indicated that As (III) was the predominating species with levels similar to those in
source water. A careful review of the field data revealed that these samples were collected as the system
was approaching backwash. It happened that the operator usually switched the chlorine injection point
from the pre- to post-chlorination location at this time to help resolve chlorine injection problems due to
buildup of back pressure at the system inlet (Figure 4-10) Because chlorine was not injected prior to the
AC location, As(III) and iron (II) remained to be untreated at the AC location.
33
-------
Arsenic Speciation at Wellhead (IN) at Prospect Bay
'12/07/04: No Sample Collected Date
Arsenic Speciation at Combined Effluent (TT) at Prospect Bay
Fl Una ••HI
n.U.H.H.n.n.n
'10/19/04: No Sample Collected uate
Arsenic Specation after Pre-Chlorination (AC) at Prospect Bay
As (participate
IAS (III)
DAS (V)
Figure 4-13. Concentration of Arsenic Species at IN, AC, and TT Sample Locations
34
-------
nlet (IN)
After Pre-Chlorination (AC)
After Tank A (TA)
After Tank B (TB)
Combined Effluent (TT)
30
40
Water Treated (1,000 BV)
Figure 4-14. Total Arsenic Breakthrough Curve
Figure 4-15 compares average concentrations of As(III), As(V), and participate As in samples collected at
the wellhead and after prechlorination, with the error bars illustrating the standard deviation of the
measurements. The averaged concentrations at the AC location did not include the samples collected on
3,
c
-------
the 10 occasions where prechlorination was not performed. As illustrated in Figure 4-14, chlorine
effectively oxidized As(III), from 91% in source water to 2% after chlorination. After chlorination, 66%
of arsenic was present as soluble As(V) and 32% as particulate As. Soluble As(V) was removed by the
SORB 33™ media via adsorption and particulate As was removed via filtration.
The performance evaluation study demonstrated that prechlorination was effective at increasing SORB
33™ media adsorptive capacity and sustaining media life. The APU-300 system treated approximately
59,800 BV, equivalent to 71,533,000 gal of water, which is about half of the vendor-estimated working
capacity. The averaged total arsenic concentration in the treated water during the last six months of
performance evaluation study was around 5 (ig/L (Figure 4-14), much less than the 10- (ig/L target
concentration requiring media rebedding.
Iron. Figure 4-16 shows total iron concentrations versus BV of water treated across the treatment train
during the performance evaluation study. Total iron concentrations in source water varied from 193 to
473 |o,g/L, with most iron present in the soluble form at concentrations ranging from 44.9 to 495 |o,g/L
(Tables 4-6 and 4-7). Except for the first four months of system operation, SORB 33™ media removed
iron almost completely, with iron concentrations in the treated water below the detection limit of 25 |o,g/L
most of the time.
The SORB 33™ media beds demonstrated the capability to remove soluble iron before the switch to pre-
chlorination (Figure 4-16), when iron in the influent to the bed was present mainly in the soluble form.
While it was not clear how soluble iron was removed, its removal did not appear to be related to iron
precipitation based on the constant Ap readings observed across the adsorption vessels (Figure 4-11).
Before the switch to prechlorination, total iron concentration in the treated water was initially below the
detection limit of 25 |o,g/L. After treating about 9,970 BV of water, total iron concentrations began to
increase, indicating breakthrough of soluble Fe.
150 -
100 -
50 -
Switch to Pre-Chlorination on 11/09/04
10,137BVTreated
-Inlet (IN)
-After Pre-Chlorination (AC)
-Tank A (TA)
-Tank B (TB)
-Combined Effluent (TT)
H/S*
10
20
30 40
Bed Volumes (1,000 BV)
50
70
Figure 4-16. Total Iron Concentrations Versus Amount of Water Treated
36
-------
After the switch to prechlorination, soluble iron in source water was oxidized to Fe(III) and precipitated
as iron solids. The average soluble iron concentration measured after chlorination reduced significantly
from about 91% in source water to 37% after chlorination (Table 4-7). Presumably, the SORB 33™
media beds removed soluble iron by adsorption and iron solids by filtration. The differential pressure
across the media beds started to increase steadily after the switch to prechlorination (Figure 4-11)
indicating gradual accumulation of oxidized solids (mainly iron particles) in the media beds.
Manganese. Figure 4-17 shows total Mn concentrations versus BV of water treated across the treatment
train. Total Mn concentrations in raw water were low, ranging from 1.2 to 14.1 |o,g/L (Tables 4-6 and 4-7)
and existing almost entirely in the soluble form. After approximately 4,500 BV of water treated, total Mn
concentrations in raw and treated water were similar with most values less than 4 |og/L. Since then, but
prior to the switch to prechlorination (at about 10,200 BV), Mn concentrations in the treated water began
to increase, and became higher than those in raw water. It is not clear why Mn concentrations increased
in the treated water.
After the switch to prechlorination in November 2004 through the end of the performance evaluation
study, total Mn concentrations in the treated water were reduced to levels lower than those in source
water. As shown in Table 4-7, the averaged total Mn concentration of the combined effluent was
approximately half of that in source water.
Inlet (IN)
After Pre-Chlorination (AC)
After Tank A
After Tank B
Combined Effluent
30 40
Bed Volumes (1,000 BV)
Figure 4-17. Total Manganese Concentrations Versus Bed Volumes
Other Water Quality Parameters. In addition to arsenic, iron, and manganese, other water quality
parameters were analyzed to provide insight into the chemical processes occurring within the treatment
37
-------
system. The results of the water quality parameters are included in Appendix B and are summarized in
Table 4-8.
Source water pH values ranged from 7.1 to 8.2 and averaged 7.8. The pH values were similar at all
sampling locations across the treatment train. Free and total chlorine were monitored at the AC location
and at a tap just prior to the distribution system (referred to as the Plant Tap, PT, as listed in Table 4-8).
Free chlorine measurements at the AC and PT locations ranged from 0.0 to 1.9 mg/L and total chlorine
levels ranged from 0.0 to 2.2 mg/L (Table 4-8). ORP measurements across the treatment train were
erratic with a wide range of values collected at the inlet (from -148 to 220 mV), and following the
treatment (from -112 to 614 mV). DO measurements also were highly variable. Several attempts were
made to verify and improve the readings, including replacing the field meter and probe and working
closely with the operator to ensure the meter was used properly. Due to the spread in these
measurements, no discernable trend could be identified from these data.
The results for alkalinity, fluoride, sulfate, silica, and nitrate remained fairly constant throughout the
treatment train, appearing unaffected by the media and prechlorination. Orthophosphate (as P) was less
than the detection limit for all samples and total phosphorous averaged 17.3 (ig/L in source water and less
than the detection limit for all samples following the effluent of the treatment system. Total hardness
ranged from 90.9 to 117 mg/L (as CaCO3), consisting of approximately 57% Ca hardness and 43% Mg
hardness, and remained constant across the treatment train.
4.5.2 Backwash Wastewater Sampling. The analytical results of the backwash wastewater
samples are summarized in Table 4-9. As described in Section 3.3.3, the analytes for backwash
wastewater samples were modified on December 16, 2005, to include total As, Fe, and Mn, and TSS. The
results presented in Table 4-9 reflect these changes.
Raw water was used for backwash. Soluble arsenic and iron concentrations in the backwash water from
both vessels were significantly lower than those in raw water, averaging 10.1 and 98.7 (ig/L, respectively
(compared to 20.6 and 220 (ig/L, respectively in raw water). The lower soluble arsenic and iron
concentrations indicated removal of some of these ions during backwash. pH values of the backwash
wastewater were similar to those of raw water. The results of all parameters measured from Vessel A
were consistent with those from Vessel B.
TDS concentrations ranged from 100 to 430 mg/L and averaged 196 mg/L; TSS concentrations ranged
from 12 to 130 mg/L and averaged 85 mg/L. Concentrations of total As, Fe, and Mn ranged from 49.7 to
468 (ig/L (averaged 248.3 (ig/L), from 2.6 to 29.1 mg/L (averaged 16.0 mg/L), and from 7.2 to 128 (ig/L
(averaged 38.5 (ig/L), respectively. On average, approximately 7.5% of As, 0.6% of Fe, and 13.2% of
Mn existed in the soluble form in the backwash wastewater. Using the above average concentrations,
approximately 0.02 Ib of As, 1.3 Ib of Fe, and 0.003 Ib of Mn were discharged, mostly as backwash
solids, during each backwash cycle.
The backwash solids were collected and analyzed in May and June 2005 (Section 3.3.4). The analytical
results are summarized in Table 4-10. The averaged As, Fe, and Mn concentrations in backwash solids
were 2.3, 400.8, and 1.1 mg/g, respectively. Based on an average TSS concentration of 85 mg/L in
backwash wastewater, approximately 7 Ib of solids were produced from backwashing both vessels.
Assuming the above average concentrations in backwash solids were representative, approximately 0.016
Ib of As, 2.8 Ib of Fe, and 0.008 Ib of Mn would be discharged from both vessels as backwash solids
during each backwash. Comparing these results with those calculated based on the analytical results of
backwash wastewater, the arsenic amounts were comparable and iron and manganese amounts were
within a factor of 2.7. This degree of consistency is promising, considering that the results were
generated by two completely independent sampling and analysis systems.
38
-------
Table 4-9. Backwash Water Sampling Results
Sampling Event
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
Date
11/17/04
01/12A)5
02/22 A)5
03/23 A)5
04/20/05
05/12/05
05/31/05
06/21/05
07/05/05
07/20/05
08/03/05
08/16/05
08/29/05
09/09/05
09/23/05
10/11/05
10/25/05
12/16/05(d)
01/24/06
02/23/06
03/10/06
04/21/06
05/23/06
06/06/06
07/10/06
08/09/06
09/05/06
Vessel A
X
S.U.
7.3
7.9
7.8
7.9
7.5
7.3
7.2
7.6
7.7
7.7
7.7
3-
^
|
NTU
600
68
16
17
25
250
18
120
23(=)
53(a)
522(a)
8
mg/L
234
100
190
220
212
210
154
178
210
202
212
%
mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
t.
•¥
HO/I-
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
i\s (Soluble)
ug/L
5.4
3.0
2.8
4.1
5.2
5.2
7.8
10.5
11.6
7.2
10.4
<\s (Particulate)
HO/I-
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
t.
V
ug/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
°>
.Q
3
O
SO.
V
ffl/L
<25
<25
<25
<25
<25
<25
<25
<25
<25
37
57
1
C
^
ug/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
Kin (Soluble)
ug/L
1.6
5.1
2.6
0.8
1.6
0.3
4.5
5.7
3.1
2.5
4.0
NA(b)
7.4
7.5
7.7
8.0
8.0
7.9
7.7
7.9
7.7
7.8
7.9
7.8
7.8
7.7
7.6
32
9
23
29
2
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
174
196
236
178
178
198
186
180(a)
222
174
188
190
162
196
190
NS
NS
NS
NS
NS
76
130
98
48
90
104
128
90
89
68
NS
NS
NS
NS
NS
178
356
369
66.1
111
323
298
257
250
193
6.0
13.7
9.0
9.3
7.9
9.0
7.9
25.9
13.1
21.3
17.6
12.3
12.3
15.9
17.8
NS
NS
NS
NS
NS
169
348
343
53.1
90.1
305
286
245
235
175
NS
NS
NS
NS
NS
20,067
24,378
21,371
3,787
10,755
20,242
19,587
29,050
5,142
10,014
27
<25
<25
<25
<25
113.76
29
781
35
101
29.4
142
25.5
<25
<25
NS
NS
NS
NS
NS
39.54
128
65.8
14.8
25.8
21.8
31.3
45.4
29.0
16.8
1.8
3.1
1.8
2.1
2.2
14.5
0.3
9.1
2.7
3.3
2.1
2.6
4.8
4.5
3.2
Vessel B
X
S.U.
7.2
7.9
7.7
7.8
7.6
7.5
7.4
7.8
7.8
7.8
7.8
7.7
7.6
7.8
7.8
7.9
NA(C)
7.9
7.8
7.8
7.7
7.8
7.9
7.8
7.8
7.7
7.7
£
•o
1
NTU
520
39
12
14
210
180
14
82
17"
17(=)
159(a)
14
26
7
20
18
NA(C)
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
CO
Q
mg/L
222
430
184
216
204
194
160
240
200
218
188
202
166
210
184
176
NA(C)
186
194
174(a)
172
176
194
172
210
190
156
g
mg/L
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
110
92
66
12
102
88
100
70
39
90
TO
I
at
-------
Table 4-10. Backwash Solids Sampling Results
Date: Location
05/1 2/05: Vessel A
Average
05/12/05: VesselB
Average
05/31/05: Vessel A
Average
05/31/05: Vessel B
Average
06/21/05: Vessel A
Average
06/21/05: Vessel B
Average
Mg
mg/g
2.71
2.66
2.77
2.71
2.53
2.50
2.48
2.50
22.1
17.8
20.0
21.0
23.3
22.2
17.3
17.1
18.8
17.7
15.0
16.3
15.6
Al
mg/g
0.17
0.18
0.17
0.17
0.19
0.19
0.18
0.19
0.39
0.37
0.38
0.82
0.84
0.83
0.53
0.38
0.46
0.46
2.33
2.34
2.33
Si
mg/g
0.17
0.06
0.10
0.11
0.06
0.05
0.08
0.06
0.60
2.76
1.68
1.66
6.05
3.86
2.61
3.74
5.69
4.01
3.58
2.51
3.04
P
mg/g
4.30
4.39
4.62
4.44
2.91
2.93
2.76
2.87
6.50
6.96
6.73
4.72
4.79
4.75
6.17
5.57
5.87
5.87
3.77
3.89
3.83
Ca
mg/g
8.63
8.88
9.73
9.08
6.07
6.33
6.42
6.27
72.3
73.6
73.0
86.7
86.4
86.5
72.1
72.6
73.2
72.6
63.6
63.4
63.5
Fe
mg/g
610
606
606
607
634
619
624
625
322
313
318
224
231
227
322
313
292
309
308
330
319
Mn
mg/g
2.11
2.09
2.07
2.09
2.07
2.03
2.06
2.06
0.81
0.62
0.71
0.51
0.52
0.51
0.45
0.45
0.46
0.45
0.69
0.68
0.69
Ni
Mg/g
108
100
101
103
114
113
110
113
38.0
87.0
62.5
126
122
124
120
113
131
121
161
141
151
Cu
Mg/g
22
20
21
21
18
18
18
18
63
68
65
65
72
69
139
81
116
112
61
81
71
Zn
Mg/g
401
406
408
405
339
339
344
341
819
778
799
353
359
356
618
593
647
619
530
536
533
As
mg/g
2.55
2.61
2.69
2.61
1.78
1.82
1.92
1.84
3.30
3.25
3.27
2.06
2.11
2.09
2.46
2.47
2.62
2.51
1.66
1.68
1.67
Cd
Mg/g
<0.15
<0.15
<0.15
<0.15
<0.15
O.15
O.15
<0.15
<1.0
1
1
<2.0
<2.0
<2.0
<2.0
<2.0
3
3
4
4
4
Pb
Mg/g
2.92
2.94
3.15
3.00
1.91
2.01
3.37
2.43
23.6
21.4
22.5
7.63
6.81
7.22
21.4
19.0
21.0
20.5
23.4
22.4
22.9
Table 4-11. Media Sampling Results
Sam pie ID
SV-Vessel A-Pre BW-Surface-A
SV-Vessel A-Pre BW-Surface-B
SV-Vessel A-Pre BW-Surface-C
SV-Vessel A-Post BW-Surface-A
SV-Vessel A-Post BW-Surface-B
SV-Vessel A-Post BW-Surface-C
SV-Vessel B-Pre BW-Surface-A
SV-Vessel B-Pre BW-Surface-B
SV-Vessel B-Pre BW-Surface-C
SV-Vessel B-Post BW-Surface-A
SV-Vessel B-Post BW-Surface-B
SV-Vessel B-Post BW-Surface-C
Mg
ug/g
1,059
1,060
1,111
1,295
1,332
1,318
1,706
1,710
1,721
1,598
1,606
1,576
Al
ug/g
164
167
174
152
155
154
202
203
206
185
159
168
Si
ug/g
218
153
129
5,393
4,763
5,943
232
582
1,026
9,321
3,981
6,016
P
ug/g
1,403
1,375
1,549
1,158
1,253
1,279
1,805
1,803
1,786
1,602
912
1,197
Ca
ug/g
2,267
2,231
2,284
2,424
2,449
2,406
2,746
2,695
2,756
2,794
2,647
2,659
Fe
ug/g
617,448
612,131
614,355
485,966
519,752
513,650
617,138
592,282
598,376
539,008
450,598
500,171
Mn
ug/g
1,636
1,632
1,626
1,270
1,322
1,315
1,652
1,595
1,626
1,417
1,123
1,206
Ni
ug/g
145
142
139
122
121
114
120
125
126
111
103
106
Cu
ug/g
11.0
12.4
11.5
12.9
13.0
13.3
16.4
16.1
16.0
16.7
16.3
16.3
Zn
ug/g
151
144
152
292
290
291
406
385
385
462
473
470
As
ug/g
850
882
916
209
267
288
1,816
1,746
1,657
843
228
405
Cd
ug/g
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
<0.25
Pb
ug/g
0.57
0.65
0.60
0.64
0.66
0.62
0.85
0.87
0.84
0.91
0.86
0.87
-------
4.5.3 Adsorptive Media Sampling. Table 4-11 presents the analytical results of media samples
collected on August 4, 2005, from the top of each media bed both before and after backwash. The spent
media collected from both Vessels A and B after backwash contained mostly iron, averaging 502 mg/g
(as Fe) or 800 mg/g (as FeOOH) of the spent media. The FeOOH content of the spent media was lower
than the 90.1% (by weight) specified by the Bayer AG for the virgin media (Table 4-2). Challenges
associated with sampling (i.e., if representative samples were taken) and sample digestion (i.e., if samples
were completely digested) were believed to have contributed, in part, to the discrepancies observed.
Average arsenic loadings on the spent media samples collected after backwash were 0.26 and 0.49 mg/g
for Vessels A and B, respectively. As shown in Table 4-11, backwash removed approximately 17.6% of
iron and 71.5% of arsenic from both Vessels A and B. The average mass ratio of the iron and arsenic
removed was 114, which is similar to that (i.e., 171) of the backwash solids as shown in Table 4-9. As
such, the iron removed during backwash was mostly the oxidized iron formed following prechlorination
and accumulating in the media beds.
4.5.4 Distribution System Water Sampling. The results of the 20 distribution system sampling
events (including four baseline sampling events) are summarized in Table 4-12. The most apparent
change in the distribution water quality since the system began operation was the decrease in arsenic
concentrations once the treatment system became operational. Baseline arsenic concentrations averaged
19.2, 19.3, and 18.6 (ig/L forthe first draw samples at the DS1, DS2, and DS3 sampling locations,
respectively. After the performance evaluation began, arsenic concentrations at DS1, DS2, and DS3
averaged 7.7, 7.7, and 9.9 (ig/L, respectively, prior to the switch to prechlorination on November 9, 2004
and 3.9, 3.0, and 3.9 (ig/L after the switch. The arsenic results from the distribution sampling mirrored
the results from the treatment system sampling in that the As concentrations dropped once the system was
put into service, rose gradually during the first four months of operation as As(III) began to break
through, and then went down again once the switch to prechlorination was made.
Lead concentrations ranged from less than the detection limit of 0.1 to 2 |o,g/L, with the exception of one
sample collected at DS3 on January 10, 2006, which had a lead concentration of 10.6 |o,g/L. Copper
concentrations ranged from 10.5 to 774 (ig/L. None of the lead and copper samples exceeded the
respective action levels for these two metals (15 (ig/L and 1,300 (ig/L for Pb and Cu, respectively). No
trend/discernable difference could be drawn or was observed between the samples collected during
baseline sampling and after system startup.
pH values collected following treatement ranged from 6.8 to 7.8, with the exception of the values
measured on December 8, 2004 and March 3, 2005, which were higher at 8.2 to 8.9. In general, the pH
values collected following treatment were consistent with those collected from baseline sampling, ranging
from 7.2 to 7.8. Similarly, no major difference was observed in alkalinity, with concentrations ranging
from 154 to 182 mg/L (as CaCO3). Total iron concentrations were generally less than the method
reporting limit of 25 (ig/L for all baseline samples except for two collected on December 17, 2003, and
February 11, 2004. Since the system became operational, iron concentrations in the distribution system
samples were consistently less than the detection limit with only two exceptions at DS3. Total Mn
concentrations in the distribution system samples were typically low, ranging from 0.5 to 22.9 (ig/L, with
the majority at less than 5 (ig/L.
4.6 System Cost
The cost-effectiveness of the system is evaluated based on the capital cost per gpm (or gpd) of the design
capacity and the O&M cost per 1,000 gal of water treated. The capital costs included equipment,
engineering, and installation costs and O&M costs included media replacement and disposal, chemical
supply, electrical power use, and labor.
41
-------
Table 4-12. 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
14
15
16
Sample Type
Flushed 11st Draw
Sampling Date
Date
12/17/03
01/14/04
02/11/04
03/19/04
07/20/04
08/31/04
09/23/04
10/26/04
11/16/04
12/8/04"'
01/05/05
02/02/05
3/3/05'"
4/12/05w
05/10/05
06/22/05
07/19/05
08/16/05
9/20/05"1
10/12/05
12/14/05
01/10/06
DS1
LCR
1st Draw
Stagnation Time
hr
8.3
8.5
7.8
7.1
10.3
8.3
8.2
7.5
9.0
8.5
^
S.U.
7.2
7.8
7.4
7.2
6.8
7.6
7.1
7.7
7.6
8.9
,
mg/L
166
159
174
156
156
167
162
164
164
162
Mg'L
18.5
17.5
21.2
19.5
3.0
7.7
8.4
11.9
12.3
1.5
0)
Mg'L
87.5
<25
107.0
<25
<25
<25
<25
<25
<25
<25
c
^
Mg'L
0.8
0.5
1.1
0.7
1.3
4.1
5.5
4.6
22. 9/
20.6
2.2
if
Mg'L
1.3
0.6
0.9
0.6
0.9
1.0
1.7
0.9
0.8
0.5
3
Mg'L
255.0
429.0
180.0
248.0
360.0
384.0
462.0
407.0
174.0
231.0
'0, (ortho)
Mg'L
0.5
0.4
0.4
0.4
2.2
0.5
1.6
1.9
1.7
0.5
Homeowner not available
8.8
8.5
8.5
8.3
8.8
8.8
7.2
7.3
7.7
7.8
7.5
7.2
171
169
178
176
163
167
0.6
1.4
1.0
1.4
3.1
1.5
<25
<25
<25
<25
<25
<25
Homeowner not ava
8.5
8.5
8.5
9.0
7.5
7.5
7.8
7.7
167
172
180
172
2.0
3.2
15.7
2.6
<25
<25
<25
<25
0.9
0.3
0.1
<0.1
0.5
0.9
0.6
0.2
0.2
0.5
0.4
0.3
581.5
281.0
373.0
481.2
114.1
123.1
4.6
1.0
1.2
1.9
1.4
1.6
lable
0.3
0.7
0.5
0.2
1.4
<0.1
2.0
0.9
222.0
30.3
432.1
327.0
1.3
0.6
0.2
0.6
DS2
LCR
1st Draw
Stagnation Time
hr
NS
8.5
10.0
7.5
10.8
^
S.U.
NS
7.6
7.3
7.2
6.9
,
mg/L
NS
163
182
160
156
Mg'L
NS
21.5
18.1
18.4
3.5
0)
Mg'L
NS
<25
47.0
<25
<25
c
^
Mg'L
NS
1.0
3.9
1.5
1.1
Mg'L
NS
<0.1
0.1
0.2
0.3
?,
Mg'L
NS
210.0
207.0
120.0
171.0
"0"
O
Mg'L
NS
1.0
0.5
0.5
0.5
Homeowner not available
9.5
9.0
7.5
8.0
7.0
11.0
9.0
9.3
7.3
8.3
10.0
16.0
8.5
8.0
7.3
7.6
7.7
8.4
7.7
7.3
8.2
7.7
7.6
7.5
7.3
7.4
7.5
7.6
162
164
164
162
165
166
174
176
176
167
172
154
176
176
8.8
10.7
13.2
3.6
1.5
0.9
1.4
1.0
1.0
2.2
1.3
1.9
2.1
4.0
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
3.0
2.6
2.7
2.3
1.8
1.0
0.5
0.5
<0.1
0.6
0.6
1.3
0.5
0.5
0.6
0.3
0.2
0.1
0.2
0.2
0.1
0.2
0.1
0.2
0.1
0.4
0.4
<0.1
65.0
146.0
126.0
83.6
280.0
159.3
267.0
253.0
242.3
101.0
234.0
115.6
111.7
10.5
2.2
1.8
1.8
0.6
0.4
1.2
1.1
1.3
1.9
1.4
1.6
1.4
1.5
0.06
Homeowner not available
9.5
7.8
172
4.5
<25
0.2
0.3
213.0
0.4
DS3
LCR
1st Draw
Stagnation Time
hr
6.0
6.0
6.0
6.0
6.0
6.0
8.3
9.0
9.0
7.0
8.0
8.0
^
S.U.
7.6
7.6
7.2
7.7
6.8
7.5
7.4
7.7
7.7
8.2
7.4
7.5
,
mg/L
164
159
161
168
160
155
162
164
164
162
178
180
Mg'L
16.0
19.5
19.5
19.2
4.6
7.0
16.7
11.2
12.4
4.3
1.4
1.1
0)
Mg'L
<25
<25
68.9
<25
<25
<25
26.9
<25
<25
26.0
<25
<25
E
^
Mg'L
0.7
16.6
9.9
1.3
1.2
3.6
8.7
2.4
11.8
1.9
1.4
0.9
Mg'L
0.5
0.4
0.5
0.4
1.1
0.8
1.6
0.5
0.3
0.3
0.3
0.4
?,
MgiL
287.6
299.0
279.0
322.0
297.0
279.0
494.0
200.0
53.0
416.0
466.0
96.8
"0"
O
Mg'L
0.5
0.6
0.4
0.4
0.5
0.6
2.3
1.9
1.6
0.6
0.6
1.0
Homeowner not ava lable
8.0
7.0
8.5
9.5
8.0
8.5
8.0
9.2
8.5
7.7
7.8
7.6
7.3
7.3
7.5
7.5
7.8
7.8
176
176
163
172
154
172
176
176
172
1.2
1.0
2.5
1.6
2.0
2.0
3.0
15.5
3.4
<25
<25
<25
<25
<25
<25
<25
<25
<25
0.4
<0.1
0.6
0.4
0.7
0.5
1.3
0.3
0.1
0.4
0.3
0.3
1.3
0.5
0.4
0.4
0.8
10.6
774.0/
541.0
438.0
160.8
293.2
151.3
148.0
57.7
304.3
470.0
1.2
1.8
1.3
1.4
1.2
1.4
0.06
0.2
0.4
to
(a) DS2 sampled on December 7, 2004.
(b) DS2 sampled on March 4, 2005.
(c) DS1 sampled on April 13, 2005.
(d) DS2 sampled on September 21, 2005.
(/) indicates re-run data with original result/re-run result.
NS = not sampled; NA = data not available
Lead action level =15 ug/L; copper action level =1.3 mg/L
BL = baseline sampling
-------
4.6.1 Capital Cost. The capital investment cost for equipment, site engineering, and installation
was $211,000 (see Table 4-13). The equipment cost was $129,500 (or 62% of the total capital
investment), which included costs for two FRP pressure vessels, 160 ft3 of SORB 33™ media ($150/ft3 or
$5.34/lb), piping and valves, instrumentation and controls, field services (including operator training,
technical support, and system shakedown), and miscellaneous materials and supplies.
The engineering cost included that for preparation of the system layout and footprint, treatment system
process flow diagram, and mechanical drawings of the treatment system equipment submitted as part of
the permit application submittal (Section 4.3.1). The final set of engineering plans were prepared by
Stearns and Wheler and included detailed construction drawings of the new treatment building, a floor
plan, and tie-ins and connections for the treatment system. The engineering cost was $36,700, which was
17% of the total capital investment.
Table 4-13. Capital Investment for Prospect Bay Treatment System
Description
APU Skid-Mounted System
E33 Media
Misc. Equipment and Materials
Vendor Labor
Vendor Travel
Equipment Total
Subcontractor
Vendor Labor
Vendor Travel
Engineering Total
Subcontractor
Vendor Labor
Vendor Travel
Installation Total
Total Capital Investment
Cost
$72,200
$24,000
$19,800
$10,000
$3,500
$129,500
28,940
$6,680
$1,080
$36,700
$35,800
$5,600
$3,400
$44,800
$211,000
% of Capital
Investment Cost
—
—
—
—
—
62%
—
—
—
17%
—
—
—
21%
100%
The installation cost includes the labor, equipment, and materials to unload and install the skid-mounted
unit, perform the piping tie-ins and electrical work, and load and backwash the media. The installation
was performed by the vendor and the installation subcontractor, Stearns and Wheler. The installation cost
was $44,800, or 21% of the total capital investment.
The QAC Department of Public Works subcontracted Stearns and Wheler to construct the addition to the
treatment building. Total construction cost for the addition was $92,630, including about $18,000 for the
building design and $75,000 for construction. The 16-ft * 23-ft treatment area was an addition to the
original 8-ft * 16-ft well house. The building was constructed using concrete block and brick siding.
Construction took approximately one month to complete including placement and setting of the vessels
within the building, which were put into place before the roof was installed.
The total capital cost of $211,000 was normalized to $703/gpm ($0.49/gpd) of design capacity using the
system's rated capacity of 300 gpm (or 432,000 gpd). The capital cost also was converted to an
annualized cost of $19,916/year by multiplying by a capital recovery factor (CRF) of 0.09439 based on a
7% interest rate and a 20-year return period (Chen et al., 2004). Assuming that the system operated 24
hr/day, 7 day/wk at the design flowrate of 300 gpm to produce 157,680,000 gal/yr, the unit capital cost
43
-------
would be $0.13/1,000 gal. During the performance evaluation study, the system operated only 6.2 hr/day
at 207 gpm on average (see Table 4-4). Based on this reduced use rate, the system would produce only
28,106,000 gal of water in one year (assuming 365 days per year) and the unit capital cost would increase
to $0.70/1,000 gal.
4.6.2 Operation and Maintenance Cost. The O&M costs include only incremental costs
associated with the APU-300 treatment system, such as media replacement, chemical supply, electricity,
replacement parts, and labor. These costs are summarized in Table 4-14.
Table 4-14. O&M Cost for Prospect Bay Treatment System
Cost Category
Volume Processed (Kgal)
Value
65,023
Assumptions
From 06/30/04 through 04/02/07
Media Replacement and Disposal
Media Cost ($/ft3)
Total Media Volume (ft3)
Media Replacement Cost ($)
Labor Cost ($)
Media Disposal Fee ($)
Subtotal ($)
Media Replacement/Disposal Cost
($/l,000 gal)
$155.80
160
$24,928
$2,120
$680
$27,728
See Figure 4-18
Purchased price
Both vessels
Purchased price
Vendor quote
Vendor quote
Vendor quote
Based upon media run length at 10-
ug/L arsenic breakthrough
Chemical Usage
Chemical Cost ($)
$0.00
No additional chemical usage required
Electricity
Electric Utility Charge ($/kWh)
Incremental Monthly Usage (kWh)
Estimated Incremental Electricity cost ($)
Incremental cost ($/l,000 gal)
$0.10
1200
$720
$0.05
Including delivery and supply charges
Average monthly incremental usage for
August and September 2004
From July to December 2004
—
Replacement Parts
Signet Flow Meter Sensors ($)
Replacement Paddle Wheel and Pin for
Flow Meter Sensor ($)
Automatic Butterfly Valve Assembly
Total Cost of Parts Replaced during
Performance Evaluation Study
Incremental Cost ($/l,000 gal)
$654
$41
$950
$1,645
$0.03
Three replacement sensors; not
including installation
Not including installation
Not including installation
-
—
Labor
Average Weekly Labor (hr)
Labor Cost ($/l,000 gal)
Total O&M Cost/1,000 gallons
1.75
$0.23
See Figure 4-18
15 mm/day, 7 day/week
Average Labor rate = $21.75/hr
Based upon media run length at 10-
ug/L arsenic breakthrough
Although media replacement and disposal did not take place during the performance evaluation study,
virgin Bayoxide E33 media were purchased at a unit cost of $155.80/ft3 for a total of $24,928 and stored
onsite to prepare for timely media replacement. The vendor estimated $27,728 to change out both
vessels, which included the purchased price of the media, freight, labor, travel expenses, and media
profiling and disposal fee. This cost was used to estimate the media replacement cost per 1,000 gal of
44
-------
water treated as a function of the projected media run length to the 10 (ig/L arsenic breakthrough (Figure
4-18).
The chemical cost associated with the operation of the treatment system included chlorine addition prior
to the adsorption vessels and injection of polyphosphate after the APU-300 system. Both of these
treatment steps were in use at the site prior to installation of the APU-300 treatment system, which did not
have a significant effect on the chlorine gas usage based on the data collected during the performance
evaluation study. Therefore, the incremental chemical cost due to the APU-300 system was negligible.
The incremental electrical power consumption was reviewed. Electrical usage during the months of
August and September 2003 were compared to usage for the same period in 2004 following installation of
the APU system. Additionally, the 2003 usage estimate was determined by adding the usage at both
Wells No. 1 and No. 2 because operation of these wells was alternated during this time. The estimated
average monthly usage for Wells No. 1 and No. 2 for August and September 2003 was about 4,160 kWh.
For August and September 2004, the average monthly usage for Well No. 1 was 5,360 kWh. Once the
APU-300 treatment system was installed at Well House No. 1, Well No. 2 was only rarely operated, if at
all. The incremental electrical usage was thus determined to be approximately 1,200 kWh per month
during the summer months when peak water demand was expected. At a rate of about $0.10/kWh
(including delivery and supply charges), an additional utility cost of approximately $120 per month to
operate the APU-300 system was calculated. Over the performance evaluation period, the incremental
utility cost to operate the treatment system was $0.05/1,000 gal. Although there are few electrical parts
on the APU-300 system that would require additional electrical consumption, the increased usage might
have been due to increased total dynamic head on the well pump and electrical consumption within the
treatment building addition (i.e., lights, heating, etc.).
During the performance evaluation study, several parts were not functioning properly and had to be
repaired and/or replaced, including three flow meter sensors, an automatic butterfly valve, and parts for
the flow meter sensors. The cost for the replacement parts was $1,645, not including installation, which
resulted in an incremental cost of $0.03/1,000 gallons of water treated.
The routine, non-demonstration-related labor activities consumed only about 15 min/day, as noted in
Section 4.4.5. Based on this time requirement and a labor rate of $21.75/hr, the labor cost was
$0.23/1,000 gal of water treated.
45
-------
$4.00 -,
$3.50 -
$3.00 -
$2.50 -
ro
o
"- $2.00 -
o
O
$1.50 -
$1.00 -
$0.50 -
$0.00
O&M Cost (including Media
Replacement)
— — Media Replacement Cost Only _
\
0 10,000 20,000 30,000 40,000 50,000 60,000 70,000 80,000 90,000 100,000 110,000 120,000 130,000
Media Working Capacity (BV)
Figure 4-18. Media Replacement and Operation and Maintenance Costs
46
-------
5.0 REFERENCES
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.
Chen, A.S.C., L. Wang, J.L. Oxenham, and W.E. Condit. 2004. Capital Costs of Arsenic Removal
Technologies: U.S. EPA Arsenic Removal Technology Demonstration Program Round 1.
EPA/600/R-04/201. U.S. Environmental Protection Agency, National Risk Management
Research Laboratory, Cincinnati, OH.
Chen, A.S.C., W.E. Condit, L. Wang, and A. Wang. 2008a. Draft Final Performance Evaluation Report:
Arsenic Removal from Drinking Water by Adsorptive Media. U. S. EPA Demonstration Project at
Brown City, MI. Prepared under Contract No. 68-C-00-185, Task Order No. 0019 for
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
Chen, A.S.C., C.T. Coonfare, L. Wang, and A. Wang. 2008b. Draft Final Performance Evaluation
Report: Arsenic Removal from Drinking Water by Adsorptive Media. U.S. EPA Demonstration
Project at Desert Sands MDWCA, NM, Prepared under Contract No. 68-C-00-185, Task Order
No. 0019 for Environmental Protection Agency, National Risk Management Research
Laboratory, Cincinnati, OH.
Cumming,L.J., A.S.C. Chen, and L. Wang 2008. Draft Final Performance Evaluation Report: Arsenic
Removal from Drinking Water by Adsorptive Media. U.S. EPA Demonstration Project at
Rollinsford, NH. Prepared under Contract No. 68-C-00-185, Task Order No. 0037 for
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
Edwards, M., S. Patel, L. McNeill, H. Chen, M. Frey, A.D. Eaton, R.C. Antweiler, and H.E. Taylor. 1998.
"Considerations in As Analysis and Speciation." J. AWWA, 90(3): 103-113.
EPA. 2001. "National Primary Drinking Water Regulations: Arsenic and Clarifications to Compliance
and New Source Contaminants Monitoring." Federal Register, 40 CFR Parts 9, 141, and 142.
EPA. 2002. Lead and Copper Monitoring and Reporting Guidance for Public Water Systems.
EPA/816/R-02/009. U.S. Environmental Protection Agency, Office of Water, Washington, D.C.
EPA. 2003. "Minor Clarification of the National Primary Drinking Water Regulation for Arsenic."
Federal Register, 40 CFR Part 141.
Meng, X.G., S. Band, and G.P. Korfiatis. 2000. "Effects of Silicate, Sulfate, and Carbonate on Arsenic
Removal by Ferric Chloride." Water Research, 34(4): 1255-1261.
Meng, X.G., G.P. Korfiatis, S.B. Band, and K.W. Band, 2002. "Combined Effects of Anions on Arsenic
Removal by Iron Hydroxides." Toxicology Letters, 133(1): 103-111.
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.
47
-------
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
48
-------
APPENDIX A
OPERATIONAL DATA
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet
Week
No.
1
2
3
4
5
6
7
8
9
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
6/28/2004
6/29/2004
6/30/2004
7/1/2004
7/2/2004
7/3/2004
7/4/2004
7/5/2004
7/6/2004
7/7/2004
7/8/2004
7/9/2004
7/10/2004
7/11/2004
7/13/2004
7/14/2004
7/15/2004
7/16/2004
7/17/2004
7/18/2004
7/20/2004
7/21/2004
7/22/2004
7/23/2004
7/24/2004
7/25/2004
7/26/2004
7/27/2004
7/28/2004
7/29/2004
7/30/2004
7/31/2004
8/1/2004
8/2/2004
8/3/2004
8/4/2004
8/5/2004
8/6/2004
8/7/2004
8/9/2004
8/10/2004
8/11/2004
8/12/2004
8/13/2004
8/14/2004
8/16/2004
8/17/2004
8/18/2004
8/19/2004
8/20/2004
8/21/2004
8/23/2004
8/24/2004
8/25/2004
8/26/2004
8/27/2004
8/28/2004
8/29/2004
Time
NM
NM
08:35
11:10
09:00
17:30
NM
NM
14:30
08:30
09:00
08:00
17:00
16:37
08:30
08:35
16:00
14:25
NM
NM
08:20
09:00
11:00
10:30
17:00
16:00
14:00
08:40
08:45
09:45
08:50
16:20
17:00
09:00
08:40
08:40
08:45
08:35
19:00
11:30
10:15
08:05
09:00
08:30
16:00
08:30
08:33
09:30
06:30
10:50
16:00
06:40
09:00
09:04
08:50
11:30
16:50
16:43
Well House #1 Reading
Opt Hours
Well!
hr
NA
NA
NA
11.3
6.2
19.8
NA
NA
35.1
13.6
9.1
6.0
16.6
12.4
1.1
8.8
12.3
3.4
NA
NA
8.8
8.4
8.0
8.3
8.7
11.5
0.2
9.7
2.0
9.3
2.1
9.7
10.2
4.1
5.9
4.2
7.1
9.5
10.1
11.2
10.9
1.4
10.2
2.3
8.8
0.3
9.9
5.6
5.3
10.4
11.2
9.2
6.3
4.5
10.4
11.0
8.8
4.8
Daily Flow
Totalizer
gal
NA
NA
NA
168,000
92,000
295,000
NA
NA
NA
201,000
135,000
87,000
246,000
181,000
17,000
129,000
183,000
48,000
NA
NA
130,000
120,000
121,000
120,000
145,000
152,000
2,000
143,000
30,000
135,000
31,000
150,000
139,000
61,000
85,000
62,000
103,000
139,000
148,000
164,000
159,000
20,000
149,000
33,000
128,000
3,000
144,000
80,000
78,000
151,000
163,000
134,000
93,000
64,000
151,000
160,000
127,000
69,000
Avg
Flowrate
gpm
NA
NA
NA
248
247
248
NA
NA
NA
246
247
242
247
243
258
244
248
235
NA
NA
246
238
252
241
278
220
167
246
250
242
246
258
227
248
240
246
242
244
244
244
243
238
243
239
242
167
242
238
245
242
243
243
246
237
242
242
241
240
APU
Electric
Meter
KWH
NM
NM
356.97
359.55
360.98
365.51
NM
NM
373.56
376.67
37876
380.13
388.94
386.77
390.04
392.06
394.89
395.67
NM
NM
402.21
405.21
406.02
407.92
410.05
412.59
41265
41489
41539
41754
41803
42039
42058
42354
42487
42586
42748
42967
43199
43456
43736
43769
44005
44057
44260
44469
44696
44824
44947
45187
45442
45662
45809
45912
46151
46403
46603
46714
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
NM
NM
110.0
115.4
116.4
116.9
NM
NM
105.5
117.6
119.1
115.2
114.5
121.2
115.0
115.0
110.9
110.3
NM
NM
111.0
114.0
112.0
113.5
117.5
116.9
115.0
115.0
115.0
115.0
110.4
112.7
113.5
110.8
115.0
112.3
113.4
114.6
112.2
115.6
115.6
115.8
115.7
114.4
115.0
115.0
114.0
115.0
116.4
115.3
114.0
116.2
113.3
117.4
116.3
114.8
110.5
112.5
Daily Flow
Totalizer
A
gal
NA
NA
NA
74,596
41,182
131,384
NA
NA
233,007
89,596
60,836
39,484
111,180
82,160
7,189
58,164
83,084
19,785
NA
NA
58,346
86,744
22,936
54,659
61,575
73,723
816
65,100
13,538
61,676
14,427
68,032
63,423
27,257
39,161
28,372
46,481
63,769
67,176
74,820
72,213
9,410
68,284
16,716
56,623
2,031
65,975
37,117
34,980
69,060
74,300
59,331
42,352
29,426
69,319
72,930
58,423
31,787
Cum.
Flow
Totalizer
A
Kgal
NA
NA
NA
75
116
247
NA
NA
480
570
631
670
781
863
959
1,017
1,100
1,120
NA
NA
1,311
1,398
1,421
1,475
1,537
1,610
1,611
1,676
1,690
1,752
1,766
1,834
1,898
1,925
1,964
1,992
2,039
2,103
2,170
2,253
2,325
2,334
2,402
2,419
2,476
2,536
2,602
2,639
2,674
2,743
2,817
2,881
2,923
2,953
3,022
3,095
3,154
3,185
Bed
Volume
Totalizer
A
BV
NA
NA
NA
125
193
413
NA
NA
802
952
1,054
1,120
1,306
1,443
1,602
1,699
1,838
1,871
NA
NA
2,190
2,335
2,374
2,465
2,568
2,691
2,693
2,801
2,824
2,927
2,951
3,065
3,171
3,216
3,282
3,329
3,407
3,513
3,626
3,764
3,885
3,900
4,015
4,042
4,137
4,238
4,348
4,410
4,468
4,584
4,708
4,814
4,885
4,934
5,050
5,172
5,270
5,323
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
NM
NM
115.0
119.4
119.8
112.8
NM
NM
115.4
118.0
112.3
118.4
118.9
112.2
117.0
118.0
114.1
115.1
NM
NM
115.0
121.0
119.3
120.1
118.0
115.2
118.2
117.0
117.4
117.0
112.8
110.1
114.4
116.7
114.0
113.7
114.6
116.3
116.5
117.8
117.8
117.4
117.3
113.7
113.0
117.0
118.5
112.0
116.2
117.8
115.0
116.1
112.5
116.3
119.4
114.7
111.1
114.4
Daily Flow
Totalizer
B
gal
NA
NA
NA
78,002
42,825
136,697
NA
NA
242,208
93,006
63,025
40,866
115,029
85,111
7,743
60,356
86,176
22,136
NA
NA
60,629
90,042
23,801
56,781
65,885
74,606
809
67,746
14,109
64,301
14,811
71,159
66,111
29,114
40,056
29,620
48,794
66,395
70,276
78,224
75,495
9,855
71,321
15,314
61,165
2,125
68,720
38,753
36,539
72,203
39,677
62,063
49,976
25,030
72,483
76,212
60,951
33,072
Cum. Flow
Totalizer
B
Kgal
NA
NA
NA
78
121
258
NA
NA
500
593
656
697
812
897
995
1,056
1,142
1,164
NA
NA
1,361
1,451
1,475
1,532
1,598
1,672
1,673
1,741
1,755
1,819
1,834
1,905
1,971
2,000
2,040
2,070
2,119
2,185
2,256
2,342
2,418
2,427
2,499
2,514
2,575
2,638
2,707
2,746
2,782
2,854
2,894
2,998
3,048
3,073
3,146
3,222
3,283
3,316
Bed
Volume
Totalizer
B
BV
NA
NA
NA
130
202
430
NA
NA
835
990
1,096
1,164
1,356
1,499
1,663
1,764
1,908
1,945
NA
NA
2,274
2,425
2,465
2,560
2,670
2,794
2,796
2,909
2,932
3,040
3,065
3,184
3,294
3,343
3,410
3,459
3,541
3,652
3,769
3,914
4,040
4,056
4,176
4,201
4,303
4,408
4,523
4,588
4,649
4,770
4,836
5,010
5,094
5,136
5,257
5,384
5,486
5,541
System Cum.
Volume
Treated
Kgal
NA
NA
NA
153
237
505
NA
NA
980
1,163
1,286
1,367
1,593
1,760
1,954
2,073
2,242
2,284
NA
NA
2,672
2,849
2,896
3,007
3,134
3,283
3,284
3,417
3,445
3,571
3,600
3,739
3,869
3,925
4,004
4,062
4,158
4,288
4,425
4,595
4,742
4,762
4,901
4,933
5,051
5,174
5,309
5,385
5,456
5,597
5,711
5,879
5,972
6,026
6,168
6,317
6,437
6,501
System
Total Bed
Volumes
Treated1"
BV
NA
NA
NA
127
198
422
NA
NA
819
971
1,075
1,142
1,331
1,471
1,633
1,732
1,873
1,908
NA
NA
2,232
2,380
2,419
2,512
2,619
2,743
2,744
2,855
2,878
2,983
3,008
3,124
3,232
3,279
3,346
3,394
3,474
3,582
3,697
3,839
3,962
3,978
4,095
4,122
4,220
4,323
4,436
4,499
4,559
4,677
4,772
4,912
4,989
5,035
5,153
5,278
5,378
5,432
Vessel AP
(psi)
A
NM
NM
2.1
2.2
2.2
2.8
NM
NM
2.2
2.2
2.0
2.2
2.0
2.0
2.2
2.2
2.2
2.2
NM
NM
2.3
2.1
2.0
2.0
2.1
2.1
2.2
2.2
2.2
2.2
2.0
2.1
2.0
2.1
2.1
2.1
2.1
2.1
2.6
2.2
2.6
2.5
2.8
2.8
2.4
2.2
2.7
2.7
2.6
2.4
2.2
2.2
2.4
2.2
2.5
2.3
2.3
B
NM
NM
2.2
2.0
2.0
2.0
NM
NM
2.0
2.4
1.9
2.2
2.1
2.0
2.0
2.0
2.0
2.1
NM
NM
2.1
2.0
2.0
2.0
2.0
2.0
2.1
2.1
2.1
2.0
2.1
2.0
2.1
2.2
2.0
2.0
2.0
2.0
2.0
1.8
2.0
2.0
2.0
2.0
2.2
2.1
2.2
2.1
2.0
2.1
2.1
2.1
2.0
2.2
2.1
2.2
2.0
System
AP
(psi)
psig
NA
NA
3
15
2
5
NA
NA
4
8
3
5
10
11
4
5
5
5
NA
NA
4
2
4
4
2
2
NA
4
4
4
4
4
2
5
5
5
3
5
4
5
5
4
2
4
4
3
4
3
4
3
2
3
5
4
4
4
6
System
Back-
wash
Yes/No
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
10
11
12
13
14
15
16
17
18
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
8/30/2004
8/31/2004
9/1/2004
9/2/2004
9/3/2004
9/4/2004
9/5/2004
9/6/2004
9/7/2004
9/8/2004
9/9/2004
9/10/2004
9/11/2004
9/12/2004
9/13/2004
9/14/2004
9/15/2004
9/16/2004
9/17/2004
9/18/2004
9/20/2004
9/21/2004
9/22/2004
9/23/2004
9/24/2004
9/25/2004
9/26/2004
9/27/2004
9/28/2004
9/29/2004
9/30/2004
10/1/2004
10/2/2004
1 0/3/2004
1 0/4/2004
1 0/5/2004
10/6/2004
10/7/2004
10/8/2004
10/9/2004
10/10/2004
10/11/2004
10/12/2004
10/13/2004
10/14/2004
10/15/2004
10/16/2004
10/17/2004
10/19/2004
10/20/2004
10/21/2004
10/22/2004
10/23/2004
10/24/2004
10/25/2004
10/26/2004
10/27/2004
10/28/2004
10/29/2004
10/30/2004
10/31/2004
Time
08:51
09:15
09:00
09:00
14:45
17:00
15:40
16:30
09:15
08:45
06:43
10:00
19:00
17:30
09:40
10:00
09:10
09:25
09:15
23:30
09:41
09:00
10:50
09:20
09:30
17:00
16:30
09:10
08:45
13:10
09:15
11:23
16:30
18:00
12:31
08:45
09:30
8:30
07:45
16:45
16:40
14:30
08:51
13:00
06:15
08:45
18:59
16:30
11:15
08:56
10:40
11:00
19:30
17:19
08:50
09:20
08:30
09:10
14:00
18:18
17:00
Well House #1 Reading
Opt Hours
Well!
hr
12.5
3.0
7.1
9.9
10.2
6.0
7.2
10.2
6.7
4.4
9.2
4.1
9.4
8.9
11.3
10.4
3.0
8.5
0.2
9.2
0.1
0.0
20.7
11.8
5.3
7.5
8.8
10.1
0.8
2.1
10.3
2.3
8.2
9.9
0.3
0.9
9.3
1.2
2.2
8.4
13.0
7.3
2.9
7.7
1.2
0.3
10.9
6.5
10.0
2.6
8.8
0.1
10.1
0.5
0.1
9.0
1.0
8.6
0.5
8.1
0.7
Daily Flow
Totalizer
qal
180,000
45,000
102,000
143,000
147,000
88,000
104,000
147,000
97,000
63,000
133,000
61,000
135,000
128,000
164,000
151,000
42,000
123,000
3,000
133,000
1,000
0
295,000
184,000
77,000
109,000
126,000
146,000
12,000
30,000
149,000
35,000
118,000
142,000
4,000
14,000
133,000
18,000
32,000
121,000
189,000
106,000
41,000
112,000
21,000
0
158,000
93,000
144,000
37,000
127,000
2,000
147,000
6,000
2,000
130,000
14,000
125,000
7,000
117,000
11,000
Avg
Flowrate
qpm
240
250
239
241
240
244
241
240
241
239
241
248
239
240
242
242
233
241
250
241
167
NA
238
260
242
242
239
241
250
238
241
254
240
239
222
259
238
250
242
240
242
242
236
242
292
NA
242
238
240
237
241
333
243
200
333
241
233
242
233
241
262
APU
Electric
Meter
KWH
47000
47070
47233
47460
47695
47834
47999
48234
48388
48489
48701
48797
49013
49216
49477
49718
49580
49984
49989
50201
50204
50207
50668
50964
51090
51267
51468
51701
51722
51772
52005
52065
52252
52479
52509
52511
52123
52723
52805
52999
53300
53469
53537
53717
53910
53252
54008
54161
54396
54457
54662
54669
55011
55021
55029
55240
55266
55466
55482
55670
55688
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
qpm
110.7
114.0
112.3
112.0
112.4
112.9
112.7
115.8
115.4
116.9
114.9
112.6
119.9
113.0
116.0
118.0
116.0
119.7
116.0
116.0
0.0
0.0
112.8
113.0
110.0
116.0
115.0
115.6
116.8
117.7
114.5
116.0
115.0
114.0
110.3
114.8
115.8
114.5
113.3
115.9
115.6
119.3
115.5
115.0
115.0
115.1
114.9
115.4
114.8
113.8
114.0
114.2
112.0
115.8
115.0
118.0
117.4
115.0
114.8
115.7
115.3
Daily Flow
Totalizer
A
qal
82,429
20,390
46,552
65,717
67,801
39,926
47,129
67,428
44,441
28,996
61,176
27,810
62,208
58,221
75,205
69,193
19,391
57,406
372
60,975
0
0
136,428
84,943
35,677
50,093
58,078
67,606
6,185
13,275
68,860
16,185
54,064
65,658
7,911
693
61,428
8,380
14,438
56,137
87,365
49,514
18,537
51,851
9,456
79
72,979
42,868
67,164
15,874
58,523
958
70,293
367
775
60,228
6,450
57,600
3,317
55,657
53,272
Cum.
Flow
Totalizer
A
Kqal
3,268
3,288
3,335
3,400
3,468
3,508
3,555
3,623
3,667
3,696
3,757
3,785
3,847
3,906
3,981
4,050
4,069
4,127
4,127
4,188
4,189
4,189
4,325
4,410
4,446
4,496
4,554
4,621
4,628
4,641
4,710
4,726
4,780
4,846
4,853
4,854
4,916
4,924
4,938
4,995
5,082
5,131
5,150
5,202
5,211
5,211
5,284
5,327
5,396
5,412
5,470
5,471
5,541
5,542
5,542
5,603
5,609
5,667
5,670
5,726
5,779
Bed
Volume
Totalizer
A
BV
5,460
5,495
5,572
5,682
5,795
5,862
5,941
6,054
6,128
6,176
6,279
6,325
6,429
6,526
6,652
6,768
6,800
6,896
6,896
6,998
6,999
6,999
7,227
7,369
7,429
7,512
7,609
7,722
7,733
7,755
7,870
7,897
7,987
8,097
8,110
8,111
8,214
8,228
8,252
8,346
8,492
8,575
8,606
8,692
8,708
8,708
8,830
8,902
9,016
9,043
9,141
9,142
9,260
9,260
9,261
9,362
9,373
9,469
9,475
9,568
9,657
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
114.9
114.7
114.8
117.5
120.2
119.8
117.4
112.6
114.9
117.6
115.4
116.7
115.9
114.0
117.2
118.6
117.9
115.9
116.0
116.0
0.0
0.0
114.0
114.0
117.0
119.0
116.0
117.9
118.6
116.8
117.8
115.0
116.0
114.0
116.7
116.3
115.3
114.8
117.7
117.5
117.5
112.1
112.0
114.1
114.5
115.7
113.3
114.0
NM
115.2
114.6
114.0
113.3
NM
116.0
115.0
114.8
114.6
113.3
116.3
117.5
Daily Flow
Totalizer
B
qal
86,046
21,267
48,640
68,830
70,859
41,777
49,304
70,507
46,486
30,355
63,947
29,065
64,951
60,651
78,686
72,236
20,268
59,956
378
63,743
0
0
142,109
87,677
36,979
52,133
60,246
70,299
6,449
13,762
71,435
16,814
56,077
68,260
8,223
715
33,834
38,685
14,984
58,266
90,817
51,276
19,419
53,812
9,816
133
75,785
44,422
69,750
16,580
61,191
487
72,836
360
745
62,643
6,614
59,760
3,510
57,678
3,461
Cum. Flow
Totalizer
B
Kqal
3,402
3,423
3,472
3,541
3,612
3,654
3,703
3,773
3,820
3,850
3,914
3,943
4,008
4,069
4,147
4,220
4,240
4,300
4,300
4,364
4,364
4,364
4,507
4,594
4,631
4,683
4,744
4,814
4,820
4,834
4,906
4,922
4,978
5,047
5,055
5,056
5,089
5,128
5,143
5,201
5,292
5,344
5,363
5,417
5,427
5,427
5,502
5,547
5,618
5,635
5,696
5,696
5,769
5,769
5,770
5,833
5,839
5,899
5,903
5,960
5,964
Bed
Volume
Totalizer
B
BV
5,685
5,721
5,802
5,917
6,035
6,105
6,187
6,305
6,383
6,434
6,541
6,589
6,698
6,799
6,930
7,051
7,085
7,185
7,186
7,292
7,293
7,293
7,531
7,677
7,739
7,826
7,927
8,044
8,055
8,078
8,197
8,225
8,319
8,433
8,447
8,448
8,505
8,569
8,594
8,692
8,843
8,929
8,962
9,051
9,068
9,068
9,195
9,269
9,388
9,415
9,518
9,518
9,640
9,641
9,642
9,747
9,758
9,858
9,863
9,960
9,966
System Cum.
Volume
Treated
Kqal
6,670
6,712
6,807
6,941
7,080
7,162
7,258
7,396
7,487
7,546
7,671
7,728
7,855
7,974
8,128
8,270
8,309
8,427
8,427
8,552
8,553
8,553
8,832
9,004
9,077
9,179
9,297
9,435
9,448
9,475
9,615
9,648
9,758
9,892
9,908
9,910
10,005
10,052
10,082
10,196
10,374
10,475
10,513
10,619
10,638
10,638
10,787
10,874
11,014
11,046
11,166
11,167
11,310
11,311
11,313
11,435
11,449
11,566
11,573
11,686
11,743
System
Total Bed
Volumes
Treated"1
BV
5,573
5,608
5,687
5,799
5,915
5,984
6,064
6,179
6,255
6,305
6,410
6,457
6,563
6,663
6,791
6,909
6,942
7,041
7,041
7,145
7,146
7,146
7,379
7,523
7,584
7,669
7,768
7,883
7,894
7,916
8,034
8,061
8,153
8,265
8,279
8,280
8,359
8,399
8,423
8,519
8,668
8,752
8,784
8,872
8,888
8,888
9,012
9,085
9,202
9,229
9,329
9,330
9,450
9,450
9,452
9,554
9,565
9,663
9,669
9,764
9,811
Vessel AP
(psi)
A
2.1
2.5
2.2
2.2
2.1
2.1
2.3
2.1
2.1
2.2
2.1
2.2
2.6
2.4
2.2
2.8
2.8
2.9
2.3
2.7
0.0
0.0
2.2
2.4
2.5
2.3
2.4
2.2
2.8
2.4
2.6
2.2
2.4
2.2
2.2
2.0
2.8
3.0
2.8
2.6
2.2
2.0
2.8
2.0
2.2
3.0
2.8
2.4
2.5
3.0
3.0
2.6
2.0
2.2
2.2
2.2
2.2
2.2
2.4
2.0
2.2
B
2.0
2.0
2.1
2.1
2.0
2.0
2.2
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.0
2.6
2.2
1.9
2.0
2.1
0.0
0.0
2.0
2.2
2.1
2.2
2.2
2.0
2.0
2.0
2.0
2.0
2.1
2.0
2.0
2.2
2.6
2.8
2.6
2.2
2.2
2.0
2.2
2.0
2.2
2.8
2.6
2.5
2.1
2.1
2.0
2.5
2.0
2.1
2.4
2.6
2.2
2.0
2.1
2.1
2.6
System
AP
(psi)
PSiq
4
4
4
4
4
5
4
4
4
5
4
4
5
2
4
4
4
4
5
5
NA
NA
4
5
3
5
2
5
5
4
4
4
4
5
5
4
4
4
4
5
5
4
5
4
10
2
4
4
5
5
5
4
5
7
2
4
6
6
5
4
4
System
Back-
wash
Yes/No
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
19
20
21
22
23
24
25
26
27
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
11/1/2004
11/2/2004
11/3/2004
11/4/2004
11/5/2004
11/6/2004
11/8/2004
11/9/2004'°'
11/10/2004
11/11/2004
11/12/2004
11/13/2004
11/14/2004
11/15/2004
11/16/2004
11/17/2004
11/18/2004
11/19/2004
11/20/2004
11/22/2004
11/23/2004
11/24/2004
11/25/2004
11/26/2004
11/27/2004
11/28/2004
11/29/2004
11/30/2004
12/1/2004
12/2/2004
12/3/2004
12/4/2004
12/5/2004
12/6/2004
12/7/2004
12/8/2004
12/9/2004
12/10/2004
12/11/2004
12/12/2004
12/13/2004
12/14/2004
12/15/2004
12/16/2004
12/17/2004
12/18/2004
12/19/2004
12/21/2004
1 2/22/2004
12/23/2004
1 2/24/2004
12/25/2004
1 2/26/2004
1 2/27/2004
1 2/28/2004
12/29/2004
12/30/2004
12/31/2004
1/1/2005
1/2/2005
Time
10:50
15:45
08:30
10:17
10:25
17:30
08:45
09:30
08:00
16:40
09:00
17:10
16:45
08:42
12:50
13:35
08:30
08:20
15:10
11:30
08:30
09:45
07:45
16:30
16:25
20:45
09:15
09:00
09:55
09:00
09:40
17:00
21:00
08:30
11:15
06:40
09:15
09:30
15:45
16:25
10:36
10:00
07:30
08:30
09:30
20:24
16:20
09:00
06:30
07:30
14:30
14:30
14:10
10:45
07:00
10:00
06:30
NA
16:00
16:45
Well House #1 Reading
Opt Hours
Well!
hr
8.3
0.5
8.7
1.0
6.7
3.4
4.5
0.0
8.9
0.5
1.5
7.8
4.1
5.6
0.4
9.3
0.3
1.6
8.3
2.2
0.1
7.9
0.1
8.8
0.1
8.8
0.7
8.7
3.1
0.5
9.4
2.0
5.2
3.9
2.0
1.5
8.7
0.1
7.2
0.9
8.4
0.1
3.0
6.7
0.7
9.7
5.9
0.1
9.2
2.2
10.6
2.7
1.6
5.7
0.4
2.3
9.3
NA
NA
1.6
Daily Flow
Totalizer
aal
120,000
7,000
125,000
15,000
96,000
49,000
63,000
0
129,000
0
29,000
111,000
59,000
79,000
7,000
130,000
0
27,000
120,000
30,000
1,000
114,000
1,000
126,000
0
128,000
10,000
125,000
42,000
8,000
132,000
29,000
76,000
55,000
28,000
21,000
123,000
2,000
114,000
0
120,000
1,000
47,000
89,000
9,000
140,000
81,000
2,000
125,000
30,000
66,000
83,000
61,000
79,000
7,000
33,000
131,000
NA
134,000
21,000
Avg
Flowrate
apm
241
233
239
250
239
240
233
NA
242
NA
322
237
240
235
292
233
NA
281
241
227
167
241
167
239
NA
242
238
239
226
267
234
242
244
235
233
233
236
333
264
NA
238
167
261
221
214
241
229
333
226
227
104
512
635
231
292
239
235
NA
NA
219
APU
Electric
Meter
KWH
55880
55893
56092
56117
56272
56355
56580
56573
56839
56901
56954
57191
57339
57490
57550
57795
57832
57878
58092
58340
58362
58567
58573
58779
58785
58997
59089
59219
59256
59363
59519
59872
59676
59787
59840
59876
60077
60083
60270
60275
60470
60476
60555
60705
60725
60958
61093
61207
61421
61476
61556
61724
61828
61960
61987
62089
62344
NM
626449
62719
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
qpm
113.2
112.2
114.0
112.7
113.0
NA
115.2
114.0
113.5
114.0
115.7
115.1
116.8
120.4
120.6
113.0
114.0
113.6
113.5
105.0
108.0
114.8
115.4
115.0
114.5
117.1
117.0
117.0
118.0
117.2
119.4
118.4
118.1
116.0
113.9
118.8
117.9
114.1
118.1
118.9
116.6
114.9
118.3
118.2
114.7
120.7
115.0
112.9
113.0
118.6
117.3
115.9
115.0
115.7
116.1
117.6
118.8
NM
116.3
118.0
Daily Flow
Totalizer
A
aal
5,306
3,603
57,521
6,715
44,495
5,971
24,165
307
59,588
3,276
10,076
52,462
28,033
38,171
3,266
63,838
2,622
10,021
55,850
14,981
510
51,827
2,515
60,649
642
65,763
609
61,763
80,938
3,805
6,240
14,265
38,344
27,502
13,968
11,862
61,600
1,174
58,547
699
61,680
1,330
21,446
88,821
5,448
30,992
43,071
840
67,298
15,682
34,011
42,802
31,925
40,560
3,208
16,983
66,355
NA
NA
11,087
Cum.
Flow
Totalizer
A
Kaal
5,784
5,788
5,845
5,852
5,897
5,903
5,927
5,927
5,987
5,990
6,000
6,052
6,080
6,119
6,122
6,186
6,188
6,198
6,254
6,318
6,319
6,370
6,373
6,434
6,434
6,500
6,501
6,562
6,643
6,647
6,653
6,668
6,706
6,733
6,747
6,759
6,821
6,822
6,881
6,881
6,943
6,944
6,966
7,055
7,060
7,091
7,134
7,168
7,235
7,251
7,285
7,328
7,360
7,400
7,403
7,420
7,487
NA
7,487
7,498
Bed
Volume
Totalizer
A
BV
9,666
9,672
9,768
9,779
9,853
9,863
9,904
9,904
10,004
10,009
10,026
10,114
10,161
10,224
10,230
10,336
10,341
10,358
10,451
10,558
10,558
10,645
10,649
10,751
10,752
10,862
10,863
10,966
11,101
11,107
11,118
11,142
11,206
11,252
11,275
11,295
11,398
11,400
11,498
11,499
11,602
11,604
11,640
11,788
11,797
11,849
11,921
11,977
12,090
12,116
12,173
12,244
12,298
12,366
12,371
12,399
12,510
NA
12,510
12,529
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
114.5
112.9
113.5
116.7
117.0
118.7
118.4
113.5
114.7
114.0
116.4
113.9
114.5
110.3
109.4
115.0
114.0
0.0
0.0
110.2
110.0
115.1
117.4
114.0
114.0
114.7
117.3
110.7
117.0
117.1
108.7
113.6
105.5
111.1
103.9
105.2
104.2
105.6
106.2
105.6
106.9
109.4
92.7
98.9
101.8
94.9
95.0
100.2
107.1
102.6
103.1
106.9
100.0
104.5
105.1
103.9
101.8
NM
104.9
100.0
Daily Flow
Totalizer
B
aal
57,348
3,745
59,592
7,051
46,148
23,800
30,428
1,208
60,214
3,206
10,159
51,398
26,286
35,151
2,965
56,559
2,197
5,912
4
709
507
50,210
436
53,276
577
57,210
531
51,917
17,309
3,291
53,833
11,705
30,674
22,476
11,310
9,352
46,889
1,065
44,047
538
46,064
711
16,333
35,533
4,197
53,058
32,119
579
50,603
12,187
25,545
32,226
24,038
30,584
2,425
12,656
50,701
NA
52,422
8,590
Cum. Flow
Totalizer
B
Kaal
6,021
6,025
6,084
6,092
6,138
6,161
6,229
6,230
6,290
6,294
6,304
6,355
6,381
6,417
6,420
6,476
6,478
6,484
6,484
6,485
6,485
6,536
6,536
6,589
6,590
6,647
6,648
6,700
6,717
6,720
6,774
6,786
6,816
6,839
6,850
6,860
6,906
6,907
6,952
6,952
6,998
6,999
7,015
7,051
7,055
7,108
7,140
7,165
7,216
7,228
7,254
7,286
7,310
7,341
7,343
7,356
7,406
NA
7,459
7,467
Bed
Volume
Totalizer
B
BV
10,061
10,068
10,167
10,179
10,256
10,296
10,409
10,411
10,511
10,517
10,534
10,619
10,663
10,722
10,727
10,822
10,825
10,835
10,835
10,836
10,837
10,921
10,922
11,011
11,012
11,107
11,108
11,195
11,224
11,229
11,319
11,339
11,390
11,428
11,447
11,462
11,541
11,542
11,616
11,617
11,694
11,695
11,722
11,782
11,789
11,877
11,931
11,973
12,058
12,078
12,121
12,175
12,215
12,266
12,270
12,291
12,376
NA
12,464
12,478
System Cum.
Volume
Treated
Kaal
11,805
11,813
11,930
11,944
12,034
12,064
12,156
12,157
12,277
12,283
12,304
12,408
12,462
12,535
12,541
12,662
12,667
12,683
12,738
12,803
12,804
12,906
12,909
13,023
13,024
13,147
13,148
13,262
13,360
13,367
13,427
13,453
13,522
13,572
13,598
13,619
13,727
13,730
13,832
13,833
13,941
13,943
13,981
14,105
14,115
14,199
14,274
14,333
14,451
14,479
14,538
14,614
14,669
14,741
14,746
14,776
14,893
NA
NA
14,965
System
Total Bed
Volumes
Treated"1
BV
9,864
9,870
9,967
9,979
10,055
10,080
10,156
10,157
10,257
10,263
10,280
10,367
10,412
10,473
10,478
10,579
10,583
10,596
10,643
10,697
10,698
10,783
10,786
10,881
10,882
10,984
10,985
11,080
11,162
11,168
11,219
11,240
11,298
11,340
11,361
11,379
11,469
11,471
11,557
11,558
11,648
11,650
11,681
11,785
11,793
11,863
11,926
11,975
12,074
12,097
12,147
12,210
12,256
12,316
12,321
12,345
12,443
NA
NA
12,503
Vessel AP
(psi)
A
2.2
2.2
2.4
2.3
2.2
2.4
2.0
2.4
3.0
2.8
3.0
3.4
3.5
4.2
4.5
2.0
2.4
2.4
2.6
2.6
2.8
3.0
3.2
3.6
3.6
3.4
3.5
4.4
4.5
4.8
4.8
4.8
4.8
5.0
5.2
5.1
5.8
5.9
5.9
5.9
7.5
7.0
6.0
6.2
6.1
6.0
6.2
6.2
6.0
6.0
6.2
6.1
6.2
6.0
6.0
6.5
6.0
NM
6.0
6.0
B
2.1
2.0
2.2
2.2
2.4
2.0
2.1
2.5
2.8
2.8
3.0
3.4
3.5
4.5
4.8
2.6
2.0
2.0
2.4
2.6
2.6
3.0
3.2
3.6
3.6
3.6
4.0
4.0
4.6
4.9
4.9
5.0
5.0
5.1
5.6
5.3
6.0
6.0
6.0
6.1
6.0
5.8
6.6
6.9
6.9
6.8
6.8
7.0
6.9
6.5
7.0
7.0
7.1
7.0
7.0
7.5
7.0
NM
6.9
6.4
System
AP
(psi)
psia
6
4
2
6
6
6
5
2
5
1
4
5
6
8
6
12
10
10
10
11
12
10
15
12
10
12
12
10
12
12
13
12
12
14
14
14
15
14
14
13
2
1
15
12
14
15
14
14
14
14
16
14
14
1
14
14
14
NA
13
10
System
Back-
wash
Yes/No
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
28
29
30
31
32
33
34
35
36
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
1/3/2005
1/4/2005
1/5/2005
1/6/2005
1/7/2005
1/8/2005
1/10/2005
1/11/2005
1/12/2005
1/13/2005
1/14/2005
1/15/2005
1/16/2005
1/18/2005
1/19/2005
1/20/2005
1/21/2005
1/22/2005
1/23/2005
1/24/2005
1/25/2005
1/26/2005
1/27/2005
1/28/2005
1/29/2005
1/30/2005
1/31/2005
2/1/2005
2/2/2005
2/3/2005
2/4/2005
2/5/2005
2/6/2005
2/7/2005
2/8/2005
2/9/2005
2/10/2005
2/11/2005
2/12/2005
2/13/2005
2/14/2005
2/15/2005
2/16/2005
2/17/2005
2/18/2005
2/19/2005
2/20/2005
2/22/2005
2/23/2005
2/24/2005
2/25/2005
2/26/2005
2/28/2005
3/1/2005
3/2/2005
3/3/2005
3/4/2005
3/5/2005
3/6/2005
Time
09:00
09:10
07:00
09:00
06:30
18:00
11:15
11:45
11:15
12:40
11:00
18:00
16:20
09:00
09:30
06:35
09:10
03:00
16:25
09:00
09:20
10:10
11:25
09:45
19:20
11:00
09:05
09:00
09:25
09:20
09:20
17:00
20:35
10:00
13:15
09:00
06:30
09:00
18:00
18:30
08:03
16:50
09:00
09:00
09:00
17:50
16:45
13:36
09:05
06:45
07:05
NA
10:10
09:05
06:45
06:55
14:50
16:30
NA
Well House #1 Reading
Opt Hours
Well!
hr
7.9
0.3
1.9
9.5
0.2
8.3
9.2
0.2
3.7
7.0
2.3
4.5
4.9
8.5
0.3
0.9
10.0
0.5
6.3
5.1
0.1
9.0
1.1
7.2
0.5
9.7
0.7
0.1
9.1
0.7
1.2
9.2
0.3
3.7
6.0
0.2
8.6
1.4
6.8
2.8
0.1
8.8
1.8
0.2
9.1
0.3
9.1
0.9
8.9
0.0
7.9
0.5
0.0
1.1
8.8
1.1
9.2
0.5
9.0
Daily Flow
Totalizer
aal
113,000
4,000
27,000
134,000
3,000
118,000
128,000
2,000
52,000
101,000
33,000
66,000
69,000
122,000
3,000
15,000
143,000
7,000
89,000
73,000
1,000
129,000
15,000
102,000
8,000
137,000
10,000
2,000
128,000
10,000
16,000
132,000
3,000
52,000
85,000
3,000
121,000
19,000
97,000
39,000
1,000
123,000
25,000
4,000
126,000
5,000
127,000
11,000
128,000
0
114,000
6,000
0
15,000
126,000
15,000
131,000
7,000
129,000
Avg
Flowrate
QDm
238
222
237
235
250
237
232
167
234
240
239
244
235
239
167
278
238
233
235
239
167
239
227
236
267
235
238
333
234
238
222
239
167
234
236
250
234
226
238
232
167
233
231
333
231
278
233
204
240
NA
241
200
NA
227
239
227
237
233
239
APU
Electric
Meter
KWH
62928
62947
62999
63227
63237
63436
63660
63668
63761
63927
63983
64030
64207
64414
64425
64484
64756
64797
65001
65146
65185
65434
65502
65711
65794
66050
66095
66141
66395
66429
66448
66687
66714
66811
66968
66984
67195
67253
67441
67523
67534
67755
67812
67831
68060
68111
68345
68419
68637
68655
68868
68915
69133
69214
69425
69477
69724
69757
69991
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
qpm
116.9
118.1
117.1
115.9
113.4
115.9
121.5
121.3
117.2
116.4
116.7
116.0
115.0
113.9
114.5
112.8
112.8
114.3
113.0
121.8
120.0
114.2
116.6
116.8
115.9
116.3
111.1
113.8
116.2
116.2
116.6
115.0
118.0
114.9
113.7
111.6
116.7
116.4
116.5
116.0
116.1
118.1
116.5
118.2
114.2
117.6
117.4
116.0
116.2
116.4
117.5
117.2
116.0
116.0
117.2
116.4
116.2
125.0
119.5
Daily Flow
Totalizer
A
aal
56,789
2,015
13,698
68,867
1,776
58,795
67,846
1,019
25,851
46,401
15,217
10,616
51,789
56,726
1,711
6,517
67,000
3,468
41,738
34,348
1,232
61,282
7,000
31,261
24,282
64,366
4,708
489
62,857
8,878
4,538
64,825
4,193
23,601
42,437
1,422
63,494
7,121
48,860
19,863
420
62,638
12,933
1,667
64,954
2,257
70,593
5,044
58,793
374
53,569
2,962
0
7,492
61,510
1,258
70,531
3,990
66,231
Cum.
Flow
Totalizer
A
Kaal
7,555
7,557
7,570
7,639
7,641
7,700
7,770
7,771
7,797
7,843
7,858
7,869
7,921
7,978
7,980
7,986
8,053
8,057
8,098
8,133
8,134
8,195
8,202
8,234
8,258
8,322
8,327
8,327
8,390
8,399
8,404
8,468
8,473
8,496
8,539
8,540
8,604
8,611
8,660
8,679
8,680
8,742
8,755
8,757
8,822
8,824
8,895
8,902
8,961
8,961
9,015
9,018
9,077
9,084
9,146
9,147
9,218
9,222
9,288
Bed
Volume
Totalizer
A
BV
12,624
12,627
12,650
12,765
12,768
12,866
12,984
12,985
13,029
13,106
13,132
13,149
13,236
13,331
13,334
13,345
13,457
13,463
13,532
13,590
13,592
13,694
13,706
13,758
13,799
13,906
13,914
13,915
14,020
14,035
14,043
14,151
14,158
14,197
14,268
14,271
14,377
14,389
14,470
14,503
14,504
14,609
14,630
14,633
14,742
14,746
14,863
14,876
14,974
14,975
15,064
15,069
15,168
15,180
15,283
15,285
15,403
15,410
15,520
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
102.7
104.4
105.2
102.1
103.0
102.3
90.3
92.7
115.4
116.5
115.1
116.7
114.0
112.0
112.0
110.7
111.3
109.2
110.0
122.9
115.4
96.4
98.8
95.6
99.3
97.6
108.7
107.9
103.9
106.2
102.5
100.2
95.1
100.8
103.1
102.7
98.7
106.1
97.0
98.4
110.1
101.6
103.2
103.3
101.1
104.6
94.3
111.5
115.8
111.3
113.4
107.9
103.0
102.0
102.7
105.1
103.9
100.0
91.8
Daily Flow
Totalizer
B
aal
44,154
1,507
10,599
51,258
1,267
43,307
47,953
711
20,376
44,884
14,512
29,204
30,315
54,297
1,649
6,180
62,201
3,170
42,803
25,719
1,096
53,683
6,051
43,979
3,655
54,326
3,866
475
52,256
7,264
3,778
52,066
3,361
18,883
33,074
1,083
49,612
5,555
37,714
14,960
329
47,767
10,049
1,281
48,515
1,679
48,066
4,637
55,869
331
48,663
2,761
0
6,351
51,329
6,008
53,845
1,127
51,624
Cum. Flow
Totalizer
B
Kaal
7,513
7,524
7,575
7,576
7,619
7,668
7,668
7,689
7,734
7,748
7,777
7,808
7,862
7,864
7,870
7,932
7,936
7,978
8,004
8,005
8,059
8,065
8,109
8,113
8,167
8,171
8,171
8,224
8,231
8,235
8,287
8,290
8,309
8,342
8,343
8,393
8,398
8,436
8,451
8,451
8,499
8,509
8,510
8,559
8,561
8,609
8,618
8,674
8,674
8,723
8,726
8,777
8,783
8,835
8,841
8,895
8,896
8,947
Bed
Volume
Totalizer
B
BV
12,552
12,554
12,572
12,658
12,660
12,732
12,813
12,814
12,848
12,923
12,947
12,996
13,047
13,138
13,141
13,151
13,255
13,261
13,332
13,375
13,377
13,467
13,477
13,550
13,556
13,647
13,654
13,654
13,742
13,754
13,760
13,847
13,853
13,884
13,940
13,941
14,024
14,034
14,097
14,122
14,122
14,202
14,219
14,221
14,302
14,305
14,385
14,401
14,494
14,495
14,576
14,581
14,667
14,677
14,763
14,773
14,863
14,865
14,951
System Cum.
Volume
Treated
Kaal
15,066
15,070
15,094
15,214
15,217
15,319
15,438
15,439
15,486
15,577
15,607
15,647
15,729
15,840
15,844
15,856
15,986
15,992
16,077
16,137
16,139
16,254
16,267
16,342
16,370
16,489
16,498
16,499
16,614
16,630
16,638
16,755
16,763
16,805
16,881
16,883
16,996
17,009
17,096
17,130
17,131
17,241
17,264
17,267
17,381
17,385
17,503
17,520
17,635
17,636
17,738
17,744
17,854
17,868
17,981
17,988
18,112
18,117
18,235
System
Total Bed
Volumes
Treated"1
BV
12,588
12,591
12,611
12,711
12,714
12,799
12,898
12,900
12,938
13,015
13,039
13,073
13,141
13,235
13,238
13,248
13,356
13,362
13,432
13,482
13,484
13,580
13,591
13,654
13,678
13,777
13,784
13,785
13,881
13,894
13,901
13,999
14,005
14,041
14,104
14,106
14,200
14,211
14,283
14,312
14,313
14,405
14,425
14,427
14,522
14,525
14,624
14,638
14,734
14,735
14,820
14,825
14,917
14,929
15,023
15,029
15,133
15,137
15,236
Vessel AP
(psi)
A
5.9
6.0
6.0
7.2
7.2
7.9
7.8
8.0
2.0
2.0
2.9
2.8
2.9
2.6
2.4
2.5
3.0
3.0
3.2
3.6
3.6
3.9
4.1
4.2
4.4
4.5
5.0
5.0
5.2
5.5
5.4
6.2
6.1
6.0
6.8
6.4
6.8
7.0
7.0
8.0
8.0
8.1
8.0
8.1
9.0
9.0
9.2
2.2
3.0
3.0
3.0
3.1
3.2
3.4
4.0
4.1
4.1
4.9
4.8
B
6.9
6.9
6.9
8.9
8.6
8.9
9.0
9.1
2.0
2.1
2.8
2.8
2.8
2.6
2.6
2.5
3.0
3.0
3.2
3.8
3.8
4.1
4.3
4.5
4.6
5.0
5.1
5.1
5.3
6.0
5.9
6.4
6.3
6.3
7.0
7.0
7.4
8.0
8.0
8.8
8.5
9.0
9.0
9.0
9.8
9.6
9.6
2.2
2.3
3.0
3.0
3.0
3.3
3.8
4.5
4.6
4.8
5.1
5.4
System
AP
(psi)
psia
15
14
15
15
16
16
17
20
7
10
12
12
10
12
18
9
10
11
12
14
10
12
13
13
13
10
14
14
14
12
14
14
14
16
14
16
15
16
16
17
16
16
16
16
18
16
18
12
10
12
12
12
13
12
10
12
13
12
14
System
Back-
wash
Yes/No
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
37
38
39
40
41
42
43
44
45
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
3/7/2005
3/8/2005
3/9/2005
3/10/2005
3/11/2005
3/12/2005
3/14/2005
3/15/2005
3/16/2005
3/17/2005
3/18/2005
3/19/2005
3/20/2005
3/22/2005
3/23/2005
3/24/2005
3/25/2005
3/26/2005
3/28/2005
3/29/2005
3/30/2005
3/31/2005
4/1/2005
4/2/2005
4/3/2005
4/5/2005
4/6/2005
4/7/2005
4/8/2005
4/9/2005
4/10/2005
4/11/2005
4/12/2005
4/13/2005
4/14/2005
4/15/2005
4/16/2005
4/17/2005
4/18/20051''
4/19/2005
4/20/2005
4/21/2005
4/22/2005
4/23/2005
4/24/2005
4/25/2005
4/26/2005
4/27/2005
4/28/2005
4/29/2005
4/30/2005
5/1/2005
5/2/2005
5/3/2005
5/4/2005
5/5//05
5/6/2005
5/7/2005
5/8/2005
Time
08:40
06:30
08:55
14:41
11:15
11:20
09:15
08:35
06:00
06:30
09:25
05:00
17:30
09:00
15:30
06:30
06:50
18:00
09:01
06:45
10:55
11:45
09:55
16:15
16:50
09:15
09:02
09:00
13:15
17:45
16:40
13:30
07:18
09:05
10:00
09:15
20:50
17:00
09:10
13:40
09:10
08:44
09:22
17:20
17:20
09:00
10:30
09:05
09:04
09:06
17:50
19:00
09:29
09:00
10:00
09:30
09:00
16:50
20:45
Well House #1 Reading
Opt Hours
Well!
hr
1.1
0.3
9.4
0.2
8.3
0.1
0.5
0.3
8.9
0.7
3.7
6.4
9.3
0.9
7.7
2.9
8.9
0.2
7.7
0.3
8.4
1.7
1.5
8.1
3.2
0.3
9.0
3.7
6.2
4.4
5.0
6.5
0.4
8.8
1.9
1.2
9.0
7.9
3.9
5.0
6.2
3.6
6.8
7.0
3.2
0.8
8.6
6.0
4.5
1.2
9.2
7.3
2.9
0.3
9.3
0.0
9.4
3.4
8.0
Daily Flow
Totalizer
aal
15,000
0
137,000
3,000
117,000
2,000
7,000
4,000
125,000
10,000
52,000
89,000
130,000
11,000
108,000
42,000
127,000
4,000
111,000
4,000
119,000
26,000
21,000
115,000
49,000
5,000
127,000
53,000
86,000
63,000
72,000
76,000
5,000
138,000
27,000
16,000
127,000
109,000
55,000
69,000
87,000
50,000
97,000
101,000
47,000
11,000
123,000
89,000
60,000
18,000
130,000
105,000
40,000
4,000
132,000
0
132,000
48,000
110,000
Avg
Flowrate
QDm
227
NA
243
250
235
333
233
222
234
238
234
232
233
204
234
241
238
333
240
222
236
255
233
237
255
278
235
239
231
239
240
195
208
261
237
222
235
230
235
230
234
231
238
240
245
229
238
247
222
250
236
240
230
222
237
NA
234
235
229
APU
Electric
Meter
KWH
70021
70036
70277
70320
70530
70553
70827
70852
71073
71107
71213
71383
71611
71699
71902
71981
72215
72231
72477
72492
72899
72753
72798
73000
73089
73271
73486
73578
73725
73839
73958
74085
74095
74325
74372
74402
74613
74796
748.89
750.05
751.5
752.36
753.98
75562
75639
756.58
758.62
759.08
761.07
761.35
763.51
765.23
765.91
765.98
768.17
769.14
770.37
771.18
773.03
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
qpm
118.8
119.4
115.8
121.5
116.7
118.1
117.0
118.6
117.5
115.0
128.7
129.4
124.6
127.8
122.7
109.7
116.7
117.3
115.7
113.6
113.4
115.1
116.0
118.6
117.0
137.9
119.6
133.2
119.9
116.9
119.0
136.9
123.2
125.0
139.9
134.5
125.4
123.0
133.1
115.4
NM
109.6
109.6
116.3
116.6
115.0
125.8
117.9
114.4
121.6
121.7
128.8
129.0
119.0
117.0
117.0
119.9
118.0
115.2
Daily Flow
Totalizer
A
aal
6,321
2,161
66,967
1,930
60,041
943
3,816
1,879
66,022
5,380
27,473
47,968
70,434
6,161
52,194
19,359
61,345
529
54,068
1,782
59,856
12,449
10,769
58,495
23,702
2,280
65,387
26,794
44,002
33,715
36,192
40,782
2,874
73,391
14,287
9,137
67,377
58,750
29,997
35,971
45,688
22,292
45,121
47,719
22,167
5,559
60,272
14,220
60,732
8,175
66,498
30,865
42,884
1,620
67,142
461
67,450
24,890
57,871
Cum.
Flow
Totalizer
A
Kaal
9,294
9,296
9,363
9,365
9,425
9,426
9,504
9,506
9,572
9,578
9,605
9,653
9,724
9,743
9,796
9,815
9,876
9,877
9,943
9,944
10,004
10,017
10,027
10,086
10,110
10,161
10,226
10,253
10,297
10,330
10,367
10,407
10,410
10,484
10,498
10,507
10,574
10,633
10,663
10,699
10,745
10,767
10,812
10,860
10,882
10,888
10,948
10,962
11,023
11,031
11,098
11,128
11,171
11,173
11,240
11,241
11,308
11,333
11,391
Bed
Volume
Totalizer
A
BV
15,531
15,534
15,646
15,650
15,750
15,751
15,882
15,885
15,996
16,005
16,050
16,131
16,248
16,281
16,368
16,401
16,503
16,504
16,614
16,617
16,717
16,738
16,756
16,854
16,893
16,978
17,088
17,132
17,206
17,262
17,323
17,391
17,396
17,518
17,542
17,557
17,670
17,768
17,818
17,878
17,955
17,992
18,067
18,147
18,184
18,194
18,294
18,318
18,419
18,433
18,544
18,596
18,667
18,670
18,782
18,783
18,896
18,937
19,034
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
110.1
110.5
102.5
104.5
102.3
106.4
86.6
96.5
98.1
95.5
92.7
95.7
84.5
87.8
88.6
101.6
99.9
101.1
110.4
108.1
107.9
103.3
106.0
106.7
107.0
94.7
92.9
99.1
93.8
89.1
88.0
97.8
74.1
86.7
99.9
71.3
85.5
85.0
85.5
93.2
NM
112.0
105.0
107.9
108.6
105.0
109.3
82.9
84.2
85.9
85.4
98.5
93.7
118.9
104.0
109.5
100.8
85.0
84.4
Daily Flow
Totalizer
B
aal
4,871
11,660
41,451
1,120
44,447
470
2,581
1,357
45,768
3,722
19,170
31,829
46,450
4,126
45,090
18,007
54,887
439
45,151
1,475
47,669
9,805
8,450
43,007
19,513
1,750
48,427
20,457
33,888
24,429
25,275
27,261
2,010
49,380
9,518
6,349
44,441
38,390
18,763
25,230
31,096
23,054
41,900
42,283
19,036
4,706
49,398
11,363
47,021
9,350
46,878
39,485
15,159
1,249
50,406
360
19,333
47,837
39,464
Cum. Flow
Totalizer
B
Kaal
8,952
8,964
9,005
9,006
9,051
9,051
9,107
9,109
9,154
9,158
9,177
9,209
9,255
9,268
9,314
9,332
9,386
9,387
9,442
9,443
9,491
9,501
9,509
9,552
9,572
9,610
9,658
9,679
9,712
9,737
9,762
9,789
9,791
9,841
9,850
9,857
9,901
9,939
9,958
9,983
10,015
10,038
10,079
10,122
10,141
10,146
10,195
10,206
10,253
10,263
10,310
10,349
10,364
10,365
10,416
10,416
10,436
10,483
10,523
Bed
Volume
Totalizer
B
BV
14,959
14,979
15,048
15,050
15,124
15,125
15,218
15,220
15,297
15,303
15,335
15,388
15,466
15,488
15,563
15,593
15,685
15,686
15,778
15,780
15,860
15,876
15,890
15,962
15,995
16,058
16,139
16,173
16,230
16,270
16,313
16,358
16,361
16,444
16,460
16,471
16,545
16,609
16,640
16,682
16,734
16,773
16,843
16,914
16,945
16,953
17,036
17,055
17,133
17,149
17,227
17,293
17,319
17,321
17,405
17,406
17,438
17,518
17,584
System Cum.
Volume
Treated
Kaal
18,246
18,260
18,369
18,372
18,476
18,478
18,612
18,615
18,727
18,736
18,782
18,862
18,979
19,012
19,109
19,146
19,263
19,264
19,385
19,388
19,495
19,518
19,537
19,638
19,682
19,770
19,884
19,931
20,009
20,067
20,129
20,197
20,202
20,324
20,348
20,364
20,476
20,573
20,621
20,683
20,759
20,805
20,892
20,982
21,023
21,033
21,143
21,168
21,276
21,294
21,407
21,477
21,536
21,538
21,656
21,657
21,744
21,816
21,914
System
Total Bed
Volumes
Treated"1
BV
15,245
15,257
15,347
15,350
15,437
15,438
15,550
15,553
15,646
15,654
15,693
15,759
15,857
15,884
15,966
15,997
16,094
16,095
16,196
16,199
16,288
16,307
16,323
16,408
16,444
16,518
16,613
16,653
16,718
16,766
16,818
16,874
16,879
16,981
17,001
17,014
17,107
17,189
17,229
17,280
17,345
17,382
17,455
17,530
17,565
17,573
17,665
17,686
17,776
17,791
17,886
17,945
17,993
17,995
18,094
18,094
18,167
18,228
18,309
Vessel AP
(psi)
A
5.2
5.5
5.8
5.6
6.0
6.2
7.1
7.1
7.5
7.5
7.6
9.0
9.0
9.2
2.2
3.0
3.1
3.1
3.8
4.0
4.5
4.4
4.5
5.0
5.2
5.8
6.0
6.0
5.2
6.9
6.9
7.2
7.2
8.0
8.8
7.8
9.0
9.2
9.2
8.1
NM
2.2
3.0
3.0
3.8
3.4
4.1
4.2
5.0
4.6
5.4
5.8
6.0
6.1
6.8
6.8
6.5
7.5
8.4
B
5.8
5.8
6.2
6.2
6.4
7.0
7.6
8.0
9.0
8.8
8.6
10.0
10.0
10.4
2.2
2.8
3.2
3.2
4.0
4.2
4.8
4.6
4.7
5.5
5.8
6.0
6.3
6.3
5.8
7.6
7.8
8.8
8.8
9.0
9.2
9.0
9.8
10.4
10.2
9.1
NM
2.2
2.9
3.1
4.0
3.6
4.6
4.6
5.4
5.2
6.0
6.2
6.6
6.3
7.4
7.4
7.0
8.4
9.2
System
AP
(psi)
psia
12
12
12
16
11
14
16
14
15
16
18
19
18
17
12
12
13
14
14
14
12
14
14
14
14
16
15
14
14
16
12
16
16
18
16
16
18
18
18
18
NA
12
12
12
14
12
9
9
14
14
14
12
16
14
16
16
15
17
18
System
Back-
wash
Yes/No
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
46
47
48
49
50
51
52
53
54
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
5/9/2005
5/10/2005
5/11/2005
5/12/2005
5/13/2005
5/14/2005
5/15/2005
5/1 6/2005
5/17/2005
5/18/2005
5/19/2005
5/20/2005
5/21/2005
5/22/2005
5/23/2005
5/24/2005
5/25/2005
5/26/2005
5/27/2005
5/28/2005
5/29/2005
5/30/2005
5/31/2005
6/1/2005
6/2/2005
6/3/2005
6/4/2005
6/5/2005
6/7/2005
6/8/2005
6/9/2005
6/10/2005
6/11/2005
6/13/2005
6/14/2005
6/15/2005
6/16/2005
6/17/2005
6/18/2005
6/1 9/2005
6/20/2005
6/21/2005
6/22/2005
6/23/2005
6/24/2005
6/25/2005
6/27/2005
6/28/2005
6/29/2005
6/30/2005
7/1/2005
7/2/2005
7/3/2005
7/4/2005
7/5/2005
7/6/2005
7/7/2005
7/8/2005
7/9/2005
7/1 0/2005
Time
09:05
05:45
09:35
10:30
08:35
16:25
19:15
09:30
08:45
06:45
13:15
08:35
17:00
17:30
08:30
08:00
NM
14:00
10:30
18:25
17:20
17:40
13:00
09:00
09:15
08:00
16:30
16:30
09:05
09:00
NM
05:47
16:50
15:15
09:15
15:45
12:05
08:45
16:45
18:40
08:40
05:45
08:30
09:15
09:30
18:30
09:00
14:15
14:15
09:45
15:55
23:20
16:50
16:30
09:55
09:45
09:45
12:10
17:20
16:30
Well House #1 Reading
Opt Hours
Well!
hr
7.8
3.2
11.2
3.4
8.9
8.7
10.4
0.2
8.9
0.3
9.9
7.0
3.2
10.3
0.1
9.2
1.3
7.8
2.0
8.9
5.5
6.4
9.5
0.1
10.2
4.0
5.9
9.8
9.1
0.2
10.3
2.0
9.4
11.7
2.0
13.7
8.2
12.0
14.5
7.9
4.8
11.2
12.4
4.9
11.4
19.8
13.9
6.9
7.6
12.0
15.5
17.7
2.8
13.7
15.6
3.4
8.0
6.0
6.0
9.2
Daily Flow
Totalizer
gal
1 1 1 ,000
44,000
156,000
45,000
128,000
126,000
148,000
3,000
127,000
3,000
142,000
100,000
44,000
144,000
2,000
128,000
19,000
110,000
27,000
123,000
80,000
88,000
131,000
2,000
146,000
57,000
84,000
138,000
128,000
3,000
143,000
29,000
130,000
156,000
27,000
188,000
115,000
163,000
198,000
109,000
66,000
156,000
180,000
65,000
160,000
279,000
192,000
97,000
102,000
165,000
211,000
244,000
39,000
188,000
214,000
50,000
111,000
86,000
82,000
132,000
Avg
Flowrate
gpm
237
229
232
221
240
241
237
250
238
167
239
238
229
233
333
232
244
235
225
230
242
229
230
333
239
238
237
235
234
250
231
242
230
222
225
229
234
226
228
230
229
232
242
221
234
235
230
234
224
229
227
230
232
229
229
245
231
239
228
239
APU
Electric
Meter
KWH
774.86
775.61
778.21
779.02
781.10
783.16
785.58
785.65
787.73
787.80
790.13
797.76
792.51
754.90
794.94
797.08
797.41
799.24
799.72
801.78
803.08
804.57
806.78
806.82
809.20
810.14
811.53
813.81
816.37
816.44
818.79
819.29
821.46
826.40
826.86
830.03
831.97
834.72
838.06
839.90
841.02
843.63
846.51
847.68
850.32
854.90
861.45
863.07
864.81
867.58
871.19
875.25
875.91
879.06
882.66
883.50
885.32
886.77
888.14
890.32
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
121.8
126.1
122.0
115.0
115.0
118.0
116.0
118.7
120.2
120.8
112.1
114.0
114.0
110.6
126.4
121.0
113.7
115.0
116.7
121.7
113.3
117.3
100.3
106.4
107.8
108.7
112.6
120.0
123.7
122.2
124.8
121.3
115.5
115.1
115.3
116.3
117.2
115.5
118.0
120.8
115.0
115.5
115.0
117.1
111.8
114.6
117.1
113.2
113.9
116.6
115.0
114.8
114.3
115.0
145.1
102.4
110.4
111.3
115.3
113.6
Daily Flow
Totalizer
A
gal
58,249
23,935
82,557
23,709
58,359
59,623
72,527
1,618
63,517
1,788
72,115
50,506
23,182
74,014
1,096
66,765
9,573
52,787
21,042
64,296
40,037
45,544
66,883
2,129
66,613
27,741
41,415
70,980
67,378
1,722
74,450
14,713
67,669
81,297
13,084
98,019
60,189
85,774
104,304
57,719
34,507
81,980
79,859
33,035
77,040
138,654
98,307
47,728
51,534
83,047
112,226
127,285
19,948
96,898
161,205
926
19,561
41,231
38,071
58,780
Cum.
Flow
Totalizer
A
Kgal
11,449
11,473
11,556
11,579
11,638
11,697
11,770
11,771
11,835
11,837
11,909
11,959
11,982
12,057
12,058
12,124
12,134
12,187
12,208
12,272
12,312
12,358
12,425
12,427
12,493
12,521
12,562
12,633
12,714
12,716
12,790
12,805
12,873
13,027
13,040
13,138
13,198
13,284
13,389
13,446
13,481
13,563
13,643
13,676
13,753
13,891
14,092
14,139
14,191
14,274
14,386
14,513
14,533
14,630
14,791
14,792
14,812
14,853
14,891
14,950
Bed
Volume
Totalizer
A
BV
19,131
19,171
19,309
19,349
19,447
19,546
19,667
19,670
19,776
19,779
19,900
19,984
20,023
20,147
20,148
20,260
20,276
20,364
20,399
20,507
20,574
20,650
20,762
20,765
20,876
20,923
20,992
21,111
21,246
21,248
21,373
21,397
21,511
21,769
21,790
21,954
22,055
22,198
22,372
22,469
22,526
22,663
22,797
22,852
22,981
23,213
23,547
23,627
23,713
23,852
24,039
24,252
24,285
24,447
24,717
24,718
24,751
24,820
24,883
24,982
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
92.7
101.1
100.0
109.0
108.0
110.0
95.7
101.5
112.0
100.6
101.9
109.0
102.8
101.7
103.1
100.0
82.6
80.0
83.7
85.4
94.9
100.1
95.8
105.5
107.4
102.4
106.9
95.0
95.8
96.6
99.0
95.8
99.0
85.2
90.0
90.8
84.8
85.5
94.9
84.5
85.5
87.0
100.0
103.2
109.3
109.0
91.6
86.7
87.4
92.0
81.5
81.5
NM
97.6
67.2
98.1
92.5
92.7
111.6
109.0
Daily Flow
Totalizer
B
gal
39,670
15,515
54,538
17,725
54,908
52,331
59,017
1,295
48,605
1,461
52,975
37,176
16,495
53,770
842
46,593
6,807
39,164
10,510
42,622
28,863
33,177
49,196
2,061
60,980
23,270
33,000
52,400
46,551
1,254
51,529
11,234
47,760
58,263
9,696
68,660
41,161
58,457
71,079
39,826
23,924
56,791
75,500
29,496
64,843
108,773
71,048
36,769
38,867
60,714
76,348
88,825
14,088
68,924
77,113
23,469
46,729
35,639
31,721
51,112
Cum. Flow
Totalizer
B
Kgal
10,562
10,578
10,633
10,650
10,705
10,758
10,817
10,818
10,866
10,868
10,921
10,958
10,975
11,028
11,029
11,076
11,083
11,122
11,132
11,175
11,204
11,237
11,286
11,288
11,349
11,372
11,405
11,458
11,514
11,515
11,567
11,578
11,626
11,735
11,745
11,814
11,855
11,913
11,985
12,024
12,048
12,105
12,181
12,210
12,275
12,384
12,527
12,564
12,603
12,664
12,740
12,829
12,843
12,912
12,989
13,012
13,059
13,095
13,126
13,178
Bed
Volume
Totalizer
B
BV
17,650
17,676
17,767
17,797
17,888
17,976
18,075
18,077
18,158
18,160
18,249
18,311
18,339
18,428
18,430
18,508
18,519
18,584
18,602
18,673
18,722
18,777
18,859
18,863
18,964
19,003
19,059
19,146
19,240
19,242
19,328
19,347
19,427
19,610
19,626
19,741
19,810
19,907
20,026
20,093
20,133
20,228
20,354
20,403
20,511
20,693
20,933
20,995
21,060
21,161
21,289
21,437
21,461
21,576
21,705
21,744
21,822
21,881
21,934
22,020
System Cum.
Volume
Treated
Kgal
22,012
22,051
22,188
22,230
22,343
22,455
22,586
22,589
22,701
22,705
22,830
22,917
22,957
23,085
23,087
23,200
23,216
23,308
23,340
23,447
23,516
23,595
23,711
23,715
23,842
23,893
23,968
24,091
24,228
24,231
24,357
24,383
24,499
24,763
24,785
24,952
25,053
25,198
25,373
25,471
25,529
25,668
25,823
25,886
26,028
26,275
26,619
26,703
26,794
26,938
27,126
27,342
27,376
27,542
27,780
27,805
27,871
27,948
28,018
28,128
System
Total Bed
Volumes
Treated1"
BV
18,391
18,424
18,538
18,573
18,668
18,761
18,871
18,873
18,967
18,970
19,074
19,148
19,181
19,287
19,289
19,384
19,397
19,474
19,501
19,590
19,648
19,713
19,810
19,814
19,920
19,963
20,025
20,128
20,243
20,245
20,351
20,372
20,469
20,689
20,708
20,848
20,932
21,053
21,199
21,281
21,330
21,446
21,575
21,628
21,746
21,953
22,240
22,311
22,386
22,506
22,664
22,845
22,873
23,012
23,211
23,231
23,286
23,351
23,409
23,501
Vessel AP
(psi)
A
9.0
9.2
9.4
2.4
3.0
3.8
4.2
4.5
5.0
5.0
5.8
5.8
6.2
7.0
7.0
8.1
8.1
8.6
9.1
9.9
9.1
8.0
2.5
2.4
2.4
3.0
3.4
4.8
5.8
5.9
6.2
6.2
7.0
9.0
9.0
10.0
10.0
10.1
10.2
9.2
10.6
10.6
2.6
3.2
4.2
5.8
8.0
8.3
9.2
10.0
10.0
9.0
9.0
9.0
4.1
2.3
3.2
3.6
3.5
5.0
B
10.0
9.6
9.8
2.2
3.0
3.8
4.6
5.0
5.8
5.8
6.0
6.2
7.0
8.0
8.0
9.0
9.0
9.6
9.8
10.6
9.0
9.0
2.5
2.3
2.3
3.8
3.7
5.4
6.2
6.0
7.0
7.0
8.0
9.6
9.6
10.6
10.8
11.2
11.2
10.2
11.0
11.0
2.8
3.8
5.0
6.4
9.0
9.3
9.8
11.0
11.0
9.6
9.6
10.0
6.0
2.2
3.4
3.9
4.4
5.3
System
AP
(psi)
psig
20
19
18
10
12
12
14
12
12
14
16
14
16
16
12
20
18
18
18
19
18
18
10
11
12
13
15
14
15
15
14
16
18
17
20
19
19
20
18
19
18
18
12
14
14
16
26
18
18
18
18
17
18
18
14
11
12
13
12
16
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
55
56
57
58
59
60
61
62
63
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
7/1 1/2005
7/12/2005
7/13/2005
7/14/2005
7/15/2005
7/16/2005
7/1 7/2005
7/18/2005
7/19/2005
7/20/2005
7/21/2005
7/22/2005
7/23/2005
7/24/2005
7/25/2005
7/26/2005
7/27/2005
7/28/2005
7/29/2005
7/30/2005
7/31/2005
8/1/2005
8/2/2005
8/3/2005
8/4/2005
8/5/2005
8/6/2005
8/7/2005
8/8/2005
8/9/2005
8/10/2005
8/11/2005
8/12/2005
8/13/2005
8/14/2005
8/15/2005
8/16/2005
8/17/2005
8/18/2005
8/19/2005
8/20/2005
8/21/2005
8/22/2005
8/23/2005
8/24/2005
8/25/2005
8/26/2005
8/27/2005
8/28/2005
8/29/2005
8/30/2005
8/31/2005
9/1/2005
9/2/2005
9/3/2005
9/4/2005
9/5/2005
9/6/2005™
9/7/2005
9/8/2005
9/9/2005
9/10/2005(B)
9/11/2005'='
Time
09:55
09:30
09:45
09:00
13:00
16:30
17:10
10:20
08:24
09:00
12:32
08:30
04:30
17:00
09:38
08:12
09:40
06:05
06:40
15:30
23:30
11:00
16:00
07:15
01:30
10:00
17:20
20:15
08:09
08:47
08:46
08:33
06:35
17:45
16:40
08:34
08:31
09:05
06:50
10:00
17:40
16:34
08:45
08:45
09:45
08:56
08:40
NM
17:00
09:00
09:30
08:47
09:00
06:30
16:35
20:15
17:30
09:00
09:00
09:21
09:03
23:45
16:45
Well House #1 Reading
Opt Hours
Well!
hr
6.3
7.6
10.5
9.9
4.4
6.3
9.4
8.0
5.0
13.4
14.4
13.2
15.9
7.5
10.5
6.8
8.5
9.8
10.0
5.7
8.1
8.3
3.5
10.9
4.9
20.2
5.9
5.2
3.2
7.3
2.6
7.9
4.5
8.2
9.3
5.6
6.2
11.3
2.5
10.1
9.5
2.1
9.9
1.5
10.7
11.8
1.4
13.0
8.2
2.3
10.3
1.6
10.1
9.9
12.3
16.0
0.0
14.4
6.9
6.0
11.4
23.4
3.6
Daily Flow
Totalizer
qal
89,000
106,000
145,000
137,000
61,000
86,000
130,000
112,000
65,000
182,000
204,000
185,000
221,000
105,000
142,000
95,000
117,000
131,000
140,000
73,000
111,000
113,000
48,000
148,000
68,000
285,000
83,000
70,000
46,000
100,000
35,000
108,000
63,000
111,000
129,000
77,000
85,000
158,000
35,000
142,000
131,000
30,000
137,000
20,000
147,000
162,000
19,000
176,000
105,000
38,000
142,000
24,000
140,700
136,300
169,000
217,000
0
196,000
95,000
80,000
155,000
315,000
47,000
Avg
Flowrate
qpm
235
232
230
231
231
228
230
233
217
226
236
234
232
233
226
232
229
223
233
213
228
227
229
226
231
235
234
224
240
228
224
228
233
226
231
229
228
233
233
234
230
238
231
222
229
229
226
226
213
275
230
250
232
229
229
226
NA
227
229
222
227
224
218
APU
Electric
Meter
KWH
891.77
893.54
895.96
898.26
899.29
900.74
902.93
904.81
905.93
909.03
912.37
915.44
919.11
920.56
923.25
924.85
926.82
929.07
931.31
932.70
934.60
936.50
937.32
939.84
941.04
945.73
947.10
948.29
949.85
950.74
951.34
953.18
954.24
956.11
958.28
959.56
961.02
963.63
964.23
966.58
968.77
969.28
971.56
971.91
974.40
977.14
977.47
980.46
982.36
982.90
985.29
985.68
988.01
990.31
993.17
NM
697.93
0.19
1.80
3.18
5.81
11.23
12.06
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
qpm
112.0
113.3
110.9
113.0
110.9
115.6
119.1
115.7
115.0
112.0
113.6
111.8
112.5
116.0
104.1
102.8
103.2
110.2
110.5
NA
NA
118.6
108.6
105.5
107.0
100.0
97.0
104.6
111.1
114.1
111.6
121.6
103.2
105.0
106.2
109.0
111.6
100.1
114.2
103.8
100.8
104.9
110.2
113.5
116.8
111.2
112.6
115.5
110.0
112.5
109.5
109.5
111.1
108.7
107.7
100.0
99.0
103.3
106.4
109.6
102.2
NA
NA
Daily Flow
Totalizer
A
qal
47,991
51,811
70,387
66,307
29,464
42,308
64,062
55,935
32,729
93,010
83,036
89,979
103,465
48,282
66,035
42,807
53,273
60,708
64,824
NA
NA
26,542
22,984
71,505
30,382
122,108
42,160
32,162
20,380
45,856
15,945
49,528
27,935
50,101
57,249
33,843
38,056
69,707
16,748
63,942
60,897
14,027
63,942
9,458
69,314
76,801
8,865
83,860
53,304
15,238
62,618
10,038
60,984
60,142
73,519
93,151
76,630
8,614
41,389
35,177
68,299
277,863
41,292
Cum.
Flow
Totalizer
A
Kqal
14,998
15,050
15,120
15,187
15,216
15,258
15,322
15,378
15,411
15,504
15,587
15,677
15,781
15,829
15,895
15,938
15,991
16,052
16,116
NA
NA
16,143
16,166
16,237
16,268
16,390
16,432
16,464
16,485
16,531
16,546
16,596
16,624
16,674
16,731
16,765
16,803
16,873
16,890
16,954
17,014
17,028
17,092
17,102
17,171
17,248
17,257
17,341
17,394
17,409
17,472
17,482
17,543
17,603
17,677
17,770
17,846
17,855
17,896
17,932
18,000
18,278
18,319
Bed
Volume
Totalizer
A
BV
25,062
25,148
25,266
25,377
25,426
25,497
25,604
25,697
25,752
25,907
26,046
26,197
26,369
26,450
26,560
26,632
26,721
26,822
26,931
NA
NA
26,975
27,013
27,133
27,184
27,388
27,458
27,512
27,546
27,623
27,649
27,732
27,779
27,862
27,958
28,015
28,078
28,195
28,223
28,330
28,431
28,455
28,562
28,577
28,693
28,822
28,836
28,977
29,066
29,091
29,196
29,212
29,314
29,415
29,538
29,693
29,821
29,836
29,905
29,964
30,078
30,542
30,611
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
89.6
86.8
93.6
92.9
94.5
104.6
101.3
74.2
90.0
84.0
89.1
95.5
97.2
110.8
102.2
100.1
91.1
100.6
100.0
NA
NA
74.4
84.6
85.0
97.7
99.0
93.0
96.6
83.3
107.9
87.4
86.0
95.8
99.5
98.3
94.5
100.1
98.1
100.5
97.9
90.6
94.4
103.4
108.4
108.9
84.9
103.1
87.2
89.1
90.2
101.0
115.2
110.3
113.3
118.0
105.0
100.0
99.9
101.2
105.6
105.7
0.0
0.0
Daily Flow
Totalizer
B
qal
34,178
40,283
55,371
53,209
23,539
31,964
48,541
41,439
23,769
67,530
89,154
75,384
87,779
42,609
57,073
39,813
47,693
53,145
54,720
NA
NA
22,862
18,358
56,590
29,314
121,016
34,010
29,681
18,299
41,204
14,900
44,334
25,760
47,529
55,199
32,771
36,898
67,768
15,739
58,222
52,895
1 1 ,963
54,509
7,956
59,208
63,506
7,401
69,824
44,174
12,168
61,825
16,803
53,110
59,256
72,574
92,694
26,183
57,958
40,380
34,431
65,654
5,708
0
Cum. Flow
Totalizer
B
Kqal
13,212
13,252
13,307
13,361
13,384
13,416
13,465
13,506
13,530
13,597
13,687
13,762
13,850
13,892
13,949
13,989
14,037
14,090
14,145
NA
NA
14,168
14,186
14,243
14,272
14,393
14,427
14,457
14,475
14,516
14,531
14,575
14,601
14,649
14,704
14,737
14,774
14,841
14,857
14,915
14,968
14,980
15,035
15,043
15,102
15,165
15,173
15,243
15,287
15,299
15,361
15,377
15,431
15,490
15,562
15,655
15,681
15,739
15,780
15,814
15,880
15,885
15,885
Bed
Volume
Totalizer
B
BV
22,077
22,144
22,237
22,326
22,365
22,419
22,500
22,569
22,609
22,721
22,870
22,996
23,143
23,214
23,310
23,376
23,456
23,545
23,636
NA
NA
23,674
23,705
23,800
23,849
24,051
24,108
24,157
24,188
24,257
24,281
24,356
24,399
24,478
24,570
24,625
24,687
24,800
24,826
24,924
25,012
25,032
25,123
25,136
25,235
25,341
25,354
25,470
25,544
25,565
25,668
25,696
25,785
25,884
26,005
26,160
26,204
26,300
26,368
26,425
26,535
26,545
26,545
System Cum.
Volume
Treated
Kqal
28,210
28,302
28,428
28,547
28,600
28,674
28,787
28,884
28,941
29,101
29,274
29,439
29,630
29,721
29,844
29,927
30,028
30,142
30,261
NA
NA
30,311
30,352
30,480
30,540
30,783
30,859
30,921
30,960
31,047
31,077
31,171
31,225
31,323
31,435
31,502
31,577
31,714
31,747
31,869
31,983
32,009
32,127
32,144
32,273
32,413
32,430
32,583
32,681
32,708
32,833
32,859
32,973
33,093
33,239
33,425
33,528
33,594
33,676
33,746
33,880
34,163
34,204
System
Total Bed
Volumes
Treated'"
BV
23,569
23,646
23,751
23,851
23,896
23,958
24,052
24,133
24,180
24,314
24,458
24,596
24,756
24,832
24,935
25,004
25,088
25,184
25,283
NA
NA
25,325
25,359
25,466
25,516
25,719
25,783
25,835
25,867
25,940
25,965
26,044
26,089
26,170
26,264
26,320
26,382
26,497
26,524
26,627
26,722
26,743
26,842
26,857
26,964
27,081
27,095
27,223
27,305
27,328
27,432
27,454
27,550
27,649
27,771
27,927
28,013
28,068
28,136
28,195
28,307
28,543
28,578
Vessel AP
(psi)
A
5.2
6.0
7.0
8.1
8.0
9.0
9.5
9.7
9.9
10.2
3.2
4.4
6.0
7.0
8.2
8.8
9.6
9.5
9.7
1.0
0.8
1.0
•1.2
0.6
3.0
4.2
6.0
7.0
7.6
8.9
8.8
9.6
10.0
8.8
8.3
8.2
8.8
3.0
4.0
5.2
6.0
6.2
7.9
8.0
9.0
10.2
10.2
10.6
10.6
11.4
3.8
4.2
6.2
7.6
9.2
10.1
11.8
10.4
11.4
11.0
11.0
8.0
8.0
B
6.0
6.6
7.4
8.9
9.1
9.5
10.0
11.1
11.0
11.5
4.0
4.9
6.5
7.9
8.0
9.2
10.2
10.0
10.5
12.0
11.4
11.2
11.2
11.3
2.8
4.6
6.2
7.0
8.0
8.7
9.4
9.8
10.8
9.0
9.0
8.8
8.8
3.1
4.1
5.6
6.7
7.0
7.9
8.5
9.2
11.2
10.8
12.0
11.8
12.6
3.8
4.2
6.0
7.8
9.3
10.4
12.0
10.6
11.9
11.6
11.2
0.0
0.0
System
ip
(psi)
PSiq
16
16
16
17
18
19
20
20
20
20
12
16
17
19
16
18
18
18
19
20
20
18
14
19
13
16
17
15
18
16
16
17
20
18
16
2
16
12
15
17
17
18
17
19
19
2
10
10
20
23
16
NA
6
18
22
20
20
22
22
20
20
22
22
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
64
65
66
67
68
69
70
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
9/12/2005
9/13/2005
9/14/2005
9/15/2005
9/16/2005
9/17/2005
9/18/2005
9/19/2005
9/20/2005
9/21/2005
9/22/2005
9/23/2005
9/24/2005
9/25/2005
9/26/2005
9/27/2005
9/28/2005
9/29/2005
9/30/2005
10/1/2005
10/2/2005
10/3/2005
10/4/2005
10/5/2005
10/6/2005
10/7/2005
10/8/2005
10/9/2005
10/10/2005
10/11/2005
10/12/2005
10/13/2005
10/14/2005
10/15/2005
10/16/2005
10/17/2005
10/18/2005
10/19/2005
10/20/2005
10/21/2005
10/22/2005
10/23/2005
10/24/2005
10/25/2005
10/26/2005
10/27/2005
10/28/2005
10/29/2005
10/30/2005
Time
09:00
09:20
09:40
09:00
09:10
05:00
04:45
09:00
09:10
08:30
09:10
13:15
13:30
NM
09:15
09:15
08:55
09:05
08:55
17:00
16:33
11:00
09:20
09:40
09:00
11:30
12:10
17:00
17:00
11:00
09:40
09:15
15:20
16:54
16:20
07:30
08:50
08:52
09:40
13:30
19:13
17:05
13:25
13:00
09:15
09:03
09:45
16:45
16:50
Well House #1 Reading
Opt Hours
Well!
hr
0.2
19.1
11.7
1.0
10.3
13.3
4.4
10.9
15.1
2.9
9.2
7.3
17.4
NA
15.3
11.5
13.8
6.8
7.8
15.3
10.1
13.6
6.0
8.1
13.5
0.3
10.7
6.9
4.8
5.2
6.5
2.2
11.7
3.8
6.5
1.4
9.8
10.1
1.4
11.2
6.6
3.6
1.1
9.2
0.1
8.9
NA
9.8
4.0
Daily Flow
Totalizer
gal
3,000
269,000
161,000
14,000
139,000
185,000
60,000
147,000
205,000
39,000
123,000
102,000
244,000
NA
212,000
158,000
189,000
94,000
106,000
211,000
138,000
189,000
83,000
112,000
183,000
5,000
143,000
95,000
65,000
70,000
91,000
31,000
163,000
53,000
90,000
20,000
134,000
138,000
22,000
149,000
91,000
49,000
14,000
130,000
2,000
124,000
NA
137,000
56,000
Avg
Flowrate
gpm
250
235
229
233
225
232
227
225
226
224
223
233
234
NA
231
229
228
230
226
230
228
232
231
230
226
278
223
229
226
224
233
235
232
232
231
238
228
228
262
222
230
227
212
236
333
232
NA
233
233
APU
Electric
Meter
KWH
12.16
16.57
19.27
19.51
21.91
24.98
26.00
28.52
32.00
32.67
34.79
36.50
40.53
NM
44.10
46.76
49.97
51.55
53.35
56.90
59.22
62.40
63.79
65.67
68.79
68.89
71.35
72.95
73.91
75.27
76.78
77.32
80.03
80.96
82.45
82.77
85.04
87.38
87.73
90.33
91.87
92.27
92.98
95.13
95.17
97.22
97.30
99.52
100.46
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
101.9
102.5
109.7
113.0
111.7
111.9
113.5
94.4
102.2
98.4
99.9
92.7
97.6
NM
99.6
91.4
96.2
90.7
100.3
104.3
107.7
95.5
99.2
91.5
93.5
94.4
88.7
88.0
85.0
92.4
94.1
95.2
84.2
84.2
84.0
92.6
98.6
89.9
88.0
85.6
88.6
89.1
95.4
90.0
87.8
90.9
91.0
95.6
90.1
Daily Flow
Totalizer
A
gal
2,458
110,547
70,416
37,345
32,613
81,840
26,559
65,159
89,768
17,370
55,167
45,442
97,901
NA
87,378
64,543
76,724
37,279
42,300
85,146
55,700
77,231
33,764
45,167
76,225
2,937
61,532
37,695
27,130
28,589
33,658
11,884
62,056
19,999
32,094
7,047
49,349
51,084
7,250
57,571
34,344
18,353
5,101
44,191
420
43,199
4,527
43,962
21,003
Cum.
Flow
Totalizer
A
Kgal
18,321
18,432
18,502
18,540
18,572
18,654
18,681
18,746
18,836
18,853
18,908
18,954
19,052
NA
19,139
19,203
19,280
19,317
19,360
19,445
19,501
19,578
19,612
19,657
19,733
19,736
19,797
19,835
19,862
19,891
19,925
19,936
19,999
20,019
20,051
20,058
20,107
20,158
20,165
20,223
20,257
20,276
20,281
20,325
20,325
20,369
20,373
20,417
20,438
Bed
Volume
Totalizer
A
BV
30,615
30,800
30,918
30,980
31,035
31,171
31,216
31,325
31,475
31,504
31,596
31,672
31,835
NA
31,981
32,089
32,217
32,280
32,350
32,493
32,586
32,715
32,771
32,847
32,974
32,979
33,082
33,145
33,190
33,238
33,294
33,314
33,418
33,451
33,505
33,517
33,599
33,684
33,696
33,793
33,850
33,881
33,889
33,963
33,964
34,036
34,044
34,117
34,152
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
102.8
106.9
108.6
109.2
104.2
100.6
106.2
99.1
100.5
94.9
95.5
90.0
99.0
NM
94.6
94.2
86.5
89.0
94.7
101.1
103.6
94.7
95.2
88.2
86.8
87.2
87.1
86.0
83.0
97.3
97.4
110.0
95.7
100.4
98.0
94.1
97.6
96.0
94.0
82.1
97.6
101.6
110. .9
100.0
105.6
109.6
107.4
106.4
112.6
Daily Flow
Totalizer
B
gal
2,826
118,130
66,639
6,844
54,804
71,217
54,656
27,930
88,306
7,806
46,266
40,302
103,142
NA
86,122
61,630
72,219
36,425
41,438
83,295
54,367
74,691
32,636
43,545
68,867
2,652
54,418
33,746
24,287
28,355
38,600
13,403
69,070
22,474
36,227
7,860
54,865
54,390
7,676
58,603
34,250
18,573
6,114
56,210
553
52,251
1,778
54,891
22,870
Cum. Flow
Totalizer
B
Kgal
15,888
16,006
16,073
16,080
16,135
16,206
16,261
16,288
16,377
16,385
16,431
16,471
16,574
#VALUE!
16,660
16,722
16,794
16,831
16,872
16,955
17,010
17,084
17,117
17,161
17,230
17,232
17,287
17,320
17,345
17,373
17,412
17,425
17,494
17,517
17,553
17,561
17,615
17,670
17,678
17,736
17,770
17,789
17,795
17,851
17,852
17,904
17,906
17,961
17,984
Bed
Volume
Totalizer
B
BV
26,549
26,747
26,858
26,870
26,961
27,080
27,172
27,218
27,366
27,379
27,456
27,523
27,696
NA
27,840
27,943
28,063
28,124
28,194
28,333
28,424
28,548
28,603
28,676
28,791
28,795
28,886
28,942
28,983
29,030
29,095
29,117
29,233
29,270
29,331
29,344
29,436
29,527
29,539
29,637
29,695
29,726
29,736
29,830
29,831
29,918
29,921
30,013
30,051
System Cum.
Volume
Treated
Kgal
34,210
34,438
34,575
34,620
34,707
34,860
34,941
35,034
35,212
35,238
35,339
35,425
35,626
NA
35,799
35,926
36,074
36,148
36,232
36,400
36,510
36,662
36,729
36,817
36,963
36,968
37,084
37,156
37,207
37,264
37,336
37,361
37,493
37,535
37,603
37,618
37,722
37,828
37,843
37,959
38,028
38,065
38,076
38,176
38,177
38,273
38,279
38,378
38,422
System
Total Bed
Volumes
Treated1"
BV
28,582
28,773
28,888
28,925
28,998
29,126
29,194
29,271
29,420
29,441
29,526
29,598
29,766
#VALUE!
29,911
30,016
30,140
30,202
30,272
30,413
30,505
30,632
30,687
30,761
30,882
30,887
30,984
31,044
31,087
31,134
31,195
31,216
31,325
31,361
31,418
31,430
31,517
31,605
31,618
31,715
31,772
31,803
31,813
31,896
31,897
31,977
31,982
32,065
32,101
Vessel AP
(psi)
A
2.9
5.8
6.1
7.0
7.0
9.3
9.3
10.4
10.2
11.6
11.0
2.2
4.5
NM
6.3
7.8
9.0
7.6
7.8
6.5
7.2
6.7
6.6
7.0
11.2
10.8
11.0
11.0
11.0
2.6
3.2
3.8
5.5
5.8
7.2
6.5
8.7
9.8
10.0
10.3
9.6
9.4
2.4
2.5
3.7
5.0
5.0
6.2
6.3
B
2.4
5.9
7.5
7.5
8.5
10.5
10.5
10.5
10.9
13.0
11.8
2.2
5.0
NM
6.7
8.2
9.6
8.3
8.1
7.1
7.3
7.2
7.0
7.2
11.8
11.6
12.0
12.0
11.4
2.2
3.4
4.0
5.6
6.0
6.9
7.5
9.2
11.0
11.4
11.6
10.2
10.2
2.3
3.1
3.8
5.2
5.2
6.9
7.0
System
AP
(psi)
psig
13
17
16
19
18
20
23
20
18
23
20
1
16
NA
18
18
20
18
19
16
18
17
17
17
22
22
32
20
20
14
15
14
16
17
16
17
18
20
18
21
19
20
12
12
15
15
16
18
20
System
Back-
wash
Yes/No
Yes
Yes
Yes
>
oo
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
71
72
73
74
75
76
77
78
79
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
10/31/2005
11/1/2005
11/2/2005
11/3/2005
11/4/2005
11/5/2005
11/6/2005
11/7/2005
11/8/2005
11/9/2005
11/10/2005
11/11/2005
11/12/2005
11/13/2005
11/14/2005
11/15/2005
11/16/2005
11/17/2005
11/18/2005
11/19/2005
11/20/2005
11/21/2005
11/22/2005
11/23/2005
11/24/2005
11/25/2005
11/26/2005
11/27/2005
11/28/2005
11/29/2005
11/30/2005
12/1/2005
12/2/2005
12/3/2005
12/4/2005
12/5/2005
12/6/2005
12/7/2005
12/8/2005
12/9/2005
12/10/2005
12/11/2005
12/12/2005
12/13/2005™
12/14/2005
12/15/2005
12/16/2005
12/17/2005
12/18/2005
12/19/2005
12/20/2005
12/21/2005
12/22/2005
12/23/2005
12/24/2005
12/25/2005
12/26/2005
12/27/2005
12/28/2005
12/29/2005
12/30/2005
12/31/2005
1/1/2006
Time
08:50
10:00
07:00
Well House #1 Reading
Opt Hours
Well 1
hr
6.3
0.1
10.0
Daily Flow
Totalizer
gal
87,000
2,000
136,000
Avg
Flowrate
gpm
230
333
227
APU
Electric
Meter
KWH
NM
101.96
104.27
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vese
A
gpm
90.4
90.8
89.2
Daily Flow
Totalizer
A
gal
29,920
401
48,343
Cum.
Flow
Totalizer
A
Kgal
20,468
20,468
20,517
Bed
Volume
Totalizer
A
BV
34,202
34,203
34,284
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vesse
B
gpm
103.2
105.1
105.7
Daily Flow
Totalizer
B
gal
35,348
447
54,430
Cum. Flow
Totalizer
B
Kgal
18,019
18,019
18,074
Bed
Volume
Totalizer
B
BV
30,110
30,111
30,202
System Cum.
Volume
Treated
Kgal
38,487
38,488
38,591
System
Total Bed
Volumes
Treated1"1
BV
32,156
32,157
32,243
Vessel AP
(psi)
A
8.0
8.0
9.4
Plant Switched Off Due to Drilling of New Well in Wellhouse No. 1 .
11:30
09:00
06:30
10:20
16:30
16:30
13:30
06:45
03:30
14:20
06:30
16:30
16:45
16:40
09:40
15:00
11:10
06:45
23:20
16:30
0.4
1.7
8.8
1.0
9.6
0.1
7.0
2.9
0.3
9.2
0.1
9.7
4.7
5.8
0.3
10.0
1.1
8.4
5.4
3.8
6,000
23,000
122,000
13,000
136,000
1,000
98,000
42,000
3,000
128,000
1,000
135,000
66,000
78,000
5,000
138,000
15,000
119,000
77,000
51 ,000
250
225
231
217
236
167
233
241
167
232
167
232
234
224
278
230
227
236
238
224
103.39
108.90
110.98
11.28
113.55
113.60
115.00
115.97
116.67
118.25
118.28
120.59
121.71
123.06
123.18
125.55
125.81
127.78
129.09
129.98
91.0
94.1
98.7
90.9
79.1
87.9
80.0
82.4
84.0
93.5
90.1
91.8
76.6
80.5
92.8
80.5
80.1
81.2
78.5
75.0
2,204
8,604
42,774
24,411
24,305
235
32,275
13,356
1,041
41,314
317
41,175
22,453
24,334
1,744
43,286
10,991
30,656
22,356
16,817
20,519
20,527
20,570
20,595
20,619
20,619
20,651
20,665
20,666
20,707
20,708
20,749
20,771
20,795
20,797
20,840
20,851
20,882
20,904
20,921
34,287
34,302
34,373
34,414
34,455
34,455
34,509
34,531
34,533
34,602
34,602
34,671
34,709
34,749
34,752
34,825
34,843
34,894
34,932
34,960
105.6
104.8
102.7
108.8
96.7
102.1
100.0
106.9
107.4
108.2
111.5
118.0
96.5
99.6
99.0
98.5
97.0
107.0
100.9
100.0
2,452
10,714
46,954
25,761
38,803
280
42,615
17,783
1,424
54,889
436
57,774
27,550
33,109
2,302
58,744
6,547
51,254
31,287
22,994
18,076
18,087
18,134
18,160
18,199
18,199
18,241
18,259
18,261
18,316
18,316
18,374
18,401
18,434
18,437
18,495
18,502
18,553
18,585
18,608
30,206
30,224
30,302
30,345
30,410
30,410
30,482
30,511
30,514
30,605
30,606
30,703
30,749
30,804
30,808
30,906
30,917
31 ,003
31,055
31,093
NA
38,615
38,704
38,754
38,818
38,818
38,893
38,924
38,927
39,023
39,023
39,122
39,172
39,230
39,234
39,336
39,353
39,435
39,489
39,529
NA
32,263
32,338
32,380
32,432
32,433
32,495
32,521
32,523
32,604
32,604
32,687
32,729
32,777
32,780
32,865
32,880
32,948
32,993
33,027
9.0
9.0
8.0
3.0
4.0
4.0
4.6
5.4
5.6
7.0
7.1
9.0
9.2
10.4
10.0
8.2
3.0
3.5
3.7
4.8
B
8.2
8.1
9.8
System
iP
(psi)
psig
18
20
20
System
Back-
wash
Yes/No
9.1
9.5
8.6
2.2
4.0
4.2
4.8
5.6
5.8
7.4
7.5
9.1
9.7
10.4
10.0
8.4
2.8
3.8
4.1
5.0
30
21
16
14
14
14
16
16
19
17
19
19
20
20
20
19
14
15
15
10
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
o
Week
No.
80
81
82
83
84
85
86
87
88
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
1/2/2006
1/3/2006
1/4/2006
1/5/2006
1/6/2006
1/7/2006
1/8/2006
1/9/2006
1/10/2006
1/11/2006
1/12/2006
1/13/20061"'
1/14/2006
1/15/2006
1/16/2006
1/17/2006
1/18/2006
1/19/2006
1/20/2006
1/21/2006
1/22/2006
1/23/2006
1/24/2006
1/25/2006
1/26/2006
1/27/2006
1/28/2006
1/29/2006
1/30/2006
1/31/2006
2/1/2006
2/2/2006
2/3/2006
2/42006
2/5/2006
2/6/2006
2/7/2006
2/8/2006
2/9/2006
2/10/2006
2/11/2006
2/12/2006
2/1 3/2006
2/14/2006
2/15/2006
2/16/2006
2/17/2006
2/18/2006
2/19/2006
2/20/2006
2/21/2006
2/22/2006
2/23/2006
2/24/2006
2/25/2006
2/26/2006
2/27/2006
2/28/2006
3/1/2006
3/2/2006
3/3/2006
3/4/2006
3/5/2006
Time
16:20
09:15
09:10
09:55
09:39
18:10
16:40
10:00
07:10
10:00
13:00
09:05
17:15
17:00
17:00
09:20
09:02
10:15
09:00
16:45
17:30
09:20
11:00
08:40
09:35
10:00
17:30
16:30
11:15
09:10
09:10
09:05
09:30
16:25
16:30
09:00
06:15
11:00
09:00
14:20
17:00
16:20
09:00
09:06
09:20
09:10
9:20
16:25
16:45
16:30
10:55
09:45
12:45
11:10
15:30
16:30
09:10
08:55
08:45
09:30
11:30
17:05
16:30
Well House #1 Reading
Opt Hours
Well!
hr
0.2
8.6
1.1
2.3
7.4
4.4
5.8
0.1
9.4
0.1
8.2
2.3
5.4
4.3
0.9
8.3
0.1
8.9
0.1
7.7
2.5
0.0
10.2
0.0
7.6
1.7
7.4
2.5
0.7
9.1
0.3
6.4
3.5
6.0
4.1
0.1
9.5
1.9
1.0
8.2
1.1
8.1
0.0
8.5
0.2
2.1
7.3
1.7
7.9
0.1
9.4
0.1
6.6
3.8
2.1
7.0
0.1
8.7
0.2
6.4
2.5
6.3
4.0
Daily Flow
Totalizer
gal
3,000
122,000
15,000
41,000
95,000
62,000
79,000
1,000
129,000
1,000
113,000
34,000
77,000
59,000
13,000
116,000
2,000
124,000
1,000
108,000
33,000
1,000
140,000
0
108,000
23,000
106,000
34,000
10,000
128,000
4,000
89,000
48,000
83,000
56,000
1,000
130,000
26,000
15,000
116,000
15,000
114,000
2,000
118,000
3,000
29,000
101,000
25,000
107,000
2,000
127,000
2,000
93,000
53,000
29,000
100,000
1,000
122,000
4,000
89,000
43,000
80,000
55,000
Avg
Flowrate
gpm
250
236
227
297
214
235
227
167
229
167
230
246
238
229
241
233
333
232
167
234
220
NA
229
NA
237
225
239
227
238
234
222
232
229
231
228
167
228
228
250
236
227
235
NA
231
250
230
231
245
226
333
225
333
235
232
230
238
167
234
333
232
287
212
229
APU
Electric
Meter
KWH
130.04
132.07
132.37
133.07
134.68
135.81
137.12
137.16
139.36
139.40
141.34
141.92
143.22
144.24
144.50
146.45
146.53
148.62
148.75
150.73
151.90
151.54
154.05
154.13
155.63
156.33
158.31
158.92
159.11
161.27
161.37
162.89
163.74
165.16
166.13
166.17
168.39
168.90
169.17
171.14
171.43
173.35
173.39
175.40
175.49
176.00
177.73
178.18
185.05
180.10
182.30
182.35
183.95
184.86
185.39
187.07
187.12
189.18
189.32
190.80
191.56
192.94
193.90
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
70.5
73.6
78.2
73.1
72.4
69.2
64.5
71.7
72.1
85.8
71.8
0.0
0.0
70.0
0.0
0.0
0.0
67.1
66.3
0.0
60.0
76.9
79.4
78.1
44.3
65.4
44.3
40.1
29.5
35.9
44.3
22.2
44.3
24.0
22.0
44.3
44.3
33.6
44.3
29.5
46.5
40.1
44.3
46.8
29.6
56.8
44.3
24.3
22.0
35.0
39.7
42.9
18.5
23.1
35.9
20.0
59.9
112.1
57.8
72.3
71.4
122.2
90.0
Daily Flow
Totalizer
A
gal
467
36,639
815
12,722
30,072
17,426
21,986
507
34,239
277
28,150
14,766
34,668
27,606
5,778
53,286
642
57,138
642
49,434
16,050
0
65,484
0
48,792
10,914
47,508
16,050
4,494
58,422
1,926
41,088
22,470
38,520
26,322
642
60,990
12,198
6,420
52,644
7,062
52,002
0
54,570
1,284
13,482
46,866
10,914
50,718
642
60,348
642
42,372
24,396
13,482
44,940
642
55,854
1,284
41,088
16,050
40,446
25,680
Cum.
Flow
Totalizer
A
Kgal
20,922
20,958
20,959
20,972
21,002
21,019
21,041
21,042
21,076
21,076
21,105
21,119
21,154
21,182
21,187
21,241
21,241
21,298
21,299
21,349
21,365
21,365
21,430
21,430
21,479
21,490
21,537
21,553
21,558
21,616
21,618
21,659
21,682
21,720
21,747
21,747
21,808
21,820
21,827
21,880
21,887
21,939
21,939
21,993
21,994
22,008
22,055
22,066
22,116
22,117
22,177
22,178
22,220
22,245
22,258
22,303
22,304
22,360
22,361
22,402
22,418
22,459
22,484
Bed
Volume
Totalizer
A
BV
34,961
35,022
35,023
35,044
35,095
35,124
35,160
35,161
35,219
35,219
35,266
35,291
35,349
35,395
35,404
35,493
35,495
35,590
35,591
35,674
35,701
35,701
35,810
35,810
35,891
35,910
35,989
36,016
36,023
36,121
36,124
36,193
36,230
36,295
36,339
36,340
36,442
36,462
36,473
36,561
36,573
36,660
36,660
36,751
36,753
36,775
36,854
36,872
36,957
36,958
37,059
37,060
37,131
37,171
37,194
37,269
37,270
37,363
37,365
37,434
37,461
37,529
37,571
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
100.5
97.4
96.1
90.7
93.5
90.4
90.0
111.4
111.9
113.1
111.1
113.3
107.5
95.5
NA
98.4
107.1
109.3
101.0
104.2
95.5
101.9
113.4
108.4
97.7
119.5
109.4
105.0
100.6
103.1
97.2
97.7
118.2
116.8
112.0
114.4
120.8
108.6
105.7
100.0
104.1
106.0
118.2
100.9
101.6
99.8
99.0
98.0
98.0
110.0
120.6
113.3
101.6
109.1
113.5
100.0
97.4
102.7
91.5
96.6
98.3
105.1
100.0
Daily Flow
Totalizer
B
gal
690
50,766
6,108
16,999
41,229
23,845
31,733
612
53,270
383
47,783
14,117
32,699
24,716
5,470
48,240
817
50,828
672
43,556
13,409
341
57,571
123
46,379
10,217
45,480
15,257
5,767
51,485
1,579
38,760
21,717
37,244
25,358
645
58,421
11,920
6,324
49,620
6,449
49,181
339
50,600
1,215
12,278
43,700
10,639
46,829
520
55,685
545
39,078
22,994
13,090
41,768
880
51,295
1,624
35,531
17,170
32,801
22,319
Cum. Flow
Totalizer
B
Kgal
18,608
18,659
18,665
18,682
18,723
18,747
18,779
18,780
18,833
18,833
18,881
18,895
18,928
18,952
18,958
19,006
19,007
19,058
19,059
19,102
19,115
19,116
19,173
19,174
19,220
19,230
19,276
19,291
19,297
19,348
19,350
19,388
19,410
19,447
19,473
19,473
19,532
19,544
19,550
19,600
19,606
19,655
19,656
19,706
19,707
19,720
19,763
19,774
19,821
19,821
19,877
19,878
19,917
19,940
19,953
19,995
19,995
20,047
20,048
20,084
20,101
20,134
20,156
Bed
Volume
Totalizer
B
BV
31,095
31,179
31,190
31,218
31,287
31,327
31,380
31,381
31,470
31,470
31,550
31,574
31,629
31,670
31,679
31,760
31,761
31,846
31,847
31,920
31,942
31,943
32,039
32,039
32,117
32,134
32,210
32,235
32,245
32,331
32,334
32,398
32,435
32,497
32,539
32,540
32,638
32,658
32,668
32,751
32,762
32,844
32,845
32,929
32,931
32,952
33,025
33,043
33,121
33,122
33,215
33,216
33,281
33,320
33,341
33,411
33,413
33,498
33,501
33,560
33,589
33,644
33,681
System Cum.
Volume
Treated
Kgal
39,530
39,617
39,624
39,654
39,725
39,767
39,820
39,821
39,909
39,910
39,986
40,014
40,082
40,134
40,145
40,247
40,248
40,356
40,358
40,451
40,480
40,480
40,603
40,604
40,699
40,720
40,813
40,844
40,854
40,964
40,968
41,048
41,092
41,168
41,219
41,221
41,340
41,364
41,377
41,479
41,493
41,594
41,594
41,699
41,702
41,728
41,818
41,840
41,937
41,938
42,055
42,056
42,137
42,185
42,211
42,298
42,299
42,406
42,409
42,486
42,519
42,592
42,640
System
Total Bed
Volumes
Treated1"
BV
33,028
33,101
33,106
33,131
33,191
33,225
33,270
33,271
33,344
33,345
33,408
33,432
33,489
33,532
33,542
33,627
33,628
33,718
33,719
33,797
33,821
33,822
33,924
33,925
34,004
34,022
34,099
34,126
34,134
34,226
34,229
34,296
34,333
34,396
34,439
34,440
34,540
34,560
34,571
34,656
34,667
34,752
34,752
34,840
34,842
34,864
34,939
34,957
35,039
35,040
35,137
35,138
35,206
35,245
35,268
35,340
35,341
35,431
35,433
35,497
35,525
35,586
35,626
Vessel AP
(psi)
A
5.0
6.0
6.2
6.4
7.8
8.2
9.1
9.0
10.1
10.2
2.4
3.0
3.5
4.6
4.8
5.8
6.0
7.0
7.2
8.0
9.0
9.2
2.2
2.6
3.2
4.2
5.0
6.0
6.0
7.6
7.8
8.0
9.2
9.5
10.3
10.1
12.0
3.0
3.0
3.6
3.8
5.6
6.0
7.0
7.2
7.6
8.8
9.2
9.2
9.8
12.0
11.0
2.8
3.1
3.2
4.5
2.6
6.0
6.0
6.1
7.8
8.0
9.0
B
5.2
6.2
6.6
6.8
8.0
8.6
9.2
9.0
10.2
10.6
2.2
3.2
3.8
4.8
4.8
6.0
6.1
7.1
7.7
9.0
9.4
9.4
2.6
2.6
3.6
4.4
5.1
6.0
6.0
7.4
7.8
8.2
9.0
9.2
10.2
10.1
11.8
3.0
3.0
3.8
4.2
5.8
5.9
7.3
7.4
7.4
9.0
9.2
9.2
9.6
10.0
11.0
2.8
3.2
3.4
4.6
5.0
6.0
6.1
6.8
7.8
8.9
9.1
System
AP
(psi)
psig
14
18
18
18
18
18
18
18
21
22
14
14
15
14
10
17
17
18
19
19
20
20
14
14
15
16
16
16
17
18
18
18
20
22
19
14
20
14
13
15
15
14
16
16
18
18
19
19
19
16
22
14
12
12
14
14
16
15
16
17
18
22
28
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
89
90
91
92
93
94
95
96
97
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
3/6/2006
3/7/20061"1
3/8/2006
3/9/2006
3/10/2006
3/11/2006
3/12/2006
3/13/2006
3/14/2006
3/15/2006
3/16/2006
3/17/2006
3/18/2006
3/19/2006
3/20/2006
3/21/2006
3/22/2006
3/23/2006
3/24/2006
3/25/2006
3/26/2006
3/27/2006
3/28/2006
3/29/2006
3/30/2006
3/31/2006
4/1/2006
4/2/2006
4/3/2006
4/4/2006
4/5/2006
4/6/2006
4/7/2006
4/8/2006
4/9/2006
4/10/2006
4/11/2006
4/12/2006
4/13/2006
4/14/2006
4/15/2006
4/16/2006
4/17/2006
4/18/2006
4/19/2006
4/20/2006
4/21/2006
4/22/2006
4/23/2006
4/24/2006
4/25/2006
4/26/2006
4/27/2006
4/28/2006
4/29/2006
4/30/2006
5/1/2006
5/2/2006
5/3/2006
5/4/2006
5/5/2006
5/6/2006
5/7/2006
Time
09:05
18:40
09:45
09:05
5:55
20:08
16:30
09:10
09:20
09:15
06:20
11:00
23:30
16:30
08:55
08:35
09:50
13:10
11:11
16:45
17:15
13:20
13:40
09:05
09:20
11:06
17:00
21:45
11:23
13:00
13:25
09:17
13:48
16:50
16:45
13:11
14:00
13:20
13:07
16:45
16:30
16:20
13:26
11:30
15:00
13:53
13:41
16:30
16:45
14:54
14:00
13:00
13:22
13:00
16:45
16:35
14:55
14:30
13:30
13:00
13:25
17:25
17:00
Well House #1 Reading
Opt Hours
Well!
hr
0.8
8.9
0.3
0.3
9.4
2.8
7.2
0.1
8.6
0.1
0.2
10.1
10.9
0.4
0.1
9.9
4.1
2.8
7.4
1.8
9.7
0.1
7.3
0.2
10.2
3.6
7.4
8.9
6.5
4.8
5.3
3.8
7.6
2.6
7.9
NA
8.5
5.7
10.1
5.0
6.4
9.8
9.9
1.5
11.1
1.3
12.9
6.9
3.7
6.4
3.5
5.5
4.2
11.0
1.8
8.9
11.3
0.7
10.9
10.8
4.1
9.2
10.0
Daily Flow
Totalizer
qal
11,000
123,000
4,000
4,000
130,000
39,000
104,000
1,000
121,000
1,000
4,000
142,000
151,000
5,000
2,000
137,000
56,000
40,000
104,000
26,000
110,000
1,000
130,000
3,000
142,000
90,000
61,000
124,000
93,000
64,000
76,000
122,000
40,000
35,000
110,000
NA
120,000
78,000
139,000
69,000
88,000
136,000
137,000
20,000
154,000
18,000
180,000
98,000
52,000
89,000
50,000
78,000
58,000
153,000
25,000
122,000
157,000
10,000
151,000
150,000
57,000
130,000
140,000
Avg
Flowrate
qpm
229
230
222
222
230
232
241
167
234
167
333
234
231
208
333
231
228
238
234
241
189
167
297
250
232
417
137
232
238
222
239
535
88
224
232
NA
235
228
229
230
229
231
231
222
231
231
233
237
234
232
238
236
230
232
231
228
232
238
231
231
232
236
233
APU
Electric
Meter
KWH
194.11
194.70
196.36
196.46
198.64
199.36
201.09
201.13
203.15
203.23
203.44
205.93
208.44
208.57
208.61
210.97
211.93
212.65
214.39
214.85
216.68
216.74
218.93
218.99
221.38
222.25
224.03
226.07
227.59
228.74
229.98
230.86
232.66
233.37
235.11
235.90
237.28
238.60
240.96
242.14
243.62
245.89
248.20
248.60
251.10
251.47
254.49
256.10
257.02
258.46
259.28
260.59
261.52
264.13
264.58
266.69
269.34
269.40
271.99
274.51
275.47
277.63
279.95
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
qpm
60.1
120.0
128.6
125.8
116.6
113.0
112.0
109.7
110.3
110.5
119.3
116.9
111.6
110.5
108.0
117.0
110.8
108.5
109.4
108.7
108.0
124.6
117.1
113.7
112.9
111.6
111.1
95.5
119.3
110.2
112.3
112.2
112.4
111.6
110.0
114.2
114.0
103.2
113.2
102.3
111.2
96.0
110.1
110.3
113.6
111.5
130.6
109.1
109.8
108.4
119.0
120.1
112.2
117.4
104.5
107.4
92.9
93.2
100.0
109.3
121.3
101.1
110.9
Daily Flow
Totalizer
A
gal
5,136
57,138
2,619
2,125
67,408
19,749
46,417
367
56,426
692
2,268
72,575
72,969
565
410
66,124
26,911
17,531
49,022
10,720
50,260
611
60,112
979
65,138
23,142
48,920
51,398
41,466
28,973
33,992
23,612
50,092
16,059
49,126
21,270
36,680
34,097
60,320
29,999
37,776
59,346
60,303
69,928
3,722
9,634
77,468
43,476
24,873
39,423
21,895
35,423
26,078
58,896
20,223
53,171
65,516
2,329
63,062
62,880
24,895
58,409
62,348
Cum.
Flow
Totalizer
A
Kgal
22,489
22,547
22,549
22,551
22,619
22,638
22,685
22,685
22,742
22,742
22,745
22,817
22,890
22,891
22,891
22,957
22,984
23,002
23,051
23,061
23,112
23,112
23,172
23,173
23,239
23,262
23,311
23,362
23,403
23,432
23,466
23,490
23,540
23,556
23,605
23,627
23,663
23,697
23,758
23,788
23,825
23,885
23,945
24,015
24,019
24,028
24,106
24,149
24,174
24,214
24,236
24,271
24,297
24,356
24,376
24,429
24,495
24,497
24,560
24,623
24,648
24,706
24,769
Bed
Volume
Totalizer
A
BV
37,580
37,676
37,680
37,683
37,796
37,829
37,907
37,907
38,002
38,003
38,007
38,128
38,250
38,251
38,251
38,362
38,407
38,436
38,518
38,536
38,620
38,621
38,721
38,723
38,832
38,871
38,952
39,038
39,107
39,156
39,213
39,252
39,336
39,363
39,445
39,480
39,542
39,599
39,699
39,749
39,813
39,912
40,013
40,129
40,136
40,152
40,281
40,354
40,395
40,461
40,498
40,557
40,601
40,699
40,733
40,822
40,931
40,935
41,040
41,145
41,187
41,285
41,389
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
100.3
90.0
87.5
87.9
91.2
103.7
100.0
98.3
97.6
95.5
99.8
95.1
93.5
93.0
96.7
104.2
103.3
103.5
101.7
105.6
104.5
105.7
107.0
107.1
110.5
107.3
108.2
100.0
108.8
105.7
107.0
116.7
110.7
111.7
105.0
124.9
120.5
102.9
114.4
111.4
118.4
110.0
108.7
111.6
120.3
122.0
122.7
112.1
110.8
111.4
115.6
116.8
118.3
113.4
115.3
119.6
115.8
113.8
116.6
121.1
124.1
106.4
111.9
Daily Flow
Totalizer
B
qal
5,470
49,107
1,789
1,428
48,199
18,211
42,656
50,490
299
611
1,966
57,856
61,066
462
321
57,261
23,241
16,215
45,972
9,852
46,588
553
55,407
901
59,976
21,518
44,250
53,425
40,162
44,010
15,917
23,071
46,654
15,284
47,342
20,106
34,995
33,954
81,644
10,805
38,495
59,561
60,171
9,743
65,542
8,525
87,455
46,776
25,998
40,856
22,609
56,095
6,821
71,361
12,319
58,374
79,913
2,736
73,816
72,574
26,917
59,848
65,174
Cum. Flow
Totalizer
B
Kgal
20,162
20,211
20,213
20,214
20,262
20,280
20,323
20,374
20,374
20,374
20,376
20,434
20,495
20,496
20,496
20,553
20,577
20,593
20,639
20,649
20,695
20,696
20,751
20,752
20,812
20,834
20,878
20,931
20,971
21,015
21,031
21,054
21,101
21,116
21,164
21,184
21,219
21,253
21,334
21,345
21,384
21,443
21,503
21,513
21,579
21,587
21,675
21,722
21,748
21,788
21,811
21,867
21,874
21,945
21,958
22,016
22,096
22,099
22,172
22,245
22,272
22,332
22,397
Bed
Volume
Totalizer
B
BV
33,690
33,772
33,775
33,778
33,858
33,889
33,960
34,044
34,045
34,046
34,049
34,146
34,248
34,249
34,249
34,345
34,384
34,411
34,488
34,504
34,582
34,583
34,676
34,677
34,777
34,813
34,887
34,976
35,044
35,117
35,144
35,182
35,260
35,286
35,365
35,398
35,457
35,514
35,650
35,668
35,732
35,832
35,933
35,949
36,058
36,073
36,219
36,297
36,340
36,409
36,446
36,540
36,552
36,671
36,691
36,789
36,922
36,927
37,050
37,172
37,217
37,317
37,426
System Cum.
Volume
Treated
Kgal
42,651
42,757
42,762
42,765
42,881
42,919
43,008
43,059
43,116
43,117
43,121
43,251
43,386
43,387
43,387
43,511
43,561
43,595
43,690
43,710
43,807
43,808
43,924
43,926
44,051
44,095
44,188
44,293
44,375
44,448
44,498
44,545
44,641
44,673
44,769
NA
44,882
44,950
45,092
45,133
45,209
45,328
45,449
45,528
45,598
45,616
45,781
45,871
45,922
46,002
46,047
46,138
46,171
46,301
46,334
46,445
46,591
46,596
46,733
46,868
46,920
47,038
47,166
System
Total Bed
Volumes
Treated"1
BV
35,635
35,724
35,728
35,731
35,827
35,859
35,933
35,976
36,023
36,024
36,028
36,137
36,249
36,250
36,250
36,353
36,395
36,424
36,503
36,520
36,601
36,602
36,698
36,700
36,805
36,842
36,920
37,007
37,076
37,136
37,178
37,217
37,298
37,324
37,405
8VALUE!
37,499
37,556
37,675
37,709
37,773
37,872
37,973
38,039
38,097
38,112
38,250
38,325
38,368
38,435
38,472
38,549
38,576
38,685
38,712
38,805
38,927
38,931
39,045
39,159
39,202
39,301
39,407
Vessel AP
(psi)
A
8.9
8.9
8.0
8.8
8.8
2.9
4.0
4.2
5.5
5.6
5.0
8.3
9.0
9.2
9.2
8.0
10.6
2.8
3.7
4.0
5.0
5.6
7.0
7.2
8.9
9.0
10.2
10.2
9.5
7.9
7.8
7.9
7.8
7.9
7.9
6.8
7.8
7.8
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
7.0
2.4
2.5
4.2
4.6
5.5
7.0
9.0
10.2
10.0
8.7
8.8
8.7
8.2
2.6
4.1
6.0
B
9.1
9.1
9.0
9.4
9.4
2.7
4.2
4.4
5.5
5.6
5.4
7.4
9.5
9.5
9.6
8.2
11.0
2.4
3.7
4.0
5.0
5.8
7.0
7.2
8.9
9.0
10.2
9.0
8.0
2.8
3.0
3.2
5.0
5.9
6.8
8.2
9.4
10.0
10.6
9.8
9.8
9.4
8.2
9.8
10.0
8.8
2.4
2.8
4.2
4.6
6.0
6.5
7.8
9.0
9.2
10.0
8.1
8.5
8.6
7.8
2.4
4.5
6.0
System
AP
(psi)
PSiq
19
18
19
20
20
14
15
14
16
16
16
18
19
19
19
18
20
13
14
15
12
12
18
18
19
19
20
18
17
14
14
14
14
16
18
18
20
22
28
20
20
22
18
20
20
18
14
14
14
16
13
16
18
20
21
21
18
19
17
18
12
12
16
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
98
99
100
101
102
103
104
105
106
107
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
5/8/2006
5/9/2006
5/10/2006
5/1 1/2006
5/12/2006
5/13/2006
5/14/2006
5/15/2006
5/16/2006
5/17/2006
5/18/2006
5/19/2006
5/20/2006
5/21/2006
5/22/2006
5/23/2006
5/24/2006
5/25/2006
5/26/2006
5/27/2006
5/28/2006
5/29/2006
5/31/2006
6/1/2006
6/2/2006
6/3/2006
6/4/2006
6/5/2006
6/6/2006
6/7/2006
6/8/2006
6/9/2006
6/10/2006
6/11/2006
6/12/2006
6/13/2006
6/14/2006
6/15/2006
6/16/2006
6/17/2006
6/18/2006
6/19/2006
6/20/2006
6/21/2006
6/22/2006
6/23/2006
6/24/2006
6/25/2006
6/26/2006
6/27/2006
6/28/2006
6/29/2006
6/30/2006
7/1/2006
7/2/2006
7/3/2006
7/4/2006
7/5/2006
7/6/2006
7/7/2006
7/8/2006
7/9/2006
7/10/2006
7/11/2006
7/12/2006
7/13/2006
7/14/2006
7/15/2006
7/16/2006
Time
06:55
09:22
11:00
09:30
13:42
17:00
16:30
08:50
10:56
08:20
11:19
13:21
00:00
17:30
10:30
11:30
09:45
08:00
8:15
18:40
17:00
17:15
09:20
10:24
13:20
16:30
17:55
10:00
14:05
14:35
14:10
14:10
16:40
16:55
14:15
09:30
13:45
06:30
6:25
17:20
00:00
14:00
06:45
06:00
10:40
11:30
17:30
20:50
13:00
10:50
13:16
13:00
13:14
18:57
15:10
09:30
16:35
14:10
14:39
13:40
19:36
17:00
10:35
14:00
10:10
13:15
11:00
16:30
16:40
Well House #1 Reading
Opt Hours
Well!
hr
8.6
1.3
11.2
7.9
3.5
9.8
14.3
2.0
5.9
0.0
13.6
9.0
13.2
1.4
9.5
10.7
5.4
13.6
13.8
12.0
8.0
14.8
10.3
7.7
11.5
11.7
5.1
6.5
14.0
1.5
16.6
1.3
8.7
11.3
13.0
0.3
11.9
3.1
10.6
13.8
21.8
8.9
0.1
9.8
12.6
5.0
6.2
9.9
0.6
8.6
4.8
7.6
3.1
9.6
8.7
3.4
10.1
6.3
4.8
6.7
4.0
8.8
6.9
12.4
0.3
10.2
7.9
8.1
7.2
Daily Flow
Totalizer
qal
121,000
18,000
154,000
81,000
78,000
136,000
116,000
42,000
152,000
0
186,000
138,000
166,000
19,000
158,000
119,000
76,000
193,000
188,000
165,000
109,000
203,000
142,000
105,000
158,000
158,000
69,000
86,000
191,000
22,000
224,000
25,000
118,000
156,000
176,000
5,000
161,000
44,000
146,000
189,000
300,000
119,000
2,000
132,000
172,000
69,000
84,000
132,000
1 1 ,000
117,000
67,000
107,000
43,000
133,000
120,000
46,000
137,000
86,000
62,000
62,000
84,000
118,000
94,000
174,000
4,000
81,000
169,000
1 1 1 ,000
96,000
Avg
Flowrate
gpm
234
231
229
171
371
231
135
350
429
NA
228
256
210
226
111
185
235
237
227
229
227
229
230
227
229
225
225
221
227
244
225
321
226
230
226
278
225
237
230
228
229
223
333
224
228
230
226
222
306
227
233
235
231
231
230
225
226
228
215
154
350
223
227
234
222
132
357
228
222
APU
Electric
Meter
KWH
281.87
282.27
284.89
286.72
287.54
289.82
291.77
292.46
295.00
295.03
298.17
300.50
303.33
303.66
306.35
308.35
309.62
312.03
315.98
318.75
320.62
324.05
330.12
331.89
334.61
337.27
338.45
339.94
343.20
343.59
347.33
347.75
349.77
352.41
355.41
355.49
358.25
359.00
361.85
365.13
369.72
371.75
371.78
374.05
377.07
378.18
379.62
381.41
382.07
384.06
385.31
387.09
387.82
390.20
392.25
393.02
345.35
396.83
397.91
399.47
400.40
402.43
404.03
406.91
406.99
409.34
411.18
413.06
414.71
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
111.6
114.6
107.9
110.2
119.7
110.8
112.3
118.2
119.0
108.0
114.6
110.4
107.2
105.4
110.7
111.7
116.3
110.2
101.7
96.5
103.4
100.9
101.4
103.1
101.8
95.0
99.6
96.2
104.6
106.1
101.7
89.9
85.5
95.6
89.0
84.1
NA
NA
107.1
91.8
89.5
97.6
97.9
95.0
NA
NA
NA
NA
NA
NA
99.5
96.8
90.5
90.2
83.9
81.5
75.0
67.4
66.4
71.5
76.9
70.0
78.1
70.0
74.7
67.6
68.4
65.5
65.0
Daily Flow
Totalizer
A
gal
54,125
7,680
68,884
47,900
20,856
59,864
51,552
38,066
46,714
521
82,019
63,408
77,515
8,348
73,450
54,007
33,438
84,656
82,745
69,210
46,604
83,946
59,031
43,715
66,918
65,391
28,581
35,449
81,391
9,563
98,022
1 1 ,090
48,754
62,393
67,023
1,536
64,065
34,212
73,513
85,833
107,102
47,199
628
53,466
80,892
32,100
39,804
63,558
3,852
55,212
30,816
40,702
15,820
54,147
35,696
14,795
43,050
25,090
17,395
25,610
15,159
33,124
25,645
51,300
1,067
40,093
30,401
29,585
26,062
Cum.
Flow
Totalizer
A
Kgal
24,823
24,831
24,899
24,947
24,968
25,028
25,080
25,118
25,164
25,165
25,247
25,310
25,388
25,396
25,470
25,524
25,557
25,642
25,725
25,794
25,840
25,924
26,074
26,118
26,185
26,250
26,279
26,314
26,396
26,405
26,503
26,514
26,563
26,625
26,693
26,694
26,758
26,792
26,866
26,952
27,059
27,106
27,107
27,160
27,241
27,273
27,313
27,376
27,380
27,435
27,466
27,507
27,523
27,577
27,613
27,627
27,671
27,696
27,713
27,739
27,754
27,787
27,813
27,864
27,865
27,905
27,935
27,965
27,991
Bed
Volume
Totalizer
A
BV
4 ,479
41 ,492
41,607
41,687
41,722
41,822
41,908
41,972
42,050
42,051
42,188
42,294
42,423
42,437
42,560
42,650
42,706
42,848
42,986
43,102
43,179
43,320
43,570
43,643
43,755
43,864
43,912
43,971
44,107
44,123
44,287
44,306
44,387
44,492
44,604
44,606
44,713
44,770
44,893
45,037
45,216
45,294
45,295
45,385
45,520
45,574
4 ,640
,746
,753
,845
,897
5,965
. 5,991
46,081
46,141
46,166
46,238
46,280
46,309
46,352
46,377
46,432
46,475
46,561
46,563
46,630
46,680
46,730
46,773
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
113.4
122.0
112.5
111.8
107.7
115.6
110.3
118.7
120.6
115.0
111.4
115.2
102.8
105.0
108.4
109.4
110.4
113.9
108.9
109.1
106.6
103.5
106.1
108.5
105.8
100.0
112.0
109.4
105.7
111.1
105.4
110.5
110.0
110.9
113.6
111.8
122.2
123.4
115.1
112.2
108.8
118.8
120.3
115.5
106.8
113.7
119.4
99.8
105.0
116.0
120.2
116.5
118.2
115.6
104.7
102.9
100.0
103.3
116.3
118.3
113.2
100.0
105.4
106.8
108.5
101.9
100.1
106.5
105.0
Daily Flow
Totalizer
B
gal
56,130
48,157
32,353
50,368
21,821
63,176
53,911
18,977
70,185
559
85,867
61,938
73,893
7,932
69,097
52,368
35,312
90,522
87,813
74,684
52,159
97,140
67,133
49,588
75,639
23,250
83,845
41,918
89,581
10,267
101,344
12,251
55,534
75,916
88,530
2,160
80,973
13,957
44,022
107,740
128,809
855
62,766
81,171
28,155
37,728
60,431
3,795
2,029
79,830
49,113
8,287
72,214
55,678
20,665
64,634
41,471
29,888
45,010
26,430
57,147
44,722
75,257
1,586
60,259
27,042
66,976
41,201
Cum. Flow
Totalizer
B
Kgal
22,453
22,501
22,534
22,584
22,606
22,669
22,723
22,742
22,812
22,813
22,898
22,960
23,034
23,042
23,111
23,164
23,199
23,289
23,377
23,452
23,504
23,601
23,772
23,822
23,898
23,921
24,005
24,047
24,136
24,146
24,248
24,260
24,316
24,392
24,480
24,482
24,563
24,577
24,621
24,729
24,858
24,915
24,978
25,059
25,087
25,125
25,185
25,189
25,191
25,271
25,320
25,328
25,401
25,456
25,477
25,542
25,583
25,613
25,658
25,684
25,742
25,786
25,862
25,863
25,923
25,950
26,017
26,059
Bed
Volume
Totalizer
B
BV
37,519
37,600
37,654
37,738
37,774
37,880
37,970
38,002
38,119
38,120
38,264
38,367
38,491
38,504
38,619
38,707
38,766
38,917
39,064
39,189
39,276
39,438
39,724
39,807
39,933
39,972
40,112
40,182
40,332
40,349
40,518
40,539
40,632
40,759
40,906
40,910
41,045
41,069
41,142
41,322
41,538
41,632
41,633
41,738
41 ,874
41,921
41 ,984
42,085
42,091
42,095
42,228
42,310
42,324
42,445
42,538
42,572
42,680
42,750
42,800
42,875
42,919
43,014
43,089
43,215
43,218
43,318
43,364
43,475
43,544
System Cum.
Volume
Treated
Kgal
47,276
47,332
47,433
47,531
47,574
47,697
47,802
47,860
47,976
47,977
48,145
48,271
48,422
48,438
48,581
48,687
48,756
48,931
49,102
49,246
49,344
49,526
49,847
49,940
50,082
50,171
50,284
50,361
50,532
50,552
50,751
50,774
50,879
51,017
51,173
51,176
51,321
51,369
51 ,487
51,681
51,917
52,020
52,022
52,138
52,300
52,360
52,438
52,562
52,569
52,627
52,737
52,827
52,851
52,978
53,069
53,104
53,212
53,279
53,326
53,397
53,438
53,528
53,599
53,725
53,728
53,828
53,886
53,982
54,050
System
Total Bed
Volumes
Treated"1
BV
39,499
39,546
39,631
39,713
39,748
39,851
39,939
39,987
40,085
40,085
40,226
40,330
40,457
40,471
40,590
40,679
40,736
40,882
41,025
41,145
41,228
41,379
41 ,647
41,725
41,844
41,918
42,012
42,077
42,220
42,236
42,403
42,422
42,509
42,625
42,755
42,758
42,879
42,919
43,018
43,179
43,377
43,463
43,464
43,562
43,697
43,747
43,812
43,916
43,922
43,970
44,062
44,137
44,158
44,263
44,339
44,369
44,459
44,515
44,554
44,613
44,648
44,723
44,782
44,888
44,890
44,974
45,022
45,103
45,159
Vessel AP
(psil
A
6.2
7.2
7.2
9.1
7.8
7.8
7.5
7.2
7.0
7.3
12.0
10.0
12.2
10.4
9.4
2.8
3.6
6.0
8.4
9.1
11.4
9.0
9.0
9.0
9.0
12.4
12.1
12.4
3.2
3.0
6.4
7.0
8.8
11.1
12.6
11.6
8.0
8.0
9.0
7.0
9.8
11.4
10.1
9.8
10.0
9.9
11.0
9.8
10.4
3.0
3.6
4.8
5.9
8.0
8.4
10.0
11.0
12.0
12.4
12.0
10.2
10.4
3.2
4.8
4.8
7.2
8.2
9.2
9.4
B
7.0
6.8
9.2
8.0
8.0
7.8
7.0
7.2
6.8
7.2
11.4
10.2
10.6
10.6
10.0
2.4
3.6
5.8
8.2
10.2
9.4
8.2
7.4
7.6
8.5
11.8
11.4
11.8
3.0
4.0
6.0
6.6
8.2
9.8
11.6
11.0
3.6
6.0
4.5
6.6
10.0
9.8
9.8
9.6
9.9
8.0
10.0
9.7
10.0
2.4
3.6
4.6
5.2
7.4
8.8
9.5
10.4
11.8
11.4
11.4
10.2
11.5
2.6
5.0
5.2
7.2
9.0
9.5
9.5
System
ip
(psil
psig
19
19
19
18
19
20
18
17
18
18
22
18
20
22
20
14
15
16
19
21
20
20
18
18
19
22
22
23
14
14
17
17
14
19
22
21
20
20
14
18
20
21
19
20
20
22
22
20
20
14
14
15
17
16
18
20
19
24
22
22
21
23
14
16
15
18
19
18
19
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
108
109
110
111
112
113
114
115
116
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
7/17/2006
7/18/2006
7/19/2006
7/20/2006
7/21/2006
7/22/2006
7/23/2006
7/24/2006
7/25/2006
7/26/2006
7/27/2006
7/28/2006
7/29/2006
7/30/2006
7/31/2006
8/1/2006
8/2/2006
8/3/2006
8/4/2006
8/5/2006
8/6/2006
8/7/2006
8/8/2006
8/9/2006
8/10/2006
8/11/2006
8/12/2006
8/13/2006
8/14/2006
8/15/2006
8/16/2006
8/17/2006
8/18/2006
8/19/2006
8/20/2006
8/21/2006
8/22/2006
8/23/2006
8/24/2006
8/25/2006
8/26/2006
8/27/2006
8/28/2006
8/29/2006
8/30/2006
8/31/2006
9/1/2006
9/2/2006
9/3/2006
9/4/2006
9/5/2006
9/6/2006
9/7/2006
9/8/2006
9/9/2006
9/10/2006
9/11/2006
9/12/2006
9/13/2006
9/14/2006
9/15/2006
9/16/2006
9/1 7/2006
Time
13:30
14:10
10:15
06:30
11:00
11:25
16:00
09:10
10:30
13:35
10:10
10:30
16:55
10:45
12:45
13:20
11:14
10:15
14:55
19:40
17:00
09:00
09:55
13:35
11:09
13:00
16:30
16:40
07:00
14:26
13:50
14:21
10:00
17:15
16:30
9:05
13:20
9:20
10:00
10:15
7:00
17:00
14:35
13:56
13:43
9:45
14:00
17:42
16:45
10:23
14:16
14:20
9:30
13:10
16:30
10:15
13:30
14:46
13:10
10:56
9:35
17:10
16:20
Well House #1 Reading
Opt Hours
Well!
hr
10.7
5.2
10.2
12.6
7.5
11.4
12.1
1.6
6.3
11.3
14.3
9.8
7.2
10.2
14.8
12.9
8.1
11.9
17.0
15.4
13.0
7.3
12.0
6.5
5.9
11.2
7.6
11.3
7.9
14.0
9.5
7.9
10.1
13.8
13.8
11.3
8.8
9.3
14.3
13.9
19.8
7.0
7.7
15.6
5.5
4.5
12.2
0.5
9.3
7.9
5.2
5.8
4.0
7.0
4.0
10.0
9.0
2.5
11.4
0.1
8.8
8.7
2.5
Daily Flow
Totalizer
gal
144,000
69,000
139,000
172,000
103,000
158,000
100,000
89,000
87,000
152,000
193,000
133,000
97,000
140,000
193,000
175,000
109,000
159,000
228,000
214,000
180,000
96,000
169,000
84,000
81 ,000
155,000
174,000
86,000
105,000
189,000
129,000
105,000
136,000
219,000
151,000
154,000
120,000
128,000
195,000
189,000
266,000
95,000
104,000
209,000
74,000
60,000
168,000
4,000
76,000
158,000
70,000
80,000
56,000
104,000
47,000
140,000
122,000
32,000
155,000
1,000
110,000
88,000
70,000
Avg
Flowrate
gpm
224
221
227
228
229
231
138
927
230
224
225
226
225
229
217
226
224
223
224
232
231
219
235
215
229
231
382
127
222
225
226
222
224
264
182
227
227
229
227
227
224
226
225
223
224
222
230
133
136
333
224
230
233
248
196
233
226
213
227
167
208
169
467
APU
Electric
Meter
KWH
417.18
418.38
420.73
423.66
425.41
428.03
429.62
431.21
432.70
435.30
438.60
440.87
442.54
444.90
448.29
451.27
453.14
455.87
459.77
463.36
466.37
468.06
471.55
472.34
473.70
476.28
479.22
480.67
482.52
485.70
487.89
489.74
492.04
495.20
498.38
501.00
503.04
505.18
508.47
511.69
516.25
517.86
519.65
523.22
529.49
525.54
528.42
528.52
530.66
532.49
533.71
535.06
536.01
537.75
538.55
540.89
542.88
543.55
546.21
546.24
548.08
549.61
550.87
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
60.0
59.3
64.3
57.3
58.6
63.7
60.0
53.2
50.9
49.7
45.1
46.1
43.9
45.0
47.0
47.8
NA
48.7
54.7
53.0
NA
54.3
NA
NA
NA
NA
NA
NA
NA
NA
NA
52.4
54.5
NA
NA
NA
NA
NA
47.1
45.5
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Daily Flow
Totalizer
A
gal
38,678
17,833
36,991
36,883
28,308
38,588
77,682
10,272
40,446
72,546
91,806
62,916
46,224
65,484
95,016
82,818
52,002
76,398
109,140
98,868
83,460
46,866
77,040
41,730
37,878
71,904
48,792
72,546
50,718
89,880
60,990
50,718
64,842
88,596
88,596
72,546
56,496
59,706
91,806
89,238
127,116
44,940
49,434
100,152
35,310
28,890
78,324
3,210
59,706
50,718
33,384
37,236
25,680
44,940
25,680
64,200
57,780
16,050
73,188
642
56,496
55,854
16,050
Cum.
Flow
Totalizer
A
Kgal
28,030
28,048
28,085
28,121
28,150
28,188
28,266
28,276
28,317
28,389
28,481
28,544
28,590
28,656
28,751
28,834
28,886
28,962
29,071
29,170
29,253
29,300
29,377
29,419
29,457
29,529
29,578
29,650
29,701
29,791
29,852
29,902
29,967
30,056
30,145
30,217
30,274
30,333
30,425
30,514
30,641
30,686
30,736
30,836
30,871
30,900
30,978
30,982
31,041
31,092
31,125
31,163
31,188
31 ,233
31 ,259
31 ,323
31,381
31,397
31,470
31,471
31,527
31,583
31 ,599
Bed
Volume
Totalizer
A
BV
46,838
46,868
46,930
46,991
47,039
47,103
47,233
47,250
47,318
47,439
47,592
47,697
47,775
47,884
48,043
48,181
48,268
48,396
48,578
48,743
48,883
48,961
49,090
49,160
49,223
49,343
49,425
49,546
49,631
49,781
49,883
49,967
50,076
NA
50,372
50,493
50,587
50,687
50,841
50,990
51,202
51 ,277
51,360
51,527
51,586
51,634
51,765
51,771
51 ,870
51,955
52,011
52,073
52,116
52,191
52,234
52,341
52,438
52,465
52,587
52,588
52,683
52,776
52,803
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
103.8
106.8
111.1
98.0
116.7
116.9
110.0
113.4
109.7
116.2
111.9
117.4
111.4
110.0
115.5
111.1
119.0
114.7
103.7
107.9
90.0
94.4
102.9
95.7
108.7
91.5
72.6
70.0
84.1
72.5
73.3
74.4
72.0
85.3
70.0
75.3
76.1
78.7
75.9
72.3
73.1
70.0
74.8
74.7
70.3
64.2
68.0
67.1
65.0
65.0
67.5
62.8
62.4
63.5
54.0
50.0
65.1
66.2
66.9
66.9
NA
60.3
60.0
Daily Flow
Totalizer
B
gal
60,540
30,187
80,707
55,622
45,019
73,559
46,597
43,318
42,674
74,335
95,040
67,243
98,582
18,838
99,522
87,908
54,057
78,459
110,557
89,073
75,074
41,503
64,612
30,155
32,335
63,276
57,849
27,990
47,400
84,000
57,000
47,400
60,600
82,800
82,800
67,800
52,800
55,800
85,800
83,400
118,800
42,000
46,200
93,600
33,000
27,000
73,200
3,000
55,800
47,400
31,200
34,800
24,000
42,000
24,000
60,000
54,000
15,000
68,400
600
52,800
52,200
15,000
Cum. Flow
Totalizer
B
Kgal
26,119
26,149
26,230
26,286
26,331
26,404
26,451
26,494
26,537
26,611
26,706
26,773
26,872
26,891
26,990
27,078
27,132
27,211
27,321
27,410
27,486
27,527
27,592
27,622
27,654
27,717
27,775
27,803
27,851
27,935
27,992
28,039
28,100
28,182
28,265
28,333
28,386
28,442
28,527
28,611
28,730
28,772
28,818
28,911
28,944
28,971
29,045
29,048
29,103
29,151
29,182
29,217
29,241
29,283
29,307
29,367
29,421
29,436
29,504
29,505
29,558
29,557
29,572
Bed
Volume
Totalizer
B
BV
43,645
43,696
43,831
43,924
43,999
44,122
44,200
44,272
44,343
44,468
44,626
44,739
44,904
44,935
45,101
45,248
45,339
45,470
45,654
45,803
45,929
45,998
46,106
46,156
46,210
46,316
46,413
46,460
46,539
46,679
46,774
46,854
46,955
47,093
47,232
47,345
47,433
47,526
47,670
47,809
48,008
48,078
48,155
48,311
48,367
48,412
48,534
48,539
48,632
48,711
48,764
48,822
48,862
48,932
48,972
49,072
49,163
49,188
49,302
49,303
NA
49,390
49,415
System Cum.
Volume
Treated
Kgal
54,149
54,197
54,315
54,407
54,480
54,593
54,717
54,770
54,854
55,000
55,187
55,317
55,462
55,547
55,741
55,912
56,018
56,173
56,392
56,580
56,739
56,827
56,969
57,041
57,111
57,246
57,353
57,453
57,552
57,725
57,843
57,942
58,067
58,238
58,410
58,550
58,659
58,775
58,953
59,125
59,371
59,458
59,554
59,747
59,816
59,872
60,023
60,029
60,145
60,243
60,308
60,380
60,429
60,516
60,566
60,690
60,802
60,833
60,974
60,976
61 ,085
61,140
61,171
System
Total Bed
Volumes
Treat ed|a|
BV
45,242
45,282
45,380
45,457
45,519
45,612
45,716
45,761
45,830
45,953
46,109
46,218
46,339
46,409
46,572
46,715
46,803
46,933
47,116
47,273
47,406
47,480
47,598
47,658
47,717
47,830
47,919
48,003
48,085
48,230
48,329
48,410
48,515
48,658
48,802
48,919
49,010
49,107
49,255
49,399
49,605
49,678
49,757
49,919
49,976
50,023
50,150
50,155
50,251
50,333
50,387
50,447
50,489
50,562
50,603
50,707
50,800
50,826
50,945
50,946
51 ,037
51 ,083
51,109
Vessel AP
(psi)
A
13.0
11.0
10.8
10.2
3.0
4.9
6.4
7.6
9.4
10.6
12.2
12.0
10.4
10.6
13.2
11.6
13.0
12.2
2.8
6.4
8.8
11.0
7.0
2.8
4.2
6.0
8.0
9.0
9.6
9.8
9.6
9.0
13.0
11.5
10.2
11.0
2.8
4.7
7.6
10.0
9.8
10.8
10.2
10.2
10.0
13.0
10.8
11.1
10.8
10.8
3.2
3.4
4.8
5.2
6.6
7.0
9.8
10.6
13.0
12.4
10.0
10.4
10.8
B
12.0
10.0
10.1
9.6
2.4
4.7
6.0
7.5
9.0
9.8
11.4
9.6
9.4
9.6
11.8
11.2
11.6
11.2
2.6
6.0
8.8
10.4
8.4
2.7
4.0
5.8
8.0
9.0
9.0
9.2
9.4
9.0
13.0
11.0
10.0
9.8
2.6
4.2
6.8
9.2
9.4
9.6
9.4
9.6
9.4
11.8
11.8
9.8
8.5
9.2
2.4
3.2
4.4
5.5
6.0
7.0
9.6
10.0
10.0
10.8
9.4
9.4
9.8
System
iP
(psi)
psig
20
19
20
20
14
16
24
19
20
21
22
22
21
26
23
22
21
21
14
18
26
20
19
14
15
14
18
26
18
19
22
20
24
20
26
20
14
16
18
20
20
20
20
20
21
24
20
20
20
18
14
16
16
14
17
18
20
22
22
27
28
19
22
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
>
Week
No.
117
118
119
120
121
122
123
124
125
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
9/18/2006
9/19/2006
9/20/2006
9/21/2006
9/22/2006
9/23/2006
9/24/2006
9/25/2006
9/26/2006
9/27/2006
9/28/2006
9/29/2006
9/30/2006
10/2/2006
10/3/2006
10/4/2006
10/5/2006
10/6/2006
10/7/2006
10/8/2006
10/9/2006
1 0/1 0/2006
10/11/2006
1 0/1 2/2006
1 0/1 3/2006
10/14/2006
1 0/1 5/2006
1 0/1 6/2006
1 0/1 7/2006
1 0/1 8/2006
1 0/1 9/2006
1 0/20/2006
10/21/2006
1 0/22/2006
1 0/23/2006
1 0/24/2006
1 0/25/2006
1 0/26/2006
1 0/27/2006
1 0/28/2006
1 0/29/2006
1 0/30/2006
10/31/2006
11/1/2006
11/2/2006
11/3/2006
11/4/2006
11/5/2006
11/6/2006
11/7/2006
11/8/2006
11/9/2006
11/10/2006
11/11/2006
11/12/2006
11/13/2006
11/14/2006
11/15/2006
11/16/2006
11/17/2006
11/18/2006
11/19/2006
Time
8:55
11:15
8:55
6:05
14:03
16:30
16:30
9:30
10:15
13:41
6:45
9:28
21:20
13:00
13:45
14:00
13:20
9:20
16:35
16:05
16:00
10:00
13:40
6:55
18:30
16:30
16:30
9:00
13:00
9:40
10:00
5:45
10:30
17:15
9:00
9:25
9:30
16:00
16:25
16:20
16:45
14:24
10:52
14:54
14:04
11:45
16:30
16:30
14:17
16:30
13:30
13:00
17:45
16:30
16:30
14:21
13:00
10:46
9:50
9:40
19:17
16:45
Well House #1 Reading
Opt Hours
Well!
hr
1.7
9.9
4.8
6.3
10.6
4.3
6.8
11.2
0.2
11.0
3.4
7.7
9.5
8.4
5.3
6.4
3.4
6.9
3.2
6.8
3.6
6.7
1.1
9.0
0.3
9.4
5.3
6.1
1.2
8.7
0.2
0.6
9.3
4.6
5.4
0.8
0.0
17.3
9.2
3.2
9.2
0.0
10.1
0.3
9.6
0.2
5.8
4.1
1.3
8.0
0.1
8.5
0.4
10.0
0.1
3.2
8.0
0.1
8.3
0.2
10.5
0.0
Daily Flow
Totalizer
gal
27,000
132,000
69,000
86,000
147,000
60,000
91,000
153,000
2,000
149,000
48,000
101,000
130,000
114,000
2,000
158,000
48,000
97,000
45,000
92,000
51,000
87,000
6,000
135,000
4,000
129,000
73,000
84,000
15,000
123,000
4,000
8,000
129,000
63,000
81,000
4,000
0
246,000
145,000
23,000
125,000
1,000
174,000
18,000
84,000
3,000
82,000
55,000
18,000
111,000
0
116,000
4,000
90,000
1,000
95,000
109,000
1,000
117,000
3,000
147,000
0
Avg
Flowrate
gpm
265
222
240
228
231
233
223
228
167
226
235
219
228
226
6
411
235
234
234
225
236
216
91
250
222
229
230
230
208
236
333
222
231
228
250
83
NA
237
263
120
226
NA
287
NA
146
250
236
224
231
231
NA
227
167
150
167
495
227
167
235
250
233
NA
APU
Electric
Meter
KWH
551.29
553.56
554.70
556.15
558.63
559.64
561.21
563.81
563.86
566.43
567.24
569.60
571 .23
573.61
573.67
576.39
577.15
578.78
579.55
581.11
581.97
583.52
583.57
585.88
585.98
588.18
589.42
590.85
591.14
593.18
593.26
593.41
595.50
596.64
598.02
598.11
598.14
598.38
605.06
605.18
607.36
607.42
609.75
609.83
612.07
612.15
613.56
614.53
614.86
616.77
616.80
618.70
618.91
621.24
622.10
622.50
623.43
623.43
625.90
625.96
628.44
628.50
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
NA
NA
NA
NA
NA
NA
NA
51.2
50.5
0.0
0.0
0.0
48.7
48.2
0.0
0.0
0.0
0.0
0.0
NA
NA
47.0
0.0
0.0
0.0
NA
NA
0.0
0.0
0.0
0.0
0.0
0.0
NA
0.0
0.0
0.0
0.0
0.0
0.0
NA
0.0
0.0
0.0
0.0
0.0
0.0
NA
0.0
0.0
0.0
0.0
0.0
0.0
NA
52.3
0.0
0.0
0.0
0.0
0.0
NA
Daily Flow
Totalizer
A
gal
10,914
63,558
30,816
40,446
68,052
27,606
43,656
71,904
1,284
70,620
21,828
49,434
60,990
53,928
34,026
41,088
21,828
44,298
20,544
43,656
23,112
43,014
7,062
57,780
1,926
60,348
34,026
39,162
7,704
55,854
1,284
3,852
59,706
29,532
34,668
5,136
0
111,066
59,064
20,544
59,064
0
64,842
1,926
61,632
1,284
37,236
26,322
8,346
51,360
642
54,570
2,568
64,200
642
20,544
51,360
642
53,286
1,284
67,410
0
Cum.
Flow
Totalizer
A
Kgal
31,610
31,674
31,705
31,745
31,813
31,841
31,884
31,956
31,958
32,028
32,050
32,099
32,160
32,227
32,261
32,302
32,323
32,368
32,388
32,432
32,455
32,498
32,505
32,563
32,565
32,625
32,659
32,698
32,706
32,762
32,763
32,767
32,827
32,856
32,891
32,896
32,896
33,007
33,066
33,087
33,146
33,146
33,211
33,213
33,274
33,276
33,313
33,339
33,347
33,399
33,399
33,454
33,457
33,521
33,521
33,542
33,593
33,594
33,647
33,649
33,716
33,716
Bed
Volume
Totalizer
A
BV
52,821
52,927
52,979
53,046
53,160
53,206
53,279
53,399
53,401
53,519
53,556
53,638
53,740
53,851
53,908
53,976
54,013
54,087
54,121
54,194
54,233
54,305
54,316
54,413
54,416
54,517
54,574
54,639
54,652
54,746
54,748
54,754
54,854
54,903
54,961
54,970
54,970
55,155
55,254
55,288
55,387
55,387
55,495
55,499
55,602
55,604
55,666
55,710
55,724
55,810
55,811
55,902
55,906
56,014
56,015
56,049
56,135
56,136
56,225
56,227
56,340
56,340
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
61.6
56.6
0.0
58.8
59.7
55.5
50.0
0.0
64.6
0.0
0.0
64.1
62.6
53.5
107.0
78.6
0.0
104.4
103.2
95.0
90.0
91.2
90.6
102.0
100.2
95.0
90.0
102.0
96.3
92.9
97.3
96.5
100.6
95.0
80.3
105.6
96.8
108.1
102.7
104.0
95.0
104.7
104.8
106.7
108.1
106.3
103.0
95.0
108.8
106.0
97.9
93.7
97.7
100.6
95.0
105.7
101.2
109.9
103.1
102.4
97.4
97.4
Daily Flow
Totalizer
B
gal
10,200
59,400
28,800
37,800
63,600
25,800
40,800
67,200
1,200
66,000
20,400
46,200
57,000
50,400
31,800
71,513
19,310
40,142
17,504
37,930
20,860
37,640
8,611
49,035
851
53,113
29,820
29,336
11,388
48,327
1,346
3,235
52,082
25,246
34,475
249
104
47,951
121,579
3,426
51,926
548
56,247
7,469
3,210
44,804
33,451
22,128
6,740
45,133
261
48,645
2,447
57,045
616
13,515
49,041
442
47,482
811
62,452
0
Cum. Flow
Totalizer
B
Kgal
29,582
29,642
29,670
29,708
29,772
29,798
29,838
29,906
29,907
29,973
29,993
30,039
30,096
30,158
30,190
30,262
30,281
30,321
30,339
30,376
30,397
30,435
30,444
30,493
30,493
30,547
30,576
30,606
30,617
30,665
30,667
30,670
30,722
30,747
30,782
30,782
30,782
30,830
30,952
30,955
31,007
31,008
31,064
31,071
31,075
31,119
31,153
31,175
31,182
31,227
31,227
31,276
31,278
31,335
31,336
31,349
31,398
31,399
31 ,446
31 ,447
31,510
31,510
Bed
Volume
Totalizer
B
BV
49,432
49,532
49,580
49,643
49,749
49,792
49,860
49,973
49,975
50,085
50,119
50,196
50,292
50,395
50,448
50,567
50,600
50,667
50,696
50,759
50,794
50,857
50,872
50,953
50,955
51 ,044
51,093
51,143
51,162
51,242
51,245
51,250
51,337
51,379
51,437
51,437
51,437
51,517
51,721
51,726
51,813
51,814
51,908
51,921
51,926
52,001
52,057
52,094
52,105
52,180
52,181
52,262
52,266
52,361
52,362
52,385
52,467
52,468
52,547
52,548
52,653
52,653
System Cum.
Volume
Treated
Kgal
61,192
61,315
61,375
61,453
61,585
61,638
61,723
61,862
61,864
62,001
62,043
62,139
62,257
62,385
62,451
62,563
62,604
62,689
62,727
62,808
62,852
62,933
62,949
63,056
63,058
63,172
63,236
63,304
63,323
63,427
63,430
63,437
63,549
63,604
63,673
63,678
63,678
63,837
64,018
64,042
64,153
64,153
64,275
64,284
64,349
64,395
64,466
64,514
64,529
64,626
64,626
64,730
64,735
64,856
64,857
64,891
64,992
64,993
65,094
65,096
65,226
65,226
System
Total Bed
Volumes
Treated"1
BV
51,127
51,229
51,279
51,345
51,455
51,499
51,570
51,686
51,688
51,802
51,837
51,917
52,016
52,123
52,178
52,272
52,306
52,377
52,409
52,477
52,514
52,581
52,594
52,683
52,686
52,780
52,834
52,891
52,907
52,994
52,996
53,002
53,095
53,141
53,199
53,203
53,204
53,336
53,487
53,507
53,600
53,601
53,702
53,710
53,764
53,802
53,861
53,902
53,914
53,995
53,996
54,082
54,086
54,188
54,189
54,217
54,301
54,302
54,386
54,388
54,496
54,496
Vessel AP
(psil
A
10.8
3.2
3.2
5.0
7.2
7.7
9.0
11.0
11.0
10.4
10.0
13.0
11.8
11.5
12.0
2.9
NA
5.0
5.4
7.4
7.8
9.2
9.1
10.8
10.9
10.0
9.8
9.0
3.0
4.8
5.2
5.2
7.5
7.8
9.8
10.0
9.9
11.0
10.8
10.8
10.2
10.2
3.2
3.2
4.6
5.5
6.5
7.5
8.4
9.3
9.5
10.0
9.9
9.2
9.4
9.4
3.0
3.0
4.8
5.0
7.2
7.2
B
9.6
2.6
3.0
4.8
6.6
7.0
8.4
10.0
10.2
9.8
9.9
11.8
16.6
10.0
9.0
2.8
NA
5.0
5.0
7.0
7.2
8.0
8.9
9.8
10.3
10.0
9.2
8.6
2.6
4.8
4.8
5.0
2.0
6.8
9.0
9.4
9.5
10.6
10.4
10.2
9.6
9.6
2.6
2.8
4.6
5.0
6.0
6.8
7.6
8.2
9.1
9.2
9.8
9.0
9.0
9.0
2.6
2.4
4.2
4.4
6.2
6.2
System
ip
(psi)
psig
20
14
14
20
18
21
NA
22
20
20
20
20
20
20
20
14
NA
15
16
17
9
18
18
20
18
20
20
18
13
16
16
16
14
26
26
20
20
20
22
20
18
20
14
14
14
18
16
18
17
18
22
20
21
18
20
18
14
20
16
16
18
20
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
126
127
128
129
130
131
132
133
134
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
1 1/20/2007
1 1/21/2007
1 1/22/2007
1 1/23/2007
1 1/24/2007
1 1/25/2007
1 1/26/2006
1 1/27/2006
1 1/28/2006
1 1/29/2006
1 1/30/2006
12/1/2006
12/2/2006
12/3/2006
12/4/2006
12/5/2006
12/6/2006
12/7/2006
12/8/2006
12/9/2006
12/10/2006
12/11/2006
12/12/2006
12/13/2006
12/14/2006
12/15/2006
12/16/2006
12/17/2006
12/18/2006
12/19/2006
12/20/2006
12/21/2006
12/22/2006
12/23/2006
12/24/2006
12/25/2006
12/26/2006
12/27/2006
12/28/2006
12/29/2006
12/30/2006
12/31/2006
1/1/2007
1/2/2007
1/3/2007
1/4/2007
1/5/2007
1/6/2007
1/7/2007
1/8/2007
1/9/2007
1/10/2007
1/11/2007
1/12/2007
1/13/2007
1/14/2007
1/15/2007
1/16/2007
1/17/2007
1/18/2007
1/19/2007
1/20/2007
1/21/2007
Time
9:45
12:12
9:40
16:34
14:20
16:45
18:00
13:18
9:17
7:00
6:30
9:40
15:48
16:15
9:45
10:00
6:45
9:30
9:15
16:00
16:20
10:20
10:00
8:45
9:37
10:40
16:44
16:30
10:00
10:00
9:00
9:10
10:43
16:30
16:30
16:00
11:15
NM
9:20
11:00
17:00
16:30
21:30
10:10
9:45
9:40
9:50
17:00
17:00
13:30
13:00
9:35
13:30
13:22
16:25
17:00
16:30
9:30
9:20
14:00
13:30
16:20
17:00
Well House #1 Reading
Opt Hours
Well!
hr
0.4
9.4
0.1
9.1
1.3
8.4
1.5
7.9
0.2
4.2
7.4
0.1
8.1
0.0
8.5
0.4
0.0
9.3
0.1
9.9
5.0
5.4
0.2
2.8
7.0
0.3
8.6
0.0
NA
8.7
5.4
4.8
0.3
8.6
4.4
5.5
0.0
9.3
0.2
7.7
2.1
5.2
5.1
0.3
8.7
0.2
2.5
7.9
2.8
6.8
0.1
2.7
6.6
0.2
8.6
0.0
0.0
5.5
9.3
0.2
7.2
3.4
0.0
Daily Flow
Totalizer
aal
4,000
131,000
1,000
124,000
19,000
114,000
21 ,000
109,000
3,000
57,000
101,000
2,000
115,000
0
122,000
0
3,000
130,000
1,000
135,000
70,000
72,000
3,000
39,000
94,000
4,000
118,000
0
NA
145,000
49,000
64,000
6,000
120,000
63,000
75,000
2,000
128,000
3,000
106,000
28,000
72,000
70,000
5,000
121,000
2,000
35,000
111,000
40,000
94,000
2,000
38,000
92,000
2,000
119,000
NA
0
77,000
128,000
2,000
100,000
47,000
5,000
Avg
Flow rate
qpm
167
232
NA
227
244
226
NA
230
250
NA
227
333
237
NA
239
NA
NA
233
167
227
233
222
250
232
224
222
229
NA
NA
278
151
222
333
233
NA
227
NA
229
250
229
222
231
229
278
232
167
233
234
238
230
333
235
232
167
231
NA
NA
233
229
167
231
230
NA
APU
Electric
KWH
625.57
630.81
630.85
632.49
633.34
635.31
635.72
637.55
637.63
638.61
640.32
640.43
642.28
642.38
644.22
644.41
644.51
646.73
646.81
649.19
650.41
651.69
651.75
652.16
654.09
654.20
656.22
656.77
658.27
658.33
659.61
660.76
660.90
662.93
664.00
665.37
665.37
667.58
667.69
669.50
670.60
671.35
672.63
672.68
674.74
674.82
675.43
677.30
677.97
679.58
679.66
680.33
681 .96
682.04
684.09
684.15
684.19
685.42
687.63
687.78
689.53
690.39
690.61
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
qpm
NA
NA
NA
NA
NA
NA
NA
0.0
0.0
0.0
67.1
0.0
0.0
NA
0.0
0.0
88.0
83.0
78.1
79.2
75.0
77.6
86.1
80.1
87.2
84.6
85.7
85.7
77.6
86.1
93.9
117.3
122.4
113.0
110.0
90.0
109.2
99.9
99.2
99.9
113.4
95.0
89.4
110.3
106.0
102.4
112.4
110.8
100.0
116.1
126.1
109.5
122.2
117.5
112.3
110.0
110.6
108.1
108.3
112.1
113.2
120.1
120.0
Daily Flow
Totalizer
aal
2,568
60,348
642
58,422
8,346
53,928
9,630
50,718
1,284
26,964
47,508
642
52,002
0
54,570
2,568
965
44,880
998
49,661
16,842
24,039
953
12,743
31,414
1,394
39,320
0
14,176
26,711
25,288
25,036
2,400
54,618
27,326
32,444
359
55,041
1,471
42,917
11,388
30,812
30,849
400
51 ,224
1,104
14,806
49,935
18,614
43,768
863
16,825
42,313
775
54,991
712
573
35,480
59,436
1,038
46,012
21,098
0
Cum.
Flow
Totalizer
Kaal
33,719
33,779
33,780
33,838
33,846
33,900
33,910
33,961
33,962
33,989
34,036
34,037
34,089
34,089
34,144
34,146
34,147
34,192
34,193
34,243
34,259
34,283
34,284
34,297
34,329
34,330
34,369
34,369
34,369
34,396
34,421
34,446
34,449
34,503
34,531
34,563
34,563
34,619
34,620
34,663
34,674
34,705
34,736
34,736
34,788
34,789
34,803
34,853
34,872
34,916
34,917
34,933
34,976
34,977
35,032
35,032
35,033
35,068
35,128
35,129
35,175
35,196
35,196
Bed
Volume
Totalizer
BV
56,344
56,445
56,446
56,544
56,558
56,648
56,664
56,748
56,751
56,796
56,875
56,876
56,963
56,963
57,054
57,059
57,060
57,135
57,137
57,220
57,248
57,288
57,290
57,311
57,363
57,366
57,431
57,431
57,431
57,476
57,518
57,560
57,564
57,655
57,701
57,755
57,756
57,848
57,850
57,922
57,941
57,993
58,044
58,045
58,130
58,132
58,157
58,240
58,272
58,345
58,346
58,374
58,445
58,446
58,538
58,539
58,540
58,600
58,699
58,701
58,778
58,813
58,813
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
qpm
102.5
103.0
110.0
110.8
108.7
103.0
103.2
111.8
110.7
105.7
63.5
69.6
57.5
57.0
46.1
49.7
108.5
124.8
124.4
NA
115.0
111.3
119.1
126.1
125.4
126.2
126.3
126.3
111.3
111.8
112.8
79.9
94.9
90.0
85.0
100.0
95.6
94.5
99.9
103.6
112.4
100.0
94.8
96.8
98.4
97.5
102.5
103.4
100.0
98.5
104.6
91.4
100.9
99.5
93.9
95.0
90.0
91.1
85.3
83.7
97.2
98.7
98.5
Daily Flow
Totalizer
B
aal
894
56,857
4,180
50,519
8,051
50,271
9,253
46,513
812
23,971
30,753
2,000
27,662
27
25,605
49,885
5,963
6,961
1,350
68,583
31 ,543
38,319
1,938
19,414
47,630
2,157
57,643
200
71,018
22,070
348
29,637
1,739
47,180
24,957
30,790
298
54,252
1,436
43,780
11,736
30,408
29,811
430
48,541
1,047
13,785
43,337
14,929
36,470
716
14,156
35,752
139
46,381
566
460
28,426
46,709
847
37,282
17,949
0
Cum. Flow
Totalizer
B
Kqal
31,510
31 ,567
31,571
31 ,622
31 ,630
31,680
31 ,690
31,736
31,737
31,761
31,792
31,794
31,821
31,821
31,847
31,897
31,903
31,910
31,911
31,980
32,011
32,050
32,051
32,071
32,119
32,121
32,178
32,179
32,250
32,272
32,272
32,302
32,303
32,350
32,375
32,406
32,407
32,461
32,462
32,506
32,518
32,548
32,578
32,578
32,627
32,628
32,642
32,685
32,700
32,737
32,737
32,751
32,787
32,787
32,834
32,834
32,835
32,863
32,910
32,911
32,948
32,966
32,966
Bed
Volume
Totalizer
B
BV
52,654
52,749
52,756
52,841
52,854
52,938
52,954
53,031
53,033
53,073
53,124
53,128
53,174
53,174
53,217
53,300
53,310
53,322
53,324
53,438
53,491
53,555
53,558
53,591
53,670
53,674
53,770
53,771
53,889
53,926
53,927
53,976
53,979
54,058
54,100
54,151
54,152
54,242
54,245
54,318
54,338
54,388
54,438
54,439
54,520
54,522
54,545
54,617
54,642
54,703
54,704
54,728
54,788
54,788
54,865
54,866
54,867
54,915
54,993
54,994
55,056
55,086
55,086
System Cum.
Volume
Treated
Kqal
65,229
65,346
65,351
65,460
65,476
65,581
65,599
65,697
65,699
65,750
65,828
65,831
65,910
65,910
65,990
66,043
66,050
66,102
66,104
66,222
66,271
66,333
66,336
66,368
66,447
66,451
66,548
66,548
66,619
66,668
66,693
66,748
66,752
66,854
66,906
66,969
66,970
67,079
67,082
67,169
67,192
67,253
67,314
67,315
67,415
67,417
67,445
67,539
67,572
67,652
67,654
67,685
67,763
67,764
67,865
67,867
67,868
67,931
68,038
68,039
68,123
68,162
68,162
System
Total Bed
Volumes
Treated'"
BV
54,499
54,597
54,601
54,692
54,706
54,793
54,809
54,890
54,892
54,934
55,000
55,002
55,068
55,068
55,135
55,179
55,185
55,228
55,230
55,329
55,369
55,422
55,424
55,451
55,517
55,520
55,601
55,601
55,660
55,701
55,723
55,768
55,772
55,857
55,900
55,953
55,954
56,045
56,048
56,120
56,139
56,190
56,241
56,242
56,325
56,327
56,351
56,429
56,457
56,524
56,525
56,551
56,616
56,617
56,702
56,703
56,704
56,757
56,846
56,847
56,917
56,950
56,950
Vessel AP
(psi)
A
7.8
9.2
9.4
10.0
10.0
10.0
9.8
9.2
9.2
9.2
0.0
0.0
0.0
0.0
0.0
0.0
6.0
8.0
9.4
0.8
11.0
10.6
11.2
12.0
11.2
12.0
10.6
10.6
10.0
10.1
10.0
3.0
3.0
5.0
5.2
7.0
7.4
9.1
9.2
9.4
9.4
9.4
7.5
9.0
8.3
8.4
8.2
4.0
4.0
5.8
6.0
6.2
8.1
8.0
9.0
9.0
9.2
9.8
9.6
9.4
9.2
3.2
3.2
B
6.8
8.1
8.6
9.0
9.4
7.4
8.8
8.2
8.2
8.0
1.2
1.2
1.6
1.6
2.0
2.0
5.8
7.9
8.0
8.7
9.2
9.0
9.6
9.8
9.4
10.0
9.0
9.0
9.4
8.6
8.6
2.8
2.6
4.0
5.0
6.5
6.6
8.2
8.6
9.2
9.0
9.0
5.6
8.0
7.4
7.6
7.5
3.8
4.0
5.6
6.0
6.0
8.0
7.8
8.4
8.6
9.0
9.6
9.4
9.2
8.4
3.2
3.2
System
ip
(psi)
PSiq
20
18
20
19
21
19
19
18
18
19
12
10
12
9
10
15
15
20
20
20
20
20
20
20
20
22
19
19
14
20
18
12
16
16
17
17
18
19
20
23
22
22
7
8
8
8
8
6
6
•6
8
7
8
9
•9
9
6
9
0
9
8
15
16
System
Back-
wash
Yes/No
Yes
Yes
Yes
Yes
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
135
136
137
138
139
140
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
1/22/2007
1/23/2007
1/24/2007
1/25/2007
1/26/2007
1/27/2007
1/28/2007
1/29/2007
1/30/2007
1/31/2007
2/1/2007
2/2/2007
2/3/2007
2/4/2007
2/5/2007
2/6/2007
2/7/2007
2/8/2007
2/9/2007
2/10/2007
2/11/2007
2/12/2007
2/13/2007
2/14/2007
2/15/2007
2/16/2007
2/17/2007
2/18/2007
2/19/2007
2/20/2007
2/21/2007
2/22/2007
2/23/2007
2/24/2007
2/25/2007
2/26/2007
2/27/2007
2/28/2007
3/1/2007
3/2/2007
3/3/2007
3/4/2007
Time
9:39
9:46
9:36
9:30
13:30
17:00
16:30
7:00
6:49
9:06
9:24
19:25
16:35
16:25
16:00
13:44
9:33
9:25
10:25
1:30
17:05
9:20
9:40
10:00
10:00
9:13
17:08
16:30
16:20
14:06
13:38
13:00
13:15
16:35
16:45
9:45
10:10
9:46
16:00
12:55
16:59
16:30
Well House #1 Reading
Opt Hours
Well!
hr
9.0
0.2
0.3
9.3
0.3
8.3
2.0
1.3
8.1
0.4
0.7
9.3
0.3
9.2
0.1
6.4
5.7
0.5
8.9
10.3
0.0
0.3
8.4
0.3
9.1
0.1
10.8
5.6
5.4
6.1
3.8
6.6
3.6
10.4
0.0
0.2
9.5
0.1
5.3
5.0
3.1
6.5
Daily Flow
Totalizer
aal
123,000
2,000
4,000
129,000
5,000
113,000
20,000
9,000
129,000
5,000
9,000
129,000
4,000
126,000
2,000
89,000
81,000
6,000
125,000
141,000
0
5,000
117,000
3,000
126,000
2,000
151,000
80,000
73,000
86,000
51,000
92,000
49,000
143,000
0
3,000
132,000
2,000
74,000
72,000
43,000
90,000
Avg
Flowrate
QDm
228
167
222
231
278
227
167
115
265
208
214
231
222
228
333
232
237
200
234
228
NA
278
232
167
231
333
233
238
225
235
224
232
227
229
NA
250
232
333
233
240
231
231
APU
Electric
Meter
KWH
692.62
692.76
692.91
695.11
695.33
697.35
697.87
697.96
700.21
700.41
700.70
702.97
703.14
705.33
705.52
707.16
708.63
708.97
711.14
713.71
713.87
713.97
716.00
716.26
713.49
718.69
721.35
722.75
724.12
725.64
726.57
728.16
729.07
731.60
739.95
731.81
734.09
734.19
735.51
736.77
737.57
739.11
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
QDm
123.7
115.2
118.2
117.2
111.9
112.9
105.7
113.0
120.2
116.6
113.5
114.6
120.5
115.0
83.5
112.7
118.2
112.6
107.2
93.2
93.0
105.6
110.3
108.6
104.4
109.1
113.9
113.0
110.0
111.0
112.2
113.4
114.6
118.5
118.0
123.8
112.1
109.5
111.6
125.0
120.7
115.5
Daily Flow
Totalizer
A
aal
57,329
1,600
1,816
57,557
1,307
48,399
12,638
304
54,948
2,077
4,700
55,981
1,659
44,991
1,464
49,171
36,105
2,362
54,891
61,209
0
1,087
50,466
1,589
54,711
6,324
65,576
33,865
33,290
38,441
23,072
41,885
22,090
66,072
0
700
59,466
939
7,373
33,103
22,267
42,302
Cum.
Flow
Totalizer
A
Kaal
35,253
35,255
35,257
35,314
35,316
35,364
35,377
35,377
35,432
35,434
35,439
35,495
35,496
35,541
35,543
35,592
35,628
35,630
35,685
35,746
35,746
35,748
35,798
35,800
35,854
35,861
35,926
35,960
35,993
36,032
36,055
36,097
36,119
36,185
36,185
36,186
36,245
36,246
36,253
36,286
36,309
36,351
Bed
Volume
Totalizer
A
BV
58,909
58,911
58,914
59,010
59,013
59,094
59,115
59,115
59,207
59,210
59,218
59,312
59,315
59,390
59,392
59,474
59,535
59,539
59,630
59,733
59,733
59,735
59,819
59,821
59,913
59,923
60,033
60,090
60,145
60,210
60,248
60,318
60,355
60,465
60,465
60,467
60,566
60,567
60,580
60,635
60,672
60,743
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
QDm
101.6
107.5
107.6
102.2
105.2
105.7
102.2
98.7
101.1
101.4
101.9
109.7
106.7
130.0
98.2
102.0
104.3
103.7
96.9
88.5
88.0
93.4
94.7
95.6
94.2
104.2
86.3
85.0
90.0
100.3
99.2
98.5
99.4
87.6
87.0
101.9
96.6
99.3
83.7
71.4
87.1
85.0
Daily Flow
Totalizer
B
aal
47,151
3,481
1,531
51,323
1,000
45,888
11,993
303
52,098
1,958
3,797
50,710
1,484
49,700
1,322
33,481
31,035
2,106
49,252
57,026
0
1,032
46,407
1,370
49,760
904
57,638
28,367
28,549
32,948
25,129
29,617
18,437
53,752
0
592
49,082
781
5,917
23,008
16,101
31,617
Cum. Flow
Totalizer
B
Kaal
33,013
33,017
33,018
33,069
33,070
33,116
33,128
33,129
33,181
33,183
33,186
33,237
33,239
33,288
33,290
33,323
33,354
33,356
33,405
33,463
33,463
33,464
33,510
33,511
33,561
33,562
33,620
33,648
33,677
33,710
33,735
33,764
33,783
33,836
33,836
33,837
33,886
33,887
33,893
33,916
33,932
33,964
Bed
Volume
Totalizer
B
BV
55,165
55,171
55,174
55,259
55,261
55,338
55,358
55,358
55,445
55,449
55,455
55,540
55,542
55,625
55,627
55,683
55,735
55,739
55,821
55,916
55,916
55,918
55,996
55,998
56,081
56,082
56,179
56,226
56,274
56,329
56,371
56,420
56,451
56,541
56,541
56,542
56,624
56,625
56,635
56,674
56,701
56,753
System Cum.
Volume
Treated
Kaal
68,266
68,271
68,275
68,384
68,386
68,480
68,505
68,505
68,612
68,617
68,625
68,732
68,735
68,830
68,832
68,915
68,982
68,987
69,091
69,209
69,209
69,211
69,308
69,311
69,415
69,423
69,546
69,608
69,670
69,741
69,789
69,861
69,902
70,021
70,021
70,023
70,131
70,133
70,146
70,202
70,241
70,315
System
Total Bed
Volumes
Treated1"
BV
57,037
57,041
57,044
57,135
57,137
57,216
57,236
57,237
57,326
57,329
57,337
57,426
57,428
57,507
57,510
57,579
57,635
57,639
57,726
57,824
57,824
57,826
57,907
57,910
57,997
58,003
58,106
58,158
58,210
58,269
58,310
58,369
58,403
58,503
58,503
58,504
58,595
58,596
58,608
58,654
58,686
58,748
Vessel AP
(psi)
A
5.7
5.8
6.0
8.0
8.2
8.8
9.0
9.0
9.2
9.6
9.4
9.0
9.0
9.0
8.8
3.4
5.0
5.2
7.2
8.0
8.0
8.8
8.0
8.2
7.6
8.0
5.0
6.0
8.0
8.2
9.0
9.5
9.1
7.6
7.6
9.0
8.4
8.6
3.0
4.6
5.0
6.0
B
5.2
5.6
5.8
7.8
7.6
9.0
9.0
8.9
8.8
9.0
9.0
8.4
8.6
8.0
8.2
2.8
4.6
4.8
7.6
7.5
7.5
8.2
7.0
7.2
6.8
7.6
9.6
5.2
7.0
8.2
8.2
9.1
8.9
7.4
7.4
8.4
7.6
7.6
2.2
3.2
3.6
5.0
System
AP
(psi)
psia
16
17
18
15
18
18
12
19
19
19
20
19
21
21
18
16
14
18
18
18
17
18
18
19
18
18
16
17
20
19
20
18
20
19
19
20
18
18
15
16
16
18
System
Back-
wash
Yes/No
Yes
Yes
Yes
>
-------
US EPA Arsenic Demonstration Project at Stevensville - Daily System Operation Log Sheet (Continued)
Week
No.
141
142
143
144
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
3/5/2007
3/6/2007
3/7/2007
3/8/2007
3/9/2007
3/10/2007
3/11/2007
3/12/2007
3/13/2007
3/14/2007
3/15/2007
3/16/2007
3/17/2007
3/18/2007
3/19/2007
3/20/2007
3/21/2007
3/22/2007
3/23/2007
3/24/2007
3/25/2007
3/26/2007
3/27/2007
3/28/2007
3/29/2007
3/30/2007
3/31/2007
4/1/2007
Time
14:00
9:30
9:40
7:00
10:35
22:45
16:30
14:00
13:30
14:00
NM
14:00
22:20
16:30
13:00
14:45
11:00
13:10
9:25
16:50
17:30
9:10
14:20
NM
8:10
7:25
17:00
17:00
Well House #1 Reading
Opt Hours
Well!
hr
0.0
8.6
0.3
1.3
9.6
10.6
0.4
1.1
8.7
0.3
NA
6.7
13.1
1.8
8.2
0.0
9.5
0.1
8.7
0.2
8.1
2.6
1.0
NA
12.7
0.4
9.8
0.6
Daily Flow
Totalizer
gal
61,000
58,000
4,000
18,000
84,000
195,000
0
20,000
120,000
4,000
NA
135,000
140,000
36,000
105,000
1,000
131,000
1,000
121,000
4,000
112,000
37,000
13,000
NA
180,000
5,000
136,000
9,000
Avg
Flowrate
gpm
NA
112
222
231
146
307
303
230
222
NA
336
178
333
213
NA
230
167
232
333
230
237
217
NA
236
208
231
250
APU
Electric
Meter
KWH
739.20
741.26
741.42
741.83
744.15
746.68
746.81
747.10
749.15
749.25
NA
751.55
753.93
754.44
756.38
756.44
758.65
758.73
760.76
760.85
762.73
763.38
767.66
NA
766.66
766.78
769.10
769.27
Instrument Panel
Vessel A Flow Meter/Totalizer
Flow
Rate
for
Vesel
A
gpm
125.9
111.6
114.2
112.5
124.5
105.8
105.8
116.6
115.1
116.8
NA
120.6
116.1
110.6
112.6
112.9
113.7
115.2
110.8
116.9
110.0
109.1
NA
NA
0.0
0.0
0.0
0.0
Daily Flow
Totalizer
A
gal
303
55,195
1,260
10,095
60,327
65,502
0
9,558
52,614
3,782
NA
61,766
64,619
12,269
50,822
20,351
16,997
20,800
53,109
719
48,570
16,900
NA
NA
7,007
1
0
1
Cum.
Flow
Totalizer
A
Kgal
36,351
36,407
36,408
36,418
36,478
36,544
36,544
36,553
36,606
36,610
NA
36,671
36,736
36,748
36,799
36,820
36,837
36,857
36,910
36,911
36,960
36,977
NA
NA
36,984
36,984
36,984
36,984
Bed
Volume
Totalizer
A
BV
60,744
60,836
60,838
60,855
60,956
61,065
61,065
61,081
61,169
61,175
NA
61,278
61,386
61,407
61,492
61,526
61,554
61,589
61,678
61,679
61,760
61,788
NA
NA
61,800
61,800
61,800
61,800
Vessel B Flow Meter/Totalizer
Flow
Rate
for
Vessel
B
gpm
99.5
98.8
102.7
88.8
94.5
90.5
90.5
93.9
100.0
95.4
NA
95.9
87.7
85.0
99.1
94.0
94.2
103.8
101.8
103.5
97.0
98.0
NA
NA
94.3
99.9
98.2
98.0
Daily Flow
Totalizer
B
gal
261
43,877
1,147
8,208
48,355
54,581
0
9,723
41,909
1,503
NA
49,338
47,103
15,155
42,012
21,299
30,381
641
46,939
639
42,589
11,992
NA
NA
9,569
1,957
53,262
3,440
Cum. Flow
Totalizer
B
Kgal
33,964
34,008
34,009
34,017
34,065
34,120
34,120
34,130
34,172
34,173
NA
34,222
34,270
34,285
34,327
34,348
34,378
34,379
34,426
34,427
34,469
34,481
NA
NA
34,491
34,493
34,546
34,549
Bed
Volume
Totalizer
B
BV
56,754
56,827
56,829
56,843
56,924
57,015
57,015
57,031
57,101
57,104
NA
57,186
57,265
57,290
57,360
57,396
57,447
57,448
57,526
57,527
57,598
57,618
NA
NA
57,634
57,638
57,727
57,732
System Cum.
Volume
Treated
Kgal
70,315
70,414
70,417
70,435
70,544
70,664
70,664
70,683
70,778
70,783
NA
70,894
71,006
71,033
71,126
71,168
71,215
71,236
71,336
71,338
71,429
71,458
NA
NA
71,474
71,476
71,530
71,533
System
Total Bed
Volumes
Treated1"
BV
58,749
58,831
58,833
58,849
58,940
59,040
59,040
59,056
59,135
59,139
NA
59,232
59,326
59,349
59,426
59,461
59,500
59,518
59,602
59,603
59,679
59,703
NA
NA
59,717
59,719
59,763
59,766
Vessel AP
(psi)
A
7.4
9.2
9.0
9.0
8.9
10.0
10.0
10.4
9.8
9.8
NA
9.6
5.2
5.4
8.0
8.0
9.5
9.6
8.0
8.6
8.8
8.0
NA
NA
6.0
6.0
7.4
7.8
B
5.4
7.0
6.6
6.8
6.2
9.0
9.0
8.4
7.8
7.6
NA
7.0
5.0
5.2
7.0
7.2
9.0
8.9
7.0
7.0
7.0
7.0
NA
NA
5.4
5.6
6.8
7.0
System
AP
(psi)
psig
18
20
20
19
20
22
22
20
20
20
NA
22
15
16
18
20
20
20
18
18
18
18
NA
NA
16
18
18
19
System
Back-
wash
Yes/No
Yes
(a) Bed volume = 160 ft3, or 1 ,196.88 gallons total for both vessels
(b) Pre-chlorination started November 9, 2004
(c) System switched to post-chlorination on April 18, 2005 due to high pressure readings across the vessels and system switched back to pre-
chlorination on April 20, 2005.
(d) The power was shut off so the electric meter was re-set on September 6, 2005.
(e) MBF-122B valve on Vessel B was broken, therefore no flow went through vessel B and all flow went through vessel A on September 10 and
September 11, 2005.
(f) System back online December 13, 2005
(g) Totalizer for Vessel A networking since January 13, 2006. Therefore, starting January 13, 2006, cumulative volume treated and cumulative
bed volumes treated are calculated from the Well 1 flow totalizer.
(h) Totalizer for Vessel A was replaced and is working as of March 7, 2006.
>
NM = Not Measured
NA = Not Available
-------
APPENDIX B
ANALYTICAL DATA
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
rng/L*'
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L(a)
mg/L«
mg/L(a)
Hg/L
|xg/L
Hg/L
|xg/L
Hg/L
|xg/L
re/L
re/L
re/L
07/07/04
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/Lw
mg/L
mg/L
mg/L®
mg/L
mg/L
NTU
-
°C
mg/L
mV
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
08/31/04
IN
-
171
0.6
5.3
<0.10
14.6
<0.04
0.9
8.0
18.0
NA
-99
-
-
-
22.4
-
-
-
-
193
-
1.5
-
TA
5.5
171
0.6
5.3
<0.10
14.5
<0.04
0.3
8.0
17.9
NA
-10
-
-
-
8.6
-
-
-
-
<25
-
5.3
-
TB
5.7
171
0.7
<5.0
<0.10
14.4
<0.04
0.5
8.0
17.7
NA
53
-
-
-
5.9
-
-
-
-
<25
-
5.4
-
09/22/04(c)
IN
-
166
0.5
3.3
<0.06
14.7
<0.04
0.6
8.0
15.4
2.2
-14
112.4
66.6
45.8
20.6
20.9
<0.1
12.8/
12.3
8. 1/
7.6
271
161/
150
2.7
3.1
TT
7.4
166
0.6
3.4
<0.06
14.2
<0.04
0.1
8.1
15.5
3.8
-62
109.3
65.2
44.1
11.1
NA
-
10.2
-
<25
-
6.7
-
10/07/04
IN
-
166
166
0.7
0.9
-
<0.06
<0.06
14.5
14.2
-
0.8
0.7
8.0
15.4
2.2
-140
-
-
-
19.2
25.8
-
-
-
-
236
315
-
3.0
2.7
-
TA
8.2
166
162
0.8
0.9
-
<0.06
<0.06
14.3
14.2
-
0.3
0.5
8.2
15.4
0.8
-63
-
-
-
13.1
11.9
-
-
-
-
77
<25
-
17.9
6.8
-
TB
8.6
166
162
0.8
0.8
-
<0.06
<0.06
14.3
13.9
-
0.6
0.5
8.3
15.4
1.0
-44
-
-
-
9.2
12.1
-
-
-
-
<25
<25
-
6.2
9.6
-
10/19/04
IN
-
162
0.7
4.0
<0.06
14.4
<0.04
0.9
8.0
15.7
1.8
-126
110.3
55.8
54.5
18.4
-
-
14.9
-
208
-
1.5
-
TT
9.2
162
0.8
4.0
<0.06
14.3
<0.04
0.3
8.1
15.8
5.4
-76
114.8
62.3
52.5
13.2
-
-
13.1
-
<25
-
5.7
-
10/26/04
IN
-
164
0.5
4.0
<0.06
14.6
<0.04
0.5
7.7
14.9
1.6
-132
116.7
63.6
53.1
19.4
19.0
0.4
19.7
<0.1
210
180
1.5
1.6
TT
9.6
164
0.6
4.0
<0.06
14.4
<0.04
0.1
7.8
14.7
5.5
-74
111.0
57.9
53.1
13.3
13.1
0.2
13.2
<0.1
<25
<25
5.8
5.9
11/03/04
IN
-
164
0.6
-
<0.06
14.1
-
0.7
7.6
18.5
1.6
-148
-
-
-
20.2
-
-
-
-
273
-
1.6
-
TA
9.8
164
0.5
-
<0.06
14.2
-
0.4
7.6
18.4
2.6
-112
-
-
-
14.8
-
-
-
-
68
-
6.2
-
TB
10.2
164
0.5
-
<0.06
14.1
-
0.4
7.7
18.6
2.2
-83
-
-
-
12.9
-
-
-
-
38
-
6.4
-
(a) As CaCO3. (b) As PO4. (c) (/) indicates re-run data with original result/re-run result.
IN = inlet; TA = after vessel A; TB = after vessel B; TT = after vessels combined.
NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
N03-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
rng/L*'
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/Lw
Hg/L
re/L
re/L
|xg/L
Hg/L
re/L
Hg/L
re/L
Hg/L
1 l/09/04(c)
TT
10.1
152
0.6
3.1
<0.06
14.9
<0.04
0.3
7.8
18.0
5.8
286
-
-
98.8
56.6
42.2
14.7
14.6
0.1
14.8
<0.1
108
61
10.1
10.4
ll/16/04fe)
IN
-
176
0.7
1.5
<0.06
15.9
<0.04
3.0
7.7
18.4
4.7
160
-
-
98.6
50.2
48.4
19.0
19.0
<0.1
18.4
0.6
802/
775
777/
796
9.8
14.3
AC
-
176
0.7
2.7
<0.06
14.6
<0.04
0.5
NA(d)
NA(d)
NA(d)
NA(d)
-
-
95.5
48.4
47.1
19.9
12.2
7.7
0.2
12.0
268
<25
2.1
0.3
TT
10.5
164
0.7
3.1
<0.06
15.4
<0.04
0.4
7.7
17.9
2.1
126
-
-
92.5
47.7
44.8
12.0
11.9
0.1
10.4
1.5
<25
<25
11.5
11.2
11/23/04
TT
10.7
162
0.8
3.5
<0.06
15.4
<0.04
0.1
NA(d)
NA(d)
NA(d)
NA(d)
-
-
111.9
66.1
45.8
0.9
0.9
<0.1
0.4
0.5
<25
<25
4.3
4.1
12/01/04 (e)(g)
IN
-
158
162
0.8
0.9
-
<0.06
<0.06
14.6
14.3
-
1.5
1.1
7.4
15.2
4.2
101
-
-
-
-
-
18.3
18.8
-
-
-
-
261
264
-
2.6
2.6
-
AC
-
154
162
1.1
0.9
-
1.6®/4.1
1.3®
14.3
14.4
-
0.2
0.1
NA(d)
NA(d)
NA(d)
NA(d)
-
-
-
-
-
0.4
0.4
-
-
-
-
<25
<25
-
2.5
2.5
-
TA
11.2
154
162
1.0
0.2
-
<0.06
<0.06
14.6
14.5
-
0.1
0.2
7.4
15.5
1.7
114
-
-
-
-
-
0.4
0.4
-
-
-
-
<25
<25
-
2.0
2.1
-
TB
11.2
154
162
0.8
0.9
-
<0.06
<0.06
14.6
14.8
-
0.2
0.1
7.2
15.5
1.4
120
-
-
-
-
-
0.3
0.3
-
-
-
-
<25
<25
-
3.0
3.0
-
12/07/04(g)
AC
-
166
0.9
6.0
<0.06
15.0
<0.04
0.3
NA(d)
NA(d)
NA(d)
NA(d)
-
-
96.4
54.8
41.6
22.1
15.2
6.9
1.6
13.6
212
<25
1.5
0.2
TT
11.3
166
0.8
6.0
<0.06
14.8
<0.04
0.2
NA(d)
NA(d)
NA(d)
NA(d)
-
-
112.1
67.5
44.6
0.6
0.7
<0.1
1.3/
<0.1
<0.1
<25
<25
2.0
1.9
12/15/04(g)
IN
-
163
0.8
3.7
<0.06
15.8
<0.04
0.5
8.1
15.2
5.5
-119
-
-
114.4
67.3
47.1
20.0
20.0
<0.1
20.3
<0.1
229
156
2.5
2.1
AC
-
167
0.9
3.7
<0.06
14.9
<0.04
0.6
7.8
14.9
NA(d)
NA(d)
0.4
0.1
113.3
66.7
46.6
18.8
19.0
<0.1
<0.1
18.0
229
173/
179
1.6
1.7
TT
11.7
163
0.9
3.7
<0.06
14.7
<0.04
0.2
7.3
15.5
5.6
88
-
-
107.8
63.9
43.9
0.3
0.2
<0.1
0.5
<0.1
<25
<25
2.0
1.5
(a) As CaCO3. (b) As PO4. (c) Pre-chlorination started November 9, 2004. (d) Weekly onsite water quality parameters not measured, (e) Weekly onsite water quality parameters measured on
December 2, 2004. ORP measured on December 3, 2004. (f) Samples were analyzed outside of hold time, (g) (/) indicates re-run data with original result/re-run result.
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B; TT = after vessels combined.
NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/Lw
mg/L
mg/L
mg/Lw
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(!l)
mg/L(!l)
mg/L(!l)
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
01/04/05(c)
IN
-
165
0.8
-
<0.06
15.2
-
0.6
7.4
15.8
3.3
-116
-
-
-
-
-
16.0
-
-
-
-
239
-
1.7
-
AC
-
-
-
-
-
-
-
-
-
-
-
-
0.04
0.0
-
-
-
-
-
-
-
-
-
-
-
-
TA
12.8
160
0.7
-
<0.06
15.2
-
0.2
7.2
16.1
1.4
84
-
-
-
-
-
1.2
-
-
-
-
<25
-
1.3
-
TB
12.6
165
0.7
-
<0.06
15.3
-
0.1
7.7
16.0
1.3
83
-
-
-
-
-
0.4
-
-
-
-
<25
-
2.6
-
01/ll/05(c)
AC
-
170
0.9
4.0
<0.06
15.0
<0.05
<0.1
7.7
17.4
1.6
256
1.1
1.4
97.3
57.8
39.5
18.7
12.8
5.9
0.3
12.5
241
<25
1.6
0.1
TT
12.8
161
0.9
4.0
<0.06
14.8
<0.05
0.2
7.7
17.6
4.4
294
-
-
92.9
56.7
36.2
0.4
0.2
0.2
0.4
<0.1
<25
<25
1.2
1.2
01/20/05
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
rag/I*'
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
02/15/05(c)
IN
-
187
0.8
4.0
<0.05
15.3
0.1
0.9
8.1
16.3
4.3
9
-
-
106.3
66.2
40.1
21.7
21.7
<0.1
22.7
<0.1
377
398
4.1
4.2
AC
-
174
0.9
4.0
<0.05
15.0
<0.05
0.3
7.9
14.4
1.1
557
0.7
2.2
100.4
59.0
41.4
21.8
11.9
9.9
0.5
11.4
313
<25
1.6
0.3
TT
14.3
178
0.8
4.0
<0.05
15.2
0.1
<0.1
7.8
15.1
3.8
612
-
-
99.1
56.5
42.6
0.5
0.2
0.3
0.4
<0.1
<25
<25
<0.1
0.2
03/02/05
IN
-
174
174
0.8
0.9
-
<0.05
<0.05
15.0
15.2
-
0.7
0.7
7.9
14.3
5.4
-87
-
-
-
-
-
21.6
21.4
-
-
-
-
327
297
-
3.0
2.5
-
AC
-
161
161
0.8
0.8
-
<0.05
<0.05
14.9
15.1
-
0.1
0.1
7.6
15.2
2.1
603
1.0
1.2
-
-
-
21.8
21.6
-
-
-
-
228
224
-
3.3
2.0
-
TA
15.5
178
174
0.8
0.8
-
<0.05
<0.05
14.9
15.1
-
<0.1
<0.1
7.5
15.4
1.3
592
-
-
-
-
-
0.8
0.6
-
-
-
-
<25
<25
-
0.5
<0.1
-
TB
14.8
165
169
0.8
0.8
-
<0.05
<0.05
15.1
15.0
-
<0.1
<0.1
7.5
15.5
1.1
614
-
-
-
-
-
0.4
0.4
-
-
-
-
<25
<25
-
0.1
<0.1
-
03/16/05
IN
-
183
0.8
4.0
<0.05
15.1
<0.05
0.8
7.8
15.3
5.8
-73
-
-
103.2
59.0
44.2
22.1
21.8
0.3
22.5
<0.1
458
495
4.0
5.3
AC
-
183
0.8
4.0
<0.05
14.9
<0.05
0.3
7.6
15.2
2.0
60
0.9
1.3
103.5
60.1
43.4
20.8
14.4
6.4
0.5
13.9
309
<25
2.2
0.3
TT
15.6
178
0.8
4.0
<0.05
14.7
<0.05
0.3
7.6
15.5
5.6
-10
-
-
101.2
55.6
45.6
0.7
0.6
1.7
0.6
<0.1
<25
<25
8.5
<0.1
03/31/05
IN
-
167
0.9
-
<0.05
14.9
-
1.6
7.4
15.0
2.8
213
-
-
-
-
-
18.1
-
-
-
-
230
-
1.7
-
AC
-
176
0.9
-
<0.05
15.0
-
0.6
7.5
15.3
3.2
215
0.1
1.4
-
-
-
17.2
-
-
-
-
239
-
1.8
-
TA
16.9
158
0.9
-
<0.05
15.0
-
0.3
7.4
15.2
2.9
212
-
-
-
-
-
0.7
-
-
-
-
<25
-
<0.1
-
TB
15.9
167
1.0
-
<0.05
14.7
-
<0.1
7.5
15.3
3.0
213
-
-
-
-
-
0.4
-
-
-
-
<25
-
<0.1
-
(a) As CaCO3. (b) As PO4. (c) Onsite water
IN = inlet; AC = after pre-chlorination; TA =
quality parameters taken on February 10, 2005.
after vessel A; TB = after vessel B; TT = after vessels combined. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/Lw
mg/L
mg/L
mg/L*'
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L«
mg/L«
re/L
Hg/L
re/L
re/L
re/L
^g/L
Hg/L
Hg/L
^g/L
04/13/05
IN
-
178
0.7
3.3
<0.05
15.6
<0.05
0.5
8.0
15.0
5.6
-80
-
-
99.7
58.1
41.6
17.6
17.8
<0.1
18.1
<0.1
267
218
1.7
1.7
AC
-
178
0.7
3.4
<0.05
15.2
<0.05
0.4
7.9
14.9
3.2
307
0.2
1.4
98.7
57.4
41.3
17.3
12.4
4.9
0.4
12.0
281
32
1.6
0.3
TT
16.9
178
0.7
3.1
<0.05
15.6
0.6
0.3
8.3
14.8
4.2
313
-
-
96.8
56.3
40.5
0.6
0.6
<0.1
0.4
0.2
<25
<25
0.1
<0.1
04/25/05
IN
-
178
0.8
-
<0.05
15.4
-
0.4
7.7
14.6
6.1
-62
-
-
-
-
-
19.9
-
-
-
-
208
-
1.3
-
AC
-
186
0.8
-
<0.05
14.8
-
0.3
7.6
15.2
3.3
-50
0.8
1.0
-
-
-
19.9
-
-
-
-
223
-
1.4
-
TA
18.4
182
0.8
-
<0.05
15.2
-
0.1
7.6
15.4
2.5
-43
-
-
-
-
-
0.9
-
-
-
-
30
-
0.3
-
TB
17.0
178
0.8
-
<0.05
14.8
-
<0.1
7.5
15.3
2.2
-44
-
-
-
-
-
0.6
-
-
-
-
<25
-
<0.1
-
05/ll/05(c)
IN
-
198
0.8
4.2
<0.05
15.3
<0.05
0.7
7.7
16.1
3.1
220
-
-
97.9
57.6
40.3
18.2
18.7
<0.1
19.4
<0.1
304
249
2.3
2.7
AC
-
185
0.8
4.3
<0.05
14.7
<0.05
0.8
7.6
15.6
2.1
210
0.4
0.5
101.0
58.7
42.0
19. 1/
20.3
18.7/
20.8
0.4/
<0.1
18.6/
20.0
O.I/
0.8
258/
202
204/
200
1.91
1.8
1.91
2.0
TT
18.5
176
0.8
4.3
<0.05
15
<0.05
0.3
7.5
15.2
2.1
166
-
-
95.7
55.1
40.6
1.11
1.1
1.51
1.6
6.2/
6.1
0.3/
0.5
1.2/
1.1
361/
293
<25/
<25
1.91
1.8
0.3/
0.3
05/24/05
IN
-
178
183
0.8
0.8
-
<0.05
<0.05
8.6
14.4
-
0.5
0.5
7.6
15.4
4.2
21
-
-
-
-
-
20.1
19.3
-
-
-
-
204
197
-
1.4
1.5
-
AC
-
183
178
0.8
0.8
-
<0.05
<0.05
14.2
14.7
-
0.2
0.3
7.6
15.5
4.1
165
0.5
0.7
-
-
-
19.6
20.4
-
-
-
-
208
242
-
1.5
1.5
-
TA
20.4
183
178
0.8
0.8
-
<0.05
<0.05
14.4
14.4
-
0.4
0.4
7.5
15.3
4.6
201
-
-
-
-
-
1.3
1.0
-
-
-
-
<25
<25
-
<0.1
<0.1
-
TB
18.5
178
178
0.8
0.8
-
<0.05
<0.05
14.2
14.4
-
0.2
0.4
7.5
15.5
3.2
220
-
-
-
-
-
0.7
0.4
-
-
-
-
<25
<25
-
<0.1
<0.1
-
(a) As CaCO3. (b) As PO4. (c) (/) indicates re-run data with original result/re-run result.
-------
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B; TT = after vessels combined. NA = data not available.
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/Lw
mg/L
mg/L
mg/L*'
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/Lw
mg/Lw
re/L
re/L
re/L
|xg/L
re/L
|xg/L
|xg/L
|xg/L
|xg/L
06/09/05
IN
-
176
0.8
-
<0.05
15.0
-
1.2
8.0
20.0
NA(C)
NA(C)
-
-
-
-
-
19.0
-
-
-
-
239
-
1.7
-
AC
-
176
0.8
-
<0.05
15.3
-
0.4
7.8
16.0
NA(C)
NA(C)
0.6
0.3
-
-
-
18.8
-
-
-
-
224
-
1.6
-
TA
21.6
176
0.8
-
<0.05
15.5
-
0.3
7.9
16.4
NA(C)
NA(C)
-
-
-
-
-
1.1
-
-
-
-
<25
-
0.1
-
TB
19.3
176
0.8
-
<0.05
15.3
-
0.2
7.9
16.2
NA(C)
NA(C)
-
-
-
-
-
0.6
-
-
-
-
<25
-
0.1
-
06/22/05
IN
-
176
0.8
4
<0.05
14.8
<0.05
1.1
8.1
16.4
7.1
-91
-
-
95.9
56.1
39.7
20.8
20.2
0.6
21.4
<0.1
228
197
1.7
1.6
AC
-
176
0.8
5
<0.05
14.8
<0.05
0.6
7.7
15.8
3.3
450
0.3
0.5
98.1
57.6
40.4
22.2
14.4
7.8
0.6
13.8
333
<25
1.7
0.5
TT
21.5
176
0.8
4
<0.05
15.0
<0.05
0.6
7.7
15.8
6.1
435
-
-
97.4
55.2
42.2
1.0
1.0
<0.1
0.6
0.4
<25
<25
0.9
1.0
07/05/05(tl)
IN
-
185
0.8
-
<0.05
15.3
-
0.5
8.1
16.8
4.3
-29
-
-
-
-
-
18.3
-
-
-
-
205
-
1.6
-
AC
-
180
0.8
-
<0.05
15.2
-
1.5
8.1
17.4
3.2
304
0.1
1.4
-
-
-
17.7
-
-
-
-
209
-
1.5
-
TA
24.9
180
0.8
-
<0.05
15.3
-
0.6
7.9
17.6
1.5
368
-
-
-
-
-
1.8
-
-
-
-
<25
-
1.2
-
TB
21.7
176
0.8
-
<0.05
14.9
-
0.2
7.9
17.4
1.4
383
-
-
-
-
-
0.9
-
-
-
-
<25
-
0.6
-
07/19/05
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L«
mg/L
mg/L
mg/L*'
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L«
mg/L«
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
08/03/05
IN
-
163
0.8
-
<0.05
14.4
-
1.3
7.8
17.3
6.6
-103
-
-
-
-
-
18.9
-
-
-
-
473
-
2.7
-
AC
-
167
0.8
-
<0.05
14.2
-
0.9
7.5
17.3
2.9
-144
0.1
0.2
-
-
-
19.3
-
-
-
-
304
-
2.1
-
TA
27.3
167
0.8
-
<0.05
14.4
-
0.2
7.5
17.2
3.1
-23
-
-
-
-
-
3.1
-
-
-
-
<25
-
0.8
-
TB
23.8
172
0.8
-
<0.05
14.1
-
<0.1
7.6
17.2
2.6
-3
-
-
-
-
-
1.0
-
-
-
-
<25
-
0.3
-
PT
-
-
-
-
-
-
-
-
7.4
17.0
-
-
0.1
0.3
-
-
-
-
-
-
-
-
-
-
-
-
08/16/05(c)
IN
-
172
0.8
4
<0.05
15.2
0.1
0.4
7.1
16.9
5.1
-121
-
-
107.0
58.7
48.4
19.7
19.1
0.6
19.6
<0.1
211
157
1.5
1.7
AC
-
167
0.8
4
<0.05
15.1
0.4
0.9
7.6
16.9
2.1
-143
0.1
0.0
102.0
57.2
44.9
18.5
18.5
<0.1
18.7
<0.1
219
189
1.6
1.7
TT
26.2
167
0.8
4
<0.05
14.7
<0.05
0.1
7.4
16.2
4.2
30
-
-
160.0
90.0
70.0
3.0
2.0
1.0
1.3
0.7
<25
<25
1.1
0.7
PT
-
-
-
-
-
-
-
-
7.4
16.9
-
-
0.2
0.8
-
-
-
-
-
-
-
-
-
-
-
-
08/30/05
IN
-
167
0.9
-
<0.05
23.4
-
0.3
8.1
17.1
4.7
-120
-
-
-
-
-
18.6
-
-
-
-
220
-
1.5
-
AC
-
154
0.8
-
<0.05
18.8
-
0.2
7.7
16.8
2.3
326
0.2
1.6
-
-
-
19.2
-
-
-
-
222
-
1.4
-
TA
29.4
167
0.8
-
<0.05
18.5
-
<0.1
7.9
18.0
1.1
394
-
-
-
-
-
1.9
-
-
-
-
<25
-
0.7
-
TB
25.7
167
0.8
-
<0.05
18.9
-
0.5
7.9
18.5
1.3
395
-
-
-
-
-
1.1
-
-
-
-
<25
-
0.7
-
PT
-
-
-
-
-
-
-
-
7.6
16.8
-
-
0.1
1.1
-
-
-
-
-
-
-
-
-
-
-
-
(a) As CaCO3. (b) As PO4. (c) Onsite water quality measurements taken on August 15, 2005.
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B; TT = after vessels combined; PT = plant tap after adsorption vessels. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Cd
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Orthophosphate
Total P (as P)
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L*'
Hg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
re/L
re/L
re/L
re/L
re/L
|xg/L
|xg/L
|xg/L
|xg/L
09/21/05
IN
-
167
0.8
4.0
<0.05
-
11.9
<0.05
0.6
8.1
16.4
5.6
-122
-
-
90.9
53.9
37.0
18.0
18.2
<0.1
17.0
1.2
205
45
1.4
1.6
AC
-
176
0.8
4.0
<0.05
-
12.0
<0.05
0.7
8.0
16.2
4.4
-136
0.2
0.0
95.9
56.6
39.3
18.0
18.4
<0.1
18.2
0.2
210
196
1.5
1.7
TT
29.4
176
0.8
4.0
<0.05
-
11.9
<0.05
0.3
8.0
16.1
5.3
76
-
-
95.7
55.1
40.6
2.0
2.1
<0.1
0.9
1.2
<25
<25
0.4
0.4
PT
-
-
-
-
-
-
-
-
-
7.8
16.6
-
-
0.1
1.2
-
-
-
-
-
-
-
-
-
-
-
-
10/05/05
IN
-
158
0.8
3.7
<0.05
-
13.7
0.2
0.4
7.5
16.0
6.1
190
-
-
-
-
-
16.7
-
-
-
-
223
-
1.2
-
AC
-
167
0.8
3.7
<0.05
-
15.2
0.2
0.2
7.7
16.1
4.8
246
0.0
0.0
-
-
-
16.8
-
-
-
-
214
-
1.2
-
TA
33.0
176
0.8
3.7
<0.05
-
14.3
<0.05
<0.1
7.3
16.2
2.5
225
-
-
-
-
-
6.1
-
-
-
-
<25
-
1.3
-
TB
28.7
176
0.8
3.7
<0.05
-
13.7
<0.05
0.3
7.3
16.5
1.6
211
-
-
-
-
-
2.3
-
-
-
-
<25
-
0.2
-
PT
-
-
-
-
-
-
-
-
-
7.1
15.9
-
-
0.1
2.1
-
-
-
-
-
-
-
-
-
-
-
-
10/12/05
IN
-
176
0.8
3.8
-
19.0
13.3
<0.05
0.4
8.1
15.9
5.0
42
-
-
100
57.2
43.1
25.2
26.0
<0.1
15.7
10.3
217
251
1.6
1.6
AC
-
172
0.8
3.8
-
19.1
14.5
<0.05
0.3
8.0
15.9
2.6
503
0.3
0.8
99.4
57.0
42.5
21.5
12.3
9.2
0.4
11.9
210
<25
1.6
0.2
TT
31.1
167
0.8
3.8
-
<10.0
14.3
<0.05
<0.1
7.8
15.7
4.3
539
-
-
98.8
56.6
42.1
1.8
1.7
0.1
0.4
1.2
<25
<25
1.6
1.5
PT
-
-
-
-
-
-
-
-
-
7.7
15.8
-
-
0.1
0.7
-
-
-
-
-
-
-
-
-
-
-
-
(a)AsCaCO3. (b) As PO4.
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B; TT = after vessels combined; PT = plant tap after adsorption vessels. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Cd
o
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Total P (as P)
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L«
mg/L
mg/L
Hg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Total P (as P)
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
Hg/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
jjg/L
jjg/L
jjg/L
jjg/L
jjg/L
re/L
re/L
re/L
os/os/oe90
IN
-
174
0.8
4.1
14.7
14.0
<0.05
5.4
7.6
15.3
4.4
-2
-
-
101
57.0
44.0
19.4
19.2
0.2
20.3
<0.1
212
209
1.7
1.6
AC
-
166
0.8
4.1
23.6
14.3
<0.05
7.3
7.6
15.3
3.7
180
0.3
0.4
102
57.9
44.0
21.6
12.8
8.8
0.4
12.4
233
<25
1.7
0.4
TT
35.8
166
0.8
4.1
<10.0
14.3
<0.05
4.2
7.5
NA
2.1
222
-
-
101
58.0
43.5
1.9
1.7
0.1
0.4
1.3
<25
<25
<0.1
0.1
PT
-
-
-
-
-
-
-
-
7.5
15.5
-
-
0.3
0.4
-
-
-
-
-
-
-
-
-
-
-
-
04/10/06
IN
-
167
0.9
4.5
18.1
14.1
<0.05
2.4
7.7
15.1
4.1
-79
-
-
95.4
57.9
37.5
18.9
18.2
0.7
17.9
0.3
280
163
4.8
3.4
AC
-
163
0.9
4.5
14.6
13.8
<0.05
1.1
7.6
15.2
3.1
74
0.4
0.5
96.3
58.5
37.8
18.6
12.5
6.0
0.2
12.3
218
<25
3.6
0.8
TT
37.9
158
0.9
4.4
<10.0
13.6
<0.05
0.6
7.6
15.3
3.1
141
-
-
91.9
55.5
36.3
1.8
1.6
0.1
0.2
1.4
<25
<25
<0.1
<0.1
PT
-
-
-
-
-
-
-
-
7.5
15.2
-
-
0.2
0.3
-
-
-
-
-
-
-
-
-
-
-
-
5/05/06
IN
-
167
0.9
-
18.1
14.7
-
0.9
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
-
-
20.1
-
-
-
-
194
-
1.5
-
AC
-
158
0.9
-
20.2
15.2
-
0.9
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
20.2
-
-
-
-
191
-
1.5
-
TA
-
167
0.9
-
24.1
15.3
-
1
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
-
-
6.8
-
-
-
-
<25
-
0.7
-
TB
37.2
167
0.8
-
<10.0
15.1
-
0.9
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
-
-
3.8
-
-
-
-
<25
-
0.5
-
PT
-
-
-
-
-
-
-
-
NA(C)
NA(C)
-
-
NA(C)
NA(C)
-
-
-
-
-
-
-
-
-
-
-
-
(a) As CaCO3. (b) Samples were taken on 03/05/06 and did not arrive to the laboratories until the 03/07/06. Therefore some analytes may be out of hold time, (c) Water quality
parameters not taken.
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B; TT = after vessels combined; PT = plant tap after adsorption vessels. NA = data not available.
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Total P (as P)
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L«
mg/L
mg/L
Hg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L«
mg/L«
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
5/17/06
IN
-
171
0.7
4.0
<10.0
15.4
<0.05
0.8
7.6
15.6
4.1
-40
-
-
98.3
54.7
43.6
21.4
21.4
<0.1
19.7
1.7
294
279
2.0
1.9
AC
-
171
0.7
4.0
<10.0
14.6
<0.05
0.7
7.6
15.5
5.2
-64
0.2
0.3
101
56.8
43.9
21.2
21.1
0.1
20.0
1.1
258
250
1.6
1.6
TA
-
-
-
-
-
-
-
-
7.6
15.4
4.7
-71
-
-
-
-
-
-
-
-
-
-
-
-
-
-
TB
38.1
-
-
-
-
-
-
-
7.6
15.4
5.1
-94
-
-
-
-
-
-
-
-
-
-
-
-
-
-
TT
40.1
159
0.8
4.0
<10.0
15.4
<0.05
0.8
7.6
15.4
6.1
-110
-
-
97.1
54.7
42.4
4.4
4.6
<0.1
1.8
2.7
<25
<25
<0.1
<0.1
PT
-
-
-
-
-
-
-
-
7.5
15.5
-
-
0.2
0.3
-
-
-
-
-
-
-
-
-
-
-
-
06/28/06
IN
-
167
0.7
4.0
17.0
15.3
<0.05
0.8
NA*'
NA(b)
NA*'
NA*'
-
-
103
58.9
43.8
21.2
19.8
1.4
17.6
2.1
424
376
4.7
3.9
AC
-
167
0.8
4.0
16.9
14.7
<0.05
0.7
NA*'
NA(b)
NA®
NAW
-
-
102
58.1
43.5
20.8
14.1
6.7
0.1
14.0
237
30.9
2.0
0.4
TT
44.0
167
0.8
4.0
<10.0
14.7
<0.05
0.7
NAW
NA(b)
NAW
NA*'
-
-
100
56.6
43.5
3.2
3.1
0.1
0.1
3.0
<25
<25
0.7
0.1
PT
-
-
-
-
-
-
-
-
NAW
NA(b)
-
-
NA*'
NA*'
-
-
-
-
-
-
-
-
-
-
-
-
07/23/06
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Total P (as P)
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/Lw
mg/L
mg/L
Hg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/Lw
mg/L(a)
mg/L(a)
jjg/L
jjg/L
re/L
re/L
re/L
re/L
re/L
re/L
jjg/L
08/16/06
IN
-
-
-
-
28.2
-
-
-
NA90
NA*'
NA*'
NA*'
-
-
99.2
60.1
39.1
22.8
21.4
1.4
20.9
0.6
206
202
1.6
1.5
AC
-
-
-
-
19.7
-
-
-
NA*'
NAW
NA*'
NAW
-
-
102
61.4
40.3
22.9
20.8
2.1
20.9
<0.1
206
198
1.4
1.4
TT
48.3
-
-
-
11.0
-
-
-
NA*'
NAW
NA*'
NA*'
-
-
95.5
57.2
38.2
6.7
6.6
0.1
2.3
4.2
<25
<25
0.2
0.2
PT
-
-
-
-
-
-
-
-
NA*'
NA*'
-
-
NA90
NA*'
-
-
-
-
-
-
-
-
-
-
-
-
09/19/06
IN
-
-
-
-
13.3
-
-
-
7.5
18.8
6.4
220
-
-
101
56.1
45.2
21.1
20.7
0.5
18.4
2.3
215
207
1.8
1.6
AC
-
-
-
-
18.6
-
-
-
7.5
18.6
4.4
205
-
-
106
59.7
46.4
21.3
13.9
7.4
0.5
13.4
212
<25
1.7
0.4
TT
51.2
-
-
-
<10.0
-
-
-
7.5
18.5
4.1
110
-
-
108
60.8
47.7
6.9
6.9
<0.1
1.2
5.7
<25
<25
0.7
0.8
PT
-
-
-
-
-
-
-
-
7.5
18.5
-
-
0.1
0.3
-
-
-
-
-
-
-
-
-
-
-
-
10/17/06
IN
-
-
-
-
-
-
-
-
7.6
15.9
4.4
120
-
-
-
-
-
23.2
20.8
2.4
18.4
2.4
232
222
1.6
1.7
AC
-
-
-
-
-
-
-
-
7.5
15.9
3.1
118
-
-
-
-
-
21.8
20.4
1.4
19.0
1.4
224
209
1.4
1.6
TT
52.9
-
-
-
-
-
-
-
7.5
16.1
1.7
80
-
-
-
-
-
5.9
6.0
<0.1
1.1
4.8
<25
<25
0.3
0.4
PT
-
-
-
-
-
-
-
-
7.5
16.1
-
-
0.1
0.2
-
-
-
-
-
-
-
-
-
-
-
-
(a) As CaCO3. (b) Water quality parameters not taken.
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B;
available.
TT = after vessels combined; PT = plant tap after adsorption vessels. NA = data not
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Cd
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Total P (as P)
Silica (as SiO2)
NO3-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L«
mg/L
mg/L
Hg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L«
mg/L
-------
Table B-l. Analytical Results from Long-Term Sampling, Stevensville, MD (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Total P (as PO4)
Silica (as SiO2)
N03-(N)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (total soluble)
As (particulate)
As (III)
As(V)
Total Fe
Dissolved Fe
Total Mn
Dissolved Mn
103
mg/L(a)
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
-
°C
mg/L
mV
mg/L
mg/L
mg/L(a)
mg/L«
mg/L(a)
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
03/07/07
IN
-
-
-
-
-
-
-
-
7.5
15.1
4.5
-40
-
-
-
-
-
21.5
19.7
1.8
15.2
4.5
211
65.2
2.5
1.6
AC
-
-
-
-
-
-
-
-
7.5
15
3.3
-22
-
-
-
20.8
21.0
<0.1
19.4
1.6
191
192
1.6
1.6
TT
58.8
-
-
-
-
-
-
-
7.5
15
2.7
-61
-
-
-
-
-
4.1
4.3
<0.1
<0.1
4.2
<25
<25
<0.1
<0.1
PT
-
-
-
-
-
-
-
-
7.5
15
-
-
0.2
0.4
-
-
-
04/02/07
IN
-
-
-
-
-
-
-
-
7.6
16.4
6.4
-40
-
-
-
-
-
21.5
20.3
1.1
17.7
2.7
208
208
1.6
1.6
AC
-
-
-
-
-
-
-
-
7.5
16.2
5.2
-60
0.2
0.2
-
-
-
20.8
13.9
6.9
0.6
13.3
196
<25
1.3
0.3
TT
59.8
-
-
-
-
-
-
-
7.5
16.1
3.8
-86
-
-
-
-
-
4.7
4.6
<0.1
0.4
4.2
<25
<25
<0.1
<0.1
PT
-
-
-
-
-
-
-
-
7.5
16.1
-
-
0.2
0.3
-
-
-
-
-
-
-
-
-
-
-
-
(a) As CaCO3.
IN = inlet; AC = after pre-chlorination; TA = after vessel A; TB = after vessel B; TT = after vessels combined; PT = plant tap
after adsorption vessels. NA = data not available.
------- |