NC0004375_Report_19991102

NPDES DOCUMENT SCANNING COVER SHEET
NPDES Permit:
NC0004375
Clariant Corporation
Document Type:
Permit Issuance
Wasteload Allocation
Authorization to Construct (AtC)
Permit Modification
Complete File - Historical
Engineering Alternatives (EAA)
Correspondence
Owner Name Change
Report: ..)
Instream Assessment (67b)
Speculative Limits
Environmental Assessment (EA)
Document Date:
November 2, 1999
This document is printed on reuse paper - ignore any
content on the resrerse side

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EVALUATION OF BEST AVAILABLE
TECHNOLOGY ECONOMICALLY
ACHIEVABLE (BAT) FOR CONTROL
OF NUTRIENT DISCHARGES
CLARIANT CORPORATION
Prepared for:
Clariant Corporation
625 East Catawba Avenue
Mount Holly, NC 28120
Prepared by:
AWARE Environmental Inc.®
9305-J Monroe Road
Charlotte, NC 28270-1490
AEI Job No. N130-24
Doc. #13024r002
October 1999

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Section No.
TABLE OF CONTENTS
Description Page No.
TABLE OF CONTENTS i
LIST OF TABLES ii
LIST OF FIGURES iii
LIST OF APPENDICES iii
1.0 INTRODUCTION 1
1.1 BACKGROUND 1
1.2 NPDES PERMIT 1
1.3 DEFINITION OF BAT 6
1.4 STATE NUTRIENT LIMITATIONS 7
1.5 BAT STUDY 7
2.0 WASTE REDUCTION AND MINIMIZATION 11
2.1 SULFUR DYE PRODUCTION 11
2.2 REFRACTORY NITROGEN SOURCES 11
2.3 NON -REFRACTORY NITROGEN SOURCES 12
W I 2.4 PHOSPHORUS SOURCES 12
2.5 POLLUTION PREVENTION 13
2.5.1 Reclamation and Reuse 13
2.5.2 Increasing In -Plant Process Yields and Reduction of Losses13
2.5.3 Water Conservation and Waste Reduction Strategies 14
2.5.4 By -Product Recovery 15
FM
2.5.5 Clariant Pollution Prevention Programs 17
2.6 INDUSTRY WIDE POLLUTION PREVENTION ACTIVITIES17
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3.0
3.1
Fim 3.2
3.3
3.4
..+ 3.4.1
3.4.2
3.4.3
.1 3.4.4
3.5
3.5.1
mr' 3.5.2
3.6
3.7
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WASTEWATER TREATMENT OPERATIONS 19
WASTEWATER TREATMENT SYSTEM 19
PROCESS WASTEWATER CHARACTERISTICS 24
REFRACTORY NITROGEN 24
NUTRIENT REQUIREMENTS 25
Sludge Age 26
Treatment Temperature 27
Carbonaceous Waste and Treatment Configuration 27
Wastewater Chemistry 28
NUTRIENT OPTIMIZATION 32
Analytical Monitoring 32
Target Nutrient Addition 34
PROCESS PERFORMANCE 34
BASELINE EFFLUENT NUTRIENT CONCENTRATIONS 36
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4.0 TREATABILITY ANALYSIS 42
p+ 4.1 GENERAL 42
4.2 ACHIEVABLE NITROGEN CONCENTRATIONS 42
4.3 ACHIEVABLE PHOSPHORUS CONCENTRATIONS 43
F.+ 4.4 SIGNIFICANCE OF TREATABILITY FINDINGS 44
5.0 COST EFFECTIVE BAT ANALYSIS OF
'"' ALTERNATIVE TERTIARY TECHNOLOGIES 46
5.1 PRECIPITATION USING FERRIC . CHLORIDE FOR
PHOSPHORUS REDUCTION 47
I.` 5.2 SODIUM -BASED ALKALINITY ADDITION FOR
PHOSPHORUS REDUCTION 50
5.3 OVERVIEW 51
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5.3.1 Single -Sludge Biological Nitrification/Denitrification 54
5.3.2 Tertiary Denitrification 57
,., 5.4 DETERMINATION OF BAT 62
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6.0 SUMMARY AND CONCLUSIONS 65
LIST OF TABLES
Table No. Description
'°" 1-1 Summary of Current and Proposed NPDES Permit Limits for East Site
WWTP
1-2 Current and Proposed Effluent Limitations
1.' 3-1 Process Design Summary Clariant East Site WWTP
3-2 Summary of Waste Treatment Operating Conditions
3-3 Summary of Nutrient Monitoring
3-4 Full -Scale Target Phosphorus Addition
3-5 Summary of Removal Efficiencies
F., 4-1 Summary of Treatability Findings
5-1 Process Design Summary for Tertiary Phosphorus Removal Using
Precipitation
RR 5-2 Process Design Summary for Sodium -Based Alkalinity Addition for
Phosphorus Reduction
5-3 Process Design Summary for Biological Nitrification/Denitrification
0.4 5-4 Process Design Summary for Tertiary Denitrification
5-5 Tertiary Treatment Technology Cost Estimates
5-6 Summary of Nutrient Surcharges from POTW's
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R.+ LIST OF FIGURES
Figure No. Description
1 Nutrient Contribution from Clariant to Lake Wylie
2 Schematic of Current WWTP System
F., 3 Equilibrium Solubility Diagram for Fe, Al, and Ca
4 Average Effluent BOD5 and TSS
5 Full-scale Phosphorus Addition and Effluent Ortho-P and BOD5
0.+ 6 Statistical Analysis of WWTP Effluent - TP
7 Statistical Analysis of WWTP Effluent - TN
8 Precipitation with Ferric Chloride
9 Caustic Addition for Alkalinity Control
10 Schematic for Proposed Single -Sludge Nitrification/Denitrification
System
`., 11 Schematic for Proposed Tertiary Denitrification System
PM
LIST OF APPENDICES
MI
A Water Quality and Nutrient Data for the Catawba River and Lake Wylie
B Summary of Full -Scale Monitoring Data
04 C Summary of Statistical Analyses
D Treatability Analysis of Nutrient Control Strategies
E Design and Cost Estimate of Alternative Tertiary Technologies
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1.1 BACKGROUND
SECTION 1.0
INTRODUCTION
The Clariant Corporation operates an integrated organic chemicals manufacturing facility on
the Catawba River at Mount Holly, North Carolina. The facility includes two sites referred to
as the east and west sites. The east site is in Mecklenburg County and is located on the south
side of NC Highway 27. The east site includes a batch organic chemical production facility
which produces dyes for use in the textile industry, a herbicide active ingredient and specialty
�► chemicals. The east site wastewater is treated in an activated sludge wastewater treatment
plant (WWTP) and discharged to the Catawba River. The west site is in the City of Mount
rim Holly and is located almost directly across the river from the Mecklenburg County site. The
west site wastewater is treated on -site in an activated sludge pretreatment facility and is
discharged to the Town of Mt. Holly sewer system.
The Clariant east site is the subject of this BAT study. The discharge of wastewaters from this
industry is regulated under the guidelines set by the U.S. Environmental Protection Agency for
the organic chemicals, plastics and synthetic fibers (OCPSF) category — Subpart H specialty
organic chemicals. The OCPSF effluent guidelines define effluent limitations in 40 CFR 414.
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1.2 NPDES PERMIT
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The treated wastewater is discharged to the Catawba River under NPDES permit No.
NC0004375, issued by the State of North Carolina (State). The discharge permit went into
effect on September 1, 1991. The NPDES discharge permit for the facility includes discharge
limits for flow, five-day biochemical oxygen demand (BODS), total suspended solids (TSS),
ammonia nitrogen (NH3-N), pH and phenols. The North Carolina Department of Environment
and Natural Resources (NCDENR) is proposing a revised permit for the Clariant discharge
which will significantly reduce the allowable discharge. A summary of the current and
proposed non -priority pollutant permit discharge limits is presented in Table 1-1.
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TABLE 1-1
SUMMARY OF CURRENT AND PROPOSED NPDES
PERMIT LIMITS FOR EAST SITE WWTP
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: C f �en»tr. L-T,�•ta,u_Y b/d54.• ;.r.-.fa t
, „ :`, r N�mert, > . , „,
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: .,: T a'SS.f: �o{!Y se(Ryd Lr
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,.,
on
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Flow
3.9 MGD
--
3.9 MGD
--
BOD5
852
2236
484
1268
TSS
976
2928
661
2003
NH3-N
651
977
651
977
Total Phenols
3.9
7.8
3.9
--
pH
--
> 6.0 and <9.0
--
> 6.0 and <9.0
Notes: (1)Limits contained in NPDES permit dated September 1, 1991.
(2)Limits proposed by NCDENR as of April 22, 1999.
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In addition, a draft permit issued by the NCDENR noted that the State plans to implement
BAT nutrient limits on the Clariant discharge. Specifically, the draft permit states as follows:
"It has been determined by the Division of Water Quality, through intensive water
quality studies, that discharges upstream of Lake Wylie, including this discharge, need
to control nutrients through the application of best available technology (BAT) that is
economically achievable. The permittee shall provide the Division with a study which
fully investigates the feasibility of meeting a monthly average TP limit of 1.0 mg/1 and
a summertime TN limit of 6 mg/1. If it is determined to be beyond reasonable BAT to
reach such concentrations of nutrients, the Division will apply BAT limits based on the
results of this study and the performance of other similar plants. The nutrient study
should be completed by November 1, 1999, and submitted to the following
address
he NCDENR-defines TN to be the sum of the ammonia nitrogen, organic nitrogen, nitrite
nitrogen and nitrate nitrogen.
,,
The US EPA basis for the OCPSF effluent limitations is included in the Development
Document for Effluent Limitations Guidelines and Standards for the Organic Chemicals.
Plastics and Synthetic Fibers, October 1987 (Development Document). This document
specifies technology requirements and in -plant controls to comply with Best Available
Technology Which Is Economically Achievable (BAT) criteria.
1.1 EPA's OCPSF effluent guidelines provide BAT criteria for a number of constituents in the
Clariant effluent. Current and proposed effluent limits for the Clariant facility, based on the
OCPSF BAT effluent guidelines for priority pollutants, are presented in Table 1-2. The
effluent guidelines are based on the use of BAT treatment technology and strictly regulate the
pollutant discharge from the Clariant facility.
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TABLE 1-2
CURRENT AND PROPOSED EFFLUENT LIMITATIONS
Parameter= s ' #$ ; ' t
: may, r t
4 � ; x . 4
_Ms. onthly Avg. ;(lb/d) F
k . c
Daily,Max (lb/d) . :
_ e
Currzent n�x�
;Proposed ? d
~ Current ¶1
.'roposed (2)
Acenaphthene
0.39
0.228
0.50
0.611
Acrylonitrile
1.69
--
4.30
29(3)
Benzene
0.75
0.383
2.70
1.409
Carbon Tetrachloride
0.32
0.186
0.67
0.394
Chlorobenzene
0.31
0.155
0.57
0.290
1,2,4-Trichlorobenzene
1.20
0.704
2.46
1.450
Hexachlorobenzene
0.26
--
0.49
0.37(3)
1,2-Dichloroethane
1.20
0.704
3.71
2.186
1,1,1-Trichloroethane
0.37
0.218
0.95
0.559
Hexachloroethane
0.39
0.218
0.95
0.559
1,1-Dichloroethane
0.39
0.228
1.04
0.611
1,1,2-Trichloroethane
0.37
0.218
0.95
0.559
Chloroethane
1.83
1.077
4.72
2.776
Chloroform
0.37
0.218
0.81
0.476
2-Chlorophenol
0.62
0.321
1.95
1.015
1,2-Dichlorobenzene
1.57
0.798
3.32
1.688
1,3-Dichlorobenzene
0.62
0.321
0.90
0.456
1,4-Dichlorobenzene
0.31
0.155
0.57
0.290
1,1-Dichloroethylene
0.28
0.166
0.44
0.259
1,2-trans-Dichloroethylene
0.37
0.218
0.95
0.559
2,4-Dichlorophenol
0.77
0.404
2.22
1.160
1,2-Dichloropropane
2.69
--
4.05
29(3)
1,3-Dichloropropylene
0.51
0.300
0.77
0.456
2,4-Dimethylphenol
0.36
0.186
0.71
0.373
2,4-Dinitrotoluene
1.99
1.170
5.03
55(3)
2,6-Dinitrotoluene
4.40
2.641
11.28
6.640
Ethylbenzene
0.65
0.331
2.20
1.119
Fluoranthene
0.47
0.259
1.20
0.704
Methylene Chloride
0.70
0.414
1.57
0.922
Methyl Chloride
1.51
0.891
3.34
1.968
Hexachlorobutadiene
0.35
0.207
0.86
0.508
Naphthalene
0.45
0.228
0.50
0.611
Nitrobenzene
0.48
0.208
1.20
0.704
2-Nitrophenol
1.23
0.425
2.08
0.715
4
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October, 1999

TABLE 1-2 - Cont'd
Mt, CURRENT AND PROPOSED EFFLUENT LIMITATIONS
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;� 1 t N.� X �
L c % 4 �? 6
3 M „4�■■ 3 ui �
s iTi01,1. i
d31 ii� YR1'/) d _ _'i
.� ��
�g': �F71• �f
`• 1 3' H 3 - "�
x2 ?�.1 . cY<,w..: •d� 1 d. ,.
} � tift�■■+F ��-
Df�L ,
� wo�i',,>x+' L
�'"
s�� E .
�iA� b/ b -„
d} �.,jq
0 4'fi:'
. f. `',+q
.
",r IK.- a..,
.'�z t. .,
} MC'tp � : � T � i-.it�5•i� h
r ,
`n;,.
��, �Y,
Curren
Ore
r , G;
4 "Pe .aii� rSr' a "X
Proposed{} .
>,ry r f
d L CN°^` .L ` �
C.urreD u
?.s, r�ra.. 'W >
Proposed '
4-Nitrophenol
2.17
0.746
3.74
1.284
2,4-Dinitrophenol
2.15
0.735
3.71
1.274
4,6-Dinitro-o-cresol
1.55
0.808
5.50
2.869
Phenol
1.56
0.155
2.70
0.269
Bis(2-ethylhexyl)phthalate
1.81
1.067
4.91
2.890
Di-n-butyl phthalate
0.48
0.280
1.00
0.590
Diethyl phthalate
1.43
0.839
3.57
2.103
Dimethyl phthalate
0.33
0.197
0.83
0.487
Benzo(a)anthracene
0.31
--
0.50
1.40")
Benzo(a)pyrene
0.40
--
0.50
1.40(3)
3,4-Benzofluoranthene
0.40
--
0.50
1.40(3)
Benzo(k)fluoranthene
0.39
--
0.50
1.40(3)
Chrysene
0.39
--
0.50
1.40(3)
Acenaphthylene
0.39
0.228
0.50
0.611
Anthracene
0.39
0.228
0.50
0.611
Fluorene
0.39
0.228
0.50
0.611
Phenanthrene
0.39
0.228
0.50
0.611
Pyrene
0.44
0.259
0.50
0.694
Tetrachloroethylene
0.39
0.228
0.99
0.580
Toluene
0.53
0.269
1.63
0.829
Trichloroethylene
0.37
0.218
0.95
0.559
Vinyl Chloride
1.82
1.077
4.70
2.776
Total Cyanide
7.39
4.350
9.01
277(3)
Total Chromium
--
11.498
--
28.692
Total Copper
--
--
--
388(3)
Total Lead
--
3.315
--
7.147
Total Nickel
--
17.505
--
41.226
Total Zinc
--
10.876
--
27.035
(1) Limits contained in NPDES permit dated September 1, 1991.
(2) Limits proposed as of April 22, 1999.
(3) Limits are in µg/1.
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October, 1999
5

1.3 DEFINITION OF BAT
The U.S. EPA describes BAT in the Development Document as follows:
"BAT effluent limitations guidelines, in general, represent the best existing
performance in the category or subcategory. The Act establishes BAT as the principal
national means of controlling the direct discharge of toxic and non-conventional
pollutants to navigable waters.
In establishing BAT, the Agency considers the age of equipment and facilities involved,
-« processes employed, engineering aspects of the control technologies, process changes,
cost of achieving such effluent reduction, and non-water quality environmental
impacts."
The Development Document and the OCPSF effluent guidelines allow OCPSF facilities to
comply with the effluent criteria using either biological or non-biological treatment
technologies. Clariant has chosen to utilize biological treatment to comply with BAT. Based
on the technology requirements and Clariant's on-going compliance with effluent limits for
biological end-of-pipe treatment facilities, AWARE Environmental Inc.® (AEI) has determined
that Clariant operates an OCPSF BAT treatment facility. Clariant has implemented additional
treatment beyond normal BAT in order to achieve optimum performance. These treatment
technologies include chemically assisted primary clarification, nutrient addition and an effluent
holding/polishing basin. Through conscientious and diligent operation of the WWTP, Clariant
has consistently been in compliance with the effluent BAT criteria. In addition, Clariant has
maintained an on-going effort to achieve optimum biodegradation and effluent quality using the
current BAT treatment facility and continues to implement changes which will improve the
consistency of treatment and the performance of the WWTP.
The statistical procedure used by the US EPA to develop monthly average effluent discharge
limits is presented in the Development Document. The procedure is based on the US EPA use
^- of the 95th percentile of the daily data as the basis for the monthly average discharge limit.
This same statistical procedure is confirmed in the US EPA NPDES Permit Writers' Manual,
December 1996 as the basis for monthly average discharge limits.
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Imi
The OCPSF BAT effluent guidelines do not include effluent limits for total phosphorus (TP)
and total nitrogen (TN). The Development Document recognizes that the operation of a BAT
biological treatment system frequently requires the addition of nutrients for optimum treatment
of OCPSF wastewaters.
1.4 STATE NUTRIENT LIMITATIONS
The NCDENR has determined that dischargers upstream of Lake Wylie need to control
nutrient discharges. It is our understanding that the objective of the nutrient limits is to reduce
eutrophication in the arms of Lake Wylie. The NCDENR is proposing nutrient limits on both
municipal and industrial discharges to decrease eutrophication in Lake Wylie caused by the
discharge of nutrients from the rivers which feed the lake. Nutrient data from the 1995
Catawba River Basinwide Water Quality Management Plan (Catawba Plan) and Clariant's
discharge monitoring reports were reviewed in order evaluate Clariant's contribution to
nutrients in Lake Wylie. Clariant discharges to the Catawba River, which flows into the main
stem of Lake Wylie. The Catawba Plan indicates that no water quality problems have been
identified in the Catawba River at Monitoring Station No. 02142938 (near S. Belmont), �L.) , 4e
downstream of the Clariant discharge. These data are presented in Appendix A. The average
nutrient contribution from Clariant to Lake Wylie is summarized in Figure 1. These data,
which are also included in Appendix A, are based on 60% transport of nutrients from the
Catawba River to Lake Wylie as discussed in the Catawba Plan. Based on these data, Clariant
is a minor contributor to the nutrients in Lake Wylie and does not contribute to nutrient
concentrations in the Catawba Creek and Crowders Creek arms of Lake Wylie, where
eutrophication problems have been identified.
1.5 BAT STUDY
A review of the historical operating data indicates that the Clariant treatment facility has not
and does not currently achieve the target 6 mg/1 TN and 1 mg/1 TP limits proposed by
NCDENR. Furthermore, this evaluation indicated that these limits would be exceeded based
on optimum operation of the treatment system. Therefore, Clariant has chosen to undertake a
detailed nutrient BAT evaluation, as requested by NCDENR, to define a "reasonable" best
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Pal
Nutrient Load (Ib/d)
7000
6000
5000
4000
3000
2000
1000
0
Figure 1. Nutrient Contribution from Clariant to Lake Wylie
® Total Load to Lake Wylie
■ Clariant's Contribution to Lake Wylie
L. Wylie = 932 Ib/d
Clariant
= 9.9 Ib/d
1
L.
Wylie = 6538 Ib/d
13024s002
Fig1
Total Phosphorus
Clariant
= 110 lb/d
Total Nitrogen
10/28/99
8

1t1
01111
available technology that is economically achievable (BAT) for control of nutrient discharges
in the Clariant discharge to the Catawba River.
There are a large number of factors that need to be considered in the development of TN and
TP BAT limitations for the Clariant facility. These include:
• Age of equipment and facilities involved;
• Processes employed;
• Engineering aspects of the control technologies;
• Cost of achieving effluent reduction;
• Non water quality environmental impacts;
• Requirements to operate treatment system in compliance with all established State and
EPA BAT effluent criteria; and
• Treatment process requirements for nutrient addition.
�► Clariant and AEI have conducted a detailed BAT analysis. The study approach considered
rott
Mel
AEA
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those factors noted above for compliance with the proposed nutrient limits. As part of the
overall analysis, the factors evaluated also included:
• Waste Reduction and Minimization Approaches;
• Optimization of the Wastewater Treatment Plant; and
• Evaluation of Alternative Nutrient Reduction Technologies.
The reasons for including these in the BAT analysis are presented in the following paragraphs:
• Waste Reduction and Minimization Approaches
The Clariant facility utilizes batch production processes to produce a wide variety of
sulfur dyes. The production of sulfur dyes can result in significant concentrations of
refractory (non -biodegradable) organic nitrogen in the effluent. The purpose of the
waste reduction and minimization phase was to consider options for decreasing waste
loads to the WWTP in order to minimize nitrogen and phosphorus discharges.
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• Optimization of the Wastewater Treatment Plant
pal OCPSF BAT technology recognizes the need for nutrient addition for the operation of a.
BAT biological treatment process. The Clariant wastewater does not contain sufficient
0.1
phosphorus for optimum biological treatment. The purpose of the WWTP optimization
phase was to provide the phosphorus required to achieve maximum biodegradation in
fart
rah
gag
order to reduce the discharge of pollutants (including organic nitrogen) in the effluent.
Throughout the optimization phase, phosphorus addition was decreased in order to
determine the minimum amount of phosphorus required while maintaining optimum
treatment performance. Phosphorus addition was reduced gradually over time in order
to minimize nutrients in the final effluent without compromising effluent quality.
• Evaluation of Alternative Nutrient Reduction Technologies
The operation of the optimized WWTP indicated that the facility would not be able to
meet the target NCDENR limits for TN and TP. The purpose of the nutrient reduction
treatment phases was to evaluate BAT limits which could potentially be achieved through
addition of treatment processes and/or treatment units. During the evaluation of the
nutrient reduction treatment phase, treatment technologies were pilot tested to determine
whether or not additional treatment would significantly decrease effluent TN and TP
concentrations.
AEI has assisted Clariant in the development and the conduct of the BAT study. This study
has included evaluation of in -plant controls and waste load reduction, optimization of the full-
scale BAT treatment system, literature reviews, and conduct of treatability tests to reduce
effluent TN and TP. A summary of the full-scale monitoring data is included in Appendix B.
Initiated in 1998, the objective of this study was to determine if Clariant can comply with
NCDENR proposed target TN and TP limits, and if not, to define BAT for the wastewater
treatment system. The findings of the BAT study are presented in this report.
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SECTION 2.0
WASTE REDUCTION AND MINIMIZATION
The objective of the waste reduction and minimization program, as it applies to TN and TP
BAT, is to minimize nitrogen and phosphorus discharges. The program can best be described
by a review of production activities and projects to reduce discharges.
2.1 SULFUR DYE PRODUCTION
Sulfur-based dye manufacturing is the primary production operation at the Clariant east site
facility and is the primary source of nitrogen in the process wastewater. Sulfur dyes are
produced from organic amines and nitrogen compounds, such as dinitrochlorobenzene, p-
nitroaniline, and N-phenyl-a-naphthylamine. Sulfur dyes are synthesized by reacting the
organic compounds with poly sulfur in a process called thionation to form various compounds
with sulfide and disulfide bonds. Finished product molecular weights range from 290 to 560
grams/mole. All production operations are batch. Due to campaigning of batches of products,
variability in BOD5, COD and molecular components in the raw wastewater is quite large. In
theory, the raw materials used to produce the dyes should be completely consumed in the
synthesis reactions. However, typically the synthesis reactions produce only 80-86% of the
theoretically expected volume of finished material. The remaining 14-20% is either unused
raw material or by-product impurities produced during synthesis. These unused raw materials
and by-product impurities cannot be used in subsequent batches and are discharged to the waste
treatment system. Because of the need for extensive clean-up activities in between batches,
approximately 1.5% of finished dye product is discharged to the waste treatment system.
2.2 REFRACTORY NITROGEN SOURCES
The finished dyestuff is made up of organic nitrogen molecules that are not easily biodegraded.
Waste streams from intermediates production are more easily biodegradable. Therefore, the
sulfur dye manufacturing process at the facility results in an effluent organic nitrogen which is
not easily biodegraded and will pass through an OCPSF BAT treatment facility. The
refractory nature of this organic nitrogen discharge means that this nitrogen would not affect
eutrophication in the receiving stream.
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There is a wide range of sulfur dyes that can be manufactured using the same basic
manufacturing equipment. Variations in the dye depend on color criteria and specific
applications. Because of the large variety of dyestuffs produced using a batch process, the
dyestuff production can vary significantly on a day-to-day basis. The batch nature of
production results in a wide variability in discharge organic nitrogen concentrations. The
discharge organic nitrogen will vary on a day-to-day basis depending on the specific dyes being
produced.
2.3 NON-REFRACTORY NITROGEN SOURCES
A review of the production procedures for nutrient waste minimization noted that non-
refractory (biodegradable) sources of nitrogen in the process wastewater include ammonia from
the use of a large scrubbing system. The synthesis and finishing of Sulfur Black dye produces
ammonia gas as a by-product. However, air regulations require the removal of this ammonia
from the air. In 1994 a large scrubbing system was installed at the east site to remove
ammonia from the process vent streams as required under North Carolina's Toxic Air Pollutant
Regulation. The scrubber system removes ammonia from the process vents and produces a
20% solution of ammonium sulfate (NH4)2SO4, much of which must be disposed of by
discharging to the waste treatment system. The spent scrubber solution is a significant
contributor of ammonia nitrogen (NH3 N) in the wastewater. The ammonia scrubbing system
ski
generates approximately 8.13 to 11.00 million pounds of 20% (NH4)2SO4 annually.
2.4 PHOSPHORUS SOURCES
There are very few sources of phosphorus in the raw wastewater streams. Concentrations of
total phosphorus (TP) in the raw wastewater are low and generally vary between 2 and 4 mg/l.
These concentrations are further reduced in the primary lime treatment process used in the
WWTP, prior to biological treatment. The residual phosphorus concentrations contained in the
wastewater entering the biological treatment process are insufficient to promote optimum
bacterial growth for treatment of the organic wasteloads. Clariant therefore adds phosphoric
acid to the activated sludge aeration basins to supply the necessary phosphorus required to
12 FINAL
October, 1999

O BI
O il
.4
aft
MIR
-
Aft
oft
promote optimal biological treatment performance and provide the highest possible quality of
treated effluent. This phosphoric acid addition maximizes the biological breakdown/oxidation
of the non -refractory nitrogen contained in the Clariant wastewater.
2.5 POLLUTION PREVENTION
An important consideration in the control of nutrient discharges is the use of in -plant pollution
prevention process controls. Clariant has a long history of implementing these programs.
Some of the specific programs are presented in the following section.
2.5.1 Reclamation and Reuse
Clariant devotes significant technical resources and operating dollars to minimizing
waste and to reclaiming saleable materials from its waste streams. However, the
facility has had extreme difficulty in finding large markets and/or outlets for reclaimed
by-product and residual materials. Materials such as ammonium sulfate from the
ammonia scrubbing system are reclaimed and sold. However, demand is highly
variable and when these products are not sold or utilized in other markets, they must be
discharged to the waste treatment system for treatment. Consequently, reclaiming and
purifying materials from wastewater streams does not guarantee that these materials
will not end up in the facility's wastewater because of the difficulty in finding a user or
buyer with consistent or continuous need for the material.
2.5.2 Increasing In -Plant Process Yields and Reduction of Losses
Over the past fifteen years, Clariant has focused on increasing product yields from
organic starting materials, which in turn decreases the quantities of waste materials that
end up in the wastewater and must be treated in the WWTP. As a result, product yields
from the organic intermediate processes have improved significantly with few
expectations. In the early 1980s, intermediate processes generally yielded 70 — 78% of
the expected theoretical yield. Optimization of in -plant operations has resulted in current
yields of 80 — 86%. Most of the yield improvements have come about by installing
13
FINAL
October, 1999

electronic automatic controls that improve the reliability and consistency of the chemical
production processes.
In an effort to reduce loss of product and reduce waste generation, the facility
manufactures products in campaigns to minimize losses caused by cleaning the reactor
vessels, piping, and storage tanks. As a result, finished goods losses, which
historically averaged 3 % of throughput, have been reduced to 1.5 % . During this same
period, several finished products that were significant sources of waste loads to the
WWTP have also been out -sourced and on -site production operations have been shut
down.
2.5.3 Water Conservation and Waste Reduction Strategies
In order to reduce the amount of waste generated, the facility has renovated production
processes and implemented in -plant controls to conserve water and reduce the amount
of waste generated at the facility. These renovations and in -plant controls are described
as follows.
Intermediate and finished pigment processes generally utilize filter presses to isolate the
active material and to wash out impurities. The site has renovated the filter press units
by installing diaphragm style plates, hydraulic squeeze systems, and improved wash
cycle technology. The improvements use less water in the washing operation. As an
example, pigment cakes that used to consume 58,000 gallons of water during the
washing cycle now consume only 14,800 gallons, a 74% reduction in water usage.
One of the facility's larger intermediates processes, dinitrochlorobenzene production,
previously generated approximately 37,000 gal/day of raw wastewater. The process was
completely redesigned and upgraded by Clariant to reduce water usage and minimize
wastewater generation. The newly designed system generates approximately 2,500
gal/day of wastewater, a 93% reduction in wastewater generation. Most of the remaining
water used in the production process is recycled.
14
FINAL
October, 1999

fx1
f=1
Historically, many cooling operations at the facility utilized "once through" process
water. Clariant has installed a number of cooling towers at the east site, and many of
these operations have been modified to use recycled cooling tower water. This has
reduced water consumption at the east site facility by approximately 150,000 gallons per
day.
Many products produced at the east site are packaged in 55-gallon drums. In the past,
Clariant would wash and re -paint 55-gallon drums that were returned by customers. The
drum washing and repainting operation consumed roughly 20,000 gallons of water per
day and was a significant contributor of organic waste in the wastewater. The facility
now contracts with a large drum recycling firm that cleans and refurbishes the drums off -
site using much more modern and efficient cleaning equipment. This has reduced waste
generation at the facility and the organic load in the wastewater.
Clariant formerly manufactured dinitrophenol and trinitrophenol at the east site. These
production processes generated approximately 50,000 gal/day of wastewater containing
elevated concentrations of phenolic nitrogen compounds. These phenolic constituents
were extremely difficult to biodegrade and during periods of cold weather inhibited the
performance of WWTP bacterial population. Both products are now being purchased
4.1 from off -site sources and all on -site production has been shutdown. This has reduced
the refractory nitrogen wasteload to the waste treatment system and has improved
biodegradation during low temperatures.
2.5.4 By -Product Recovery
Clariant has developed considerable efforts in identifying and marketing usable by-
products from the east site. Several by-products are recovered from production and
sold to consumers. These products include sodium thiosulfate, ammonium sulfate and
sulfuric acid. The following is a description of activities at the facility to recover these
15
fact
FINAL
October, 1999

Owl
by-products in order to reduce waste generation and waste loads on the treatment
system.
Sodium thiosulfate (Na2S203) is a by-product of sulfur black synthesis chemistry.
Between 5 to 8 million pounds per year of Na2S2O3 exits the dyestuff process as a 26%
solution. It is the single largest source of BOD5 that requires treatment in the facility's
WWTP. In addition, the biological breakdown of Na2S2O3 in the WWTP results in
significant consumption of wastewater alkalinity which requires addition of significant
quantities of lime in order to maintain the pH within levels suitable for biological
treatment. The facility reclaims sodium thiosulfate, removes impurities through
filtration, and markets the material as a dechlorination product. Approximately 60% of
this material produced at the east site is currently being sold.
Ammonium sulfate (NH4)2SO4 is generated in the ammonia scrubbing system during the
production of Sulfur Black dye. Between 8.13 and 11.00 million pounds of 20%
ammonium sulfate solution is generated in the scrubber annually. Clariant is able to
give the majority of the (NH4)2SO4 material, approximately 70%, to local hay producers
free of charge. The farmers use the material to spray their fields. The remaining 30%
of the (NH4)2SO4 material must be treated in the waste treatment system. The demand
for the material fluctuates with the seasons and there are periods when the facility must
treat all of the (NH4)2SO4 in the waste treatment system. This typically occurs from
mid -December through mid -March when wet weather conditions prevent farmers from
spraying their fields. During this four -month period, the facility is forced to treat
higher volumes of (NH4)2SO4 in the waste treatment system. The facility has not been
able to identify other markets for this by-product.
Sulfuric acid is utilized in the dinitrochlorobenzene synthesis process. This process
generates approximately 7 to 12 million pounds of 75 % sulfuric acid waste annually.
Historically, the spent acid solution had been considered a waste product because it
contained a significant amount of organic impurities. In order to recover the spent acid
16
FINAL
October, 1999

ral
Mitt
MCI
ffta
gni
solution and minimize waste, Clariant installed a countercurrent liquid -liquid extraction
system to remove organic compounds from the acid stream. Treatment using liquid- -
liquid extraction reduces organic concentrations in the acid stream to less than 50 mg/l.
The recovered acid solution is currently being sold for use in fertilizer manufacturing.
Clariant has recently been able to market 100% of the recovered acid solution. The
recovered organics from the extraction system are recycled back into the synthesis
process. As a result of this operation and other improvements in performance, process
yield has increased by 4 % .
2.5.5 Clariant Pollution Prevention Programs
Clariant currently has several pollution prevention activities in -place. These activities
include the following:
1. Dewatering of wastewater sludge in order to reduce the volume of waste
produced;
2. Implementation of a solid waste recycling program;
3. Steel drum recycling;
4. Cardboard recycling;
5. Office paper recycling;
6. Unsolicited publication reduction; and
7. Aluminum can recycling.
2.6 INDUSTRY WIDE POLLUTION PREVENTION ACTIVITIES
Clariant is participating on an on -going basis in several formal programs with the goal of
improving waste reduction practices and procedures at the facility. These include:
1. Responsible Care - Clariant, as a member of the Synthetic Organic Chemical
Manufacturers Association (SOCMA), participates in the Responsible Care® program,
which includes a Pollution Prevention Code of Management Practice.
2. ETAD/EPA - The dyestuff manufacturer's trade organization (ETAD), of which
Clariant is a member, and the EPA's Office of Pollution Prevention have entered into a
joint effort to monitor and encourage P2 and waste minimization efforts in the dye stuff
17
FINAL
October, 1999

1)
j
industry. As an EPAD member, Clariant has agreed to complete annual assessments of
the number of pollution prevention opportunities that are in place at the facility.
18
FINAL
October, 1999

SECTION 3.0
WASTEWATER TREATMENT OPERATIONS
3.1 WASTEWATER TREATMENT SYSTEM
The process wastewaters from the Clariant facility are treated in an integrated BAT biological
treatment system composed of a primary lime treatment process followed by a two-stage,
single-sludge activated sludge process. A schematic of the wastewater treatment process is
presented in Figure 2 and a summary of the process design is presented in Table 3-1. The
treatment system includes a two-tank lime neutralization process, primary clarification, aerobic
biological treatment, secondary clarification, chemical sludge conditioning and belt press
dewatering. In conjunction with OCPSF BAT recommendations, nutrients are added to the
biological treatment process.
Phosphoric acid is the nutrient added to the biological process in order to provide for healthy
biological growth of the mixed liquor microorganisms. Polymer is added to aid secondary
clarifier settling. Following final clarification, the treated effluent is either discharged directly
to the Catawba River or stored in the effluent holding basin for future re-treatment in the
WWTP and subsequent discharge. Waste primary and secondary sludges are dewatered using
two belt filter presses and transported to an on-site landfill for disposal.
A summary of the waste treatment system operating conditions is presented in Table 3-2.
Actual conditions are monitored and adjusted based on the target operating conditions.
In order to consistently comply with the effluent criteria, polymer addition is needed in the
secondary clarifiers to aid settling. The poor solids settling characteristics and the need for
polymer addition appear to be a direct result of the Clariant wastewater characteristics and
•• normal changes in wastewater temperatures and production.
19 FINAL
- October, 1999

ACID
WASTEWATER
FINAL
EFFLUENT
DISCHARGED -A
TO CATAWBA
RIVER
LIME FOR
pH
CONTROL
LIME FOR
pH
CONTROL
NEUTRALIZATION TANKS
ALKALINE
WASTEWATER
� J
FLOW
CONTROL
FLUME
WASTED
SLUDGE
PHOSPHORIC
ACID
PRIMARY
CLARIFIERS
LIME FOR LIME FOR
pH pH
CONTROL CONTROL
TTTTTTTiTJ
AERATION BASIN
ZO3A
to cn
A A
POLYMER
AERATION BASIN
Z04
SECONDARY
CLARIFIERS
FILTRATE
00 °
> t_� o (_)
SLUDGE
TO
ON —SITE
LANDFILL
BELT FILTER PRESS
360 MG
HOLDING
BASIN
PUMP
STATION
SCHEMATIC OF CURRENT WWTP
SYSTEM
CLARIANT
SCALE NTS
DATE
OCT. 1999
APPROVED BY :
DRAWN BY: MRW
October 27. 1999 2:59:57 p.m.
Drawing: V: \N130\13024P01 ADWG
DESIGNED BY :
REVISED
PROJECT NUMBER
N130-24
Al!/�A
INC E O'S/ `T�
DRAWING NO.
FIGURE 2
20

TABLE 3-1
PROCESS DESIGN SUMMARY
CLARIANT EAST SITE WWTP
pH Neutralization Tanks
Total No. of Tanks(')
Type
Volume per Tank
Tank Diameter
Tank Height
Detention Time per Tank @ 1.42 MGD
Primary Clarifiers
Total No. of Tanks
Volume per Tank
Diameter per Tank
Side Water Depth per Tank
Surface Area per Tank
Surface Loading Rate @ 1.42 MGD
Aeration Basin ZO3A
Description
Volume
Depth
Detention Time @ 1.42 MGD
Basin ZO3A Aeration/Mixing System
Number of Units
Minimum 02 Transfer
Aerator rpm
Size
Aeration Basin Z04
Description
Volume
Depth
Detention Time @ 1.42 MGD
Basin Z04 Aeration/Mixing System
Number of Units
Size
2
FRP
20,000 gallons
14ft
19ft
20 min
2
146,800 gallons
50 ft
12ft
1963 ft2
362 gpd/ft2
Rectangular with HDPE Liner
4.5 MG
16ft
3.2 days
5 Surface Aerators, 5 Mixers
2.5 lbs 02/hr/hp
1200 rpm
40 hp
Rectangular with HDPE Liner
2.5 MG
15ft
1.8 days
7 Surface Aerators, 1 Mixer
50 hp
21
FINAL
October, 1999

TABLE 3-1 (Coned)
PROCESS DESIGN SUMMARY
CLARIANT EAST SITE WWTP
a
Secondary Clarifiers
Total No. of Tanks
Volume per Tank
Diameter per Tank
Side Water Depth per Tank
Surface Area per Tank
Surface Loading Rate Using 1
Clarifier @ 1.42 MGD (2)
Effluent Storage Basin — ZO2C
Volume
Surface Area
Depth
Filter Press
Number of Units
Type
Sludge Handling Capacity
Average Cake Solids
2
500,000 gallons
80 ft
12ft
5026 ft2
282 gpd/ft2
360 MG
25 acres
40 ft
2
Belt
120 gpm
25-30%
(1) Lime addition for neutralization is alternated between tanks. (i.e. lime is not
added simultaneously to both tanks.)
(2) Typically only 1 clarifier is used.
22
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October, 1999

TABLE 3-2
SUMMARY OF WASTE TREATMENT OPERATING CONDITIONS
Parameter
Operating Condition
Target
Average (1/99-9/99)
ZO3A
Z04
MLSS
3,000-5,000 mg/1
2,940 mg/1
3,782 mg/1
F/M (COD)'
NA
0.46
Aeration Basin pH
7.0-8.0
7.2
7.5
D.O.
>2 mg/1
6.0
8.9
Sludge Age (MCRT)
15-35 days
32
(1) F/M is based on COD instead of BOD5.
23
FINAL
October, 1999

Wj(1-L-
3.2 PROCESS WASTEWATER
S EWATER CHARACTERISTICS
Clariant produces a wide variety of sulfur based textile dyes. This is a batch production
system and is highly variable on a day-to-day basis due to customer demands for different
dyes. Typically, the facility produces 25(±5) different dyes during an average production
week. Production of the dyes utilizes a batch-type campaign process, which means that the
dyes are produced in individual batches with a rotation of batches of similar dyes over
campaign periods.
The operation of a batch dye manufacturing facility results in a highly variable wastewater.
Because of the many different dyes that the facility manufactures (up to 75±5 different dyes),
the chemical composition of the wastewater changes daily. Each individual batch of dye
produces a wastewater with somewhat different chemical characteristics. Because of the
fluctuating wastewater flow and variable chemical composition, the wastewater treatment
process is more difficult than in other types of production facilities, such as a textile plant or a
commodity based OCPSF chemical manufacturing plant. In these other types of facilities, the
same product is produced continuously each day and results in a wastewater that does not vary
significantly in chemical composition and flow in comparison to a batch-type production
process. The varying chemical composition of the wastewater and fluctuating influent flow,
due to the batch-type production process at the Clariant facility, makes consistent performance
of the wastewater treatment system difficult.
3.3 REFRACTORY NITROGEN
The wastewater discharge for a sulfur dye manufacturing facility contains a significant amount
of organic nitrogen. Because of the daily changes in dye production, the chemical composition
of the wastewater is highly variable. Sulfur dyes contain varying levels of organic nitrogen,
depending on the dye formulation and dye intermediates being produced, which causes
variability in the influent wastewater nitrogen concentration.
The waste treatment system is effective in treating the process wastewater to reduce BOD5 and
TSS with relatively low concentrations of phosphorus, ammonia nitrogen, nitrate and nitrite
24 FINAL
October, 1999

1� 1 S Q rG, c �'c c k, ci / (Cc e�r.
rr 7 J
ILO
i
nitrogen. Because of variations in nitrification performance and influent ammonia loadings,
the concentration of NH3-N in the effluent varies seasonally. However, there is normally a
significant concentration of the organic nitrogen in the wastewater which is not biodegradable
using aggressive biological wastewater treatment and is refractory. The effluent is non-toxic
(based on whole-effluent toxicity test results), does not appear to affect water quality (based on
available Catawba River water quality data), and does not cause a problem in the environment.
Because of the non-biodegradable nature of the effluent refractory organic nitrogen, it will not
be available as a nutrient to the algae in the receiving waters and does not contribute to
eutrophication. Effluent total nitrogen (TN) limits are being considered by the NCDENR in
order to decrease the eutrophic conditions in Lake Wylie. However, a significant portion of
the effluent nitrogen from Clariant is non-biodegradable and should not contribute to
eutrophication in the Catawba River or in Lake Wylie.
3.4 NUTRIENT REQUIREMENTS
A major work effort was implemented in order to optimize the nutrient feed to the Clariant
OCPSF BAT treatment system. The objective of this program was to continue to comply with
all effluent requirements while providing only that level of nutrient addition required for good
treatment plant performance.
Nitrogen and phosphorus are essential nutrients necessary for proper system performance in
biological wastewater treatment applications. The EPA OCPSF development document notes
that nutrient addition is required for operation of an OCPSF biological BAT treatment system.
The OCPSF development document states the following:
d v,,..k "For a biological system to function properly, nutrients such as organic carbon,
,t 4 ,, nitrogen, and phosphorus must be available in adequate amounts. While domestic'
) wastewaters usually have an excess of nutrients, industrial wastewaters are sometimes
deficient. If a deficiency is identified, the performance of an industrial wastewater
l5`d 7 t ' treatment plant can be improved through nutrient addition."
Proper nutrient addition is needed for optimum oxidation of the organics in wastewater, good
solids - liquid separation, and to allow good sludge growth, nutrient utilization and minimum
25 FINAL
October, 1999

I�l
fami
effluent nutrient levels..A lack of sufficient nutrients usually results in inconsistent organic
removal, poor settling due to the formation of unhealthy biological floc or overpopulation of
filamentous organisms, and increased discharges of non -limited nutrients. Nutrient addition
usually improves the treatment performance in nutrient -deficient systems because of more
complete oxidation of organics and healthier microorganisms.
It is essential to add nutrients in a form that can be easily utilized by the wastewater
microorganisms, such as phosphoric acid and urea. Usually in wastewater treatment
applications, phosphorus is added in the form of phosphoric acid (ortho-phosphorus) and
nitrogen is added in the form of urea. The generally recommended nutrient needs of activated
sludge are one kg of phosphorus and five kg of nitrogen for every 100 kg of BOD5 oxidized (a
BOD5:N:P ratio of 100:5:1). This ratio has worked for treatment of most industrial
Fmt wastewaters. A typical bacterial cell has the following chemical composition:
C106H181O45N16P. The exact amount of nitrogen and phosphorus needed is dependent on the
carbonaceous yield factor, which is a variable dependent on substrate type. Assuming a yield
of 0.5 kg of bacteria produced per kg of BOD oxidized, the stoichiometric need for nitrogen
E and phosphorus would be a BOD:N:P ratio of 100:4.6:0.65. The generally used ratio of
100:5:1 is usually sufficient to satisfy the stoichiometric need for nutrients. However, some
floR
Pal
14114
wastewaters with a high carbonaceous yield factor could have a higher need for nutrients.
There are several factors which affect nutrient needs. These include: sludge age, treatment
temperature, carbonaceous waste and treatment configuration, and wastewater chemistry.
3.4.1 Sludge Age
The bacterial growth in an activated sludge system is the sum of two major processes,
cell synthesis and cell decay. Cell decay is the natural death rate of bacteria combined
with the cell maintenance requirements and endogenous respiration often expressed as a
fraction of the biomass per day. Cell decay releases nutrients which are internally
recycled, reducing the nutrient requirements. Longer sludge ages can minimize
nutrient requirements. Typically sludge ages in excess of 20 days have been successful
26
FINAL
October, 1999

FRI
Irf
Pal
to reduce nutrient requirements. As noted earlier, the sludge age at the Clariant system
averages approximately 32 days, which provides a system with minimum nutrient
requirements.
3.4.2 Treatment Temperature
Treatment temperature can significantly affect the nutrient requirements for good
treatment. Cell maintenance needs are higher at higher temperatures, which leaves less
BOD for cell growth and lower nutrient needs per kg of BOD treated. The mesophilic
range for activated sludge operation, which is the commonly utilized process in the
OCPSF facilities, is 4-39°C. The Clariant system typically operates at temperatures
between 10 ° C and 30 ° C which provides a basis for minimum nutrient requirements. In
general, more bioavailable phosphorus is required per kg of BOD5 treated by the
microorganisms during winter conditions than during summer conditions.
3.4.3 Carbonaceous Waste and Treatment Configuration
Rapidly simulated soluble carbonaceous substrates require a higher concentration of
soluble nutrients for proper treatment compared to substrates that are more slowly
degraded. This is because wastewater treatment bacteria rapidly take up readily
degradable soluble substrates by facilitated transport while inorganic nutrients such as
nitrogen and phosphorus must enter the cells simply by diffusion. The facilitated
carbon uptake rate can exceed the nutrient diffusion rate, causing nutrient deficiency
within the biomass. This imbalance can only be overcome by increasing the nutrient
concentration around the biomass, causing an increase in the nutrient diffusion rate into
the biomass.
The Clariant wastewater has a high carbonaceous uptake rate and correspondingly a
high oxygen uptake rate. Because of these high uptake rates and the utilization of a
complete mix activated sludge process, which is required for a highly variable batch
production facility, the nutrient requirements can be elevated for this type of operation.
In addition, wastewaters that have a phosphorus diffusion limitation require higher bulk
27
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October, 1999

concentrations of soluble phosphorus for good treatment. Systems with high soluble
BOD5 and high oxygen uptake rates can result in sludges with elevated polysaccharides
concentrations, which will then prevent good solid-liquid separation.
3.4.4 Wastewater Chemistry
Phosphorus is usually present as phosphoric acid. Although many forms of residual
phosphorus can be chemically measured, phosphate residual is usually measured as two
fractions, soluble ortho-phosphate and total phosphorus. Only the soluble ortho- (,,A ,
phosphate is available as a nutrient for the biological treatment system, and in many �l
cases the measured ortho-phosphate is not bioavailable. Phosphorus can be complexed
as sparingly soluble salts of calcium, iron, and aluminum depending on the wastewater
pH. A plot of phosphorus solubility and precipitation with respect to pH for calcium,
iron and aluminum is presented in Figure 3. As shown in this figure, phosphorus is
complexed by calcium, which is a significant component of lime added in both the
primary neutralization/clarification system and the activated sludge basin at the Clariant
facility. The chemical precipitation of soluble ortho-phosphate yields a soluble
phosphorus complex that filters and colormetrically measures as soluble phosphorus but
is not readily bioavailable. The literature indicates that effluent ortho-phosphate
concentrations of at least 2.5 mg/1 can be required in order to have sufficient
concentrations of bioavailable phosphorus for healthy microorganism growth when
phosphorus complexing chemicals (such as calcium) are present.
Unlike municipal wastewater, which is naturally high in nitrogen and phosphorus,
industrial wastewater is more likely to be deficient in nutrients due to the lack of
domestic wastewater in the influent. Like many industrial wastewaters, Clariant's
process wastewater is deficient in nutrients. The wastewater influent is very low in
phosphorus concentrations and is deficient in phosphorus in a form that is readily
available to the microorganisms, especially after the addition of lime during primary
treatment.
28 FINAL
October, 1999

Figure 3. Equilibrium Solubility Diagram for Fe, Al, and Ca
4
-2
0
-3 a
cn
4 `0
CL n
a)
CD
-5 > o E
0)
-6 •cn
0
0)
7 J
-8
4.5 5 5.5 6 6.5 7 7.5 8 8.5 9 9.5 10
pH

lia
The Clwastewater normally contains sufficient nitrogen for biological treatment.
A portion of the organic nitrogep in the influent is refractory in nature and is therefore
in a form that cannot be readily utilized by microorganisms. However, the Clariant
wastewater typically contains sufficient ammonia nitrogen for healthy biological
treatment. Therefore, only phosphoric acid must be added to the 151 stage aeration
basin in order to provide the nutrients needed for proper biological growth and
optimum treatment performance.
As discussed in Section 1.2, a significant reduction in Clariant's limits for BOD5, NH3-N and
OCPSF constituents has been proposed by NCDENR. The treatment plant was in compliance
with Clariant's current effluent criteria at the initiation of the BAT study. However, the
treatment plant performance was not adequate to consistently meet the BOD5 and NH3-N limits
being proposed by NCDENR and there was a high degree of variability. Therefore, a nutrient
optimization program was implemented at the Clariant WWTP in December 1998 with addition
of phosphoric acid beginning on December 3, 1998. The objective of this program was to
improve biodegradation and optimize the performance of the treatment system using the
current BAT treatment technology to improve nitrification, degradation of organic nitrogen and
removal of BOD5. Average effluent BOD5 and NH3-N concentrations are plotted in Figure 4
and include the periods prior to and following implementation of nutrient addition. These
values show that there was a significant reduction in both effluent BOD5 and NH3-N following
the implementation of phosphoric acid addition, especially during winter months when
performance of the biological treatment process has frequently declined. In addition, effluent
concentrations of BOD5 and NH3-N have been more consistent with the addition of
phosphorus. Since the implementation of phosphorus addition, the frequency and severity of
treatment upsets has decreased significantly.
IMO
Overall, the system provides better biodegradation, better nitrification, and more reliable
performance since implementation of the phosphoric acid addition. The data presented in
Figure 4 demonstrate that the addition of phosphorus to the wastewater is critical in optimizing
30
FINAL
October, 1999

Effluent BOD5 and NH3-N (mg/L)
Figure 4. Full -Scale Effluent BOD5 and NH3-N
(7-Day Running Averages)
0
9/22/98 10/22/98 11 /21 /98 12/21/98 1/20/99 2/19/99 3/21/99 4/20/99 5/20/99 6/19/99 7/19/99 8/18/99 9/17/99
13024s004
Figure 4
10/21/99

Rog
PtI
11
biodegradation, effluent quality and overall treatment performance. Based on this data, it is
obvious that without the addition of phosphorus, the performance of the treatment plant would
suffer and effluent quality would significantly deteriorate.
It is AEI's opinion that the Clariant WWTP would not be able to meet the new BOD5, NH3-N
and OCPSF effluent limits being proposed by NCDENR unless sufficient ortho-phosphate
concentrations are maintained in the aeration basins through phosphoric acid addition.
3.5 NUTRIENT OPTIMIZATION
Clariant initiated a program to optimize nutrient usage in the full-scale WWTP. The primary
objective of the program was to reduce the effluent nutrient concentrations to the lowest levels
possible while providing sufficient nutrients for maintaining optimum treatment performance.
Phosphoric acid was continuously added to the aeration basins. Sufficient bioavailable
nitrogen is normally contained in the Clariant wastewater for optimal biological treatment.
The objective in optimizing the phosphoric acid addition was to develop a baseline nutrient
level from which BAT nutrient limits could be defined. Nutrients were optimized by close
0.' monitoring, process optimization, and implementation of a program to gradually reduce
phosphorus concentrations over a 10-month period. During this period, nitrogen and
1.1
phosphorus concentrations in the system and effluent quality were closely monitored.
Following each reduction in phosphoric acid feed, the performance of the system was
n
evaluated to ensure optimum performance was being maintained.
3.5.1 Analytical Monitoring
The nutrient optimization program included analytical monitoring of nutrients throughout
the waste treatment system. A summary of the full-scale monitoring performed throughout
the study is presented in Table 3-3. The monitoring data is included in Appendix B.
Generally, nutrients were monitored up to three times per week. Throughout the program,
NH3-N and o-PO4 were monitored in the final effluent
32 FINAL
October, 1999

FIR
PRI
F=I
SiIR
TABLE 3-3
SUMMARY OF NUTRIENT MONITORING
2i'ha�� t 4rr �' )
Pi.aram•.Y.r.e.tr.:.._. 4. ._r.._..
iiw:,% 'ej��t.'c ,�4
;.Surce »!>�
-1. 7 ;:��ty
r,, �
eMonitoi**: 1i - 'a'
. .�.i+..,�nm•
, A -.+ WWI
'le
er _
l
.,.. ?,%t_..},' .._ c, ,
Ammonia (NH3-N)
INF
3/wk
Composite
Ammonia (NH3-N)
FE
5/wk
Composite
Nitrite/Nitrate (NO2/NO3-N)
INF, FE
2/wk
Composite
Total Kjeldahl Nitrogen (TKN)
INF, FE
2/wk
Composite
Organic Nitrogen (Org-N)
INF, FE
2/wk
Composite
Total Nitrogen (TN)
INF, FE
2/wk
Composite
ortho-Phosphorus (o-PO4)
FE
2/wk
Composite
Total Phosphorus (TP)
INF, FE
2/wk
Composite
Total Phosphorus (TP)
AB
1/mo
Grab
(1) Abbreviations are as follows:
INF = influent to aeration basin
AB = aeration basin
FE = final effluent
33
FINAL
October, 1999

ri.,
since these represented nutrient forms most readily available to the microorganisms. For
'' the period of March 8, 1999 through September 30, 1999, TKN and NO3/NO2-N were
monitored in the influent and effluent along with effluent carbonaceous BOD5 (CBOD5).
3.5.2 Target Nutrient Addition
gm
The treatment plant operating data were evaluated to determine a baseline phosphoric acid
addition rate. The phosphorus addition dosages were gradually reduced over a 10-month
pm
,.,
1998 to January 1999, phosphoric acid was added to the aeration basin in excess based on
an approximate ratio of 1:100 for phosphorus to BOD5. Usually a 1-2 mg/1 residual of o-
PO4 and NH3-N indicates that sufficient nutrients are available. From January 1999
0.1 through September 1999, target o-PO4 dosages were gradually reduced. The initial effluent
data (December 1998) indicated an immediate significant reduction in effluent BOD5 with
the implementation of phosphorus addition. As data were collected that indicated that
sufficient phosphorus was being added and the treatment performance of the system was
0.4 being maintained, the phosphorus dosages were decreased. Target dosages were decreased
gradually in order to maintain effluent quality and not upset the system. In addition,
'`' because of the long sludge ages (approximately 32 days) and the high levels of calcium and
period while maintaining optimum treatment performance. The target phosphorus dosages
are summarized in Table 3-4. During the initial period of nutrient addition, December
resulting complexed phosphorus in the mixed liquor, a reduction in phosphoric acid feed
Mil
did not immediately impact the performance of the WWTP. Therefore, it was necessary to
allow several weeks of operation at the target nutrient levels in order to reach equilibrium
and to ensure that performance had not been compromised by the reduction in nutrient
addition.
R.,
3.6 PROCESS PERFORMANCE
The process performance of the treatment plant was monitored on an on -going basis throughout
I.,the study. This included data for BOD5, TSS, MLSS and hydraulic loading. These data are
included in Appendix B. As previously noted, prior to the initiation of the nutrient optimization
34 FINAL
October, 1999

TABLE 3-4
FULL-SCALE TARGET PHOSPHORUS ADDITION
12/3/98 - 1/11/99
1 / 12/99 - 3/2/99
3/3/99 - 4/20/99
4/21/99 - 9/30/99
1371b P/day (11.5 mg P/L)
961b P/day (8.1 mg P/L)
72.5 lb P/day (6.1 mg P/L)
47.3 lb P/day (4.0 mg P/L)
35
FINAL
October, 1999

rti
program, there was wide variability in effluent BOD5 levels on a weekly basis. Through the
system optimization, significant improvements in the treatment plant quality were achieved. A
summary of these data is shown in Figure 5. These data show that there was a significant
immediate reduction in effluent BOD5 following the implementation of the nutrient control
program. Following the implementation of phosphoric acid addition, the variability in the
effluent levels also decreased significantly and the system has been able to provide overall
improved biodegradation. However, the biodegradation declined slightly and the effluent BOD5
subsequently increased slightly approximately two weeks after implementation of the 4.1 mg/1
phosphorus addition rate. This level of phosphorus addition was therefore determined to be
optimal for addition of sufficient phosphorus for good biological treatment and minimal effluent
TP levels without degradation of effluent quality.
These data indicate that the system can consistently provide good quality effluent BOD5 but is
prone to some variability in effluent NH3-N during winter conditions. Secondary polymer
addition is required in order to control the effluent TSS levels. Overall, these data indicate a very
good level of treatment with feeding of sufficient phosphoric acid in spite of significant
variability in influent characteristics and wasteloads.
3.7 BASELINE EFFLUENT NUTRIENT CONCENTRATIONS
Over the course of the study, the treatment system has averaged approximately 97% BOD5
removal and 55% TN removal. TN removals in the existing Clariant WWTP processes are
primarily due to nitrogen uptake by bacteria in the removal of carbonaceous BOD5. Based on the
full-scale WWTP data collected, current nitrogen utilization and removal is approximately 3.7
mg/1 TN per 100 mg/1 BOD5 removed (i.e. BOD5:N ratio of 100:3.7). A summary of removal
efficiencies is included in Table 3-5. These data indicate that optimal phosphorus addition levels
were reached during this study. It is felt that further reduction in phosphorus addition would
result in a deterioration of effluent quality. Furthermore, the Clariant WWTP would not be able
to meet the new BOD5, NH3-N and OCPSF constituent limits being proposed by NCDENR at
lower levels of phosphorus addition.
36
FINAL
October, 1999

3
3
3
1
3
3
1
$
1
3
3
3
1
II
1
1
1
1
Effluent ortho-P and Phosphorus Added (mg/L)
18
Figure 5. Full -Scale Phosphorus Addition and Effluent orth-P and BOD5
(30-Day running Averages)
11/1/98
13024s009
Fig.5
12/1/98
12/31/98
1/30/99
3/1/99
3/31/99
4/30/99
5/30/99
—♦— P Added (mg/L)
—e— Eff Ortho-P (mg/L)
Eff BOD (mg/L)
6/29/99
7/29/99
8/28/99 9/27/99
10/21/99

Fmt
latl
islA
TABLE 3-5
SUMMARY OF REMOVAL EFFICIENCIES
Parameter ..> ;
,,'
e
Average Concnirat an mg/l
rce -Pen t
-RemovalY
:Influent
MEffiuent Y.
BOD5 (1)
519
16
97 %
NH3-N (2)
28.1
12.5
56 %
NO2/NO3-N (2)
0.2
2.8(4)
--
TKN (2)
34.8
12.3
65 %
Organic N (2)
15.4
2.9
81 %
N (2)
33.5
15.1
55%
TNN (2
19.6
12.6
36%
TP (3)
5.36
1.40
74 %
(1) BOD5 concentrations based on monitoring data from October 1, 1998 to
September 30, 1999.
(2) Nitrogen concentrations based on monitoring data from April 1, 1999 to
September 30, 1999.
(3) Phosphorus concentrations based on monitoring data from May 5, 1999 to
September 30, 1999. Influent concentrations include average phosphorus
addition.
(4) Increase in nitrite/nitrate nitrogen due to nitrification of ammonia nitrogen.
(5) All data was evaluated and outlying data was not used in calculating average
concentrations.
v,�► CwL3rt-r1�
�w c
ot. '
vo-4 '
38
toy-.?ter'
FINAL
October, 1999

0.9
Using the US EPA methodology summarized in Section 1.3, AEI evaluated baseline effluent
TN and TP wasteload based on the statistical analysis of the full-scale operating data under
optimized conditions to define appropriate average monthly effluent limits. The TP was based
on the data for the five (5) monthly periods May 5, 1999 through September 30, 1999, which
corresponds to the period during which phosphorus addition was minimized. The TN analysis
is based on the data from April 1, 1999 through September 30, 1999, which corresponds to
summer operating conditions.
The statistical analyses of the TP and TN data presented in Figures 6 and 7, respectively.
These data, which are included in Appendix C, indicate 95 percentile concentrations of 2.6
mg/1 TP „and 37.5 mg/1 TN. These concentrations represent the baseline concentrations and the
monthly average oncentration limits that could be met by the existing optimized BAT
treatment plant w thout incorporation of additional treatment processes. Based on the long
term average (L A) flows previously determined by the NCDENR for the Clariant discharge
flow of 1.42 D, the proposed monthly average mass discharge limits are:
TP
N
30.8 lbs/day
444.1 lbs/day
The baseline TN represents a 32% reduction in nitrogen from Clariant's current ammonia
nitrogen (NH3-N) limit, of 651 lb/d.
6P�
- (� ;Jr."'
-�, --ifj
t 7
39
FINAL
October, 1999

11111■111.1.-
FIGURE 6
Statistical Analysis of WWTP Effluent TP (5/5/99-9/30/99)
4.0
1.0
0.0
0.01
0.4
•
r-
•
•
•
5 10 20 30 40 50 60 70 80
PROBABILITY (%)
WPM
9.0
IM
•
•
90 95
99
99.9
99.99

l ] ) 11i 1 9
45
40
30
cn
20
41)
-
10
0
FIGURE 7
Statistical Analysis of WWTP Effluent TN (4/1/99-9/30/99)
I
II 11111111��111111ll
I II Ili
om
I II
m ppm I
111
im
II 1111H
CD I i ■ 111111114111111111111111111
��lu1 hi I �ii��iui� i�i�
�� !I� ' ���°iiili I 1
11111111111111111111011111111111114110
u 1 .,c ����n �
n �mu� i
a
u u uun �
0.01 0.4 1
111 I 1 111111 II 11
III 1 111 1 HIT 1 I 11�
1
11� 1 ill
I
NJ I �1 � ill 1
111I111111 1 �1111111 i1� 1
pilli II II 1111I� I� 1 111 �
w III u 'Hui 1 1
uu���u m
III II 11
III III
HI II
III 11 II
II
'u II u II uyu,u I m I
1
u u III II II
i a i�ili! m i
Iimmuit 1
IiimplA
iii 1
III I
III I
�ii ii1
i Ii II �iiiii1
i�i� 1 111 i 1
Inlii • ill li
ul ii 114
� uuu�iiii iu�III
1
'1Mili�9 �II!!IIiiII!!i11I.
I I in i u1
I��n.�illn i Howl
moon 1H1"'1'11IIIIIIIflUIIOlIIIIIII1iiii111
1111111111 II I 1111111111Iii1��lIIIIIllllll����i���iiiii i 1
, °��°���iH,il��i�IIIlll1111!!! IIIinm ii Hi 1
10 20 30 40 50 60 70 80 90 95 99 99.9 99.99
PROBABILITY (%) AW 'ATE IHc

neWn
SECTION 4.0
TREATABILITY ANALYSIS
4.1 GENERAL
An analysis of the wastewater treatment facilities indicates that Clariant operates a BAT
treatment facility. However, due to the nature of the wastewater, the facility has been unable
to provide highly consistent biological nitrification especially during winter conditions. An
evaluation of alternative treatment technologies, applicable to the Clariant facility, was
conducted. A review of the historical operating data plus environmental considerations at the
Mt. Holly site indicate that of the alternatives evaluated, biological treatment offered the
greatest potential to provide cost-effective removal of nitrogen which would be consistent with
BAT technology. In order to reduce the level of effluent total nitrogen (TN), upgrade of the
existing nitrification process and addition of denitrification will be required. The full-scale
treatment system has provided a high level of biological nitrification in the summer and at least
partial nitrification in the winter with the addition of sufficient phosphoric acid. Therefore,
this technology appears to be consistent with the Clariant facility.
A biological treatability analysis of nutrient control strategies was conducted. There were two
objectives of this study. One was to define the effluent TN that could potentially be achieved
with installation of a single -sludge nitrification/denitrification process at the Clariant plant.
The second objective was to confirm the total phosphorus (TP) discharge consistent with
optimized treatment plant performance. Complete information on the treatability analysis is
presented in a report included in Appendix D.
4.2 ACHIEVABLE NITROGEN CONCENTRATIONS
In order to determine the TN which would be discharged from a full-scale system based on the
results of these pilot studies, a statistical analysis of the steady state operating data was
conducted. Consistent with the EPA OCPSF procedure, the 95`h percentile concentration was
selected as maximum month. This indicates the baseline level of treatment that could be
expected if the wastewater treatment plant is upgraded to achieve nitrification and
42
FINAL
October, 1999

r4r4
denitrification. Based on the results of the pilot study, the effluent level which could be
expected from the upgrade of the Clariant treatment plant to include single -sludge biological
nitrification and denitrification is 19 mg/1 TN. To be consistent with the OCPSF effluent
limits for the plant, mass -based limits using the long term average (LTA) flow of 1.42 MGD
are recommended. This results in a recommended baseline of 225 lbs/day TN. These pilot
test levels represent average removals of approximately 72 % TN removal from the Clariant
wastewater.
4.3 ACHIEVABLE PHOSPHORUS CONCENTRATIONS
Based on a statistical analysis of the effluent phosphorus values for pilot unit 2, the 95th
percentile total phosphorus concentration consistent with anticipated monthly average winter
conditions was 1.5 mg/1.
The pilot unit results indicate that the WWTP could potentially achieve a monthly average total
,., phosphorus concentration of 1.5 mg/1 with sodium -based alkalinity addition in lieu of lime.
For comparison, the optimized full-scale WWTP had an effluent total phosphorus
concentration of 2.6 mg/1 while using lime for pH control, which results in greater phosphorus
content in the TSS. Since NaHCO3 was used for pH control in the pilot units, the effluent TP
concentrations achieved in the pilot appear to be lower than can be achieved in long-term full-
scale operation using lime. When lime is used for pH control, this significantly reduces the
` phosphorus bioavailability, requiring higher effluent TP residuals in order to have adequate
dissolved orthophosphate available for biological treatment. The higher percentages of
particulate phosphorus in the sludge solids occur due to formation of calcium phosphate
precipitates and adsorption of phosphorus to gypsum (CaSO4) and other precipitates formed as
raM
a result of the lime addition. This increases the phosphorus content of the effluent TSS, which
also increases the effluent total phosphorus. To be consistent with the OCPSF limits for the
Clariant plant, it is recommended that the phosphorus limit be maintained on a mass basis
based on the 2.6 mg/1 TP concentration. At the LTA 1.42 MGD flow rate, this is equivalent
to 30.8 lbs/day TP.
43 FINAL
October, 1999

SKI
4.4 SIGNIFICANCE OF TREATABILITY FINDINGS
'." The results of the treatability analysis provided additional information on the baseline effluent
TP levels which would be required for consistent biological nitrification/denitrification of the
4.' Clariant wastewater. In addition TN levels which would be consistent with application of
biological nitrification/denitrification, were defined. The baseline effluent quality and the
achievable effluent quality with the application of biological nitrification/denitrification
technology are presented in Table 4-1. These effluent quality levels provide the basis for
evaluating BAT and conducting a cost-effective analysis to determine if the addition of
treatment technology would be applicable for the Clariant facility and consistent with BAT
applications.
raq
E,
44
FINAL
October, 1999

TABLE 4-1
SUMMARY OF TREATABILITY FINDINGS
Parameter/Condition ,,s
t
[ �' i..
s , = 'S i ,� �� ' .
.�r4:fN •
r D�schargee�el
Con' : '(mg/1) T
Mass' (lb/daa')(s�•
Baseline TP with Lime Alkalinity Addition°
2.6
30.8
Baseline TP with Sodium -Based Alkalinity Additionw
1.5
17.8
Baseline TN(3)
37.5
444.1
TN with Advanced Nitrification/Denitrificationn44
19.0
225.0
Notes:
(1) Baseline TP with lime alkalinity addition is based on results of full-scale Clariant WWTP
receiving Clariant east site waste from May 5, 1999 to September 8, 1999.
(2) Baseline TP with sodium -based alkalinity addition is based on results of pilot unit 2 receiving
Clariant east site waste and operated at 10 ° C.
(3) Baseline TN is based on results of full-scale Clariant WWTP receiving east site waste from
April 1, 1999 to September 8, 1999.
ANN
(4) Achievable TN levels are based on results of pilot unit 1 receiving Clariant east site waste and
operated at 18°C.
(5) Mass, lbs/day discharge levels are based on the LTA flow of 1.42 MGD.
Plitk
45
f,
FINAL
October, 1999

eXt
fftt
twl
gib
taR
etza
SECTION 5.0
COST EFFECTIVE BAT ANALYSIS OF
ALTERNATIVE TERTIARY TECHNOLOGIES
Through the treatability analysis and full-scale WWTP optimization program, the baseline total
phosphorus and nitrogen wasteload from the existing Clariant BAT OCPSF treatment system
and achievable discharge levels have been developed. The objective of this section is to review
the technically feasible systems for providing additional levels of treatment for reduction of
total nitrogen (TN) and total phosphorus (TP). The objective of these technologies is to
provide treatment to levels that can meet or approach the NCDENR target nutrient limits of 6
mg/1 TN and 1 mg/1 TP, if possible.
Typically, phosphorus removal can be achieved by precipitation using a chemical coagulant
such as ferric chloride. Based on the nature of the wastewater, tertiary treatment with ferric
chloride was deemed appropriate for phosphorus removal. For the Clariant WWTP, a lower
effluent TP could also be achievable by switching from lime addition to caustic (sodium
hydroxide) addition for alkalinity control. Nitrogen removal can be achieved by various
biological and physicochemical treatment technologies. Based on the success of the treatability
study, it was determined that single -sludge biological nitrification/denitrification was the most
appropriate alternative for nitrogen reduction. Further removal of NO2/NO3 nitrogen for
reduction of effluent TN could be achieved using tertiary denitrification with methanol
addition. Both tertiary precipitation and substitution of sodium based alkalinity addition for
phosphorus removal/reduction and both single -sludge biological nitrification/denitrification and
tertiary denitrification for nitrogen removal were evaluated.
Process designs were developed for each of the nutrient removal technologies mentioned above
and were developed based on typical waste loads in the full-scale system. The process designs
are presented in this section along with a discussion of their specific merits and preliminary
cost estimates. The basis of the designs and calculations are included in Appendix E. A
maximum monthly flow rate of 1.55 MGD was utilized for sizing process components. A cost
effectiveness analysis has been conducted to determine if implementation of these technologies
46
FINAL
October, 1999

Fan
MCA
is consistent with BAT technology criteria. Cost analyses were based on equivalent annual
costs assuming a capital recovery factor for 10 years at 9% interest and including annual
operating costs. This section focuses on a presentation of the actual design parameters and the
estimated cost to implement and operate each of these treatment technologies.
5.1 PRECIPITATION USING FERRIC CHLORIDE FOR PHOSPHORUS REDUCTION
Precipitation using ferric chloride is a treatment technology for reducing phosphorus
concentrations to very low levels. A tertiary treatment system was designed and the design
information is presented in Table 5-1. The system was designed as a tertiary treatment system
and should be implemented following secondary clarification. A process flow diagram of the
system is presented in Figure 8.
The system includes a rapid mix tank, a flocculation tank, tertiary clarification and
neutralization. The rapid mix tank provides flash mixing for chemical addition. Liquid ferric
chloride is flow -paced to the rapid mix tank using a chemical metering pump and a magnetic
flow meter. Polymer is added in the rapid mix tank to aid settling in the tertiary clarifier.
rstN Slow mixing is provided in the flocculation tank to allow proper formation of floc particles. In
addition, the pH of the wastewater is adjusted in the flocculation tank in order to provide
1.4 proper pH conditions for phosphorus precipitation. The addition of ferric chloride to
wastewater causes a slight reduction in pH. Typically, the optimum pH range for phosphorus
fvC precipitation is 4.5-5.0; however, optimum pH varies depending upon the constituents in the
wastewater and tends to be higher for industrial wastewater. It is expected that the addition of
ferric chloride will cause a significant decrease in pH because of low alkalinity levels in the
wastewater. Therefore, the pH will need to be increased using sodium hydroxide in order to
r.
n
achieve effective phosphorus removal. The flocculation tank is equipped with a pH control
system to adjust pH to the target pH using sodium hydroxide.
Each tertiary clarifier is designed to handle slow solids settling with an overflow rate of 300
gpd/ft2. A portion of the settled solids from the tertiary clarifiers is pumped back to the
flocculation tank to serve as a seed in order to enhance precipitation. The remaining settled
47
FINAL
October, 1999

afi
im,
TABLE 5-1
PROCESS DESIGN SUMMARY FOR TERTIARY PHOSPHORUS
REMOVAL USING PRECIPITATION
` Parameter �c,
Design 'Value
Maximum Monthly Average Flow
Average Flow
1.55 MGD
1.42 MGD
Phosphorus
Influent Phosphorus (I)
Effluent Phosphorus
Phosphorus Removal
1.4 mg/1
1.0 mg/1
0.4 mg/1
Ferric Chloride Dose
4 mg/1
Polymer Dose
5 mg/1
Caustic Dose
2.9 mg/1
Rapid Mix Tank
Volume
Detention Time @ 1.55 MGD
480 gal
0.5 min
Flocculation Tank
Volume
Detention Time @ 1.55 MGD
15,200 gal
15 min
Tertiary Clarifiers
Number
Diameter
Surface Area
Side Water Depth
Hydraulic Loading Rate
2
81 ft
5153 ft2
12 ft
300 gpd/ft2
Neutralization Tank
Volume
Detention Time @ 1.55 MGD
5,450 gal
5 min
Estimated Sludge Generation
Settled Tertiary Solids (1 % Solids)
Dewatered Sludge (25 % Solids)
Dry Sludge
275 gal/d (0.2 gpm)
92 lb/d (1.5 ft3/d)
23 lb/d
(1) Influent phosphorus to the precipitation system is based on full-scale final effluent
data collected from 5/5/99 - 9/30/99 during optimum treatment conditions and
phosphorus addition. The full-scale average effluent TP is 1.40 mg/1.
48
FINAL
October, 1999

J ZI B
1 fJ
I 01
POLYMER
STORAGE
POLYMER FEED
SYSTEM PUMPS
FERRIC
CHLORIDE
STORAGE
SECONDARY
• CLARIFIER
EFFLUENT
ea -
FERRIC
CHLORIDE
METERING
PUMPS
RAPID MIX TANK
FM
pH
LEGEND
FLOW METER
pH CONTROLLER
October 21. 1999 1:21:04 p.m.
Drawing: V: \N130\13024P01.DWG
r
r-
1
NaOH
METERING
PUMPS
}
fan
FLOCCULATION TANK
AND pH ADJUSTMENT i TERTIARY
L I CLARIFIERS
I
�----� TO SLUDGE DEWATERING
NaOH
STORAGE
pH
NaOH
METERING
PUMPS
}
214751339
NEUTRALIZATION
TANK
FINAL EFFLUENT
DISCHARGED TO
CATAWBA RIVER
CLARIANT
PRECIPITATION WITH FERRIC CHLORIDE
SCALE N.T.S.
DATE OCT. 1999
PROJECT NUMBER
N 130- 24
APPROVED BY :
DESIGNED BY : L. GELLNER
AWAVI ,
[NVIR lMLNiAI IIIC
DRAWN BY: M R w
REVISED
DRAWING NO.
S11'1 .1 MONROI 1?1►. 1: IA121(11 11 N': ,M,,f FIGURE 8

tertiary solids are handled by the existing sludge handling equipment. Based on the estimated
solids generation rate of 23 lbs/day (0.2 gpm of 1 % solids) resulting from tertiary
precipitation, the existing sludge press has sufficient capacity to handle the estimated additional
solids load.
Following clarification, it may be necessary to increase the pH of the wastewater using sodium
hydroxide in order to meet Clariant's effluent permit limit of 6.0. This will depend on the
target pH in the flocculation tank. The neutralization system has been sized using sodium
hydroxide and equipped with a pH probe and pH control system. The pH controller is used to
meter sodium hydroxide to the neutralization tank. Following neutralization, the treated
wastewater is discharged to the Catawba River.
gal
This treatment technology is expected to reduce the average effluent phosphorus concentration
from 1.40 mg/1 to 1.00 mg/l. However, treatability testing should be performed to confirm the
effectiveness of this technology on the Clariant wastewater and to determine the optimum pH
for phosphorus precipitation. Construction and installation of the new facilities will cost
h approximately $1,658,000 with an annual operating cost of $38,900. The annualized cost for
this treatment technology is $297,300 per year. Based on an average phosphorus removal of
r 0.40 mg/1 at 1.42 MGD, the cost of treatment is $172/1b P.
5.2 SODIUM -BASED ALKALINITY ADDITION FOR PHOSPHORUS REDUCTION
The average full-scale effluent TP concentration from May 5, 1999 to September 30, 1999 was
1.40 mg/L. Based on the results of the treatability analysis, the average monthly levels in the
Clariant effluent could be reduced to approximately 0.90 mg/1 TP if addition of sodium -based
alkalinity was used in lieu of the current lime addition for pH control. This is an average
phosphorus reduction of 0.50 mg/l. Use of lime for pH control reduces the bioavailability of
phosphorus in the biological treatment process and increases the level of particulate phosphorus
in the sludge solids due to formation of calcium phosphate precipitates. This in turn requires
higher levels of phosphoric acid addition for biological treatment and increases the required
Mtt
50
n
FINAL
October, 1999

1A1
eretl
level of dissolved and particulate phosphorus in the effluent from the biological treatment
process.
A pH control system, which would utilize 50% sodium hydroxide (caustic) for pH control,
was designed and the design information is presented in Table 5-2. A process flow diagram of
the system is presented in Figure 9. The system includes 2 caustic storage tanks and a caustic
metering pH control system for addition of caustic to the primary neutralization system and the
activated sludge basins for control of pH.
This treatment alternative is expected to reduce the average effluent phosphorus concentration
from 1.40 mg/1 to 0.90 mg/1. Construction and installation of the new facilities will cost
approximately $772,580 with an annual operating cost of $2,702,000. The annualized cost for
this treatment technology is $2,822,400 per year. Based on a reduction of 0.50 mg/1 of TP at
a flow of 1.42 MGD, the cost of treatment is $1,306/1b P.
5.3 OVERVIEW
_, In order to achieve nitrogen removal both single -sludge nitrification/denitrification and an
optimized activated sludge nitrification followed by tertiary denitrification with methanol
addition were evaluated. Single -sludge nitrification/denitrification uses the influent BOD5 as
the primary carbon source for denitrification, while tertiary denitrification uses methanol
1.4 additional as the primary carbon source. Single -sludge nitrification/denitrification is not as
efficient in reducing effluent NO2/NO3-N as tertiary denitrification since the nitrified waste is
recirculated to the head end of the system. This should not cause an increase in effluent BOD5.
The tertiary denitrification system is expected to provide lower effluent NO2/NO3-N
concentrations and lower TN, however, the system could result in elevated effluent BOD5
concentrations due methanol addition. Sufficient methanol needs to be added in order to
provide sufficient carbon for denitrification.
falt
51
FINAL
October, 1999

r-+
024
Mcf
CAP
TABLE 5-2
PROCESS DESIGN SUMMARY FOR SODIUM -BASED ALKALINITY
ADDITION FOR PHOSPHORUS REDUCTION
SL t r Ee: aramete.> } -- ,
4':-�`Design Yalue:. i -
Average Flow
1.42 MGD
Phosphorus
Influent Phosphorus
Effluent Phosphorus
Phosphorus Removal
1.40 mg/1
0.90 mg/1
0.50 mg/1
Caustic Addition
NaOH Dose
Daily Addition of 50% NaOH
2226 mg/1 (26360 lb/d)
52,750 lb/d (4135 gpd)
Caustic Storage Tank Capacity
30,000 gal
(1) Full-scale average effluent phosphorus is 1.40 mg/1 from 5/5/99-9/30/99.
Met
fztv
Nib
52
FINAL
October, 1999

3
0
11
ACID
WASTEWATER
CAUSTIC
FOR pH
CONTROL
r
NO.1 NO.2
NEUTRALIZATION TANKS
ALKALINE
WASTEWATER
October 27. 1999 3:16:02 p.m.
Drawing: V: \N130\13024P02A.DWG
CAUSTIC STORAGE
A
A
WASTED
SLUDGE
PHOSPHORIC
ACID
PRIMARY
CLARIFIERS
CAUSTIC
FOR pH
CONTROL
AERATION BASIN
ZO3A
AERATION BASIN
Z04
RAS FROM SECONDARY CLARIFIERS
WAS FROM SECONDARY CLARIFIERS
FROM
HOLDING
BASIN
TO BELT
. FILTER
PRESS
TO
-0-SECONDARY
CLARIFIERS
CAUSTIC ADDITION FOR
ALKALINITY CONTROL
SCALE N.T.S.
DATE OCT. 1999
PROJECT NUMBER
N 130- 24
APPROVED BY : DRAWN BY: MRW
DESIGNED BY : REVISED
A l'; vr� DRAWING NO.
NVQ AR.� ,11 FIGURE 9
9.30'.- .1 Mf)WRf 11� 1217. �:IIARi f)1 li , N�: JR7Yf) '

t�1
lart
mei
rAm
mit
Igza
5.3.1 Single -Sludge Biological Nitrification/Denitrification
The Clariant wastewater contains significant concentrations of influent ammonia. As
was shown in treatability testing, single -sludge biological nitrification/denitrification
can be used to reduce effluent NO2/NO3-N and TN concentrations. Necessary additions
to the Clariant WWTP were designed, and the design information is presented in Table
5-3. A process flow diagram is presented in Figure 10.
The modifications to the Clariant WWTP which would be required for implementation
of the single -sludge nitrification/denitrification process include a new 0.34 MG
denitrification basin, installation of submersible mixers in aeration basin Z03A, a new
recirculation pump station, a steam injection system and additional process piping.
BOD5 in the influent wastewater will normally be utilized as the carbon source for
denitrification. Provisions for standby feeding of supplemental methanol would be
included to ensure maximum nitrate removal during any low influent BOD5 periods.
Improved biological nitrification would be necessary in order for removal of nitrogen
by denitrification to be possible. Based on the results of the treatability analysis, the
performance of the biological nitrification process should be improved by heating the
incoming wastewater as required to maintain a minimum mixed liquor temperature of
18 ° C through the winter, addition of phosphoric acid to the mixed liquor, and thorough
mixing of the entire 4.5-MG volume of aeration basin Z03A to maintain aerobic (oxic)
conditions throughout the basin and prevent settling of mixed liquor solids in the basin.
Based on the data previously presented in Table 3-5, the average full-scale effluent TN
is 15.1 mg/1. Based on the results of the treatability analysis, this treatment system
should be capable of reducing the average TN concentrations to approximately 13.3
mg/1. This is a reduction 1.8 mg/1 TN.
54
FINAL
October, 1999

A'I
as
rat
p►
TABLE 5-3
PROCESS DESIGN SUMMARY FOR BIOLOGICAL
NITRIFICATION/DENITRIFICATION
'aranieter` _.. x
, k L °' Desgnw'valiew:, q
Maximum Monthly Average Flow
Average Flow
1.55 MGD
1.42 MGD
Nitrification/Denitrification System (1)
Effluent TN w/o Nit/Denit (2)
Effluent TN w/ Nit/Denit (3)
Additional TN Removed
15.1 mg/1
13.3 mg/1
1.8 mg/1
Steam Injection
Target Wastewater Temperature
Est. Steam Required:
18°C
20.87x106 lb/year
Additional Aeration Mixing
Number of Mixers
Horsepower, each
4
40 Hp
Denitrification Basin
Volume
Detention Time @ 1.55 MGD
0.34 MG
5.3 hrs
(1) Nitrogen removal is estimated based on current average full-scale BOD5 and TN
removals and enhanced nitrification to oxidize ammonia to nitrate nitrogen based
on observed pilot scale efficiencies.
(2) Based on the average full-scale effluent concentrations under optimum treatment
conditions and phosphorus removal (April 1, 1999 - September 30, 1999).
(3) Based on the average pilot treatability effluent concentrations.
55
FINAL
October, 1999

Construction and installation of the system will cost approximately $1,252,400 with an
annual operating cost of $156,800. The annualized cost for this treatment technology is
$351,900 per year. Based on an average reduction of effluent TN from current levels of
15.1 mg/I to 13.3 mg/1 (nitrogen removal of 1.8 mg/1) at an average flow of 1.42 MGD,
the cost of treatment is $78/lb N removed based on nitrogen removal from April 1
through November 1.
5.3.2 Tertiary Denitrification
Tertiary denitrification using methanol addition for removal of NO2/NO3 nitrogen is a
treatment technology which could be applied for reducing TN levels in the Clariant
effluent discharge. Necessary additions to the Clariant WWTP were designed and the
design information is presented in Table 5-4. A process flow diagram is presented in
Figure 11.
The Clariant wastewater contains significant concentrations of influent ammonia. In
order for tertiary denitrification to be successful at the Clariant WWTP, improved
biological nitrification would be necessary. Based on the results of the treatability
analysis, the performance of the biological nitrification process should be improved by
heating the incoming wastewater as required to maintain a minimum mixed liquor
temperature of 18°C through the winter, addition of phosphoric acid to the mixed
liquor, and thorough mixing of the entire 4.5-MG volume of aeration basin ZO3A in
order to maintain aerobic (oxic) conditions throughout the basin and prevent settling of
mixed liquor solids in the basin.
The modifications to the Clariant WWTP which would be required for implementation
of the tertiary denitrification process include a new anoxic denitrification filter,
installation of submersible mixers in aeration basin ZO3A, addition of steam heating
capabilities to the WWTP, and installation of a methanol storage and feed system. This
treatment technology should be capable of reducing NO2/NO3 nitrogen levels to
approximately 1 mg/1. Based on results of the treatability analysis, this would reduce
57
FINAL
October, 1999

mei
TABLE 5-4
PROCESS DESIGN SUMMARY FOR TERTIARY DENITRIFICATION
Paramet
, Designalue
Maximum Monthly Average Flow
Average Flow
1.55 MGD
1.42 MGD
Nitrification/Denitrification System (1)
Effluent TN w/o Nit/Denit (2)
Effluent TN w/ Nit/Denit (3)
Additional TN Removed
15.1 mg/1
11.6 mg/1
3.5 mg/1
Steam Injection
Target Wastewater Temperature
Est. Steam Required:
18°C
20.87x106 lb/year
Additional Aeration Mixing
Number of Mixers
Horsepower, each
4
40 Hp
Denitrification Filter Unit
Total Surface Area
Hydraulic Loading Rate CO 1.55 MGD
Methanol Addition
741 ft2
1.45 gpm/ft2
18.6 mg/1 (33.2 gpd)
(1)
Nitrogen removal is estimated based on current average full-scale BOD5 and TN
removals and enhanced nitrification to oxidize ammonia to nitrate nitrogen based
on observed pilot scale efficiencies.
(2) Based on the average full-scale effluent concentrations under optimum treatment
conditions and phosphorus removal (April 1, 1999 — September 30, 1999).
(3) Based on the average pilot treatability effluent concentrations.
58
FINAL
October, 1999

9
3
NEW
STEAM
INJECTION
PRIMARY
CLARIFIER
EFFLUENT
NOTE:
METHANOL
STORAGE
TANK
ORP
rr
METHANOL
METERING
PUMP
NEW
STANDBY
METHANOL
FEED
SYSTEM
ORP
CONTROLLER
NEW
RECIRCULATION
PUMP STATION
NEW
DENITRIFICATION
BASIN
EXISTING EXISTING
AERATION BASIN AERATION BASIN
ZO3A Z04
'— EFFLUENT
DISCHARGED TO
'wii°'b' CATAWBA RIVER
EXISTING
SECONDARY
CLARIFIER
1. 160 Hp ADDITIONAL MIXING IN
AERATION BASIN ZO3A
October 22. 1999 8:24:43 o.m.
Drowing: V: \N130\13024P02.DWG
EXISTING RETURN
SLUDGE PUMP
STATION
SCHEMATIC FOR PROPOSED SINGLE —SLUDGE
NITRIFICATION/DENITRIFICATION SYSTEM
CLARIANT
SCALE N.T.S.
APPROVED BY : DRAWN BY: MRW
DATE OCT. 1999 DESIGNED BY : REVISED
PROJECT NUMBER DRAWING NO.
N 130- 2 4 9305 MOHPOE PD. CHARLOTTE, !IC 2.52 FIGURE 10

Construction and installation of the system will cost approximately $1,252,400 with an
annual operating cost of $156,800. The annualized cost for this treatment technology is
$351,900 per year. Based on an average reduction of effluent TN from current levels of
15.1 mg/1 to 13.3 mg/1 (nitrogen removal of 1.8 mg/1) at an average flow of 1.42 MGD,
the cost of treatment is $78/lb N removed based on nitrogen removal from April 1
through November 1.
5.3.2 Tertiary Denitrification
Tertiary denitrification using methanol addition for removal of NO2/NO3 nitrogen is a
treatment technology which could be applied for reducing TN levels in the Clariant
effluent discharge. Necessary additions to the Clariant WWTP were designed and the
design information is presented in Table 5-4. A process flow diagram is presented in
Figure 11.
The Clariant wastewater contains significant concentrations of influent ammonia. In
order for tertiary denitrification to be successful at the Clariant WWTP, improved
biological nitrification would be necessary. Based on the results of the treatability
analysis, the performance of the biological nitrification process should be improved by
heating the incoming wastewater as required to maintain a minimum mixed liquor
temperature of 18°C through the winter, addition of phosphoric acid to the mixed
liquor, and thorough mixing of the entire 4.5-MG volume of aeration basin ZO3A in
order to maintain aerobic (oxic) conditions throughout the basin and prevent settling of
mixed liquor solids in the basin.
The modifications to the Clariant WWTP which would be required for implementation
of the tertiary denitrification process include a new anoxic denitrification filter,
installation of submersible mixers in aeration basin ZO3A, addition of steam heating
capabilities to the WWTP, and installation of a methanol storage and feed system. This
treatment technology should be capable of reducing NO2/NO3 nitrogen levels to
approximately 1 mg/1. Based on results of the treatability analysis, this would reduce
57
FINAL
October, 1999

Fwl
duv
4.4
PIM
TABLE 5-4
PROCESS DESIGN SUMMARY FOR TERTIARY DENITRIFICATION
+ f Parameter
�i. ' ,Desigfl aloe
Maximum Monthly Average Flow
Average Flow
1.55 MGD
1.42 MGD
Nitrification/Denitrification System (1)
Effluent TN w/o Nit/Denit (2)
Effluent TN w/ Nit/Denit (3)
Additional TN Removed
15.1 mg/1
11.6 mg/1
3.5 mg/1
Steam Injection
Target Wastewater Temperature
Est. Steam Required:
18°C
20.87x106 lb/year
Additional Aeration Mixing
Number of Mixers
Horsepower, each
4
40 Hp
Denitrification Filter Unit
Total Surface Area
Hydraulic Loading Rate @ 1.55 MGD
Methanol Addition
741 ft2
1.45 gpm/ft2
18.6 mg/1 (33.2 gpd)
(1)
Nitrogen removal is estimated based on current average full-scale BOD5 and TN
removals and enhanced nitrification to oxidize ammonia to nitrate nitrogen based
on observed pilot scale efficiencies.
(2) Based on the average full-scale effluent concentrations under optimum treatment
conditions and phosphorus removal (April 1, 1999 — September 30, 1999).
(3) Based on the average pilot treatability effluent concentrations.
58
FINAL
October, 1999

fig
effluent NO2/NO3 nitrogen levels from 2.7 mg/1 to 1 mg/1 and produce an average
effluent TN of 11.6 mg/1. This is a reduction of 3.5 mg/1 TN from the full-scale
effluent average of 15.1 mg/1.
Construction and installation of the system will cost approximately $1,883,600 with an
annual operating cost of $185,100. The annualized cost for this treatment technology is
$478,600 per year. Based on an average effluent reduction of 3.5 mg/1 TN and an
average flow of 1.42 MGD, the cost of treatment is $54/1b N removed based on nitrogen
removal from April 1 through November 1.
Aft
A summary of the estimated costs for each treatment technology is presented in Table
CCM
5-5. These costs are based on a 10-year capital recovery factor at 9% interest. Also
included in Table 5-5 is a summary of the expected nutrient removal and the cost per
pound of nutrient removed.
60
FINAL
October, 1999

y
I
1
STEAM
INJECTION
PRIMARY
CLARIFIER
EFFLUENT
NOTE:
`gv / \ ogv
/--11110-
EXISTING
AERATION BASIN
ZO3A
1. 160 Hp ADDITIONAL MIXING IN
AERATION BASIN ZO3A
EXISTING
AERATION BASIN
Z04
ORP
CONTROLLER
ORP
EXISTING
CLARIFIERS
METHANOL
STORAGE
TANK
METHANOL
METERING
PUMP
DENITRIFICATION
FILTER
FINAL EFFLUENT
DISCHARGED TO
CATAWBA RIVER
SCHEMATIC FOR PROPOSED TERTIARY
DENITRIFICATION SYSTEM
CLARIANT
SCALE N.T.S.
DATE OCT. 1999
APPROVED BY :
DESIGNED BY :
DRAWN BY: MRW
REVISED
October 22. 1999 8:24:43 o.m.
Drawing: V: \N130\13024P02.DWG
PROJECT NUMBER
N 130- 24
i�� le Pa DRAWING NO.
'�t�'
9305-J FIGURE 11
►�OlIROE F'. CHAFL':tTT£, 11C 28�'C•

1
TABLE 5-5
TERTIARY TREATMENT TECHNOLOGY COST ESTIMATES
Treatment Technology .
,
k d i2a.
,41
>-��L .ID.
Ss. COT t
L„,. �-.�. �t. Y .<) ��: d"
! 'M ^:lz:°F✓�:'4 t 9'.$+ g;s; 1 , .r6wK.,-
}a. ;i2i�.i t•�; ;�S. i'S r }�:e �i. }}+a.�� f'3 'Fi f-:"
i. 9T� � ..C�j .'�'�4 � Ao :f '�
-.,,. y -i -=s;•
«.: �-..• .'41.r,•_, r�^.''� ..5`
i ^ 1`) r r,_ T.,
i,.Y` ..i.. _.tl r , r. t
_t J
_ -. . . .'i':� ' ,�
_ -y�
- .x' .-`t4. t%� ,r,`,y.
}}�� ������Y.. -cyy�, .,�
. "vr. .. .. Y.4� �
Estimated Costs
.-precipitation_ .
-:withYFerric
:'y sy; . i
�'�y�" . t s
tom. � 'V 1
�!f .%f�yy� FF
L � 4i •�' _ � F� 'i
'!, i-.i e }r
>��. .!'. ' 1
.S. �:��.+ .�l�o�d�Y '}'�...r.t+
..�" .,
t...r 'pt '• .i
y^c.'tis� i. . `,:-
.A _ :.:tiF. 2 ...��. t
��- t;:.:.
. A
..', S'' rz cx••'
.T ,`?� w .�!
•� i.
Sodium Based
Alkaliu�{L"�{.J—
t�eee v ^F, D• S
, �'F, �y�
ts,: Af..
Jo.": .T� f'
fq ki�� SAY
� • ♦.. t Y
{ �.�' }} `°5q>v!.xP
Y. �`.S. a ln� y�Yi.7! -
P° �Add�tio Y.
ter•.,. � rr �
' •'3�rot"' R. .V
_'r,. .s � #', i{.
.s- Ar'.;: i :
�3' N� '¢d
t .!4: .
f , .'' r;,,e,. V:
Cs• E '� -.
s`'�.e� 1..�•.i�'t.
Single Sludge
�4Biolo " 'ca•l.
.s r 1 C'*..
rt� •�"
��' .t.•,..: j . �r � . I
.e7': }� U
Vr 1}v.lt wy v ����/� "f< 4
� 'J♦Li�� 'n1,. �.
z1. �.� �' _�1
.0 . i..+;
;e.
'+•5 :� {
'�.'-:r. }jam
; t
... Y x 3 trt•
.. ..�inga �:'�.
Tertiary
Denitrification
..�.Y .t f•�. i
} } ,�..` r-
r'. ,:,t _T•
•i:if.9'
r;
� t':•i"
-•�
x � � f ,
, y+,
F•
9�. r.
�..m;: Y �i. .._crtt '4Y, s{
Total Project Cost
$1,658,000
$772,580
$1,252,400
$1,883,600
Annual Operating Cost
$38,900
$2,702,000
$156,800
$185,100
Equivalent Annual Cost (1)
$297,300
$2,822,400
$351,900
$478,600
Achievable Effluent Levels
TN, mg/1 (2)
TN, lbs/day (3)
TP, mg/1 (2)
TP, lbs/day (3)
--
--
1.0
11.8
--
--
1.5
17.8
19.0
225
--
--
15.8
187
--
--
Cost for Nutrient Removal
Total Nitrogen, $/ lb N(4)
Total Phosphorus, $/ lb Pm
--
$172/1b
--
$1, 306/Ib
$78/lb
--
$54/1b
--
Cost for Nutrient Removal
(based on 95th percentile)
Total Nitrogen, $/ lb N(3)
Total Phosphorus, $/ lb P(3)
--
$43/1b
--
$594/lb
$7.54/lb
--
$8.75/lb
--
(1)
(2)
(3)
(4)
Based on a Capital Recovery Factor for 10 years @ 9 % interest and includes annual operating cost.
95th percentile concentrations from pilot treatability testing.
Based on 95th percentile concentrations and an average flow of 1.42 MGD.
Based on average effluent concentrations and an average flow of 1.42 MGD.
61
FINAL
October, 1999

fart
faml 5.4 DETERMINATION OF BAT
Clariant has commissioned this study at the request of NCDENR to define a "reasonable" best
MI available technology that is economically achievable (BAT) for control of nutrient discharges
in the Clariant discharge to the Catawba River. The existing Clariant east site WWTP
r' currently includes treatment processes and meets the criteria for BAT as defmed in the US
EPA OCPSF effluent guidelines.
MN
The current baseline effluent TN level of the Clariant discharge is 37.5 mg/1 or 444.1 lbs/day.
This represents a current average TN removal of approximately 55 percent by the Clariant
WWTP as shown previously in Table 3-5. The current baseline effluent TP level of the
Pal
Clariant discharge is 2.6 mg/1 or 30.8 lbs/day. This level of TP is necessary for optimum
performance of the existing biological treatment process as required for compliance with new
PM
BOD5, TSS and NH3-N effluent limits recently proposed by the NCDENR for the Clariant
discharge. This study has defmed and evaluated four treatment technologies that could be
MI
added to the Clariant WWTP for further reduction of TN and/or TP effluent levels. Each
pin alternative would result in different respective TN or TP levels in the discharge. The
incremental costs per pound for removal of TN and TP increase as the resulting TN or TP
levels are lowered. As shown in Table 5-5, the costs for reduction of TN in the Clariant
discharge from the current average effluent TN concentration of 15.1 mg/1 to average effluent
rasa concentrations of 13.3 mg/1 and 11.6 mg/1 are $78/lb N and $54/lb N, respectively. The costs
for reduction of TP in the Clariant discharge from the current average effluent TP
PMconcentration of 1.40 mg/1 to average effluent concentrations of 1.0 mg/1 and 0.9 mg/1 are
$172/1b P and $1,306/lb P, respectively.
Pzi
In order to determine if these alternative treatment technologies represent reasonable and
PM
economically achievable BAT treatment for the Clariant discharge, a comparison has been
made of the costs summarized above relative to the cost per pound of TN and TP removed
MI
when implemented at a POTW.
am
62
FINAL
October, 1999

Oft
Using this type of information in conjunction with the Catawba River basin planning process,
the overall costs per pound to the community for reduction of the TP and TN contributions to
Lake Wylie can be optimized to produce the lowest possible nutrient levels that can be
achieved at a reasonable cost. In this way, the use of community environmental and financial
resources can be optimized.
In order to develop this economic basis for comparison, a survey was conducted of nutrient
surcharges from some of the major municipalities in the eastern and southeastern United States
which have nutrient surcharges. A summary of the nutrient surcharges is presented in Table 5-
6. The results of this survey indicate that the average POTW cost for nitrogen removal is
$0.55 per pound of nitrogen and the average POTW cost for phosphorous removal is $1.96 per
pound of phosphorus. In order to determine that the treatment technologies defined in this
evaluation represent reasonable and economically achievable BAT, the cost should be equal to
or lower than the cost for POTW. The results of this comparison, as shown in Table 5-6,
riter, indicate that the costs for reducing the TN and TP levels in the Clariant discharge are beyond
reasonable BAT. The results also indicate that the current treatment technologies of the
peg Clariant WWTP represent reasonable BAT for removal of nutrients. Based on these results,
the baseline limits of 444.1 lbs/day TN and 30.8 lbs/day TP would correspond to BAT limits
for nutrients in the Clariant discharge.
PM
pop
pie
63
FINAL
October, 1999

Ago
gam
ash
IZR
TABLE 5-6
SUMMARY OF NUTRIENT SURCHARGES FROM POTW'S
r; ^.�. ';.,Y �� � % � � ,,E,.-yam �,y„ �,t R,��wi �;� °f �2,�;? 4T Mx �: F F'� 4�»'L`. z�4,8„�
, ,' .a 3 ,r ., ' '_ :¢: ( ,
�,�'6, Y� ? :" '�. i' i� t: �'h�it•K `j-V + '� 6
3:. -1�
p _..� LSY
r +"st'.. 'c' « i :�u
'.'•.iiLi £j»�,Yd. fir'' E €S+e.Y ?s� lint
. upf � utrient=Surchar ;e
'r` r i ' L ' ...f, '� 1 } 1 Y
.' � b..,✓ ^.. ,. t:. i Y ?'+n
�"
ti '! A. ..-!. .L ! ci Y. � f ,f ,�{ i $if ` ( A
i' i�� � .� � �f..-.'.; �f7v.� �
AJ-a},•. ��rt y -t }.31,3 = T.i'3`yt
fJ
i......'`��I..^5
.!�1 T �. i }��
4 :iiiiit,�i „
,�r.��,
,
ri f 'i S•" Y?s$•
i"Y..H'ii\i`
Z �^��}-...�IxY
• �
� ' . .
Gastonia, NC ( 1 )
$23
$0.404
Norfolk, VA (Hampton Roads Sanitation District)
$20.36
$129
Raleigh, NC
$72
NA
Savannah, GA
$45
NA
Birmingham, AL
NA
$200
Baltimore, MD
$50
$200
Pensacola, FL (Escambia County Utilities)
$90
$254
Average Nutrient Surcharge from Surveyed
$55.47/ 1001b
$195.75/ 1001b
POTW's (1)
($0.55/lb)
($1.96/1b)
Cost for Clariant to Reduce Nutrients Using
Additional Treatment
Precipitation with Ferric Chloride
__
172/1b P
Sodium -Based Alkalinity Addition
--
$1,306/1b P
Single -Sludge Biological Nitrification/Denitrification
$78/lb N
__
Tertiary Denitrification
$54/lb N
(1) Gastonia surcharges were not included in the average nutrient surcharge from surveyed
POTW's.
64
FINAL
October, 1999

f=1
SECTION 6.0
SUMMARY AND CONCLUSIONS
The Clariant Mount Holly east site is an integrated organic chemicals manufacturing facility
which includes a batch organic chemical production facility that produces sulfur dyes for use in
the textile industry, a herbicide active ingredient and specialty chemicals. Wastewater
produced at the facility is treated in an on -site wastewater treatment plant (WWTP) which
utilizes a primary lime treatment process followed by a two -stage, single -sludge activated
sludge process and is thereafter discharged to the Catawba River. The Clariant WWTP has
been determined to represent BAT treatment as defined by the US EPA OCPSF Guidelines,
and the Clariant discharge routinely complies with all effluent limitations and conditions of its
current NPDES permit. The Catawba River Basin Plan, prepared by the NCDENR, indicates
that no water quality problems have been identified at monitoring stations downstream of the
Clariant discharge.
The wastewaters generated by the Clariant facility result primarily from the batch production
of sulfur dye products and are characteristically highly variable. A large portion of the
nitrogen contained in the wastewater originates from a large air emission treatment system
installed by Clariant in 1994 to remove ammonia gases from process vent streams as required
under North Carolina's air regulations. Prior to treatment, the wastewater contains relatively
high concentrations of nitrogen, most of which are in the form of ammonia (NH3-N). A
portion of the nitrogen is composed of non -biodegradable (refractory) organic nitrogen
compounds resulting from sulfur dye production. The Clariant wastewaters do not contain
Pala
sufficient levels of phosphorus for consistent biological treatment.
Clariant has implemented a significant waste reduction and minimization program at the Mount
Holly east site in recent years. Significant items included:
• reclamation and reuse programs for ammonium sulfate, sodium thiosulfate and
sulfuric acid generated as a part of dye production process;
65
FINAL
October, 1999

f1
• investment in considerable automatic controls to improve production process yields
and reduce losses of manufactured dyes and intermediate compounds to
wastewaters;
• water conservation and reduction in volumes of wastewater generated; and
• numerous pollution prevention activities throughout the facility.
These efforts have resulted in significant reduction of BOD5, organic nitrogen and ammonia
nitrogen in the wastewater. However, fluctuating market demand for the reusable waste
products still results in high periodic loading of these materials to the WWTP.
The NCDENR has recently proposed new effluent limits for BOD5, NH3-N, TSS and OCPSF
priority pollutants in the Clariant discharge, which will require significant improvement in
treatment process performance. It has been determined that addition of phosphoric acid to the
activated sludge is required for optimal performance of the biological treatment process and
,,a compliance with the new NCDENR proposed limits.
Due to eutrophication problems which have been identified in the Catawba Creek and
Crowders Creek arms of Lake Wylie, the NCDENR is proposing nutrient limits on municipal
and industrial discharges to streams which feed Lake Wylie. Clariant commissioned the study
presented herein at the request of the NCDENR to define a "reasonable" best available
technology that is economically achievable (BAT) for control of nutrient discharges in the
Clariant discharge to the Catawba River. The Clariant discharge is only a minor contributor of
nitrogen and phosphorus in Lake Wylie and does not contribute to nutrient concentrations in
the Catawba Creek and Crowders Creek arms of Lake Wylie, where eutroplication problems
have been identified.
rim
Based on the US EPA methodology for determination of average monthly effluent limits, the
Clariant discharge currently contains baseline monthly average concentrations of 37.5 mg/1
(444.1 lb/d) total nitrogen (TN) and 2.6 mg/1 (30.8 lb/d) total phosphorus (TP).
Approximately 6 % of this TN level is refractory organic nitrogen which is not bioavailable and
66
FINAL
October, 1999

F=1
should not contribute to eutrophication in the Catawba River or Lake Wylie. The Clariant
WWTP currently removes approximately 55 % percent of the TN contained in the wastewater.
The baseline TP level represents the lowest effluent phosphorus concentration that will support
''x' optimal biological treatment by the Clariant WWTP and allow compliance with new BOD5,
NH3-N and TSS limits recently proposed by the NCDENR for the Clariant discharge.
POI
Four alternative treatment technologies were defined which could be added to the Clariant
WWTP for further reduction of TN and/or TP effluent levels. Each technology would result
in different incremental reductions in TN or TP contained in the discharge. Capital costs and
annual O&M costs for each of these alternatives were developed and costs per pound of TN or
TP removed were calculated.
The costs for reduction of TN in the Clariant discharge are $78/lb N and $54/1b N to achieve
average effluent TN levels of 13.3 mg/1 and 11.6 mg/1, respectively. The costs for reduction
of TP are $172/lb P and $1,306/lb P to achieve average effluent TP levels of 1.0 mg/1 and 0.9
mg/1, respectively. For comparison, the average costs for reduction of nutrients in effluent
discharges from POTW's are $0.55/lb N and $1.96/lb P, respectively. Based on this analysis,
AEI has determined that: 1) the costs for reducing TN and TP levels in the Clariant discharge
are beyond reasonable BAT and 2) the current treatment technologies of the Clariant WWTP
represent reasonable BAT for removal of nutrients. The results of this study indicate that the
baseline limits of 444.1 lbs/day TN and 30.8 lbs/day TP would correspond to BAT limits for
nutrients in the Clariant discharge.
Owl
13024c002
67
FINAL
October, 1999

APPENDIX A
WATER QUALITY AND NUTRIENT DATA FOR
THE CATAWBA RIVER AND LAKE WYLIE

Chemical Monitoring Summary Report
CATAWBA RIVER AT S BELMONT - CROSS REF C4210000
Pa2e 1
P,F, North Carolina Division of Water Quality
r=+
gawl
Station Number: 02142938
Secondary Number: CTB 103
Third Number:
STORET Number: C4220000
Water Quality Class: B WSIV
Criterion
Tvoe
Basin: CAT
Subbasin: 030834
Reg. Office: MRO
County: MECKLENBURG
Drainage Area (sq.mi.):
Average FIow (cfs):
7Q 10 (cfs):
Summer 7Q10 (cfs):
30Q2 (cfs):
Parameter Name
NC State
M'
M
First
Last
Dissolved Oxygen (mg/I)
I FAQI15)
"
76
..
....
0
..�
,. .....,
0I 0
In
5.4
au
..a�
8.85
w
12
aaitiiJic
1/27/92
aampie
10/16/97
pH (SU)
1 FAQI 6.0-9.0
76
0
1
1.3
6
7.045
9.07
1/27/92
10/16/97
Conductivity (µMhos)
LJ
N/C
76
0
8
81
258
1/27/92
10/16/97
Chlorophyll a (Corr)(1.1.2/1)
I FAQI
40
66
23
I0l
o
1
2!
30
1/27/92
9/9/97
Fecal Coliform (#/100m1)
FHH
200
64
34
2
3.1
I 9
16
340
1/27/92 9/9/97
Total Phosphorus (mgl1)
II
N/C
66 � 2�I�
0.01
0.03
0.13
1/27/92 9/9/97
Ammonia -Nitrogen (me/1)
L_9
J
N/C
66 UUU
-
0.01
0.06
0.2
1/27/92 9/9/97
Nitrate/Nitrite-N (mg/1)
N/C
66 !211J
0.01
0.2
0.45
1/27/92 9/9/97
T Kjeldahl Nitrogen (mJ1)
N/C
66 UUU
-
0.1
0.2
0.5
1/27/92 9/9/97
Turbidity (NTU)
1 FAQ]
50
65 0
1.5
3
7.5
65
1/27/92 9/9/97
Hardness (mg/1)
WS
100
65
0
0
8
20
36
1/27/92
9/9/97
Total Residue (mg/1)
WS
500 65 0 Ol 0
25
71
140
1/27/92 9/9/97
Total Suspended Res (mg/I)
1
N/C
66 1UU
1
6(
18
1/27/92 9/9/97
Aluminum (µg/1)
J
N/C 66 UUU
50
285
1400
1/27/92 9/9/97
Arsenic (4/1)
1 FAQI
50 66 66 0
10
10
10
1/27/92 9/9/97
Cadimum (µg/1)
I FAQI 2 66 65
0I
2
2j
10 1/27/92 9/9/97
Chromium (µg/1)
I FAQI 50 66
66 u 0
25
25
25
1/27/92 9/9/97
Copper AL (1.ig/1)
FAL
I 766
15
u 7.6
U13
48
1/27/92 9/9/97
Iron AL (4/1)
FAL
1000 66
1
3
8
335
_
150011/27/92
19/9/97
Lead (µg/1)
I FAQI
25 66
66
U 0
10
10
50
1/27/92
9/9/97
Mercury (µg/1)
1 FAQ!
0.012 66
66
l oI 0
0.2
0.2
0.2
1/27/92
9/9/97
Manganese (4/1)
WS
50
66
0
12 18.2
12
32
140
1/27/92
9/9/97
Nickel (4/1)
WS
25 66
65
0
10
10
12
1/27/92
9/9/97
Zinc AL (4/1)
FAL
50 66
41
4.5
10
10
98
1/27/92
9/9/97
Summer Summary (April -October
Parameter Name
Dissolved Oxygen (mg/I)
pH (SU)
Total Phosphorus (mg/1)
Ammonia -Nitrogen (mg/1)
Nitrate/Nitrite-N (mg/1)
Conductivity (µMhos)
Chlorophyll a (Corr)(4/1)
Total Suspended Res (mg/1)
Samples
Samples < net Minimum Median Maximum
1 4811 011 5.411 7.8511 11.21
481__0,1 611 711 9.071
I 4011 011 O.O 1 !1 0.0411 0.13!
401___ 311 O.011l 0.06f1 0.19I
40 211 0.01 0.16511 0.341
I 480 on 811 9511 2581
I 4011 711 111 31 30
4o UI 211 611 181
Abbreviations: n=number of samples; Det=number of samples less than the detection limit; AL=action level; N/S=no samples
Crit=number of samples above or below the criterion; % Crit=percentage of samples above or below the criterion; N/C=no criterion
Notes: Median values are calculated using the detection level for samples classified as below detection. The Median value for Fecal
Coliform is actually the Geometric Mean value. Data include only surface samples. Samples recorded at less than detection are
considered at detection level for this summary. Criterion Type Codes: FAQ --Freshwater Aquatic Life; SAQ--Saltwater Aquatic Life;
FHH--Freshwater Human Health; SHH--Saltwater Human Health; FAL-Freshwater Action Level; SAL --Saltwater Action Level;
SA --Saltwater SA Criterion; TR--Trout Water Criterion; WS--Water Supply Criterion; WSII--Water Supply II Criterion; WSIII--Water
Supply III Criterion
7
�t
R e ick RsSRss ryu//1+
Cu).* • Icl?g. Lfckoa.. I0011
C6t)ia.L> bay. vcA.
1

-ATAWBA RIVER AT S BELMONT - CROSS REF C4210000
oummer Summary (June -September)
'arameter Name
gLi.ssolved Oxygen (mg/1)
pry (SU)
Ental Phosphorus (mg/1)
4nmoniaNitrogen (mg/1)
Nitrate/Nitrite-N (mg/1)
nductivity (j.tMhos)
_'lorophyll a (Corr)(µg/1)
Total Suspended Res (mg/1)
aearly Summaries
._issolved Oxygen (mg/1)
Samples
Trar Samples < Det Minimum Median
:' ,)92 II 1411 Oil 6.211 9.151
ma 11993 11 1111 011 5.411 8.91
111494 11 1111 Oil 6.211 8.31 11.5
095 11 1211 011 6.211 8.351 10.4
6' iJ996 11 1311 Oil 6.511 9.41 11.6
.% f)97 II 1511 01l 6.811 8.61 10
Conductivity (µMhosi
j2+92 11 1411 011 6111 70.511 1811
i L 993 II 1111 011 5411 1001 172
m 0994 II 1111 011 811 811 131
49s II 1211 011 5811 71.51 258
11996 1I 1311 011 6011 841 118
L'"? 97 11 1511 011 6511 821 144
7ta1 Suspended Res (mg/1)
' ' I1:;,1-)93
1992 iI 1211 0(1 111 61 17
11 1111 011 111 61 18
[1994 0 1111 011 311 61 11
e' t+-1) 9 5 11 1211 011 111 6.511 111
i -)96 11 1111 011 30 611 141
, 11997 11 911 Olt 211 611 111
Page 2
Samples
Samples < net
29 of
291-1
I 2411 01
I 2411 21
I 2411 21
I 2911 01
I 2411 31
I 2411 of
Maximum
12
10.3
Minimum
5.41
6.21
0.011
0.011
0.011
8(
11
21
Median
7.21
6.91
0.041
0.051
0.141
981
41
61
pH (SU)
Samples
Year Samples < Det Minimum
11992 11 1411 011 61
11993 II ii11 011 6.511
11994 II 1111 011 6.81
11995 11 1211 o1I 6.71
(1996 II 1311 011 6.71
11997 11 1511 011 6.71 71
Total Phosphorus (mg/1)
Maximum
10.4
8.9
0.12
0.17
0.31
181
30
18
Median Maximum
7.1511 8.91
7.21f 8.51
7.1111 8.191
7.0051 7.84
7.11 9.07
7.5
11992 II 1211 Oil 0.0111 0.021 0.13
11993 II 1111 011 0.0211 0.051 0.11
11994 11 1111 0 (1 0.0111 0.031 0.09
11995 II 1211 OH 0.0111 0.0351 0.08
(1996 11 1111 Oil 0.011 0.031 0.06
1997 91 0 0.01 ( 0.031 0.12
Ammonia -Nitrogen (mg/1)
11992 II 1211 011 0.0111 0.0511 0.21
11993 II 1111 011 0.0111 0.0911 0.191
11994 II 1111 0(I 0.0111 0.0611 0.171
11995 II 120 0(1 0.0211 0.0611 0.21
11996 II 1111 Oil 0.0111 0.0711 0.111
11997 11 911 0(1 0.010 0.0311 0.111
121.-C : -60.alriwi d2 Yk2,n+- I'?icor-}- . Ca-g-aA).)106, ve-,r
Cw.%. i9Q8 coy e627
ram
212

Long Creek
Gastonia 8.0 MGD
TP - 408 Ibs/d (6.1 mg/I)
TN - 1069 Ibs/d (16.0 mg/I)
JPS 4.0 MGD
TP - 90 Ibs/d (2.7 mg/I)
tS TN - 293 Ibs/d (8.8 mg/I)
Co
Gs
A �A
O�� �y
9
•0d�C 00 6sa
6
a16s°" 40%
d
Gastonia 9.0 MGD
TP - 282 Ibs/d (3.8 mg/I)
TN - 955 Ibs/d (12.7 mg/I)
Catawba Creek
Crowders Creek
Catawba
River
Mt. Holly
ak 4.0 MGD
IF TP - 110 Ibs/d
(3.3 mg/1)
TN - 304 Ibs/d
(9.1 mg/I)
Belmont
TP-801 Ibs/d 5.0 MGD
TN-7346 Ibs/d TP - 345 Ibs/d
(8.3 mg/I)
60% TN - 624 Ibs/d
(15 mg/I)
LAKE WYLIE
j Nutrient loadings Qbs'/day)
ITP_ 301, TN 991_ F
I Preis Avg: Ch 74 tig/l 4y�_ 12%
Bessemer City 1.5 MGD
TP - 30 Ibs/d (2.4 mg/I)
TN - 328 Ibs/d (26 mg/I)
I Nutrient loadings Qbs/day)
I TP 150,' TN 895
I Pred Avg Gill a 43 ug/I '.
12%
Gastonia 6.0 MGD
TP - 100 Ibs/d (2.0 mg/1)
TN - 423 Ibs/d (8.4 mg/I)
Legend/Explanation of terms
r
Nutrient Loadings:
TP - 1 195 Ibs/d
TN - 9726 Ibs/d
Predicted average
ChI-a: 18.2 ug/I
To Lake Wylie Dam
Major NPDES Discharger locations with facility name and avg. 93-94 daily nutrient loads for total nitrogen
(TN) and phosphorus (TP).
r 7 Nutrient sensitive lake areas where the state standard of 40 ug/I for chlorophyll -a is predicted to occur
L _I at some time during the growing season. Standard violations were observed twice in a 1989-90 study.
77-4 Areas where predicted average Chl-a concentrations exceed the state standard of 40 ug/I and where chronic
algal bloom conditions have been observed.
Note: Daily nutrient loadings in the 4 lake arms are based on 89-90 measured background levels plus
actual average 93-94 loadings from dischargers. Nutrient loading in the main lake is based on percentages
of the lake arm loadings that are thought to reach the lake based on a field -calibrated in -lake nutrient
transport model.
Figure 3.4 Schematic Diagram of Lake Wylie Showing Nutrient Loadings and Predicted
Chlorophyll -a Concentrations in the 4 Major Arms and the Mainstem of the Lake
RI u e r s i n tvi dam. \ 4-e.-r c kc1 Mo ivt l -

EVALUATION OF NUTRIENT CONTRIBUTION FROM CLARIANT TO LAKE WYLIE
Data for Nutrient concentrations taken from the
Catawba River Basinwide Water Quality Management Plan (1995)
Source
TP (Ib/d)
TN (lb/d)
% Transported to Lake
Wylie (1)
Estimated Mass TP
Transported to Lake
Wylie (lb/d)('"
Estimated Mass TN
Transported to Lake
Wylie (Ib/d)(2)
Catawba River
801
7346
60%
481
4408
South Fork
993
4760
40%
397
1904
Catawba Creek
301
991
12%
36
_
119
Crowders Creek
150
895
12%
18
107
Total
2245
13992
932
6538
(1) Percent transported obtained from Catawba Plan, 1995.
(2) These values were calculated from the % transported values.
Clariant Discharge
Flow
(MGD) (1)
TP Discharge from
Clariant
TN Discharge from
Clariant
Clariant Transported to
Lake Wylie (2)
% Nutrients in Catawba
River from Clariant
% Nutrients in Lake
Wylie from Clariant
(mg/L)
(lb/d)
(mg/L)
(lb/d)
TP (lb/d)
TN (lb/d)
TP
TN
TP
TN
Case 1 (example)
1.42
3.0
35.5
50
592
21.3
355.3
4.4%
8.1%
2.3%
5.4%
Case 2 (example)
1.42
2.0
23.7
25
296
14.2
177.6
3.0%
4.0%
1.5%
2.7%
Case 3 (ay. disch) (3)
1.42
1.4
16.6
16
184
9.9
110.1
2.1 %
2.5%
1.1%
1.7%
Case 4 (proposed)(4)
1.42
1.0
11.8
6.0
71
7.1
42.6
1.5%
1.0%
0.8%
0.7%
(1) Long Term Average: Based on NCDENR 5-year long term average of 1.42 from 1991-1995.
(2) Assumed 60% transport of nutrients in the Catawba River to Lake Wylie based on information in Catawba Plan, 1995.
(3) Average TP based on full-scale effluent data from 5/5/99 - 9/30/99 and average TN based on full-scale effluent data from 4/1/99-9/30/99.
(4) Limits being proposed by NCDENR, TP = 1 mg/L and TN = 6 mg/L.
13024s002
Lake Wylie 1
10/27/99

APPENDIX B
SUMMARY OF FULL-SCALE MONITORING DATA

FPI
rs►
11
Mgt
asa
13024s006
Data
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Influent
Date
BOD5
Flow
- TP
NH3-N (2)
TKN (3)
NO3/NO2-N
Org-N
TN (1)
TNN
Raw
Added
Total
mg/L
mg/L
mg/L
mglL
mglL
mg/L
mg/L
mg/L
10/1/98
1.585
10/2/98
180
1.4868
8.6
10/3/98
1.528
10/4/98
1.5314
10/5/98
911
1.3702
44.92
10/6/98
1.2681
10/7/98
611
1.6482
15.34
10/8/98
1.4505
10/9/98
410
1.1434
23.01
10/10/98
1.3077
10/11/98
1.1602
10/12/98
431
1.3422
40.36
10/13/98
1.3788
10/14/98
501
1.4424
17.7
10/15/98
1.2871
10/16/98
541
1.3655
21.91
10/17/98
1.0479
10/18/98
1.082
10/19/98
676
1.0311
46.39 •
10/20/98
1.0578
10/21/98
645
1.2583
59.5
10/22/98
1.1487
10/23/98
300
1.1595
39.27
10/24/98
1.254
10/25/98
1.409
10/26/98
245
1.1286
38.84
10/27/98
1.3205
10/28/98
370
1.3334
29.91
10/29/98
1.3286
10/30/98
491
1.3736
55.22
10/31/98
1.0633
11/1/98
1.1218
11/2/98
190
1.6768
44.62
11/3/98
1.3145
11/4/98
240
1.2225
20.1
11/5/98
1.099
11/6/98
365
1.2699
14.93
11/7/98
1.263
11/8/98
1.193
11/9/98
481
1.378
16.85
11/10/98
1.3962
11/11/98
516
1.4633
21.17
11/12/98
1.3427
11/13/98
481
1.349
21.93
11/14/98
1.6387
11/15/98
1.3708
11/16/98
511
2.0353
19.75
11/17/98
1.6767
11/18/98
866
1.4551
16.61
11/19/98
1.1654
11/20/98
130
1.0661
14.78
11/21/98
0.8895
11/22/98
0.9251
11/23/98
491
1.0883
23
11/24/98
1.0232
11/25/98
0.9095
11/26/98
0.6321
11/27/98
0.9948
11/28/98
1.2588
11/29/98
1.1916
11/30/98
20
1.7215
9.61
12/1/98
1.9653
12/2/98
150
1.7083
10
12/3/98
1.1706
0.8
14.04
14.84
12/4/98
320
1.299
10.67
12/5/98
1.4305
10/27/99
1 of 12

cows
+�I
13024s006
Data
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Influent
Date
BOD5
Flow
- TP
NH3-N (2)
TKN (3)
NO31NO2-N
Org-N
TN (1)
TNN
Raw
Added
Total
mg/L
mg/L
mgfL
mglL
mglL
mg/L
mg/L
mg/L
12/6/98
1.0022
12/7/98
275
0.9879
0.3
16.63
16.93
27.7
12/8/98
1.0411
12/9/98
1.2827
18.36
12/10/98
425
1.1995
0.1
13.70
13.8
12/11/98
496
1.0634
18.83
12/12/98
1.4146
12/13/98
1.6873
12/14/98
160
1.299
0.15
12.65
12.8
3
12/15/98
1.97
12/16/98
686
1.3531
24.65
12/17/98
1.3494
1.1
12.18
13.28
12/18/98
180
1.4036
17.97
12/19/98
1.0145
12/20/98
2.3617
12/21/98
506
1.3603
0.8
12.08
12.88
41.21
12/22/98
1.3739
12/23/98
540
1.5495
39.12
12/24/98
2.1728
12/25/98
1.3901
12/26/98
1.2258
12/27/98
1.2412
12/28/98
1.3465
1.1
12.20
13.3
12/29/98
1.2104
12/30/98
1.164
12/31/98
1.0511
0.44
15.63
16.07
1/1/99
0.9504
1/2/99
1.8640
1/3/99
1.0599
1/4/99
90
1.1448
0.5
14.35
14.85
3.02
1/5/99
1.5738
1/6/99
90
1.2878
11.29
1/7/99
1.7240
0.4
9.53
9.932
1/8/99
315
1.7285
11.82
1/9/99
2.0145
1/10/99
1.8795
1 / 11 /99
150
1.5137
0.5
10.86
11.36
14.07
1/12/99
1.5888
1/13/99
661
1.4697
38.02
1/14/99
1.5289
0.2
7.53
7.729
1/15/99
686
1.4377
17.59
1 1/16/99
1.4240
1/17/99
1.7510
1/18/99
120
1.5490
0.8
7.43
8.231
17.54
1/19/99
1.4483
1/20/99
511
1.5874
17.62
1/21/99
1.4655
2
7.85
9.854
1/22/99
1.2432
33.46
1/23/99
2.0238
1/24/99
1.4626
1/25/99
295
1.1777
1.02
9.77
10.79
55.84
1/26/99
1.0127
1/27/99
1051
1.4427
20.99
1/28/99
1.2460
2
9.24
11.24
1/29/99
626
1.2797
43.99
1/30/99
1.2025
1/31/99
1.2334
2/1/99
531
2.2453
0.46
5.13
5.587
19.73
2/2/99
1.3276
2/3/99
486
1.2486
22.47
2/4/99
1.3132
2
8.77
10.77
2/5/99
661
1.187
25.05
2/6/99
1.1186
2/7/99
1.0548
2/8/99
420
1.3929
2.5
8.26
10.76
32.69
2/9/99
1.3361
10/27/99
2 of 12

t=1
fst
Est
tit
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Influent
Date
BOD5
Flow
- TP
NH3-N (2)
TKN (3)
NO3/NO2-N
Org-N
TN (1)
TNN
Raw
Added
Total
mg/L
mg/L
mg/L
mglL
mglL
mg/L
mg/L
mg/L
2/10/99
200
1.7612
23.77
2/11/99
1.2606
2.5
9.13
11.63
2/12/99
190
1.1768
26.75
2/13/99
1.3265
2/14/99
1.302
2/15/99
1.2426
2.5
9.26
11.76
26.25
2/16/99
1.3504
2/17/99
1.6725
18.45
2/18/99
310
1.553
1.85
7.41
9.262
2/19/99
2.1454
2/20/99
1.6115
2/21/99
1.4138
2/22/99
1.3934
2
8.26
10.26
45.5
2/23/99
1.5094
2/24/99
1.41
29.89
2/25/99
1.2434
3.5
9.26
12.76
2/26/99
1.2591
34.14
2/27/99
1.3252
2/28/99
1.3038
3/ 1 /99
1.171
1.3
9.83
11.13
36.86
3/2/99
1.4234
3/3/99
1.2692
13.89
3/4/99
781
1.3505
5.8
6.45
12.25
3/5/99
1.1547
46.29
3/6/99
1.4463
3/7/99
1.4173
3/8/99
1.3304
1.55
6.55
8.096
13.42
3/9/99
1.8937
3/10/99
1.4501
42.6
3/11/99
410
2.0024
1.25
4.35
5.599
31.7
0.09
31.79
3/12/99
1.6438
44.46
3/13/99
1.6821
3/14/99
1.5766
3/15/99
1.4272
2.45
6.10
8.552
22.23
0.01
22.24
3/16/99
1.7016
3/17/99
1.8462
54.45
3/18/99
1682
2.2208
3.4
3.92
7.321
20.2
0.09
20.29
3/19/99
1.294
21.31
3/20/99
0.7255
3/21/99
0.693
---
3/22/99
1.0396
1.3
8.38
9.677
.6
37
1.00
14.40
38.00
23.60
3/23/99
1.3695
3/24/99
1.6497
34.73
3/25/99
170
1.681
0.64
5.18
5.821
25.7
0.18
25.88
3/26/99
1.5083
17.22
3/27/99
1.4168
3/28/99
1.589
3/29/99
1.4026
0.92
6.21
7.129
38.49
22.2
0.06
\�
38.55
38.55,
3/30/99
1.4463
-_ _
3/31/99
1.403
45.41
4/1/99
380
1.1389
0.7
7.65
8.347
0.12
4/2/99
1.5905
4/3/99
1.1569
4/4/99
0.5411
--�
4/5/99
1.2418
1.03
7.01
8.043
33.7
45.8
1.30
12.10
47.10
35.00
4/6/99
1.243
4/7/99
1.3679
27.82
4/8/99
626
1.0607
1.04
8.21
9.25
0.11
4/9/99
1.3657
69.79
4/10/99
1.7097
4/11/99
1.9718
4/12/99
1.2853
0.6
6.78
7.376
36.15
4/13/99
1.4357
4/14/99
1.0696
28.08
4/15/99
430
1.2379
4.45
7.04
11.49
70.5
4/16/99
0.7618
138.1
13024s006
Data
10/27/99
3 of 12

01114
+C1
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Influent
Date
BOD5
Flow
TP
NH3-N (2)
TKN (3)
NO3/NO2-N
Org-N
TN (1)
TNN
Raw
Added
Total
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
4/17/99
0.8396
4/18/99
0.7519
4/19/99
0.9934
1.5
8.77
10.27
37.76
0.65
• . 38:41°. `
38.41
4/20/99
1.3885
4/21/99
1.5267
42.27
4/22/99
1.026
1.44
5.54
6.976
48.6
0.51
49.11
4/23/99
1.615
44.34
4/24/99
1.3102
4/25/99
1.0245
4/26/99
1.669
1.25
3.40
4.653
49.84
60.6
10.76
4/27/99
1.4845
4/28/99
2.1224
100.54
4/29/99
365
2.347
35.9
4/30/99
1.8268
62.34
5/1/99
1.2344
5/2/99
1.3307
5/3/99
1.5138
49.96
5/4/99
1.9231
5/5/99
1.4706
72.13
5/6/99
1381
1.6699
1.13
3.40
4.531
52.7
0.08
52.78
5/7/99
1.7048
67.52
5/8/99
1.2853
5/9/99
1.2911
5/10/99
1.5073
0.9
3.77
4.668
52.35
72.3
0.04
19.95
72.34
52.39
5/11/99
1.5328
5/12/99
0.8435
56.43
5/13/99
386
1.3184
0.28
4.31
4.588
34.8
0.29
35.09
5/14/99
1.0388
88.68
5/15/99
0.919
1.34
5/16/99
1.0897
5/17/99
1.4067
0.56
4.04
4.598
41.39
38.2
0.32
t•. 41.71:. y ; =
41.71
5/18/99
5/19/99
2.1852
1.9078
1.34
2.98
4.317
39.17
47.8
0.22
8.63
48.02
39.39
5/20/99
420
1.4319
5/21/99
1.769
32.07
5/22/99
0.9673
5/23/99
2.0073
5/24/99
1.6734
1.25
3.39
4.644
13.78/13.26
27.7
0.07
14.44
27.77 .
13.33
5/25/99
1.2472
5/26/99
1.4363
2.6
3.95
6.554
24.03/24.3
46.4
0.03
22.10
46.43
24.33
5/27/99
841
1.4078
5/28/99
1.0521
38.99
5/29/99
0.9863
5/30/99
0.8211
5/31/99
1.5603
1.25
3.64
4.89
9.87
0.01
9.88
6/1/99
1.3932
28.38
6/2/99
1.4323
2
3.97
5.965
23.65/18.25
34.2
0.04
15.95
34.24
18.29
6/3/99
931
1.7649
17.15
6/4/99
1.3915
24.09
6/5/99
1.3055
6/6/99
1.3521
6/7/99
1.4701
0.75
3.86
4.613
24.06/28.25
39.3
0.10
13.05
39.40
26.35
6/8/99
1.504
6/9/99
1.4102
16.08
6/10/99
561
1.4234
6/11/99
0.9395
2.15
6.05
8.195
18.18/18.5
27.4
0.10
8.90
27.50
18.60
6/12/99
0.7671
6/13/99
0.9846
6/14/99
1.9196
0.44
2.96
3.399
14.75/11.8
18.5
0.10
6.70
18.60
11.90
6/15/99
1.6185
6/16/99
2.1984
21.37
6/17/99
405
1.4966
6/18/99
1.2063
1.95
4.71
6.658
13.92/14.2
24.4
10.20
6/19/99
1.248
6/20/99
1.0906
6/21/99
1.2997
1.38
4.37
5.75
7.63/8.72
24.3
0.10
17.58
24.40
6.82
13024s006
Data
4 of 12
10/27/99

e=l
+�1
CLARIANT CORPORATION - BAT STUDY
FULL SCALE VWVTP DATA
AEI JOB NO. N130-248
Influent
Date
BOD5
mglL
Flow
- TP
NH3-N (2)
mg/L
TKN (3)
mglL
NO3/NO2-N
mglL
Org-N
mglL
TN (1)
mg/L
TNN
mglL
Raw
Added
Total
mglL
6/22/99
1.303
6/23/99
0.9978
2.6
5.69
8.292
19.16/17.8
44.8
0.31
27.00
45.11
18.11
6/24/99
541
1.2415
6/25/99
1.2593
4.76
6/26/99
0.5563
6/27/99
0.6778
6/28/99
0.8253
3
6.88
9.882
19.66/36
38.9
<.01
2.90
38.91
36.01
6/29/99
0.8456
6/30/99
1.0409
1.3
5.46
6.756
9.19/3.1
8.16
<.01
5.06
8.17
3.11
7/1/99
124
1.2957
7/2/99
0.8151
15.84
7/3/99
1.2762
7/4/99
1.2913
7/5/99
0.9554
7/6/99
1.4833
1.09
3.83
4.919
18.4
36.4
<.01
18.00
36.41
18.41
7/7/99
1.5477
7/8/99
1.4492
7/9/99
1.2975
3.4
4.38
7.777
4.7
16
0.12
11.30
16.12
4.82
7/10/99
1.3077
7/11/99
1.4362
7/12/99
2.0227
1.94
2.81
4.748
14.87/13.7
30.9
0.25
17.20
31.15
13.95
7/13/99
1.5638
7/14/99
1.6563
3.07
3.43
6.499
8.07/7.2
30.2
<.01
23.00
30.21
7.21
7/15/99
140
1.6298
7/16/99
1.5913
6.21
7/17/99
1.7007
7/18/99
1.9330
7/19/99
1.8478
0.765
3.07
3.84
7.39/3.9
13.2
0.16
9.30
13.36
4.06
7/20/99
1.8317
7/21/99
1.8727
1.6
3.03
4.633
14.57/11.7
54.1
0.04
42.40
54.14
11.74
7/22/99
420
1.6828
7/23/99
1.5425
25.10
7/24/99
1.7262
7/25/99
•
1.7234
7/26/99
2.2520
1.36
2.52
3.882
9.65
18.2
0.01
8.55
18.21
9.66
7/27/99
1.3942
7/28/99
1.4198
0.64
4.00
4.64
10.24
43.9
0.20
33.66
44.10
10.44
7/29/99
1381
1.4596
•
7/30/99
1.4564
18.51
7/31/99
1.5478
8/1/99
1.5045
8/2/99
1.3762
0.63
4.13
4.757
22.47
51.6
<.01
29.13
51.61
22.48
8/3/99
1.6856
8/4/99
1.2935
0.92
4.39
5.311
15.16
36
0.01
20.84
36.01
15.17
8/5/99
1141
1.266
8/6/99
1.4716
15.19
8/7/99
1.4202
8/8/99
1.4241
8/9/99
1.3411
1
4.24
5.235
15.37
40.7
<.01
25.33
40.71
15.38
8/10/99
1.6135
8/11/99
1.6536
0.4
3.43
3.835
13.81
25.2
0.03
11.39
25.23
13.84
8/12/99
576
1.5908
8/13/99
2.0402
18.03
8/14/99
1.9381
8/15/99
1.3628
8/16/99
1.599
0.9
3.55
4.452
20.93
35.3
0.08
14.37
35.38
21.01
8/17/99
1.6011
8/18/99
1.4512
0.9
3.91
4.814
26.75
40.8
0.02
14.05
40.82
26.77
8/19/99
346
1.1258
8/20/99
1.4333
26.16
8/21/99
1.0916
8/22/99
1.0898
8/23/99
1.4896
0.71
3.81
4.523
35.15
49.5
<0.02
14.35
49.52
35.17
8/24/99
1.5256
8/25/99
1.3499
0.75
4.21
4.957
37.82
37.4
0.03
, 3785
,:
37.85
8/26/99
1201
1.3915
13024s006
Data
5 of 12
10/27/99

f�1
AIM
ral
I
+�1
13114
NMI
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-248
Influent
Date
BODE
Flow
• TP
NH3-N (2)
TKN (3)
NO3/NO2-N
Org-N
TN (1)
TNN
Raw
Added
Total
mg/L
mglL
mglL
mglL
mglL
mglL
mglL
mg/L
8/27/99
1.3573
16.41
8/28/99
1.6959
8/29/99
1.0433
8/30/99
1.2264
0.93
4.63
5.561
10.67
34.6
1.80
23.93
36.40
12.47
8/31/99
1.155
9/1/99
1.1926
0.5
4.76
5.262
11.82
6.95
0.34
1216.
12.16
9/2/99
270
1.3968
9/3/99
0.8902
31.19
9/4/99
0.765
9/5/99
1.2961
9/6/99
1.2401
9/7/99
1.6106
0.97
3.53
4.496
7.85
0.10
7.85
7.95
9/8/99
1.779
0.86
3.19
4.053
9.87
9.87
0.84
0.00
10.71
10.71
9/9/99
691
1.9502
9/10/99
1.6792
15.22
9/11/99
1.3508
9/12/99
1.248
9/13/99
1.3934
1.35
4.08
5.426
15.34
30.9
0.10
15.56
31.00
15.44
9/14/99
1.5602
9/15/99
1.43
4.37
3.97
8.342
14.28
29.3
0.06
15.02
29.36
14.34
9/16/99
1712
1.6242
9/17/99
1.3419
11.04
9/18/99
1.2263
9/19/99
0.9607
9/20/99
1.3248
1.1
4.29
5.387
8.87
13.1
<.01
4.23
13.11
8.88
9/21/99
1.769
9/22/99
1.4684
0.115
3.87
3.983
15.96
9/23/99
1231
1.2509
9/24/99
1.1151
31
9/25/99
1.0974
9/26/99
1.165
9/27/99
1.7628
13.75
9/28/99
1.7436
9/29/99
1.835
9/30/99
746
1.572
24.54
13024s006
Data
6of12
10/27/99

raq
rAI
014
ran
Fun
r�
pia
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Mixed Liq
Effluent
Date
TP
mg/L
MLSS
(4)
mg/L
P/TSS
Temp
C
. TP
mg/L
Ortho•P
mg/L
NH3
-N(2)
mg/L
TKN (3)
mg/L
NO3/
NO2-N
mg/L
Org-N
mg/L
TN (1)
mg/L
TNN
mg/L
TSS
mg/L
CBOD5
mg/L
BOD5
mg/L
H3PO4
gpd
10/1/98
10/2/98
10/3/98
10/4/98
10/5/98
10/6/98
10/7/98
10/8/98
10/9/98
10/10/98
10/11/98
10/12/98
10/13/98
10/14/98
10/15/98
10/16/98
10/17/98
10/18/98
10/19/98
10/20/98
10/21/98
10/22/98
10/23/98
10/24/98
10/25/98
10/26/98
10/27/98
10/28/98
10/29/98
10/30/98
10/31/98
11/1/98
11/2/98
11/3/98
11/4/98
11/5/98
11/6/98
11/7/98
11/8/98
11/9/98
11/10/98
11/11/98
11/12/98
11/13/98
11/14/98
11/15/98
11/16/98
11/17/98
11/18/98
11/19/98
11/20/98
11/21/98
11/22/98
11/23/98
11/24/98
11/25/98
11/26/98
11/27/98
11/28/98
11/29/98
11/30/98
12/1/98
12/2/98
12/3/98
12/4/98
12/5/98
1210
1970
1940
2900
2330
1680
3190
2970
6110
3420
5370
2950
2990
4550
2560
2380
2800
3510
1800
2080
2950
2870
2490
2140
1710
1440
1790
1150
4480
1540
1330
2020
1550
1530
1840
1630
950
2170
1700
830
1760
3610
4030
1340
1810
1620
1570
2380
1970
2470
2620
300
7410
2430
2436
1290
1120
2330
1520
1800
1870
1620
2150
24
21
22
24
24
23
24
23
22
21
21
21
21
20
19
20
18
19
21
20
18
18
16
17
16
18
18
19
19
20
20
19
20
17
17
16
15
14
15
16
20
18
15
16
17
17
19
19
17
18
19
15
13
16
17
15
15
14
13
13
16
15
15
16
16
19
0.04
0.10
0.13
0.14
15.2
12.4
8.78
9.97
13.44
16.83
12.91
7.67
16.43
16.51
15.48
14.39
12.27 •
14.23
15
21.62
19.94
27.61
22.21
24.67
21.79
19.41
12.23
18.03
10.33
12.15
10.35
8.87
3.1
1.48
2.96
6.71
5.86
9.13
9.79
8.37
5.99
6.7
7.3
9.8
7.14
7.92
6.61
5.35
4.84
11
10
13.2
11.2
8
1
8
7
14
12
9
10
15
18
18
18
19
15
74
12
11
19
13
14
21
16
17
29
17
16
18
15
13
23
19
14
7
19
12
11
22
3
10
33
18
24
14
25
25
•
32
19
24
28
26
43
36
36
42
53
56
42
41
37
44
53
36
40
27
50
38
34
15
19
43
70
44
36
38
48
71
55
29
25
37
33
34
53
25
29
19
26
18
36
24
43.4
43.4
43.4
13024s006
Data
7 of 12
10/27/99

CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Mixed Liq
Effluent
Date
TP
MLSS
P/TSS
Temp
TP
Ortho-P
NH3
TKN (3)
NO3/
Org-N
TN (1)
TNN
TSS
CBOD5
BODS
H3PO4
(4)
-N(2)
NO2-N
mg/L
mg/L
C
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
gpd
18/6/98
2750
19
43.4
12/7/98
2240
20
2.8
2.40
2.81
23
25
43.4
12/8/98
2770
21
2.96
14
21
43.4
12/9/98
2590
18
2.37
28
18
43.4
12/10/98
2650
15
1.9
2.00
5.47
25
7
43.4
12/11/98
3290
15
6.23
20
8
43.4
12/12/98
3210
14
43.4
12/13/98
3560
15
43.4
12/14/98
3080
13
3.8
3.60
7.06
32
4
43.4
12/15/98
3410
14
6.95
32
4
43.4
12/16/98
3400
14
6.09
15
8
43.4
12/17/98
3820
13
1.3
1.10
5.37
24
2
43.4
12/18/98
4060
13
7.21
8
10
43.4
12/19/98
4130
14
43.4
12/20/98
3730
16
43.4
12/21/98
3000
12
0.55
0.43
5.97
21
8
43.4
12/22/98
3510
16
4.4
32
37
43.4
12/23/98
5290
12
2.73
21
29
43.4
12/24/98
10
3.1
16
48
43.4
12/25/98
10
43.4
12/26/98
8
43.4
12/27/98
8
43.4
12/28/98
2830
10
3.3
3.30
5.8
4
12
43.4
12/29/98
10
5.6
5
7
43.4
12/30/98
1880
9
5.3
7
6
43.4
12/31/98
8
5.9
5.60
4.2
7
6
43.4
1 /1 /99
8
43.4
1/2/99
8
43.4
1/3/99
7
43.4
1/4/99
3850
5
2.4
2.20
2.81
3
2
43.4
1/5/99
2730
5
1.48
2
4
43.4
1/6/99
3340
6
1.48
4.8
1.56
10
5
43.4
1 /7/99
3580
9
2.1
2.15
1.51
10
7
43.4
1/8/99
3570
11
1.6
8
3
43.4
1/9/99
2800
13
43.4
1/10/99
3370
11
43.4
1/11/99
3880
11
6.5
5.40
9.93
10
11
43.4
1/12/99
3880
12
9.61
23
•
17
30.4
1/13/99
3640
14
6.53
25
15
30.4
1/14/99
45
3920
0.011
17
3.1
2.50
11.26
31
26
30.4
1/15/99
4200
14
7.27
20
10
30.4
1/16/99
2240
13
30.4
1/17/99
2550
14
30.4
1/18/99
4020
15
1.2
0.95
10.72
12
21
30.4
1/19/99
3450
14
9.6
25
26
30.4
1/20/99
4430
13
9.18
13
32
30.4
1/21/99
4710
15
2.2
0.83
12.68
29
25
30.4
1/22/99
4180
17
16.38
20
30.4
1/23/99
4140
18
30.4
1/24/99
5190
17
30.4
1/25/99
4680
15
2.2
2.00
17.25
7
15
30.4
1/26/99
3620
14
9.16
9
7
30.4
1/27/99
4320
15
14.48
14
23
30.4
1/28/99
4780
16
2.1
1.60
15.07
16
26
30.4
1/29/99
4700
16
13.45
8
11
30.4
1/30/99
4710
15
30.4
1 /31 /99
4920
14
30.4
2/1/99
4680
13
1.4
1.10
13.74
6
6
30.4
2/2/99
4950
13
12.4
12
8
30.4
2/3/99
4860
14
12.67
10
12
30.4
2/4/99
5260
15
3
2.60
8.9
19
24
30.4
2/5/99
5050
14
6.08
13
18
30.4
2/6/99
2950
16
30.4
2/7/99
6340
17
30.4
2/8/99
4160
15
3.2
2.90
12.02
11
10
30.4
2/9/99
5150
16
10.38
8
19
30.4
13024s006
Data
8 of 12
10/27/99

fam1
raM
r1a
sal
rat
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Mixed Liq
Effluent
Date
TP
MLSS
P/TSS
Temp
TP
Ortho-P
NH3
TKN (3)
NO3/
Org-N
TN (1)
TNN
TSS
CBOD5
BOD5
H3PO4
(4)
-N(2)
•
NO2-N
mg/L
mg/L
C
mglL
mg/L
mg/L
mglL
mglL.
mg/L
mglL
mglL
mg/L
mg/L
mg/L
gpd
20f0/99
4900
16
14.56
_
7
15
30.4
2/11/99
5320
16
3.2
2.30
15.27
11
13
30.4
2/12/99
8740
16
9.06
10
12
30.4
2/13/99
5550
12
30.4
2/14/99
5680
11
30.4
2/15/99
130
4260
0.031
12
4.75
3.10
12.32
14
6
30.4
2/16/99
5380
13
14.81
10
23
30.4
2/17/99
4830
15
10.78
9
30
30.4
2/18/99
4280
15
2.3
2.00
15.21
11
24
30.4
2/19/99
4260
13
16.13
15
15
30.4
2/20/99
3360
12
30.4
2/21/99
4120
10
30.4
2/22/99
4000
10
3.6
3.00
27
6
18
30.4
2/23/99
3430
10
29.56
9
18
30.4
2/24/99
3000
11
23.02
3
13
30.4
2/25/99
3150
10
6.2
5.50
27.42
10
13
30.4
2/26/99
4150
12
25.04
12
11
30.4
2/27/99
2650
15
30.4
2/28/99
2210
15
30.4
3/1/99
2800
15
4.1
3.30
17.96
18
33
30.4
3/2/99
4320
13
15.41
22
26
30.4
3/3/99
4110
13
9.45
21
14
23.0
3/4/99
3690
10
2.2
1.83
18.41
14
19
23.0
3/5/99
3780
11
15.27
9
7
23.0
3/6/99
4180
15
23.0
3/7/99
4880
13
23.0
3/8/99
3920
12
2.9
2.90
10.28
7
22
28
23.0
3/9/99
3760
12
13
9
29
23.0
3/10/99
3580
13
13.91
16
20
23.0
3/11/99
55
3720
0.015
13
4.4
4.60
9.73
18.2
3.99
8.47
22.19
13.72
12
17
32
23.0
3/12/99
3160
12
14.39
9
22
23.0
3/13/99
3610
12
23.0
3/14/99
3780
12
23.0
3/15/99
3800
11
2.9
2.30
19.09
6.55
4.75
: 23 84
23.84
11
27
43
23.0
3/16/99
4090
15
17.55
11
25
23.0
3/17/99
3820
16
20.86
16
20
23.0
3/18/99
4140
17
5.62
5.20
8.57
18.6
9.5
10.03
28.1
18.07
19
36
23.0
3/19/99
3860
15
15.86
10
45
23.0
3/20/99
4270
14
23.0
3/21/99
4470
13
23.0
3/22/99
3930
12
2.52
2.40
11.25
11.4
10.6
0.15
22
21.85
14
7
12
23.0
3/23/99
4780
15
13.18
13
13
23.0
3/24/99
4180
16
19.51
12
16
23.0
3/25/99
4190
17
3.5
2.70
12.29
26.2
1.3
13.91
27.5
13.59
10
14
21
23.0
3/26/99
4050
15
29.08
14
19
23.0
3/27/99
4170
14
23.0
3/28/99
2720
15
23.0
3/29/99
3970
16
2.75
2.30
21.67
18.6
3.4
= 5;017 i
25.07
12
7
4
23.0
3/30/99
4270
14
24.83
14
4
23.0
3/31/99
4350
17
31.07
18
5
23.0
4/1/99
4370
18
2.5
2.05
26.63
7
'A33463',w
33.63
18
7
5
23.0
4/2/99
18
23.0
4/3/99
3290
20
23.0
4/4/99
3340
20
23.0
4/5/99
3560
20
1.91
1.40
16.54
15.3
5.9
[:22:44.•
22.44
11
<2
2
23.0
4/6/99
4230
18
17.73
10
4
23.0
4/7/99
3720
20
24.35
18
4
23.0
4/8/99
76
3720
0.020
20
2.3
2.00
23.8
19.9
0.41
: 2421::
24.21
7
3
3
23.0
4/9/99
4020
22
23.15
4
3
23.0
4/10/99
3990
21
23.0
4/11/99
4230
21
23.0
4/12/99
58.4
3890
0.015
18
1.85
1.70
29.33
7
3
1
23.0
4/13/99
4150
17
31.63
6
2
23.0
4/14/99
3830
15
14.56
16
2
23.0
4/15/99
4110
18
2.15
1.92
36.56
28.5
11
2
1
23.0
4/16/99
4150
16
36.23
5
5
23.0
13024s006
Data
9 of 12
10/27/99

San
Fort
yea
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Mixed Liq
Effluent
Date
TP
MLSS
P/TSS
Temp
.TP
Ortho-P
NH3
TKN (3)
NO3/
Org-N
TN (1)
TNN
TSS
CBOD5
BOD5
H3PO4
(4)
-N(2)
NO2-N
mg/L
mglL
C
mglL
mg/L
mg/L
mg/L
mglL
mg/L
mg!L
mg/L
mg!L
mg/L
mg/L
gpd
4017/90
3290
15
23.0
4/18/99
4190
14
23.0
4/19/99
3810
15
1.6
1.43
33.4
8.25
,; .4;485 "::
41.65
7
2
2
23.0
4/20/99
3830
17
37.1
11
2
23.0
4/21 /99
3940
19
39.61
16
2
15.0
4/22/99
63
2310
0.027
21
2.13
2.00
35.95
29.6
2.1
'3805' '
38.05
12
<2
1
15.0
4/23/99
3710
22
37.91
9
1
15.0
4/24/99
4120
20
15.0
4/25/99
4230
21
15.0
4/26/99
4710
21
3.5
2.40
41.24
35.3
19
5
15.0
4/27/99
4470
22
35.95
12
4
15.0
4/28/99
3730
19
35.77
5
5
15.0
4/29/99
3510
17
1.60
40.17
33.2
13
6
15.0
4/30/99
3350
15
40.14
16
16
15.0
5/1/99
2880
15
15.0
5/2/99
2910
16
15.0
5/3/99
33.8
2420
0.0139
17
1.63
39.84
27.6
20
45
34
15.0
5/4/99
2800
20
36.36
25
28
15.0
5/5/99
2110
20
24.8
15
33
15.0
5/6/99
2520
22
1.2
1.08
7.69
18.9
3
11.21
21.9
10.69
13
15
18
15.0
5/7/99
2280
23
22.01
14
23
15.0
5/8/99
1920
22
15.0
5/9/99
2350
22
15.0
5/10/99
1680
23
0.98
0.90
23.94
27.3
0.02
3.36
27.32
23.96
7
12
18
15.0
5/11/99
2100
22
34.9
10
13
15.0
5/12/99
1740
21
36.85
16
34
15.0
5/13/99
1790
21
0.4
0.70
38.72
30.3
2.6
4'E 32-
41.32
20
19
28
15.0
5/14/99
3220
18
33.73
11
37
15.0
5/15/99
3250
17
15.0
5/16/99
4000
19
15.0
5/17/99
4090
21
1.28
0.70
27.3
33.4
2
6.1
35.4
29.3
10
6
13
15.0
5/18/99
4230
22
26.07
20
12
15.0
5/19/99
4010
22
1.23
2.40
27.67
33.1
0.26
5.43
33.36
27.93
18
5
7
15.0
5/20/99
4180
22
24.86
26
6
15.0
5/21/99
4550
23
16.85
17
6
15.0
5122/99
3110
23
15.0
5/23/99
5230
24
15.0
5/24/99
3700
23
0.85
0.97
0.67/9.9
13.5
0.1
3.55
13.6
10.05
12
- <2
12
15.0
5/25/99
3910
21
11.1
8
6
15.0
5/26/99
3280
22
1.51
1.30
1.85/11.
14.7
2.8
3
17.5
14.5
11
2
26
15.0
5/27/99
3460
21
12.18
10
3
15.0
5/28/99
2350
21
9.45
10
18
15.0
5/29/99
4490
22
15.0
5/30/99
4380
23
15.0
5/31/99
22
2.7
0.60
5.95
9.29
2.5
3.34
11.79
8.45
2
15.0
6/1/99
4210
22
5.17
5
13
15.0
6/2/99
15.5
2440
0.0064
24
1.5
1.19
0.37/8.0
11.3
2.95
3.23
14.25
11.02
10
2
8
15.0
6/3/99
3490
25
11.12
9
9
15.0
6/4/99
3680
24
13.62
10
9
15.0
' 6/5/99
3750
23
15.0
6/6/99
3420
24
15.0
6/7/99
23.5
3010
0.0078
24
1.6
1.64
4.34/13.
16.2
0.7
3.2
16.9
13.7
11
6
13
15.0
6/8/99
3470
24
10.88
13
7
15.0
6/9/99
4040
24
11.92
19
5
15.0
6/10/99
4500
25
14.09
9
5
15.0
6/11/99
25
4060
0.0062
23
1.48
1.25
0.05/10.
13.9
0.15
3.1
14.05
10.95
9
3
5
15.0
6/12/99
3420
22
15.0
6/13/99
2590
21
15.0
6/14/99
2810
24
1.9
1.55
9.18/8.4
12.6
2.4
4.2
15
10.8
18
<2
9
15.0
6/15/99
3340
24
9.46
9
29
15.0
6/16/99
3440
23
15.75
9
12
15.0
6/17/99
3320
22
10.85
6
4
15.0
6/18/99
3270
21
2.25
2.08
3.6/3.35
5.6
0.7
2.25
6.3
4.05
7
<2
10
15.0
6/19/99
2370
23
15.0
6/20/99
3320
21
15.0
' 6/21/99
3550
23
1.75
1.50
.69/1.4
5.53
0.08
4.1
5.61
1.51
15
3
2
15.0
13024s006
Data
10 0f 12
10/27/99
n

ORN
req
r
ICA
Clatt
tftl
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA
AEI JOB NO. N130-24B
Mixed Liq
Effluent
Date
TP
MLSS
P/TSS
Temp '
TP
Ortho-P
NH3
TKN (3)
NO3/
Org-N
TN (1)
TNN
TSS
CBODS
BODS
H3PO4
(4)
-N(2)
NO2-N
mglL
mg/L
C
mglL
mg/L
mg/L
mg/L
mglL
mglL
mg/L
mg/L
mglL
mglL
mglL
gpd
6122/98
3690
23
1.48
5
1
15.0
6/23/99
4710
23
2
1.40
1.47/<1
3.78
0.12
2.78
3.9
1.12
7
<2
3
15.0
6/24/99
4830
24
2.22
6
3
15.0
6/25/99
4000
23
2.1
21
5
15.0
6/26/99
4300
23
15.0
6/27/99
4060
24
15.0
6/28/99
3430
26
3.4
2.18
.07/5.5
8.57
0.09
2.99
8.69
5.67
19
3
4
15.0
6/29/99
3580
26
5.62
9
7
15.0
6/30/99
58
2790
0.0208
25
2.55
2.20
5.14/7.8
13
1.1
5.2
14.1
8.9
12
<2
4
15.0
7/1/99
3230
26
11.37
12
5
15.0
7/2/99
3590
25
1.77
5
7
15.0
7/3/99
26
15.0
7/4/99
3680
27
15.0
7/5/99
27
15.0
7/6/99
3970
27
1.84
1.70
<1
1.54
5.75
0.54
7.29
6.75
2
5
6
15.0
7/7/99
25
1
3
2
15.0
7/8/99
4240
27
1
5
3
15.0
7/9/99
28.6
2630
0.0109
27
1.7
1.14
<1
2.15
7
1.15
9.15
8
6
10
4
15.0
7/10/99
4640
25
15.0
7/11/99
24
15.0
7/12/99
4220
22
2.01
1.30
<1
2.78
6.2
1.78
8.98
7.2
4
7
7
15.0
7/13/99
4090
23
2.96
_
13
5
15.0
7/14/99
4660
23
2.3
1.50
<1
1.03
4.8
0.03
5.83
5.8
9
6
5
15.0
7/15/99
3630
24
3.25
9
1
15.0
7/16/99
3760
25
3.7
14
2
15.0
7/17/99
4660
26
15.0
7/18/99
4160
26
15.0
7/19/99
3910
27
1.4
1.50
<1
3.21
4.6
2.21
7.81
5.6
14
<2
1
15.0
7/20/99
2690
27
1.48
12
3
15.0
7/21/99
3980
26
1.4
1.14
2
5.42
3.15
3.42
8.57
5.15
12
<2
4
15.0
7/22/99
3950
29
3.55
14
3
15.0
7/23/99
4310
30
1.12
22
3
15.0
7/24/99
4940
15.0
7/25/99
28
15.0
7/26/99
2780
27
1.03
0.97
1
2.74
2.3
1.74
5.04
3.3
12
<2
1
15.0
7/27/99
4220
28
1
9
3
15.0
7/28/99
40
3492
0.011
27
1.05
1.00
1
2
4.6
1
6.6
5.6
13
<2
1
15.0
7/29/99
3660
28
2.22
13
1
15.0
7/30/99
3980
28
1.77
11
2
15.0
7/31/99
4100
28
15.0
8/1/99
4720
28
15.0
8/2/99
4720
28
1.1
1.10
2.51
2.52
2.89
0.01
5.41
5.4
8
<2
1
15.0
8/3/99
4280
26
2.48
16
1
15.0
8/4/99
4460
26
0.6
0.60
2.81
4.27
0.69
1.46
4.96
3.5
18
<2
2
15.0
8/5/99
4680
2.72
23
1
15.0
8/6/99
4810
26
1.89
16
3
15.0
8/7/99
4670
27
15.0
8/8/99
4290
28
15.0
8/9/99
3750
28
0.9
0.80
2.39
5.75
0.34
3.36
6.09
2.73
12
7
8
15.0
8/10/99
4540
27
2.6
9
7
15.0
8/11/99
24
4588
0.005
27
0.85
0.80
2.22
5.81
0.42
3.59
6.23
2.64
14
8
4
15.0
8/12/99
4010
26
3.34
18
6
15.0
8/13/99
3990
27
7.69
14
9
15.0
8/14/99
5130
27
15.0
8/15/99
3720
27
15.0
8/16/99
2000
28
0.64
0.62
10.07
13.5
0.44
3.43
13.94
10.51
11
9
11
15.0
8/17/99
3310
27
9.48
14
9
15.0
8/18/99
2490
26
0.9
0.63
10.07
13
1.1
2.93
14.1
11.17
23
11
13
15.0
8/19/99
3000
25
9.98
13
5
15.0
8/20/99
2910
24
11.6
16
7
15.0
8/21/99
3430
23
15.0
8/22/99
4150
24
15.0
8/23/99
3150
25
1.11
0.83
13.62
18.9
6.1
5.28
25
19.72
19
14
16
15.0
8/24/99
3250
25
13.23
.
14
14
15.0
8/25/99
31
4012
0.008
27
1
0.71
12.46
13.6
11.2
1.14
24.8
23.66
13
17
10
15.0
8/26/99
4480
28
12.03
15
11
15.0
10/27/99
13024s006
Data
11 of 12

Pan
/i
cal
014
dilk
OW
WI
rttl
1=t
lalb
CLARIANT CORPORATION - BAT STUDY
FULL SCALE VVWTP DATA
AEI JOB NO. N130-24B
Mixed Liq
Effluent
Date
TP
MLSS
PlTSS
Temp
TP
Ortho-P
NH3
TKN (3)
NO3/
Org-N
TN (1)
TNN
TSS
CBOD5
BOD5
H3PO4
(4)
-N(2)
NO2-N
mglL
mglL
C
mg/L
mg/L
mglL
mg/L
mglL
mglL
mg/L
mglL
mg/L
mglL
mglL
gpd
8127/90
3260
26
2.93
14
5
15.0
8/28/99
4580
26
15.0
8/29/99
3480
25
15.0
8/30/99
4010
23
0.95
0.92
2.07
3.86
2.7
1.79
6.56
4.77
14
3
10
15.0
8/31/99
3710
22
2.18
13
6
15.0
9/1/99
21
3347
0.006
20
1.05
0.92
4.07
4.12
2.3
0.05
6.42
6.37
11
3
8
15.0
9/2/99
3720
22
3.78
7
6
15.0
9/3/99
3560
22
10.14
10
8
15.0
9/4/99
2510
23
15.0
9/5/99
3330
23
15.0
9/6/99
24
15.0
9/7/99
3010
25
1.37
0.51
5.7
8.01
5.6
2.31
13.61
11.3
5
3
9
15.0
9/8/99
3100
25
1.6
1.21
7.39
10.1
0.8
2.71
10.9
8.19
9
<2
6
15.0
9/9/99
3060
26
6.41
15
7
15.0
9/10/99
3110
24
6.59
4
8
15.0
9/11/99
4260
22
15.0
9/12/99
2350
21
15.0
9/13/99
4410
24
1.35
1.31
2.39
4.64
0.11
2.25
4.75
2.5
12
<2
16
15.0
9/14/99
3400
23
2.19•
4
10
15.0
9/15/99
16.1
3590
0.004
23
0.45
0.98
2.93
6.13
6.9
3.2
13.03
9.83
8
<2
8
15.0
9/16/99
3960
22
2.89
4
8
15.0
9/17/99
3380
19
2.78
11
2
15.0
9/18/99
3450
20
15.0
9/19/99
2580
20
15.0
9/20/99
3370
20
0.75
0.70
1.48
2.54
0.02
1.06
2.56
1.5
9
<2
2
15.0
9/21/99
2440
22
1.63
4
2
15.0
9/22/99
2340
19
0.62
0.60
1.77
11
<2
1
15.0
9/23/99
2470
20
1.92
5
1
15.0
9/24/99
2610
19
1.07
4
2
15.0
9/25/99
3110
21
15.0
9/26/99
3060
23
15.0
9/27/99
2510
24
3.58
11
5
15.0
9/28/99
2510
25
5.49
11
2
15.0
9/29/99
2040
25
13.68
4
7
15.0
9/30/99
2750
20
14.19
10
4
15.0
(1) Shaded TN values were calculated using NH3 due to TKN < NH3
(2) NH3 Data: Bold data analyzed by Hydro Analytical. All other data analyzed by Clariant. Hydro Analytical data was used when available.
(3) TKN Data: Bold values signify days in which TKN < NH3. These data points were not used in any calculations.
(4) MLSS Data: Bold values signify data analyzed by Hydro Analytical
10/27/99
13024s006
Data
12 of 12

n
ac+
ar,
414
fan
ofti
Pah
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA SUPPLIED BY CLARIANT
AEI JOB NO. N130-24B
Date
MLSS
Z03A
mg/L
Z04
mg/L
F/M Cil
Aeration
Z03A
Basin pH
Z04
DO
Z03A
Z04
Sludge Age ll)
(MCRT)
days
01 /01 /99
6.80
7.00
13.8
13.3
01/02/99
7.00
7.00
12.7
13.1
01/03/99
6.80
7.00
12.6
13.3
01/04/99
1340
3850
0.05
6.80
6.90
12.6
13.7
21
01/05/99
2290
2730
8.90
7.00
11.3
14
32
01/06/99
2080
3340
0.13
9.00
7.70
10.5
13.5
24
01/07/99
3480
3580
7.40
6.90
9.7
12
35
01/08/99
1920
3570
0.37
6.70
7.00
6.9
10.7
25
01/09/99
2850
2800
6.40
6.80
8
10.2
34
01/10/99
2380
3370
6.50
6.70
7.3
10.5
60
01/11/99
2770
3880
0.37
6.60
7.00
6.8
10.4
25
01/12/99
2630
3880
6.60
6.90
3.8
9.7
27
01/13/99
2550
3640
0.58
6.40
6.70
6.1
9.9
24
01/14/99
4920
3920
6.70
6.90
6
9.3
46
01/15/99
1640
4200
0.08
6.40
6.80
4.7
10.6
22
01/16/99
2980
2240
6.60
7.30
4.6
10.5
25
01/17/99
4560
2550
6.00
7.60
6.4
9.4
35
01/18/99
4020
4020
0.54
6.80
7.00
3.4
9.6
26
01/19/99
2640
3450
6.80
7.40
5.8
9.7
26
01/20/99
2140
4430
0.75
6.60
6.80
3.2
9.5
27
01/21/99
2740
4710
6.80
7.10
3.3
8.3
32
01/22/99
3280
4180
0.47
6.90
7.20
3.5
9
23
01/23/99
4600
4140
7.30
7.40
6.4
8.9
26
01/24/99
6770
5190
6.80
7.10
4.8
9.3
40
01/25/99
4490
4680
0.54
7.30
7.00
7.1
9.9
27
01/26/99
2520
3620
6.70
7.00
7.7
10.7
18
01/27/99
1930
4320
0.73
6.40
7.00
2.5
8.5
22
01/28/99
4640
4780
6.80
7.30
6.3
10
24
01/29/99
3240
4700
0.29
7.40
7.40
4.6
9.5
19
01/30/99
2300
4710
7.30
7.10
7.2
9.6
18
01/31/99
4040
4920
7.00
6.90
5.6
10.9
23
02/01/99
2520
4680
1.32
7.10
7.30
7.9
10.5
20
02/02/99
5990
4950
7.10
7.20
6.6
10.2
21
02/03/99
2630
4860
0.25
7.20
7.10
7.6
10.6
20
02/04/99
5040
5260
7.10
7.10
8.2
10.4
25
02/05/99
5670
5050
0.17
7.00
7.30
6.6
10.5
35
02/06/99
4120
2950
7.00
7.10
7
9.3
21
02/07/99
6750
6340
7.20
7.30
7.8
9
40
02/08/99
4440
4160
0.32
7.30
7.20
8
9.8
26
02/09/99
4090
5150
7.40
7.40
8.7
9.9
21
02/10/99
5590
4900
0.33
7.40
7.20
7.9
10
23
02/11/99
3520
5320
7.20
7.20
6.7
9
16
02/12/99
7260
8740
0.05
7.10
7.40
6.6
9.9
20
02/13/99
5230
5550
7.40
7.30
8.5
10.4
24
02/14/99
5680
5680
7.40
7.30
8.9
11.6
27
02/15/99
2600
4260
0.37
7.50
7.10
9.2
10.7
18
02/16/99
3870
5380
7.20
7.20
8.7
10.6
21
02/17/99
3400
4830
0.22
7.40
7.20
8.2
10.1
22
02/18/99
3030
4280
7.50
7.30
8.6
10.1
19
02/19/99
3780
4260
0.34
8.20
7.50
10.4
10.9
22
02/20/99
3540
3360
7.50
7.30
8.7
11.1
22
02/21/99
4080
4120
7.50
7.20
7.3
11.2
27
02/22/99
3170
4000
0.46
7.20
6.70
6.8
11.5
21
02/23/99
2970
3430
7.50
7.10
7.1
11.4
23
02/24/99
1610
3000
0.32
7.10
7.10
6
11.1
16
02/25/99
5230
3150
7.20
7.30
7.2
10.5
26
02/26/99
3380
4150
7.10
7.50
4.7
10.3
25
13024s006
Clariant Data
1 of5
10/28/99
r=1

n
1061
fibt
Tx►
aa►
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA SUPPLIED BY CLARIANT
AEI JOB NO. N130-24B
Date
MLSS
ZO3A
mg/L
Z04
mg/L
F/M (1)
Aeration
ZO3A
Basin pH
Z04
DO
ZO3A
Z04
Sludge Age")
(MCRT)
days
02/27/99
2180
2650
7.40
7.00
5.2
8.9
21
02/28/99
3190
2210
8.50
8.30
6.3
9.1
23
03/01/99
2880
2800
0.28
7.10
7.40
7
9.9
22
03/02/99
2610
4320
7.00
7.40
5.6
10.3
21
03/03/99
4890
4110
0.27
8.00
7.80
7.9
10.4
32
03/04/99
2430
3690
7.60
7.60
10.2
9.9
21
03/05/99
3170
3780
7.30
7.50
11.3
10.8
24
03/06/99
3890
4180
7.30
7.60
6.2
9.9
51
03/07/99
2790
4880
7.30
7.30
7.4
10.7
28
03/08/99
2860
3920
7.40
7.50
8.5
12.1
22
03/09/99
2550
3760
7.60
7.20
9.9
12.2
22
03/10/99
3090
3580
0.20
8.10
7.50
9.1
11.8
23
03/11/99
3200
3720
7.60
7.40
4.7
10.3
24
03/12/99
2280
3160
7.80
7.50
7.6
10.7
18
03/13/99
2790
3610
7.60
7.50
7.6
11.5
24
03/14/99
3380
3780
7.70
7.80
8.2
10.9
27
03/15/99
2310
3800
0.51
7.60
7.40
4.7
11.2
30
03/16/99
3840
4090
7.40
7.50
3.8
10
24
03/17/99
3480
3820
0.52
7.50
7.80
3.2
9.1
27
03/18/99
4180
4140
7.30
7.50
0.4
8.5
24
03/19/99
3030
3860
7.40
7.70
4.3
9.7
20
03/20/99
3770
4270
7.60
7.70
8.3
10.5
59
03/21/99
2870
4470
7.60
7.80
8.5
10.4
41
03/22/99
2920
3930
0.13
7.90
7.80
7.7
10.9
37
03/23/99
2810
4780
8.00
7.90
8.6
10.9
22
03/24/99
3610
4180
0.31
8.00
7.90
6.6
10
25
03/25/99
3320
4190
0.22
7.60
7.70
3.4
9.2
22
03/26/99
2810
4050
8.40
7.70
5.8
10.1
21
03/27/99
3350
4170
8.30
7.80
9.2
9.7
28
03/28/99
2080
2720
5.60
7.90
7.2
9.5
22
03/29/99
2580
3970
0.68
7.90
8.10
6.3
9.6
24
03/30/99
3970
4270
7.60
7.20
5
9.5
26
03/31/99
1300
4350
1.04
8.00
7.60
6.7
9.3
30
04/01/99
2430
4370
8.20
7.60
8.5
9.5
23
04/02/99
8.50
7.80
8.6
9.8
04/03/99
3820
3290
7.90
7.80
8.2
8.5
51
04/04/99
2480
3340
7.90
7.90
8.2
8.9
30
04/05/99
3610
3560
0.12
8.10
7.90
7.9
9
47
04/06/99
2380
4230
8.20
8.00
8.2
9.5
30
04/07/99
3920
3720
0.10
8.10
7.80
3.7
8.6
29
04/08/99
2170
3720
7.40
7.90
4.2
8.4
22
04/09/99
2990
4020
7.40
7.90
6
8.2
26
04/10/99
3270
3990
7.90
7.90
6.8
8.6
18
04/11/99
3270
4230
7.80
8.00
5.4
8.5
24
04/12/99
2980
3890
0.27
8.40
8.10
7.3
9.3
18
04/13/99
2950
4150
7.80
8.10
6.3
9.4
21
04/14/99
2920
3830
0.14
7.70
7.80
4
8.8
17
04/15/99
3390
4110
8.10
7.70
5.5
8.2
23
04/16/99
5710
4150
0.18
8.10
7.90
8.3
10
29
04/17/99
2610
3290
7.80
8.00
6.1
10.2
18
04/18/99
1830
4190
7.70
8.00
8.4
10.1
17
04/19/99
3090
3810
7.90
8.20
7.7
9.5
21
04/20/99
1930
3830
7.90
7.90
6.3
9.1
18
04/21/99
2900
3940
0.38
7.40
7.40
3.4
8.8
18
04/22/99
3090
3960
7.00
7.30
3.9
8.4
20
04/23/99
3350
3710
6.50
7.70
1.4
7.5
22
04/24/99
3360
4120
7.70
7.10
2.5
7.2
18
13024s006
Clariant Data
2of5
10/28/99
rya

f=I
MR
404
rsa
ma
f►
WI
Plet
r1
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA SUPPLIED BY CLARIANT
AEI JOB NO. N130-24B
Date
MLSS
ZO3A
mg/L
Z04
mg/L
F/M t"
Aeration
ZO3A
Basin pH
Z04
DO
ZO3A
Z04
Sludge Agee"
(MCRT)
days
04/25/99
3180
4230
6.40
7.10
5.5
7.4
37
04/26/99
4670
4710
0.49
7.50
7.40
4.8
7.6
21
04/27/99
3280
4470
7.50
8.80
5.7
8.1
13
04/28/99
2390
3730
0.57
7.80
7.00
5.3
8.2
16
04/29/99
2300
3510
7.80
7.30
5.5
7.4
11
04/30/99
2220
3350
7.80
8.30
7.9
8.8
13
05/01/99
2570
2880
8.20
7.50
6.7
9.4
22
05/02/99
2080
2910
7.50
7.60
6.9
9.2
28
05/03/99
1810
2440
0.84
7.10
7.20
3.4
8.9
22
05/04/99
1670
2800
7.20
6.30
2.8
8.7
19
05/05/99
2190
2110
0.74
7.80
8.30
4.8
9.6
17
05/06/99
1900
2520
7.10
8.50
4.2
8
23
05/07/99
1450
2280
7.90
6.90
4.2
8
17
05/08/99
1220
1920
7.20
6.80
3.4
8.4
16
05/09/99
1180
2350
7.00
7.30
1.4
9.9
19
05/10/99
1400
1680
2.40
7.10
6.50
2
7.4
21
05/11/99
1460
2100
7.20
6.40
7.7
10.1
16
05/12/99
1370
1740
0.64
6.50
8.00
8.2
9.8
8
05/13/99
1390
1790
7.50
7.60
3.8
9.9
21
05/14/99
3810
3220
7.20
7.20
6.8
7.1
31
05/15/99
4890
3250
7.60
7.70
8
10.4
30
05/16/99
4270
4000
7.40
7.80
13
15.3
31
05/17/99
2780
4090
0.27
7.30
7.70
9.3
11.8
24
05/18/99
2760
4230
7.90
7.50
5
9.9
15
05/19/99
2900
4010
0.51
7.30
7.60
6.1
9.9
9
05/20/99
2640
4180
7.20
7.30
5.4
13.6
16
05/21/99
2500
4550
6.70
7.60
5
11
17
05/22/99
2900
3110
7.30
7.40
7.2
7.9
13
05/23/99
2790
5230
6.40
7.40
7.8
10
20
05/24/99
3060
3700
0.17
7.30
7.50
7.1
8
19
05/25/99
2260
3910
7.00
7.50
3
9.2
16
05/26/99
2220
3280
0.69
7.50
7.60
10.1
13.2
17
05/27/99
2650
3460
7.30
7.60
7.4
10.6
34
05/28/99
2660
2350
7.50
7.60
7.7
10.1
25
05/29/99
2420
4490
7.40
7.80
9.1
11.2
20
05/30/99
2890
4380
7.10
7.40
7.6
8.1
18
05/31/99
7.40
7.50
8.6
8.3
06/01/99
3950
4210
6.80
7.50
6.7
9.3
15
06/02/99
3100
3640
0.35
6.90
7.40
6
8.9
15
06/03/99
2640
3490
6.30
7.10
3.4
6.5
10
06/04/99
1810
3680
6.90
7.40
4.7
7.2
7
06/05/99
1910
3750
6.70
7.60
2.8
7.8
13
06/06/99
3140
3420
7.00
7.40
6.1
7.4
14
06/07/99
4090
3720
0.41
7.00
7.80
5.2
7.2
19
06/08/99
2230
3470
6.30
7.60
3.1
7.4
15
06/09/99
2170
4040
6.90
7.40
2.1
6.8
15
06/10/99
3360
4500
0.77
7.40
7.60
4.6
7.4
15
06/11/99
2650
4110
0.08
7.10
8.00
6.9
7.8
12
06/12/99
3070
3420
7.10
7.80
7.2
7.8
20
06/13/99
2570
2590
7.10
7.70
6.8
8.2
18
06/14/99
1970
2810
7.10
7.70
6.6
5
16
06/15/99
1790
3340
7.00
8.00
5.8
8.1
19
06/16/99
2260
3440
0.42
6.90
7.90
5.1
7.9
14
06/17/99
2570
3320
7.00
7.30
6.2
7.7
13
06/18/99
2740
3270
6.50
7.60
6.5
8.5
17
06/19/99
2200
2370
6.70
7.20
4.5
7.9
15
06/20/99
1890
3320
6.10
7.60
3.4
8.5
14
13024s006
Clariant Data
3of5
10/28/99

rakt
raa
ra
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA SUPPLIED BY CLARIANT
AEI JOB NO. N130-24B
Date
MLSS
ZO3A
mg/L
Z04
mg/L
F/M (1)
Aeration
ZO3A
Basin pH
Z04
DO
ZO3A
Z04
Sludge Age (1)
(MCRT)
days
06/21/99
2430
3550
0.42
6.70
7.20
0.7
7
17
06/22/99
3350
3690
6.80
7.10
3.7
6.8
21
06/23/99
3460
4710
0.67
6.70
7.80
3.3
6.8
16
06/24/99
2910
4830
6.60
7.80
6.4
7.7
16
06/25/99
4070
4000
6.50
7.70
6.9
7.8
22
06/26/99
3640
4300
6.80
7.70
7.4
8
26
06/27/99
2320
4060
6.40
7.80
7
7.7
24
06/28/99
2720
3430
0.12
6.70
7.80
7.7
8.3
24
06/29/99
3010
3580
6.10
7.90
7
7.7
20
06/30/99
2640
3490
0.08
6.70
8.00
6.9
7.7
13
07/01/99
2570
3230
7.10
8.10
6.8
7.7
15
07/02/99
2030
3590
6.90
7.70
7.1
7.8
13
07/03/99
7.30
7.80
7.5
7.8
07/04/99
2130
3680
6.80
8.30
6.3
6.8
62
07/05/99
6.90
7.70
6.4
6.7
07/06/99
1070
3970
7.00
7.50
5.1
7.2
53
07/07/99
6.70
7.40
3.6
7.2
07/08/99
3150
4240
6.70
8.00
6.4
7.6
21
07/09/99
7.20
7.80
6.3
7.2
07/10/99
2710
4640
6.80
7.80
6.2
7.5
20
07/11/99
6.70
7.60
6.5
8.3
07/12/99
2580
4220
0.25
6.80
7.50
5.6
7.9
24
07/13/99
3250
4090
6.60
7.50
5.6
8.3
11
07/14/99
3090
4660
0.64
6.40
8.10
7.1
8
13
07/15/99
2440
3630
6.70
7.90
7
8.1
12
07/16/99
3660
3760
4.80
8.30
5.70 7.50 16
07/17/99
3270
4660
7.20
8.30
10.6
12.5
16
07/18/99
3020
4160
6.80
8.30
6.5
6.5
15
07/19/99
2390
3910
0.14
6.80
7.90
6
7.1
19
07/20/99
2330
2690
7.30
8.20
5.9
7.2
10
07/21/99
2720
3980
0.38
7.20
6.90
6.2
10.1
47
07/22/99
2810
3950
6.70
6.90
4.4
5.8
13
07/23/99
1370
4310
6.70
7.00
3.00
6.60
12
07/24/99
2580
4940
27
07/25/99
7.00
7.10
6
7.6
07/26/99
2550
2780
0.42
6.70
7.30
4.6
7.1
10
07/27/99
2430
4220
6.70
7.10
5.3
6.9
18
07/28/99
2970
3690
0.72
6.30
7.40
4.3
7.1
18
07/29/99
1960
3660
6.50
7.50
4.1
6.6
13
07/30/99
2540
3980
7.10
7.80
0.7
6.8
16
07/31/99
2800
4100
6.40
7.50
1.4
6.1
17
08/01/99
3260
4720
6.70
6.70
0.9
5.8
16
08/02/99
3420
4720
0.84
6.80
7.20
0.6
6.3
17
08/03/99
2140
4280
6.50
6.60
1.2
6
11
08/04/99
2530
4460
0.71
6.60
7.60
1
5.6
17
08/05/99
4180
4680
6.70
7.20
2.2
6.4
19
08/06/99
3050
4810
6.30
7.40
3.4
6.6
18
08/07/99
3500
4670
6.40
7.50
3.6
6.9
16
08/08/99
2970
4290
7.20
7.70
2.7
6.8
13
08/09/99
3450
3750
0.71
6.80
7.50
3
6.5
12
08/10/99
3450
4540
7.10
7.30
5.8
7.1
13
08/11/99
2920
4370
0.41
6.40
7.30
2.8
7.3
12
08/12/99
2610
4010
6.50
7.40
6.9
7.2
12
08/13/99
2910
3990
7.60
7.70
1.4
6.4
11
08/14/99
1420
5130
7.40
7.40
1.6
6.6
8
08/15/99
3060
3720
6.40
7.40
2.4
7.4
14
08/16/99
2450
2000
0.54
6.90
7.60
4.4
7.3
8
13024s006
Clariant Data
4of5
10/28/99
r"

lit
Aa
<Le+
cal
Furl
ROI
raa
CLARIANT CORPORATION - BAT STUDY
FULL SCALE WWTP DATA SUPPLIED BY CLARIANT
AEI JOB NO. N130-24B
Date
MLSS
ZO3A
mg/L
Z04
mg/L
F/M "I
Aeration
ZO3A
Basin pH
Z04
DO
ZO3A
Z04
Sludge Age (1)
(MCRT)
days
08/17/99
2400
3310
6.90
8.10
4.8
7.4
17
08/18/99
2250
2490
0.93
7.00
8.10
5.2
7.2
14
08/19/99
1710
3000
7.40
7.60
6.4
7.6
13
08/20/99
2630
2910
7.10
7.50
6.8
7.9
17
08/21/99
2840
3430
7.90
7.40
5.1
8
21
08/22/99
2430
4150
6.80
7.70
5.1
6.9
23
08/23/99
3020
3150
0.93
7.50
7.70
3.7
7.2
15
08/24/99
2560
3250
6.50
8.20
2.2
7.4
11
08/25/99
3310
4700
0.53
7.20
7.80
1.4
6.5
15
08/26/99
3350
4480
6.90
7.80
1
6.4
19
08/27/99
3190
3260
7.80
7.80
6.3
7.6
16
08/28/99
2430
4580
7.20
8.50
3.6
8.8
12
08/29/99
2340
3480
7.80
8.10
4.7
7.6
9
08/30/99
2590
4010
0.58
7.80
8.00
7
8.2
17
08/31/99
3120
3710
8.20
8.00
8.9
10.9
19
09/01/99
3250
3630
0.07
7.40
8.00
6.3
8.3
17
09/02/99
3170
3720
6.70
8.30
3.6
7.1
19
09/03/99
1780
3560
6.80
8.00
7.3
8.1
16
09/04/99
3310
2510
7.40
9.30
7.9
7.9
28
09/05/99
2870
3330
6.70
7.80
7.9
7.9
20
09/06/99
7.10
7.40
7.9
8
09/07/99
1670
3010
6.90
8.00
7.9
8.3
12
09/08/99
2450
3100
0.02
6.50
7.60
5.6
7.6
13
09/09/99
3590
3060
6.90
7.70
3.8
8.9
17
09/10/99
1140
3110
0.23
7.20
7.60
4.2
7.2
8
09/11/99
1860
4260
7.80
8.00
6
7.7
21
09/12/99
1910
2350
7.10
7.80
3.1
8.4
17
09/13/99
4070
4410
0.28
7.50
7.60
4.6
8
23
09/14/99
2590
3400
7.20
7.70
6.1
7.8
15
09/15/99
3180
3820
0.35
7.30
7.40
3.2
7.7
13
09/16/99
2520
3960
7.00
8.50
5.8
8
10
09/17/99
2530
3380
7.20
7.60
6.3
8.7
11
09/18/99
2770
3450
7.30
8.00
6.5
8.5
27
09/19/99
2820
2580
7.40
7.90
7.7
8.7
42
09/20/99
2800
3370
0.26
7.80
7.80
7.1
8.4
22
09/21/99
2650
2440
7.40
6.90
6.5
8.6
20
09/22/99
2530
2340
0.53
7.30
7.60
6
10
10
09/23/99
2250
2470
7.90
7.90
3
8.3
11
09/24/99
2410
2610
8.40
7.40
7.3
8.8
24
09/25/99
2240
3110
8.40
7.60
7.8
8.6
1735
09/26/99
2680
3060
8.00
7.60
7.7
8.6
1071
09/27/99
2740
2510
0.54
7.80
7.90
6.9
7.9
29
09/28/99
2170
2510
8.60
7.50
5
7.7
21
09/29/99
2120
2040
1.32
8.40
7.80
4.9
7.3
13
09/30/99
1880
2750
8.50
7.90
5.8
6.3
18
Full Data Avg
2937
3782
0.46
7.21
7.54
6.02
8.90
31.8
(1) F/M and MCRT assume an effective volume in ZO3A of 2.6 MG and an effective volume in Z04 of 1.8 MG,
as discussed with Clariant
13024s006
Clariant Data
5of5
10/28/99

APPENDIX C
SUMMARY OF STATISTICAL ANALYSES

CLARIANT BAT STUDY
STATISTICAL DATA
TOTAL PHOSPHORUS AND TOTAL NITROGEN
I
TP (1)
mg/L
Prob
TN (2)
mg/L
Prob
1
0.4
2%
2.56
2%
2
0.6
5%
3.9
4%
3
0.62
7%
4.75
7%
4
0.64
10%
4.96
9%
5
0.75
12%
5.04
11
6
0.85
15%
5.41
13%
7
0.85
17%
5.61
15%
8
0.9
20%
5.83
17%
9
0.9
22%
6.09
20%
10
0.95
24%
6.23
22%
11
0.98
27%
6.3
24%
12
1
29%
6.42
26%
13
1.03
32%
6.56
28%
14
1.05
34%
6.6
30%
15
1.05
37%
7.29
33%
16
1.1
39%
7.81
35%
17
1.11
41 %
8.57
37%
18
1.2
44%
8.66
39%
19
1.23
46%
8.98
41
20
1.28
49%
9.15
43%
21
1.35
51 %
10.9
46%
22
1.37
54%
11.79
48%
23
1.4
56%
13.03
50%
24
1.4
59%
13.6
52%
25
1.48
61%
13.61
54%
26
1.5
63%
13.94
57%
27
1.51
66%
14,05
59%
28
1.6
68%
14.1
61
29
1.6
71%
14.1
63%
30
1.7
73%
14.25
65%
31
1.75
76%
15
67%
32
1.84
78%
16.9
70%
33
1.9
80%
17.5
72%
34
2
83%
21.9
74%
35
2.01
85%
22.44
76%
36
2.25
88%
24.21
78%
37
2.3
90%
24.8
80%
38
2.55
93%
25
83%
39
2.7
95%
27.32
85%
40
3.4
98%
33.36
87%
41
33.63
89%
42
35.4
91
43
3805;
93%
44
41.32
96%
45
41.65 ` `
98%
46
47
48
49
50
(1) Total phosphorus data taken from 5/5/99-9/30/99
(2) Nitrogen data taken from 4/1/99-9/30/99
' Shaded data was calculated using NH3 rather than TKN (TKN<NH3)
13024s008
Prob_10_25
10/28/99

APPENDIX D
TREATABILITY ANALYSIS OF NUTRIENT CONTROL STRATEGIES

•
TREATABILITY ANALYSIS
OF NUTRIENT CONTROL STRATEGIES
CLAMANT CORPORATION
Prepared for:
Clariant Corporation
625 East Catawba Avenue
Mount Holly, NC 28120
Prepared by:
AWARE Environmental Inc.®
9305-J Monroe Road
Charlotte, NC 28270-1490
AEI Job No. N130-24
AEI Document No. 13024r001
October 1999

Section No.
TABLE OF CONTENTS
Description Page No.
TABLE OF CONTENTS i
LIST OF FIGURES ii
LIST OF TABLES ii
LIST OF APPENDICES ii
1.0 INTRODUCTION 1
1.1 Background and Objectives 1
1.2 Previous Pilot Study Results 3
1.3 Target Effluent Parameters 3
2.0 PILOT TESTING PROGRAM 6
2.1 Pilot System Description 6
2.2 Operating Conditions 6
2.2.1 Operation of Seasonal Nitrification/Denitrification 9
2.2.2 Treatability Evaluation of Phosphorus 9
2.3 System Operation And Monitoring 11
2.3.1 Unit Feeding 11
2.3.2 Aeration Cycling 13
2.3.3 Analytical 13
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4.0 PILOT STUDY CONCLUSIONS 34
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3.0 ANALYSIS OF TEST RESULTS 16
3.1 Data Summary 16
3.3.1 Nitrogen Removal Performance 16
3.1.2 Effect of Phosphorus on Performance 21
3.1.3 Overall Performance Summary 24
3.2 Estimation Of Achievable Nitrogen Concentrations 28
3.3 Estimation Of Achievable Phosphorus Concentrations 31
1
Final
October 1999

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LIST OF FIGURES
Figure No. Title Page No.,
2-1 Pilot System Flow Schematic 7
2-2 Influent Preparation Clariant Treatability Study 12
2-3 Diagram of Separate Stage Denitrification System 14
3-1 Unit 1: Weekly Average Effluent NH3-N,
NO3/NO2-N, Organic-N, and TN 17
3-2 Unit 3: Weekly Average Effluent NH3-N,
NO3/NO2-N, Organic-N, and TN 18
3-3 Unit 4: Weekly Average Effluent NH3-N,
NO3/NO2 N, Organic-N, and TN 19
3-4 Unit 2: Weekly Average Influent and Effluent
Phosphorus 22
3-5 Unit 2: Weekly Average Influent Total BOD5 and
Effluent Soluble BOD5 23
3-6 Unit 2: Mixed Liquor Particulate P/TSS 25
3-7 Statistical Analysis of Effluent - TN Unit 1 29
3-8 Statistical Analysis of Effluent - TP Unit 2 32
Table No.
LIST OF TABLES
Title Page No.
1-1 Summary of Conditions Simulated in
Treatability Study 2
1-2 Target Effluent Parameters 5
2-1 Unit Operating Parameters - Clariant BAT
Treatability Study 8
2-2 Analytical Schedule - Clariant BAT Treatability Study 10
3-1 Summary of Pilot Study Data - Conventional Pollutants 26
3-2 Nitrogen Removal Summary 27
3-3 Effluent Nitrogen Levels 30
LIST OF APPENDICES
Appendix A - Pilot Study Data
11
Final
October 1999

SECTION 1.0
INTRODUCTION
1.1 BACKGROUND AND OBJECTIVES
The Clariant Corporation (Clariant) operates two chemical plants in Mt. Holly, North Carolina
which are in closeproximity.Oneplant is the former Sandoz facility
(east plant) which has a
NPDES permit and discharges its treated wastewater to the Catawba River. The other plant is
the former Hoechst facility (west plant) which discharges its pretreated wastewater to the City
of Mt. Holly.
In conjunction with the BAT evaluation project, pilot treatability tests were conducted by
AWARE Environmental Inc.® (AEI) to evaluate BAT for continuing separate discharges and
BAT for the combined discharge. The objectives of the pilot treatability study were to
determine:
(1) process modifications to the existing Clariant WWTP required to achieve
denitrification and total nitrogen removal;
(2) the effluent total nitrogen limit which can be achieved through BAT; and
(3) the effluent residual total phosphorus which can be achieved while providing
adequate nutrients to achieve full permit compliance and additional nitrogen
removal.
The pilot system was designed to model the Clariant east site WWTP with process
modifications to achieve denitrification and total nitrogen removal. The study evaluated
treatment of the east site wastewater alone and treatment of the combined east and west site
�► wastewaters through the east site WWTP.
The conditions simulated in the pilot study are summarized in Table 1-1. The pilot study was
based on an east site influent flow of 1.4 MGD and a west site flow of 0.12 MGD. The 1.4
PIES
MGD flow rate corresponds to the current average east site flow. The 0.12 MGD west site
flow corresponds to maximum flow conditions. The pilot units were sized to provide the same
1 Final
October 1999

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Oft
Ara
TABLE 1-1
SUMMARY OF CONDITIONS SIMULATED
IN TREATABILITY STUDY
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6 1
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, o.,
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Influent flow (MGD)
1.4
1.52
Aeration basin effective volume (MG)
Z03
4.5
4.5
Z04
--
2.5
Total
4.5
7.0
Hydraulic residence time (days)
3.21
4.61
Aeration basin MLVSS (mg/I)
3,000
3,000
2
Final
October 1999

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hydraulic retention times as the full-scale system with the process modifications being
evaluated. Alternatives for achieving denitrification include aerator cycling to achieve anoxic
periods for denitrification, the use of a separate stage anoxic reactor and tertiary
denitrification. Supplemental carbon addition can be used as necessary to promote anoxic
conditions and denitrification.
1.2 PREVIOUS PILOT STUDY RESULTS
A previous pilot study had been performed to evaluate the ability of the Clariant east site
WWTP to meet revised NPDES permit limits for BOD5, which were proposed as of April 30,
1998. These proposed limits are significantly more stringent than the previous limits, and the
pilot study was performed to determine modifications to the wastewater treatment facility and
operations required to meet the proposed limits. This study evaluated treatment of the east site
wastewater alone and treatment of the combined east and west site wastewaters. From this
study it was determined that phosphorus addition to the Clariant wastewater is required to
achieve BOD5 removal. This determination agrees with the US EPA defmition of nutrient
addition as part of BAT treatment for OCPSF wastewaters. Therefore, the phosphorus limit,
which can be achieved, will be defined by the minimum effluent phosphorus residual required
to achieve the effluent BOD5 limits on a consistent basis.
This study determined that the operation of the Z03 aeration basin with improved mixing and
nutrient addition would provide adequate retention time to meet the proposed permit limits and
would achieve ammonia nitrogen conversion to nitrate nitrogen (nitrification) under spring and
summer conditions treating the east site wastewater alone. The study indicated that the both
the Z03 and Z04 basins would need to be operated to treat the combined east and west site
wastewaters.
1.3 TARGET EFFLUENT PARAMETERS
The primary objective of the pilot study was to determine the total nitrogen and phosphorus
limitations while achieving consistent compliance with the limits contained in the proposed
NPDES permit being developed by the North Carolina Department of Environmental and
3
Final
October 1999

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Natural Resources (NCDENR). The proposed limits are summarized in Table 1-2, and are
mass -based (lb/day) . In order to evaluate the performance of the pilot system, effluent
concentrations corresponding to these limits were calculated based on the average east site flow
of 1.4 MGD and the west site flow of 0.12 MGD. The resulting effluent concentrations are
included in Table 1-2. As indicated in Table 1-2, the proposed NPDES permit limits include
ammonia nitrogen limits. However, a primary objective of the study was to define the
minimum ammonia nitrogen concentration which is consistent with defining the total nitrogen
limits which could be achieved.
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4
Final
October 1999

TABLE 1-2
TARGET EFFLUENT PARAMETERS
Parameter
LimitsU (lb/day)
Target Concentrations') (mg/I)
Monthly Avg.
Daily Max.
Monthly Avg.
Daily Max
BOD5
476
1251
38
99
TSS
654
1979
52
156
Phenolics
3.9
7.8
0.31
0.62
NH3-N
657(3'
977(3)
5?(3)
77`'
Total N
NA
NA
(4)
`4)
(TKN + NO3-N + NO,-N)
Total P
NA
NA
(4)
(4)
Notes:
(1) Limits proposed as of April 30, 1998.
(2) Target concentrations calculated based on mass based limits and an estimated east site flow
of 1.4 MGD and west site flow of 0.12 MGD.
(3) Values indicated are based on NPDES limits being proposed as of April 30, 1998.
However, an objective of the study was to define the minimum effluent NH3-N which can
be achieved, as part of defining the minimum total nitrogen which can be achieved.
(4) The objective of the study was to determine the effluent TN and TP limits which can be
achieved.
5
Final
October 1999

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SECTION 2.0
PILOT TESTING PROGRAM
2.1 PILOT SYSTEM DESCRIPTION
A schematic of the pilot system is presented in Figure 2-1. The system was operated at Hydro
Analytical Laboratory (owned and operated by AEI) in Clemmons, North Carolina. The
system included four (4) continuous flow activated sludge units operated in parallel. Through
the use of four pilot units, several different operating conditions could be evaluated
simultaneously.
The activated sludge units were fed on a continuous basis using peristaltic feed pumps. Mixing
was provided by mechanical mixers, and aeration was provided using air pumps and air stones.
The units included integral clarifiers to allow settling and return of sludge on a continuous
basis to simulate the full-scale activated sludge system as closely as possible. The desired
temperature in each reactor was maintained by circulating a refrigerated bath through cooling
coils placed in each of the units. The pH was controlled in the units by feeding sodium
bicarbonate (NaHCO3) using automated pH control systems.
2.2 OPERATING CONDITIONS
The operating conditions for each of the units are summarized in Table 2-1. Units 1, 3 and 4
were operated to achieve denitrification in order to determine the effluent total nitrogen limits
which can be met. Effluent phosphorus was not a primary focus for these units. It was felt
that phosphorus requirements could be best defined through optimization of the full-scale
system and operation of a single reactor aimed at defining phosphorus criteria. The operating
objective for Unit 2 was to define the minimum effluent phosphorus level which can be
achieved while still providing adequate nutrients to the system. Since the operating strategy
for Units 1, 3 and 4 differed from that of Unit 2, they are discussed separately.
6
Final
October 1999

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INFLUENT SAMPLES
}
Fri
SUPERNATANT
AIR
REACTOR 1
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7.0 L/DAY
UNITS 1 & 2
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UNITS 3 & 4
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REACTOR 2
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REACTOR 3
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EFFLUENT EFFLUENT EFFLUENT EFFLUENT
CONTAINER CONTAINER CONTAINER CONTAINER
October 04. 1999 8:48:11 a.m.
Drawing: V: \N130\13023P01.DWG
FIGURE 2-1
PILOT SYSTEM FLOW SCHEMATIC
AEI PROJECT No. N130-23

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TABLE 2-1
UNIT OPERATING PARAMETERS
CLAMANT BAT TREATABILITY STUDY
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Conditions
East Early
East -Winter
East-
East &
East &
Spring
Summer
West
West Early
Early Summer
Summer
BAT Test
TN, TP
TP Only
TN, TP
TN, TP
TN, TP
Volume (1)
11.25
11.25
11.25
17.5
17.5
Flow (1/day)
3.5
3.5
3.5
3.8
3.8
HRT (days)
3.2
3.2
3.2
4.6
4.6
Temperature (°C)
18
10
25
18
18
pH
6.5-7.5
6.5-7.5
6.5-7.5
6.5-7.5
6.5-7.5
DO (mg/1)
1.5-5.0m
2-6
1.5-3.0 (1)
1.5-5.0
1.5-5.0(1)
Aeration Cycles
Oxic (hr)
6
Continuous
6
--(2)
6
Anoxic (hr)
2
N/A
2
--(2)
2
MLVSS (mg/1)
3000
3000
3000
3000
3000
Influent Waste Characteristics
Variable
Constant
Variable
Variable
Variable
Notes:
(1) Aeration cycled on and off to achieve denitrification. D.O. less than 1.0 mg/1 during non -
aerated (anoxic) cycle periods. Allowable oxic D.O. range was originally 1.5-3.0 mg/1 but
was later modified to 1.5-5.0 mg/1.
(2) Separate stage anoxic treatment.
PEI
8
Final
October 1999

2.2.1 Operation of Seasonal Nitrification/Denitrification
Units 1, 3 and 4 simulated spring and summer conditions and utilized aerator cycling to
achieve both biological nitrification and denitrification. These units were used to define
the total nitrogen limits which can be achieved. Nitrogen removal was not evaluated
under winter conditions, since the NCDENR BAT requirements for nitrogen removal
are under summer conditions only. As indicated in Table 2-2, the units were set up
with an oxic (aerated) period of 6 hours, followed by an anoxic period of 2 hours with a
total cycle time of 8 hours. The operating plan for Units 1, 3 and 4 included
monitoring the performance of the anoxic and oxic cycles closely and to implement
modifications, as needed, to optimize the system performance and defme the nitrogen
limits which can be achieved. Units 1 and 3 simulated treatment of the east site
wastewater alone, using the Z03 aeration basin. Unit 1 simulated spring operating
conditions (18°C mixed liquor temperature) and Unit 3 simulated summer conditions
(25°C mixed liquor temperature).
Unit 4 simulated treatment of the combined east and west site flows under spring
conditions. This required operation of both the Z03 and Z04 aeration basins. As
indicated in Table 2-1, Unit 3 was later modified to treat the combined east and west
site flows under spring conditions using a separate stage anoxic reactor.
mr, Sufficient phosphorus was added to Units 1, 3 and 4 so as to prevent any nutrient
limitation. Phosphoric acid (H3PO4) was fed directly to each unit to satisfy nutrient
requirements.
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2.2.2 Treatability Evaluation of Phosphorus
The critical condition to defme phosphorus requirement is during winter operation.
Unit 2 simulated treatment of the east site wastewater alone under winter conditions.
This unit was operated to determine the effluent phosphorus limit which can be met
while still providing adequate dissolved ortho-phosphate for optimum bacterial growth
and BOD5 removal. Since the treatment kinetics are normally slower and nutrient
9
Final
October 1999

MCI
TABLE 2-2
ANALYTICAL SCHEDULE - CLARIANT BAT TREATABILITY STUDY
�: 5 j.}3 .Location
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(East and East/West)
BOD5
COD
Total P
TKN
NH3-N
NO2/NO3-N
pH
2/wk
2/wk
2/wk
2/wk
2/wk
2/wk
6/wk
1/2 wk
1/2 wk
1/2 wk
1/2 wk
1/2 wk
1/2 wk
1/wk
Aeration Basin
MLSS(3)
MLVSS(3)
DO(3) (4)
ORP(4)
pH(3) (4)
Temperature
02 Uptake()
SVI(3)
SVI/TSS
NH3-N(3) (4)
NO2/NO3-N(3) (4)
2/wk
2/wk
2/day
6/wk
2/day
Daily
3/wk(2)
3/wk(2)
1/wk
2/wk(1)
2/wk(1)
2/wk
2/wk
2/day
NA
2/day
Daily
3/wk(2)
3/wk(2)
1/wk
2/wk(1)
2/wk(1)
Effluent
Soluble BOD5
Total BOD5
Soluble CBOD5
TSS
PO4-P Soluble
TP
TKN
NH3-N
NO2/NO3-N
Phenolics
Alkalinity
3/wk(2)
3/wk(2)
1/wk
3/wk
3/wk
3/wk(2)
3/wk(2)
3/wk(2)
3/wk(2)
1/wk
1/wk
3/wk(2)
3/wk(2)
l /wk
3/wk
3/wk
3/wk
3/wk
3/wk
3/wk
2/wk
1/wk
Note:
(1) 2/wk until cycle period, DO and ORP adjusted, then 1/wk. Two samples collected during aerobic
period, one at the beginning and one at the end.
'=' (2) 1/wk until cycle period, DO and ORP are adjusted, then 3/wk.
(3) Monitor during aerobic period.
(4) Monitor during anoxic period.
10
Pal
Final
October 1999

fin
demands are normally highest under winter conditions, the unit was operated under winter
FL, conditions. The unit did not include anoxic cycling since denitrification is not required
under winter conditions.
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The operating strategy for Unit 2 was to feed the unit a consistent waste stream over a
period of several weeks. The phosphorus addition to the system was initially set at a
level which would prevent any nutrient limitation on the system. The phosphorus
addition was then gradually reduced in an effort to determine a critical residual
phosphorus level at which system performance begins to deteriorate.
2.3 SYSTEM OPERATION AND MONITORING
2.3.1 Unit Feeding
Daily composite samples of the east site and west site WWTP influent were collected
by Clariant personnel for feed to the pilot units. The east site samples were collected
just upstream of the primary clarifiers and the west site samples were collected from the
equalization tank discharge.
0.1
Initially, for the feed to Units 1, 3 and 4, the daily composite samples were combined
to make weekly composite samples for the pilot units. This was done to allow more
consistent control of the oxic and anoxic cycling using the pilot apparatus. Later during
the study the individual daily composite samples were used as daily feed samples to the
pilot units in order to observe impacts of the daily variations in influent composition.
Figure 2-2 presents a schematic of the feed preparation process. Unit 4 treated the
combined east and west site flows. As indicated in Table 2-1, Unit 3 originally treated
the east site waste alone, but was later modified to treat the combined east and west site
flows. For these units the east and west site composite samples were blended in
proportion to the full-scale flow. Prior to feeding, the influent samples for each of the
units were settled to simulate primary clarification.
11 Final
October 1999

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STEP 1
BLENDING
EAST PLANT
SAMPLE
5 GALLONS
WEST PLANT
SAMPLE
1 GALLONS
9.5L
REMAINDER
(APPROX. 9.4L)
814ML
1
UNIT 1 & 2 (CONTROL) UNIT 3 & 4 (TEST)
SETTLING CONTAINER SETTLING CONTAINER
NOTE:
SHAKE UP EACH SAMPLE THOROUGHLY BEFORE BLENDING. ALSO MIX WELL AFTER BLENDING.
STEP 2
SETTLING
UNIT 1 & 2 (CONTROL) UNIT 3 & 4 (TEST)
SETTLING CONTAINER SETTLING CONTAINER
NOTE;
SETTLE FOR APPROXIMATELY 60 MINUTES.
STEP _3
DECANTING
DISPOSABLE
PIPETTE
DECANT PUMP DECANT PUMP
UNIT 1 & 2 (CONTROL)
SETTLING CONTAINER
CLAMP TO
SIDE OF
REACTOR
NOTE;
USE DECANT PUMP TO DRAW OFF SUPERNATANT
BEING CAREFUL NOT TO DRAW IN SLUDGE.
STEP 4
FEEDING
7.00 L
UNIT 1 & 2
FEED CONTAINER
SAMPLE
STORAGE
CONTAINER
(> 10L)
%/
UNIT 3 & 4 (TEST)
SETTLING CONTAINER
7.60 L
UNIT 3 & 4
FEED CONTAINER
BE CAREFUL
TO AVOID
DRAWING UP
SLUDGE
SAMPLE
STORAGE
CONTAINER
(> 10L)
NOTE;
ADD THE EXACT AMOUNT INDICATED TO THE FEED CONTAINERS. THE LEFT OVER SAMPLE CAN BE USED
FOR INFLUENT SAMPLE ANALYSIS.
FIGURE 2-2
INFLUENT PREPARATION
CLARIANT TREATABILITY STUDY
October 04. 1999 8:50:18 a.m.
Oro sing: V: ` i130\13022P02.DWG
AEI PROJECT No. N130-23

Me,
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were used as feed to Units 1, 3 and 4 in order to reduce the variability in waste loads
and to allow the DO to be controlled more closely. Following this period, the oxic DO
was controlled less stringently at a level of 1.5 to 5 mg/1. The daily influent composite
samples were used as feed.
For Unit 2 a composite sample was developed from several of the daily composites,
and was fed to the unit over a period of several weeks. This was done to provide a
consistent feed composition in order to evaluate the effects of incremental reductions in
phosphorus dosage on system performance.
2.3.2 Aeration Cycling
The anoxic cycling in Units 1, 3 and 4 was accomplished using cycle timers connected
to the air pumps. The DO and ORP in the units was measured at periodic intervals
before, during and after the anoxic cycle. The air flow was adjusted in order to
maintain the oxic phase DO within a specified range. This was done to ensure that
anoxic conditions would not be prevented from occurring due to high DO at the
beginning of the anoxic cycle. During the first six weeks of the study the oxic phase
DO was controlled at 1.5 to 3 mg/l. During this period weekly composite samples
As indicated in Table 2-1, Unit 3 was later modified to include a separate denitrification
stage. A schematic of Unit 3 with the separate denitrification stage is included in
0.1 Figure 2-3. As shown in Figure 2-3, the unit included a separate clarifier. Influent,
return sludge and mixed liquor recycle were fed to the anoxic stage using peristaltic
pumps.
2.3.3 Analytical
The analytical schedule is presented in Table 2-2. All of the analyses were performed
by Hydro Analytical Laboratories. The monitoring included monitoring of DO and
ORP at intervals prior to, during and after the anoxic cycle in order to assist in
adjusting the air flow rates to promote denitrification.
Fig
13
Final
October 1999

B l B B B B B B B B B B B B B ] B
INFLUENT
RECYCLE PUMP
7.6 L/d
v
N
ANOXIC
STAGE
AIR
OXIC
STAGE
8
CLARIFIER
RAS PUMP
3.8 L/d
L
1EFFLUENT
r
DIAGRAM OF SEPARATE STAGE
DENITRIFICATION SYSTEM
SCALE AS NOTED
DATE SEPT. 1998
APPROVED BY :
DESIGNED BY :
DRAWN BY: A.B.K.
REVISED
Of.li)ber 04. 199'/ 8.57. SO n.rn.
Iltnwutri. V. \N1,in\1 S(1241 I)I.OW[;
PROJECT NUMBER
N130-24
A RD. ��•mc
NG NO.
9305-J MONROEFIGURE 2-3
CHARLOTTE, NC 28270

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The effluent samples were collected from the effluent composite collection containers.
Initially, the effluent sample collection procedure included mixing of the effluent
containers prior to pouring the sample into the effluent sample bottles, in order to
ensure that samples were homogeneous. However, due to mechanical and hydraulic
limitations inherent with pilot systems, the effluent TSS values were higher and more
variable than what would be expected in a full-scale system. The sample collection
procedure was modified to minimize carryover of settleable solids into the effluent
samples. Starting September 21, 1998 the collection procedure was modified so that
supernatant from the effluent containers was decanted off and the excess settleable
solids in the effluent containers were not included in the effluent samples. This
provided effluent TSS levels which were more representative of the full-scale Clariant
WWTP.
15
Final
October 1999

SECTION 3.0
ANALYSIS OF TEST RESULTS
, , 3.1 DATA SUMMARY
The primary objective of Units 1, 3 and 4 was to determine the effluent total nitrogen (TN)
concentrations which can be achieved under spring and summer conditions using BAT
treatment. The objective for Unit 2 was to define the minimum phosphorus level required to
mn achieve adequate BOD5 removal.
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3.3.1 Nitrogen Removal Performance
Figure 3-1 presents a chronology of the weekly average effluent organic N, NH3-N,
NO3/NO2-N and TN for Unit 1. Figures 3-2 and 3-3 present similar chronologies for
Units 3 and 4. Organic N was calculated as TKN minus NH3-N. All of the pilot study
data are included in Appendix A. Units 1, 3 and 4 performed similarly. The effluent
NH3-N values were typically less than 3 mg/1 in all three units. These data indicate that
biological nitrification was achieved under the conditions of this study. The nitrate -
nitrite data shows that denitrification occurred and the anoxic cycling did not appear to
have any adverse affect on nitrification performance.
As indicated in Figure 3-1, the anoxic cycling was initiated on August 21. Mechanical
adjustments, including installation of floating covers, were made to the pilot units
during the week of August 24. As indicated in Figures 3-1 through 3-3, the effluent
R., NO3-N dropped in Units 1, 3 and 4 following the initiation of anoxic cycling, indicating
denitrification was achieved. Effluent NO3-N values in Units 1, 3 and 4 were typically
in the range of 1 to 3 mg/1, with the exception of one period in which anoxic cycling
was temporarily discontinued in Unit 3. In comparing Unit 4 with the other two units,
"m there was no adverse effect of the west site wastewater on the nitrogen removal
performance.
MA
,M 16 Final
October 1999

20 -
0)
E
0
15-
L
d
u
0
U
10
8/3/98
Figure 3-1
Unit 1: Weekly Average Effluent NH3-N, NO3/NO2-N, Organic-N, and TN
8/13/98
8/23/98
9/2/98
9/12/98
Date
- - Organic-N
--F— NH3-N
—�-- NO3/NO2-N
—TN
9/22/98
10/2/98
10/12/98 10/22/98
25577

60
50
40
E
0
30
u
0
U
20
10
0
Figure 3-2
Unit 3: Weekly Average Effluent NH3-N, NO3/NO2-N, Organic-N and TN
•
, ~
`
'•
M
4
Discontinued
Started Anoxic Anoxic Cycling
Cycling (8/21) (8/31'918)
Anoxic Cycling
(9/9-9/25)
Separate Stage Anoxic (9/25)
. /
• - - - -
, ,
•
, /
►•
*`
`
•
►
- + - Organic-N
--�— NH3-N
NO3/NO2-N
—>�--
--ITN
r
8/3/98 8/13/98 8/23/98 9/2/98 9/12/98 9/22/98 10/2/98 10/12/98 10/22/98
Date
25577

1 I 1 1 $ 1 1 1 J 1 11 1 I 1 ] 3. i 1 I ]
30 -
Figure 3-3
Unit 4: Weekly Average Effluent NH3-N, NO3/NO2-N, Organic-N, and TN
25 -
20 -
J
ith
C
0
15-
h.
4.
C
0
C
0
0
10-
5
i♦
•
♦
♦
♦
♦
o
•
•
•
•
II
Started Anxoic Cycling (8/21)
III
•%
• vi
• •
• •
•
•
•
•
•
•
IN
- - -
- • - Organic-N
--�—NH3-N
--at— NO3/NO2-N
—)( TN
1.------______e o
•
-
8/3/98
25577
8/13/98
8/23/98
9/2/98
9/12/98
Date
9/22/98
10/2/98
10/12/98
10/22/98

fxl
Pitt
faq
aim
modifications.
In Unit 3 (Figure 3-2), the anoxic cycling was discontinued during the period of August
31 through September 8. This was done to verify that NO3-N removal was actually
occurring in the reactor and not in the effluent collection container, and to verify that
the analytical method being used would accurately detect increases in effluent NO3-N.
As expected, the Unit 3 effluent NO3-N increased significantly during this period.
Following re -initiation of' the anoxic cycling on September 9, the effluent NO3-N
dropped to the 1 to 3 mg/1, range which was comparable to the other units.
The conventional approach to implement denitrification on a full scale system is
through the use of a separate denitrification stage. Therefore, on September 25 Unit 3
was modified to include a separate denitrification stage. This was done to verify that
similar results could be obtained using a separate denitrification reactor. As shown in
Figure 3-3, the unit performance was similar or slightly better with the separate stage
anoxic reactor.
From the initiation of the study through September 25, the oxic period DO in Units 1, 3
and 4 was controlled closely with a target of 1.5 to 3 mg/1, in order to ensure that high
DO levels at the beginning of the anoxic period would not prevent anoxic conditions
from occurring. Weekly average feed samples were fed during this period. From
September 25 through the end of the study, the oxic DO was controlled less stringently
at 1.5 to 5.0 mg/1, and daily composite feed samples were fed to the units. This was
done to verify that daily variations in feed strength and less than optimal DO control
would not have a significant adverse effect on performance. In reviewing Figures 3-1
through 3-3 there was no apparent adverse effect from the feed and DO control
The results of these tests indicated that there was a significant refractory (non-
...9 biodegradable) organic nitrogen concentration in the wastewater. In reviewing the
effluent data from Units 1, 3 and 4 during the period in which denitrification was
achieved, the primary component comprising the total nitrogen was organic nitrogen.
20 Final
October 1999

n
Mgt
As indicated in Figures 3-1 through 3-3, in Units 1, 3 and 4 there was a residual
refractory organic N of 5 to 12 mg/1 which occurred regardless of the BOD5 removal
and nitrification performance.
3.1.2 Effect of Phosphorus On Performance
As discussed earlier, the phosphorus dosage to Unit 2 was gradually reduced during the
study to determine the minimum residual phosphorus threshold to prevent nutrient
' limitation. Units 1, 3 and 4 were fed excess phosphorus to ensure that nitrogen
removal would not be inhibited by phosphorus limitation and were not evaluated with
regard to phosphorus limitation. The influent total phosphorus and effluent total and
ortho phosphorus for Unit 2 are presented in Figure 3-4.
piq
As indicated in Figure 3-4, the effluent total and ortho phosphorus gradually declined
along with the decline in influent phosphorus feed. The effluent phosphorus levels
were greater than the influent levels during part of the study due to the gradual release
of phosphorus which had accumulated in the sludge solids.
Figure 3-5 presents a chronology of the Unit 2 influent and effluent BOD5. As
indicated in Figure 3-5, the reduction in phosphorus addition over the course of the
study did not result in an increase in effluent BOD5 until the last week of the study
when an increase in effluent BOD5 occurred. During the last week of the study the
effluent soluble BOD5 increased from less than 10 mg/1 up to approximately 30 mg/l.
'i This coincided with an increase in influent BOD5 and the lower phosphorus addition.
The influent phosphorus addition was gradually reduced and was discontinued on
October 17. There was a residual phosphorus in the mixed liquor solids, soluble and
particulate phosphorus, which was still being released in the effluent at a low level
through the end of the study. The soluble phosphorus release appeared to have
21
Final
October 1999

1 1 1 $ 111M1M1111
25
20
J
03
E
C
• 15
L
C
0
o
C
0
V
L 10
0
s
a
0
O
t
a
0
Figure 3-4
Unit 2: Weekly Average Influent and Effluent Phosphorus
- 9< - Influent TP
—o— Effluent TP
—is— Effluent PO4-P
M In
do
9<
ce 4, e
�J J,0
4\ 4,N\e N
Date
25577

Influent Total BOD5 (mg/L)
25577
Figure 3-5
Unit 2: Weekly Average Influent Total BOD5 and Effluent Soluble BOD5
1800 - 70
1600 —
1400 —
1200 --
1000 —
800 —
600 —
400 —
200 - -
--R—Influent Total BOD5
Effluent Soluble BOD5
MUER
-- 60
50
- J
E
--40p
m
. 0
— 30 11
m
— 20W
-- 10
0- E t t f -0
e
,\00 ��0� O�O� 0�00 cob cp0 ,,,
O�� O�� '\O\O��
Date

r1
11
tamp
owl
rag
stabilized at approximately 0.1 to 0.5 mg/1. Effluent total phosphorus during the period
from October 17 through the end of the study had a 95th percentile effluent level of 1.5
mg/l.
The phosphorus availability to the mixed liquor bacteria is typically gauged by the
effluent ortho phosphorus concentration. However, based on the low effluent ortho
phosphorus levels, it is apparent that much of the phosphorus demand was being
satisfied by phosphorus already accumulated in the sludge solids. As another measure
of phosphorus availability, the phosphorus content of the mixed liquor was measured.
Figure 3-6 shows the decrease in the phosphorus content of the mixed liquor solids over
the period of study as phosphorus addition was reduced. The system continued to show
no reduction in performance with mixed liquor phosphorus levels as low as 0.005 g P/g
MLSS.
3.1.3 Overall Performance Summary
Table 3-1 summarizes the performance of the pilot units and the full-scale facility in
conjunction with the pilot study. As shown in Table 3-1, the effluent total and soluble
BOD5 and phenolics concentrations for all of the pilot units were below the target
concentration limits and consistent with full-scale performance. Due to mechanical and
hydraulic limitations which are inherent with pilot systems, the pilot unit effluent TSS
values were higher and more variable than in the full-scale system. As a result, the
pilot unit total BOD5 values are skewed slightly higher than what would occur with
clarification performance equivalent to the full-scale system.
The nitrogen removal performance of Units 1, 3 and 4 was very similar. As indicated
in Table 3-2, Units 1, 3 and 4 achieved approximately 77 to 81 percent removal of
TKN, 92 to 94 percent removal of NH3-N and 72 to 79 percent removal of total
nitrogen. Effluent total nitrogen concentrations of 10 to 16 mg/1 were achieved in
Units 1, 3 and 4.
24
Final
October 1999

3. 3 1 1 fl 8 1 3 3 1 i 3 1 i 1 1 3
1
Figure 3-6
Unit 2: Mixed Liquor Particulate P/TSS
10/12/98
Date
25577

Part
rim
MEI
attic
r,
TABLE 3-1
SUMMARY OF PILOT STUDY DATA — CONVENTIONAL POLLUTANTS
f {��f���p� p�
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Effluent BOD5 (mg/1)(')
.
Total
19
35
24
11
27
38
99
Soluble
10
14
8
8
Effluent TSS (mg/1)(1)
38
62
49
21
11.4
52
156
Effluent Phenolics (mg/1)(1)
0.17
0.26
0.20
0.12
0.10
0.31
0.62
Note:
(1) All data are averages for period of August 31 - October 18, 1998.
(2) East site WWTP average effluent data for August 31 - October 18, 1998.
(3) Target concentrations calculated based on proposed NPDES limits and an east site flow of 1.4
MGD and a west site flow of 0.12 MGD.
gel
26
Final
October 1999

SRI
ints
Mat
calla
Pet
Aar
f1
Fogi
TABLE 3-2
NITROGEN REMOVAL SUMMARY
� .„..�.: :-
i ..�r ^Y. y�y . u� '1se
1 b :* ., ��';` C 11Y sT .4L•"yi✓.. �^.,
�It �t °
£� r .3.� � r1 .f _'
lM►�uY�'.,4 3 ' w,
�iT�, � �
�-,:5 /''�:
P.Y ,FL i • -- ..
�,
�;Ii‘ - -r
� ,.' '"Y
,h Y !_3
".�L :4, _ �` Sit•
�m��4-�L=�
fi � Iqf �.
iS . L{�r
.k�'i�'Y "': µ>•.Fi:a2
���Fu_Scale
• p ,(y .fy. 1. W..
_A.� �i._._. "lri.
�''VT
K
Influent
45.9
60.2
40.25
42.6
Effluent
10.4
24.8
9.3
8.2
% Removal
77%
59%
77%
81%
NH3-N
Influent
35.4
38.6
25
34.1
27.8
Effluent
2.7
16
1.4
2
14
% Removal
92%
59%
94%
94%
50%
NO3-N
Effluent
2.7
14.8
1.9
2.2
Organic N
Influent
10.5
21.6
15.25
8.5
Effluent
7.7
8.8
7.9
6.2
% Removal
27%
59%
48%
27%
Total N
Influent
48.2
63.4
42.3
49.9
Effluent
13.3
39.6
11.2
10.3
% Removal
72%
3 8 %
74%
79%
Note:
(1)
All data are averages for period of August 31 - October 18, 1998 except Unit 3
nitrogen data which are averages for the September 14 - October 18, 1998.
All units in mg/1 except percent removals.
(2) East site WWTP average effluent data for August 31 - October 18, 1998.
27 Final
October 1999

MEP
Pal
AM
MO
OP
A significant portion of the effluent total nitrogen was composed of refractory organic
nitrogen. The refractory organic nitrogen levels appeared to be relatively consistent
despite the excellent BOD5 and NH3-N removal performance.
3.2 ESTIMATION OF ACHIEVABLE NITROGEN CONCENTRATIONS
Total nitrogen (TN) is comprised of organic nitrogen, NH3-N and NO3-N. Units 1, 3 and 4
achieved very good NH3-N and NO3-N removal. As discussed earlier, most of the residual
total nitrogen in the treated effluent was composed of refractory organic nitrogen. In order to
determine the TN which would be discharged from a full-scale system based on the results of
these pilot studies, a statistical analysis of the steady state operating data was conducted. The
statistical data for Unit 1 east plant is presented in Figure 3-7. Consistent with the EPA
OCPSF procedure, the 95th percentile concentration was selected as maximum month. The
results of the statistical analysis for Units 1, 3 and 4 are presented in Table 3-3. This indicates
the baseline level of treatment that could be expected if the wastewater treatment plant is
upgraded to achieve nitrification and denitrification. Subsequent phases of this investigation
will need to be conducted to determine if this level of treatment is cost effective.
It is currently anticipated that Clariant will not combine the East and West plants. Therefore,
pm
the effluent levels which could be expected from the up -grade of the treatment plant to include
biological nitrification and denitrification for the east plant is 19 mg/1 TN as shown by the
performance of Unit 1. To be consistent with the OCPSF effluent limits for the plant, mass -
based limits using the long-term average flow of 1.42 MGD are recommended. This results in
a recommended baseline of 225 lbs/day TN.
28
Final
October 1999

1
1
1
1
3
1
1
1
1
1
1
20
FIGURE 3-7
Statistical Analysis of Effluent— TN Unit 1
•
I
•
.
1.1
•
y
•
•
0.01 0.4
5 10 20 30 40 50 60 70 80 90 95 99 99.9 99.99
PROBABILITY (%) Agamr-

RIM
Mot
peci
r,
Mit
Ott
TABLE 3-3
EFFLUENT NITROGEN LEVELS
•*-' .
�d.+t i .r fi wl" . *t 1 ) l,
u.�
,,. -'
,(a
'J,'-• , S � i
s'?�a':
r. -7l„.�'
'
East and West Plant
Early Summer
Conditions
: y�+ E. 4f ,1�• �
!. s+k._. kr
�/'
East and West Plant
Early Summer
Conditions
Conditions
East Plant
Early Summer
Conditions
Operation
Integral Anoxic
External Anoxic
Integral Anoxic
Baseline TN (mg/1)
19
16
18
30
Final
October 1999

Pon
1
wig
order to have adequate dissolved ortho-phosphate available for biological treatment. The
3.3 ESTIMATION OF ACHIEVABLE PHOSPHORUS CONCENTRATIONS
Figure 3-4 shows the Unit 2 influent total phosphorus and effluent total and ortho phosphorus
over the period of study. As discussed earlier, the phosphorus addition was gradually
decreased. The effluent phosphorus gradually declined along with the influent phosphorus
addition. During some periods, the effluent phosphorus was greater than the influent
phosphorus. As illustrated in Figure 3-6, this is the result of phosphorus stored in the sludge
solids being gradually released.
The lowest effluent concentrations were achieved after the phosphorus addition was
discontinued altogether on October 17, 1998. It appears that during this period the phosphorus
demand was being satisfied by phosphorus stored in the sludge from the previous phosphorus
feeding. There was a gradual release of the stored phosphorus which contributed to the
effluent phosphorus. This period represents the absolute minimum effluent phosphorus
residual which could be achieved.
A statistical analysis of the effluent phosphorus values for Unit 2 over the last period of the
study is presented in Figure 3-8. The 95th percentile total phosphorus concentration consistent
with anticipated monthly average winter conditions was 1.5 mg/l. The average effluent TSS
over the period was 60 mg/1, which slightly exceeded the maximum allowable monthly average
TSS limit for the Clariant east site WWTP of 56 mg/l.
The pilot unit results indicate that the WWTP can achieve a minimum monthly average total
phosphorus concentration of 1.5 mg/l. For comparison the optimized full-scale WWTP had an
effluent total phosphorus concentration of 2.6 mg/1 while using lime for pH control, which
results in greater phosphorus content in the TSS. Since NaHCO3 was used for pH control in
the pilot units, the effluent TP concentrations achieved in the pilot appear to be lower than can
be achieved in long term full-scale operation. When lime is used for pH control, this
significantly reduces the phosphorus bioavailability, requiring higher effluent TP residuals in
31
Final
October 1999

1
1
1
1
1
1
1
1
1
1
1
4.0
30
cn
E
0
H
20
4-
4-
1
.0
0
0.01
0.4
FIGURE 3-8
Statistical Analysis of Effluent— TP Unit 2
6-
•
•
•
5 10 20 30 40 50 60 70 80
PROBABILITY (%)
•
411.
90 95
PIM
99
99.9
99.99

AEI
foci
PPR
SOIR
flufl
higher percentages of particulate phosphorus in the sludge solids occurs due to formation of
calcium phosphate precipitates and adsorption of phosphorus to gypsum (CaSO4) and other
precipitates formed as a result of the lime addition. This will increase the phosphorus content
of the effluent TSS which will increase the effluent total phosphorus. To be consistent with the
OCPSF limits for the Clariant plant, it is recommended that the phosphorus limit be maintained
on a mass basis based on the 2.6 mg/1 TP concentration. At a long-term average flow of 1.42
MGD, this is equivalent to 30.8 lbs/day TP.
33 Final
October 1999

or!
SECTION 4.0
PILOT STUDY CONCLUSIONS
Based on the pilot study results the following conclusions are presented:
1. With adequate phosphorus addition and mixing, nitrification can be achieved under spring,
summer and fall conditions.
2. Denitrification can be achieved in the treatment of the Clariant wastewater and
denitrification does not adversely impact nitrification.
3. Daily fluctuations in influent loads did not significantly impact nitrification, denitrification
or overall performance of the pilot units.
4. Maintenance of aeration basin DO levels in the range of 1.5 to 5.0 mg/1 during the oxic
phase should allow anoxic conditions and denitrification to be established in anoxic phase.
5. Addition of the Clariant West Site wastewater does not hinder nitrogen removal, and may
improve system performance.
Hal 6. Aerator cycling and use of a separate stage anoxic reactor produced similar results in the
pilot study. However, it is AEI's opinion that in full-scale application, the separate stage
anoxic treatment will provide superior performance and ease of operation.
7. Through nitrification and denitrification, the effluent total nitrogen levels can be
significantly reduced from current levels. Total nitrogen removals averaged 72 to 79
percent in the pilot units. However, a significant portion of the effluent total nitrogen is in
the form of refractory organic nitrogen.
8. The total nitrogen and phosphorus effluent limits which can be achieved are affected by the
effluent TSS which can be achieved.
9. Based on the pilot results and the historical average effluent TSS levels from the full-scale
WWTP, the long-term average total phosphorus concentration which can be achieved with
the existing BAT facility is estimated at 2.6 mg/1. The recommended long term TP limit is
30.8 lbs/day.
10. Based on pilot results the anticipated effluent TN which could be achieved with the
installation of a nitrification/denitrification system is 225 lbs/day.
13024r001
34
Final
October 1999

APPENDIX A
PILOT STUDY DATA

1 l i J l
CLARIANT BAT TREATABILITY STUDY
SUMMARY OF WEEKLY AVERAGE DATA
UNIT 1
Period
BOD5
MLVSS
F/M
TSS
TKN
NH3-N
NO3-N
Influent
Effluent
SVI/TSS
Eff
Inf
Eff
%
Removed
Inf
Mix Liq
Eff
%
Removed
Inf
Mix Liq
Eff
TBOD
TBOD
SBOD
SCBOD
' Oxic
Anoxic
Aug 10-16
1400
48
14
2875
0.15
175
42.0
17.9
57%
26.2
7.0
73%
0.04
Aug 17-23
690
21
4
2
3108
0.07
100
53.8
11.2
79%
35.3
1.8
95%
0.34
17
Aug 24-30
392
37
29
4
3393
0.04
153
24
65.8
10.6
84%
64.4
4.2
94%
0.01
4.0
2.5
12.3
Aug 31-Sep 6
2850
60
40
26
2914
0.31
35
69
64.2
18.5
71%
59.5
9.0
11.6
81%
1.50
7.8
5.8
1.7
Sep 7-13
972
28
6
<2
3275
0.09
57
110
49.5
12.8
74%
41.5
2.9
<1
98%
3.50
5.5
2.0
3.2
Sep 14-20
575
7
2
2
2552
0.07
28
32
34.8
6.9
80%
23.8
2.0
<1
96%
1.50
7.3
4.6
1.6
Sept. 21-present: Effluent collection procedure modified to reduce TSS in effluent samples.
Sep 21-27
404
5
2
2
2686
0.05
12
10
46.0
7.9
83%
34.4
<1
< 1
97%
3.0
7.7
2.3
2.0
Sep 28-0ct 4
755
11
9
2
2858
0.08
1
2
40.6
7.0
83%
29.6
1.7
1.2
96%
1.5
5.7
2.2
4.0
Oct 5-11
1367
16
8
4
3196
0.13
15
37
40.6
9.2
77%
23.6
<1
1.1
95%
2.5
6.7
2.2
2.5
Oct 12-19
762
8
6
2
3151
0.08
11
8
10.6
8.5
1.9
1.5
5.3
3.3
4.2
Avg. Sep 21-Oct 18
822
10
6
3
2973
0.08
10
14
42.4
8.7
81%
29.2
3.1
1.3
96%
2.1
6.3
2.5
3.2
Avg. Aug 31-0ct 18
1098
19
10
6
2947
0.12
23
38
45.9
10.4
78%
35.4
3.7
2.7
94%
2.1
6.6
3.2
2.7
Period
Total Nitrogen
Organic N
Eff Part N
(Estimated)
Eff. Sol
Org. N
(Estimated)
Total Phosphorous
0-PO4
Influent
BOD:N:P
Inf
Eff
%
Removed
Inf
Eff
%
Removed
Influent
Nut (PO4)
Inf+Nut
Eff Total
P
Removed
Eff PO4
PO4
Removed
Aug 10-16
42.0
17.9
57%
15.8
11.0
31%
22.0
22.0
18.13
100:3:1.6
Aug 17-23
54.1
28.2
48%
18.5
9.4
49%
1.00
19.3
20.3
23.8
-3.5
16.0
3.25
100:8:2.9
Aug 24-30
65.8
23.0
65%
1.4
6.5
-362%
1.25
19.3
20.5
15.8
4.8
10.0
9.25
100:17:5.2
Aug 31-Sep 6
65.7
20.2
69%
4.7
6.9
-48%
0.30
9.6
9.9
21.2
-11.3
13.2
-3.59
100:2:0.3
Sep 7-13
53.0
15.9
70%
8.0
11.8
-47%
0.64
9.6
10.3
24.8
-14.5
17.3
-7.66
100:5:1.1
Sep 14-20
36.3
8.5
76%
11.0
5.9
46%
0.60
9.6
10.2
9.1
1.1
8.9
0.78
100:6:1.8
Sept. 21-present: Effluent collection procedure modified to reduce TSS in effluent samples.
Sep 21-27
49.0
9.9
80%
11.6
6.9
41%
1.1
1 5.8
0.60
9.6
10.2
9.7
0.5
7.1
2.54
100:12:2.5
Sep 28-0c14
42.1
11.0
74%
11.0
5.8
47%
0.3
5.6
0.59
9.6
10.2
9.3
1.0
7.9
1.71
100:6:1.4
Oct 5-11
43.1
11.7
73%
17.1
8.1
52%
4.0
4.1
0.48
9.6
10.1
14.4
-4.3
12.0
-2.37
100:3:0.7
Oct 12-19
14.8
8.7
0.8
7.9
7.2
9.8
7.7
Avg. Sep 21-Oct 18
44.7
11.9
75%
13.2
7.4
47%
1.6
5.8
0.56
9.0
10.2
10.8
-0.9
8.7
0.6
100:5:1.2
Avg. Aug 31-Oct 18
48.2
13.2
74%
10.6
7.7
15%
0.54
9.3
10.2
14.0
-4.6
10.6
-1.4
100:4:0.9
Note: Effluent Part N estimated based on 0.11 Part N/TSS
24949
Updated: 10/27/99

3 II 3 I 3 3 3
CLAMANT BAT TREATABILTTY STUDY
SUMMARY OF WEEKLY AVERAGE DATA
I 1 3 1 1 3 1 1
UNIT 2
Period
SODS
MLVSS
F/M
TSS
TKN
NH3-N
NOr-N
Influent
Effluent
SVI(FSS
Eff
Inf
Eff
%
Removed
Inf
Mix Liq
Eff
%
Removed
Inf
Mix Litt
Eft
TBOD
TBOD
SBOD
SCBOD
Oxic
Aug 10.16
1400
64
66
2992
0.15
240
42.0
7.8
81%
26.2
3.7
86%
0.04
Aug 17-23
690
25
13
4
2725
0.08
35
53.8
15.7
71%
35.3
7.8
78%
0.34
18.17
Aug 24-30
961
55
34
15
2542
0.12
1
39
74.5
23.5
68%
58.4
19.7
66%
2.5
12.50
Aug 31-Scp 6
961
72
18 •
10
2369
0.13
141
211
74.5
27.6
63%
58.4
22.3
62%
2.5
13.83
Sep 7-13
961
68
15 •
34
3243
0.09
88
78
74.5
39.3
47%
58.4
37.8
31.1
47%
2.5
14.00
19.00
Sep 14-20
961
33
12 •
13
2774
_ 0.11
72
76
74.5
48.3
35%
58.4
31.1
35.2
_ 40%
2.5
19.80
22.17
Sept. 21-present: Effluent collection procedure modified to reduce TSS in effluent samples.
Scp 21.27
961
47
22 ••
25
2660
0.11
60
17
74.5
38.4
48%
58.4
35.8
32.3
45%
2.5
12.83
15.33
Sep 28-0ct7
961
31
11 ••
9
2415
0.12
64
19
74.5
36.6
51%
58.4
31.3
30.4
48%
2.5
13.80
23.80
Oct 8-18
1050
19 ••
7 ••
8
2692
0.12
60
21
46.1
46.1
15.3
67%
22.2
2.8
3.9
82%
4.8
15.88
17.88
Oct 19-25
1050
24 ••
9 ••
4
2350
0.14
20
17
12.7
72%
22.2
1.9
91%
4.8
15.00
Oct 26- Nov 1
1050
18 ••
11 ■•
5
2459
0.13
40
26
46.1
9.4
80%
22.2
1.4
94%
4.8
10.83
Nov 2-8
1050
18 ••
11 ••
10
2830
0.12
200
67
46.1
6.3
86%
22.2
3.1
86%
4.8
9.17
Nov 9-15
1375
10 ••
7 ••
7
3063
0.14
140
77
50.0
10.3
79%
22.2
0.0
3.0
86%
1.0
14.00
Nov 16-22
1683
40 ••
31 ••
33
2789
0.19
245
68
55.3
29.2
47%
17.8
2.8
11.2
37%
2.0
15.88
1.25
Avg. Sep 21-0ct 18
1147.50
25.97
13.63
12.63
2657.2
0.13
103.56
38.98
54.83
19.78
66%
30.71
14.52
10.90
71%
3.42
14.60
13.41
Avg. Aug 31.04318
1080
35
14
14.4
2695
0.13
102.68
61.44
60.20
24.85
62%
38.26
20.22
15.98
0.65
3.17
15.36
14.75
Period
Total Nitrogen
Organic N
Eff Part N
(Estimated)
Eff. Sol
Org. N
(Estimated)",
Total Phosphorous
0-PO.
Part P/
TSS
Influent
BOD:N:P
Inf
Eff
%
Removed
Inf
Eff
%
Removal
Influent
Nut (PO4)
Inf+Nut
Eff Total
P
Removed
Eff PO,
PO4
Removed
Aug 10-16
42.0
7.8
81%
15.8
4.1
74%
22.0
22.0
18.73
100:3:1.6
Aug 17.23
54.1
33.8
38%
18.5
7.9
57%
1.00
19.3
20.3
15.2
5.1
14.77
4.52
100:8:2.9
Aug 24-30
77.0
36.0
53%
16.1
3.8
76%
0.74
19.3
20.0
16.4
3.7
10.43
8.85
100:8:2.1
Aug 31-Sep 6
77.0
41.4
46%
16.1
5.3
67%
0.74
9.6
10.4
19.3
-8.9
12.73
-3.09
100:8:1.1
Sep 7-13
77.0
58.3
24%
16.1
8.2
49%
0.74
9.6
10.4
14.1
-3.8
8.27
1.38
100:8:1.1
Sep 14-20 _
77.0 _
70.5
8%
16.1
13.1
19%
0.74
5.6
6.3
11.5
-5.2
6.13
-0.53
100:8:0.7
Sept. 21-present: Effluent collection procedure modified to reduce TSS in effluent samples.
_
Sep 21-27
77.0
53.7
30%
16.1
6.2
62%
1.9
4.3
0.74
2.8
3.6
5.4
-1.8
3.87
-1.02
0.090
100:8:0.4
Sep 28-Oct 7
77.0
60.4
22%
16.1
6.2
62%
2.1
4.1
0.74
2.3
3.0
5.2
-2.2
3.20
-0.95
0.105
_
100:8:0.3
Oct. 8-18
50.9
33.2
35%
23.9
11.4
52%
2.3
9.1
1.14
1.0
2.1
1.8
0.3
1.29
40.29
0.026
100:5:0.2
Oct. 19-25
50.9
27.7
46%
23.9
10.8
55%
1.9
8.9
1.14
0.0
1.1
1.7
-0.6
0.65
-0.65
0.063
_
100:5:0.1
Oct 26- Nov 1
50.9
20.2
60%
23.9
8.0
66%
2.9
5.1
1.14
0.0
1.1
0.6
0.5
0.11
-0.11
0.020
100:5:0.1
Nov 2-8
50.9
15.5
70%
23.9
3.2
87%
7.4
-4.2
1.14
0.0
1.1
0.7
0.4
0.50
-0.50
0.003
-
100:5:0.1
Nov 9-15
51.0
24.3
52%
27.9
7.3
74%
8.4
-1.1
1.55
0.0
1.6
0.7
0.9
0.10
-0.10
0.007
100:4:0.1
Nov 16-22
57.3
30.5
47%
37.5
18.0
52%
7.5
10.5
0.35
0.0
0.4
0.7
-0.4
0.30
-0.30 _
0.006
0.0
100:3:0
Avg. Sep 21-Nov 22
58
33.2
45%
24
9
64%
4.3
4.6
1.0
0.8
1.8
2.1
-0.4
1.3
-0.5
100:5:0.2
Avg. Aug 31-Nov 22
63
39.6
40%
22
9
59%
4.3
4.6
0.9
2.8
3.7
5.6
-1.9
3.4
-0.6
0.0
100:6:0.3
Notes: Effluent Pan N estimated based on 0.11 Part N!FSS
• unseedcd
•• polyseeded
24949
Updated: 10/19/99

1
CLIRIANT LAT TREAFABILIT\ STUDY 1
SUMMARY OF WEEKLY AVERAGE DATA
UNIT 3
Period
BOD5
MLVSS
F/M
TSS
TKN
NH3-N
NO3-N
Influent
Effluent
SVI/TSS
Eff
Inf
Eff
%
Removed
Inf
Mix Liq
Eff
%
Removed
Inf
Mix Lig
Eff
TROD
TBOD
SBOD
SCBOD
Oxic
Anoxic
Aug 10-16
1400
69
45
3200
0.14
138
42.0
24.1
43%
26.2
10.4
60%
0.0
Aug 17-23
690
55
17
3
3092
0.07
380
53.8
15.7
71%
35.3
4.8
86%
0.3
20.0
Aug 24-30
392
50
35
4
3275
0.04
_ 20
99
_ 65.8
_ 12.0
82%
64.4
3.2
95%
0.0
12.5
11.0
14.3
Aug 31-Sep 8: No anoxic phase (completely
aerobic)
Aug 3I-Sep 8 I 2088
I 35
I 8 I 2 I 2167 1 0.30 1 28 I 335 I 59.3 I 13.7 I 77% 1 52.8 I 1.3 I 2.3 I 96% I 2.8 127.0 I I 16.0
Sep 9-present: Resume anoxic phase
Sep 9-13
618
43
9
2375
0.08
22
44.6
13.7
69%
36.9
3.3
<1
97%
3.0
17.0
11.0
38.5
Sep 14-20
575
16
2
2
2156
0.08
_ 30
116
34.8
11.5
67%
23.8
1.2
1.1
96%
1.5
7.1
2.3
2.1
Sept. 21-present: Effluent collection procedure modified to reduce TSS in effluent samples.
Sep 21-24 I 868 I 17 I 2 I 16 I 2140 I 0.13 I 24 I 1 I 40 I 14.4 I 64% I 26.9 I 1.1 1 <1 I 96% I 1.5 I 6.5 I I 1.8
Sept. 25-present: Began separate anoxic stage
Sep 25-0ct 4
1094
I 12
9
2
3550
0.07
52
3
44.8
4.0
91%
26.6
1.2
<1
96%
1.8
4.8
2.0
2.0
Oct 5-11
1684
35
23
15
3542
0.10
28
12
41.4
7.8
81%
22.8
1.9
1.4
94%
3.5
9.0
1.7
2.0
Oct 12-18
1317
9
5
2 _
3578
0.08 _
19
4
8.8
6
2.6
3.8
2.0
1.8
Avg. Sep 25-Oct 18
1365
19
12
6
3557
0.08
33
6
43.1
6.9
86%
24.7
3.1
1.7
9S%
2.6
5.9
1.9
1.9
Avg. Sep 14-Oct 18
1107
1 18
8
7
2993
0.09
31
27
40.3
9.3
76%
25.0
2.3
1.4
95%
2.1
6.2
2.0
1.9
Period A
Total Nitropzen
Organic N
Eff Part N
(Estimated)
Eff. Sol
Org. N
(Estimated)
Total Phosphorous
0-PO4
Influent
BOD:N:P
Inf
Eff
%
Removed
Inf
Eff
%
Removed
Influent
Nut (PO4)
Inf+Nut
Eff Total
P
Removed
Eff PO,
PO,
Removed
Aug 10-16
42.0
24.1 _
43%
15.8
13.8
13%
22.0
22.0
17.5
_
100:3:1.6
Aug 17-23
54.1
35.7
34%
18.5
10.9
41%
1.00
19.3
20.3
14.0
6.3
11.3
7.99
7.89
100:8:2.9
Aug 24-30
65.8
26.2
60% _
1.4
8.8
-526%
1.25
19.3
20.5
19.3
1.2
11.4
100:17:5.2
Aug 31-Sep 8: No anoxic phase (completely
aerobic)
Aug 31-Sep 8 _I 62.1 1
29.7
I 52% 1 6.5 I 11.4 I -75% I I I 0.54 I 9.6 I 10.2 I 33.2 I -23.0 I 14.0 I -4.36 I 100:3:0.5
Sep 9-present: Resume anoxic phase
Sep 9-13
47.6
52.2
-10%
7.7
12.7
-65%
0.50
9.6
10.1
23.2
-13.1
11.3
-1.61
100:8:1.6
Sep 14-20
36.3
13.6
63%
11.0
10.4
5%
0.60
9.6
10.2
_ 12.9
-2.7
8.1
1.54
100:6:1.8
Sept. 21-present: Effluent collection procedure modified to reduce TSS in effluent samples.
Sep 21-24 I 41.7 1 16.1 I 61% I 13.3 I 13.4 I -1 % I I I 1.1 I 9.6 I 10.7 I 11.0 I -0.3 1 8.3 I 1.34 I 100:5:1.2
Sept. 25-present: Began separate anoxic stage
Sep 25-Oct 4
46.5
6.0
87%
18.2
3.0
83%
0.4
2.7
1.49
9.5
11.0
10.1
0.9
' 8.6
0.85
100:4:1
Oct 5-11
44.9
9.8
78%
18.6
6.4
65%
1.4
5.1
0.81
10.1
10.9
19.9
-9.0
17.6
-7.48
100:3:0.6
Oct 12-18
10.6
6.2
0.4
5.8
6.1
6.1
12.0
-5.8
8.6
-2.41
100:0:0.5
Avg. Sep 25-Oct 18
45.7
8.8
83%
18.4
5.2
74%
0.7
4.5
1.2
8.6
9.3
14.0
-4.6
11.6
-3.0
100:3:0.7
Avg. Sep 14-Oct 18
42.4
11.2
72%
15.3
7.9
38%
0.7
4.5
1.0
9.0
9.8
13.2
-3.4
10.2
-1.2
100:4:0.9
Note: Effluent Part N estimated based on 0.11 Part N/TSS
24949
Updated: 10/19/99

I I I I I 1 1 1 I 1 i 1 i 1 i 1 3 J
CLARIANT BAT TREATABILITY STUDY
SUMMARY OF WEEKLY AVERAGE DATA
UNIT 4
Period
BODS
MLVSS
F/M
TSS
TKN
NH3-N
NO3-N
Influent
Effluent
SVUTSS
Eff
Inf
Eff
%
Removed
Inf
Mix Liq
Eff
%
Removed
Inf
Mix Liq
Eff
TROD
TBOD
SBOD
SCBOD
Oxic
Anoxic
Aug 10-16
1620
7
4
3375
0.10
235
48.2
6.2
87%
27.3
3.9
86%
0.03
Aug 17-23
1060
21
8
2
2983
0.08
50
53.8
12.6
77%
33.8
3.6
89%
0.32
7.8
Aug 24-30
530
45
10
12
3069
0.04
31
55
70.0
25.0
64%
58.1
5.3
91%
0.07
14.1
__
8.0
3.0
Aug 31-Sep 6
5600
9
<2
<2
2573
0.47
83
46
9.0
68.8
2.9
2.4
96%
2.00
10.0
5.5
2.2
Sep 14-20
1000
5
2
2
3261
0.07
12
45
38.9
9.7
75%
23.8
2.7
1.0
96%
2.00
6.5
_ 2.0
1.7
Sept. 21-present: Effluent collection
procedure modified to reduce TSS in effluent samples.
Sep 21-27
1160
3
2
2
3050
0.08
4
12
45.5
6.1
87%
29.9
1.5
1.0
97%
1.50
5.5
2.0
1.8
Sep 28-0ct 4
1027
19
17
4
2850
0.08
36
7
44.4
6.7
85%
25.0
3.0
1.4
94%
2.00
3.8
1.8
2.0
Oct 5-11
1684
14
11
5
3525
0.10
20
7
41.4
6.7
84%
22.8
3.2
1.2
95%
3.50
6.8
1.7
2.0
Oct 12-18
1317
14
10
2
3356
0.09
1
8
10.9
10.3
5.1
5.8
2.5
2.8
Avg. Sep 21-Oct 18
1297
12
10
3
3195
0.09
15
8
43.8
7.6
85%
25.9
4.5
2.2
95%
2.3
5.5
2.0
2.2
Avg. Aug 31-0ct 18
1965 1
11
8
3
3102
0.15
26
21
42.6
8.2
83%
34.1
3.9
2.0
96%
1.8
7.5
3.3
2.2
Pcriod
Total Nitr jen
Organic
Eff
N
%
Removed
Eff Part N
(Estimated
Eff. Sol
Org. N
(Estimated)
Total Phosphorous
0-PO4
Influent
BOD:N:P
Inf
Eff
%
Removed
Inf
Influent
Nut (PO4
lnf+Nut
Total
P
Removed
Eff PO,
PO,
Removed
Aug 10-16
48.2
6.2
87%
20.9
2.4
89%
20.0
20.0
19.0
100:3:1.2
Aug 17-23
54.1
20.4
62%
20.0
9.0
55%
2.2
17.0
19.2
18.0
1.2
15.6
1.40
100:5:1.8
Aug 24-30
70.1
28.0
60%
11.9
19.7
-65%
1.8
17.0
18.8
24.9
-6.2
12.6
4.40
100:13:3.5
Aug 31-Sep 6
11.1
6.5
3.2
8.5
11.7
21.9
-10.2
11.1
-2.63
100:0:0.2
Sep 14-20
40.9
11.4
, 72%
15.1
8.7
42%
1.1
8.5
9.6
12.7
-3.1
10.2
-1.73
100:4:1
Sept. 21-present: Effluent collection
procedure modified to reduce TSS in effluent samples.
Sep 21-27
47.0
7.9
83%
15.6
5.1
67%
1.3
3.8
1.6
8.5
10.1
12.7
-2.6
11.7
-3.23
100:4:0.9
Sep 28-Oct 4
46.4
8.7
81%
19.5
5.3
73%
0.7
4.6
1.4
8.5
9.9
13.6
-3.7
11.0
-2.46
100:5:1
Oct 5-11
44.9
8.7
81%
18.6
5.5
70%
0.8
4.7
0.8
8.5
9.3
15.8
-6.5
12.1
-3.59
100:3:0.6
Oct 12-18
13.7
5.8
0.8
5.0
5.7
5.7
11.0
9.9
Avg. Sep 21-Oct 18
46.1
9.8
82%
17.9
5.4
70%
0.9
• 4.5
1.3
7.8
8.8
13.3
-4.2
11.2
-3.1
100:3:0.5
Avg. Aug 31-Oct 18
44.8
10.2
79%
17.2
6.2
63%
0.9
4.5
1.6
8.0
9.4
14.6
-5.2
11.0
-2.7
100:3:0.7
Note: Effluent Part N estimated based on 0.11 Part NITSS
24949
Updated: 10/19/99

1 1 1 1 1 1 1 1 1 1 1 1 1 3 3 3 3 113
Clariant BAT Pilot Study Data
AEI Job No. N130-24
INFLUENT (AFTER SETTLING) INFLUENT (AFTER SETTLING)
DATE
Unit 1
Unit 2
FED
Bush Fed
Batch No.
BODS
COD
Total P
TKN
NH3-N
NO2/NO3-
Initial pH
Adjusted
H2SO4
H2SO4
Batch No.
HODS
COD
Total P
TKN
NH3-N
NO2/NO3-
Phenolics
Initial pH
Adjusted
H2SO4
H2SO4
N
pH
added
conc.
N
pH
added
conc.
1/basch,
I/batch
1/batch
1/batch
Ubatch
I/batch
6/wk
6lwk
(m!)
Normal
1/batch
1/hatch
1/batch
1/batch
i/hatch
1/batch
6/wk
6/wk
(ml)
Normal
10-Aug
11-Aug
11.7
11.7
11.7
11.7
12-Aug
11.54
11.54
11.54
11.54
13•Aug
1-A
1-A
1400
1765
0.264(ortho)
42
26.2
0.04•
11.75
11.75
1•A
1400
1765
0.264(or2o)
42
26.2
0.04•
11.35
11.35
14-Aug
t-A
1•A
11.7
11.7
1-A
11.75
11.75
15-Aug
I -A
1-A
11.59
11.59
1-A
11.52
11.52
16•Aug
I -A
1-A
1-A
17•Aug
1•A
1-A
11.73
11.73
1-A
11.73
11.73
-
18-Aug
1-A
I -A
11.7
11.7
1-A
11.7
11.7
19-Aug
1-A
I -A
11.4
11.4
1-A
11.43
11.43
20-Aug
2-A
2-A
9.06
9.06
2-A
9.06
9.06
21•Aug
3-A
3-A
690
1
53.8
35.3
0.34•
9.62
9.62
3-A
690
1
53.8
35.3
0.34•
9.62
9.62
•
22-Aug
3-A
3-A
6.72
6.72
3-A
6.64
6.64
23-Aug
3-A
3•A
3-A
24•Aug
4-A
4-A
392
17%
1.25
65.8
64.4
0.01
9.38
9.38
1-8
8.92
8,92
25-Aug
4-A
4-A
9.78
9.78
2-4
650
1694
0.55
81.2
71
0.1•
9.26
9.26
26-Aug
4-A
4-A
2-B
27-Aug
4-A
4-A
24
28-Aug
4-A
4-A
2-B
29•Aug
4-A
4-A
2-B
30-Aug
4•A
4-A
2-B
31-Aug
5-A
5-A
2850
1565
0.3
64.2
59.5
<1.5/1
2-B
1-Sep
5-A
5-A
2-B
2-Sep
5•A
5-A
2-B
3-Sep
5-A
5-A
2-B
4-Sep
5-A
S-A
2-B
5-Sep
5-A
5-A
24
6-Sep
5-A
5-A
2-B
7-Sep
5•A
5-A
,
2-B
8-Sep
6-A
6-A
1325
2437
0.78
54.4
46.1
4.0
10.96
10.96
2-B
1284
2270
1.6
81.5
56.8
9.18
9.18
9-Sep
7-A
7-A
618
1550
0.50
44.6
36.9
3.0
11.66
11.66
2-8
967
1750
0.4
67.5
60.3
5.0
9.26
9.26
10-Sep
7•A
7-A
11.91
11.91
2-B
9.31
9.31
11•Scp
7-A
7-A
11.70
11.70
2-B
9.05
9.05
I2-Sep
7•A
7-A
2-B
9.05
9.05
I3•Scp
7-A
7-A
2-B
9.05
, 9.05
14-Sep
7-A
7-A
11.78
11.78
2-B
8.96
8.96
15-Sep
8-A
8-A
575
1975
0.6
34.8
23.8
1.5
11.76
11.76
2-8
8.92
8.92
16-Sep
8-A
8-A
11.85
11.85
2-B
9.02
9.02
17-Sep
8-A
8-A
7.09
2-B
7.30
18•Sep
8-A
8-A
7.1
2-B
7.01
I9-Sep
8-A
8-A
24
7.01
20-Sep
8-A
8-A
2-B
7.01
21-Sep
8-A
8•A
7.23
2.7
36
-B
6.75
0.2
36
22-Sep
8-A
8-A
7.51
3.0
36
2-B
6.78
0.2
36
23-Sep
9/15
9/15-9/17
404
1845
0.6
46
34.4
3.0
7.02
5.3
36
2-8
7.12
0.15
36
24-Sep
9/16
9/15.9117
2-8
25-Sep
9/17
9/15-9/17
7.09
2-B
943
1745
0.4
67.8
45.6
2.5
6.80
0.65
36
26-Sep
9/18
9/18-9/20
759
1500
0.48
41.9
26.8
<1.5
2-13
27-Sep
9/19
9/18-9/20
2-B
28-Sep
9/20
9/18-9/20
7.06
0.25
36
2-8
6.95
0.25
36
29•Sep
9/21
9/21.9/24
750
1610
0.7
39.2
32.4
1.5
7.14
0.20
36
2-B
7.12
0.20
36
30-Sep
9/23
9/21-9/24
7.10
2-B
7.12
0.2
36
1.0ct
9/24
9r21.9/24
11.43
7.02
3
36
2-8
11.88
7.09
-7.5
36
2.0ct
9/25
9/25-9/28
1800
1835
0.58
53.76
34.1
3.5
7.0
0.2
36
2-8
7.03
0.45
36
3-Oct
9/26
9/25-9/28
0.2
36
2-B
0.40
36
4-Oct
9/27
9/25.9/28
_
_
0.3
36
24
_
0.25
36
24749
Page 1 of 23
Updated: 10/19/99

Clariant BAT Pilot Study Data
AEI Job No. N130-24
INFLUENT (AFTER SETTLING) INFLUENT (AFTER SETTLING)
DATE
Unit 1
Unit 2
FED
Batch Fed
Batch No.
GODS
COD
Total P
UN
NH3-N
NO2/NO3-
N
Initial pH
Adjusted
PH
H2SO4
added
H2SO4
rnnc
Batch No.
BODS
COD
Total P
TICN
NH3-N
NO2/NO3-
N
Phenolics
Initial pH
Adjusted
pH
H2SO4
added
H2SO4
conc.
I/bauh
1/batch
1/batch
1/binds
1/batch
1/batch
6/wk
6/wk
(ml)
Normal
1/batch
1/batch
1/batch
1/hatch
1/batch
1/hatch
6/wk
6/wk
(ml)
Normal
5-Oct
9/28
9/25-9/28
7.34
0.15
36
2.8
0.11
6.83
0.2
36
6-Oct
9/29
9/29.10/1
933
1530
0.38
27.44
13
<1.5
6.77
0.35
36
9/22
6.78
2.60
36
7-Oct
9/30
9/29.10/1
10.84
6.58
0.50
36
9/22
12.03
6.52
2.4
36
8-Oct
10/1
9/29.10/1
11.32
7.17
0.55
36
9/22
1400
2887
0.85
35.28
16.1
1.5
1.46/0.2ORR
11.91
6.94
2.45
36
9-Oct
10/2
1012-10/5
762
1425
1.5
9.63
6.92
0.60
36
9/22
12.18
6.96
8.1
36
10-Oct
10/2
10/2.10/5
6.92
0
36
9/22
6.96
11.Oct
10/4
10/2.10/5
6.92
0
36
9/22
6.96
12-Oct
10/5
10/2.10/5
11.74
7.21
1.8
36
9/22
12.02
7.13
2.60
36
13-Oct
10/6
9.03
7.13
0.3
36
9/22
12.06
7.12
2.5
36
14-Oct
10/7-10/8
9.14
6.78
0.45
36
9/22
12.17
6.97
5.0
36
15.001
10/8
6.78
0.45
36
9/22
6.97
5.0
36
16-Oct
10/9.10/11
7.29
6.95
0.1
36
9/22
12.18
6.98
' 7.5
36
I7-Oct
10/9-10/11
6.95
0.1
36
9/22
6.98
7.50
36
18-Oct
10/9.10/11
6.95
0.1
36
9/22
6.98
7.5
36
19.0ct
7.96
6.93
0.1
36
9/22
11.9
7.34
2.40
36
20.Oct
9/22
21.Oct
9/22
22.0ct
9.50
6.80
0.1
36
9/22
12.20
6.84
2.3
36
23.0ct
7.12
9/22
12.23
7.17
8.1
36
24-Oct
9/22
25-Oct
9/22
26-Oct
8.1
6.9
0.2
36
9/22
12.2
7.0
2.3
36
27-001
9.54
7.03
0.4
36
9/22
12.03
7.01
2.2
36
28-Oct
9.73
7.0
0.20
36
9/22
NA
3340
0.56
34.72
25.1
11.0
12.01
6.56
2.4
36
29-Oct
9.01
7.2
0.15
36
9/22
12.03
7.17
2.25
36
30-Oct
8.83
7.24
0.4
36
9/22
12.24
6.87
8.0
36
31-Oct
9/22
-Nor
9/22
2-Nov
10.33
7.15
0.25
36
9/22
11.75
6.67
2.30
36
3-Nov
9.60
7.20
0.45
36
9/22
11.62
6.72
2.45
36
4-Nov
9.03
7.15
0.3
36
9/22
11.13
7.37
2.7
36
5-Nov
9.16
7.53
0.40
36
9/22
11.26
7.17
2.20
36
6-Nov
9.76
6.80
1.00
36
9/22
12.22
6.69
8.50
36
7-Nov
9/22
8-Nov
9/22
9-Nov
10.39
6.93
0.4
36
9/22
700
3050
2.0
68.3
25.5
2.0
11.95
7.72
1.90
36
10-Nov
9.33
7.00
0.10
36
9/22
11.98
7.07
2.10
36
11-Nov
10.33
6.89
0.25
36
9/22
12.06
7.24
2.1
36
12-Nov
11.09
7.24
0.35
36
9/22
12.11
7.04
2.20
36
13-Nov
7.08
5.0
6
11/8-11/10
1700
1898
1.5
31.5
17.0
1.0
7.04
14-Nov
11/8-11/10
I5•Nov
11/8-11/10
16-Nov
7.04
0.5
36
11/8-11/10
2200
2185
1.6
80.4
27.3
1.0
_
7.03
0.5
6
17•Nov
11/8.11/10
11.88
18-Nov
11.57
7.09
1.10
36
11/8-11/10
11.57
7.05
1.10
36
19•Nov
11.61
6.92
3.5
36
11/11-11/14
1167
2505
0.35
30.2
17.8
2.0
11.58
6.92
3.5
36
20-Nov
21-Nov
22-Nov
24749
Page 2 of 23
Updated: 10/19/99

1
1 1 1 +J 1 1 1 1 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
INFLUENT (AFTER SETTLING)
DATE
Unit 3
Unit 4
FED
Bach Fat
Batch No.
BODS
COD
Total P
TKN
NH3•N
NO2/NO3-
N
Initial pH
Adjusted
pH
H2504
added
H2SO4
conc.
Batch Fed
Batch No.
HODS
COD
Total P
TKN
NH3-N
NO2/NO3-
N
Initial pH
Adjusted
pH
H2SO4
added
H2SO4
co.ra:
1/batch
1/batch
1/batch
1/batch
1/batch
1/botch
6/wk
6/wk
(ml)
Normal
1/batch
1/batch
1/batch
1/hatch
I/batch
I/batch
6/wk
6/wk
(m1)
Normal
10-Aug
1l-Aug
11.7
11.7
11.7
12•Aug
11.54
11.54
11.63
13-Aug
I -A
I -A
1400
1765
0.264(ortho)
42
26.2
0.04•
11.75
11.75
1-A4
I -A 4
1620
2350
0.647(ortho)
48.2
27.3
0.03•
11.56
14-Aug
I -A
1-A
11.7
11.7
1-A-4
1-A-4
11.53
15-Aug
1-A
1-A
11.59
11.59
I-A-4
1-A-4
11.54
16-Aug
I -A
1-A
_
I-A-4
I-A-4
17-Aug
1-A
1-A
11.73
11.73
I-A-4
1-A-4
_
11.63
18-Aug
I -A
1-A
11.7
11.7
I-A-4
1-A-4
11.61
19-Aug
1-A
1-A
11.4
11.4
1-A-4
1-A-4
11.49
20-Aug
2-A
2-A
9.06
9.06
2-A-4
2-A-4
9.2
21-Aug
3-A
3-1.
690
1
53.8
35.3
0.34•
9.62
9.62
3-A-4
3-A-4
1060
2.2
59.4
33.8
0.32•
9.66
22-Aug
3-A
3-A
6.72
6.72
34-4
3-A-4
7.33
23-Aug
3-A
3-A
3-A4
3-A-4
24-Aug
4-A
4-A
392
1796
1.25
65.8
64.4
0.01
9.38
9.38
4-A-4
4-A4
530
2280
1.75
70
58.1
0.07•/0
9.54
25-Aug
4-A
4-A
9.78
9.78
4-A-4
4-A4
9.48
26-Aug
4-A
4•A
4-A-4
4-A-4
27-Aug
4-A
4-A
4-A-4
4-A4
28-Aug
4-A
4-A
4•A4
4-A4
29-Aug
4-A
4-A
4-A-4
4-A-4
30-Aug
4-A
4-A
4-A-4
4-A4
31-Aug
5-A
5•A
5-A-4
5-A-4
5600
3.2
68.8
2
1•Scp
5-A
5-A
5-A-4
S-A-4
2-Sep
5-A
5-A
2850
1565
0.30
64.2
59.5
< 1.5/I
5-A-4
S-A-4
3-Sep
5-A
S-A
5-A-4
S-A4
4-Sep
5-A
5-A
5-A-4
5-A4
5-Sep
5-A
5-A
5-A-4
5-A-4
6-Sep
5-A
5-A
5-A-4
S-A4
7-Sep
5-A
5-A
5-A-4
5-A-4
8-Sep
6-A
6-A
1325
2437
0.78
54.4
46.1
4.0
10.96
10.96
6-A-4
6-A4
2000
2588
2.3
60.9
43.2
3.0
9.4
9-Sep
7-A
7•A
618
1550
0.50
44.6
36.9
3.0
11.66
11.66
7-A-4
7-A-4
1223
1775
1.2
38.6
32.2
3.0
11.6
10-Sep
7-A
7-A
11.91
11.91
7-A-4
7-A-4
11.71
I1-Sep
7-A
7-A
11.70
11.70
7-A-4
7-A4
11.64
12-Sep
7-A
7-A
7-A-4
7-A4
11.64
13-Sep
7-A
7-A
7-A-4
7-A-4
11.64
14•Sep
7-A
7•A
11.78
11.78
7-A-4
7-A4
_
11.84
15-Sep
8-A
8-A
575
1975
0.6
34.8
23.8
1.5
11.76
11.76
8-A-4
8-A-4
1000
2385
1.1
38.9
23.8
2.0
11.7
16-Sep
8-A
8-A
11.85
11.85
8-A-4
8•A4
11.78
17-Sep
8-A
8-A
7.09
8-A-4
8-A-4
6.88
18-Scp
8-A
8-A
7.1
8-A-4
8-A4
7.03
I9-Sep
8-A
8-A
8-A-4
8-A-4
20-Sep
8-A
8-A
8-A-4
8-A-4
21-Sep
8-A
8-A
7.23
2.7
36
8-A
8-A
7.05
1.3
36
22-Sep
8-A
8-A
7.51
3.0
36
8-A
8-A
7.05
23-Sep
9/15
9/15-9/17
1160
2490
1.6
45.5
29.9
<1.5
7.02
5.3
36
9/15
9/15-9/17
1160
2490
1.6
45.5
29.9
<1.5
7.25
2.3
36
24-Sep
9/16
9/15-9/17
9/16
9/15-9/17
25-Sep
9/17
9/15.9/17
7.25
9/17
9/15-9/17
7.25
26-Scp
9/18
9/18-9/20
1027
2415
1.6
46.2
23.1
2
7.25
9/18
9/18-9/20
1027
2415
1.6
46.2
23.1
2
27-5e9
9/19
9/18-9/20
_
7.25
9/19
9/18-9/20
28-Sep
9/20
9/18-9/20
7.16
0.45
36
9/20
9/18-9/20
_
7.16
0.45
36
29-Sep
9/21
9/21-9/24
1.28
42.6
26.8
' 6.95
0.55
36
9/21
9/21-9/24
1.28
42.6
26.8
6.95
0.55
36
30-Sep
9/23
9/21.9/24
7.35
6.9
36
9/23
9/21-9/24
7.35
6.9
36
1.0ct
9/24
9/21.9/24
7.04
0.8
36
9/24
9/21.9/24
7.04
0.8
36
2.0ct
9/25
9/25-9/28
2050
3305
0.92
47.04
27.3
5.5
9.07
7.1
0.2
36
9/25
9/25-9/28
2050
3305
0.92
47.04
27.3
5.5
9.07
7.1
0.2
36
3-Oct
9/26
9/25.9/28
9/26
9/25-9/28
4-Oct
9/27
9/25-9/28
_
_
_
9/27
9/25-9/28
24749
Page 3 of 23
Updated: 10/19/99

3 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
INFLUENT (AFTER SETTLING)
DATE
Unit 3
Unit 4
FED
Batch Fed
Batch No.
HODS
COD
Total P
TKN
NH3-N
NO2N 03•
Initial pH
Adjusted
Hadde�d
H2SO4�
Batch Fed
Batch No.
GODS
COD
Total P
TKN
NH3-N
NO2N 03-
Initial
Adjusted
H2SO4
H2SO4 -
N
pH
pH
added
conc.
1/batch
I/batch
1/batch
1/batch
1/hatch
I/hatch
6/wk
6/wk
(ml)
Normal
I/batch
1/batch
1/batch
lfiatch
111utch
1/batch
6lwk
6lwk
(nil)
Normal
_
19461Y
9/28
9/25-9/28
7.24
0.55
36
9/28
9/25-9/28
7.24
0.55
36
6-Oct
9/29
9/29-10/1
1317
2725
0.7
35.84
18.3
< 1.5
7.01
0.65
36
9/29
9/29.10/1
1317
2725
0.7
35.84
18.3
< 1.5
7.01
0.65
36
7-Oa
9/30
9/29.10/1
11.01
6.87
0.85
36
9/30
9/29-10/1
11.01
6.87
0.85
36
8-Oct
10/1
9/29-10/1
11.43
6.90
1.30
36
10/1
9/29-10/1
<1.5
6.90
1.30
36
9-Oct
10/2
10/2-10/3
1317
2730
1.5
9.79
7.23
1.5
36
10/2
10n-10/5
1317
2730
1.5
9.79
7.23
1.50
36
10-Oct
10/2
10rza0/5
10/2
10/2-10/5
11-Oct
10/4
10/2-10/5
10/4
10/2.10/5
12-0a
10/5
10/2.10/5
11.68
6.81
3.60
36
10/5
10/2-10/5
11.68
6.81
3.60
36
13.Oct
10/6
9.07
6.93
0.6
36
10/6
9.07
6.93
0.6
36
14.0ct
1on. 10/8
9.58
7.26
1.0
36
10/7-10/8
9.58
7.26
1.0
36
15-Oct
10/8
7.26
1.0
36
10/8
7.26
1.0
36
16-Oct
10/9-10/11
7.69
6.95
0.5
36
10/9-10/11
7.69
6.95
' 0.50
36
17-Oct
10/9-10/11
10/9-10/11
18-Oct
10/9-10/11
10/9-10/11
19-Oct
7.93
6.67
0.15
36
7.93
6.67
0.15
36
20-Oct
21-Oa
22-Oct
10.10
6.77
0.3
36
10.10
6.77
0.3
36
23-Oa
8.40
7.28
0.7
36
8.40
7.28
0.7
36
24-Oct
25-Oct
26-Oct
8.2
7.1
0.45
36
8.2
7.1
0.45
36
27-Oct
9.63
6.84
0.8
36
9.63
6.84
0.8
36
28-Oct
10.26
7.38
0.4
36
10.26
7.38
0.4
36
29-Oct
9.3
7.21
0.4
36
9.3
7.21
0.4
36
30.Oct
9.28
7.16
1.2
36
9.28
7.16
1.2
36
31.Oct
1-Nor
2-Nov
10.52
7.25
0.60
36
10.52
7.25
0.60
36
3-Nov
9.65
7.03
0.95
36
9.65
7.03
0.95
36
4-Nov
9.26
7.44
0.6
36
9.26
7.44
0.6
36
5-Nov
8.98
7.47
0.7
36
8.98
7.47
0.7
36
6-Nov
9.80
6.67
3.00
36
9.80
6.67
3.00
36
7-Nov
8-Nov
9-Nov
10.57
7.01
0.85
36
10.57
7.01
0.85
36
10-Nor
9.58
7.00
0.25
36
9.58
7.00
0.25
36
11-Nor
10.61
6.81
0.7
36
10.61
6.81
0.7
36
12-Nov
11.13
7.34
0.9
36
11.13
7.34
0.9
36
13-Nov
14-Nov
15-Nov
16-Nov
17-Nov
18-Nov
19-Nov
20-Nov
21-Nor
22-Nov
24749
Page 4 of 23
Updated: 10/19/99

1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
FEED TANKS
EFFLUENT VOLUMES
NaHCO3 FEED
DATE
Unit 1
Unit 2
Unit 3
Unit 4
Unit 1
Unit 2
Unit 3
Unit 4
Unit 1
Unit 2
Unit 3
Unit 4
FED
Volume
Remaining
Volume
Remaining
Volume
Remaining
Volutnc
Remaining
Daily
Daily
Daily
Daily
Volume Fed
Volume Fed
Volume Fed
Volume Fed
Start of day
Start of Say
Start of day
Stan of day
(L)
(L)
(1.)
(1.)
(m1)
(m1)
(rni)
On!)
10-Aug
0
0
0
0
325
0
0
365
11-Aug
0
0
0
0
3.5
3.5
3.5
3.75
120
35
260
155
12-Aug
0
0
0
0
3.5
3.5
3.2
3.5
135
0
105
105
13-Aug
0
0
0
0
3.5
3.5
3.5
3.8
85
55
105
60
14-Aug
0
0
0
0
3.5
3.5
3.5
3.8
150
250
150
125
15-Aug
0
0
0
0
3.6
4.2
3.4
4.3
145
174
140
145
16-Aug
0
0
0
0
17-Aug
0
0
0
0
7.3
7.3
7.2
7.2
300
315
310
280
18-Aug
0
0
0
0
0.5
3.75
5.75
3.3
50
145
285
125
19-Aug
0
0
0
0
1.5
3.6
5.0
3.9
40
150
250
185
20-Aug
0
0
0
0.5
3.6
3.6
4.5
3.3
160
140
175
205
21-Aug
2.3
0.1
2.3
1.3
3.5
3.4
1.2
2.5
80
75
60
0
22-Aug
200
150
100
100
23-Aug
24-Aug
0
0
0
0
185
0
35
100
25-Aug
0
0
0
0
3.5
3.6
3.5
3.9
95
115
100
75
26-Aug
0
0
0
0
3.4
3.5
3.6
3.8
175
160
190
160
27-Aug
28-Aug
0
0
0
0
3.5
3.5
3.4
3.9
120
150
110
100
29-Aug
5.5
5.5
6.0
4.0
210
245
225
145
30-Aug
31-Aug
0
0
0
-1.0
6.0
6.8
6.6
6.8
175
300
240
250
1-Sep
0
0
0
0
3.4
3.6
3.4
3.5
150
130
130
140
2-Sep
0
0
0
0
3.3
3.2
3.6
3.5
3-Sep
0
0
0
0
4
4
4
3.5
4-Sep
0
'0.2
0
'0.5
3.0
3.2
3.2
2.5
170
130
145
35
5-Sep
2
4
t
3.5
75
170
165
140
6-Sep
7-Sep
3.5
7
6.5
150
190
280
420
8-Sep
1.5
3.9
3.2
2.8
165
260
210
55
9-Sep
4
0
4
0
2.25
2.4
0.5
2.6
165
260
210
55
10-Sep
1.0
1.0
1.0
0.2
2.75
2.9
3.10
3.25
65
115
75
100
11-Sep
2.9
3.2
3.2
3.0
115
130
70
50
12-Sep
2.9
3.1
2.5
3.0
50
165
85
90
13-Sep
14-Sep
3
1
3
1
6.6
6.6
6.4
6.5
120
225
175
150
15-Sep
0.780
0.350
0.780
0.250
3.2
3.2
3.0
3.4
125
115
100
225
16-Sep
0.530
0.300
0.530
0.180
3.2
3.3
3.0
3.2
105
120
135
30
17-Sep
1
'0.5
1
'0.5
3.2
3.25
3.1
3.2
170
135
135
165
18-Sep
0.75
0.20
0.75
1.2
3.2
3.1
3.2
2.1
175
125
165
125
19-Sep
3.35
3.30
2.90
2.00
160
180
220
230
20-Sep
21-Sep
0.330
0.385
0.330
4.4
6.5
6.5
6.8
4.0
315
150
365
155
22-Scp
1.1
6.4
1.1
3.7
3.3
3.8
3.3
0.1
210
115
160
110
23-Sep
1.17
0.88
1.17
0.00
2.8
2.8
3.2
3.8
125
165
150
175
24-Sep
3.2
2.8
2.7
2.9
225
130
240
190
25-Scp
0.420
0.450
2.60
2.60
2.8
2.8
2.5
2.6
130
95
150
250
26•Scp
3.1
3.0
3.0
3.0
165
135
50
0
27-Sep
28-Sep
0.280
0.570
2.80
2.80
6.8
7.0
7.3
7.9
160
275
150
500
29-Sep
0.00
0.450
0.340
0.34
3.4
3.4
3.4
3.5
175
120
125
200
30-Scp
0.500
0.830
0.450
0.450
2.8
2.8
3.4
3.6
135
95
160
365
1-Oct
0
0.15
0.31
0.31
3.1
3.3
3.4
3.6
150
120
225
250
2-Oct
3.2
3.2
3.3
3.3
115
100
0
0
3-Oct
3.2
3.1
3.50
3.60
195
130
500
175
4-Oct
3.1
3
3.2
3.5
150
125
400
150
5-Oct
0.32
1.1
2.1
2.1
3.5
3.2
3.3
3.7
350
135
0
275
6-Oct
0.22
0.03
0.92
0.92
3.4
3.4
3.8
3.7
215
125
500
240
7-Oct
0.250
0.200
0.410
0.410
3.4
3.4
3.5
3.6
265
255
10
305
24749
Page 5 of 23
Updated: 10/19/99

11
Clariant BAT Pilot Study Data
AEI Job No. N130-24
FEED TANKS
EFFLUENT VOLUMES
NaHCO3 FEED
DATE
Unit 1
Unit 2
Unit 3
Unit 4
Unit 1
Unit 2
Unit 3
Unit 4
Unit 1
Unit 2
Unit 3
Unit 4
FED
Remaining
Volume
Remaining
Volume
Remaining
Volume
Remaining
Daily
Daily
Daily
Daily
Daily
Volume Fat
Volute Fad
Volume Fed
Volume Fad
Stan of day_Stan
of day
Stan of day
Stan of dag
(L)
(L)
(L)
(4L
(m1)
(m1)
(m1)
(m!)
8-Oct
0.300
0.00
2.3
2,3
3.5
3.5
3.6
2.0
130
270
215
110
9-0a
0.00
0.00
1.0
3.2
3.5
3.0
3.0
60
285
75
100
10-Oct
3.0
3.0
3.0
3.0
101
325
95
30
11-00
3.5
3.75
3.75
3.5
75
210
80
60
12-Oct
0.32
1.200
2.540
2.540
3.2
2.8
3.0
3.1
125
0
75
50
13.Oct
0.400
0.100
0.810
0.810
3.3
3.5
3.3
3.5
125
435
175
150
14-Oct
2.1
2.1
3.3
3.4
3.5
1.7
165
320
125
75
15-Oa
3.1
3.4
3.3
3.3
140
350
120
100
16.Oct
0.2
1.2
1.5
1.5
3.1
3.3
3.4
3.1
70
285
85
145
17-Oct
3.25
3.25
3.2
3.25
200
300
100
150
18-Oct
3
3.0
3.3
3.4
100
200
100
250
19.0ct
0.690
0.430
1.02
1.02
3.7
3.8
3.8
3.8
85
35
125
125
20-Oct
0.250
0.200
0.600
0.600
3.4
4.0
3.3
3.5
500
21-Oct
0.5
0.65
1.48
1.48
3.0
3.0
3.0
3.2
165
165
190
345
22-Oct
0.120
0.45
1.210
1.210
3.6
3.7
3.7
3.7
100
300
70
0
23-Oct
320
0.200
0.610
0.610
3.1
3.3
3.4
3.7
90
250
120
400
24-Oct
25-Oct
26-Oct
0.490
0.650
1.350
1.350
6.8
6.9
7.3
7.3
220
500
185
120
27-Oa
0.210
0.470
0.690
0.690
3.3
3.4
3.3
3.4
165
385
170
140
28-Oct
0.380
0.400
0.680
0.680
3.3
3.3
3.5
3.5
150
290
155
250
29-Oct
0.130
0.385
0.550
0.550
3.4
3.5
3.7
3.8
140
205
110
30-Oct
0.200
0.210
0.520
0.520
3.00
3.00
3.30
3.30
105
250
175
325
31-Oct
I -Nov
2-Nov
O O O O O
offi�
1.120
1.400
6.8
6.3
7.3
7.2
275
390
385
315
3-Nov
0.350
0.630
4.3
3.7
3.4
3.5
250
80
120
4-Nov
0.33
0.530
0.530
3.3
3.4
3.5
3.5
360
100
120
5-Nov
0.69
0.550
3.3
3.3
3.5
3.5
135
340
6-Nov
0.170
0.540
0.540
3.5
3.5
3.4
3.3
290
135
120
7-Nov
3.6
3.7
3.6
3.6
375
285
200
8-Nov
9-Nov
0.290
0.560
1.590
1.590
6.6
6.6
7.1
6.9
445
210
_
440
10-Nov
0.080
0.360
0.700
3.5
3.4
3.6
3.5
355
410
225
11-Nov
0.010
0.020
0.440
3.5
3.6
3.6
3.5
280
90
140
12-4ov
0.140
0.130
0.850
0.850
3
3.3
3.3
290
120
95
13-Nov
0.24
0.15
0.68
0.68
3.4
3.5
3.5
3.5
270
160
125
14-Nov
2.9
2.9
150
15-Nov
16-Nov
0.10
0.20
7.0
6.7
30
1744ov
0.000
0
3.4
3.4
185
18-Nov
0.100
0.100
3.2
3.4
185
19-Nov
0.75
0.30
3.2
3.2
250
20-Nov
3
3
135
21-Nov
22-Nov
24749
Page 6 of 23
Updated: 10/19/99

1 1 1 1 1 1 1: 1 1 1 1 1. 1 1 1 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
24749
AERATION BASIN
Unit 1
DO.
H3PO4
DO.
DO,
1:30
DO.
ORP.
ORP.
pH
H3PO4
aided
Sludge
MLSS
MLVSS
SV1
SVVfSS
02 Uptake
8:30 am
9:45 am
pm
4:30 pm
10 am
12 pm
pH oxic
anoxic
Temp.
NO3/NO2
NO3/NO2
NH3-N
added (m1)
(rng/1)
Wasted
DATE
2/wk
2/wk
2/wk
1/wk
3/wk
Daily
Daily
Daily
Daily
6/wk
6/wk
a.m.
p.m.
Daily
Oxic
Anoxic
Oxic
Daily
Daily
(L)
10-Aug
4125
2350
10.2
,
7.1
25
22.5
28.9
0.05
11-Aug
6.1
7.2
25.3
22.5
28.9
12-Aug
4400
3050
154.5
7.1
16
15
19.3
0.05
13-Aug
5.5
7.3
16.1
15
19.3
14-Aug
4625
3225
138.4
0.17
8.5
7.1
17
15
19.3
0.05
15-Aug
8.6
7.3
17
30
38.6
16-Aug
0
0.0
17-Aug
4775
3300
108.9
8.5
7.3
17
15
19.3
0.05
18-Aug
8.5
7.3
17.5
15
19.3
19-Aug
4175
3000
115.2
10
7.4
17.2
15
19.3
0.05
20-Aug
8.4
7.1
16.9
15
19.3
21-Aug
4150
3025
96.4
0.5
1.3
1.4
1.2
204
74
7.2
17
15
19.3
0.05
22-Aug
4.8
7.2
17.5
30
38.6
23-Aug
0
0.0
24-Aug
4125
3000
70.3
1.9
1.9
2.4
242
95
7
17.4
20 (HR)
34 (UR)
15
19.3
0.1
25-Aug
<1
0.7
60
34
7
17.3
12.5 (HR)
15
19.3
0.05
26-Aug
4200
3250
71.4
6.7
0.8
2.5
257
147
7.1
18.4
<10 (HR)
<10 (HR)
15
19.3
0.1
27-Aug
6.5
3.6
241
7.2
17.6
14.5 (HR)
10.5 (HR)
15
19.3
0.1
28-Aug
3920
2930
81.6
153
3.1
2.7
214
94
7.0
17.6
4.0
2.5
15
19.3
0.1
29-Aug
<1
6.9
20.0
30
38.6
30-Aug ,
0
0.0
31-Aug
4079
3132
85.8
44
0.6
0
7.1
17.8
7.5
7.5
9.6
0.1
1-Sep
0.5
2.6
2.8
227
37
7.1
17.5
6.5
1.5
15.1
7.5
9.6
0.2
2-Sep
3620
2760
82.9
25
4.5
2.6
197
72
6.9
17.5
9.5 '
1.5
2.9
7.5
9.6
0.2
3-Sep
<1
7.0
20
7.5
9.6
4-Sep
3775
2850
72.8
1.9
2.0
206
55
17.8
14.5
7.5
9.6
5-Sep
2.1
7.5
18
15
19.3
6-Sep ,
0
0.0
7-Sep
4.7
7.7
7.5
9.6
8-Sep
4950
3850
65.7
57
0.47
2.6
1.5
2.6
2.5
222
119
17.6
10
1.5
3.4
7.5
9.6
0.2
9-Sep
58.6
0.18
5.6
2.9
3.9
0.6
271
121
7.45
7.42
17.4
2.5
1.9
1.8
7.5
9.6
0.2
10-Sep
3500
2700
64.3
0.14
4.2
2.2
3.4
2.4
254
113
7.45
7.45
17.5
1.3
7.5
9.6
0.2
II -Sep
3.8
2.1
3.6
1.3
204
84
7.1
7.3
17.5
4.0
2.5
5.0
7.5
9.6
0.2
12-Sep
3.6
76
7.1
17.5
15
19.3
13-Sep
0
0.0
14-Sep
3433
2617
67
0.36
5.4
4.1
0.5
2.9
17
-82
7.1
6.9
17.5
8.5
0.0
1.1
7.5
9.6
0.2
15-Sep
5.3
2.5
3.2
2.6
234
73
6.9
6.9
17.8
8.5
2.0
2.2
7.5
9.6
0.2
16-Sep
3080
2500
74.7
36
0.36
4.5
1.3
3.9
204
46
6.9
7.1
17.6
5.0
2.5
1.9
7.5
9.6
0.2
17-Sep
3260
2540
70.6
20
0.39
4.5
1.6
2.6
1.9
87
3
7.3
7.4
18.2
10
4.5
2.5
7.5
9.6
0.2
18-Sep
3.2
2.3
3.2
1.9
216
45
7.2
7.1
17.6
4.5
14.0
2.4
7.5
9.6
0.2
l9-Sep
6.7
7.1
20
15.0
19.3
20-Sep
21-Sep
3360
2760
77.4
12
0.70
4.5
3.3
3.0
1.0
166
-9
7.1
7.1
18.4
4.0
2.5
< 1
7.5
9.6
0.2
22-Sep
3.3
5.6
82
16
6.9
17.9
7.5
9.6
23-Sep
3154
2612
79.3
0.36
4.5
4.4
3.9
1.6
143
-5
7.0
7.1
17.7
14.5
2.0
1.0
7.5
9.6
0.2
24-Sep
3.8
144
7.1
18.3
7.5
9.6
25-Sep
4.7
3.7
152
-49
6.9
7.0
17.7
4.5
2.5
<1
7.5
9.6
0.2
26-Sep
7.3
21
15.0
19.3
27-Sep
0
0.0
28-Sep
3500
2783
82.9
< I
0.61
6.2
5.5
6.0
177
47
7.2
7.3
18.5
3.0
2.0
< I
7.5
9.6
0.2
29-Sep
6.0
6.5
7.4
7.9
207
7.1
7.1
17.5
7.5
9.6
30-Sep
3550
2933
84.5
6.3
5.9
5.6
2.9
170
73
7.1
7.1
18.0
5.0
2
2.4
7.5
9.6
0.2
1-Oct
5.1
4.8
4.1
212
52
7.1
6.9
18.0
9
2.5
1.7
7.5
9.6
0.15
2-Oct
6.6
6.0
2.2
3.2
223
48
7.0
18.0
7.5
9.6
3-Oct
4.4
7.0
18.5
15.0
19.3
4-Oct
8.2
_
_
6.9
18.0
0
0.0
Page 7 of 23
Updated: 10/19/99

1 3: 1. 1 1 i
Clariant BAT Pilot Study Data
AEI Job No. N130-24
AERATION BASIN
Unit 1
DO,
H3PO4
DO,
DO,
1:30
DO,
ORP.
ORP.
pH
H3PO4
added
Sludge
MISS
MLVSS
SV1
SV1/TSS
02 Uptake
8:30 am
9:45 am
pm
4:30 pm
10 am
12 pm
pH oxic
anoxic
Temp.
NO3/NO2
NO3/NO2
NH3-N
added (m1)
(mg/)
Wasted
DATE
2/wk
2/wk
2/wk
1/wk
3/wk
Daily
Daily
Daily
Daily
6/wk
6/wk
a.m.
p.m.
Daily
Oxic
, Anoxic
Oxlc
Daily
Daily
(L)
5-0c1
3750
3217
88.0
15
0.49
4.7
4.7
-
<1
4.7
94
32
7.4
7.1
7.1
17.5
8.0
3.5
7.5
9.6
6-Oct
< I
3.6
4.0
105
-13
7.1
6.9
17.5
7.5
9.6
7-0ct
3767
3175
95.6
6.4
3.6
238
27
1 6.9
7.0
7.1
17.5
3.5
1.5
<1
7.5
9.6
0.2
8-0ct
0.16
4.8
4.9
4.0
4.3
222
151
1 7.1
7.1
7.0
18.0
7.5
9.6
9-Oct
5.4
5.3
< l
185
48
7.1
7.1
6.9
17.5
8.5
<1.5
1.1
7.5
9.6
0.175
10-Oct
3.9
7.1
18.5
7.5
9.6
11-Oct
0.5
6.9
18.5
7.5
9.6
12-Oct
3609
3067
108.1
11
_
2.7
2.7
5.6
-101
7.2
7.3
7.1
17.5
4.5
<1.5
4.1
7.5
9.6
0.200
13-Oct
0.39
6.5
5.6
5.0
214
94
7.1
7.2
7.1
17.5
7.5
9.6
14-0ct
3734
3325
101.8
5.6
5.6
5.2
203
137
7.0
6.9
7.0
17.5
1.5
<1.5
16.1
7.5
9.6
0.2
15-0ct
8.7
6.5
7.6
6.9
219
136
7.1
7.3
7.2
17.0
7.5
9.6
16-Oct
0.20
7.5
5.6
5.5
5.3
176
128
7.21
7.3
7.2
17.5
10.0
7.0
5.4
7.5
9.6
0.15
17-Oct
7.2
7.2
18.0
1.0
1.3
18-Oct
: 5.7
7.2
18.0
1.0
1.3
19.0ct
3620
3060
6.1
5.2
7.2
17.5
1.0
,
0.05
20-Oct
6.7
6.7
7.0
17.5
1.0
21.Oct
7.5
6.9
18.0
1.0
22-Oct
23-Oct
24.Op
25-Oa
24749
Page8Of23
Updated: 10/19/99

i ) 1 11I 1 J 3 1 1 1 1 1 1 1 J 1 1 1 J
Clariant BAT Pilot Study Data
AEI Job No. N130-24
24749
AERATION BASIN
Unit 2
H3PO4
113PO4
added
Sludge
MLSS
MLVSS
SVI
SVUTSS
02 Uptake
DO
pH
Temp.
NH3-N
NO2/NO3
added (ml)
(mg/l)
Wasted
DATE
2/wk
2/wk
2/wk
l/wk
3/4:
a.m.
p.m.
a.m.
p.m.
Dail
3/wk
3/wk
Daily
Daily
(L)
10-Aug
4225
3025
10.2
8
13
22.5
28.9
11-Aug
7
8.6
11.8
22.5
28.9
12-Aug
3850
2800
90.9
8.5
11.6
15
19.3
13-Aug
6.8
7
11.4
15
19.3
I4-Aug
4375
3150
77.7
5.5
7.1
11.3
15
19.3
15-Aug
>9
7.41
10.7
30
38.6
I6-Aug
0
0.0
I7-Aug
3950
2800
70.9
9.6
7.4
11.5
15
19.3
18-Aug
9.5
6.9
11.1
15
19.3
I9-Aug
3300
2475
87.9
>10
6.9
11
15
19.3
20-Aug
8.6
6.9
10.6
15
19.3
21-Aug
3825
2900
86.3
1.9
7.2
10.6
15
19.3
22-Aug
>10
7.2
11
30
38.6
23-Aug
-
-
0
0.0
24-Aug
3025
2600
76
VVV V VV
000000
7
11
15
19.3
25-Aug
7.1
11.1
15
19.3
26-Aug
2950
2525
72.9
7.1
11.7
15
19.3
27-Aug
7.1
10.9
15
19.3
28-Aug
2971
2500
77.4
<1
7.0
11.1
15
19.3
29-Aug
7.1
12
30
38.6
30-Aug
0
0.0
31-Aug
2825
2425
74.3
242
0.27
>10
7.2
11.9
7.5
9.6
1-Sep
> 10
6.9
11.0
7.5
9.6
2-Sep
2940
2400
78.2
40
9.6
7.2
11.2
7.5
9.6
3-Sep
> 10
7.0
14.0
7.5
9.6
4-Sep
2917
2283
77.1
> 10
11.2
7.5
9.6
5-Sep
> 10
7.4
11.0
15.0
19.3
6-Sep
0
0.0
7-Sep
10
7.2
11
7.5
9.6
8-Sep
3957
3243
63.2
88
0.36
9.8
11.1
38.5
14.5
7.5
9.6
9-Sep
58.1
0.15
8.5
7.39
10.9
38.3
13.5
7.5
9.6
10-Sep
0.26
6.0
7.38
10.9
35.7
7.5
9.6
11-Sep
9.6
6.9
11.0
38.8
14
7.5
9.6
12-Scp
9.8
7.0
11.2
15.0
19.3
13-Sep
0.0
0
14-Sep
3583
2883
61.4
0.32
9.8
7.1
11.3
35.3
16
7.5
9.6
15-Scp
9
7.0
11.5
26.9
17.5
5.5
7.1
16-Scp
3483
2900
63.2
40
0.31
9.4
7.1
11.1
18.0
3.5
4.5
17-Scp
3120
2540
70.5
104
0.36
7.3
7.3
11.5
>25
3.5
4.5
18-Sep
7.8
7.3
11.5
22.5
3.5
4.5
19-Sep
7.6
7.2
12.1
7.0
9.0
20-Sep
0
0
21-Sep
3080
2700
71.4
60
0.17
9.4
7.1
12.2
37.7
14.0
3.5
4.5
0.175
22-Scp
8.3
7.1
11.7
3.5
4.5
23-Sep
3240
2620
61.7
0.21
9.4
7.1
11.5
32.2
10.5
1.5
1.9
0.175
24-Sep
8.9
7.2
11.5
1.75
2.3
25-Sep
9.2
6.9
11.7
37.4
14.0
1.75
2.3
0.125
26-Scp
7.2
7.1
14
3.5
4.5
27-Sep
0
0.0
28-Sep
2920
2460
71.9
44
0.17 •
9.8
7.1
12.5
30.2
14.5
1.75
2.3
0.175
29-Sep
9.7
7.1
11.0
1.75
2.3
30-Sep
3283
2800
64.0
9.1
7.1
11.5
31.7
13.5
1.75
2.3
0.175
I -Oct
8.8
8.6
7.1
7.1
11.5
40.1
12
1.75
2.3
0.125
2.0ct
11.0
7.1
12.5
1.75
2.3
3-Oct
10.4
7.1
13.5
3.5
4.5
4-Oct
_
_
10.2
7.0
13.0
0
0.0
Page 9 of 23 Updated: 10/19/99

i 1 i i i J i 'J 9
1111.31)111
Clariant BAT Pilot Study Data
AEI Job No. N130-24
AERATION BASIN
Unit 2
H3PO4
H3PO4
added
Sludge
MLSS
MLVSS
SVI
SVI/fSS
02 Uptake
DO
pH
Temp.
NH3-N
NO2/NO3
added (ml)
(mg/1)
Wasted
DATE
21wk
2/wk
2/wk
l/wk
3/wk
a.m.
p.m.
a.m.
p.m.
Daily
3/wk
3/wk
Daily
Daily
(L)
5-0c1
2617
2233
66.9
83
0.16
9.7
6.9
7.2
11.5
15.5
1.75
00
N N N N N
0.175
6-Oct
9.5
6.9
7.1
11.5
1.75
7-0ct
2583
2167
69.7
7.7
10.0
6.9
6.9
11.5
23.1
13.5
1.75
0.175
8.0ct
0.31
9.3
8.9
7.1
7.1
12
1.75
9-Oct
8.1
9.2
7.1
7.1
11.5
18.5
1.75
0.150
10-Oct
>9
7.2
7.2
12.5
0.75
11.Oct
>9
7.5
12.5
0.75
12.0ct
3067
2633
65.3
60
8.1
6.1
7.2
7.2
11.5
5.5
16.0
0.75
1.0
0.175
13.Oct
0.36
8.7
7.1
7.1
11.5
0.75
1.0
14-Oct
2983
2750
67.0
9.5
6.9
7.1
11.5
1.8
8
0.75
1.0
0.175
15-Oct
9.8
7.9
7.1
7.0
12.5
0.75
1.0
16-Oc
0.31
9.0
5.1
7.03
7.1
12.0
<1
21.0
0.75
1.0
0.125
I7.Oct
7.8
6.9
12.0
0
0
18.Oct
9.3
7.4
11.0
0
0
19.0ct
2583
2233
20
9.6
9.5
7.1
11.5
0
0
0.05
20-Oct
9.6
7.1
12.5
0
0
21.0ct
2883
2467
9.7
7.1
0
0
0.05
22-Oct
8.2
7.0
12.0
0
0
0
23.Oct
8.6
6.9
12
0
0
24-Oct
25.Oct
26-Oct
2700
2400
40
6.9
12.5
0
0
27-Oct
8.1
7.0
11.0
0
0
28-0:t
2783
2517
8.6
7.2
0
0
29.Oct
6.4
7.1
12.5
0
0
30-Oct
8.4
7.2
0
0
0.6
31-Oct
1-Nov
2-4ov
3640
2830
52.2
200
7.1
11.5
0
000000
0.05
3-Nov
> .63
6.5
6.9
9.0
0
4-Nov
3720
53.8
4.2
7.1
10.5
0
5-Nov
6.2
7.1
10.5
0
6-Nov
4.4
6.9
10.5
0
7-Nov
7.4
7.1
10.5
0
8-Nov
9-Nov
3725
3063
53.7
140
7.1
_
10.5
0
0
0.05
10-Nov
6.3
7.1
10.5
0
0
11-Nov
56.4
>.27
5.3
7.0
10.5
0
0
12-Nov
6.7
7
10.5
0
0
13-Nov
6.7
7.0
10.5
0
0
14-Nov
5.4
7.1
10.5
0
0
15-Nov
0
0
16•Nov
7.9
7.1
11.0
0
0
I7-Nov
0
0
18-4ov
5088
4038
245
6.1
7.0
10.0
0
0
19-Nov
0.42
4.3
6.9
10.0
20-Nov
1720
1540
3.8
7.0
21-Nov
22-Nov
24749
Page 10 of 23 Updated: 10/19/99

1 1- / 1 1 ] 3 3 3; 1 1 ] # 1 1 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
AERATION BASIN
Unit 3
DATE
02
DO.
DO,
DO.
DO.
ORP.
ORP,
pH
Oxie
H3PO4 added
H3PO4 added
MLSS
MLVSS
SV1
SVI/TSS
Uptake
8:30 a
9:45 am
1:30 p
4:30 pm
10 am
12 pm
pH oxic
anoxic
Temp.
NO3/NO2
NO3/NO2
NH3-N
(m1)
(mgli)
SAMPLED
2/wk
2/wk
2/wk
I/wk
3lwk
Daily
Daily
Daily
Daily
6/wk
6/wk
2/day
Daily
Oxic
Anoxic
5/wk
Daily
Daily
10-Aug
4800
3550
10.2
,
7.9
25
22.5
28.9
11-Aug
6.2
7.7
25.2
22.5
28.9
12-Aug
4075
3100
85.9
7.1
25
15
19.3
13-Aug
5.6
7.3
25.3
15
19.3
14-Aug
4375
2950
84.6
7.5
7.3
25.2
15
19.3
15-Aug
5.7
7.08
25.5
30
38.6
16-Aug
0
0.0
17-Aug
4400
I900
68.2
6
7.6
25.5
15
,
19.3
I8-Aug
6.5
7.6
25.6
15
19.3
19-Aug
3775
2950
70.2
6.4
7.3
25.8
15
19.3
20-Aug
>10
7.3
27.8
15
19.3
21-Aug
4275
3425
72.5
1.9
3.5
4.3
1.6
256
170
7.1
26.2
15
19.3
22-Aug
4.6
7.2
24
30
38.6
23-Aug
0
0.0
24-Aug
4150
3200
72.3
3.6
4.5
2.4
242
95
7.1
24
17.5 (HR)
<10 (FIR)
15
19.3
25-Aug
<1
0.6
107
228
7
24
24.0(HR)
15
19.3
26-Aug
4350
3675
73.6
6.3
0.8
1.1
257
188
7.2
24
18.5 (HR)
15
19.3
27-Aug
1.5
1.5
165
7.0
24
14 (HR)
11.5 (HR)
15
19.3
28-Aug
3650
2950
86.3
20
2.6
1.6
163
73
7.0
24
0
0
15
19.3
29-Aug
< 1 i
7.2
25
30
38.6
30-Aug
0
0.0
31-A08
5098
2732
47.1
31
0.4
_
5.1
197
47
7.3
24.6
4.5
9.5
7.5
-
9.6
1-Sep
2.3
2.2
162
6.9
24.6
6.0
No Anoxic
1.4
7.5
9.6
2-Sep
2680
2160
82.1
20
2.6
2.6
256
7.0
24.8
21.0
Cycle
1.1
7.5
9.6
3-Sep
1.5
7.1
25
8/31-9/8
7.5
9.6
4-Sep
2786
2214
75.4
5.3
1.8
252
24.4
80
7.5
9.6
5-Sep
1.9
7.3
24
15
19.3
6-Sep
0
0.0
7-Sep
7.5
9.6
8-Sep
1960
1560
56.1
34
0.17
2.4
2.2
5.1
5.5
253
oxic
24.0
23.5
>4
1.5
7.5
9.6
9-Sep
51.0
0.24
5.7
2.9
2.1 1
2.4
233
49
7.37
7.32
24.9
>20
11
1.8
7.5
9.6
10-Sep
3025
2375
52.9
0.23
5.6
3.1
5.8
3.6
203
53
7.38
7.28
25.3
1.6
7.5
9.6
11-Sep
4.4
3.3
3.6 1
2.9
228
61
7.0
7.2
24.4
14
6.6
7.5
9.6
12-Sep
3.1
55
7.2
24.6
15.0
19.3
13-Sep
-
0.0
0.0
14-Sep
2850
2183
52.6
0.27
2.3
3.1
3.2
1.9
212
42
7.0
7.2
24.9
7.0
2.5
1.1
7.5
9.6
15-Sep
3.7
3.4
3.4
2.7
228
29
7.0
7.2
24.1
8
1.5
1.3
7.5
9.6
16-Scp
2650
2067
62.3
40
0.26
2.7
2.5
3.7
254
-1
7.1
7.0
24.3
6.5
1.5
7.5
9.6
17-Sep
2850
2217
56.1
20
0.37
4.5
2.6
2.6
3.1
127
-30
7.2
7.2
24.4
9.5
4.5
7.5
9.6
18-Sep
2.7
2.4
2.8
2.3
202
-9
6.9
7.1
25.0
4.5
<1.5
7.5
9.6
19-Sep
4.6
7.1
13.8
IS
19.3
20-Sep
_
0
0.0
24749 Page 11 of 23 Updated: 10/19/99

1 1 1 1 1 1 1 1 )' 1 s 1 , 1 1 i 1 1 3 1 $ 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
AERATION BASIN
ANOXIC BASIN
Unit 3
Unit 3
DATE
02
DO,
DO.
Oxic
H3PO4 added
H3PO4 added
Sludge
N031NO2
MLSS
MLVSS
SVI
SVUTSS
Uptakc
8:30 a
4:30 pm
ORP
pH oxic
Temp.
NO3/NO2
NH3-N
(m1)
(mg/1)
Wasted (L)
pH
Temp.
ORP
SAMPLED
2lwk
2lwk
2/wk
1/wk
3/wk
Daily
Daily
6/wk
a.m.
p.m.
Daily
Oxlc
Daily
Daily
a.m.
p.m.
a.m.
p.m.
21-Sep
2750
2320
69.1
24
0.29
4.1
2.6
172
6.9
24.0
7.0
< 1
7.5
9.6
0.2
-21
-,
22-Sep
2.9
2.7
213
7.0
24.5
7.5
9.6
-21
23•Sep
2460
1960
81.3
0.26
3.9
2.3
185
6.9
24.1
6.0
1.2
7.5
9.6
0.2
-29
24-Sep
2.7
7.0
23.5
7.5
9.6
25-Sep
6.4
7.3
17.8
6.5
1.9
7.5
8.9
0.15
9.67
22
•172
-270
1.5
26-Sep
6.5
7.1
18.5
15.0
17.8
7.07
27-Sep
0.0
0.0
28-Sep
4250
3633
82.4
52
0.15
7.0
6.5
7.2
19.0
4.5
< 1
7.5
8.9
0.2
7.04
7.01
21
•139
-139
2.0
29-Sep
7.0
5.2
7.1
17.5
7.5
8.9
6.56
6.92
21
-41
-112
30-Sep
3950
3467
93.7
5.7
4.8
7.0
17.5
4.0
< 1
8.5
10.1
0.200
6.35
7.38
-38
3.0
1-0ct
6.0
4.9
7.8
18
4.0
< 1
8.5
10.1
0.15
22
-121
-121
1.5
2-Oct
7.3
7.5
7.0
16.5
8.5
10.1
3-Oct
8.1
7.7
18.0
17
20.1
21.5
-140
4.Oct
9.7
7.2
18.0
0
0.0
7.20
20.5
-155
5.0ct
3900
3517
97.4
28
0.23
6.6
4.2
146
6.9
17.25
14.0
8.5
10.1
0.2
6.6
19.0
-22
-10
1.5
6-Oct
2.8
110
7.0
17.5
8.5
10.1
7.0
20.5
-104
-126
7.0c1
4067
3567
100.8
6.4
1.9
145
6.9
7.1
17.5
7.0
8.5
10.1
0.2
6.9
21.5
-26
-90
2.0
8-Oa
0.17
5.3
5.3
155
7.1
7.2
18.0
8.5
10.1
6.72
6.91
20.5
-76
-77
9-Oct
7.5
6.3
176
7.1
17.5
6.0
1.9
8.5
10.1
0.175
6.75
20.0
-66
-111
<1.5
10-0ct
8.2
8.2
7.1
17.5
8.5
10.1
6.81
20.5
-87
11.Oa
8.0
7.1
17.5
8.5
10.1
6.80
19.5
-94
12.0ct
4017
3550
149.4
19
7.2
4.9
6.9
7.1
17.5
8.0
1.7
NN Ws VI VI OO
CO 07 OD 00 00 ... ...
10.1
0.200
7.3
20
-84
3.0
13-0ct
0.23
5.5
191
7.0
7.1
17.5
10.1
7.1
7.09
20
•57
-62
14-0ct
3950
3617
202.5
6.2
166
7.1
7.1
17.5
1.5
7.1
10.1
0.2
6.9
20
-106
< 1.5
15.Oct
7.6
6.0
6.9
7.1
17.0
10.1
7.1
19
-105
16-Oct
0.22
6.7
6.2
127
6.94
7.1
17.5
2.0
9.9
10.1
0.15
6.71
6.77
21.5
-103
< 1.5
17-Oct
5.7
6.9
17.5
1.2
6.90
20.5
-105
18.0ct
5.4
7.1 .
18.0
1.2
6.86
21.0
-127
19-Oct
4100
3567
5.5
5.1
6.9
17.5
1.0
1.2
0.05
20-Oct
5.6
5.6
7.0
17.5
1.0
1.2
21-Oct
6.4
7.1
18
1.0
1.2
22-Oct
23-0«
24-Oct
25.Oct
24749
Page 12 of 23
Updated: 10/19/99

24749
Clariant BAT Pilot Study Data
AEI Job No. N130-24
AERATION BASIN
Unit 4
Sludge
DATE
DO,
DO,
D0,
DO,
ORP,
ORP,
pH
H3PO4 added
H3PO4 added
Wasted
MLSS
MLVSS
SVI
SVII TSS
02 Uptake
8:30 am
9:45 am
1:30 pm
4:30 pm
10 am
12 pm
pH oxic
anoxic
Tcmp.
NO3/NO2
NO3/NO2
NH3-N
(ml)
(mg/1)
(L)
SAMPLED
2/wk
2hvk
3/wk
I/wk
3lwk
Daily
Daily
Daily
Daily
6/wk
6/wk
a.m.
p.m.
Daily
Oxic
Anoxic
5lwk
Daily
Daily
10-Aug
4950
3425
_
8.4
7.3
25
27.5
32.6
11-Aug
<1
7.5
25.3
27.5
32.6
12-Aug
4975
3500
180.9
7.2
16.3
17
20.1
13-Aug
<1
7.1
17.1
17
20.1
I4-Aug
4750
3200
189.4
0.18
3.4
6.9
17.2
17
20.1
15-Aug
7.9
7.08
17
34
40.3
16-Aug
0
0.0
17-Aug
5100
3850
121.6
7.6
7.2
17.1
17
20.1
18-Aug
7.4
6.9
17.9
17
20.1
19-Aug
2525
1925
316.8
8.9
7.2
17.6
17
20.1
20-Aug
4.1
7.7
17.1
17
20.1
21-Aug
4400
3175
72.7
2
0.9
0.7
1.5
209
55
7.2
16.8
17
20.1
22-Aug
4.5
6.9
17.4
34
40.3
23-Aug
0
0.0
24-Aug
4425
3275
74.6
1.1
1.1
3.6
223
10
7.1
18.4
36.5 (HR)
< 10 (HR)
17
20.1
25-Aug
<1
0.9
43
-27
7.2
17.6
< 10 (HR)
17
20.1
26-Aug
4688
3488
74.7
6.0
2.6
1.8
205
-11
7
18.6
< 10 (HR)
< 10 (HR)
17
20.1
27-Aug
4.0
3.7
231
6.9
17.8
< 10 (HR)
< 10 (HR)
17
20.1
28-Aug
3157
2443
%.6
31
4.2
3.8
272
72
7.0
17.8
0
0
17
20.1
29-Aug
<1
7.0
20
34
40.3
30-Aug
0
0.0
31-Aug
3333
2641
93.0
133
0.28
0.8
197
13
7.1
17.9
7.0
3.0
8.5
10.1
1-Sep
3.0
1.2
2.3
231
-55
7.1
17.7
7.5
1.5
3.9
8.5
10.1
2-Sep
3140
2520
106.7
33
3.3
2.9
262
74
7.3
18.0
8.5
1.5
1.8
8.5
10.1
3-Sep
<1
7.3
20
8.5
10.1
4-Sep
3314
2557
120.7
4.4
2.7
283
165
18.3
17
16
8.5
10.1
5-Sep
2.4
7.2
18
17
20.1
6-Sep
0
0.0
7-Sep
8.5
10.1
8-Sep
3617
2950
143.8
16
0.22
2.2
1.2
1.4
1.7
263
-46
17.9
<1.5
<1.5
2.0
8.5
10.1
9-Sep
96.8
0.19
4.2
1.8
0.5
2.4
271
-32
7.3
7.3
18.0
1.75
1.8
2.1
8.5
10.1
10-Sep
4160
3460
98.6
0.21
3.2
1.8
2.2
2.5
268
-29
7.3
7.3
17.4
1.0
8.S
10.1
11-Sep
2.8
2.8
3.4
1.3
286
26
7.0
6.9
17.4
4
2.5
9.6
8.5
10.1
12-Sep
3.1
1
7.2
17.6
17
20.1
13-Sep
0
0.0
14-Sep
4183
3233
74.1
0.25
2.2
2.4
2.1
2.4
220
-8
7.2
7.0
17.7
6.5
2.0
1.2
8.5
10.1
15-Sep
2.7
2.4
2.6
1.9
276
1
7.5
7.0
17.7
8.0
2.0
1.1
8.5
10.1
16-Sep
3750
3117
102.7
20
0.23
2.2
1.5
3.8
254
-43
7.0
7.2
17.6
8.5
2.5
4.8
8.5
10.1
17-Sep
4267
3433
77.3
4
0.15
0.7
2.6
1.2
1.9
259
-60
7.0
7.3
18.2
3.1
8.5
10.1
18-Sep
4.1
1.4
2.4
2.1
274
-13
7.0
7.2
17.9
3.0
<1.5
3.2
8.5
10.1
19-Sep
5.2
7.6
20.1
17
20.I
20-Sep
0
0.0
21-Sep
_
3860
3260
97.2
4
0.16
1.9
1.1
3.2
1.0
154
-56
7.2
18.4
4.0
1.5
<1
8.5
10.1
0.20
22-Sep
4.9
4.1
263
181
7.1
17.9
8.5
10.1
0
23-Sep
3400
2840
102.9
0.20
1.0
2.3
3.0
1.1
254
-28
7.0
7.1
17.8
6.0
2.0
1.3
8.5
10.1
0.20
24-Sep
1.8
256
7.0
18.3
8.5
10.1
1.50
25-Sep
2.6
2.3
199
-91
7.0
7.1
17.7
6.5
2.5
2.2
8.5
10.1
0.15
26-Sep
<1
7.2
20.5
17.0
20.1
0
27-Sep
0.0
0.0
0
28-Sep
3017
2550
%.1
36
0.55
< 1
0.8
2.5
-324
7.8
19.0
3.0
6.9
8.5
10.1
0.2
29-Sep
3.9
3.4
4.0
2.0
186
6.9
7.2
17.5
8.5
10.1
0
30-Scp
3533
3150
99.1
3.6
3.4
3.0
2.4
190
-130
7.8
7.8
18.0
4.0
1.5
< 1
8.5
10.1
0.2
1-0ct
4.5
4.6
2.4
159
-110
7.0
7.3
18
4.5
2.0
< 1
8.5
10.1
0.15
2.0ct
5.0
5.4
5.2
6.2
216
86
7.0
17.5
8.5
10.1
3-Oct
4.9
7.2
18.5
17
20.1
4-Ocl
3.4
7.1
_
18.5 _
0
0.0
Page 13 of 23
Updated: 10/19/99

Clariant BAT Pilot Study Data
AEI Job No. N130-24
AERATION BASIN
Unit 4
Sludge
DATE
DO,
DO.
DO.
DO,
ORP.
ORP.
pH
H3PO4 added
H3PO4 added
Wasted
MLSS
MLVSS
SV1
SVIITSS
02 Uptake
8:30 am
9:45 am
1:30 pm
4:30 pm
10 am
12 pm
pH oxic
- anoxic
Temp.
NO3/NO2
NO3/NO2
NH3-N
(ml)
(mg/1)
(L)
SAMPLED
2/wk
2lwk
3/wk
l/wk
3/wk
: Daily
Daily
Daily
Daily
6/wk
6/wk
a.m.
p.m.
Daily
Oxic
Anoxic ,
5/wk
Daily
Daily
5-0a
3617
3233
117.5
20
0.35
4.9
3.7
3.8
2
75
-109
7.2
7.2
7.0
12.25
10.0
2.0
5.4
8.5
10.1
0.2
6-Oct
2.2
2.4
3.2
132
-103
7.0
7.1
17.5
8.5
10.1
7-Oct
4417
3817
176.6
5.2
4.5
168
-124
7.0
7.5
6.9
17.5
5.0
1.5
<1
8.5
10.1
0.2
8.0ct
0.15
5.6
6.8
4.8
3.1
203
40
7.4
7.1
7.1
18.0
8.5
10.1
9-Oct
2.1
1.7
1.6
204
-33
7.0
7.2
7.2
17.5
5.5
< 1.$
8.5
10.1
0.175
10-Oct
7.6
7.1
17.5
8.5
10.1
11.Oct
_
7.6
7.1
17.5
8.5
10.1
12-Oct
3950
3467
202.5
<1
6.1
5.9
1.3
8
7.0
7.0
7.0
17.5
6.0
4.5
3.2
8.5
10.1
0.200
13-0ct
0.27
5.1
5.1
4.2
239
47
7.1
7.0
7.1
17.5
8.5
10.1
14.Oct
3733
3400
214.3
6.9
4.8
3.1
237
48
7.4
7.1
7.1
17.5
1.5
<1.5
13.5
8.5
10.1
0.2
15.Oct
6.2
5.4
5.3
4.5
211
62
7.0
7.0
7.1
16.5
8.5
10.1
16.04x
0.18
6.0
4.0
3.8
4.1
116
-56
6.57
7.2
7.0
17.5
10.0
1.5
14.2
8.5
10.1
0.15
17-Oct
3.4
7.2
17.5
1.0
1.18
18-Oct
3.6
7.3
17.5
1.0
1.18
19-Oct
3900
3200
4.2
3.2
7.0
17.5
1.0
1.2
0.05
20-Oct
4.1
4.1
7.2
17.5
1.0
1.2
21-Oct
4.0
7.6
18.0
1.0
1.2
22-Oct
23.Oct
24.Oa
25.Oct
-
-
24749 Page 14 of 23 Updated: 10/19/99

24749
1 i 1. 1 3 1 1 1: 1 1 D 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
EFFLUENT
DATE
Unit 1
SAMPLED
TBODS
SBODS
sCBOD5
sod PO4-P
TP
TKN
TKN
NH3-N
NO3/NO2
NO3/NO2
Phenolics
Alkalinity
Volume
TSS
TSS
seed
unwed
seed
unseal
(filtered)
Clarifier
mixed
(unmixed)
(mixed)
3/wk
3/wk
3/wk
3/wk
llwk
3/wk
3/wk
3/wk
3/wk
I/wk
I/wk
TSS (L)
(mg/L)
(mg/L)
10-Aug
14.5
11-Aug
12-Aug
73
10
18.3
17.9
8.6
160
13-Aug
14-Aug
23
17
21.6
5.3
190
15-Aug
16-Aug
17-Aug
2
14.3
1.1
6.0
_
18-Aug
19-Aug
20-Aug
14
<2
<2
19.3
23
8.4
1.8
23
103
20
21-Aug
27
9
14.5
24.6
14
2.6
22
180
22-Aug
23-Aug
24-Aug
2
<2
10.8
16.5
7.8
<1
19
30
25-Aug
26-Aug
54
53
4
9.8
15.8
14.6
9
13
0.36
176
40
27-Aug
28-Aug
54
31
9.5
15
9.5
2.5
5
2
29-Aug
30-Aug
31-Aug
98
49
72
27
10.6
17.7
18.5
14
1.0
13
1-Sep
2-Sep
59
54
34
25
26
9.4
19
17.4
1.5
0.22
188
155
3-Sep
4-5ep
24
20
14
4
19.7
27
3.28
2.5
40
5-Sep
6-Sep
7-Sep
8-Sep
9-Sep
39
39
13
2
<2
24
27.9
16.2
< 1
2.3
140
167
10-Sep
39
29
2
2
14.75
32.4
16.0
< 1
160
11-Sep
6
5
<2
2
13.15
14.1
6.07
<1
4.0
5.0
0.06
3
12-Sep
13-Sep
14-Sep
10
11
<2
<2
9.4
11.0
7.47
< 1
1.0
1.0
44
IS -Sep
2.0
2.0
16-Sep
3
<2
<2
<2
<2
8.3
7.1
6.09
< 1
2.0
2.0
0.20
124
10
17-Sep
7
6
<2
<2
8.9
9.3
7.2
<1
2.5
42
18-Sep
<1.5
4.0
19-Sep
20-Sep
21-Sep
5
<2
8.5
10.4
6.26
<1
1.5
2.0
23
22-Sep
23-Sep
7
<2
<2
7.5
10.3
12.8
< 1
2.5
153
7
68
24-Sep
0.20
25-Sep
<2
<2
5.3
8.5
4.63
< I
2.0
< I
20
26-Sep
27-Sep
28-Sep
24
20
10.0
12.3
4.21
<1
2.0
2.0
3
4
29-Sep
0.16
30-Sep
4
3
2
7.2
8.27
11.2
1.5
5.0
139
1
< I
I-0ct
4
3
6.6
7.2
5.6
< t
5.0
1.2
3
< 1
2-Oct
3-Oct
4-Oct
Page 15 of 23
1 1
Updated: 10/19/99

1
1
1 r 1.
1 1 1 1 1 1 l 1 3 1
33
Clariant BAT Pilot Study Data
AEI Job No. N130-24
EFFLUENT
DATE
Unit 1
SAMPLED
TBOD5
SBOD5
sCBOD5
sol PO4-P
TP
TKN
TKN
(filtered)
NH,-N
NO3/NO2
NO3/NO2
Clarifier
Phenolics
Alkalinity
Volume
mixed
TSS
(unmixed)
TSS
(mixed)
seed
unseal
seed
un seed
3/wk _
3/wk
3/wk
3/wk
1/wk
31wk
3/wk
3lwk _
3/wk
Ilwk
I/wk
TSS IL)
(mg/L)
(mg/L)
5-Oct
19
12
14.15
15.5
8.29
1.3
3.5
2.0
1.5
11
34
6-Oct
<0.05
7-Oct
19
10
4
11.4
15.25
9.52
< 1
2.5
115
1.4
34
282
8-Oct
9-Oct
11
3
10.45
12.5
9.86
< I
<1.5
1.2
65
142
10-Oct
11-Oct
_
12-Oct
9
8
8.5
12.1
17.7
< 1
1.5
1.2
14
13.Oa
0.08
14-Oa
4
7
<2
9.95
11.1
8.96
2.6
4.5
79
1.3
4
40
15-Oa
16-Oct
11
3
6.97
7.4
3.1
6.5
1.3
5
33
17-Oa
18.Oct
-
19-Oct
5.23
6.05
8.51
3.92
<1
52
20-Oct
21.Oct
22-Oct
23-Oa
24-Oct
25-Oct
24749
Page 16 of 23 Updated: 10/19/99

1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
EFFLUENT
DATE
Unit 2
SAMPLED
TBODS
SBOD
sCBODS
sol PO4-P
TP
TKN
TKN
NHs-N
N021N034.1
NO2/NO3-N
Phenolics
Alkalinity
Volume
TSS
TSS
seed
unseed
Polyseed
sccd
unwed
Polyseed
(filtered)
Clarifier
mixed
(unmixed)
(mixed)
3/wk
3/wk
31wk
31WK
3/wk
3lwk
llwk
3/wk
3/wk
3lwk
3lwk
3/wk
2/wk
I/wk
TSS (_L)
(mg/L)
(mg1L)
10-Aug
5.3
11-Aug
12-Aug
4
3
21.1
7.8
3.7
260
13-Aug
14-Aug
124
128
29.8
13.6
220
15-Aug
16-Aug
17-Aug
15
18.3
7.6
20.5
18-Aug
19-Aug
20-Aug
26
9
4
13.5
16
15.1
7.6
19
57
10
21-Aug
23
14
12.5
14.4
16.2
8.1
15
.b0
22-Aug
23-Aug
24-Aug
24
24
11.4
16.7
19
12.1
7.0
b0
25-Aug
26•Aug
56
47
15
10.5
20.1
26.9
24.6
16.5
0.525
58
52
27-Aug
28-Aug
84
31
9.4
12.3
24.6
22.3
14
4
29-Aug
30-Aug
31-Aug
106
69
21
28
9.7
21.5
46.5
20.6
13.0
415
I -Sep
2-Sep
59
36
16
16
10
11.4
16.3
10.8
23.9
13.5
0.40
69
148
3-Sep
4-Sep
51
47
23
10
17.1
20
25.4
22.4
15
69
5-Sep
6-Sep
7-Sep
8-Sep
9-Sep
94
51
58
17
34
8
15.2
40.1
30.7
17.5
160
10-Sep
56
48
36
16
8
16
38.4
29.6
24.0
25
72
11-Sep
54
41
15
11
8.8
11.2
33
15.5
16
<1
12-Sep
13-Sep
14-Sep
44
32
13
11
7.2
18.7
35.4
36.8
24.5
I4
88
15-Sep
25
16•Scp
36
31
13
13
13
5.5
7.6
33.8
32
24.5
24.0
0.530.13RR
424
62
17-Sep
18
27
19
11
5.7
8.2
75.7
36.8
22.5
0.36/0.14RR
77
18-Sep
17.5
19
19-Sep
20-Sep
21-Sep
46
31
27
21
4.5
6.4
43.0
34.7
11.5
19.0
38
22-Sep
23-Sep
68
58
36
33
25
4.3
6.1
37.8
31.3
10.0
0.45
25
21
306
24-Sep
0.210.52RR
25-Sep
28
19
9
11
2.8
3.8
34.5
30.8
24.5
13
56
26-Sep
27-Sep
28-Sep
25
14
7
II
2.38
2.6
34.6
24.0
23.0
10
96
29-Sep
0.19
30-Sep
23
15
10
12
9
1.82
2.3
34.7
28.0
25.0
37
8
40
1-Oct
28
21
11
9
1.69
2.42
38.1
32.0
22.5
0.25
1.0
17
48
2-Oct
3-Oct
4-Oa
24749
Page 17 of 23
Updated: 10/19/99

a 1 B. 3 3B i 1 1 3 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
EFFLUENT
DATE
Unit 2
SAMPLED
7BOD5
SBOD
sCBODS
sol PO4-P
TP
7KN
TKN
NH,-N
NO2/NO3-N
NO2/NO3-N
Phenolics
Alblinity
Volume
TSS
TSS
seed
useed
Polyseed
sad
usced
Polyseed
(filtered)
Clarifier
mi:cd
(unmixed)
(mixed)
3/wk _
3/wk
3/wk
3/WIC
3lwk
3/wk
l/wk
3/wk
3/wk
3/wk
3/wk
3/wk
2/wk
I/wk
TSS (L)
(mg/L)
(mt/L)
5-On
33
20
11
12
6.5
12.6
62.16
26.6
22.5
19.5
1.2
45
1050
6-Oa
7-Oct
48
48
17
I1
9
3.6
5.9
36.%
30.9
>25
0.25/0.78RR
41
1.4
16
10
8-Oct
9-0.t
15
11
6
6
1.25
1.89
17.92
10.32
22.5
0.30
1.5
8
32
10-Oct
11-Oct
12-0ct
124
124
136
126
1.11
1.9
22.96
3.3
4.0
1.0
18
%
13-Oct
14.0ct
18
16
11
10
8
1.23
1.69
10.08
1.0
24.0
0.22
53
1.4
20
206
15-Oct
0.18
16-Oct
23
4
4
6
1.53
10.3
<1
21.0
1.5
38
1127
17-Oct
18-Oct
19-Oct
48
15
1.23
3.6
19.49
9.63
3.7
16.0
0.39
150
20-Oct
21-Oct
12
5
4
0.5
0.98
10.3
< 1
16.0
21
22-Oct
23-Oct
13
8
0.21
0.55
8.29
< 1
13.0
0.09
1.3
13
24-Oct
25-Oct
26-Oct
27-Oct
19
9
0.1
0.39
8.51
< I
15.5
0.23
26
165
28.Oct
150
7
5
0.05
0.99
10.64
< I
14.5
1.3
17
102
29-Oct
0.11
30.0cs
18
14
0.18
0.5
9.0
2.14
2.5
35
31.Oct
1-Nov
2-Nov
122
126
53
60
0.95
1.2
4.68
3.5
3.7
36
92
3-Nov
0.12
4-Nov
22
15
10
0.15
0.55
8.1
2.4
11.5
1.3
107
127
S-Nov
0.15
6-Nov
14
7
0.4
0.45
4.5
2.3
12.5
1.5
58
240
7-Nov
8-Nov
9-Nov
12
4
0.1
0.55
6.0
3.4
13.5
72
10-Nov
0.24
11-Nov
II
8
7
0.1
1.0
16.8
2.7
11.5
84
228
12-Nov
9
8
0.1
0.4
8.12
2.9
17.0
0.37
74
254
13-Nov
14-Nov
15-Nov
16-Nov
17-Nov
18-Nov
54
33
33
0.35
1.1
21.3
12.6
1.0
74
19-Nov
0.18
20-Nov
33
29
0.25
0.3
37.1
9.82
1.5
62
21-Nov
22-Nov
_
24749
Page 18 of 23
Updated: 10/19/99

24749
1 I il i I i+ 1. i J 1. I l 3 l 3
Clariant BAT Pilot Study Data
AEI Job No. N130-24
EFFLUENT
DATE
Unit 3
SAMPLED
TBODS
SBOD
sCBODS
so! PO4-P
TP
TKN
TKN
NHs.N
NO2/NO3•N
Phenolics
Alkalinity
Volume
TSS
TSS
seed
utsseod
seal
unsseed
(filtered)
mixed
(umnixed)
(mixed)
3/wk
3/wk
3/WK
3/wk
1/wk
3/wk
3/wk
3/wk
3/wk
3/wk
1/wk
1/wk
TSS (L)
(mill)
(mR/L)
10•Aug
10.8
11-Aug
12-Aug
> 118
76
14.5
24.1
9.7
76
13-Aug
14-Aug
19
13
27.3
11
200
15-Aug
16-Aug
_
17-Au:
24
13.6
7.7
20.5
18-Aug
19-Aug
20•Aug
18
14
3
9
11
13.4
4.9
19.5
56
30
21-Aug
92
12
11.3
17
17.9
1.8
20
730
22-Aug
23•Aug
24-Aug
7
<2
11.2
22.8
14
<1
>25
235
25•Aug
26-Aug
62
55
4
12.5
20.8
12.9
6.9
22
0.378
141
60
27-Aug
28-Aug
80
48
10.5
14.3
9.0
1.7
8
<1
29-Aug
30-Aug
31-Aug
30
62
20
<2
10.1
29
25.8
4.8
2.0
329
1-Sep
2-Sep
48
52
<2
<2
<2
15
35.6
5.69
1.1
13.0
267
567
3-Sep
4-Sep
28
26
<2
<2
16.9
35
9.57
<1
19
108
5-Sep
6-Sep
7-Sep
8-Sep
9-Scp
10-Sep
30
20
15
4
11.25
22.9
7.77
< 1
65.0
42
11-Sep
55
49
2
2
11.25
23.5
19.7
< 1
12.0/13.5••
0.26
< 1
12-Sep
13-Sep
14-Sep
21
17
<2
<2
9.6
12.2
9.58
< I
2.0/2.0••
66
15-Sep
3.0••
16-Sep
18
15
<2
<2
<2
7.0
12.5
16
1.2
2.5
0.18
167
163
17-Sep
8
10
<2
<2
7.7
14
8.92
<1
1.5
120
18-Scp
< 1.5/5.5••
19-Sep
20-Scp
,
21-Sep
32
2
9.1
14.4
23.2
< 1
1.5
276
22-Sep
23-Scp
<2
<2
16
7.5
7.6
5.56
< 1
2.0
125
<1
47
24-Sep
0.16
25-Sep
11
5
8.3
9.0
4.62
<1
2.0
9
88
26-Sep
27-Scp
28-Scp
30
24
10.0
.11.5
3.42
< 1
2.0
< 1
< 1
29-Sep
0.09
30-Sep
3
3
2
8.75
10.0
3.4
< 1
2.0
79
2
28
1.0ct
3
<2
7.53
10.0
4.6
< I
2.0
1.3
1
< 1
2-Oct
3-Oct
4-Oct
Page 19 of 23
Updated: 10/19/99

I i D
$ 1 H i 1' 1 1 f 1 1 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
EFFLUENT
DATE
Unit 3
SAMPLED
TBODS
SBOD
sCBOD5
sol PO4-P
TP
'IKN
TKN
(Meted)
NH,-N
NO2/NO3-N
Phenolics
Alkalinity
Volume
mixed
TSS
((mixed)
TSS
(mixed)
seed
umeed
seed
unsccd
3/wk
3/wk
3/WK
3/wk
I/wk
3/wk
3/wk
3/wk
3/wk
3/wk
I/wk
1/wk
TSS (L)
(m;/L)
(mt/L)
5-Oct
23
12
15.5
19
6.5
< l
2.0
1.3
8
28
6-Oct
0.25
7-Oct
60
48
15
20.63
21.6
8.29
2.2
2.5
208
1.6
15
46
8-Oct
9-Oct
22
10
16.6
19.0
8.74
<1
1.5
1.0
14
85
10-Oct
11.Oct
12.Oct
8
4
10.0
15.7
8.74
<1
1.5
1.0
-
5
94
13-Oct
0.09
14-Oct
3
3
<2
10.58
13.75
5.15
<1
2.0
99
1.5
1
90
15-Oct
16-Oct
16
8
9.48
10.98
5.9
2
1.5
5
63
17-Oct
18.Oct
19-Oct
4.14
6.50
10.3
6.72
2.1
_
27
20-Oct
21.Oct
22-Oct
23-Oct
24-Oct
25-Oct
-
_
24749 Page 20 of 23 Updated: 10/19/99

24749
1 1 1 1 1 I Il i I 1 I 1 I 1 I 1
Clariant BAT Pilot Study Data
AEI Job No. N130-24
Effluent
DATE
Unit 4
SAMPLED
TBODS
SBOD
sCBODS
sol PO4-P
TP
TKN
TKN
N}ls-N
NO2/NO3-N
NO2/NO3-N
Phenolics
Alkalinity
Volume
TSS
TSS
seal
unseal
seed
unsecd
(filtered)
Clarifier
mixed
(unmixed)
(mixed)
3/wk
3/wk
3/WK ,
3/wk
1/wk
3/wk
3/wk
3/wk
3/wk
3/wk
1/wk
1/wk
TSS (1.)
(m2/i.)
(mg/l.)
I0-Aug
17
11-Aug
12-Aug
5
4
14.2
6.2
< 1
300
13-Aug
14-Aug
8
4
25.7
6.7
170
15-Aug
16-Aug
17-Aug
2
19.5
2
10.5
18-Aug
19-Aug
2O-Aug
13
10
<2
13.8
17
12.3
4.5
9
24
20
21-Aug
29
13
13.5
19
12.9
4.3
4
80
22-Aug
23-Aug
24-Aug
<2
<2
12.3
23.7
15.7
5.2
1.5
160
25-Aug
26-Aug
45
13
12
13
22
21.8
8.1
4.0
0.125
122
4
27-Aug
28-Aug
88
14
12.5
29
37.5
2.7
3.5
2
29-Aug
30-Aug
3l-Aug
2
9
<2
<2
10.5
19.3
9.5
3.4
2.0
22
1-Sep
2-Sep
8
8
<2
<2
<2
11
15.4
9.96
2.9
2.5
0.08
110
50
3-Sep
4-Sep
16
13
<2
<2
11.9
31
7.43
<1
2.0
65
5-Sep
6-Sep
7-Sep
8-Sep
9-Sep
2
10
24
<2
<2
12.5
13.8
9.1
< 1
1.5
137
92
10-Sep
23
10
2
3
11.5
13.9
7.46
<1
68
II -Sep
8
9
<2
<2
11.25
19.2
8.72
<1
3.5
3.5
0.06
50
12-Sep
13-Sep
14-Sep
6
6
<2
<2
10.5
11.9
11.9
<1
1.0
1.0
43
IS -Sep
2.5
16-Sep
7
8
<2
<2
<2
9.7
12.1
8.23
<1
2.5
1.0
46
17-Sep
<2
5
<2
<2
10.5
14
8.92
<1
4.5
47
18-Sep
1.5
3.5
19-Scp
20-Sep
21-Sep
3
<2
12.2
13.0
6.98
<1
1.5
1.5
18
22-Sep
23-Sep
<2
<2
<2
12.1
12.8
6.22
<1
2.0
97
< I
129
24-Sep
0.09
25-Sep
3
<2
10.9
12.3
5.10
<1
2.0
16
24
26-Sep
27-Sep
28-Sep
37
35
12.43
14.8
8.09
2.5
1.5
1.5
9
32
29-Sep
<1.0
0.11
30-Scp
17
14
4
10.65
13.5
5.6
<1
2.5
93
2
24
1-Oct
4
<2
9.8
12.5
6.3
<1
2.0
1.5
9
8
2-Oa
3.0.1
4-0m
Page 21 of 23
Updated: 10/19/99

I IliI I I I I I I
Clariant BAT Pilot Study Data
AEI Job No. N130-24
Effluent
DATE
Unit 4
SAMPLED
TBODS
SBOD
sCBODS
sot PO4P
TP
TKN
TKN
(filtered)
NH3.N
NO2/NO3-N
NO2/NO3•N
Clarifier
Phenolics
Alkalinity
Volume
mixed
TSS
(unmixed)
TSS
(mixed)
seal
unwed
seed
unseal
3/wk
3/wk
3/WK
3/wk
l/wk
3/wk
3/wk
3/wk
3/wk
3/wk
1/wk
I/wk
TSS (L
(mid L1
(mg/L)
5-0ct
11
8
13.45
17.5
8.29
1.6
2.0
1.5
1.7
11
45
6-Oct
0.07
7-Oa
25
21
5
11.58
15.25
6.05
<1
2.5
182
1.6
5
73
9-Oct
5
4
11.25
14.6
5.82
< 1
1.5
1.0
6
23
10-Oct
11-Oct
12-Oct
4
<2
11.1
13.0
7.06
< 1
< 1.5
1.1
2
20
13-Oct
0.27
14-Oct
13
7
2
13.15
14.8
10.08
4.0
4.5
37
1.0
9
40
15•Oct
16-Oct
24
21
10.93
11.25
15.46
10.2
2.5
1.8
12
403
17-Oct
I8.Oct
-
19-Oct
4.6
4.8
8.96
5.94
1.9
1.1
28
20-Oct
21-Oct
22-Oct
23-Oct
24-Oct
25-Oct
24749
Page 22 of 23 Updated: 10/19/99

1 1 1
1 1 1 i 1 1 l 3
Clariant BAT Pilot Study Data
AEI Job No. N130-24
1
1
COMMENTS
11-Aug
- Floating sludge in Unit 3. Unit 2 and 3 pH have been drifting upward.
12-Aug
- Started adjusting influent pH to 7.0 in all units. Each unit seeded with 1 liter of Elledge sludge.
13-Aug
- Start of 7-day batch feeding.
14-Aug
- Unit 4 airstone broken, replaced. Added sludge seed to Unit 4.
21-Aug
- Start of air cycling in Units 1, 3 and 4.
31-Aug
- Unit 1 DO dropped to <1 over weekend due to air pump problem. Unit 3 stopped air cycling 8/31-9/8.
8-Sep
- Unit 3 lost solids due to stopper being left in overflow rube. Analyst noted that acid preservation of influent caused
cloudiness which interferences with colorimetric tests.
21-Sep
- Effluent sample collection procedure charged. Samples decanted from effluent container.
22-Sep
- Oxic DO maintained at 1.5-5 mg/L in Units 1, 3 and 4. Start of feeding daily influent samples. The influent analyses
done on 3-day influent composites.
25-Sep
- Unit 3 separate anoxic stage installed.
28-Sep
- DO <1 over weekend due to rotometer failure in Unit 4. Unit 4 aerated -through the morning anoxic period to stabilize.
30-Sep
- Unit 4 overfed NaHCO3. Cleaned pH probe.
1-Oct
- Unit 4 NaHCO3 overfed, probe replaced with standard lab pH probe.
6-Oct
- Unit 2 feed batch changed.
7-Oct
- Unit 4 NaHCO3 overfed, probe replaced with new industrial unit. Low pH in Unit 3.
12-Oct
- Solids buildup in clarifier, mixed liquor appears thin. Clarifier adjusted.
31-Oct
- Cease collecting influent and effluent samples for Units 1, 3 and 4. Maintain operation with minimal monitoring.
2-Nov
- Began using NaOH for pH control in Unit 1.
3-Nov
- Refrigerating circulator tubing was clogged. Unclogged.
13-Nov
- Shut down Units 3 and 4. Began variable feed for Unit 2. (Same feed as Unit 1).
17-Nov
- Analyst found excessive floating sludge. in Unit 2 clarifier. Somewhat septic smell. Baffle was shoved down. Began
aerating immediately. No effluent samples collected.
20-Nov
- Shut down Unit 1 and 2. Baffle was not lifted prior to sampling. Therefore, solids in the clarifier section of reactor were
not mixed with aeration basin solids. Resulted in a lower than normal MLSS & MLVSS.
24749
Page 23 of 23
Updated: 10/19/99

APPENDIX E
DESIGN AND COST ESTIMATE OF
ALTERNATIVE TERTIARY TECHNOLOGIES
• Precipitation Using Ferric Chloride For Phosphorus Removal
• NaOH For Alkalinity Control And Phosphorus Control
• Single -Sludge Biological Nitrification/Denitrification
• Tertiary Denitrification

Precipitation Using Ferric Chloride For Phosphorus Removal

r�l
ram► CLARIANT - TERTIARY TREATMENT FOR PHOSPHORUS REMOVAL
PRECIPITATION USING FERRIC CHLORIDE
r2A1
fir
OMR
tug
rya
DESCRIPTION
VALUE
Maximum Monthly Average Flow
Average Flow
1.55 MGD
1.42 MGD
Phosphorus Removal
Secondary Clarifier Effluent TP
Estimated Phosphorus Removal
Final Effluent Phosphorus
Annual Phosphorus Removal
1.40 mg/L
0.40 mg/L
1.0 mg/L
1729 Ib/yr
Estimated Ferric Chloride Addition
Ferric Chloride Dose (1)
Daily Addition of 40% Ferric Chloride
4 mg/L
119 Ib/d (10 gal/d)
Estimated Polymer Addition
Polymer Dose
Daily Addition of Polymer (2)
5 mg/L
59 Ib/d (6 gal/d)
Estimated NaOH Addition (based on addition of 20 mg/L FeCI3)
NaOH Dose
Daily Addition of 25% NaOH
2.9 mg/L
136 Ib/d (13 gal/d)
Estimated Sludge Generation, based on FePO4 produced
Dry Sludge Produced
Dewatered Sludge (est. 25% solids)
Settled Sludge (est. 1% solids)
23 Ib/d
92 Ib/d (1.5 ft3)
275 gal/d (11.5 gph)
Flash Mix Tank
Capacity
Detention Time @ 1.55 MGD
Dimensions (LxWxH)
Side Water Depth
Materials of Construction
Mixer, Hp
480 gallons
0.5 min detention
4'x4'x5'
4'
Concrete
0.65 Hp
Flocculation Tank
Capacity
Detention Time @ 1.55 MGD
Dimensions (LxWxH)
Side Water Depth
Materials of Construction
Mixer, Hp
16,400 gallons
15 min
13'x13'x15'
13'
Concrete
1.0 Hp
Tertiary Clarifier
Number of Units
Diameter
Side Water Depth
Hydraulic Loading Rate
2
81 ft
12 ft
300 gpd/ft2
Neutralization Tank
Capacity
Detention Time @ 1.55 MGD
Dimensions (LxWxH)
Side Water Depth
Materials of Construction
Mixer, Hp
5,450 gallons
5 minutes
9'x9'x11'
9'
Concrete
2.0 Hp
(1) Ferric chloride dose based on 2x theoretical dose to remove 0.4 mg/L phosphorus.
Assumed 2x theoretical dose due to competing reactions.
(2) Based on an average polymer density of 10 lb/gal.
13024s001
Summary
10/21/99

Foal
Pal
Fart
an
as
Plal
rag
PPR
PIP
PIP
CLARIANT - TERTIARY TREATMENT FOR PHOSPHORUS REMOVAL
PRECIPITATION WITH FERRIC CHLORIDE - BUDGETARY COST ESTIMATE
ESTIMATOR: L.Gellner DATE: 10/21/99
l
DESCRIPTION
(Design Basis - Site grading not
included. Assume no extensive
excavation necessary.)
Quantity
Material & Labor
No. of
Units
Unit of
Meas.
Per Unit
TOTAL
Magnetic Flow Meter wl Transmitter
1
LS
$4,500
$4,500
Installation
$1,000
$1,000
Rapid Mix Tank - 480 gallons, square (4'x4'x5', LxWxH)
Concrete
Slab: 1' thick, 6" overhang
2
yd3
$250
$500
Walls: 1' thick, 1' freeboard
4
yd3
$400
$1,600
Excavation: 2:1 slope
50
yd3
$3
$200
0.65 Hp Mixer
1
ea.
$3,000
$3,000
Mixer Installation
$500
$500
FeCl3 Metering Pump: 0-8 gph, w/ Enclosure
2
LS
$1,900
$3,800
Installation (provide duplicate pumps in parallel for safety)
LS
$500
$500
FeCl3 Storage Tank - 4000 gallon (Insulated FRP)
1
LS
$13,500
$13,500
Polymer Blend & Feed System w/Enclosure: 0-2 gph
2
LS
$7,000
$14,000
Installation
LS
$1,000
$1,000
Flocculation Tank - 15,200 gallons, square (13'x13'x15', LxWxH)
Concrete
_
Slab: 1' thick, 6" overhang
10
yd3
$250
$2,500
Walls: 1' thick, 2' freeboard
31
yd3
$400
$12,400
_
Excavation: 2:1 slope
680
yd3
$3
$2,100
1.0 Hp Mixer wNFD
1
ea.
$14,000
$14,000
Mixer Installation
$500
$500
pH Control System (dual pH probes)
Self -Cleaning Probe, Pre -amp, Chart Recorder, and Enclos
2
LS
$4,000
$8,000
PLC and Control Panel
1
LS
$10,000
$10,000
Programming
1
LS
$5,000
$5,000
Installation
$1,000
$1,000
Tertiary Clarifier - 2 units, each 81 ft Dia., 12 ft. SWD
Equipment - clarifier mechanism , bridge, misc.
2
LS
$238,000
$476,000
_
Concrete
Slab: 81' Dia, 1' thick (2 tanks)
411
yd3
$250
$102,800
_ _
Walls: 1' thick (2 tanks)
229
yd3
$400
$91,600
Excavation: 2:1 slope (2 tanks)
15966
yd3
$3
$47,898
Neutralization Tank - 5,500 gallons, square (9'x9'x11', LxWxH)
Concrete
Slab: 1' thick, 6" overhang
6
yd3
$250
$1,500
Walls: 1' thick, 2' freeboard
16
yd3
$400
$6,400
Excavation: 2:1 slope
325
yd3
$3
$1,000
2.0 Hp Mixer
1
ea.
$6,500
$6,500
Mixer Installation
$500
$500
pH Controller w/Self-Cleaning Probe, Chart Recorder and Enc.
1
LS
$5,500
$5,500
Installation of pH Controller
LS
$500
$500
Major Processes Subtotal Page 1:
[
$839,798
fml
13024s001
COAGFLOC
Page 1 of 3
10/21/99

,p CLARIANT - TERTIARY TREATMENT FOR PHOSPHORUS REMOVAL
PRECIPITATION WITH FERRIC CHLORIDE - BUDGETARY COST ESTIMATE
Foin
PPR
REP
PRI
M+
MI
r=1
W,
rag►
fug
ESTIMATOR: L.Gellner DATE: 9/30/99
I
DESCRIPTION
Quantity
Material & Labor
No. of
Units
Unit of
Meas.
_ Per Unit
TOTAL
NaOH Metering Pumps: 0-8 gph, w/ Enclosure
4
LS
$1,900
$7,600
Installation (provide duplicate pumps in parallel for safety)
LS
$500
$500
NaOH Storage Tank - 4000 gallon w/ Nexus Veil (Insulated FRP)
1
LS
$14,000
$14,000
Tertiary Clarifier Solids Pumps
4
LS
$3,600
$14,400
Insulated Chemical Feed Building: 12'x20', 12' High
1
LS
$22,000
$22,000
I -beams for Mounting Mixers
Rapid Mix Tank
140
Ib.
$1
$140
Flocculation Tank
350
Ib.
$1
$350
Neutralization Tank
255
Ib.
$1
$255
Piping and Tubing - Distances Assumed
Wastewater and Tertiary Solids: Below Ground Piping, 16" FR
600
100 ft.
$5,800
$34,800
Trenching
600
ft.
$25
$15,000
Fittings and Valves
LS
$5,000
$5,000
NaOH Tubing: 0.5" O.D. Heat Trace Tubing
300
ft.
$20
$6,000
FeCI3 Tubing: 0.5" O.D. Teflon Heat Trace Tubing
300
ft.
$20
$6,000
Polymer Tubing: 0.5" Teflon Heat Trace Tubing
300
ft.
$20
$6,000
Tubing Carrier Pipe: 4" Sch 40 (Underground)
300
ft.
$50
$15,000
Major Processes Subtotal Page 2:
$147,045
Major Processes Subtotal Page 1:
$839,798
Major Processes Cost Total:
$986,843
Electrical
10%
$98,684
Engineering
10%
$98,684
Contingency
30%
$296,053
Contractor OH+P
18%
$177,632
Total Project Cost:
$1,658,000
Equivalent Annual Capital Cost:
$268,300
Daily Cost of Chemicals
40% FeCI3
119
lb.
$0.18
$21
25% NaOH
136
Ib.
$0.10
$14
Polymer
59
Ib.
$1.00
$59
Total Annual Cost of Chemicals:
$34,300
Annual Disposal Costs (RCRA Landfill):
17
ton
$220.00
$3,740
Annual Power Requirements:
26,000
kW-H
$0.034
$900
Annual Operating Cost:
$38,900
Equivalent Annual Cost:
$297,300
cm Notes:
Equivalent Annual Cost based on a Capital Recovery Factor for 10 years at 9% interest
LS = Lump Sum
as
Imil
13024s001
COAGFLOC
Page 2 of 3
10/21/99

NaOH For Alkalinity Control And Phosphorus Control

Cal
Fat
rya
FM
CLARIANT - SUBSTITUTION OF LIME WITH CAUSTIC
SUMMARY OF CAUSTIC FEED SYSTEM FOR PHOSPHORUS REDUCTION
DESCRIPTION
VALUE
Average Flow (based on LTA flow)
1.42 MGD
Estimated NaOH Addition (1)
NaOH Dose
• Daily Addition of 50% NaOH
2226 mg/L (26362 Ib/d)
52750 (4135 gpd)
Caustic Storage Tank
Number of Tanks
Type
Capacity
Dimensions
Materials of Construction
Secondary Containment Area
Accessories
2
Flat Bottom, Dome Top
15,000 gallons
12' Dia. x 20'-3"
FRP with Vinylester resin
and Nexis Veil
24'x20'
Heater, Insulation, Vent
Chemical Feed Building
Type
Size
Accessories
Concrete Block
20'x12'
Heated, Insulated,
Exhaust Fan, Lighting
(1) Based on Treatability Study Results - Unit 2
13024s005
Summary_NaOH
10/27/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE OF CAUSTIC FEED SYSTEM FOR PHOSPHORUS REDUCTION
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
Meas.
Per
Unit
TOTAL
Caustic Storage Tank
Caustic Storage Tank: 15,000 gallon FRP
2
ea.
$29,300
$58,600
Miscellaneous Tank Accessories
2
LS
$2,850
$5,700'
Installation
LS
$8,500
$8,500
Level/Alarm: Foxboro, 316ss
4
ea.
$2,850
$11,400
Control Valve: Foxboro
2
ea.
$5,700
$11,400
Concrete Containment: Slab
46
yd3
$200
$9,200
Concrete Containment: Walls
38
yd3
$350
$13,300
Chemical Feed Building (20'x12')
1
ea.
$28,200
$28,200
Building Slab
1
ea.
$2,100
$2,100
Caustic Metering Pumps: Milton Roy, 170 gph
6
ea.
$9,200
$55,200
Accessories
ea.
$9,600
$9,600
Estimated Installation
$8,600
$8,600
pH Control System
pH Controllers: Signet 9030, 4-20mA
3
ea.
$2,500
$7,500
pH Control Cable
1200
ft.
$3
$3,600
Westronics Smartview Recorder
2
ea.
$5,700
$11,400
Estimated Installation
LS
$1,000
$1,000
Estimated Site Work
LS
$14,100
$14,100
Unloading Area•
Concrete Unloading Area
38
yd3
$350
$13,300
Estimated Excavation
LS
$2,800
$2,800
Coating Unloading Area: Tnemic
3200
ft2
$14
$44,800
_
Unloading Platform
2
LS
$13,100
$26,200
Piping and Tubing
Building and Tank Piping
1
LS
$16,900
$16,900
Heat Trace Inside Bldg Piping
1
LS
$3,500
$3,500
NaOH Piping: 3/4" OD w/ PVC Jacket, Heat Trace to 80F
1000
ft.
$21
$21,000
Estimated Installation
1
LS
$2,900
$2,900
Cable: 1/4" 7x19 Aircraft Cable, SS
1000
ft.
$3
$3,000
Tubing Carrier Pipe: 4" Sch 40
700
ft.
$70
$49,000
4" Sch 40 Above -Ground Carrier Pipe
300
ft.
$36
$10,800
6' Steel Carrier Pipe @ Roads
4
ea.
$2,800
$11,200
_
Cable Supports
4
ea.
$2,100
$8,400
Water Pipe: 1" Copper
1600
ft.
$3.50
$5,600
Total Material/Labor Costs:
Electrical:
Engineering:
Contractors, Misc., OH and Profit:
Contingency:
Total System Cost:
10%
18%
30%
I
$478,800
$16,000
$47,880
$86,200
$143,700
$772,580
13024s005
NaOH_Cost
10/27/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE OF CAUSTIC FEED SYSTEM FOR PHOSPHORUS REDUCTION
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
Meas.
Per
Unit
TOTAL
CHEMICAL FEED SYSTEM CAPITAL COST
$772,580
EQUIVALENT ANNUAL CAPITAL COST
$120,400
Daily Cost of Chemicals
NaOH (50%)
52750
lb
$0.14
$7,400
TOTAL ANNUAL COST OF CHEMICAL
$2,701,000
ANNUAL POWER REQUIREMENTS
28500
kW-H
$0.034
$1,000
TOTAL ANNUAL OPERATING COST
$2,702,000
EQUIVALENT ANNUAL COST
$2,822,400
13024s005
NaOH_Cost
10/27/99

Single -Sludge Biological Nitrification/Denitrification

rap CLARIANT: SUMMARY OF SINGLE -SLUDGE
Fill
11411
ral
Mgt
r�A
BIOLOGICAL NITRIFICATION/DENITRIFICATION SYSTEM
DESCRIPTION
VALUE
Design Flow (Based on Maximum Monthly Average)
Average Operational Flow (Based on Long -Term Average)
1.55 MGD
1.42 MGD
Nitrogen Removal
Influent Total Nitrogen
Effluent Total Nitrogen
Nitrogen Removal
15.1
13.3
1.8 mg/L (21.3 lb/day)
Estimated Methanol Addition (Based on 2.5 mg McOH/mg NO3-N) (''
Methanol Dose
Daily Addition of Methanol
9.38 mg/L
111.1 Ib/d (17 gpd)
Heating System - Steam Injection (For Proper Nitrification) (2)
Steam Injection Period
Assumed steam requirement to increase basin 1 C (3)
Required aeration basin temperature
November -March
1460 lb
18 C
Upgrade of Basin ZO3A Mixing - Submersible Mixers (2)
Number of Mixers
Manufacturer
Model
Drive Size
4
Flygt
4680
40 Hp
Methanol Storage Tank
Capacity
Configuration
Dimensions
Materials of Construction
2000 gallons
Horizontal
64" Dia. X 12'
Steel
Denitrification Basin
Period of Use
Capacity
Detention Time
Denitrification Rate
Dimensions
Materials of Construction
Mixer, Hp
March 1 - Oct 31
342,000 gallons
5.3 hr detention
10 mg/Uday
63.5'x63.5'x14'
Concrete
15.0 Hp
(1) Only required in periods of low influent BOD
(2) Increased mixing and steam injection will improve nitrification
(3) Based on information provided by Clariant
13024s005
Summary_BioDenit
10/26/99

raa
CLARIANT CORPORATION, MOUNT HOLLY, NC
COST SUMMARY: SINGLE -SLUDGE NITROGEN REMOVAL SYSTEM
IMP
PAN
r+R
fssl
PSI
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
Meas.
Per
Unit
TOTAL
STEAM INJECTION SYSTEM
$164,100
MIXING SYSTEM
$515,200
DENITRIFICATION SYSTEM
$573,100
TOTAL PROJECT COST
$1,252,400
EQUIVALENT ANNUAL CAPITAL COST
$195,100
TOTAL ANNUAL COST OF STEAM
20870000
lb
$0.0066
$137,700
ANNUAL POWER REQUIREMENTS
560800
kW-H
$0.034
$19,100
TOTAL ANNUAL OPERATING COST
$156,800
EQUIVALENT ANNUAL COST
$351,900
Nitrogen Limits for VWI TP Effluent are from
April 1st - Oct. 31.
Steam is to be injected to maintain constant temperature of 18 C in
basin ZO3A.
Steam costs were calculated assuming a December -February
loading of 6716 Ib/hr and a March -May loading of 146 lb/hr.
The denitrification system will be used throughout the
period between March 1st - Oct. 31 to ensure that proper nitrogen
removal occurs.
13024s005
Cost_BioNitDenit
10/26/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE AERATION BASIN HEATING SYSTEM
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
. Meas.
Per
Unit
TOTAL
Fluid System
6" FRP
4
ft.
$26
$104
6" Stainless Steel Pipe
34
ft.
$52
$1,775
6" Stainless Steel Gate Valve with Nut Actuator & Extension
2
ea.
_
$3,200
$6,400
6" Stainless Steel 90 Degree Elbow
5
ea.
$350
$1,750
Excavation for Two 6" Tie -Ins to the 16" FRP Line
26
C.Y.
$45
$1,170
Modify Influent Pipe (Below Surface)
1
ea.
$2,000
$2,000
6" FRP T-Miter Tie-in to the Existing 16" FRP Line
2
ea.
$1,000
$2,000
Backfill and Compact Excavations
26
C.Y.
$10
$260
6"X6" S.S. Centrifugal Pump (Self -Priming) w/ 10 HP Motor
1
ea.
$13,000
$13,000
Pump and Motor Installation
1
ea.
$1,000
$1,000
6" Stainless Steel Check Valve
` 1
ea.
$2,600
$2,600
6" Magnetic Flowtube and Meter (Tube Mounted)
1
ea.
$3,920
$3,920
Pressure Gage - Including Necessary Piping
1
ea.
$232
$232
6" Stainless Steel Lateral Wye
1
ea.
$225
$225
6" Stainless Steel Throttle Valve
1
ea.
$3,443
$3,443
Temperature Switch with Audible Alarm
1
ea.
$600
$600
Steam System
Fluid Heating System - Penberthy
1
ea.
$12,260
$12,260
Fluid Heating System Installation
1
ea.
$2,500
$2,500
2" Pressure Reducing Valve
1
ea.
$3,400
$3,400
Steam Pressure Gage
1
ea.
$250
$250
2" Steam Flow Cut -Off Valve
1
ea.
$2,100
$2,100
Steam Flowmeter and Totalizer
1
ea.
$1,900
$1,900
2" Steam Piping Overhead (2.0" insulation w/ aluminum jacket)
240
ft.
$17
$4,080
2" Steam Piping Bored/Cased (2.0" insulation w/ aluminum jacket)
100
ft.
$60
$6,000
2" Steam Piping Cased (2.0" insulation w/ aluminum jacket)
50
ft.
$50
$2,500
2" Steam Piping Underground (2.0" insulation and aluminum jacket)
100
ft.
$30
$3,000
Steam Piping Supports
total
$9,800
$9,800
Inverted Bucket Type Steam Traps/Condensate Drains
8
ea.
$450
$3,600
Equipment Pad and Enclosure
Concrete Slab at Grade
6.5
C.Y.
$450
$2,925
Equipment Enclosure
1
ea.
$12,500
$12,500
Protective Bollards
10
ea.
$25
$250
Electrical
$3,200
Total Material/Labor Costs:
Engineering
Contractors, Misc., OH and Profit:
Contingency:
Total Project Cost:
10%
18%
20%
I
$110,800
$11,100
$20,000
$22,200
$164,100
13024s005
Cost Steam
10/26/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE UPGRADE OF BASIN ZO3A MIXING
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
Meas.
Per
Unit
TOTAL
SUBMERGED MIXERS
$168,500
Four (4) 40 Hp w/ Mast and Hoist, Concrete Mast Structures
WALKWAY
$98,600
Includes Piers, Walkway Slab, Handrails, and Installation
AERATOR RELOCATION
$10,000
ELECTRICAL
$71,000
SUBTOTAL
$348,100
ENGINEERING
10%
$34,800
CONTRACTOR OVERHEAD AND PROFIT
18%
$62,700
CONTINGENCY
20%
$69,600
ESTIMATED CONSTRUCTION TOTAL
$515,200
13024s005
Cost Mix
10/26/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE SINGLE -SLUDGE DENITRIFICATION SYSTEM
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
'Unit of
Meas.
Per
Unit
TOTAL
Denitrification Tank
Concrete Tank - 362,000 gallons: 63.5'X63.5'X12'
Slab: 1' Thick, 6" Overhang
164
yd3
$250
$41,000
Walls: 1' Thick, 2' Freeboard
134
yd3
$400
$53,600
Excavation: 2:1 Slope
5700
yd3
$3
$17,100
Submersible Mixer: FLYGT 4600, 15.0 HP w/ Hoist
1
ea.
$13,500
$13,500
Installation:
$3,000
Methanol Addition
Storage Tank: Above -ground, horizontal, steel tank - 2000 gallons
1
ea.
$2,800
$2,800
Level Controls/Alarms
2
ea.
$3,000
$6,000
Secondary Containment: 11.5'x 18'x 1.5', Concrete
Slab: 1' Thick, 6" Overhang - 21'x14.5'
17
yd3
$250
$4,250
Walls: 1' Thick, 1.5' High
4
yd3
$400
$1,600
Excavation: 2' Depth
35
yd3
$3
$200
ORP Control System
1
ea.
$5,500
$5,500
Installation
$500
Unloading Area/Platform (Includes Installation)
1
LS
$10,000
$10,000
Methanol Metering Pumps: 0-2 gph,
2
ea.
$1,100
$2,200
Recirculation Pump
Centrifugal Pump - 2000 gpm, 200% Flow
2
ea.
$25,600
$51,200
Pump Station
LS
$95,000
$95,000
Piping and Tubing - Distances Assumed
Wastewater: Below Ground Piping, 16" FRP
200
ft
$58
$11,600
Trenching
200
ft
$25
$5,000
Fittings and Valves
LS
$2,000
$2,000
McOH Tubing: 0.5"
200
ft
$20
$4,000
_ _ _ _ _
Tubing Carrier Pipe: 4" Sch 40 (Underground)
200
ft
$50
$10,000
Fittings, Tank Piping
LS
$1,000
Total Material/Labor Costs:
Electrical:
Engineering:
Contractors, Misc., OH and Profit:
Contingency:
Total System Cost:
10%
10%
18%
30%
$341,100
$34,100
$34,100
$61,400
$102,400
$573,100
13024s005
Cost_DenitTank
10/26/99

Tertiary Denitrification

rmt
CLARIANT: SUMMARY OF DENITRIFICATION FILTER SYSTEM
..r
MO
Sin
Vogl
paa
IF
- DESCRIPTION
VALUE
Design Flow (Based on Maximum Monthly Average)
Average Operational Flow (Based on Long -Term Average)
1.55 MGD
1.42 MGD
Nitrogen Removal
Influent Total Nitrogen
Effluent Total Nitrogen
Nitrogen Removal
15.1
11.6
3.5 mg/L (41.4 lb/day)
Estimated Methanol Addition (Based on 2.5 mg McOH/mg NO3-N)
Methanol Dose
Daily Addition of Methanol
18.6 mg/L
220 Ib/d (33.2 gpd)
Heating System - Steam Injection (For Proper Nitrification) (1)
Steam Injection Period
Assumed steam requirement to increase basin 1 C (2)
Required aeration basin temperature
November -March
1460 lb
18 C
Upgrade of Basin ZO3A Mixing - Submersible Mixers (1)
Number of Mixers
Manufacturer
Model
Drive Size
4
Flygt
4680
40 Hp
Methanol Storage Tank
Capacity
Configuration
Dimensions
Materials of Construction
2000 gallons
Horizontal
64" Dia. X 12'
Steel
Denitrification Filter System
Period of Use
Number of Reactors
Total Surface Area
Hydraulic Loading Rate
March 1 - Oct 31
3
741 ft2
1.45 gpm/ft2
M+ (1) Increased mixing and steam injection will improve nitrification
(2) Based on information provided by Clariant
WI
00
"I' 13024s005
SummaryTertDenit
10/26/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE TERTIARY DENITRIFICATION FILTER SYSTEM
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
Meas.
Per
Unit
TOTAL
STEAM INJECTION SYSTEM
$164,100
MIXING SYSTEM
$515,200
DENITRIFICATION SYSTEM
$1,204,300
TOTAL PROJECT COST
$1,883,600
EQUIVALENT ANNUAL CAPITAL COST
$293,500
Daily Cost of Chemicals
Methanol
220
Ib
$0.60
$130
TOTAL ANNUAL COST OF METHANOL
$31,700
TOTAL ANNUAL COST OF STEAM
20870000
Ib
$0.0066
$137,700_
ANNUAL POWER REQUIREMENTS
463000
kW-H
$0.034
$15,700
TOTAL ANNUAL OPERATING COST
$185,100
EQUIVALENT ANNUAL COST
$478,600
Nitrogen Limits for WWTP Effluent are from
April 1st - Oct. 31.
Steam is to be injected to maintain constant temperature of 18 C in
basin ZO3A.
Steam costs were calculated assuming a December -February
loading of 6716 Ib/hr and a March -May loading of 146 Ib/hr.
The denitrification system will be used throughout the
period between March 1st - Oct. 31 to ensure that proper nitrogen
removal occurs.
13024s005
Cost_Tert
10/26/99

CLARIANT CORPORATION, MOUNT HOLLY, NC
COST ESTIMATE TERTIARY DENITRIFICATION SYSTEM
DESCRIPTION
QUANTITY
MATERIAL AND LABOR
# of
Units
Unit of
Meas.
Per
Unit
TOTAL
Denitrification Filter System
1
ea.
$450,000
$450,000
Includes Site Work, Buildings, Motor Controls
Installation
1
LS
$200,000
$200,000
Methanol Addition
Storage Tank: Above -ground, horizontal, steel tank - 2000 gallons
1
ea.
$2,800
_
$2,800
Level Controls/Alarms
2
ea.
$3,000
$6,000
Secondary Containment: 35'x14'x3', Concrete
Slab: 1' Thick, 6" Overhang - 36'x15'
17
yd3
$250
$4,250
Walls: 1' Thick, 3' High
4
yd3
$400
$1,600
Excavation: 2' Depth
35
yd3
$3
$200
ORP Control System
1
ea.
$5,500
$5,500
Installation
$500
Unloading Area/Platform (Includes Installation)
1
LS
$10,000
$10,000
Methanol Metering Pumps: 0-2 gph,
2
ea.
$1,100
$2,200
Piping and Tubing - Distances Assumed
Wastewater: Below Ground Piping, 16" FRP
200
ft
$58
$11,600
Trenching
200
ft
$25
$5,000
Fittings and Valves
LS
$2,000
$2,000
McOH Tubing: 0.5"
200
ft
$20
$4,000
Tubing Carrier Pipe: 4" Sch 40 (Underground)
200
ft
$50
$10,000
Fittings, Tank Piping
LS
$1,000
Total Material/Labor Costs:
Electrical:
Engineering:
Contractors, Misc., OH and Profit:
Contingency:
Total System Cost:
10%
10%
18%
30%
I
$716,700
$71,700
$71,700
$129,100
$215,100
$1,204,300
13024s005
Cost_TertDenit
10/26/99