WATER POLLUTION CONTROL RESEARCH SERIES • 12130 EDX 07/70
Joint Treatment
of
Municipal Sewage
and
Pulp Mill Effluents
U.S. ENVIRONMENTAL PROTECTION AGENCY
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WATER POLLUTION CONTROL RESEARCH SERIES
The Water Pollution Control Research Series describes the
results and progress in the control and abatement of pollution
In our Nation*s waters. They provide a central source of
information on the research, development, and demonstration
activities in the Environmental Protection Agency, through
inhouse research and grants and contracts with Federal, State,
and local agencies, research institutions, and industrial
organizations.
Inquiries pertaining to Water Pollution Control Research Reports
should be directed to the Head, Publications Branch (Water),
Research Information Division, R&M, Environmental Protection
Agency, Washington, D.C. 20460,
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JOINT TREATMENT
OF
MUNICIPAL SEWAGE AND PULP MILL EFFLUENTS
The Green Bay Metropolitan Sewerage District
2231 Quincy Street
Green Bay, Wisconsin 54305
a report for the
ENVIRONMENTAL PROTECTION AGENCY
Program #12130 EDX
Grant #WPRD 60-01-6?
July, 1970
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EPA Review Notice
This report has been reviewed by the Environmental
Protection Agency and approved for publication. Approval
does not signify that the contents necessarily reflect
the views and policies of the Environmental Protection
Agency, nor does mention of trade names or commercial
products constitute endorsement or recommendations for
use.
For sale by the Superintendent of Documents, U.S. Government Printing Office
Washington, D.C. 20402 - Price $6
Stock Number 5501-0206
ii
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ABSTRACT
This research project determined the technical and economic feasibility
of jointly treating the influent to the present treatment facilities of the
Green Bay Metropolitan Sewerage District in combination with the weak
effluents from the pulping sections of four local paper mills, specifically
American Can Company, Charmin Paper Products Company, Fort
Howard Paper Company and Green Bay Packaging, Inc.
Four activated sludge processes (conventional, step aeration, contact
stabilization, and Kraus) were studied in parallel using 1-gpm pilot
plants. At the end of the 12 months, the conventional and step aeration
processes were eliminated from further consideration. The contact
stabilization and Kraus processes were studied for an additional four and
one-half months. Contact stabilization was selected as the most promising
process and units were operated for an additional five months to obtain
refined design and operating parameters for a full-scale treatment plant.
Shortly after initial start-up, the pilot plants became infested with fila-
mentous organisms identified as a bacterial species of the genus Thiothrix,
a sulfur-storing organism. Of various procedures implemented, chlorina-
tion of the return activated sludge successfully controlled the growth of
filamentous organisms which caused sludge bulking. It was also necessary
to add nutrients to achieve the desired BOD:N:P ratios.
The operation of the pilot plant units during the last study phase gave the
following results:
BOD
TSS
Primary Influent - 478 mg/1
Final Effluent - 43 mg/1
Percent Removal - 91%
Primary Influent
Final Effluent
Percent Removal
- 224 mg/1
- 50 mg/1
- 78%
Extensive solids-handling unit process studies were conducted at the
pilot plant site and in the cooperating manufacturer's laboratories.
The capital costs to the individual participants, based on becoming a
part of the joint venture or providing separate facilities, are presented.
American Can Company and Charmin Paper Products Company are
joining with the Green Bay Metropolitan Sewerage District in a joint
treatment plant program. Fort Howard Paper Company and Green Bay
Packaging, Inc. have elected to provide their own facilities.
This report was submitted in fulfillment of Grant No. WPRD-60-01 -67
between the Federal Water Quality Administration and the Green Bay
Metropolitan Sewerage District.
Key Words: Joint Treatment - Weak Pulp Mill Effluent - Municipal
Sewage - Pilot Plants - Activated Sludge - Filamentous
Bacteria - Sludge Disposal - Capital Costs .
111
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CONTENTS
Abstract iii
Conclusions 1
Recommendations 2
Introduction 3
Waste Characteristics and Joint Treatment Options 7
Schedule of Major Events 11
Laboratory Reactor Studies 13
Pilot Plant Design and Construction 29
Laboratory Staff, Equipment, Procedures and Data Reduction 47
Pilot Plant Operation 63
Primary Clarification 69
Introduction to Pilot Plant Research Program 97
Pilot Plant Research - Phase I 99
Pilot Plant Research - Phase II 137
RAS Chlorination - Phase II 181
Pilot Plant Research - Phase ILL 191
Pilot Plant Research - Phase IV 219
Cost Estimates For Joint Treatment And Separate Treatment
Facilities 237
Solids Handling Unit Process Studies 245
BTU Value of Sludges 257
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CONTENTS (Cont'd)
Page
Oxidation of Sulfides in Primary Clarifier Effluent 261
Final Effluent Chlorination 267
Total Carbon Correlations 275
Acknowledgements 285
References 287
Appendices 289
Abbreviations 409
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TABLES
Table No. Page
1 Average Mill and Metro Waste Characteristics Utilized For
Final Full-Scale Plant Design 9
2 Laboratory Reactor Studies 15
3 R5, 15-Liter Reactor, Laboratory Data 21
4 R3, 5-Liter Reactor, Laboratory Data 23
5 R4, 5-Liter Reactor, Laboratory Data 25
6 Pilot Plant Equipment Costs 45
7 Project Personnel 49
8 Laboratory Equipment 51
9 Pilot Plant Sampling Program 65
10 Pilot Plant Measurements 67
11 Primary Clarification Investigation, Sample Composition,
11/11/68 71
12 Primary Clarification Investigation, Mill and Metro
Combination, 11/11/68 73
13 Primary Clarification Investigation, Industrial Mill and
Metro Wastes, 1/13/69 75
14 Primary Clarification Investigation, Sample Composition
and Volume, 2/26-27/69 77
15 Primary Clarification Investigation, Composite Samples,
2/26-27/69 79
16 Primary Clarification Investigation, Composite Samples,
2/26-27/69 81
17 Projected Full-Scale TSS and BOD Removal - Imhoff Cone
Studies 83
VI
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TABLES (Cont'd)
Table No. Page
18 Projected Full-Scale TSS and BOD Removal - Pilot
Clarifier Operation 85
19 Pilot Clarifier Operation, May-July, 1969 89
20 Comparison of Pilot Clarifier and Primary Clarifier
Operation, May-July, 1969 91
21 Pilot Clarifier Operation, 9/1-10/19/69 95
22 Microbiological Analyses - Phase I 104
23 Pilot Plant Operation - Phase I 119
24 Pilot Plant Operational Parameters - 8/1/68 133
25 BOD and TSS Removal - Phase I 135
26 Statistical Experimental Design Schedule 139
27 Theoretical Pilot Plant Operation - Phase II 141
28 Biological Analyses - Conventional Unit - January, 1969 187
29 Biological Analyses - Step Aeration - January, 1969 189
30 Theoretical Pilot Plant Operation - Phase III 193
31 BOD and TSS Removal - Phase III 201
32 Special Laboratory Studies - Phase III 207
33 Average Pilot Plant Operating Data - September, 1969 225
34 Plant A Operating Data - October, 1969 229
35 Special Laboratory Studies - Phase IV 231
36 Full-Scale Design Parameters for Contact Stabilization
Treatment Plant 239
Vll
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TABLES (Cont'd)
Table No. Page
37 Distribution of Capital and Operating Costs 241
38 Distribution of Estimated Treatment Plant Construction
Costs 243
39 Solids Handling Process Studies 247
40 Sample Analyses Schedule - Solids Handling Processes 251
41 Minimum and Maximum Solids Handling Data 253
42 BTU Value of Sludges 259
43 Final Effluent Chlorination -6/3/69 269
44 Final Effluent Chlorination - 6/13/69 271
45 Total Coliform In Final Effluent 273
46 BOD - Total Carbon Ratios 277
47 BOD And Total Carbon Models 279
48 BOD And Total Carbon Models 281
VT.X1
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FIGURES
Figure No. Page
1 Green Bay Metropolitan Sewerage District - Service Area 5
2 Perspective Drawing of Pilot Plants 31
3 Pilot Plant Floor Plan 33
4 Pilot Plant Flow Schematic 35
5 Pilot Plant Equipment Photos 37
6 Pilot Plant Equipment Photos 39
7 Electrical Schematic for Proportional Samplers 43
8 Pilot Clarifier Flow Schematic 87
9 Pilot - Primary Clarifier Flow Schematics 93
10 Pilot Plant Flow Schematic - 2/6/68 - 2/22/68 101
11 Biological Microphotographs 107
12 Microphotographs - Filamentous Bacteria Containing Sulfur
Granules 109
13 Pilot Plant Flow Schematic - 2/23/68 - 3/19/68 111
14 Pilot Plant Flow Schematic - 3/19/68 - 5/20/68 113
15 Pilot Plant Flow Schematic - 5/21/68 - 7/25/68 115
16 Pilot Plant Flow Schematic - 7/26/68 - 9/17/68 117
17 Pilot Plant Operation - Phase I - Conventional Unit 123
18 Pilot Plant Operation - Phase I - Step Aeration Unit 125
19 Pilot Plant Operation - Phase I - Contact Stabilization Unit 127
20 Pilot Plant Operation - Phase I - Kraus Unit 129
21 Pilot Plant Flow Schematic - 9/18/68 - 1/14/69 143
IX
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FIGURES (Cont'd)
Figure No. Page
22 Pilot Plant Flow Schematic - 1/15/69 - 1/31/69 145
23 Pilot Plant Operation - Phase II - Conventional Unit 147
24 Pilot Plant Operation - Phase II - Step Aeration Unit 149
25 Pilot Plant Operation - Phase II - Contact Stabilization Unit 151
26 Pilot Plant Operation - Phase II - Kraus Unit 153
27-34 Statistical Experimental Data Summary 159
35 Effects of RAS Chlorination - Conventional Process 183
36 Effects of RAS Chlorination - Step Aeration Process 185
37 Pilot Plant Flow Schematic - 3/3/69 - 7/16/69 195
38 Pilot Plant Flow Schematic - 7/17/69 - 8/10/69 197
39 Pilot Plant Operation - Phase III 199
40 Laboratory Digester Studies, May-July, 1969 213
41 Laboratory Digester Equipment 215
42 Pilot Plant Flow Schematic - 8/11/69 - 9/11/69. 221
43 Pilot Plant Flow Schematic -9/12/69-12/15/69 223
44 Average Pilot Plant Operation - 8/1/69 - 12/15/69 233
45 Pilot Plant Operation - Phase IV 235
46 Special Studies Schedule - Phase IV 249
47 Sulfide Content vs. Chlorine Dosage 263
48 Sulfide Content vs. Time of Preaeration 265
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CONCLUSIONS
The following major conclusions were reached during this research project:
1. A combination of weak pulping effluents from the ammonia base
sulfite, calcium base sulfite, deinking, and neutral semichemical
pulping processes can be successfully treated jointly with
municipal sewage in an activated sludge treatment plant.
2. Activated sludge systems which incorporate reaeration of the
return activated sludge are more stable in treating this particular
combination of wastes. Of the four activated sludge processes
studied (conventional, step aeration, contact stabilization,
Kraus), the contact stabilization process proved to be the most
successful in treating this particular combination of wastes.
3. Filamentous sulfide bacteria growth in the mixed liquor was
successfully controlled by the continuous addition of 5-10 mg/1
of chlorine to the return activated sludge. Low dissolved oxygen
concentrations were not successful in controlling the filamentous
sulfide bacteria. The addition of chlorine to the return activated
sludge did not control non-filamentous bulking.
4. Nitrogen and phosphorus additions were required to achieve
satisfactory biological operation. There was no advantage to
adding the nutrients in the reaeration section as opposed to
the contact section of the activated sludge process.
5. Satisfactory operation was achieved at dissolved oxygen levels
between 0.5 and 1.5 mg/1.
6. It is more advantageous to bypass the mill effluents directly to
the secondary treatment unit than provide primary clarification.
7. During a consecutive period of four and one-half months contact
stabilization pilot plant operation, the BOD, TSS, and color
removal averaged 91%, 78% and 19%, respectively. Increased
TSS removals are expected in a full-scale final clarifier.
8. Total estimated costs for full-scale operation are as follows:
CAPITAL ANNUAL
O + M Capital Invest
Joint Facilities $31,127.000 $3,087,000 $3,705,000
Separate Facilities 37,796,000 4,496,000 4,496,000
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RECOMMENDATIONS
The following recommendations for future research activities are made:
1. Determine the optimum quantity of nutrients to be added to
maximize the process operation and minimize the quantity of
nutrients discharged in the effluent. Satisfactory operation
was maintained for extended periods at BOD: ortho phosphorus
(as P) ratios of 100:0.5.
2. Determine the minimal amount of chlorine addition to the return
activated sludge necessary to minimize the filamentous sulfide
bacteria population in the activated sludge.
3. Determine an effective means of greater color reduction through
the process.
4. Study the SVI test to determine the maximum permissible MLTSS
to still obtain meaningful values of SVI.
5. Investigate the occurrence of poor effluent quality associated
with poor settling, non-filamentous type activated sludge in
relation to:
a) BOD:N:P ratios
b) return activated sludge chlorination rates
c) high carbohydrate content in the influent sewage
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INTRODUCTION
History
The Green Bay Metropolitan Sewerage District (GBMSD) is a separate
and distinct municipal corporation created in accordance with Wisconsin
State Statutes in December, 1931. I1) Early in the developing stages of
the District, the following major policy decision was made with regard
to the pulp and paper industry;
As the integrated pulp and paper mills represented a large
flow volume and since primary treatment of these effluents
would produce little BOD reduction, it was mutually decided
to omit all effluents from this industry except sanitary wastes
generated by employees.
Interceptor sewers, a river crossing and a 9.0 MGD primary treatment
plant were completed by 1937. A trickling filter plant was placed in
operation in 1955.
In 1958, upon redefinition and enlargement of the policy decision
regarding pulp and paper mill effluents, joint treatment studies were
initiated between the Charmln Paper Products Company and the GBMSD.
This marked the beginning of joint industrial-municipal treatment
studies between the GBMSD and the pulp and paper industry of Green
Bay.
The studies during 1958 and 1959 concerned evaluation of the treatability
of Charmin yeast plant effluents with GBMSD (Metro) sewage using
trickling filters. These studies indicated that the combined wastes
required more filter capacity per pound of BOD removed than the
municipal wastes alone; on this basis the concept was uneconomical
and the studies were concluded at that time.
In 1964, joint treatment studies were again initiated between Charmin
Paper Products Company and the Green Bay Metropolitan Sewerage
District. (2> 3) At that time the GBMSD was formulating plans for
expansion and was considering the activated sludge process. Charmin
desired to study the treatment of dilute effluents from their pulping
processes and in-plant treatment systems. Therefore, laboratory
studies utilizing 15-liter reactors were begun in 1964. These studies
were expanded to a large-scale continuous-flow pilot plant study,
utilizing a contact stabilization package plant, to determine the treat-
ability of the combined wastes in a continuous-flow system. These
studies were concluded in 1966.
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The results of the studies between 1964 and 1966 showed that the
combined wastes were amenable to biological treatment. However,
the problem of separating the biological solids from the treated liquid
due to filamentous organisms had to be solved before a full-scale
plant could be built.
Realizing that additional studies were necessary to solve these problems
and also recognizing that the three remaining major pulp and paper
industries in Green Bay may be interested in a joint venture, the Green
Bay Metropolitan Sewerage District invited American Can Company,
Fort Howard Paper Company and Green Bay Packaging, Inc. , to join
with Charmin Paper Products Company and themselves in a joint
industrial-municipal research project. The relative locations of the
Mills and the existing sewage treatment plant are shown in Figure 1.
Present Research Program
Application was made by the GBMSD for a Research and Development
Grant from the Federal Water Quality Administration, U.S. Department
of the Interior; the GBMSD was awarded this grant in December, 1966.
The total budget for the project was $335, 000, of which 75% was funded
by the FWQA and Z5% was shared equally between the five participants.
The purpose of this research project was to determine the technical and
economic feasibility of jointly treating the influent to the present treat-
ment facilities of the GBMSD in combination with the weak effluents
from the pulping sections of the four pulp mills.
The proposed research program was to study the four activated sludge
processes (conventional, step aeration, contact stabilization and Kraus)
simultaneously for twelve months in four 1-gpm pilot, plants utilizing
the combined wastes. During this time the effluent quality, operating
parameters, design variables and cost relationships for each process
would be established. At the end of the first year, the most promising
process would be selected and studied in detail for a second year, during
which time refined design, operating and cost parameters for the
selected process would be obtained for a full-scale treatment plant.
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0 I t
te*LC IN MILI1
LEGEND
DISTRICT LIMITS
CD GREEN BAY PACKAGING, INC.
(2 CHARMIN PAPER PRODUCTS COMPANY
(3 AMERICAN CAN COMPANY
B) FORT HOWARD PAPER COMPANY
GREEN BAY
METROPOLITAN SEWERAGE DISTRICT
SERVICE AREA
FIGURE I PAGE 5
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WASTE CHARACTERISTICS AND JOINT
TREATMENT OPTIONS
Detailed descriptions of the effluents from each pulp mill and GBMSD
sewage are as follows:
American Can Company (Mill 1)
This is a calcium-base bisulfite pulping operation producing aspen
pulp. The effluent stream consists of condensate from the liquor
evaporation system which is composed mainly of acetic acid and
some formic acid plus other miscellaneous volatile organic acids.
It also contains the uncollectable liquors and effluent from chemical
pulping and bleaching operations which contain carbohydrates and
calcium lignosulfonates. The suspended solids are mainly fines and
fibers from pulp washing operations.
Charmin Paper Products Co. (Mill 2)
This pulp mill uses the ammonia-base sulfite pulping process on
regional hardwoods. The effluent is a composite of the dilute pulp
wash waters and condensate from the liquor evaporator system.
The BOD results primarily from volatile organic acids (acetic and
formic) in the evaporator condensate. The balance is made up of
carbohydrates and complex lignosulfonate compounds not collectable
in the counter-current pulp washing system. The suspended solids
are broken fibers, ray cells and other, almost collodial, solids
that are not retained in the primary system of mechanical and
flotation-type savealls.
Fort Howard Paper Co. (Mill 3)
The effluent from this plant consists of wastewaters collected from
the de-inking of waste paper and excess white water from paper
machines. The BOD is from the inks, starches, and other organics
removed from paper that is subjected to the de-inking process. The
suspended solids are the very fine clays and other filler materials
from the de-inked paper along with some fiber fines. Since the
effluent has already passed through primary treatment, only very
fine or neutral buoyancy particles remain.
Green Bay Packaging, Inc. (Mill 4)
This company uses the neutral sulfite semi-chemical pulping process
to manufacture unbleached board grade (high-yield) product. The
effluent consists of the excess white water discharge from the paper
making operation. The BOD loading is from spent neutral sulfite
semi-chemical liquor which is not collectable in the pulp washing
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systems. The effluent contains dissolved sodium salts of complex
lignosulfonic compounds together with smaller amounts of acetic,
formic, and butyric sodium salts. The suspended solids are
residual fibers not removed by drum filtration and flotation of the
excess pulping and papermaking effluents. As such, the suspended
material will range down to semi-collodial sizes.
Green Bay Metropolitan Sewerage District
The municipal sewage received at the treatment facilities is derived
from five municipalities having a connected population of approxi-
mately 110, 000 people and several •wet industries composed of two
large meat packing plants, two large vegetable canning operations,
a pickle processing plant, a tomato canning operation, and various
milk processing establishments.
The quantity and characteristics of each waste used for the final
full-scale plant design are shown in Table 1. More complete data on
the individual wastes are presented in Appendix C.
Joint Treatment Options
As shown in Figure 1 , Mills 1, 2, and 4 are located near the GBMSD
Treatment Plant while Mill 3 is located upstream approximately 31/2
miles. During the research project the assumption was that effluent
from Mills 1, 2, and 4 would be conveyed to the treatment plant in a
joint interceptor sewer constructed solely for that purpose. It was
further assumed that an interceptor sewer would be constructed for
Mill 3 effluent from the Mill site to a point approximately 1 mile from
the treatment plant where it would discharge into the existing GBMSD
interceptor sewer system.
In the initial planning of the project, major emphasis was placed on the
assumption that all Mills would participate in the proposed full-scale
joint treatment venture. Because of the costs for sewer construction,
it was assumed that of the four mills, Mill 3 would be most likely to
provide separate treatment facilities.
Treatment options studied were as follows:
Primary Clarification Studies
1. Each Mill alone.
2. Metro alone - average and simulated storm flow.
3. Mills 1, 2, and 4.
4. Mills 1, 2, 4 and Metro.
8
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AVERAGE MILL AND METRO WASTE CHARACTERISTICS
UTILIZED FOR FINAL FULL-SCALE PLANT DESIGN
H
er
(t
Mill 1
Flow, MGD 5.0
BOD, mg/1 1440
TSS, mg/1 240
NH3 as N, mg/1
Ortho phosphor us
as P, mg/1
PH
Mill 2 Mill 3 Mill 4 Metro Composite
5.0 13.25 0.6 30.0 53.85
720 600 2800 240 510
100 120 1000 180 175
19.4
1.6
6.8
OP
(D
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5. Mill 3 and Metro.
6. All Mills and Metro.
7. All Mills and Metro plus WAS return to Primary Clarifier.
Secondary Treatment Studies
1. Mills 1, 2, 4 and Metro - average flow*
2. Mills 1,2,4 and Metro - storm flow*
3. All Mills and Metro - average flow.
* Studies 1 and 2 were conducted with Metro only receiving primary
clarification; Mills 1, 2, and 4 were sent directly to the secondary
treatment unit.
10
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SCHEDULE OF MAJOR EVENTS
The major events which occurred during the research project are
summarized below to provide an overall view of the research schedule:
January 1 - June 1, 1967
Coordination and implementation of the grant award between the
municipal and industrial participants.
June, 1967
Began laboratory reactor studies on a combination of proposed
wastes to be fed to the pilot plants. Pilot plant design started.
August, 1967
Pilot plant construction began.
February 6, 1968
Started up pilot plants on Metro sewage.
February 27, 1968
Reached 100% feed of Metro and pulp mill wastes.
March, 1968
Aeration units became infested with filamentous organisms.
August, 1968
Concluded that the mixture of wastes was biologically treatable
although the problem of separation of biological solids from the
treated liquid still existed.
September, 1968 - January, 1969
Statistical experimental design conducted to assist in selection of
the most desirable process.
January, 1969
Chlorination of return activated sludge appeared successful for
controlling filamentous organisms.
February 1, 1969
Shut down pilot plants for cleaning and maintenance.
February, 1969
Conventional and step aeration units eliminated from further
consideration. Studies continued on the contact stabilization
and Kraus units.
11
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February 24, 1969
Started up pilot plants on Metro sewage.
March 21, 1969
Reached 100% feed of Metro and pulp mill wastes.
April, 1969
Chlorination of return activated sludge proven effective in controlling
filamentous organisms.
July, 1969
Contact stabilization unit selected as the most desirable unit.
September, 1969 - December 15, 1969
Extensive solids-handling unit process study conducted to gain
information on the disposal of sludge produced from the contact
stabilization process.
December 16, 1969
Pilot plants were shut down.
February 13, 1970
Presentation of the final cost estimate to the Steering Committee.
July i, 1970
Termination date of the research project.
12
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LABORATORY REACTOR STUDIES
Since there was no available information in the literature concerning
the treatability of this particular combination of pulp mill effluents
and municipal sewage, bench-scale laboratory reactors were operated
to obtain preliminary information concerning BOD and TSS removals,
nutrient requirements, potential filamentous microorganism bulking
problems, required detention times, etc.
The "fill-and-draw" reactors utilized in this study were similar to
glass carboys with the bottoms removed. The reactors were inverted
and placed in a support stand. Two lines were marked around the
circumference of each reactor; the top line indicated the total operating
volume of the reactors; the bottom line indicated that volume of mixed
liquor (return activated sludge, R) retained at each feeding. The volume
between the two lines represented the volume of sewage (feed, Q) added
at each "feeding". The recirculation ratio (R/Q) is the ratio of return
activated sludge (R) retained to the feed (Q) added.
Each reactor was aerated for 5-1/2 hours after the addition of the feed.
The aeration stone was then removed and the biological solids allowed
to settle under quiescent conditions for one-half hour. The supernatant
liquid was siphoned off until the liquid level reached the bottom line.
A fresh batch of feed was then added and the aeration stone was replaced.
Feeding times were 0400, 1000, 1600, and 2200. Once a day a
calculated quantity of the reactor contents was withdrawn and wasted
to maintain a relatively constant mixed liquor suspended solids con-
centration.
Laboratory analyses conducted on the final effluent were BOD, nitrogen
(ammonia, total organic, nitrite, nitrate),ortho plus condensed phosphorus,
pH and sludge volume index (SVI). Several of these analyses are a
direct function of the suspended solids concentration in the samples
and therefore are dependent not only on the quiescent-settling character-
istics of the biological solids, but also on the degree of care exercised
in removing the treated effluent. Therefore, a fill-and-draw reactor
can be used primarily for studying the treatability of wastewater, whereas
a continuous-flow reactor may also indicate potential problems due to
poor sludge settleability;
On July 8, 1967, a 15-liter fill-and-draw reactor, R5, was started on
Metro influent sewage. This sewage was settled for 10 minutes, a
portion of the supernatant was decanted, mixed, sampled for laboratory
analyses, and an appropriate amount then added to the reactor. Small
13
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quantities of each of the mill wastes were delivered to the GBMSD
laboratory weekly. They were added in gradually increasing amounts
to the Metro sewage, reaching 100% of the potential industrial feed by
August 1. The summary of reactor operations is presented in Table 2.
Average monthly operating data for R5 is presented in Table 3.
On August 11, a 5-liter reactor, R3, was started up to provide a
reservoir of mixed liquor when poor mixed liquor settling properties
developed in R5. The SVI in R5 had reached a high of 175 due possibly
to the increased BOD to volatile suspended solids ratio (also known as
food to microorganism ratio, or F/M ratio). R3 was started with
waste activated sludge taken from R5, and was initially fed only Metro
sewage. Average monthly operating data for R3 are presented in
Table 4.
A second 5-liter reactor, R4, was started on August 25; it received
the same feed as R5. It had an R/Q = 1.0 and was operated at a lower
biological solids concentration resulting in a higher F/M ratio. Average
monthly operating data for R4 are presented in Table 5.
Microscopic examinations were made on the reactors periodically. The
microscopic structure and arrangement of mixed liquor solids (floe)
differed greatly between the municipal-fed (R3) and the industrial-
municipal fed (R4, R5) reactors. An unusual biological growth in the
reactors was observed during August; lacking a positive identification,
it was referred to as "coral". In February, 1968, it was identified as
a "zoogleal" growth.
The return activated sludge volume of R5 was initially set at 5 liters,
(R/Q = 0.5). However, due to the poor settleability of the mixed liquor
solids, the clear supernatant volume after the one-half hour settling
period was less than the volume of sewage to be fed to the reactor.
Therefore, the recirculation ratio (R/Q) was then changed to 1.0,
August 16, reducing the feed volume to 7.5 liters.
A dissolved oxygen (DO) analysis was made on R5 during August. After
batch feeding of the unit, the DO remained at zero for a period of 15-30
minutes. The DO value then rose steadily until it reached 5-7 mg/1 at
the end of the 5-1/2 hour aeration period. This alternating aerobic-
anaerobic condition did not have any apparent effect on the organisms.
However, it may have been beneficial in reducing or eliminating certain
varieties of filamentous organisms. This DO profile may also explain
the previous experience of the GBMSD between 1964 and 1966, when
superior results were achieved in fill-and-draw reactors as compared
to continuous-flow pilot plants.
14
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LABORATORY REACTOR STUDIES
Date
Reactor 3 (R3)
Reactor 4 (R4)
Reactor 5 (R5)
a-
I—I
ffi
IV
OQ
t— '
Ul
7/8/67
8/1/67
8/11/67
8/16/67
8/23/67
9/13/67
9/25/67
10/13/67
5-liter fill-and-draw reactor
started on Metro sewage,
using waste activated sludge
from R5; R/Q = 0. 5
5-liter fill-and-draw reactor
started using waste activated
sludge from R5; same feed
as R5; R/Q = 1.0
Began adding chlorine after
each feeding. SVI is 70-80
SVI is 50-60
15-liter fill-and-draw
reactor started on Metro
sewage; R/Q = 0.5
100% Industrial plus
Metro sewage feed
reached
Changed R/Q to 1.0 due
to poor settling sludge
SVI is 70-80
SVI is over 100
SVI dropped below 100
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Date
OQ
'CD
11/1/67
11/16/67
Reactor 3 (R3)
12/Z/67
12/21/67
1/6/68
1/13/68
1/27/68
1/31/68
2/10/68
Reactor changed to contact
stabilization; unit; MLVSS and
feed at one-half of R5 to
obtain same F/M as R4 andRS
Reactor 4 (R4)
Reactor 5 (R5)
11/29/67 Filaments first observed
11/31/67
No filaments
Considerable number of
filaments
Trace of filaments
No filaments
Stopped chlorine feeding
No filaments
No change noted due to
stopping G\2 addition
2/12/68
Began feeding 2 mg/1 CU
after each feeding; SVI
69-123 between 11/1 and
11/16
Filaments first observed
Final effluent more turbid
since adding Cl^; no
major change in SVI
between 11/16 and 11/30
No filaments
Stopped addition of C^
No filaments
Filaments present
Considerable number of
filaments
Excessive number of
filaments present, inter-
fering with movement of
protozoa
Began adding 3 mg/1
-------
Date
Reactor 3 (R3)
Reactor 4 (R4)
Reactor 5 (R5)
2/13/68
2/16/68
2/17/68
2/20/68
2/21/68
2/22/68
2/23/68
2/27/68
2/28/68
Considerable number of
filaments
Decrease in filaments
No mixed liquor settling
problems. SVI average
below 100
1 liter of R5 mixed liquor
added to increase filament
concentration
Increase in filaments
SVI= 400
Excessive numbers of
filaments present
No filaments
SVI = 190, Reactor operation
discontinued.
Filaments first observed
Trace of filaments
Reactor operation
discontinued
Increased C\2 dosage to
6 mg/1
Increase in filaments
Increase in filaments
Decrease in filaments,
increase in larger, more
desirable organisms.
Added 30 mg/1 of C\2 a't
1600 feeding
Reactor operation
discontinued
TO
CD
-------
R 5, 15-LITER REACTOR
Laboratory Data
7/67
8/67
9/67
10/67
11/67
12/67
1/68
2/68
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
TSS,mg/l
%
Inf
157
214
106
149
192
72
181
232
140
203
256
120
213
308
112
233
408
108
262
388
136
251
368
84
Eff
13
23
4
26
314
2
21
38
6
32
52
8
42
115
16
43
132
14
31
68
4
34
98
4
Red
91.7
97. 3
83. 3
82.7
98. 3
63.6
88. 4
95.7
79. 8
84. 1
95. 5
74. 0
80. 5
92. 1
48.7
81.4
94. 6
41. 1
88. 2
98. 1
73. 5
86. 5
98. 4
66. 1
BOD, mg/1
%
Inf
350
485
130
532
708
330
566
735
419
564
900
453
653
862
538
603
710
436
592
755
258
586
690
510
Eff
7
11
5
19
136
6
9
13
5
17
31
12
29
63
12
25
60
12
18
42
5
19
46
5
Red
98. 0
98.9
92.3
96.4
98.7
77. 3
98. 4
99. 3
97.2
96.9
98. 1
90.2
95.6
98. 1
90. 2
95. 8
98.2
87.4
96. 9
99. 1
93.9
96. 8
99. 1
89.2
Aeration
Unit
TSS
4449
5520
3836
4631
5508
3848
4742
5632
3972
4663
5448
4232
4678
5820
3760
4520
5128
3420
4640
5528
3580
3480
5304
2428
VSS
3591
4276
3120
4092
4940
3380
4122
4856
3340
4059
4548
3620
4127
5156
3288
4050
4648
3192
4000
4776
3020
2962
4412
2116
%
Vol
81. 0
85. 5
70, 0
88.4
91.2
85.8
86. 9
89. 6
83. 5
87. 1
89.7
83.5
88.2
94.9
84.2
89. 6
97.4
85. 3
86.2
90.9
81. 6
85. 1
91.8
80.2
Wasted
Sludge
ml
2247
3500
1000
1426
3600
0
2018
3500
800
2161
3000
1000
2397
3500
1500
2558
3400
1500
2668
3600
1000
417
2700
0
SVI
255
290
200
600
830
270
485
780
300
467
410
260
419
630
320
417
620
300
591
860
320
832
970
650
V
op_
l£
w
55
64
47
129
175
61
100
148
59
90
123
69
92
132
64
127
184
64
127
184
79
243
330
162
N.HT
T.O.
AS NITROGEN
Inf
11.6
15. 5
6.8
17.6
26.7
8.6
24. 3
34. 9
10. 8
30. 2
37. 3
24. 3
23. 3
31.9
16. 5
23.2
34.8
14.2
21. 1
26. 0
18. 5
23. 2
26. 1
20.7
Eff
0
0
0
5.7
85.9
0
3. 3
10. 6
0
. 1
3. 6
0
0.8
6.0
0. 0
3.7
12.2
0
1. 3
9. 1
0
3.9
11.6
0
Inf
12. 0
17. 0
7.2
10.9
14.6
7. 1
12.8
17. 6
8.2
12. 6
15. 1
7. 7
13.4
18.9
8. 4
14. 1
19.7
9.2
1.4
19.7
9.2
12.9
15. 3
10.4
Eff
2.9
4.4
1. 3
5. 3
37. 3
2.9
5. 0
8. 3
3. 1
7. 5
12. 5
4. 5
7. 1
12. 5
4. 5
5.6
7. 5
4. 0
5. 1
12.3
3.7
5.7
9.2
4. 1
PHOS
O&C
AS P
Inf
6.0
8.7
. 8
4.7
6. 1
2. 0
5. 0
6.2
3. 0
5.2
6.8
2.6
4.6
6.0
2. 3
4.8
6.3
1.2
6.4
9.2
3.2
5. 0
6.7
3.4
Eff
2.49
8.7
. 14
.43
.79
. 10
.26
. 38
. 14
. 39
. 59
. 26
.30
.49
. 08
. 38
.73
. 11
.4
1.. 7
. 18
. 22
. 53
. 11
pH
Inf
7. 5
6. 1
7.6
6. 5
7.6
1. 5
7.7
6.6
7. 5
7. 0
8.2
3. 3
7. 2
7. 5
6.8
Eff
8. 2
7. 5
8. 1
7. 3
8. 0
7. 3
8.2
7.6
8. 2
7. 3
8. 5
7.4
7. 3
8. 3
7.4
%
Cell
N
8.8
9.8
6.7
8.7
9. 5
6.4
8.6
9. 9
5.7
8.7
13. 1
7. 5
9.2
9.0
7.6
8. 3
9-6
6.4
8. 6
8. 8
8. 3
BOD
NH3
30.7
51.9
12.4
33
66
19
25. 0
51. 0
13. 0
19
30
13
28
46
17
28
44
16
29
37
15
26
30
22
F
M
.29
. 39
. 18
. 29
. 53
. 16
. 28
. 37
. 16
. 28
. 43
. 12
. 32
. 42
. 24
. 30
. 36
. 22
. 30
.42
. 16
. 20
. 39
. 05
Q
L/D
29. 8
30. 0
27.9
30
30
30
30
30
30
30
30
30
30
30
30
15.9
30
5. 8
-------
R3, 5-LITER REACTOR
Laboratory Data
Date
Aeration Unit
TSS VSS %
mg/1 Vol.
Wasted
Sludge
ml
Settled Sludge
Volume
ml
SVI
TSS, mg/1
Inf Eff %Red
BOD mg/1
Inf Eff % Red
H
p
9-67
10-67
11-67
12-67
1-68
2-68
•a
P
CTQ
(D
Cs)
OO
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
5203
5564
4888
5258
5956
4612
2859
4916
1976
2550
3148
2160
2422
3468
1892
2515
3492
1808
4278
5228
3940
4260
4804
3820
2504
3928
1892
2293
2756
1976
2118
3240
1584
2122
2952
1536
82.2
83.6
78.7
81.0
86.4
78.8
87.6
95.7
79.7
89.9
97.4
87.0
87.4
93.4
77.3
84.4
91.8
76.4
345
800
0
440
1000
0
1019
2500
300
950
1500
300
731
1000
0
741
1200
0
316
430
210
220
260
190
115
215
90
189
270
120
195
300
130
202
400
140
61
83
41
42
50
37
41
50
25
75
112
45
82
148
51
81
115
55
261 58 77.8 649 48 92.6
408 132 88.0 710 72 96.1
120 28 67.4 561 25 88.3
TSS - Total suspended solids
VSS - Volatile suspended solids
-------
R4, 5-LITER REACTOR
Laboratory Data
Date
9-67
10-67
11-67
12-67
1-68
2-68
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Aeration Unit Wasted Settle
TSS VSS % Sludge Vol
mg/1 Vol. ml r
dSludge B.O.D. mg/1
ume SVI
Til , Inf. Eff % Red
4662 4079 87.5 673 362 79
5836 5056 90.8 1500 720 146
4172 3440 85.0 400 1
85 47
4233 3689 87.2 750 219 52 587 18 96.8
5152 4620 89.3 1000 2
85 68 900 30 98.0
3792 3316 84.7 600 140 34 462 12 94.1
4407 3863 87.7 925 233 54
7520 6704 93.9 1750 290 68
3660 3112 81.7 750 1
75 28
4157 3685 88.6 953 360 89
4956 4336 92.6 1150 700 179
3100 2480 80.0 450 1
4223 3695 87.5 1190 3
70 37
10 74
5895 5375 99.2 2300 890 237
2704 2308 81.5 0 1
80 51
4294 3653 85.1 1259 440 105
5620 4628 90.3 2000 820 229
2808 2384 79.9 700 270 55
pj
OP
0>
in
-------
On November 16, the addition of 2 mg/1 of chlorine to R5 with each
feeding was started to determine the effect on SVI. Other than a
noticeable increase in suspended solids in the final effluent, no signifi-
cant changes were noted. Chlorination was discontinued January 6.
During February, phase-contrast microscopic analyses were made on
a sample of mixed liquor from R5. These analyses showed that free
sulfur and a filamentous sulfur bacteria, which utilized sulfides as an
energy source, were present.
The problem of filaments and associated sludge bulking became quite
severe during February. Since the mixed liquor solids did not settle
to the desired level, the total amount of feed could not be added to the
reactor. As a result, the biological solids production decreased and
proper solids control could not be maintained. The F/M ratio dropped
from a desirable 0.3 - 0.4 to as low as 0.09.
On February 12, chlorine was fed at 3 mg/1 at each feeding in an attempt
to improve the settling characteristics of the mixed liquor. By February
17 no visible improvements were observed, therefore, the chlorine dosage
was increased to 6 mg/1. On February 27, the density of filaments in
R5 had decreased, and larger, more desirable forms of microorganisms
were observed in increasing numbers.
As R5 was to be discontinued on the 28th, it was decided to experiment
with a stronger chlorine dosage. On February 27 a 30 mg/1 dose of
chlorine was added to the mixed liquor prior to shutting off the air for
the one-half hour settling period. The supernatant liquor did not contain
residual chlorine after the one-half hour period. The reactor contents
were then siphoned off to the bottom line which permitted the full volume
of feed to be added. In so doing, about 3-1/2 to 4 liters of activated
sludge were wasted. Operators were then instructed to continue to
draw off to the bottom line, even if it meant including solids in the final
effluent, and to continue feeding the full volume of feed to maintain a
1:1 recirculation ratio. An improvement in the biological solids
settleability was noted the same day.
The average R5 laboratory data for February are misleading as they
indicate good BOD and suspended solids removals; however, had the
required liquid volume been removed, rather than just the supernatant,
the concentration of solids in the final effluent would have been sub-
stantial, resulting in laboratory data which would have shown poor
performance of the reactor.
On November 1, R3, receiving municipal sewage only, was converted
26
-------
to the contact stabilization process, and began receiving the combined
industrial-municipal feed. In order to maintain the same F/M ratio
as R4 and R5, the mixed liquor solids concentration of R3 was reduced to
1/2 of the previous value and the unit was fed at alternate 6-hour periods.
At the end of the first 5-1/2 hour period, the reactor contents were
settled in the same manner as the other reactors and the supernatant
was withdrawn. During the subsequent 6-hour period only the return
activated sludge was aerated. At the end of this 6-hour period the
feed was added to the reactor and again aerated for 5-1/2 hours. This
cycle was continuously repeated thus simulating the contact stabilization
process.
Although R3 did contain some filamentous organisms, settling problems
did not occur during February. On February 21, 1 liter of R5 mixed
liquor was added to R3 to purposely increase the filament population in
an attempt to create poor settling conditions; an increase in the settled
volume (to 400 ml) was recorded on February 23. However, by
February 28, the settled volume had reduced to 190 ml which was
within the normal range of prior operation. R3 was discontinued at that
time. R4 was also discontinued February 28. Although this reactor
did develop some filaments it did not have the severe problems that
R5 experienced.
An extensive analysis of system performance was not conducted on the
three reactors. The average values for mixed liquor total suspended
solids (MLTSS), SVI, and BOD and total suspended solids (TSS) removals
(excluding the February, 1968 data for R5 only) are as follows:
Reactor
R3
R4
R5
MLTSS
mg/1
3468
4329
4618
SVI
64
76
99
BOD, mg/1
In
649
587
551
Out
48
18
18
% Red
92.6
96.8
96.9
TSS, mg/1
In
261
200
Out
58
30
% Red
77.8
85.3
This information confirms that this particular combination of pulp mill
effluents and Metro sewage is biologically treatable in small laboratory
reactors. However, the problem of filamentous organisms did occur
which would make a continuous -flow plant inoperable. Therefore, the
question of the treatability of this combination of effluents remained to
be answered.
On February 28, two 5-liter reactors, RIP and R5P, were started up in
27
-------
the pilot plant room. RIP was fed Metro sewage only and was operated
in the normal manner discussed for R5. The industrial-municipal feed
to R5P was preaerated for 5-1/2 hours in an attempt to oxidize any
sulfides present to a higher ionic form, thus inhibiting the growth of
filamentous sulfur bacteria.
R5P was started up utilizing five liters of R5 mixed liquor. Improved
settling of the biological solids was noted immediately upon startup as
compared to the previous poor settling characteristics of R5. This
immediate improvement could have been due to the 30 mg/1 dosage of
chlorine to R5, February 27, and not the preaeration of the feed to
R5P. However, it was concluded that the continued good settling
characteristics of the mixed liquor was attributable to the preaeration
of the feed. The reactors were continued in operation through January, 1969,
The reactors were fed four times daily. Mixed liquor suspended solids
analyses were made daily and wasting rates adjusted accordingly. The
reactors operated quite well as compared to the pilot plants where
problems were encountered due to poor sludge settleability. This
confirms the fact that the treatability of a waste can be determined in
a fill-and-draw reactor, but that the problems associated with the
settleability of the sludge and resultant carry-over of solids can best
be determined in a continuous-flow system.
The occurrence of filamentous organisms in the reactors was a prelude
to the problems forthcoming in the operation of the pilot plants. The
filamentous growth problems encountered in the pilot plant operation,
the identification of the filaments, and the methods recommended for
control of the filaments are discussed in detail in subsequent sections
of this report.
28
-------
PILOT PLANT DESIGN AND CONSTRUCTION
The location selected for the pilot plants was a storage area inside the
Green Bay Metropolitan Sewerage District treatment plant. The room
dimensions were approximately 22" x 44' in plan, and the clear height
varied from 9' to 12'6".
During the previous research studies in 1966, a continuous plug-flow
pilot plant was assembled utilizing six 55-gallon drums in series.
However, because of space requirements and questionable mixing
regimes, it was decided to construct rectangular tanks with large
height to width ratios for this current research program.
The preliminary design of the pilot plants was based on the following
parameters:
Total Flow to Four Pilot Plants, GPM:
Minimum - 2.85
Average - 4.00
Maximum - 5.72
The pulp mill component was assumed constant at 1.85 gpm.
Storage Tanks
Maximum design head room = 8'; maximize volume for floor
area available.
Primary Clarifier
Overflow rate = 600 gpd/ft2; detention time = 2 hours.
Aeration Tanks
Conventional, Step Aeration, Contact Stabilization
MLTSS = 3330 mg/1; 75% volatile solids content; return activated
sludge (RAS) = 10, 000 mg/1; R/Q = 0.5; detention time on
conventional unit approximately 6 hours at maximum flow.
Kraus
MLTSS = 3380 mg/1; 70% volatile solids content; RAS = 10,000
mg/1; R/Q = 0.5; flow to nitrifying tank = 0.015 x average Q.
All Plants
F/M between 0.3 and 0.5 (BOD/MLVSS).
Final Clarifier s
Overflow rate approximately 500 gpd/ft2; solids loading approxi-
mately 20 Ib/ft2/day.
29
-------
Based on these parameters a 10-cell aeration tank (each cell = 1' x 1'
x 7') was chosen for each plant. Removable, watertight baffles
provided the necessary flexibility for volume changes.
An artist's rendition of the pilot plant facilities is presented in Figure 2,
The floor plan and flow schematic are illustrated in Figures 3 and 4
respectively. An As-Built drawing is in Appendix A. Photographs of
various items of the pilot plant are illustrated in Figures 5 through 6.
Fiberglass Mill Effluent Storage Tanks and Mixers
Boston motorized gear reducers, stainless steel shafts, and wooden
paddles were used to construct mixers for the storage tanks. A nylon
bearing support, which was molded into the bottom of the tank to
support the mixer, gave excellent performance. There were no
problems with the fiberglass tanks and mixing units during the 22
months of operation.
High-speed mixers were originally planned for the storage tanks. How-
ever, it was felt that excessive aeration would occur resulting in a
change in waste characteristics.
Pumps
Three basic types of positive displacement pumps were used; Brosites
6-in-l pumps, Jabsco flexible-impeller pumps, and Viking gear pumps.
Three Model O Brosites pumps (500 mis/minute/tube maximum) and
one Model OA Brosite pump (1000 mis/minute/tube maximum) were
used in the pilot plant operations. The Model OA and two Model O
pumps were used for mill waste pumping. The third Model O unit
was utilized to pump miscellaneous flows such as nutrients, chlorine,
digester supernatant and waste activated sludge.
Two sizes of Jabsco pumps were used; Model B-37 (3/8 inch) and Model
JC (1/2 inch). The Model JC pump was utilized for variable speed
pumping of Metro sewage from the grit chamber room to the pilot plant
room. The Model B-37 Jabsco pumps were used for pumping return
activated sludge from the final clarifiers to the aeration tanks.
As the Jabsco pump did not maintain consistent pumping rates when the
RAS became quite concentrated, a Viking Gear Pump (Model FH 32, 1/2"
suction and discharge, 3 gpm at 1800 RPM) was installed in place of one
of the Jabsco pumps during the last 6 months of pilot plant operation.
30
-------
c
m
ro
CD
m
(M
GREEN BAY
METROPOLITAN SEWAGE DISTRICT
MUNICIPAL-INDUSTRIAL
WASTE TREATMENT RESEARCH
FOUR ONE-GPM ACTIVATED SLUDGE
TREATMENT PROCESSES
FEDERAL WATER POLLUTION CONTROL ADMINISTRATION PROJECT 11060 EDX
PERSPECTIVE DRAWING OF PILOT PLANTS
-------
V /' X /' I I I I I I I
)< )< CONTACT STABILIZATION
S\l/\l i i i i i I i
UOOO-™ ,,* T
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
—1>— PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
^^ POSITIVE DISPLACEMENT PUMP
£2 CELL FILLED WITH TAP WATER i {DEAD CELL)
^—DIGESTER SUPERNATANT FEED SYSTEM
GREEN BAY METROPOLITAN SEWERAGE DISTRICT
INDUSTRIAL-MUNICIPAL RESEARCH PROJECT
FLOOR PLAN - PILOT PLANT
ACTIVATED SLUDGE TREATMENT PROCESSES
DONOHUE B ASSOCIATES,INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
BROSITES PUMPS
RAPID-MIX TANK 8 SPLITTER BOX
SPLITTER BOX
AERATION TANK 8 BAFFLES
PILOT PLANT EQUIPMENT PHOTOS
FIGURE 5 PAGE 37
-------
FINAL CLARIFIERS 8 FINAL EFF SAMPLERS
WAS VALVES 8 TIMER
WAS SOLENOID VALVE
FINAL EFFLUENT SAMPLERS
PILOT PLANT EQUIPMENT PHOTOS
FIGURE 6 PAGE 39
-------
This pump performed quite well, maintaining consistent pumping rates
as the concentration of RAS varied.
Flow Meter
A Foxboro 1-1/2 inch magnetic flow transmitter and accompaning
indicator-recorder-totalizer were utilized to measure the total flow
through the four plants. The instrument required calibration several
times but basically worked quite well. It was also necessary to
occasionally put a voltage of 110 volts across the meter probes which
extend into the liquid flow to remove grease and other materials that
had accumulated on the probes.
Aeration Tanks
There was considerable difficulty in solving the problem of sealing the
individual baffles in the aeration tanks. Since the cells which were not
in use were filled with tap water to equalize the hydraulic pressure on
the division baffle, it was necessary to have a water-tight seal to prevent
intermixing of tap water and mixed liquor. The solution was to use a
1/8 - inch thick, single-piece PVC baffle with a flexible PVC gasket
sealed to the edge of the baffle. Stainless steel channels were mounted
to the sides and bottoms of each aeration tank at one-foot intervals.
The baffles were then placed into the channels forming a relatively
water-tight seal.
Air Compressor
The primary air compressor was a Spencer Turbo Compressor; (170
scfm at 3500 rpm). The standby air compressor was a Yeomans
positive displacement, multi-cellular, high speed rotary air compressor,
(Model 45, 70 scfm at 1750 rpm). The compressed air passed through
two Microclean (Model 1B2G) air line filters. During the research
project the Yeomans unit was never utilized as the turbo compressor
operated continuously with no problems.
Air Flow Meters, Valves and Diffusers
A Wallace and Tiernan glass tube Varea-Meter was installed on the air
header to each aeration tank and needle valves were used for individual
air control to each cell.
40
-------
Filtros porous diffuser stones were obtained for diffusing air into the
mixed liquor, and were sealed with an RTV silastic material into 10"
square x 2" deep stainless steel pans leaving a 1" plenum chamber
beneath the stone. However, shortly after plant startup the sealant
proved unsatisfactory for this application. Many different adhesives
were tried but none were successful in retaining a bond to the stainless
steel. As an alternate solution, a pan was made from PVC material
and a porous stone bonded to the pan with an epoxy adhesive.
Shortly after startup, foaming problems developed on the surface of
the aeration tanks due to the very fine bubble diffusion. In order to
minimize the foaming, all diffuser stones were removed and replaced
with a hose extending to the bottom of each aeration cell which provided
adequate coarse-bubble aeration.
Sampling System
Continuous composite samples, proportional to the total flow through
the pilot plants, were taken of the primary influent, primary effluent,
and four final effluents. Each sampler consisted of a rotating arm and
cup mounted above a rectangular box inserted in the liquid flow line.
Pictures of the samplers are shown in Figure 6. An electrical
schematic diagram of the sampling system is shown in Figure 7.
Miscellaneous Feeding Systems
As it was difficult to maintain accurate low flows when utilizing a
Brosites pump to feed dilute solutions of various liquids to the pilot
plants, another feeding system was devised. The solution to be fed
was continuously pumped through a sampling box. A continuously
rotating cup dipped into the box and transferred a portion of the solution
to a trough leading to the desired location.
Two other feeding systems used were:
1. An Essex Brass Corporation "Sight Feed Lubricator" was
utilized to feed a defoaming agent dropwise into the front
section of the primary effluent splitter box.
2. A 1000 ml glass intravenous solution bottle with associated
fittings and feed controls was used temporarily as a nutrient-
feeding system.
41
-------
ELECTRICAL SCHEMATIC FOR PROPORTIONAL SAMPLERS
MAGNETIC
FLOW
METER
INTERMITTENT
ELECTRICAL SIGNAL
TO TOTALIZER MOTOR
NORMALLY OPEN
CAM-ACTIVATED
SWITCH
TIME
DELAY
RELAY
o
c
10
|TJ
SOLENOID
SWITCH
TOTALIZER
MOTOR
MOV.
A.C.
MERKLE-KORFF
O.I R.PM. MOTOR
110 V.
A.C.
MERKLE-KORFF
12 R.RM.
SAMPLER MOTOR
O
ni
OJ
-------
Labor and Equipment Costs
The first items of pilot plant equipment were moved into the pilot plant
room October 18; pilot plant startup with sewage was February 6, 1968.
The pilot plant equipment costs, exclusive of labor, are summarized
in Table 6. Approximately 2500 man-hours were required to construct
the pilot plant facilities.
44
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PILOT PLANT EQUIPMENT
Unit Cost
Brosites, Jabsco and Viking pumps and related speed
controllers and spare parts $ 4,140
Mill effluent storage tanks and mixers $ 7,560
Preliminary treatment for grit removal $ 70
Primary clarifier $ 1,060
Pilot clarifier--' $ 600
Aerationtanksandbaffl.es $ 2,250
Diffused aeration system including porous stones, air
flow meters, piping and valves $ 1,080
Final clarifiers $ 3,740
Pilot digesters $ 200
Miscellaneous including sampling system, electrical
switchgear, miscellaneous piping and maintenance items- $ 2, 300
TOTAL $23,000
Table 6 Page 45
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LABORATORY STAFF, EQUIPMENT,
PROCEDURES AND DATA REDUCTION
Since the research project was short in duration, it was difficult to
obtain qualified laboratory technicians. Therefore, individuals were
trained as necessary to meet the qualifications and responsibilities of
the particular position in question. The schematic of full-time and
part-time personnel is illustrated in Table 7.
The laboratory was operated 6 days per week. Samples collected on
Sunday were held over and analyzed on Monday. As estimate of the
number of routine tests made during a typical month (May, 1969) is as
follows:
BOD --- 440
COD 30
Nitrogen analyses 225
Phosphorus analyses 100
Solids Analyses 1000
These estimates do not include the laboratory analyses associated with
the special studies being conducted at the same time. The major
laboratory equipment utilized for conducting the analyses is presented
in Table 8.
The following tests were made routinely:
1. Biochemical oxygen demand - (BOD)
2. Chemical oxygen demand - (COD)
3. Ammonia, nitrite, nitrate nitrogen
4. Total organic nitrogen (biological cell nitrogen)
5. Ortho and total phosphorus
6. Solids analyses
A. Total suspended and volatile suspended solids on influents
and effluents - Gooch crucible method
B. Total, total suspended and volatile suspended solids on
sludges - Solids by difference method
Analyses for BOD, COD, and total organic nitrogen were conducted as
specified in the 12th edition of "Standard Methods for the Examination
of Water and Waste Water"(4). The procedure used for suspended solids
analyses is as presented in Standard Methods with a Reeve Angel, grade
934AH, 2.4 cm, glass fiber filter used in lieu of an asbestos mat. The
procedures for nitrogen and phosphorus are presented in Appendix B.
47
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PROJECT PERSONNEL
H
P
•ti
p
-------
LABORATORY EQUIPMENT
Item
Model
Manufacturer
en
oo
p
oq
CD
in
Calculator-Computer Epic 3000
Balance-Christian
Becker
Balance-Sartorius
Dis s olved Oxygen Mete r
and Probe
Dissolved Oxygen
Recorder
Oven
Furnace
pH Meter
Specific Ion Meter
Sulfide Probe
Style AB-1, Serial#A 13586
0-200 grams capacity
Model 2403, Serial#135222
Model 54
Model 80
Monroe International, Inc., Orange, New
Jersey
Christian Becker, Clifton, New Jersy
Brinkman Instruments, Inc., Cantiague
Road, Westburg, New York
Yellow Springs Instrument Co., Inc. ,
Yellow Springs, Ohio
n 11
Model OV-484a, Serial #Q-A1753 Blue M Electric Co. , Blue Island, 111.
Model E-555C-1, Serial
#MF 564V
n n
pH Recording Meter Model 30 cordless
Zeromatic II, Model 96A,
Serial #009604-1000904
Model 404
Model 94-16
Analytical Measurements, Inc., 31 Willow
St., Chatham, New Jersey 07928
Beckman Instruments, Inc., Fullerton,
California 92634
Orion Research Inc ., 11 Blackstone St. ,
Cambridge, Mass. 02139
-------
cr
i—'
(D
00
TO
CD
Ul
U)
LABORATORY EQUIPMENT
(Continued)
Item
Model
Manufacturer
Process Carbonaceous
Analyzer
Micro-Kjeldahl
Distillation Apparatus
Heating Mantle
Variable Autotrans-
former
No. 1389364, Range: 0-1000
mg/1 Total Carbon; Leeds
and Northrup type H Strip
Chart; Model IR 315 Infrared
Analyzer
Keeny Still
5000 ml flask
2PF1010
Beckman Instruments, Inc., Process
Instruments Division, Fullerton, Calif.
92634
Erway Glass Blowing, 686 Oak St.,
Oregon, Wisconsin 53575
Glas-Col. Apparatus Co., 711 Hulman
St. , Terre Haute, Indiana
Staco, Dayton, Ohio
Spectrophotometer
Spectronic 20, Serial No,
3493 4B
Bausch & Lomb, Inc., Rochester, New
York
Phase Contrast
Microscope
AO Series 10 Phasestar
Scientific Instrument Division; American
Optical Corporation, P.O. Box 66499,
Chicago, Illinois 60666
-------
The following special tests were conducted during the research project:
1. Color
2. Filterability index - (F.I.)
3. Oxygen uptake rate
4. Oxygen transfer
5. Specific filtration resistance - (SFR)
6. Sulfides
7. Total carbon - (TC)
Nitrogen Analyses
Prior to the research project the GBMSD laboratory routinely ran
ammonia, nitrate and total organic nitrogen as presented in the llth
Edition of Standard Methods. These methods were satisfactory for the
normal mixture of domestic and industrial wastes received at the
treatment plant and for the research conducted jointly with Mill 2
between 1964 and 1966. However, upon starting the laboratory reactors
in 1967, it was found that the nitrate procedure (phenoldisulfonic acid
method) could not be used for the reactors containing combined Mill and
Metro wastes.
The Standard Methods procedure for the nitrate determination requires
that nitrites be converted to nitrates, and that a parallel test for
nitrites be made to obtain, by difference, the true value of nitrates.
Hydrogen peroxide and potassium permanganate were tried but neither
was satisfactory for converting the nitrites to nitrates. The potassium
permanganate was especially troublesome, causing a black precipitate
in the sample which did not dissolve when the phenoldisulfonic acid and
ammonium hydroxide were subsequently added. The nitrite-nitrate
procedure satisfactorily measured these components in the samples
obtained from the laboratory reactor receiving Metro sewage only.
Therefore, the problem was apparently due to interferences present
in the Mill effluents.
Project consultants and the Pulp Manufacturer's Research League were
contacted for assistance in developing an alternate nitrate procedure.
Each responded with a number of suggested methods to solve the
problem but none of those proposed had ever been used to analyze this
particular combination of wastes. Most of the recommended procedures
also required some form of pretreatment to remove the color inter-
ferences. (The normal procedures for color removal listed in Standard
Methods were not successful in pretreating this combination of wastes
to remove the color.) Limited nitrite and nitrate data were subsequently
obtained on the reactors by using a combination of methods, but the
54
-------
results were not consistent. Due to the lack of time to investigate the
problem in depth, no nitrite or nitrate data were obtained for the pilot
plants during the first year of operation.
In October, 1968 two additional procedures for measuring forms of
nitrogen were discovered:
1. A similar FWQA research project at Erie, Penn. utilized an
Orion Specific Ion-Nitrate Probe to measure nitrate. They did
not attempt to measure nitrites. (5)
2. Studies at University of Wisconsin, Wausau, were being
conducted in which nitrogen analyses were being run on highly
colored liquids such as manure pile seepage. The equipment
utilized was a Micro-Kjeldahl Distillation Apparatus.
Due to previous problems associated with specific ion probes regarding
sulfide measurements, the decision was made to first investigate the
procedures utilized at the University of Wisconsin, Wausau.
Samples of the most troublesome combinations of effluents were taken
to Wausau in February, 1969 and analyzed under the direction of Dr.
Crabtree '• There were no analytical problems in determining the
ammonia, nitrite and nitrate concentrations in each of the samples.
The procedure of direct distillation with the Micro-Kjeldahl unit,
presented in Appendix B, solved the problem of measuring nitrite and
nitrate nitrogen in the combination of mill wastes and GBMSD sewage.
All nitrogen analyses were performed during the second year of pilot
plant operation.
Phosphorous Analyses
For this research project, the phosphorus in a given sample was assumed
to be composed of orthophosphorus, condensed phosphorus and organic
phosphorus; the sum of which was the total phosphorus. Ortho plus
condensed phosphorus was the primary phosphorus test conducted by
the GBMSD laboratory prior to the research project. The procedure
utilized was adopted from the Association of American Soap and
Glycerine Producers Committee report. ( ^) It is basically a modifi-
cation of the solvent extraction procedure as presented in the Water
Analysis section of Standard Methods. There was uo procedure presented
in Standard Methods for the analyses of phosphorus in sewage or
industrial wastes at the time this research was conducted.
Ortho plus condensed phosphorus analyses were made on the laboratory
55
-------
reactors periodically. Upon startup of the pilot plants, the decision
was made to determine ortho and total phosphorus separately to permit
BOD:N:P ratios to be calculated in the raw and nutrient-supplemented
primary effluent.
This procedure is a slight modification of that for ortho plus condensed
phosphorous; potassium persulfate is added in the digestion step to
insure complete conversion of total phosphorus to ortho phosphorus(S)
This procedure is presented in Appendix B.
Solids by Difference
When making solids analyses on samples with a high solids concentration,
(mixed liquor, return and waste activated sludges) it was necessary to
utilize a procedure which was accurate and yet rapid. The procedure
utilized was developed by Drs. Polkowski and Boyle during 1964-6612,3).
Color
Dr. Wiersma " ' provided assistance in developing a suitable procedure
for color analyses. Samples of the final effluents were analyzed on a
spectrophotometer at wave lengths between 375 and 610 millimicrons.
A plot of absorbance versus wave length showed a decreasing absorbance
with increasing wave length. Therefore, during the first year, the
absorbance and transmittance at 375,420,525 and 610 millimicrons were
recorded. During the second year the 375 millimicron wave length was
selected as the standard upon which all color measurements were made.
A platinum cobalt standard, which had the equivalent of 500 color units,
was used to prepare a curve of percent transmittance versus color units
at 375 millimicrons. With this curve the color, in standard color units,
could be obtained for the given sample. This procedure is presented
in Appendix B.
Filterability Index Test
This test, which was developed to measure the relative ability to filter
the four final effluents, was utilized as a criterion in selecting the most
desirable process.
The procedure used was adapted from the work of Hahm *0). The
equipment utilized during the project required that two persons conduct
the analyses to obtain the best accuracy; the interpretation of the results
56
-------
was quite subjective and the information gained was of relative value
only. This test was utilized only during the first year of research.
Oxygen Uptake and Transfer
The procedures for oxygen uptake and oxygen transfer are presented in
Appendix B. Small laboratory reactors, containing mixed liquor from
the respective pilot plants, were utilized to obtain oxygen uptake and
transfer values between February, 1968 and August, 1969. During the
fall of 1969, when the contact stabilization process was being studied
intensively, the oxygen uptake analyses were conducted in the aeration
cells of the particular pilot plant being analyzed.
Specific Filtration Resistance
This procedure was adapted from the method presented by
Sulfides
Due to the presence of filamentous sulfur bacteria in the pilot plants
during March, 1968, it became necessary to measure the quantity of
sulfides in the various streams associated with the pilot plants. A
specific ion-sulfide probe manufactured by Orion Research, Inc. was
used with a Beckman ZeromaticpH meter and single-junction reference
electrode. Millivolt and pH readings were obtained to determine the
total sulfide content.
Since a single-junction rather than a double-junction reference probe
was erroneously used between March, 1968 and February, 1969, the
values obtained during the first year are primarily useful as relative
values of the sulfide concentration. However, this information led to
the decision to begin chlorinating the return activated sludge streams
of the conventional and step aeration units in January, 1969.
An Orion Model 404 Specific Ion Meter was used for pH and sulfide
measurements during the second year; a double-junction reference
electrode was also obtained for making correct sulfide measurements.
The Sulfide values obtained during the second year are considered to be
as accurate as the limits of the equipment and procedure would permit.
Based on information provided by Orion Scientific, Inc. , measured total
sulfide concentration values less than 10"' moles/liter (.003 mg/1)
57
-------
would be highly questionable. In regard to the minimum limits of
detection of total sulfides in an unknown, Dr. Lee(12) stated that the
minimum concentration accurately measurable would be about 0.01
mg/1 as total sulfides when measuring pH to the nearest 0.1. He
further stated that values less than 10-4 mg/1 total sulfides should be
reported as a trace, negligible, or value in question.
Although Orion Research, Inc. has developed procedures for a direct
meter readout of total sulfide concentration called the "Known Addition
Method" and the "Known Subtraction Method", it was the conclusion of
the project laboratory staff and Dr. Wiersma, who assisted in developing
the procedure, that the procedure utilizing millivolt and pH measurements
is much simpler and much less cumbersome than any other procedure
developed to date. This is primarily because the "Known Addition" and
"Known Subtraction Methods" require a multiplicity of standards when
the range of the total sulfide concentration in the unknown is not known
and the fact that these standards are not stable for long periods of time.
In summary, the measurements of sulfides was a very difficult procedure
to accurately develop for the research project. However, once the
proper equipment had been obtained, and the procedure had been
developed satisfactorily, the measurement of the sulfides became a
routine test. The procedure for total sulfide concentration measurements
is in Appendix B.
Total Carbon
A Beckman Process Carbonaceous Analyzer was used for total carbon
analyses. The analyzer had a range of 0 to 1000 mg/1 total carbon, and
utilized a Leads and Northrup type H strip chart and a Model IR315
infrared analyzer. A manual injection procedure was utilized.
The following samples were analyzed periodically for total carbon (TC)
during 1968 and 1969:
1. Four Mill wastes.
2. Metro sewage.
3. Combined primary clarifier influent.
4. Primary clarifier effluent.
Total carbon analyses were made on final effluents during the first year.
The BOD/TC ratios obtained were so variable that no correlation was
apparent. Therefore, no final effluents were analyzed for total carbon
during the second year.
58
-------
During August, 1968, preliminary studies were conducted to remove
inorganic carbon by acidifying the samples to a low pH and then heating
the samples to drive off CO2. The procedure was quite time-consuming
and did not appreciably change the total carbon content of the sample.
Blending the individual samples of Mill wastes, Metro sewage, combined
primary influent, and primary effluent in a Waring Blender with a
special high-shearing head was also investigated; there were no
significant differences in the total carbon values obtained for the
blended and unblended samples. Therefore, the decision was made to
analyze the samples with no pretreatment, acknowledging the fact that
there may be some inorganic carbon present which is measured with
the organic carbon in the sample. Therefore, all values presented in
this report are as total carbon, not total organic carbon.
The results of the correlation studies between BOD, COD, total carbon,
and total suspended solids are presented in the section entitled Total
Carbon Correlations.
Laboratory Data Reduction
As the laboratory analyses were conducted, the results were entered on
work sheets. Sample computer printout laboratory data sheets are
presented in Appendix B.
Selected parameters were plotted on graph paper to aid in monitoring
the daily operation of the pilot plants. The parameters plotted during
the first year were:
1. Primary effluent: pH, BOD, COD, BOD:N:P
2. Conventional process:
Aeration tank:
MLVSS - Cell 10
RAS - TSS
Settled Sludge Volume - SVI Test
SVI
F/M ratios -.BOD/MLVSS, COD/MLVSS
Final effluent:
BOD, mg/1 - filtered and unfiltered
BOD, % reduction - filtered and unfiltered
TSS, mg/1
Final clarifier sludge level
59
-------
3. Step aeration process:
The values graphed for the step aeration process were
identical to the conventional process; in addition the MLVSS
for Cells 4, 6 and 8 were also plotted.
4. Contact stabilization
The information plotted was the same as for the conventional
process; in addition the MLVSS of the last cell of the
reaeration section was also plotted.
5. Kraus process:
The items plotted were the same as for the contact stabiliza-
tion process.
In addition to the graphs of selected parameters, a summary of the daily
operational logs and the periodic microbiological examinations was also
chronologically recorded on graphs for each process.
During the second year, the same parameters were plotted for the
contact stabilization and Kraus processes with the following exceptions:
1. The F/M ratio, COD/MLVSS, was not plotted for either process.
2. The final effluent-filtered BOD was not plotted for either
process.
An example of the graphs is presented in Appendix B.
In the early stages of the research project, the possibility of compu-
terizing the data obtained from the laboratory analyses to perform
various correlation studies was evaluated and the decision was made to
proceed with this method of data reduction. An IBM 1401 computer was
used with the Auto-Coder computer language. This language was
selected in" lieu of Fortran because of the availability of programmers
locally. A program was developed which printed out the laboratory
data in a facsimile of the laboratory data sheets. The format of the
laboratory data sheets was changed for the second year, necessitating
a considerable revision of the Auto-Coder program.
One benefit of computerizing the data was the ability to cross check the
calculations made by laboratory personnel and the computer. Due to
the large quantity of laboratory data generated, the possibility of errors
was great. By cross checking the computer data with the laboratory
data sheets, errors were discovered both on the computer printout and
on the laboratory data sheets thus permitting the appropriate corrections
to be made.
60
-------
Having laboratory data neatly typed on a computer printout sheet is ideal
for clear photo-reduction and incorporation into reports as desired.
However, in retrospect, computerization of the data was not justified
in this project due the fact that: (1) there were a considerable number
of variations in the laboratory forms between the first and second
year, (2) there were many variations in plant operation which required
changing the volumes of the aeration sections and the flow rates thus
necessitating a change of constants involved in the computer programs,
and (3) the Auto-Coder language was not easily adaptable to make
correlations of the laboratory data obtained. It is recommended that
computerization of laboratory data only be considered under the conditions
were (1) a scientific language is used, (Z) a minimum of individual
processes generate the data and (3) these processes be limited to a
minimum of operating changes during the period of study.
61
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PILOT PLANT OPERATION
Mill Effluent Transportation and Storage
Between June and August, 1967, laboratory studies were conducted to
determine if there were any significant changes in the initial BOD and
pH values of the Mill wastes due to long-term storage. It was concluded
that changes in these parameters due to storage were not significant
when compared to the expected variations in waste characteristics over
the period of the project. Mill wastes were hauled to the pilot plant
site in a 5, 000 gallon tank trailer and pumped into storage tanks for
use in the pilot plants as desired.
Mill Effluent Contracts
As the GBMSD was the sole grant applicant, it was necessary to develop
contracts between the Mill participants and the GBMSD to provide for
the construction of necessary pumping and storage facilities at the Mill
site and disposal of this equipment at the conclusion of the project.
The procedure which was developed is as follows:
1. Each of the Mills installed the necessary equipment to load the
tank trailer with characteristic Mill wastes.
2. The salvageable value of the equipment was subtracted from
the total cost of the installation and the balance constituted a
payment to the Mill by the research project.
Arrangements were made to lease a 5, 000 gallon stainless steel tank
trailer at a flat rate of $50.00 per week. The cost for a tractor and
driver was $10.00 per hour during the first year and $10.50 per hour
during the second year.
A summary of the total volumes and cost of delivery of the respective
mill wastes is presented below.
2/16/68 - 12/12/69 Volume, Gallons Cost Cost/1000 Gallons
Milll 291,015 $1145.17 $3.94
Mill 2 345,200 1691.69 4.90
Mill 3 561,650 2583.89 4.60
Mill 4 122,760 1646.03 13.41**
Total 1,320,625 $7066.78 $ 5.35
**Note: The average tank trailer load for Mill 4 was approximately
1000 gallons per trip resulting in the high unit cost shown.
63
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Pilot Plant Operation
The pilot plants were operated continuously 24 hours per day, 7 days
per week. The pilot plant operator was on duty 51/2 days per week.
In the absence of the pilot plant operator, the GBMSD treatment plant
operators checked the pilot plants at least once hourly, taking required
samples, reading final clarifier sludge levels, and making routine checks
for mechanical problems. If a mechanical problem was discovered which
could not be quickly repaired, project personnel were called in.
In order to control the pilot plant operation, it was necessary to take
many samples of the streams associated with each pilot plant. The
routine sampling program is presented in Table 9.
In order to properly control the pilot plant operation, equations were
developed to mathematically estimate the required flow rates for feed
bypass, return activated sludge (RAS) and waste activated sludge (WAS).
During the periods of operation in which the mixed liquor had poor
settling characteristics, it was necessary to bypass a portion of the
primary effluent in order to maintain the F/M (food/microorganism)
ratio in the desired range. As the plant improved, the quantity of
bypass would be gradually reduced to zero. The COD/BOD ratio was
used so that daily changes to the bypass rate could be made as necessary.
The primary objective of controlling the RAS and WAS flows was to
maintain the proper quantity of mixed liquor volatile suspended solids
under aeration. In doing so, the F/M ratio was maintained at the
selected level.
The daily procedure was to mathematically calculate the theoretical
values for RAS and WAS and then, based upon previous operating history
use these values to adjust the flows accordingly. For example, if the
particular plant had been operating at a very steady condition over
several days, the calculated value would normally be used as the setting
for the next day. However, if the operation had been fluctuating greatly
and there was a low concentration of solids in the return activated sludge
thus resulting in a very high calculation for the RAS flow setting for the
next day, the RAS flow actually set would be less than that calculated.
This procedure was also applied to the waste activated sludge flow. For
example, if a sludge blanket was building up in the final clarifier, the
amount of activated sludge wasted would be greater than that calculated
to maintain the blanket at the desired level.
Mill wastes were pumped from storage tanks on a constant flow basis.
Pumping rates for Metro sewage were adjusted manually to approximate
64
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PILOT PLANT SAMPLING PROGRAM
H
p
a4
i—*
n>
Source
PI, PE, 4 FE's*
Nutrients (N & P)
Digester Supernatant
Chlorine
Aeration Tank
Mixed Liquor
Return Activated
Sludge (RAS)
Procedure
Waste Activated
Sludge (WAS)
Automatic sampling, 24 hours per day, 7 days per week, proportional to
total flow to four pilot plants.
Weighted grab samples of freshly-filled nutrient-feed barrel, composited
and analyzed at selected intervals or daily as operation dictated.
Grab sample of freshly-filled supernatant-feed barrel; normally a daily operation.
Strength of concentrated chlorine solution added to chlorine feed barrel
determined; concentration of chlorine fed to pilot plants calculated using
known dilution factor.
Daily grab sample of specified cells of aeration tank.
2/6/68 to 8/29/68 - Representative grab sample of total WAS collected
previous 24 hours. If no wasting occurred, then a grab sample of RAS was
taken at the same time as the mixed liquor grab sample.
8/30/68 - 12/15/69 - Composite grab samples, on odd hours, 24 hours per
day, 6 days per week.
Solids concentration assumed to be same as RAS, therefore no separate
samples of WAS taken.
* PI - Primary influent
PE - Primary effluent
FE - Final effluent
-------
flow variations through the GBMSD plant. Adjustments were made
hourly or when significant changes in flow occurred.
The frequency of measuring pilot plant operating parameters is presented
in Table 10.
66
-------
PILOT PLANT MEASUREMENTS
H
cr
i—"
CD
Source
Mill Storage Tank Pumps
Metro Sewage Pump
Magnetic Flow Meter
Bypass
RAS
WAS
Nutrients
Digester Supernatant
Chlorine
Dissolved Oxygen:
All Cells
Temperature, Cell 10
Final Clarifier Sludge Levels
Mixed Liquor SVI
Flow Rate
1 /week
1 /month
6 days/week
Volume
Miscellaneous
11
11
it
ii
11
7 days/week
7 days/week
6 days/week
Even hours - 7 days/wee!
6 days/week
TO
CD
-------
PRIMARY CLARIFICATION
During the pilot plant design, the provision of primary clarification was
questioned due to the fact that the industrial wastes which were
approximately 50% of the hydraulic flow, had relatively few settleable
solids. The decision was made that primary clarification would be
provided to properly evaluate it's desirability in a full-scale plant.
A single primary clarifier was installed to serve the four secondary
treatment units. The details of the primary clarifier construction are
shown on the as-built drawing in Appendix A. The unit was designed to
provide a two-hour detention time at four gallons per minute.
Five special studies on primary clarification were made:
1. Preliminary evaluation of primary clarifier performance --
July 25, 1968.
2. Imhoff cone and gravity settling column tests -- November 11,
1968 - January 16, 1969.
3. Imhoff cone and gravity settling column tests -- February 26-27,
1969.
4. Pilot clarifier studies -- May 1 - July 31, 1969.
5. Pilot clarifier studies -- September 1 - October 19, 1969.
As discussed previously, joint treatment options required study of the
following combinations:
1. Each Mill alone.
2. Metro alone - average and simulated storm flow.
3. Mills 1, 2 and 4.
4. Mills 1, 2, 4 and Metro.
5. Mill 3 and Metro.
6. All Mills and Metro.
7. All Mills and Metro plus WAS return to the primary clarifier.
Preliminary Evaluation of Primary Clarifier Performance - 7/25/68
Primary clarifier BOD and total suspended solids (TSS) removal data
for the period between March 1 and June 30, 1968, averaged 4.2% and
33% respectively when treating the combination of all Mills plus Metro
wastes. On the basis of BOD removal alone, primary clarification could
not be justified. Also, a total suspended solids removal of 33% is
considerably less than average values of 50-60% normally obtained in
primary treatment units treating domestic wastes. However, proper
evaluation of primary clarification must also consider these additional
factors:
69
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1. Efficiency of primary clarification on various combinations of
the five individual wastes.
2. Increase in sulfide concentration of the sewage as it passes
through a primary clarifier.
3. Preaeration of the sewage prior to entering the aeration tank.
4. Reduction in waste activated sludge produced due to removing
solids in primary clarification.
5. Evaluation of primary and secondary sludge characteristics.
6. Desirability of returning waste activated sludge to the primary
clarification units.
Until these factors could be investigated, it was decided to continue
primary clarification of all influents to the pilot plants.
Imhoff Cone and Gravity Settling Column Tests, 11/1/68 - 1/16/69
A series of Imhoff cone settling analyses was made for four combinations
of Mill and Metro wastes on November 11, 1968. The combinations
analyzed, the testing procedure, and the laboratory data for the initial
composite samples are shown in Table 11 and 12. Samples of supernatant
were taken after 30 minutes of settling, and after pH adjustment and 30
minutes of settling. It was assumed that the mill -waste flows were
fairly uniform over a 24-hour period as opposed to diurnal variations
of Metro sewage flow. However, a single grab sample of Metro sewage
was used in the studies, thus injecting a degree of uncertainty into the
answers obtained.
An Imhoff cone study was made on the five individual wastes on January 13,
1969. These data are presented in Table 13. Gravity settling column
tests were run on the five individual wastes on January 15-16 utilizing
a 3 1/2 inch I.D. plastic settling column with a 12-foot sidewater depth.
(See the section entitled "Final Clarification-Laboratory Procedure -
Phase II in Appendix B).
The Mill samples used for the tests between January 13-16 were obtained
from storage tanks which had been filled on the 6th and the 10th of
January, (see notes on Table 13). Some changes in waste characteristics
may have occurred during the storage period. The Metro sewage grab
sample for the gravity settling column test was obtained from the hose
which discharged to the rapid-mix unit in the pilot plant.
The data obtained from the gravity settling column tests were very
disappointing and of little value. It was not possible to draw percent
removal curves through the data as is typically done in data analysis.
70
-------
a4
i—i
tt
OQ
•^J
PRIMARY CLARIFICATION INVESTIGATION
Imhoff Cone Analyses
Mill and Metro Combinations
November 11, 1968
SAMPLE COMPOSITION
A. Mill 1 (4 MGD)
B . Mill 2 (5 MGD)
C. Mill3 (7 MGD)
D. Mill 4 (2.25 MGD)
E. Metro (20 MGD)
F. Mill 1
Mill 2
Mill 4
G. Mill 1
Mill 2
Mill 4
Metro
H. Mill 1
Mill 2
Mill 3
Mill 4
Metro
I. Mill 3
Metro
TESTING PROCEDURE
3.57 liters
4.43 liters
2. 00 liters
1.29 liters
1. 60 liters
0.72 liters
6.39 liters
1. 05 liters
1.31 liters
1. 83 liters
0. 59 liters
5.22 liters
2.59 liters
7.41 liters
TOTAL MIXTURE
pH ADJUSTMENT TO 7. 0
I
1/2 hr. SETTLING 1/2 hr. SETTLING
ANALYSES
SUPERNATANT
ANALYSES
©
SUPERNATANT
ANALYSES
-------
PRIMARY CLARIFICATION INVESTIGATION
Imhoff Cone Analyses
Mill and Metro Combinations
November 11., 1968
BOD - unfiltered
Total Suspended Solids
NH3 - Nitrogen
1350
264
968
344
213
563
228
1155
324
292
344
~~ ~ _^__^^ Samples
Analyses, mg/1 " " ___
BOD -Unfiltered
BOD -Filtered
Total Solids
Total Volatile Solids
Total Suspended Solids
Vol. Suspended Solids
NHg - Nitrogen as N
Ortho-Phosphorus as P
Total-Phosphorus as P
Volatile Acids as Acetic
PH
Settled Sludge Vol. mis.
F
1 2 3
1275 1122 1114
1105 887 1173
2876 2784 2916
1924 2036 1420
168 64 72
120 60 88
86.8 86.2 87.9
000
0.4 0.3 0.3
555 593 574
5.25 5.3 6.8
7 - 6.0
G
1 2 3
719 629 623
591 459 507
1768 1648 1716
1048 960 828
264 88 100
240 116 96
47.0 56.6 48.2
3.5 3.2 3.1
7.5 6.9 6.8
278 259 257
6.7 6.6 6.8
13 14
H
1 2 3
725 640 640
514 519 519
1760 1660 1680
948 884 872
204 92 128
200 88 112
39.0 33.4 39.5
3.0 3.3 2.7
10.6 5.8 5.6
288 281 278
6.7 6.7 6.9
10 10
I
1 2 3
507 422 459
309 306 310
1732 1604 1560
532 444 428
296 160 168
280 156 148
17.8 17.0 8.0
5.1 4.7 4.4
9.5 9.2 8.5
155 145 174
7.2 6.9 6.9
10 10
u-
I—1
(D
fO
P
TO
(D
a. 1 - Total mixture
2 - Supernatant after 1/2 hour quiescent settling
3 - Supernatant after pH adjustment and 1/2 hour quiescent settling
b. Data reported under A, B, C and D are based on grab samples from freshly-filled storage tanks, 11/8/68.
c. Data reported under E are based on a 24-hour influent composite sample for 11/11/68.
d. Data reported under F, G, H and I are based upon mixtures composited from grab samples from the mill effluent
storage tanks and Metro influent on 11/11/68.
-------
PRIMARY CLARIFICATION INVESTIGATION
Imhoff Cone Studies
Individual Mill and Metro Wastes
January 13, 1969
' ' — — -»_§ ample s
Analyses, mg/1 " — — -~^_
BOD-Unfiltered
BOD -Filtered
Total Solids
Total Volatile Solids
Total Suspended Solids
Vol. Suspended Solids
NH3 -Nitrogen as N
Ortho-Phosphorus as P
Total-Phosphorus as P
Volatile Acids as Acetic
pH
Settled Sludge Vol. mis.
A - Mill 1
1 2 3
1564 1428 1428
1530 1428 1411
3548 3348 3976
2508 2332 1568
172 128 148
172 104 132
000
0.2 0.2 0.25
0.9 0.61 0.82
559 669 565
3.3 3.3 7.0
7 5
B - Mill 2
1 2 3
357 306 323
357 306 315
1464 1348 1220
976 784 716
204 100 132
200 100 120
52.4 50.4 50.4
0.01 0 0
0.26 * 0.22
171 174 169
6.5 6.5 7.0
18 18 18
C - Mill 3
1 2 3
629 612 655
612 553 476
1920 1840 1912
720 708 600
284 256 268
176 168 164
000
0.1 0.1 0.1
0.94 0.8 0.83
243 274 245
5.9 5.9 6.7
1.7 .6
" — Samples
Analyses, mg/1 """""•—— — _
BOD— Unfiltered
BOD -Filtered
Total Solids
Tot. Vol. Solids
Total Sus. Solids
Vol. Sus. Solids
NH3 -Nitrogen
Ortho Phosphorus
Total Phosphorus
Volatile Acids as Acetic
PH
Settled Sludge Vol. mis.
D
1
1326
1292
3972
1432
280
273
0
0.03
0.73
771
6.0
- Mill
2
1275
1207
3876
1336
266
233
0
0.01
0.61
812
6.0
4
4
3
1292
1173
3992
1196
246
220
0
0
0. 82
757
7.0
3
E
1
209
105
988
340
168
156
13.1
2.7
4.04
40
7.5
- Metro
2
114
105
868
236
92
76
11.6
2.2
4.5
45
7.2
24
3
127
95
440
108
68
68
13.4
2.3
4.26
38
7.0
19
Note:
a. 1 - Total Mixture
2 - Supernatant after 1/2 hour quiescent settling.
3 - Supernatant after pH adjustment and 1/2 hour quiescent settling.
b. Samples A and B are grab samples from storage tanks filled 1/6/69.
c. Samples C and D are grab samples from storage tanks filled 1/10/69.
d. Sample E is a 24-hour composite sample obtained 1/13/69.
* Analyses inconclusive
Table 13 Page 75
-------
Apparently, a majority of the particulate material in the Mill wastes is
colloidal in nature and would not be removed by clarification. This is
further indicated by the Imhoff cone studies conducted on January 13,
in which the quantity of settled sludge is quite small for three of the
four Mill wastes.
Imhoff Cone and Gravity Settling Column Tests, 2/26-27/69
As the Imhoff cone studies performed November 11, 1968 utilized grab
samples of Metro sewage rather than composite samples over a period
of 24 hours, a series of tests on composite samples was conducted a
second time between 0800, February 26, and 0800 February 27, 1969.
The sample compositions and relative volumes are presented in Table 14.
Two hour composite samples were obtained by taking Metro grab
samples every 15 minutes proportional to the existing flow through the
plant. The grab sample was then added to the constant volume of Mill
samples and at the end of each two-hour interval the total composite
sample was utilized for an Imhoff cone study.
Analyses were made on each two-hour composite sample during the
24-hour period to determine the influence of the varying Metro sewage
flow and characteristics. The laboratory data obtained for each two-
hour composite are presented in Tables 15 and 16. Based upon the
Imhoff cone settling data and the actual Metro and projected Mill flow
rates, the total pounds of TSS and BOD theoretically removed in a full-
scale primary clarifier for each two-hour interval was calculated.
This information is presented in Table 17.
During the same 24-hour interval, six consecutive gravity settling
column analyses were conducted on four-hour composite samples of
Metro plus Mill 3. The results of the gravity settling column tests
were again very disappointing. The data did not yield correlations
between depth, detention time, overflow rate and percent removal of
TSS.
The 15-minute grab sample of Metro sewage was added immediately to
the particular composited mill samples rather than compositing the
Metro sewage separately over the two-hour interval and then mixing the
two components together prior to taking the samples for the Imhoff cone
study. This procedure may have created an unrealistic pH adjustment
which could affect the precipitation of dissolved solids.
The pilot plant primary clarifier data obtained between September 25,
76
-------
H
f"
cr
PRIMARY CLARIFICATION INVESTIGATION
Imhoff Cone and Settling Column Analyses
Mill and Metro Combinations
February 26 - 27, 1969
SAMPLE COMPOSITION AND VOLUME
TWO-HOUR COMPOSITE SAMPLES FOR IMHOFF CONE ANALYSES
A.
B.
C.
D.
Metro
Mill 3
Metro
Mill 1
Mill 2
Mill 4
Metro
Mill 1
Mill 2
Mill 3
Mill 4
Metro
- 20 mgd
- 7 mgd
- 20 mgd
- 4 mgd
- 5 mgd
- 2.25 mgd
- 20 mgd
- 4 mgd
- 5 mgd
- 7 mgd
2.25 mgd
- 20 mgd
Meter Reading, mgd *
Average Daily Flow = 20 mgd * 8 = Slze ol I5 min^e grab sample
2.59 liters
7.41 liters*
1.28 liters
1.60 liters
0.72 liters
6.40 liters *
1.04 liters
1.31 liters
1.83 liters
0.59 liters ,
5.23 liters*
FOUR -HOUR COMPOSITE SAMPLES FOR SETTLING COLUMN ANALYSES
E.
Mill 3
Metro
- 7 mgd
- 20 mgd
14. 69 liters
Meter Reading, mgd 42.06 liters*
X
(5
-J
-J
Avg. Daily Flow = 20 mgd
*Total liters desired at existing average daily flow rate.
16
= Size of 15 min. grab sample
-------
PRIMARY CLARIFICATION INVESTIGATION
Imhoff Cone Analyses
Mill and Metro Combinations
February 26-27, 1969
COMPOSITE SAMPLE
Interval
08-10
10-12
12-14
14-16
16-18
18-20
20-22
22-24
24-02
02-04
04-06
06-08
SAMPLE A
pH
a b
7.3 7.4
7.3 7.3
7.4 7.6
7.4 7.5
7.7 7.4
7.4 7.4
7.3 7.3
7.3 7.3
7.4 7.4
7.3 7.6
7.2 7.5
7.3 7.4
TSS
a b
212 108
244 140
240 164
232 172
240 164
260 160
256 136
248 160
228 152
244 152
204 128
156 76
VSS
a b
192 100
216 136
220 148
216 180
216 156
240 164
216 128
220 148
188 116
192 124
172 84
132 68
BOD
a b
306 201
275 213
249 202
225 194
249 212
293 208
225 143
239 174
208 138
240 185
163 110
132 79
Set
Sludge
b
4 .5
7.5
7.5
6.5
5.5
5.5
6.5
6.0
5.5
3.5
4.5
4.0
% Red.
TSS BOD
49.1 34.3
42.6 22.6
31.7 18.9
25.9 13.8
31.7 14.9
38.5 29.0
46.9 36.4
35.5 27.2
33.3 33.7
37.7 22.9
37.3 32.5
51.3 40.2
SAMPLE B
PH
a b
8.1 8.0
8.0 7.9
8.0 8.1
7.9 8.0
8.1 7.9
8.0 8.0
7.9 7.9
7.9 7.9
7.9 7.9
8.0 8.1
8.0 8.0
8.1 8.0
TSS
a b
200 164
276 156
252 172
244 160
220 204
268 104*
248 160
252 160
240 164
216 188
224 168
152 116
VSS
a b
156 132
184 124
200 136
196 136
168 136
208 88
196 112
196 116
184 92
184 124
168 108
116 80
BOD
a b
312 264
312 274
315 258
282 237
289 262
330 248
266 225
285 245
229 214
289 260
248 206
229 189
Set
Sludge
b
4.5
5.5
5.0
5.0
4.0
4.0
5.0
4.0
4.5
4.5
3.5
3.0
% Red.
TSS BOD
18.0 15.4
43.5 12.2
31.7 18.1
34.4 16.0
7.3 9.3
61.2* 24.8
35.5 15.4
36.5 14.0
31.6 6.6
13.0 10.0
25.0 16.9
23.7 17.5
1—
Ul
OQ
a. - Composite Sample Analyses
b. - Analyses of supernatant obtained 2 inches below liquid surface after 1/2 - hour settling
All concentrations - mg/1; all volumes - ml
* Estimated
-------
PRIMARY CLARIFICATION INVESTIGATION
Imhoff Cone Analyses
Mill and Metro Combinations
February 26-27, 1969
COMPOSITE SAMPLE
Time
Interval
08-10
10-12
12-14
14-16
16-18
18-20
20-22
22-24
24-02
02-04
04-06
06-08
SAMPLE C
pH
a b
6.7 6.8
6.7 6.7
6.7 6.8
6.5 6.7
6.9 6.7
6.7 6.7
6.6 6.6
6.6 6.6
6.5 6.6
6.6 6.7
6.5 6.6
6.6 6.6
TSS
a b
184 132
240 152
232 156
236 168
224 180
200 148
232 164
252 116
236 144
268 196
228 148
180 132
VSS
a b
172 132
228 132
200 148
220 164
200 180
192 148
204 148
232 116
204 124
224 156
184 128
160 124
BOD
a b
550 499
540 383
540 398
505 455*
490 450
485 477
485 424
490 450
510 473
545 469
555 484
560 488
Set
Sludge
b
5.5
6.0
8.0
5.0
6.0
6.0
5.5
6.0
5.0
3.5
4.0
4.0
% Red.
TSS BOD
28.3 9.3
36.7 29.1
32.8 26.3
28.8 9.9*
19.6 8.2
26.0 1.6
29.3 12.6
54.0 8.2
39.0 7.3
26.9 13.9
35.1 12.8
26.7 12.9
SAMPLE D
PH
a b
6.9 6.8
6.8 6.9
6.9 7.0
6.8 6.9
7.0 6.9
6.9 6.9
6.7 6.8
6.9 6.8
6.8 6.9
6.8 6.9
6.7 6.9
6.8 6.8
TSS
a b
196 148
212 172
212 188
216 160
220 164
216 172
208 140
228 148
240 168
269 184
212 152
176 120
VSS
a b
180 128
196 148
180 168
196 160
180 132
184 156
188 132
176 100
196 144
224 148
180 100
156 108
BOD
a b
580 495
600 315
520 319
500 488
545 450
545 488
480 450
505 480
495 480
585 544
565 506
585 507
Set
Sludge
b
4.0
6.0
5.5
5.0
5.5
5.0
5.0
5.0
3.5
3.0
3. 5
4.5
% Red.
TSS BOD
24.5 14.7
18.9 47.5
11.3 38.7
25.9 2.4
25.5 17.4
20.4 10.5
32.7 6.3
35.1 5.0
30.0 3.0
31.6 7.0
28.3 10.4
31.8 13.3
P
cr
o
TJ
TO
a. - Composite Sample Analyses
b. - Analyses of supernatant obtained 2 inches
All concentrations - mg/1; all volumes - ml
* Estimated
below liquid surface after 1/2 - hour settling
-------
p>
cr
QTQ
00
OO
PRIMARY CLARIFICATION
Imhoff Cone Analyses
Mill and Metro Combination
February 26-27, 1969
PROJECTED TOTAL SUSPENDED SOLIDS AND BOD REMOVAL IN FULL-SCALE
PRIMARY CLARIFICATION
Typical Calculation for Sample C:
1600-1800: Average GBMSD flow = 26.75 MGD; Industrial flow = 11.25 MGD; Total flow = 38.0 MGD
Projected Full-Scale TSS Removal During 2-Hour Interval-
38.0 MGD x 8.34 Ibs/gal x 1/12 day x 224 ppm TSS (in) = 5916 Ibs TSS (in)
38.0 MGD x 8.34 Ibs/gal x 1/12 day x 180 ppm TSS (out) = 4754 Ibs TSS (out)
Total Ibs TSS Removed =1162 Ibs for 2-Hour Interval
Percent Removal =19.6%
TOTAL SUSPENDED SOLIDS
Sample Name
A. GBMSD
B. GBMSD + Mill 3
C. GBMSD + Mill 1, 2, 4
D. GBMSD + All Mills
A. GBMSD
B. GBMSD + Mill 3
C. GBMSD + Mill 1, 2, 4
D. GBMSD + All Mills
Libs.
In
47092
61139
67243
77255
BIOCHEMICAL
47739
74007
154575
192428
Lbs.
Out
29292
41813
45549
56844
OXYGEN DEMAND
35178
62957
134866
163542
Lbs .
Removed
17800
19326
21694
20411
12561
11050
19709
28886
Percent
Removal
37.8
31.6
32.3
26.4
26.3
14.9
12.8
15.0
-------
1968 and January 31, 1969 were also utilized to project full-scale
removals of BOD and TSS. This information is presented in Table 18.
The data in this Table show the effect of varying the detention time and
overflow rate on the removal of BOD and TSS.
The primary clarification data obtained between September, 1968 and
February, 1969, show that increased BOD removals could be obtained
when the combination of Metro plus all Mills was given primary
clarification as compared to any other combinations studied. Based
upon the 24-hour gravity settling column and Imhoff cone analyses, and
upon the data obtained on the pilot plant primary clarifier between
September 25, 1968 and January 31, 1969, the projected BOD and TSS
removals for the combination of Metro plus all Mills were as follows:
BOD removal - approximately 10%
TSS removal - approximately 38%
At the time of this review it was contemplated that only Metro plus Mill
3 wastes would receive separate grit removal. Mills 1, 2 and 4 would
join the grit chamber effluent for subsequent primary clarification.
Pilot Clarifier Studies - May 1 - July 31, 1969
Additional clarifier studies were conducted to obtain information on
items which would have the greatest effect on cost estimates. Two of
these items were:
1. The cost of sludge handling, which is dependent on the sludge
concentration from the primary clarifier.
2. The effect of returning waste activated sludge to the primary
clarifier.
A pilot clarifier for one activated sludge unit was constructed to study
sludge characteristics and BOD and TSS removals when returning
waste activated sludge. Details on unit design and test procedures
are as follows:
1. Pilot Clarifier Design
Internal diameter - 20 in.
Sidewater depth - 72 in.
Overflow rate - 540 GPD/sq ft
Detention time - 2 hours
A glass window in the side of the tank, approximately 2-1/2 in.
•wide by 60 in. high allowed the level of the sludge blanket to be
observed.
84
-------
PRIMARY CLARIFICATION
Projected Full-Scale Total Suspended Solids and BOD Removals
Based Upon Pilot Plant Primary Clarifier Operation
September 25, 1968 - January 31, 1969
Date
1968-69
9/25-10/14
10/15-11/1
11/2-11/21
11/22-12/11
12/12-1/4
1/5-1/31
Desired Flow
Pilot
Plant
L/D
17908
8954
8954
13431
17908
13431
Equiv.
Full-
Scale
MGD
38.25
38.25
38.25
38.25
38.25
38.25
Actual Flow
Pilot
Plant
L/D
16656
8678
7818
13735
17018
15098
Equiv.
Full-
Scale
MGD
35.58
37.07
33.40
39.12
36.35
43.00
Det.
Time
Hours
Hours
2.49
4.79
5.31
3.02
2.44
2.75
Overflow
Rate
GPD/sqft
480
250
225
396
490
435
Total Suspended Solids
mg/1
206
128
243
127
236
118
237
153
248
151
218
117
Ibs/day
61121 (in)
37978 (out)
75129 (in)
39265 (out)
65734 (in)
32867 (out)
77315 (in)
49912 (out)
75181 (in)
45776 (out)
78174 (in)
41956 (out)
Removed
Ibs/day
23143
35864
32867
27403
29405
36218
%
37.9
47.7
50.0
35.4
39.1
46.3
Biochemical Oxygen Demand
mg/1
562
528
570
473
679
598
568
507
593
565
494
449
Ibs/day
166747 (in)
156659 (out)
176228 (in)
146238 (out)
189123 (in)
166562 (out)
185296 (in)
165396 (out)
179768 (in)
171280 (out)
177148 (in)
161011 (out)
Removed
Lbs/day
10088
29990
22561
19900
8488
16137
%
6.0
17.0
11.9
10.7
4.7
9.1
H
P
0*
i— >
ffl
00
Full-Scale Influent Ratio
Mill 1 - 4.0 mgd
Mill 2 - 5.0 mgd
Mill 3 - 7.0 mgd
Mill 4 - 2.25 mgd
GBMSD - 20.0 mgd
Total - 38.25 mgd
Primary Clarifier Dimensions
TV +• 'J K f4-
Surface Settling Area-9.2 sq ft
(U
OP
CD
Ul
-------
2. The influent to the pilot clarifier was the same combined waste
(all Mills plus Metro) being fed to the large pilot plant primary
clarifier.
3. Grab samples of the effluent were taken on the odd hours, 7
days a week, and composited over 24 hours for analyses of
BOD and TSS removal efficiency.
4. Waste activated sludge from either the contact stabilization
control plant or the Kraus control plant was fed continuously
to the pilot clarifier.
5. The waste activated sludge fed to the pilot clarifier each day
was that collected during the previous day. The waste activated
sludge was continuously mixed while being fed to the pilot
clarifier.
6. The pilot plant operator made sludge draws, up to 8 times daily,
to maintain a 12-inch sludge blanket. The draws did not exceed
4 gallons. Based upon the volume drawn, proportional samples
of the pilot clarifier sludge were collected and composited daily
for TSS and VSS analyses. The sludge level variations were
recorded on the even hours, 7 days a week.
The flow schematic for the operation of the pilot clarifier is shown in
Figure 8.
The pilot clarifier was started up on April 14, 1969. Waste activated
sludge from the Kraus- control plant was fed to the pilot clarifier,
beginning April 22. The average, maximum and minimum values for
each operating parameter are presented in Table 19. A comparison of
the pilot and primary clarifier operations is presented in Table 20.
The following conclusions were made on the effect of adding waste
activated sludge to the pilot clarifiers:
1. No effect on TSS removal was apparent.
2. Unfiltered BOD increased in the effluent.
3. Clarifier sludge concentration decreased. However, this
procedure would significantly reduce the total volume of waste
activated sludge to be handled in subsequent processes.
Due to the wide fluctuation in sewage flow to the GBMSD treatment plant
the use of primary clarification facilities as a reliable method for thick-
ening waste activated sludge cannot be justified. During a high flow
condition the thickened solids in the primary clarifiers could possibly
86
-------
PRIMARY CLARIFICATION
PILOT CLARIFIER FLOW SCHEMATIC
MAY, JUNE, JULY, 1969
o
c
3D
m
00
0
m
CD
METRO
SEWAGE
RAPID -MIX
TANK
SPLITTER
BOX
MILLS
1,2,3 a 4
PILOT CLARIFIER
WAS
BARREL
ruwir
^V
I
WAS BARREL '
PUMP
TO SEWER
FINAL CLARIFIER
AERATION TANK
SPLITTER BOX
*- TO
AERATION
TANK
PRIMARY CLARIFIER
-------
PRIMARY CLARIFICATION INVESTIGATION
Pilot Clarifier Operation
May 1 - July 31, 1969
MONTH
May
June
July
Avg.
Max.
Min.
Avg.
Max.
Min.
Ave.
Max.
Min.
Q
fwd
L/D
4270
4958
2999
4333
4958
3047
4173
5095
3620
WAS
feed
T,/D
65
208
0
85
136
19
54
133
0
Q
total
L/D
4340
4852
3041
4415
5117
3138
4227
5167
3718
WAS
added
grams/day
TSS
1080
3236
0
1072
2502
203
586
1392
0
VSS
874
2692
0
902
1920
175
483
1176
0
EFFICIENCY ANALYSIS, mg/1
Tot. Sus. Sol.
PI
233
456
104
229
336
108
218
288
108
PE
164
296
88
161
284
44
167
248
92
%red
29.6
59.0
0
29.7
75.5
0
23.4
48.6
0
Vol. Sus. Sol.
PI
184
356
96
178
248
80
176
248
88
PE
121
204
70
127
196
36
133
236
52
%red
34.2
61.1
0
28.7
67.9
0
24.4
45.8
0
1
Unfilt. BOD
PI
567
689
482
490
623
340
486
615
363
PE
581
674
450
493
742
380
477
629
380
%red
15.7
0
22.9
0
1.9
18.2
0
color
unit
S~
PE
320
469
264
319
507
208
248
302
191
PE
—
.293
.500
.0398
.574
.794
.500
RAW PILOT SLUDGE
Vol. Solids Anal, mg/1
L/D
26.6
121. 1
0
23.8
94.6
0
19.2
109.8
0
TSS
36029
60696
19272
39708
46328
32968
35216
54652
29300
VSS
29664
53368
16064
32703
38120
26987
29527
44456
23564
WAS Feed: May 1 - June 3, 1969; Kraus - Control waste activated sludge.
June 4 - July 31, 1969; Contact Stabilization-Control waste activated sludge.
cr
l—'
CD
TO
a>
00
-------
PRIMARY CLARIFICATION INVESTIGATION
Comparison of Pilot Clarifier and Primary Clarifier Operation
May 1 - July 31, 1969
MONTH
May
June
July
Avg.
Max.
Min.
Avg.
Max.
Min.
Avg.
Max.
Min.
WAS
Feed
L/D
65
208
0
85
136
19
54
133
0
Total Suspended Solids rng/1
PI
233
456
104
229
336
108
218
288
108
Effluent
Primary
175
312
68
186
304
104
165
220
60
Pilot
164
296
88
161
284
44
167
248
92
Volatile Suspended Solids mg/1
PI
184
356
96
178
248
80
176
248
88
Effluent
Primary
121
192
80
136
192
56
131
184
52
Pilot
121
204
70
127
196
36
133
236
52
BOD, mg/1
PI
567
689
482
490
623
340
486
615
363
Effluent
Primary
553
669
415
463
617
349
433
567
289
Pilot
581
674
450
493
742
380
477
629
380
Sludge Draws
% TSS
Primary
5.5
6.4
4.5
6.7
10.1
5.3
7.3
11.4
3.7
Pilot
3.8
6.1
1.9
4.0
4.6
3.3
3.7
5.5
2.9
cr
15
era
tt
-------
be flushed into the secondary system, resulting in subsequent problems
in that unit. However, the data obtained on the pilot clarifier operation
did show that, under normal flow conditions, return of the waste
activated sludge to the primary clarification units can significantly
increase the concentration of waste activated sludge without causing
serious detrimental effects on the primary effluent. Therefore, it is
recommended that piping be included in the full-scale plant to permit
the return of waste activated sludge to the primary clarifier if so
desired.
Pilot Clarifier Studies - September 1 through October 19, 1969
Additional studies conducted with Pilot Plant A connected directly to the
pilot clarifier were as follows:
1. Elimination of Mill 3 effluent to Pilot Plant A.
2. Increased hydraulic loadings on the primary and secondary
processes to approximate a storm flow condition.
3. Bypass Mill 1, 2 and 4 wastes around primary clarification
directly to the secondary system.
Between September 1 and October 19, Pilot Plant A was operated such
that Metro sewage only was receiving primary treatment and Mill 1, 2
and 4 wastes were added to the pilot clarifier effluent. Composite
sampling of Metro flow, pilot clarifier effluent and Plant A aeration
tank feed was begun for routine laboratory analyses.
The high-flow studies began October 3 by increasing the Metro sewage
flow. Between October 7 and October 19, tap water was added to the
Metro sewage to reduce the BOD to approximately 100 mg/1, simulating
a storm flow condition. The flow schematic illustrating the operation
of the pilot clarifier under storm flow conditions is presented in Figure
9. The average, maximum and minimum pilot clarifier operating
values for September 1 through October 19 are presented in Table 21.
Summary of Primary Clarification Studies
This concluded the special studies to evaluate various options for primary
clarification. The decisions regarding primary clarification which
were utilized in the final cost estimate are as follows:
1. Only Metro sewage would normally receive primary clarification.
2. The mill effluents would not be discharged into existing inter-
ceptor sewers but would be conveyed to the treatment plant in
a separate interceptor sewer system.
92
-------
PILOT-PRIMARY CLARIFIER FLOW SCHEMATICS
September 1 through October 19, 1969
Tap Water Metro Sewage Mills 1,2,4
Mill 3
Pilot Clarifier
Primary Clarifier
Bypass
Mills 1,2, 4
To Plant A
To Plants B, C,D
-------
PRIMARY CLARIFICATION
Pilot Clarifier Operation
September 1 through October 19, 1969
1969
9/1-9/30
10/1-10/6
10/7-10/19
Ave.
Max.
Min.
Ave.
Max.
Min.
Ave.
Max.
Min.
Flow to Pilot Clarifier
Liters /Day
Mills
1
0
531
531
531
531
531
531
2
0
531
531
531
531
531
531
3
0
0
0
0
0
0
0
4
0
64
64
64
64
64
64
Metro
3516
4575
2680
4649
5780
3226
7048
10863
4846
Tot.
3516
4575
2680
5775
6906
4352
8175
11989
5972
Pilot Clar. Influent
pH
7.6
7.8
7. 1
6.9
6.9
6.9
7.2
7.4
L7. 0
mg/1
TSS
298
672
150
507
1108
164
128
239
79
VSS
249
540
142
435
972
140
113
209
68 .
BOD
286
560
102
245
336
120
117
189
33
Pilot Clarifier Effluent
PH
7. 6
7.7
7.2
7.2
7.2
7.2
7. 3
7.3
7.2
mg/l
TSS
133
192
66
120
188
82
61
160
14
VSS
113
176
58
92
188
62
54
92
34
%
Red.
55.4
82. 9
29.4
76. 3
87. 0
29. 9
52. 3
85. 3
0
mgA
BOD
237
387
95
262
334
116
232
203
22
%
Red.
17. 1
56.4
0
15. 1
0
72.2
0
Pilot Clarifier
Slud
Vol.
L/D
6.4
15. 1
0
4. 0
7.6
1.9
7.9
56.8
1.9
ge Draws
rnp/1
TSS
42583
69460
23308
39833
43748
35644
23762
42480
7280
VSS
33618
57464
17172
34261
37092
30948
19890
35264
6240
H
I"
o"
OQ
-------
3. Piping would be installed to allow the Mill wastes to be
introduced into or bypass primary clarification as desired.
4. Piping would be installed to allow waste activated sludge to be
returned to the primary clarifier if so desired.
(Cost distribution studies conducted after completion of the pilot plant
studies indicated that it was more economical to treat only the Metro
sewage in primary clarification and convey the Mill wastes directly to
the secondary system.)
96
-------
INTRODUCTION TO PILOT PLANT RESEARCH PROGRAM
Pilot plant research was conducted between February 6, 1968 and
January 31, 1969 and again between February 24, 1969 and December 15,
1969- During these two time intervals the pilot plants operated
continuously 24-hours a day, seven days a week, totaling 22 months
of continuous operation.
The research program is divided into four major phases as follows:
PHASES OF PILOT PLANT RESEARCH
PHASE STUDY DATES
I Startup--Filamentous Biological February 6, 1968 to
Growths August 31, 1968
II Statistical Experimental Design September 1, 1968
to January 31, 1969
III Contact Stabilization and Kraus February 24, 1969
Detailed Studies to July 31, 1969
IV Contact Stabilization Design and August 1, 1969 to
Operating Parameters--Solids December 15, 1969
Handling Studies
Each Phase will be discussed individually in the following sections of
this report.
97
-------
PILOT PLANT RESEARCH - PHASE I
Pilot Plant Startup
The four activated sludge pilot plant units were started up on Metro
sewage on February 6, 1968. The flow arrangement for the four
processes at startup is shown in Figure 10. All units were operated
as conventional activated sludge units during buildup of the mixed
liquor suspended solids.
The first load of mill waste was delivered February 16. The industrial
flows were fed to the pilot plants (which were at about 2500 mg/1
MLTSS) at a gradually increasing rate as follows:
Date Mill Wastes to Pilot Plants
February 16 25% of Full Value
February 20 50% of Full Value
February 23 75% of Full Value
February 27 100% of Full Value
At each industrial flow setting the Metro sewage flow was adjusted to
maintain a continuous 4. 0 gpm flow to the splitter box. The mill and
Metro wastes were fed at constant rates during Phase I. Three of the
units were subsequently converted from conventional (C) to contact
stabilization (CS), step aeration (SA), and Kraus (K) activated sludge
processes.
It was necessary to continuously add defoamer to each aeration tank
shortly after startup. Diffuser stones being used for aeration were
removed from several cells in an effort to reduce the foaming problem
and were replaced with a plastic pipe extending to the bottom of the
respective cells. This provided adequate dissolved oxygen and
eliminated the foaming problems in those particular cells. On April 16,
all remaining diffuser stones were removed from the aeration sections
and replaced with plastic pipe.
A thick gelatinous material was present on the surface of the stones
which were removed. When viewed under a microscope, this material
did not resemble any growths observed in previous samples from the
pilot plants. It is not known why this growth tended to accumulate on
the surface of the stones.
99
-------
PILOT
PLANT
RFACTORS
KRAUS
' i« IT i' i' i"
CONTACT STABILIZATION
SAMPLE
REFRIGERATOR
MAGNETIC
FLOW METER
WASTE SLUDGE FACILITIES
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
—f>- PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
PLACEMENT PUMP
CELL FILLED WITH TAP WATER: (DEAD CELL]
PILOT PLANT OPERATION 2/6/68-2/22/68
2/6 C.SA, CS.K STARTED PLANTS WITH CONVENTIONAL FLOW SCHEMATICS
PILOT PLANT FLOW SCHEMATICS
DONOHUE & ASSOCIATES,INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
SCALE '/,," • I'-O"
-------
The desired full-flow operating conditions were as follows:
Pilot Plant Operating Parameters
February 27 - May 30, 1968
Cell 10
MLVSS RAS-TSS Detention Time,
Plant Q, gpm R/Q mg/1 mg/1 Hours (R + Q)
SA
CS
K
1.0
1.0
1.0
1.0
1.0
1.0
1.0
4000
4000
4000
1.0* 4000
9000 3.8
9000 3.8
9000 3.0 - Stab.
1.5- Contact
9000 21.4 - Nitrify.
1.5- Contact
F/M
0.48
0.47
0.40
0.37
*Kraus RAS flow: 85% to contact section, 15% to nitrifying section;
digester supt. addition = 0.015 x Q.
Estimated PE-BOD - 600 mg/1; dissolved oxygen - 2 mg/1; no nutrient
feed.
Filamentous Microorganisms
During February, samples of mixed liquor from the laboratory reactors
were analyzed by Dr. G. J. Farquhar(13, 14)> University of Wisconsin,
Madison. The dominant feature of the sample from Reactor 4 was the
presence of lobate, finger-like growths associated with some of the floe,
which consisted of bacterial cells incased in a hyaline capsule. This is
characteristic of a condition called zoogloeal bulking. There were very
few filamentous microorganisms present in this sample.
The dominant feature of the mixed liquor samples from Reactor R5 was
a substantial growth of filamentous microorganisms associated with all
sizes of floe. The filamentous microorganisms was identified as a
species of the genus Thiothrix. Identifying factors were it's ability to
store sulfur in a sulfide environment and also certain morphological
characteristics such as base tip differentiation.
Based upon Dr. Farquhar's previous research, it was suggested that
preaeration or prechlorination be considered to reduce the sulfide
102
-------
content in the feed to the reactor. Dr. Farquhar's report also stated
that if zoogloeal bulking presented a problem, then the recommendations
of Heukelekian and Weisberg'15) should be followed. These recommen-
dations consisted of (1) reducing the food to microorganism ratios at
normal mixed liquor suspended solids concentrations and (2) chlorination
of the return activated sludge. However, the presence of zoogloeal
growths was noted in the reactor for several months and did not cause
any apparent settling problems.
Through February 22, no filaments were observed in the pilot plant
aeration units although unidentified filamentous growths were observed
in Mill 3 and 4 waste storage tanks. Filamentous microorganisms
were first reported in the pilot plant aeration units on February 27.
Due to uncontrollable rising sludge blankets in the final clarifiers,
mixed liquor solids were lost over the final clarifier weirs in the C,
SA and K units beginning March 5. On March 11, the mixed liquor
solids in the CS unit were also being lost over the final clarifier weir.
On March 7, mixed liquor and mill waste samples were analyzed by
Dr. Farquhar; the analyses were as follows:
Filament
Pilot Plant Concentration Ecology
Conventional Excessive Sphaerotilus; Thiothrix - trace.
Step Aeration Moderate Sphaerotilus; Thiothrix - trace.
Contact Slight Thiothrix and Sphaerotilus in
Stabilization about equal numbers.
Kraus Moderate Thiothrix; Sphaerotilus -trace.
Storage Tanks
Mill 3 None
Mill 4 None
Additional samples of aeration tank, laboratory reactor, and mill waste
storage tank contents were analyzed on March 14 by Dr. Farquhar.
The results of these analyses are presented in Table 22.
103
-------
MICROBIOLOGICAL ANALYSES - PHASE I
March 14, 1968
Sample General Ecology
G-10* Excessive filaments.
SA-10 Excessive filaments; a
few stalked protozoa.
CS -10 Slight filamentous
growths; small floe; a
few stalked flagellates.
K-10
R-l
R-5
M-l
M-2
M-3
M-4
Moderate filaments;
large floe; very few
protozoans.
Slight amount of fila-
ment; excessive fibrous
debris; many stalked
protozoans; sludge worms.
Excessive filaments;
many worms; some
stalked protozoans.
Trace of filaments,
some fibers.
Dominant Species
Sphaerotilus
Sphaerotilus
Thiothrix
Thiothrix and
Sphaerotilus
Unknown species
dominant,
probably Sphaer-
olitus species
Trace of Beggiatoa
and Thiothrix
Some Thiothrix
Traces of Sphaerotilus
and Beggiatoa
Trace of Beggiatoa
Trace of Beggiatoa
and fungi
Unknown species, Trace of Thiothrix
as in R-l, domi-
nant; exists in
bundles.
Moderate fungus growth; other single cell life.
Very few filaments.
No filaments; some fibers; many single cells.
* Cell 10 of the conventional unit.
Table 22 Page 104
-------
Samples of C-10*, SA-10, CS-6, CS-10, K-6, and K-10 mixed liquor
were sent to E. F. Houghton and Co., Philadelphia, Pa., March 27
for microbiological analyses. The following conclusions were made:
"In general, the bacterial plate counts for the samples from
the six locations were fairly uniform. The samples were
relatively low in coliform organisms, with sizable numbers
of the genus Proteus. All of the samples had large numbers
of sulfur bacteria of the genera Thiothrix and Beggiatoa.
Numberous cultures of Zoogloea ramigera were also noted."
An important point in these conclusions was that Sphaerotilus natans
was not observed in significant quantities in the samples.
Samples from Cell 10 of the conventional and contact stabilization units
were submitted to Buckman Laboratories, Inc., Memphis, Tenn. on
April 4 for biological analyses. The report on these analyses is
summarized as follows:
"The two activated sludge samples were received in thermos
bottles, but at temperatures above those which are necessary
to prevent decomposition. A large population of sulfate-
reducing bacteria had developed."
Contact stabilization - Cell 10: "This sludge appeared to
have a highly diversified microflora which contained considerable
amounts of filamentous microorganisms. The filamentous
microorganisms primarily associated with this sludge were
Sphaerotilus natans, Beggiatoa spp., Thiothrix spp., and
fungus (believed to be Phytophthora sp.).
Thiothrix appeared to be the predominant influence on bulking
of the sludge, as many gelatinous hold-fasts were observed in
which true bacteria agglomerates were attached. However,
the influence of S. natans and Beggiatoa were significant
contributors to the bulking process.
Conventional - Cell 10: "This sludge appeared to have more
finely dispersed particles but much less filamentous micro-
organisms. There was no fungus observed in this sludge;
however, the same type of filamentous bacteria were observed.
In addition, there appeared to be a significant amount of
filamentous algae (Oscillatoria and Ulothrix)".
* i.e., Cell 10 of the conventional unit
105
-------
All units became infested with filamentous microorganisms during
March causing sludge bulking and subsequent loss of biological solids
in the final effluents. The predominant filaments in the conventional
unit were identified as Sphaerotilus natans. In an effort to control this
microorganism, the mixed liquor dissolved oxygen level was varied
from very low to high values. This approach had no apparent success.
By the end of the month, the filament population had changed from
predominantly Sphaerotilus natans to predominantly Thiothrix.
In the step aeration unit the predominant filament initially was
Sphaerotilus natans but likewise changed to predominantly Thiothrix
by the end of March. Dissolved oxygen variations were also utilized
as a possible control with no apparent success. However, the change
from Sphaerotilus natans to Thiothrix occurred prior to the variation
of the dissolved oxygen content.
The filamentous growths in the contact stabilization unit were evenly
divided between Sphaerotilus natans and Thiothrix early in March.
Thiothrix became the predominant filamentous microorganism byApril 1.
The Kraus unit, which was not truly a Kraus process since the addition
of digester supernatant was not started until March 27, was infested
predominantly with Thiothrix throughout the month.
In order to better understand the relationship between sulfide concen-
trations and the presence of filaments, a specific ion probe was
obtained to measure the sulfide concentrations in the various pilot
plant streams. In addition, in order to be able to specifically identify
the filamentous microorganisms, and to routinely monitor the aeration
units, a phase contrast microscope with attached polaroid camera was
ordered. A report entitled "Identification and Classification of
Filamentous Microorganisms in Activated Sludge"(1°) was prepared
for use by the project staff. (See Appendix B for routine procedure
used for microbiological analyses.)
Arrangements were made with Dr. H.H. Heitzman, St. Mary's Hospital,
Green Bay to take photographs of the mixed liquor samples, utilizing
phase contrast microscopy, until a microscope was obtained. Micro-
photographs obtained April 15 are shown in Figures 11 to 1Z. The
filamentous organisms containing sulfur granules are quite clearly
shown in these photographs.
Operational Variations to Control Filamentous Microorganisms
During Phase I, many variations in plant operation were made in an
106
-------
•
TYPICAL ACTIVATED SLUDGE FLOC.
FILAMENTOUS MICROORGANISMS
SEGMENTED FILAMENT FILAMENT ROSETTE
BIOLOGICAL MICROPHOTOGRAPHS FIGURE " PAGE l07
-------
.
FILAMENTOUS BACTERIA CONTAINING SULFUR GRANULES
FIGURE 12 PAGE 109
-------
effort to eliminate filamentous microorganisms. Some of the operational
features instituted were:
1. Variation in dissolved oxygen content in mixed liquor.
2. Preaeration of primary effluent.
3. Bypassing primary effluent to maintain desired F/M ratios.
4. Addition of nitrogen and phosphorus to maintain desired
BOD:N:P ratios.
5. Shock chlorination of aeration tanks and final clarifier
contents.
Changes in the pilot plant flow schematics during Phase I are shown in
Figures 13-16. A summary of these and other operational changes is
presented in Table 23.
The graphical relationships between primary effluent sulfide concen-
tration, RAS sulfide concentration, BOD:N:P ratio, preaeration of
primary effluent, mixed liquor dissolved oxygen level, shock chlorination
and filament concentration are presented in Figures 17-20 for each of
the four pilot plants. These graphs for the period from March 1 to
August 31 illustrate the various operational changes made in an effort
to minimize the filamentous bulking problems. The following comments
apply to these figures:
1. The sulfide analyses of the primary effluent and RAS are not
complete due to problems in developing procedures for sulfide
measurement. These sulfide data were obtained using a
single junction sulfide probe resulting in values which would
tend to be lower than that actually existing in the given sample.
2. The desired BOD:N and BOD:P ratios are shown by a solid line.
The numbers below the solid lines are the average ratios for
the time interval shown. For example, the average BOD:N and
BOD:P ratios for the conventional unit during July were 7.0 and
1.5, respectively.
3. The dissolved oxygen levels shown were the values that were
maintained, as closely as possible, for the aeration units.
4. The letters N, T, S, M, X and E in the "Filaments" section
represent none, trace, slight, moderate, excessive and
epidemic concentrations, respectively.
110
-------
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
—1>- PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
<^> POSITIVE DISPLACEMENT PUMP
E] CELL FILLED WITH TAP WATER, (DEAD CELL)
PILOT PLANT OPERATION 2/23/68-3/19/68
2/2 J CS FEED FLOW TO CELL 7
2/26 K FEED FLOW TO CELL 7
3/19 K RAS FLOW SPLIT Rn i Re • ,50 '.50
PILOT PLANT FLOW SCHEMATICS
DONOHUE a ASSOCIATES,INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
SCALE '/„" • I'-O"
-------
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
—C>— PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
^m POSITIVE DISPLACEMENT PUMP
g] CELL FILLED WITH TAP WATER, (DEAD CELL I
H PREAERATION CELL
§§/••• DIGESTER SUPERNATANT FEED SYSTEM
PILOT PLANT OPERATION 3/19/68-5/20/68
3/19 CS STARTED PREAERATION
S/£7 K STARTED DIGESTER SUPERNATANT FEED; RAS SPLIT Rn'Rc -.15 ' .85
4/5 K RAS FLOW SPLIT Rn* Re-.30 • .70
4/10 SA STARTED STEP FEEDING
4/17 C STARTED PREAERATION •, CONTACT ZONE REDUCED TO 8 CELLS
PILOT PLANT FLOW SCHEMATICS
DONOHUE » ASSOCIATES,INC. CONSULTING ENGINEERS
SHEBOTGAN, WISCONSIN
SCALE 3/|6" • I'-O"
AIR COMPRESSORS
-------
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
—>- PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
<0> POSITIVE DISPLACEMENT PUMP
H CELL FILLED WITH TAP WATERi IDEA!
• PREAERATION CELL
©-•• DIGESTER SUPERNATANT FEED SYSTEM
N NUTRIENT FEED SYSTEM
PILOT PLANT OPERATION 5/21/68-7/25/68
S/21 C.SA.CS STARTED FEEDING PHOSPHORUS & BOD • P - 100' 1.5
6/21 C.SA.CS STARTED FEEDING NITROGEN (q) BOD - N ' 100- 5.0
7/2 C REDUCED PREAERATION JONE •, INCREASED CONTACT ZONE
7/23 SA STARTED PREAERATION
PILOT PLANT FLOW SCHEMATICS
DONOHUE B ASSOCIATES, INC. CONSULTING
SHEBOYGAN, WISCONSIN
SCALE 3/IR'
. I'-O"
FEDERAL WATER QUALITY ADMINISTRATION
PROJECT 12130 EDX
-------
MILL EFFLUENTS
FROM
TANK TRAILER
LE6END
—1>- PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
fflTO POSITIVE DISPLACEMENT PUMP
£3 CELL FILLED WITH TAP WATER; (DEAD
• PREACRATION CELL
@— DIGESTER SUPERNATANT FEED SYSTEM
N NUTRIENT FEED SYSTEM
PILOT PLANT OPERATION 7/26/68-9/17/68
7/26 C INCREASED PREAERATION ZONE; REDUCED CONTACT ZONE
7/26 SA INCREASED PREAERATION ZONE
PILOT PLANT FLOW SCHEMATICS
DONOHUE 8 ASSOCIATES.INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
SCALE V." • I'-O"
-------
PILOT PLANT OPERATION - PHASE I
Date
Plant
Action
C SA CS K
February 6 x
February 16 x
February 23
February 26
March 19
March 19
March 27
March 27
April 3
April 10
April 17 x
April 25
May 2
May 10
May 24
May 24
x
X
X X
X X
X X
X
X
X
X
XX XX
Startup as C units on Metro feed.
Began mill waste feed.
Converted C schematic to CS schematic.
Converted C schematic to K schematic.
Began preaeration of PE.
Split RAS flow 50-50 to nitrifying and
contact sections.
x RAS split changed to Rn-15%, Rc-85%.*
x Digester supernatant feed started
at 0.015 x Q.
x RAS split changed to Rn-30%, Re-70%.
Began step feeding at 1/4 points.
Began preaeration of PE; aeration
section reduced to 8 cells.
Shock chlorination
Shock chlorination
Shock chlorination
PE-bypassing system installed to main-
tain F/M between 0.35 and 0.40.
Phosphoric acid fed to maintain
BOD:Ortho P (as P) at 100:1.5 in PE.
*n - nitrification section
c - contact section
Table23 Page 119
-------
PILOT PLANT OPERATION - PHASE I (Continued)
Date
Plant
Action
May 24
June 19
June 21
June 21
July 1
July 2
July 12
July 23
July 26
C SA CS K
x x
X X
X X
X
X
Began mathematical calculations for
daily adjustment of RAS flow, WAS
flow and PE-bypass flow.
Shock chlorination.
Shock chlorination.
Ammonium chloride fed to maintain
BOD:NH3 (as N) at 100:5.0 in PE.
Dissolved oxygen in aeration sections
reduced to overcome denitrification in
final clarifiers.
Reduced preaeration section to one cell.
Shock chlorination.
Began preaeration of PE.
Increased preaeration section to two
cells.
Table 23 Page 121
-------
PILOT PLANT OPERATION - PHASE I - 3/1/68 - 8/31/68
CONVENTIONAL UNIT
BOD:N
BOD:P
Preaeration
Mixed Liquor
Shock
March ' April
7.0 I 4.9
1.5
n
1.1
May
June
July
August
-tlO
10
-1
o 3
•4-H
"3
CO
UH
10
-2
2
0
2
0
2
0
90
60
30
0
^lO1
10l
O
UH O
?:;
P o
PQ
PQ
c
o
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n)
C
o
s
u
10
-I 10
E
X
M
S
T
N
,
CO ^
' bO
-2
0)
S
rt
Figure 17 Page 123
-------
PILOT PLANT OPERATION - PHASE 1-3/1/68 TO 8/31/68
STEP AERATION UNIT
BOD:N
BOD:P
Preaeration
Mixed Liquor
Shock
I 7.0 | 4.9
I 1.5 I 1.1
n
I
March I April I May I June «
-, io-J
10
3
10
10
-, 6
4
2
0
2
, to --
- i (JO
-2
' a
0
2
0
90
o J2
£ U
6^
p a
c
O
60 g
30 o
i—i
0 U
10
1
July I August
Figure
c^C
10"1 co S
-•lo-2
E
X
M
S
Tr-Ti
1-1
N
18 Page 125
c
(LI
a
-------
PILOT PLANT OPERATION - PHASE I - 3/1/68 TO 8/31/68
CONTACT STABILIZATION UNIT
BOD:N
BOD:P
Preaeration
Mixed Liquor
Shock
I 7.0 I 4.9
I 1.5 I 1.1
1—JL
March | April | May I June I July
10
-1
10° S
-I 10
6
4
2
-2
ft o
Q £
90 |
60 |
• i-l
30 o
0 5
10
10
E
X
M
S
T
N
-1
-2
OS
ra
-4->
C
£
ri
August
Figure 19 Page 127
-------
PILOT PLANT OPERATION - PHASE 1-3/1/68 TO 8/31/68
KRAUS UNIT
BOD:N
BOD:P
Preaeration
Mixed Liquor
Shock
2.4
3.0
0.2 I 0.3
n
March I April ' May
-i 10
-1
10V
10"1 W
-> 10
6
4
2
-2
Pn O
0
2 <«
0 £
2
0
90 |
60 g
30 o
t—I
0 O
10
1
10
CO
-llO-2
E
X
M
S
T
N
I June ' July ' August
Figure 20 Page 129
-------
Nutrient addition was based on the concentration of BOD, ammonia (as
N) and ortho phosphorus (as P) in the primary effluent. Utilizing
ammonia and ortho phosphorus in the ratio, rather than total nitrogen
and total phosphorus, assured that adequate nitrogen and phosphorus
were available for biological growth. Ammonium chloride and phos-
phoric acid were added as required to maintain the desired BOD:N:P
ratios.
Digester supernatant addition during Phase I and Phase II was set at
1.5% of the primary effluent flow to the Kraus unit, based upon previous
operating records for the Kraus process at other locations. During
Phase III, digester supernatant was used as a phosphorus source; the
quantity added was controlled to obtain the desired BOD:P ratio. The
ammonia nitrogen concentration in the supernatant was usually in
excess of that required to maintain the desired BOD:N ratio when
satisfying the phosphorus requirements.
Since the ratio of the suspended solids in primary effluent and supernatant
was used in Kraus plant operational control at other locations, this ratio
was calculated and presented on the data sheets during Phase III.
Shock chlorination of the aeration tank and final clarifier contents was
conducted at dosages of 30 to 90 mg/1 in an attempt to overcome the
filamentous bulking problems. There was normally an immediate
improvement in the settling characteristics of the mixed liquor after
shock chlorination; however, the improvement was usually temporary.
Best results were obtained at a dosage of 90 mg/1.
Changes in pilot plant operating parameters were also made in an effort
to obtain satisfactory operating conditions. The operating parameters
at startup are presented on Page 102. On May 24, the decision was
made to limit the maximum F/M ratio to 0.375 by bypassing primary
effluent. Adjustments in the concentration of volatile suspended solids
in the mixed liquor were made on May 31, June 12 and July 9 to parallel
the average BOD of the primary effluent.
On July 18 the following conclusions were reached on possible causes of
poor operation:
1. Based upon oxygen uptake data for the conventional unit, the
detention time (based upon R + Q) should be about five hours.
2. The solids loadings on the final clarifiers were high which
could result in the final clarifier being a limiting unit process
in the overall system.
130
-------
3. The maintenance of mixed liquor volatile solids concentrations
in excess of 4000 mg/1 is not in accordance with present-day
practice and may result in limited flexibility in the present
operation.
On August 1, pilot plant operating parameters were revised as follows:
1. Average primary effluent BOD - 540 mg/1.
2. Maximum F/M ratio - 0.375.
3. Maximum total suspended solids loading on final clarifiers -
20 Ibs/sq ft/day.
4. Estimated return activated sludge volatile suspended solids
concentration - 9000 mg/1.
5. Maximum overflow rate on final clarifiers - 600 gpd/sq ft.
6. Maximum allowable recirculation ratio, R/Q - 0.75.
7. Average daily flow to pilot plants - 4100 liters/day; (a
reduction from 1 gpm to 0.75 gpm per plant).
The new operational parameters used are presented in Table 24. The
above changes resulted in an immediate and significant reduction of the
sludge blanket levels in the C, CS and K processes to a level below the
bottom of the final clarifier windows. The SA sludge blanket remained
near mid-depth during August.
The average BOD and TSS values for Phase 1 are presented in Table 25.
Based upon the performance of the units during August, which was the
best overall period of operation since startup of the units, the conclusion
was reached that the combination of wastes being fed to the pilot plants
was biologically treatable in a continuous-flow system. Additional
studies for the next phase were then outlined to attain the following
objectives:
1. Obtain good reliable solids separation in the final clarifiers.
2. Conduct additional studies to estimate capital and operating
costs for each process.
3. Select the most desirable process based upon costs and
operational features.
131
-------
PILOT PLANT OPERATIONAL PARAMETERS
August 1, 1968
Table
NJ
P
(D
Plant No. of Cells
Preaeration Reaeration Contact
Conventional 2 8
Step Aeration 1 8
Contact
Stabilization 1 44
Kraus 4 4
Notes
1. Due to utilizing two cells of the conventional
portion of the flow to that plant to obtain the
conventional unit was 3660 liters/day rather
2. N and P were added to C, SA and CS Units.
3. Digester supernatant feed to the Kraus unit =
Mixed Liquor
Volatile Suspended Solids
mg/1
Cell 10 - 3860
Cell 4 - 6750
Cell 10 - 3860
Cell 10 - 3860
Cell 10 - 3860
RAS Q Max.
VSS R/Q
mg/1 1/d
9000 3660 0.75
9000 4100 0.75
9000 4100 0.75
9000 4100 0.75
F/M
0.375
0.32
0.25
0.25
unit for preaeration, it was necessary to bypass a
desired F/M ratio. Thus, the forward flow to the
than 4100 liters /day.
= 1.5% of average Q.
u>
UJ
-------
BOD AND TSS REMOVAL - PHASE I
Primary Influent
Primary Effluent
Final Effluent*
Conventional
Step Aeration
Contact Stabilization
Kraus
February 6 - August
mg/1
BOD
529
505
68
89
91
96
31, 1968
TSS
237
152
121
159
128
143
Percent
BOD
4.5
86.6
82.4
82.0
81.0
Removal*
TSS
35.9
20.4
0
15.8
5.9
a4
i—'
0>
* The final effluent percent removals are based on the difference between PE and FE values;
the values shown are secondary treatment removal efficiencies only.
OJ
Ul
-------
PILOT PLANT RESEARCH - PHASE II
Statistical Experimental Design
A statistical experimental design was utilized to compare the four
activated sludge processes under a variety of operating conditions.
The primary objective was to determine which of the four processes
was best in terms of effectiveness and stability. A secondary objective
was to determine the best operating conditions for the respective
processes.
In choosing the independent and dependent variables for the experimental
design, the relationships between operating parameters such as flow
rate, mixed liquor suspended solids, F/M ratio, and detention time
were investigated. The purpose was to choose two independent
variables which would produce the maximum change in the response
variables observed. The two independent variables selected were the
mixed liquor total suspended solids concentration and the flow rate.
The question of biasing the experimental design in favor of one process
arose, since preaeration or nutrient feeding was not presently a part of
the Kraus process. (The digester supernatant feed to the Kraus unit
was based on forward flow; however, checks on the BOD:nutrient ratios
indicated there were no serious nutrient difficiencies.) The conclusion
was that four individual processes were being investigated, each with
its own specific operating parameters. The addition of preaeration
and nutrient feeding to three of the four processes was an integral part
of those particular processes in order to operate them in an acceptable
manner.
The permissible range for the forward flow rate and mixed liquor total
suspended solids concentration was a function of the allowable solids
loading on the final clarifier and the estimated return activated sludge
concentration. The average solids loading for the final clarifiers to
maintain good operation was previously selected during Phase I to be
about 20 Ibs/sq ft/day TSS. For this experimental design a maximum
loading of 30 Ibs/sq ft/day at average flow was chosen to provide an
operating condition of maximum stress on the units. The maximum
MLTSS concentration selected was 5000 mg/1; the estimated average
RAS concentration was 10, 000 mg/1 TSS.
137
-------
Utilizing these maximum operating values, the following five operating
conditions for each plant were established:
CONDITION I II III IV V
MLTSS, mg/1 5000 5000 3500 2000 2000
FLOW, gpm 0.8 0.4 0.6 0.4 0.8
RUN NUMBER 1 2 4, 6 3 5
Each of the above conditions was run until an apparent equilibrium of
the processes was achieved for that given condition. Response data
were then accumulated over a 7-day period. The schedule of operation
is presented in Table 26. One condition was duplicated in order to
evaluate the variability of the data obtained.
The theoretical conditions of pilot plant operation are presented in Table
27. The flow schematics utilized during the experimental design are
presented in Figures 21 and 22.
The relationships between preaeration, dissolved oxygen, chlorination,
nutrients, sulfides, and filamentous microorganisms during the six
runs are shown in Figures 23-26.
Summary of Pilot Plant Operation During Phase II
During all phases, the mill wastes were pumped at a continuous rate to
the pilot plant units. Beginning September 16, 1968, and continuing
through Phases II, III, and IV, the Metro sewage pumped to the pilot
plants was varied proportionately to the flow through the existing GBMSD
full-scale treatment plant. (Refer to the section entitled Pilot Plant
Operation.)
The average primary effluent BODs for Runs 1-6, respectively, were 469,
530, 609, 522, 667 and 372 mg/1. During Phase II and III the average
quantities of ammonia and ortho phosphorus contributed by the digester
supernatant to the Kraus unit were included in the BOD:N:P ratio
calculations.
138
-------
STATISTICAL EXPERIMENTAL DESIGN SCHEDULE -- 1968-1969
8-
i—i
fl>
N)
(U
TO
Run
1
2
3
4
5
6
Operating
Condition
I
II
IV
III
V
III
Acclimation
September 9 -- October 7
October 15 October 25
November 2 November 14
November 22 -- December 4
December 12 --December 28
Data Collection
Orf-oKpr Q _ _ __ _ Orfr>Vi<=>r 14-
October 26 November 1
November 15 --November 21
December 5 December 11
December 29 --January 4
January 25 January 31
Total Length
of Run,
Days
36
18
20
20
24
27
OJ
-------
THEORETICAL PILOT PLANT OPERATION - PHASE II
I
n
m
IV
V
Q
gpm
0.80
0.40
0.60
0.40
0.80
R
gpm
0.80
0.40
0.32
0
0.10
0.20
R/Q
1.00
1.00
0.54
0.25
0.25
Dig.*
Sup.
gpm
0.012
0.006
0.009
0.006
0.012
Detention Time, Hours
Contact
R + Q + Dig. Sup.
C
3.8
7.5
6.5
12.0
6.0
SA
3.8
7.5
6.5
12.0
6.0
CS
1.9
3.8
3.3
6.0
3.0
K
1.9
3.7
3.2
5.9
3.0
Reaeration
R+Dig. Sup.
CS
3.8
7.5
9.3
30.0
15.0
K
11.9
23.8
28.3
84.0
41.7
MLTSS
mg/1
5000
5000
3500
2000
2000
F/M
(BOD/VSS)
C
0.38
0.19
0.41
0.48
0.96
SA
0.30
0.15
0.29
0.30
0.60
CS
0.26
0. 13
0.21
0. 16
0.32
K
0.27
0.14
0.23
0.17
0.34
Final Clarifier
Solids Loading
Lbs/5q ft/day
30.6
15.3
12.4**
3.8**
7.6**
* Kraus unit only.
** Kraus values for these conditions are 12.5, 3.9 and 7.7 Lbs/Sq ft/day respectively.
cr Note:
»— ' — — — -
(D
CD
}—•
#»
1. MLVSS estimated at 90% of MLTSS for C, SA and CS units and at 85% for K unit.
2. RAS-TSS estimated at 10, 000 mg/1.
-------
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
~C*~ PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
^^ POSITIVE DISPLACEMENT PUMP
[§| CELL FILLED WITH TAP WATER; (DEAD
• PREAERATION CELL
@— DIGESTER SUPERNATANT FEED SYSTEM
N NUTRIENT FEED SYSTEM
C -CHLORINE FEED SYSTEM
PILOT PLANT OPERATION 9/18/68- 1/14/69
9/18 C.SA.CS CHANGED NUTRIENT FEED POINT TO CONTACT ZONE
KVI C.SA STARTED PRECHLORINATION
PILOT PLANT FLOW SCHEMATICS
DONOHUE 8 ASSOCIATES,INC. CONSULTING ENGINEERS
SHEBOYOAN, WISCONSIN
SCALE 5/,6" • 1-0"
PROJECT 12130 EDX
-------
FINAL
CLARIFIERS .*
v .' TO SEWER
WASTE SLUDGE FACILITIES
LEGEND
—&— PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
ASTE ACTIVATED SLUDOE PIPING
OSITIVE DISPLACEMENT PUMP
ELL FILLED WITH TAP WATER) (DEAD CELL)
REAERATION CELL
IQESTER SUPE
N NUTRIENT FEED SYSTEM
C CHLORINE FEED SYSTEM
l/IS/69- 1/31/69
PILOT PLANT OPERATION
I/IS C STARTED RAS CHLORINATION
I /23 SA STARTED RAS CHLORINATION
PILOT PLANT FLOW SCHEMATICS
DONOHUE 8 ASSOCIATES.INC. CONSULTING
SHEBOYGAN, WISCONSIN
SCALE '/,." • l'-0°
-------
PILOT PLANT OPERATION - PHASE II - 9/1/68 TO 1/31/69
CONVENTIONAL UNIT
I 3.3
BOD:N
I 11.8 I 9.9 I 9. 1 I 5.7 I 6.4 I 12.4
BOD:P
I 1.9 I 0.9 I 0.9 I 1.7 I 3.5
Preaeration
Mixed Liquor
Shock
Prechlorination
RAS
September I October I November 'December I
-i 10
-1
-i ' a
10 W
ft
10
6
4
0
2
0
2
0
90
60
30
0
-I 10
-2
1
§§
m m
o-J2
. •->
o .?
.
p E
o
•H
4->
rt ^
.S bo
O
II)
•o
10
-1
03
-------
PILOT PLANT OPERATION - PHASE II - 9/1/68 TO 1/31/69
STEP AERATION UNIT
BOD:N
I 11.6 I 10.4 I 9.1 I 5.3 I 6.0 I 10.0
BOD:P
I 3.3 I 2.0 I 0.9 I 0.8 I 1.5 I 2.7
Preaeration
Mixed Liquor
Final Clarifier
Shock
P rechlorination
RA
10
-1
in
10
0
in
ft
io-2
6
4
2
0
2
0
2
0
90
60
30
0
IO1
10°
io-1
o
P
O
m
.3
o «
bo
g
d
o
u
io
E
X
M
S
T
N
-2
a
n)
September' October ' November ' December January
Figure 24 Page 149
-------
PILOT PLANT OPERATION - PHASE II - 9/1/68 TO 1/31/69
CONTACT STABILIZATION UNIT
BOD:N
I 9.1 I 10.0 I 9.2 I 5.3 I 6.1 I 10.0
BOD:P
I 2.4 I 1.9 I 0.9 I 0.8 I 1.5 I 2.7
Preaeration
Mixed Liquor
Final Clarifier
Shock
September ' October
November ' December ' January
10
-i
10° «
-1 10
-2
O
0
2
0
2
0
90
60
30
0
§8
PQ pq
o
I
.
p 6
c
o
U
10
10
0 ?
-1
>-2
E
X
M
S
T
N
en
-JJ
C
E
a)
Figure 25 Page 151
-------
PILOT PLANT OPERATION - PHASE II - 9/1/68 TO 1/31/69
KRAUS UNIT
BOD:N
8.9 I 7.9 I 10.8 I 6.2 I 5.1 I 5.8
BOD:P
1.2 I 0.7 | 0.8 | 0.9 I 0.7 | 0.7
Preaeration
Mixed Liquor
10
-1
-------
Operational Summary
Run 1, Condition I
CS - Best physical operation of the four plants.
CS and K - Decrease in treatment efficiency compared to August;
process more stable than C and SA.
K - Good-settling mixed liquor; higher TSS and BOD in effluent
than CS.
C and SA - Did not achieve desired MLTSS concentration.
SA - Higher TSS and BOD in effluent than C.
Run 2, Condition II
CS - Best overall performance, followed by C.
SA - Least-stable process; did not achieve desired MLTSS; RAS
concentration did not exceed 9000 mg/1; final clarifier
sludge blanket rose to weir level.
K - Quite stable, but higher TSS and BOD in final effluent than
C and CS.
Run 3, Condition IV
C - Best operation of four plants.
C, CS - Clear effluent.
SA, K - Cloudy effluent.
SA, CS, K -Erratic RAS concentration; difficult to maintain correct
MLTSS in K unit.
Four plants generally operated well during this Run; no
apparent problems due to filamentous microorganisms.
154
-------
Run 4, Condition III
K - Superior performance, followed in order by CS, C and SA.
C, SA - Did not achieve desired MLTSS concentration; had high TSS
and BOD in final effluent; RAS-TSS less than 5000 mg/1.
Filaments - C-moderate; SA-slight; CS-excessive; K-slight.
Run 5, Condition V
During this run the pilot plants were subjected to the most over-
loaded operating conditions of the experimental design. As a result,
filamentous growths occurred in the C, SA and CS plants causing
severe bulking conditions and subsequent loss of biological solids
in the final effluent. The K unit, although containing filaments and
exhibiting poor effluent quality, did not have any filamentous bulking
problems.
Run 6, Condition III
The purpose of this Run was to repeat the operating condition of
Run 4, Condition III. As this Run followed Run 5, Condition V,
which was a highly-overloaded operating condition, the plants
required a period of time to recover and begin operating at the
desired conditions for Run 6.
On January 5, the C, SA and CS plants were shock chlorinated;
bypassing of the feed to the C, SA and CS plants between January 5
and January 25 was also conducted to reduce the F/M values to a
level to allow the plants to regain good operation. On January 14,
the C, SA and CS plants were again shock chlorinated in an effort
to eliminate the bulking conditions.
On January 5, there were excessive filaments in the C, SA and CS
plants which appeared to be of the Sphaerotilus natans variety; (no
sulfur granules were observed). About January 11, a biological
change took place in that a Thiothrix variety appeared to become
the more dominant filament present. The amount of filaments in
the four pilot plants was slight to moderate during the seven-day
period of tests, January 25 to January 31. The microbiology report
stated that the biological conditions were as good as had been
observed for some time.
155
-------
Chlorination of the return activated sludge at 30 mg/1 for the C and
SA units was begun January 15 and 23, respectively. An immediate
increase in RAS concentration resulted.
In summary, the pilot plants operated as well during Run 6 as any
time during the experimental design. This can probably be
attributed to the lower primary effluent BOD and also to the
chlorination of the return activated sludge for the C and SA units.
Statistical Experimental Design - Laboratory Data
Data were obtained for 13 response variables during the last seven days
of each run. The response variables in order of importance were:
1. Final effluent filtered BOD (7)
2. Final effluent total suspended solids (7)
3. Final clarification (1)
4. Filament concentration (2-3)
5. Pounds oxygen re quired/pound BOD removed (1)
6. Return activated sludge concentration (7)
7. Sludge production (7)
8. Specific filtration resistance of WAS (1)
9. Air flotation of mixed liquor and WAS (1)
10. Final effluent filterability index (1-3)
11. Final effluent unfiltered BOD (7)
12. Final clarifier sludge level (7)
13. Final effluent color (2-3)
The numbers in parentheses are the number of tests averaged to obtain
the values for each plant:for each run.
156
-------
The summary of data obtained for each of these 13 responses is presented
in Figures 27 to 34. Figure 27 shows the operating conditions and
respective run numbers located according to the mixed liquor total
suspended solids and forward flow for that particular run. Figure 34
shows the MLTSS concentration and the detention time in the contact
and reaeration section which actually occurred during each run. The
following comments apply to these Figures:
1. The data shown are the average of the values obtained during
the last seven days of each run. (Where appropriate, data
columns are identified in the lower right hand corner of the
Figures.)
2. Standard deviations were computed for several of the response
variables and are listed under the abbreviation, S.D.
3. Final effluent filtered BOD's were run on samples filtered
through Whatman No. 5 filter paper.
4. The abbreviations C.R. and TC for the response variable,
final clarification, refer to the clarification rate (gpd/sf) and
time of concentration (minutes) to obtain a 1% underflow
c one entration.
5. The sludge production data are based upon both unfiltered
BOD's (PE and FE BOD values) and' filtered BOD's (filtered
PE and filtered FE BOD values).
6. SFR = specific filtration resistance
7. The color data are as standard units, based upon a platinum
cobalt standard.
8. The procedures for the final clarification studies, air flotation
studies and sludge production calculations are presented in
Appendix B. All other test procedures utilized in the experimental
design are presented in the section entitled Laboratory Staff,
Equipment, Procedures and Data Reduction.
9. During Run 6, Condition 3 (1/5/69-1/31/69) the C and SA units
began receiving RAS chlorination as indicated by an asterisk.
157
-------
STATISTICAL EXPERIMENTAL DESIGN SCHEDULE
0.8-
6
a
60
o
0.6-
0.4-
CONDITION V
Run 5
12/12/68 - 1/4/69
CONDITION I
Run 1
9/9/68 - 10/14/68
CONDITION in
Run 4
11/22/68 - 12/11/68
CONDITION HI
Run 6
1/5 /69 - 1/31/69
(#-Keceiving RAS-C12)
CONDITION IV
Run 3
11/2/68 - 11/21/68
CONDITION II
Run 2
10/15/68 - 11/1/68
FINAL EFFLUENT FILTERED BOD, (mg/1)
SA 83
K 98
C 101
CS 101
C 1
SA 1
0
9
CS 30
K 42
1
30
17
31
46
Run 4
CS 18 12
SA 25 18
K 36 23
C 45 31
5
16
18
31
1
C
SA
CS
K
Run 6
CS 22 6
SA 25 6 *
K 36 11
C 53 14 *
1
CS
SA
K
C
1
11
1.2
15
19
Avg|
11
12
13
14
1
4
6
9
4
S.D. |
9
10
14
9
6
ex
a
0.8-
0.6-
0.4-
2000 3500 5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 27 Page 159
-------
FINAL EFFLUENT TSS, (mg/1)
0.8-
£
a,
00
£
Q
^"^ 0 o ^
Tl
In
rt
0
0.4-
K
C
CS
SA
K
C
SA
CS
97
269
408
481
53
54
56
83
42
207
147
230
Run 4
K 45 33
CS 62 81
C 130 66
SA 296 230
29
18
29
82
C
K
CS
SA
Run 6
CS 20 10
K 36 19
SA 52 12 *
C 60 18 *
CS
C
K
SA
24 17
71 22
82 119
94 95
Uvgls.D.
26 14
29 15
40 14
118 175
FINAL CLARIFICATION
K
CS
C
SA
CS
K
C
SA
1474
1]
37
509
345
3544
2360
1266
898
89
244
383
489
Run 4
K 1062 93
CS 1092 107
C 497 299
SA 455 355
64
93
128
164
CS
K
C
SA
Run 6
C 1616 39 *
SA 1400 60 *
CS 862 90
K 754 95
1
CS
K
C
SA
694
456
434
1.94
C.R.
539
388
208
278
204
191
287
702
TC|
166
264
357
377
0.8 -
£
a
00
h
•C
It
*
0.6 -
0.4 -
5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 28 Page 161
-------
FILAMENT CONCENTRATION
0.8-
l
60
0.6-
nt
O
0.4-
K slight
SA moderate
C excessive
CS excessive
Run 4
K slight
SA slight
C moderate
CS excessive
C slight
K slight
CS moderate
SA moderate
K slight
C moderate
CS moderate
SA excessive
Run 6
C slight *
CS slight
K slight-moderate
SA slight-mode rate *
C slight
CS moderate
K moderate
SA moderate
1
1
Lbs. OXYGEN REQUIRED / Lb. BOD REMOVED
0.8-
g
a,
CD
O
£ 0.6-
Li
a
o
h
0.4-
CS
SA
C
K
CS
C
SA
K
1.00
1.03
2.31
4.92
Run 4
C 1.20
SA 1.21
K 1.65
CS 2.27
1.55
1.56
1.67
1.95
C
CS
SA
K
Run 6
SA 1.08 *
C 1.30 *
CS 2.07
K 2.69
K
C
CS
SA
0.61
0.88
0.95
1.06
1.72
1.72
1.78
2.00
2000 3500 5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 29 Page 163
-------
RAS CONCENTRATION. (TSS. mg/1)
0.8-
6
a
M
>
h 0.6-
rH
T)
rt
0
fc
0.4-
K
C
CS
SA
K
SA
CS
C
15693
3027
2639
2123
14547
10677
9752
6809
i
5989
1440
613
598
Run 4
K 15672 3572
CS 10270 624
C 4957 884
SA 4593 474
4059
2217
1193
698
K
CS
C
SA
Run 6
K 12304 1953
CS 10937 1000
9255
8187
6371
6353
1013
1176
795
654
C 10467 2019 *
SA 9031 2460 *
K
CS
C
SA
Avg.
10841
10443
8385
7651
S.D.
1677
393
423
593
SLUDGE PRODUCTION. (Lbs. TSS Produced/Lb. BOD Removed)
K 0.
C 0.
CS 0.
SA 1.
SA 0.
C 0.
CS 0.
K 0.
77
81
94
11
42
55
56
70
0.84
0.69
0.79
0.90
Run 4
C 0.46 0.49
CS 0.48 0.55
K 0.49 0.55
SA 0.85 0.75
0.44
0.60
0.62
0.77
C
CS
SA
K
Run 6
C 0.53 0.58 -
0.60
0.84
0.86
1.10
L.
r*
0.62
0.86
0.83
1.05
SA 0.53 0.61 *
CS 0.54 0.67
K 0.84 0.99
C
SA
K
CS
U-BOD
0.35
0.6.0
0.65
0.67
F-BOD
0.38
0.56
0.68
0.74
O
-h
0.8-
s
a
DO
I
0.6-
0.4-
2000 35~00 5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 30 Page 165
-------
SFR - WASTE ACTIVATED SLUDGE. ( x 107 sec2/grams)
0.8-
1
t>0
fc
Forward Flo*
o
•
o
1
0.4-
0.8-
e
a
W)
r-t ^ ,
k 0.6-
-o
*•
(d
0
h
0.4-
CS 435
SA 912
K 2440
C 3770
CS 240
K 370
C 380
SA 1060
1
AIR
K
CS
SA
C
SA 267
K 303
CS 320
C 730
Run 4 Run 6
CS 234 CS 195
K 569 K 400
SA 814 SA 540 *
C 1810 C 1460 *
CS 159
K 166
SA 234
C 362
1 ~~ I
FLOTATION of WAS & MIXED LIQUOR
CS
C
SA
K
Run 4 Run 6
C CS
K K
SA C *
CS SA *
NOTE: Run Nos. 1 and 6 utilized WAS, all others M.L.
Relative ranking shown.
CS
K
C
SA
CS
SA
K
C
2000 3500 5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 31 Page 167
-------
FINAL EFFLUENT FILTERABILITY INDEX
0.8-
a
60
0.6-
o
h
0.4-
SA
K
C
CS
C
SA
K
CS
0.
0.
0.
0.
0.
Q.
0.
0.
0530
0662
3240
6480
Run 4
K 0.0795
CS 0.0828
C 0.1093
SA 0.1248
0342
0365
0657
0972
SA
C
CS
K
Run 6
C 0.0449*
SA 0.0463*
CS 0.0464
K 0.0894
C
CS
SA
K
0.0228
0.0303
0.0369
0.1336
0.0294
0.1261
0.1704
0.2202
FINAL EFFLUENT UNFILTERED BOD, (mg/1)
0.8-
£
a
0.6-
•a
d
0.4-
K 188 44
C 290 85
CS 295 86
SA 296 84
C 84 43
CS 91 45
SA 114 41
K 114 53
Run 4
CS 64 65
K 96 33
C 126 54
SA 181 88
Run 6
CS 34 8
SA 56 14 *
K 64 13
C 103 16 *
C 35 17
CS 5.8 63
SA 79 81
K 92 21
|Avg|S^|
CS 45 18
C 47 29
K 66 29
SA 115 140
—1 1 1"
2000 3500 5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 32 Page 169
-------
FINAL CLARIFIER SLUDGE LEVEL, (inches)
0.8-
H
a
£
h 0.6-
nt
0
h
0.4-
K 3 6
C 51 28
SA 69 6
CS 70 5
Run 4
K 4 11 K
CS 50 11 C
C 50 15 S
SA 51 12 C
COO
SA 0 0
CS 0 0
K 0 0
I
K 38 5
C 42 4
CS 52 13
SA 57 14
Run 6
1 4 11
; 12 15 *
A 26 10 *
:s 30 o
Avg S.D.
CS 21 10
K 41 10
C 42 5
SA 55 12
1
FINAL EFFLUENT COLOR. (S.U.)
0.8-
g
a
w>
|
h 0. 6-
-o
to
tS
*
to
0
h
0.4-
CS
C
SA
K
SA
K
C
CS
482
488
488
522
Run 4
CS 293
K 299
SA 311
C 336
399
439
461
461
C
SA
CS
K
Run 6
SA 170 *
K 179
CS 186
C 195 *
SA
C
CS
K
330
330
339
360
378
380
386
388
_ •
2000 3500 5000
Mixed Liquor Total Suspended Solids, mg/1
Figure 33 Page 171
-------
ACTUAL, MLTSS (mg/1) AND DETENTION TIME (Hours)
0.8-
6
a
t>0
*
J
h 0.6-
-o
14
1 3.3 35.7
\JVILTSS
C 5230
SA 4621
CS 5189
K 5603
5.4
5.2
2.1 4.
2.0 13.
Cont Re«
7.8
7.8
4.5 9.
5.2 42.
1
6
ier
6
3
2000 3500 5000
Desired Mixed Liquor Total Suspended Solids, mg/1
Figure 34 Page 173
-------
Statistical Analysis of the Response Data (*7
A. Response Surface Estimation
If the two independent variables (flow and MLTSS) and the dependent
variable (response) were plotted on a three-dimensional graph, a surface
would be generated. Since only a limited amount of data was available
for each response variable, a linear mathematical model was selected
as the best first approximation to fit the response surface generated by
the data. The model was of the form: Y = bQ + b} (flow) + b2 (TSS),
where Y is the predicted response, flow is the flow rate in gpm, TSS
is the mixed liquor TSS in mg/1 , and bg, bj and b^ are constants.
It was found that a plane surface did not adequately describe the surface
generated by the response data. The lack of fit of the model to the data
was excessive due in part to the generally extreme responses which
were obtained during Run 5, Condition V. Confidence limits for the
coefficients were also extremely large, so that the prediction equations
were of little value.
B. Analysis of Variance
Another approach, that of a simple analysis of variance (ANOVA) was
then conducted. Because the processes were at similar operating
conditions on each Run, and because the processes all received the
same input on each Run, it was possible to consider a model of the
form: Ypc = u + Pp + Cc + (PC)pc, where
Y = Predicted value for the response variable for a given pilot
plant and condition of operation.
u = The grand mean for that particular response variable.
Pp = The effect of a given pilot plant on that particular response
variable.
Cc = The effect of a given operating condition on that particular
response variable, and
(PC)pC = The interaction of the pilot plant and the operating conditions.
(There were not enough data to evaluate this interaction,
therefore this term was used as an error term.)
Knowledge of Cc was not considered important at this time, therefore
the analyses were confined to P and it's.effect on the response variable.
174
-------
The error estimates, based on the estimated value of error from the
fitted model above and also the estimate of error due to the duplicate
data on Condition III, were combined to reduce the confidence limits
for the response variables.
These analyses were conducted on 11 response variables; the standard
deviation for the data, where replicate data existed, was also analyzed.
The response variables analyzed were:
1. Final effluent filtered BOD
2. Final effluent total suspended solids
3. Final clarification
4. Filament concentration
5. Pounds oxygen required/pound BOD removed
6. Return activated sludge concentration
7. Air flotation
8. Final effluent filter ability index
9. Final effluent unfiltered BOD
10. Final clarifier sludge level
11. Final effluent color
For each of the response variables the ANOVA calculations for the
grand mean and its 95% confidence interval were plotted on rectangular
graph paper. The 95% confidence interval for the standard deviations for
final effluent unfiltered BOD and TSS, and RAS concentration were also
plotted. The remaining responses either had extremely large confidence
intervals for the standard deviation, or else no estimate of the standard
deviation was available. The arithmetic values for the grand mean and
the 95% confidence interval were plotted on the abscissa and the natural
log of the standard deviation was plotted on the ordinate for the respective
responses.
The following numerical values were applied to each plant for each
predicted response:
0 -- The predicted value lies within the 95% confidence limits for
the grand mean and the standard deviation.
tl -- The predicted value lies outside the 95% confidence limits for
the mean. (+) = on the desirable side of the grand mean; (-) =
on the undesirable side of the grand mean.
-1 -- The predicted value lies outside the 95% confidence limits for
the standard deviation.
175
-------
A particular response could have one of the following summations:
+ 1+0 = +1 (-1) + 0 = -1
0+0 =0 (-1) + (-1) = -2
(+1) + (-1) = 0
By multiplying this summation times the weighted value of the response
variable (see below ), total summations for the 11 response variables
were obtained, as follows:
Conventional -10
Step Aeration -11
Contact Stabilization -5
Kraus -7
Because of the extreme variability of the data obtained during the six
runs, these results cannot be considered absolutely conclusive. How-
ever, these analyses did indicate that the contact stabilization and
Kraus processes were superior to the conventional and step aeration
processes during the experimental design.
Ranking
Several sanitary engineers were requested to rank the processes for each
of the thirteen responses. The response data were coded and randomized
according to Plant A, B, C and D; the reviewers did not know which
plant was conventional, step aeration etc. The response variables were
then weighted according to their relative importance in plant design:
Response Variable Weighted Value
Final effluent filtered BOD 10
Final effluent total suspended solids 10
Final clarification 10
Filament concentration 9
Pounds oxygen required/pound BOD removed 9
Return activated sludge concentration 7
Sludge production 7
Specific filtration resistance 5
Air flotation 5
Final effluent filterability index 5
Final effluent unfiltered BOD 3
Final clarifier sludge level 3
Final effluent color 3
176
-------
By multiplying the response weight times the process rank value (4-
best, 1-worst) and summing these for each process, average weighted
sums were obtained as follows:
Conventional 210
Step Aeration 188
Contact Stabilization 237
Kraus 249
Maximum possible 344
Minimum possible 86
These results also indicated the contact stabilization and Kraus
processes were superior to the conventional and step aeration processes,
The step aeration process was eliminated from further consideration at
that point, based upon the analyses of the response data and the poor
operation experienced during the statistical experimental design.
Selection of Most Promising Process
The following items were taken into consideration when the results of
the statistical analysis were studied:
1. There was almost continuous preaeration and prechlorination
of the primary effluent feed to the conventional and step aeration
units during the experimental design.
2. Although preaeration was used continuously, prechlorination
was never applied to the CS unit.
3. Neither preaeration nor prechlorination were applied to the K
unit.
For these reasons it is apparent that, from the stability standpoint, the
K unit was superior. Had preaeration and prechlorination not been used
on the C, SA and CS processes, the statistical analysis of the data would
quite likely have shown a greater variation between the processes, much
poorer treatment efficiencies for the conventional and step aeration
units, and somewhat poorer efficiency for the CS unit.
The following subjective factors were also considered in selecting the
most promising processes:
1. Stability of biological process.
177
-------
2. Ability to meet all required effluent standards.
3. Effect of ambient temperature variations upon the process.
4. Versatility of the flow schematic.
5. Ease of mechanical operation.
6. Ease of plant expansion assuming no land limitations.
7. Ultimate solids disposal as related to a specific treatment
process.
8. Adaptability to include advanced treatment processes at a
later date.
These subjective factors are summarized as follows:
Significant Differences Exist Between the Processes
1st 2nd 3rd
1. Process Stability K CS C
2. Effluent standards:
Filtered BOD CS C K
Filterability Index C CS K
3. Versatility of flow schematic K CS C
4. Ease of mechanical operation C CS K
5. Ease of plant expansion C CS K
No Significant Differences Between Processes Are Apparent
1. Effluent standards: TSS, unfiltered BOD, color
2. Ultimate solids disposal
3. Advanced treatment adaptability
Insufficient Information Available
1. Effluent standards: nutrients
2. Effect of ambient temperature variations
178
-------
One subjective factor not listed is the overall plant reliability for
continuous operation, which can be differentiated from plant stability.
The operating reliability of a Kraus process, which contains an aerobic
and anaerobic biological system, would be expected to be less than a
C, SA or CS process which has only one biological system that requires
monitoring and control.
Drs. Polkowski and Boyle, of Polkowski, Boyle and Associates,
Madison, Wisconsin, utilized the laboratory data obtained during the
experimental design to develop theoretical full-scale design parameters
for the C, CS and K flow schematics. These design parameters are
summarized in Appendix F. (In some cases it was necessary to use
alternate rather than the theoretical design parameters due to the
resulting configuration of the full-scale units. These alternate values
are also summarized in Appendix F.)
The design parameters were used by Donohue and Associates, Inc. ,
Sheboygan, Wisconsin, to develop preliminary estimates of comparative
capital and operating costs for the three plants. The flow, BOD and
TSS quantities and the design scale-up parameters used in the cost
estimates are presented in Appendix F. The comparative cost estimates
were as follows:
Preliminary Estimates*
Process Capital Costs Operating Costs
Conventional $15,094,000 $2,116,000
Contact Stabilization $12,970,000 $1,559,000
Kraus $13,005,000 $1,415,000
*(These estimates are based on 1969 dollars and do not include
allowances for administration, engineering, contingencies,
inflation during construction, and some facilities common to
all processes. )
Utilizing the information from the statistical experimental design, the
review of the subjective factors involved, and the preliminary estimates
for capital and operating costs, the contact stabilization and Kraus
processes were selected for additional studies during Phase III. It
was decided that additional detailed information on oxygen utilization,
sludge production, and sludge characteristics was necessary to select
the most desirable of these two treatment processes. An effort would
also be made to ascertain the reason for the biological stability of the
Kraus unit to learn if this factor could be applied to the contact stabiliza-
tion process.
179
-------
RAS CHLORINATION - PHASE II
Upon reviewing the sulfide content in the various streams associated
with the pilot plants, it was observed that a significant concentration of
sulfides was present in the return activated sludge (RAS) streams.
Therefore, chlorination of the RAS was started on the conventional and
step aeration units January 15 and 23, 1969, respectively. The effect
of this procedure on process operating parameters is shown in Figures
35 and 36. (The drop in RAS concentration for the two processes at
the end of the month is due to overwasting WAS from the final clarifier.)
Note also the improved removals of TSS and unfiltered BOD characteristics
of the final effluent and the improved mixed liquor settleability for Run 6
as shown in Figures 28 and 32. The significant drop in RAS-S= and
filament concentrations is quite clearly shown in Figures 23 and 24.
The changes in process microbiology are also presented in Tables 28
and 29.
These data illustrate that RAS chlorination was quite successful in
controlling filamentous bulking problems.
181
-------
EFFECTS OF RAS CHLORINATION - CONVENTIONAL PROCESS
2 3 4 5 6 7 a 9 !O 1 1 12 13 14 15 16 17 18 19 2O 21 22 23 24 25 26 27 2B 29 3O 31
Figure 35 Page 183
MDNTH
-------
EFFECTS OF RAS CHLORINATION - STEP AERATION PROCESS
-liter Cylinder
• t • • ' 4 i
: I : ! J
' 2 3 4 5 6 7 8 9 ' O 1 1 1 2 13 1A 1 5 16 17 18 19 2O 21 22 23 2a 23 26 37 28 29 3O 31
MONTH-
January
.19
69
Figure 36 Page 185
-------
BIOLOGICAL ANALYSES
Date, 1969
January 4
January 7
January 11
January 13
January 15
January 18
January 21
January 25
January 28
January 31
Conventional Process
Excessive filaments present which appear to be Sphaerotilus
natans; no S= granules present.
Filaments have decreased slightly; no S~ granules.
Moderate amount of filaments present; 60% contain S~
granules; appears to be a change over from Sphaerotilus
natans to Thiothrix.
Excessive to epidemic amount of filaments; no S granules;
some flagellates beginning to appear.
STARTED RAS CHLORINATION
Decrease in amount of filaments; no S~ granules.
Only a slight amount of filaments present; no S~ granules;
higher biological forms absent.
Very few filaments of any kind; no S~ granules.
Trace of filaments only; biological condition greatly
improved.
In good condition except for lack of higher biological life;
only a trace of filaments.
Table 28 Page 187
-------
BIOLOGICAL ANALYSES
Date, 1969
Step Aeration Process
January 4 Excessive filaments present which appear to be Sphaerotilus
natans.
January 7
January 11
January 14
January 18
January 21
January 23
January 28
January 31
Excessive filaments present; no S granules.
Slight decrease in filaments; 70% contain S~ in large
quantity; appears that Thiothrix is becoming dominant
species.
Continued decrease in amount of filaments; no S granules;
many flagellates.
Increase in filaments; small amount of S= granules
present.
Moderate amount of filaments present; no S granules;
no higher forms present.
STARTED RAS CHLORINATION
Only a slight amount of filaments present; no S~ granules.
Only a trace of filaments present; higher biological forms
present.
Table 29 Page 189
-------
PILOT PLANT RESEARCH - PHASE III
The pilot plants were shut down for cleaning and maintenance during
February, 1969, having operated continuously from February 6, 1968
to February 1, 1969. The plants were started up using Metro sewage
on February 24, 1969. Mill wastes were gradually added and 100% of
the desired mill flow was reached on March 21, 1969.
Two pilot plant units were operated as control plants and the remaining
two units were set up for variable operation. The plant designations
were as follows:
Designation
Process Primary Alternate
Contact Stabilization - Variable CS-V A
Contact Stabilization - Control CS-C B
Kraus - Variable K-V C
Kraus - Control K-C D
The objectives of Phase III were to obtain additional information on:
1. Oxygen transfer and utilization
2. Sludge production
3. Methods of sludge handling
4. Optimization of operating parameters
a. Detention time in aeration units
b. Mixed liquor solids concentration
c. Nutrient addition
d. RAS chlorination
The primary response variables were:
1. Final effluent unfiltered BOD
2. Final effluent TSS
3. Filamentous microorganism population
191
-------
The control plants were operated on the basis of the theoretical full-
scale design parameters developed at the completion of the statistical
experimental design. The operating parameters for the variable plants
were chosen to minimize the volume of the aeration units (and not
exceed an F/M ratio of 0.4) while maintaining the final clarifier
loadings within an acceptable operating range. The designs were also
selected to have Sat (MLVSS x contact section detention time) values
within the range of those selected for the first preliminary cost
estimate.
The pilot plant operating parameters for the initial startup are presented
in Table 30, flow schematics in Figures 37 and 38, and the relationship
between RAS chlorination and filament concentration in Figure 39. (See
Phase I for nomenclature on Figure 39.)
The average BOD and TSS removals for Phase III, excluding startup
during March, are presented in Table 31. Except for March, the
plants were operated quite closely to the theoretical parameters.
Summary of Pilot Plant Operation During Phase III
March
Due to the slow build-up of biological solids, waste activated sludge
from the Kraus plants was added to the CS-V plant. By April 1, the
CS plants had reached the desired solids concentration in the contact
sections of the aeration units. The Kraus units developed solids quite
rapidly and operated well during March. It was necessary to begin
RAS chlorination of the CS-V unit about mid-March in order to inhibit
the growth of the filamentous microorganisms. This was quite
successful and the plant continued to operate in a normal manner.
April and May
The CS-V, CS-C and K-V units had no operational problems although
the CS-C plant did contain excessive filamentous microorganisms at
various times during April. To counteract the excessive filaments,
RAS chlorination was started April 10 and this was successful in
reducing the filament population.
192
-------
THEORETICAL PILOT PLANT OPERATION - PHASE in
February 24 - July 31, 1969
Parameter
CS Variable CS Control K Variable K Control
Q Forward, 1/d
MLTSS, mg/1
MLVSS, mg/1
RAS-TSS, mg/1
RAS-VSS, mg/1
R/Q
D. -Contact, hrs.
Dj.-Reaeration, hrs.
Sat, mg/l-hr.
4310
4550
4000
9100
8000
1.0
1.9
1.9
7600
4310
3980
3500
9100
8000
0.78
2.7
4.6
9270
4310
5370
4300
12500
10000
0.78
Rn=20%
Rc = 80%
2.2
12.6
9270
4310
4370
3500
12500
10000
0.54
Rn=20%
Rc = 80%
4.3
26.4
15050
F/M
0.35
0.27
0.31
0.21
Nutrient Addition
Dig. Sup. Addition
BOD:N:P
100:5:1
BOD:N:P
100:5:1
BOD:P
100:0.8
BOD:P
100:0.8
Table 30 Page 193
-------
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KRAUS-CONTROL
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PILOT PLANT OPERATION 3/3/69-7/16/69
OW SCHEMATICS
MILL EFFLUENTS
FROM
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— — RETURN ACTIVATED SLUDGE PIPINS
WASTE ACTIVATED SLUDGE PIPING
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PILOT PLANT FLOW SCHEMATICS
DONOHUE 8 ASSOCIATES, INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
SCALE '/i," • I'-O"
PROJECT 12130 EDX
-------
MILL EFFLUENTS
FROM
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RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUOGE PIPING
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T/17 C,D STARTtB FICCHMG NITROGEN (PHOSPHORUS
T/li C,0 CONVERTIO TO CONTACT STABILIZATION FLOW SCHEMATICS
PILOT PLANT FLOW SCHEMATICS
OONOHUE ft ASSOCIATES,INC. CONSULTING ENGINEERS
SHCTCTMN, WISCONSIN
ICALE 5/|6' • I'-O"
-------
PILOT PLANT OPERATION - PHASE III - 3/ 1 /69 TO 7/31 /69
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The K-C operation during April and May was as follows:
4/1-4/20 Normal operation.
4/21 Increase in unfiltered BOD in FE.
4/22 Sludge blanket began rising in final clarifier.
4/23 RAS concentration began decreasing; excessive filaments
containing a significant amount of sulfur granules were
present in mixed liquor.
4/26 Significant increase in TSS in FE.
4/28 Sludge blanket went over weir; sludge blanket level
reduced by slug-wasting WAS; filaments were breaking
up, were branched, and contained less sulfur granules.
4/30 Increased the digester supernatant feed to about 140% of
average flow rate.
5/1 Bypassed 20% of PE feed to reduce F/M ratio; increased
digester supt. feed to about 190% of average flow rate;
sludge blanket over weir.
5/5 Increased digester supt. feed to about 240% of average
flow rate; moderate amount of branched filaments
present - some sulfur granules.
5/6 Bypassing of PE feed increased to 25%. There was no
noticeable effect on the filamentous bulking problem due
to the increased digester supernatant feed.
5/8 Began RAS chlorination at 25 mg/1.
5/9 Decreased digester supernatant feed to average flow
rate. A significant drop in sludge blanket, BOD and
TSS in FE, and increase in RAS concentration occurred.
5/10 Stopped bypassing PE feed.
5/12 Reduced RAS-C12 to 15 mg/1; filaments were breaking
up and were less branched.
5/13 Reduced RAS-C12 to 10 mg/1.
202
-------
5/22 Stopped RAS-chlorination; only a slight number of
filaments present.
5/28 RAS concentration was about 30, 000 m.g/1 and sludge
blanket level at 16 inches.
The CS-V, CS-C, and K-V plants operated well during May. Based
upon the May laboratory data, the CS-V plant had the best BOD removal
efficiency. If an inexplicably high daily value of 624 mg/1 TSS in the
FE for CS-V is eliminated from the monthly data, then this plant also
had the best TSS removal efficiency.
The bulking of the K-C plant due to filamentous microorganisms was
the first occurrence since recovery of the Kraus unit after the upset in
March, 1968. This latest.event was unexpected due to the stable
biological operation of the Kraus unit during Phases I and II. One of
the primary reasons for continuing the study of the Kraus process was
the fact that it was not prone to excessive growths of filamentous
microorganisms during the first year of operation.
Based on the experience in the K-C plant, the conclusion was reached
that RAS chlorination was much more effective than digester supernatant
addition for the control of sulfur-containing filamentous microorganisms.
June
A cursory examination of the effect of nutrient deficiency on process
operation was conducted during June and July. On June 17 the
supplemental feed rate of N and P to the CS plants was reduced to
50% of the normal values and on June 18 the digester supernatant feed
rate to the K units was reduced to 75% of the normal values. On June 24,
the supplemental nutrient feed (including the digester supernatant) to
all the plants was reduced to zero.
The CS plants and the K-C plant operated well during June. The K-V
unit had operational problems during the last half of June. On June 17,
23, and 26, WAS -was slug-wasted in an effort to keep the sludge blanket
below the weir. The split of RAS was also changed to return 50% to the
nitrifying section and 50% to the contact section in an effort to obtain a
lower sludge blanket in the final clarifier. None of these operations
resulted in a continuously lower sludge blanket. The fact that no
digester supernatant was being added after June 24 no doubt aggravated
the situation.
203
-------
In summary, the K-C unit had the best BOD and total suspended solids
removals during June, followed by the two CS units which performed
about equally well. The K-V unit had a slightly lower efficiency, than
the CS units.
July
CS-V
July 28 Supplemental P addition, at BOD:P ratio of 100:0.6,
started in an attempt to create a better settling floe.
CS-C
July 18 Arbitrarily stopped RAS chlorination.
July 22 Settled sludge volume in SVI test began to increase.
July 23 Settled sludge volume exceeded 900 ml.
July 28 Began RAS chlorination and supplemental P addition.
Both K units operated without digester supernatant feed, July 1 to 18.
On July 18, the plants were changed to the CS flow schematic by
returning all RAS to the reaeration section.
K-V
July 1 Began RAS chlorination to counteract high sludge blanket.
July 5 Changed RAS split to 100% to reaeration section.
July 16 Changed RAS split to 20%-reaeration, 80%-contact; no
beneficial effects due to previous setting.
July 17 Began supplemental P feeding.
July 19 Significant increase in RAS concentration.
July 24 Sludge blanket began to subside.
204
-------
K-C
July 1 No sludge blanket visible.
July 8 Sludge blanket visible and increasing rapidly.
July 17 Began supplemental P addition at BOD:P ratio of 100:0.6.
July 19 Sludge blanket over weir.
July 28 Began RAS chlorination.
July 31 Slight increase in RAS concentration.
The CS-V unit had the best BOD and TSS removal efficiency. The CS-C
unit had a somewhat poorer treatment efficiency than CS-V, while both
K units experienced problems with sludge going over the final clarifier
weirs. The CS units operated without any apparent detriment due to the
reduction of supplemental nutrient feedings; the two Kraus units
exhibited a poor-settling sludge and on July 17 the sludge went over
the weirs in both the K-V and the K-C plants. The poor-settling
sludge was not due to filamentous microorganisms, as in the past, but
was due to the characteristics of the floe which would not allow it to
settle and compact.
In general, RAS chlorination of the K-V unit had little effect on
decreasing the sludge blanket and increasing the RAS concentration.
The P addition appeared to have a more significant effect in improving
these parameters in this plant. The P addition to the K-C unit did not
cause a significant improvement as in the K-V unit. The slight
increase in the RAS concentration and small drop in the sludge blanket
level at the end of July were apparently due to the RAS chlorination.
In conclusion, the operation of the K units during July indicated that
RAS chlorination is not effective in controlling non-filamentous bulking
problems.
Special Laboratory Studies
Special studies conducted on the four plants during May and June, in
addition to the normal laboratory routine, were as follows:
1. Oxygen uptake
2. Oxygen transfer
205
-------
3. Sludge production
4. Air flotation of waste activated sludge
5. Gravity thickening of waste activated sludge, and WAS plus
primary clarifier sludge
6. Specific filtration resistance of WAS plus primary clarifier
sludge
7. Anaerobic sludge digestion
8. Return of waste activated sludge to the pilot clarifier
9. BTU value of sludges
10. Chlorine demand of final effluents
Items 8, 9 and 10 are discussed in the Sections entitled Primary
Clarification, BTU Value of Sludges, and Chlorine Demand of Final
Effluents, respectively.
The laboratory data for items 1 through 6 are presented in Table 32;
comments on these tests are as follows:
Oxygen Uptake
The oxygen uptake studies were conducted on composite samples of
aeration tank mixed liquor and return activated sludge, and on primary
effluent which had previously been transferred to a laboratory reactor.
The effective detention time in the reaeration zone was selected to be
the same as the total detention time in the contact zone for oxygen
uptake study purposes. (The contents of reaeration zone undergo the
same time of aeration as the contents of the contact zone to remove a
given unit of BOD.)
The two values shown for the oxygen uptake rates are (1) the initial rate
at the beginning of the test and (2) the final rate at the conclusion of the
test. The two values shown for the BOD concentration measured during
the oxygen uptake studies are (1) the initial theoretical calculated value
for the composite sample, and (2) the final measured BOD in the reactor
at the conclusion of the test.
Oxygen Transfer
The oxygen transfer studies were conducted utilizing grab samples from
206
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SPECIAL LABORATORY STUDIES - PHASE III
02 UPTAKE
REAERATION ZONE
Effective D. T. , hr.
MLVSS, mg/1
Uptake Rate, mg/l/hr.
CONTACT ZONE
Total D.T. , hr.
MLVSS, mg/1
Uptake Rate, mg/l/hr.
BOD cone. , mg/1
Lbs. D£ Required
Lb. BOD Removed
O2 TRANSFER
REAERATION ZONE
Alpha (d.)
Beta (0)
CONTACT ZONE
Alpha W
Beta (fi)
SOLIDS PRODUCTION
H
g. Lbs TSS Produced
5" Lb BOD Removed
Contact Stabilization-Variable
5/7 5/22 6/4
2.31 2.58 2.41
8634 9908 7750
165;75 88;55 71;47
2.31 2.58 2.41
4174 4110 3996
528;100 288;52 192;53
332;38 424;20 338;26
2. 51 0. 82 1. 18
5/13 5/23 6/10
.57;. 80 1.15-,. 66 1.40;. 61
.90;. 85 .93;. 93 90;. 87
.70;. 85 .73;. 81 1.05:1.20
.80;. 93 .96;. 98 .80;. 95
5/5-12 5/19-26 6/4-11
0. 68 0. 46 0. 69
Contact Stabilization- Control
5/8 5/21 5/29 6/5
3.16 3.27 3.18 3.51
10128 9652 10828 8310
204;58 81;52 180;74 68;52
3.16 3.27 3.18 3.51
4056 1656 5010 3862
402;50 96;30 330;58 165;36
322;15 437;102 419:41 363;51
2.02 0.84 1.81 1.14
5/13 5/23 6/10
.81;. 88 .83;1.25 -95;1. 52
.83;. 84 .90;. 89 . 97;. 92
. 80;. 93 . 72;. 92 . 56;. 81
.73;. 94 .93;. 93 1.13;. 85
5/5-12 5/19-26 6/4-11
0. 50 0. 52 0. 68
Kraus -Variable
5/9 5/19 6/6
2.43 2.59 2.85
12750 10388 11452
258;109 213;89 309:101
2.43 2.59 2.85
4870 3974 3954
396;62 312;42 330;47
357;25 460;55 356;27
1.70 1.11 1. 52
5/13 5/23 6/10
.68;. 74 .61;. 78 . 60;. 70
.75;. 78 .78;. 84 . 59;. 81
.73;. 83 .87;!. 05 .79;. 76
.81;. 91 .91;. 94 .74;. 88
5/5-12 5/19-26 6/4-11
1.21 0.89 1.46
Kraus -Control
5/12 5/20 6/9
4.20 4.65 5.36
8084 12222 7864
96;66 120;75 171;72
4.20 4.65 5.36
4436 4606 2596
111;43 264;36 78;47
403;51 353;17 548;62
1 . 47 1.70 1.30
5/13 5/23 6/10
. 86;. 60 . 58;. 66 . 80. 59
. 83;. 82 .82;. 92 .82;. 83
. 82;. 81 . 86;1. 12 . 55;. 88
.64;. 88 .97;. 98 .83;. 90
5/5-12 5/19-26 6/4/11
1. 13 0. 80 1. 20
-------
SPECIAL LABORATORY STUDIES - PHASE III
AIR FLOTATION
WAS concentration, mg/1
(Duplicate Test)
Final Concentration, mg/1
(Duplicate Test)
Rate of Ascent, ft/min
(Duplicate Teet)
Pressurized Flow Volume:
Sample Volume
(Duplicate Test)
GRAVITY THICKENING
Sample Composition
Volume Ratio-WAS:PC
Initial Cone. , mg/1
Final Cone., mg/1
Length of Test, min.
Supernatant Analyses:
BOD, mg/1
TSS, mg/1
SFR (BUCHNER FUNNEL)
_
£< Sample Composition
tV
£ Volume Ratio-WAS:PC
*t) Total Solids Cone., mg/1
£, SFR x 10 secz/gram
o
5/1-15
10656
10656
28957
30636
0.578
0.475
3.00:1
1.90:1
5/14
A*
9682
23052
165
5/14
B
3:1
30260
274
Contact Stabilization-Variable
5/16-31
11652
11652
26702
23304
0.688
0.332
2.65:1
1.78:1
5/26
A
7992
28543
120
5/26
B
3:1
32750
104
6/1-15
8420
8420
25458
23913
0.504
0.415
2.89:1
1.77:1
6/11 6/3 6/6
ABB
8:1 14.7:1
12b32 10168 17652
29144 21406 43054
180 180 180
132 290 90
124 232 128
5/1-15
9392
9392
17151 :
23276
0.554
0.332
3.76:1
2.56:1
5/14
A
11236
23655
150
5/14
B
3:1
31000
345
Contact
5/16-31
11620
11620
25661
21949
0.806
0.368
2.81:1
1.94:1
5/26
A
11960
23223
120
5/26
B
3:1
31380
115
Stabilization- Cont r ol
6/1-15
10448
10448
28595
26866
0.451
0.320
2.88:1
1.81:1
6/11 6/13 6/10
ABB
8:1 13:1
8712 17856 14736
26806 35012 35086
180 180 240
68 154 109
72 236 100E
5/1-15
10972
20573
0.285
2.33:1
5/14
A -
14684
25761
150
5/14
B
3:1
32330
334
Kraus-Va
5/16-31
13824
13824
21799
18816
0.205
0.257
4.00:1
3.12:1
5126
A
16260
25015
140
5/26
B
3:1
31740
278
riable
6/1-15
15020
15020
15020
13232
0.214
0.148
6.65:1
4.46:1
6/6 6/12
A B
10.6:1
21020 19224
29194 40050
360 240
160 160
124 216
Kraus-Control
5/1-15 S/16-31
11548 15740
11548 15740
23524 24215
20665 22298
0.261 0.318
0.186 0.435
2.65:1 4.00:1
1.94:1 2.96:1
5/15 6/9
A A
7.8:1
14964 16108
30230 33076
225 240
110
124
5/14 5/26
B B
3:1 3:1
32670 38270
216 579
6/1-15
14904
14904
21425
24592
0.491
0.448
7.70:1
5.06:1
6/13
B
17000
38636
240
227
224
* A = WAS; B = WAS + PC
-------
the particular cells in the pilot plant units. The two values shown for
Alpha and Beta are the values for the first cell and the last cell
respectively of the reaeration zone or the contact zone.
Sludge Production
The procedure for calculating the sludge production is described in
Appendix B. The only difference is the time period used for the
calculation.
The solids production calculations for the Kraus units include the total
suspended solids contributed by the digester supernatant but do not
include the BOD associated with the digester supernatant.
Air Flotation
The air flotation studies on WAS utilized the samples as obtained; they
were not diluted with final effluent as were the samples studied during
Phase II. No chemicals were added during the air flotation studies.
Gravity Thickening
The tests were conducted on two sets of samples:
a. Grab samples of waste activated sludge.
b. Grab samples of waste activated sludge plus grab samples of
primary clarifier sludge mixed together in the volumetric
ratios shown in the Table.
The laboratory procedure used for these studies is presented in Appendix B,
Specific Filtration Resistance
Individual samples of WAS and primary clarifier sludge were prethickened
and combined as follows:
a. Grab samples of primary clarifier sludge thickened in a 1-liter
cylinder, without stirring, for 30 minutes.
210
-------
b. Grab samples of WAS thickened in 1-liter cylinder, with
stirring, for 3 hours.
c. The two thickened samples were composited in a volumetric ratio of
one part primary sludge to three parts WAS.
d. If the primary sludge grab sample was at least 3% TSS, it was
not prethickened.
The specific filtration resistance data indicated that none of the raw
sludges analyzed could be filtered economically without sludge conditioning.
Sludge Digestion
Three laboratory digesters were set up as follows:
1. Digester #1 - Received GBMSD primary clarifier sludge.
2. Digester #2 - Received pilot clarifier sludge which contained
WAS from K-C (May 1-June 30; Phase A) or
CS-C (July 1-July 31; Phase B).
3. Digester #3 - Received a composite of pilot plant primary
clarifier sludge and thickened WAS from K-C
unit.
The #3 digester was fed at a ratio of one pound of primary clarifier
sludge VSS to every three pounds of WAS-VSS. The desired loading
rate was 0.1 pound of VSS per cubic foot per day.
Gas production and total and volatile solids added and removed from
each digester was measured daily. pH, alkalinity and volatile acids
were monitored routinely. Cubic feet of gas produced per pound of
volatile solids reduced and the reduction in volatile solids were also
calculated.
The laboratory digester studies showed that the particular combinations
of sludges were readily digestable with good gas production. The
values obtained from Digester #1 (being fed GBMSD primary clarifier
sludge) compared quite well with those values obtained for the full-
scale treatment plant digesters.
Graphs of selected operating parameters for the laboratory digesters
are presented in Figure 40. Photographs of the experimental equipment
are shown in Figure 41.
211
-------
LABORATORY DIGESTER STUDIES, MAY-JULY, 1969
PLOT OF SELECTED PARAMETERS vs. TIME
o
o
o
a
u;
6 200
190
OT I8°
* 170
< ISO
I 140
I '30
_i
o I 20
a:
Z
o
z
o
o
UJ
27
25
23
21
19
17
15
13
II
PHASE PHASE
B
MAY JUNE JULY
PHASE PHASE
B
MAY JUNE JULY
FIGURE 40 PAGE 213
-------
LABORATORY DIGESTER EQUIPMENT
EXTERIOR VIEW OF INCUBATOR.
GAS COLLECTION BOTTLES SHOWN
AT BOTTOM OF PHOTO.
REACTOR CONTENTS BEING MIXED
AFTER FEED HAS BEEN ADDED.
FIGURE 41 PAGE 215
-------
Selection of the Most Promising Process
The laboratory data obtained both from the daily pilot plant operation
and the special studies conducted between May 1 and June 15 were
utilized to develop theoretical full-scale design parameters. (See
Appendix F). These parameters were then utilized to develop pre-
liminary comparative capital and operating cost estimates for full-scale
contact stabilization and Kraus plants. (See Appendix F for the flow,
BOD and TSS quantities, and design scale-up parameters used in the
cost estimates.)
The estimated comparative costs were as follows:
Preliminary Estimates*
Capital Cost Operating Cost
Contact Stabilization $16,262,000 $2,094,000
Kraus $18,409,000 $2,262,000
*(These estimates are based on 1969 dollars and do not include
allowances for administration, engineering, contingencies,
inflation during construction, and some facilities common to
both processes.)
The following factors were also considered in selecting the most optimum
process:
1. Metro and Mill 3 wastes would be combined in an existing
interceptor sewer; the wastes from Mills 1, 2, and 4 would be
conveyed to the treatment plant in a separate sewer. All
wastes would receive primary treatment during average flow;
during peak storm flow conditions the wastes from Mills 1, 2,
and 4 would be pumped directly to secondary treatment.
2. Anaerobic sludge digestion is a potentially troublesome unit
operation.
3. The use of digester supernatant feed for filamentous control was
not entirely successful. Also, a situation of excess phosphorous
feed to the process could occur when attempting to use digester
supernatant for biological control.
4. RAS chlorination was successful in controlling the filamentous
216
-------
microorganisms in both flow schematics. Since receiving RAS
chlorination, the CS unit was the more stable of the two processes
5. The K unit had a lower sludge production rate than the CS unit.
6. The CS unit has a simpler flow schematic and thus would be
easier to control.
7. The CS process had superior BOD and TSS removal efficiencies
during Phase III.
8. The preliminary cost estimate was based upon CS and K plant
designs which would provide equivalent treatment.
9. The CS process had the lower estimated capital and operating
costs .
Based upon the preceding information, the contact stabilization process
was selected for the proposed full-scale treatment plant.
217
-------
PILOT PLANT RESEARCH - PHASE IV
On July 18, the two Kraus units were converted to contact stabilization
flow schematics. All four pilot plants then had the same flow schematic.
The plants were assigned the following identification symbols:
New Designation Previous Designation
Plant A Contact Stabilization-Variable
Plant B Contact Stabilization-Control
Plant C Kraus-Variable
Plant D Kraus-Control
The major objectives of Phase IV were to obtain refined design
parameters pertaining to:
1. Oxygen transfer and utilization
2. Sludge production
3. Methods of primary clarifier and waste activated sludge
conditioning and disposal.
In addition, the following operating situations were studied:
1. Elimination of Mill 3 waste from pilot plant influent.
2. Increased hydraulic loadings to approximate storm flow
conditions.
3. Bypassing of Mill 1, 2 and 4 wastes around primary clarification
directly to the secondary system.
The four plants were utilized as follows to accomplish these objectives:
Plant A
Between September 1 and October 19, the pilot clarifier was
connected directly to Plant A. Plant A was then operated such that
Metro sewage only was receiving primary treatment and Mill 1, 2
and 4 wastes were added to the pilot clarifier effluent.
The high-flow studies began October 3 by increasing the Metro
sewage flow. Between October 7 and October 19, tap water was
added to the Metro sewage to reduce the BOD to approximately
100 mg/1, simulating a storm flow condition. (Refer to the
section entitled "Primary Clarification" for pilot clarifier flow
schematics and operating data.) The pilot clarifier was taken out
of service on October 20. Between October 20 and December 15,
219
-------
Plant A then received the full complement of Mill and Metro feed
and was used for miscellaneous studies.
Plant B
This plant was operated as a reserve unit to provide additional WAS
for the solids handling studies. Some miscellaneous studies were
also conducted on this plant.
Plants C and D
These two plants were operated to provide WAS for the solids
handling studies. The oxygen uptake and transfer studies, and
sludge production studies were also conducted on these plants.
The pilot plant flow schematics used during Phase IV are illustrated in
Figures 42 to 43. The plants were operated according to the theoretical
values shown in the following summary.
THEORETICAL PILOT PLANT OPERATION - PHASE IV
September 1 - December 15, 1969
Q Forward, 1/d 4310
MLTSS, mg/1 4070
MLVSS, mg/1 3500
RAS-TSS, mg/1 10000
RAS-VSS, mg/1 8600
R/Q 0.69
Dt - Contact, hrs. (R + Q) 2.3
Dt - Reaeration, hrs. (R) 2.8
RAS Chlorination, mg/1 10
Final Clarifier
Dt(Q)hrs. 3.2
Overflow Rate, gpd/sf 360
Solids Loading,
Ibs/sf/day 20.8
220
-------
PILOT CLARIFIER EFFLUENT a MILLS 1,2 a 4 FEED
On SECTION IN TEXT
PILOT PLANT OPERATION 8/11/69- 9/11/69
LE6END
—C>- PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPING
<^> POSITIVE DISPLACEMENT PUMP
^ CELL FILLED WITH TAP WATER, (DEAD CELL)
N— NUTRfENT FEED SYSTEM
C CHLORINE FEED SYSTEM
REDUCED PROCESS VOLJME
REDUCED PROCESS VOLUME
PILOT PLANT FLOW SCHEMATICS
DONOHUC ft ASSOCIATES,INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
SCALE '/„• • I'-O'
-------
PILOT CLAHIFIER EFFLUENT 6 MILLS 1.2 a 4 FEED
REFER TO PRIMARY CLARIFICATION SECTION IN TEXT
MILL EFFLUENTS
FROM
TANK TRAILER
LEGEND
—£>— PROPORTIONAL SAMPLER UNIT
RETURN ACTIVATED SLUDGE PIPING
WASTE ACTIVATED SLUDGE PIPIN6
<^> POSITIVE DISPLACEMENT PUMP
El CELL FILLED WITH TAP WATER; (DEAD CELL)
N NUTRIENT FEED SYSTEM
C CHLORINE FEED SYSTEM
PILOT PLANT OPERATION 9 / 12/69 - I2/15/69
9/12 C,D CHANGED NITROGEN a PHOSPHORUS FEED POINT
PILOT PLANT FLOW SCHEMATICS
DONOHUE 8 ASSOCIATES, INC. CONSULTING ENGINEERS
SHEBOYGAN, WISCONSIN
SCALE '/|6" • I'-O"
PROJECT 12130 EDX
-------
Due to the elimination of Mill 3 wastes, the Metro and Mill 1, 2 and 4
flows to Plant A were increased proportionately to provide the same
flow quantity as that received by Plants B, C, and D. Between
October 3 and 19, (the storm flow studies) the above summary did not
apply to Plant A.
Plant B MLVSS was initially set at 4000 mg/1, but was reduced to 3500
mg/1, September 15.
Not shown are the F/M values and BOD:N:P ratios. The F/M value for
Plant A was 0.35 and for Plants B, C and D was 0.37. This difference
was due to the elimination of Mill 3 feed from Plant A between
September 1 and October 19. After that time Plant A also had a
theoretical F/M value of 0.37.
The theoretical BOD:N:P ratios were varied during Phase IV as follows:
Date Plant A Plant B Plant C Plant D
9/1* 100:2.5:0.5 100:5.0:0.5 100:5.0:0.5 100:5.0:0.5
9/H 100:5.0:1.0 100:5.0:1.0
10/21 100:5.0:0.5
11/24 100:5.0:0.5
12/9 100:5.0:1.0 100:5.0:1.0 100:5.0:1.0
*No nitrogen or phosphorus addition was required for Plant A
between 9/1 and 10/19 due to elimination of Mill 3 feed. Nitrogen
was added to B, C and D and phosphorus was added to C and D.
Both nutrients were added to all plants beginning 10/22.
Elimination of Mill 3 Wastes from Feed to Plant A
The elimination of Mill 3 wastes from Plant A and the diverting of Mills
1, 2 and 4 around primary clarification directly to secondary treatment
was studied both at average flow (September 1 - October 2) and storm
flow (October 3-19) conditions.
The average operating data for September 1-30 are shown in Table 33.
Between September 11 and September 15, high BOD and TSS occurred
in the effluents of Plants A, C and D, but not in Plant B. This period
224
-------
AVERAGE PILOT PLANT OPERATING DATA
September, 1969
Plant A Plant B Plant C Plant D
MLVSS, mg/1
F/M Ratio, BOD/VSS
Aeration Tank Influent
NH3 as N, mg/1
Ortho phosphate as P, mg/1
BOD:N, 100:
BOD:P, 100:
R/Q
BOD, mg/1
Unfiltered PE
Unfiltered FE
Filtered FE
% BOD Removal
Unfiltered FE
Filtered FE
TSS in PE, mg/1
TSS in FE, mg/1
% TSS Removal
pH of FE
Settled Sludge Vol. ml
SVI
RAS-VSS, mg/1
Waste VSS, kg/day
3370
.29
22.5
4.7
6.2
1.3
0.29
369
62
29
83.2
90.6
138
64
53.6
7.6
587
153
11793
0.6
3647
.33
23.7
3.2
5.8
0.8
0.44
401
35
16
91.3
95.5
126
31
75.4
7.7
426
101
10079
0.2
3583
.31
23.7
4.7
5.8
1.2
0.39
401
46
23
88.5
93.5
126
58
54.0
7.7
789
192
11309
0.6
3355
.36
23.7
4.7
5.8
1.2
0.48
401
70
31
82.5
91.2
126
87
31.0
7.7
593
160
9110
0.2
Table 33 Page 225
-------
of poor operation in these three plants was apparently due to insufficient
dissolved oxygen in the mixed liquor. During this time Plant B was
being operated at a DO of 5 to 6 mg/1 whereas the desired DO values in
the other three plants were 0. 5 to 1 mg/1 (September l-12)andl-2 mg/1
(September 12-19). However, the actual DO values during this period
are subject to question due to possible errors in the procedure for DO
mea sur ement.
The final effluent BOD and TSS values for Plant A during the days in
question were as follows:
DATE
9/11/69
9/12/69
9/13/69
9/14/69
9/15/69
FE-TSS. mg/1
104
114
86
74
72
FE-BQD,
147
225
150
134
86
mg/1
If these values are omitted, then the monthly averages for FE-TSS and
unfiltered FE-BOD are 59 mg/1 and 45 mg/1, respectively (57.2 and
87. 8% removals, respectively).
Another parameter of concern when eliminating Mill 3 wastes from
Plant A feed was the pH of the combined feed to the aeration tank. The
average pH data for various plant streams for September and October,
1969 were as follows:
Period
1969
9/1-9/30
10/1-10/19
10/20-10/31
Plant
A
B.C.D
A
B
C
D
A
B
C
D
pH Values
Clarifier
Influent^)
7.6
6.8
7.1
6.9
ii
"
6.8
ii
Clarifier
Effluent(a)
7.6
6.8
7.3
6.9
"
"
6.8
ii
Secondary
' Influent (b)
7.0
6.9
Final
Effluent
7.6
7.7
7.5
7.9
7.7
7.8
7.7
7.8
11
II
II
II
II
11
(a) Pilot clarifier data -Plant A and primary clarifier data - Plants B, C,
D, 9/1-10/19; primary clarifier data - all plants, 10/20-10/31.
(b) Combination of pilot clarifier effluent plus Mills 1, 2 and 4.
226
-------
Based on these pH data, there were no apparent pH related problems
in the plant operation.
When taking into consideration the minor upset in mid-September, the
conclusion was reached that neither the absence of Mill 3 wastes nor
the bypassing of Mills 1, 2 and 4 around primary clarification impaired
the efficiency of the secondary treatment process.
Storm Flow Studies
The storm flow studies on Plant A were started Octobers by increasing
the Metro sewage flow. Between October 7 and October 19 tap water
was added to the Metro sewage to reduce the BOD to approximately 100
mg/1. The full compliment of tap water was reached October 8 and the
study was continued through October 19. (See the report section entitled
"Primary Clarification" for details on pilot clarifier operation.)
The storm flow data for Plant A are presented in two sections, October
1-19 and October 20-31, in Table 34. During the high flow operation
the pilot plant was not upset, although there was a decrease in overall
plant performance with regard to TSS and BOD removals. This poor
performance is attributed to the inability of the final clarifier to
maintain good suspended solids removals under the high flow conditions.
Note that according to the SVI data, the settling characteristics of the
biological floe did not change significantly. Also the filtered final
effluent BOD's (listed below) did not indicate any significant reduction
in biological treatment efficiency due to the high hydraulic loadings.
Plant A Filtered Final Effluent BOD
10/1 19 mg/1
10/8 16 mg/1
10/16 14 mg/1
10/23 17 mg/1
10/30 23 mg/1
Special Laboratory Studies
Special studies conducted on Plants C and D during Phase IV, in
addition to the normal laboratory routine, were as follows:
1. Oxygen uptake
2. Oxygen transfer
3. Sludge production
227
-------
PLANT A OPERATING DATA
Item
Forward Flow
MLVSS, mg/1
F/M (BOD/VSS)
SVI
Final Clarifier
Df., hrs.
Solids loading,
Ibs/sqft/day
Overflow rate,
gpd/sf
PETSS, mg/1
FETSS, mg/1
% Removal
PE BOD, mg/1
FE BOD, mg/1
% Removal
October -1-19
172% of Average
Range - 101% - 278%
Min. Avg. Max.
2784 3588 4500
0.17 0.37 0.55
56 69 83
1.2 1.9 3.2
15 27 42
366 624 1009
50 124 372
19 70 138
44%
150 312 476
34 64 143
80%
October 20-31
Average
Min . Avg . Max .
2900 3780 4472
0.23 0.29 0.34
47 57 64
2.5 3.1 3.9
14 18 23
296 377 460
76 136 180
20 43 62
68%
358 441 530
30 46 72
90%
Table 34 Page 229
-------
The data obtained during the special studies are presented in Table 35.
With the exception that the oxygen uptake studies were conducted on
grab samples from the particular aeration section being studied, the
procedures utilized and the data presented are the same as described
in the special studies section of Phase III.
Final effluent chlorination was also studied and is discussed in the
report section entitled, "Final Effluent Chlorination."
Summary of Pilot Plant Operation During Phase IV
The results of the special studies on Plant A were as follows:
1. The elimination of Mill 3 effluent from the composite feed to
the plant and the bypassing of Mills 1, 2 and 4 around primary
clarification did not adversely affect the performance of the
plant,
2. Operating the unit at a hydraulic flow averaging 172% of the
normal daily flow for 2 1/2 weeks did not adversely affect the
biological treatment efficiency of the plant. However, it did
cause poorer TSS removals in the final clarifier which resulted
in decreased TSS and BOD removal efficiencies across the
secondary unit.
Plants C and D were operated under constant conditions to produce
waste sludges for the solids handling studies and to permit some
additional special studies. Average operating data for Plant C and D
between August 1 and December 15, 1969 are illustrated in Figure 44.
These plants achieved overall removals of 91% and 78%, respectively,
for BOD and TSS. A higher degree of TSS removal would be expected
for a large-scale treatment plant due to increased final clarifier
efficiency.
The relationship between RAS chlorination and filament concentration
for the four units is illustrated in Figure 45. (See Phase I for nomen-
clature on Figure 45.) The average, maximum and minimum
laboratory data for each month during Phase IV are presented in
Appendix D.
230
-------
SPECIAL LABORATORY STUDIES - PHASE IV
O2 UPTAKE
REAERATION ZONE
Effective D. T. , hr.
MLVSS, mg/1
Uptake Rate, mg/l/hr.
CONTACT ZONE
Total D. T. , hr.
MLVSS, mg/1
Uptake Rate, mg/l/hr.
BOD cone. , mg/1
Lbs. O2 Required
Lb. BOD Removed
02 TRANSFER
REAERATION ZONE
Alpha «)
Beta (I)
CONTACT ZONE
Alpha (oC)
Beta (3)
SOLIDS PRODUCTION
g. Lbs. TSS Produced
£• Lb. BOD Removed
w
PLANT C
9/8/69 9/23
2.56 2.84
8840 10792
59; 48 108; 96
2.56 2.84
4736 3230
78; 36 73; 36
340; 29 209; 23
.70 2.02
9/8/69
. 32; . 53
.91; .92
.68; . 56
.96; 1.03
9/1-15 9/15-30
0.64 0.42
10/8-9 10/22
3.44 2.72
10588 12416
81; 80 84; 81
3.44 2.72
4012 4220
74; 42 90; 44
56; 25 246; 9
1.45 .94
10/8-9 10/22
. 62; .77 . 57; .86
.77; .74 .87; .83
.80; . 89 .69; .77
.87; . 95 .90; .91
9/30-10/15 10/15-11/15
0.53 0.70
11/19
4.88
11748
93; 84
4.88
3096
72; 42
319; 22
1.59
11/19
.94;. 95
.85; .86
.86; 1. 19
.72; .90
11/5-12/1 12/1-15
0.63 0.78
PLANT D
9/8
2.40
8924
60; 48
2.40
3368
75; 39
102; 42
.70
9/8
. 49; . 89
.96; .92
.67; .64
.95; 1.00
9/1-15 9/15-30
0.32 0.43
10/8-9 10/22 11/19
3.32 2.92 4.80
9236 11660 11592
72; 57 77; 71 75; 72
3.32 2.92 4.80
3708 3604 3544
72; 39 114; 36 83; 36
51; 14 116; 21 46; 18
1.23 .95 1.34
10/8-9 10/22 11/19
.96; .80 . 64; .63 .92; . 64
.81; .84 .86; .90 .80; .85
. 67; .68 .49; .85 .81; 1. 01
.84; .92 .95; .99 .76; .87
9/30-10/15 10/15-11/5 11/5-12/1 12/1-15
0. 50 0. 51 0. 55 0. 57
-------
PLANT C
TSS---
VSS---
153 (32%)
123 (31%)
PE--
PEF-
100:4. 2:0. 4
100:5.7:0. 9
PLANT D
C
3)
m
T)
J>
O
m
ro
OJ
cu
PRIMARY CLARIFIER
TSS«- 12885
VSS--- 1109Z
0t 5.3 hrs (R)
TSS---4268
VSS--- 3696 (87%)
F/M-- 0. 30
Dt 2. 9 hrs (R+Q)
SVI
161
Dt---3. 8 hrs (Q)
16. 9# TSS /ft2 /day
O. R.-320 gpd/ft2
T /
t
TSS--- 52 (77%)
VSS ---42
BOD-- 44 (91%)
pH 7.7
Color- 223 (9%)
TSS--224 me/1
VSS--179 mg/1
BOD -47 8 mg/1
pH --6.8
Dt
O.R
= 2.9 hrs
= 430 gpd
ft2
BOD-- 450 (6%)
COD-- 985
TC--- 486
Color- 244 units
«--/
TSS--- 13903
VSS--- 12008 (87%)
R/Q---.37
TSS--- 11834
VSS--- 10042
Dt 5. 0 hrs (R)
TSS---4166
VSS--- 3606 (87%)
F/M-- 0.31
Dt 2.8 hrs (R+Q)
SVI
122
Dt ---3.8 hr (Q)
16. 7#TSS/ft2/day
O. R. -320 gpd/ft2
i l
i
t
lOS 4y (/H"/o)
VSS---41
BOD-- 42 (91%) "
pH 7.7
Color- 219 (10%)
REAERATION
TSS--- 12400
VSS--- 10692 (87%)
R/Q-- 0. 39
CONTACT
FINAL CLARIFIER
AVERAGE PILOT PLANT OPERATION - AUGUST 1, 1969 TO DECEMBER 15, 1969
-------
PILOT PLANT OPERATION - PHASE IV - 8/1 /69 TO 12/15/69
n
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-------
COST ESTIMATES FOR JOINT TREATMENT
AND SEPARATE TREATMENT FACILITIES
The pilot plants were operated through December 15, 1969. The lab-
oratory information obtained on the pilot plant operation and special
studies between July 17 and December 15, with the exception of the
solids-handling unit process data, was utilized for development of full-
scale design parameters. A summary of the more important design
parameters is presented in Table 36. (See Appendix F for a complete
summary of the theoretical design parameters. Note that the BOD and
TSS loads to the secondary unit do not include any allowance for return
sidestreams from the solids handling unit processes.)
These revised parameters were then utilized for preparation of cost
estimates for a full-scale contact stabilization plant. Information
relative to the solids-handling unit process studies was sent to each
manufacturer who then submitted flow schematics, operating parameters,
and cost estimates. Since the solids handling unit process schematic was
not finalized at that time, an averaged cost, based upon seven possible
flow schematics developed from the individual cost and performance
estimates presented by the participating manufacturers, was used in the
final cost estimate. (See Appendix F for the flow, BOD and TSS
quantities, and design scale-up factors used in the cost estimates.)
These capital and operating cost estimates were utilized by Black &
Veatch Consulting Engineers to prepare a cost distribution report for
the GBMSD. ("' The main parameters utilized'to develop the cost
distribution were:
Average Flow Rate, MGD
Peak Flow Rate, MGD
BOD, Tons/Day
TSS, Tons/Day
The cost distributions for the joint treatment concept for each Mill and
GBMSD were developed from the Black & Veatch report, (see Table 37).
The costs for the separate treatment concept for GBMSD were also
developed from this report. The remaining values shown in the Table
were either obtained from the Mills or estimated by the project staff.
Note that under capital investment co.sts listed in Table 37 is included
an allowance for operating contingency reserve and normal annual
capital improvements. To maintain a utility in a sound financial
position,it is necessary to provide a contingency reserve to insure that
237
-------
FULL-SCALE DESIGN PARAMETERS
FOR
CONTACT STABILIZATION TREATMENT PLANT
Primary Clarification (Metro Only)
Average Flow 30.0 MGD
Peak Flow 120.0 MGD
Detention Time 2.7 Hours
BOD Removal 33.0 %
TSS Removal 60.0 %
Primary Sludge 60.300GPD; 5. 5% TSS, 83 . 7 % Volatile
Secondary Treatment
Average Forward Flow (Q) 53.9 MGD
Peak Forward Flow (Q) 94.0 MGD
BOD (470 mg/1) 106.1 Tons/Day
TSS (110 mg/1) 25.3 Tons/Day
Mixed Liquor VSS (86% Volatile) 3500 mg/1
Lbs. BOD Applied/lb. MLVSS Under Aeration 0.3
Detention Time
Reaeration (R) 4.1 Hours
Contact (R + Q) 2.9 Hours
R/Q 0.7
Lbs. O2 Required/lb. BOD Removed @ 26 . 6° C-- 1.6
Waste Activated Sludge
Lbs. TSS Produced/lb. BOD Removed 0.65
Volume - 1.6 MGD
TSS Concentration 1.0 %
final Clarification
Solids Loading, lb. TSS/ft2/day--- 23
Overall Efficiency
BOD Removal Exceed 90%
TSS Removal Exceed 90%
Table 36 Page 239
-------
a>
DISTRIBUTION OF CAPITAL AND OPERATING COSTS
Mill 1 Mill 2 Mill 3 Mill 4 GBMSD Total
Average Flow, MOD
Peak Flow, MGD
BOD, Tons/Day
TSS, Tons/Day
5.
6.
30.
5.
0
3
0
0
5.
6.
15.
2.
0
3
0
0
13.
16.
33.
6.
25
5
2
6
0.6
0.7
7.0
2.5
30.
120.
29.
23.
0
0
5
0
53.
143.
114.
39.
85
8
7
1
Joint Treatment Concept
Estimated Share of Capital
Cost (a) $5,501,000 $2,995,000 $7,034,000 $1,328,000 $14,269,000 $31,127,000
Estimated Share of Operation
and Maintenance Costs (b) $ 643,000 $ 373,000 $ 887,000 $ 147,000 $ 1,037,000 $ 3,087,000
Capital Investment Costs (e) $ 658, OOP $ 356, OOP $ 838,000 $ 158,000 $ 1, 695, OOP $ 3,705, OOP
Estimated Total Annual Costs $1,301, OOP $ 729, OOP $1, 725, OOP $ 305, OOP $ 2,732.000 $ 6, 792, OOP
Separate Treatment Concept
Estimated Capital Costs (a) (c) $8,500,000 $6,0-00,000 $3,000,000 $1,600,000 $18,696,000 $37,796,000
Estimated Operation and
Maintenance Costs (b) (d) $1,112,000 $ 645,000 $1,005,000 $ 391,000 $ 1,343,000 $4,496,000
Capital Investment Costs (d)fe) $1, Oil, OOP $ 714, POO $ 357,000 $ 190,000 $ 2, 224, OOP $ 4,496,000
.
Estimated Total Annual Costs $2,123,PPP $1,359, PPP $1, 362, PPO $ 581,000 $ 3, 567, OOP $ 8, 992, OOP
^
a. Estimated total capital costs (including allowance for administration, engineering, contingencies and inflation
P during construction) at completion of construction -- 9/30/72
n> b. Estimated operating and maintenance costs for fiscal year ending 3/31/75
£J c. Mill 1 estimate made by project staff, Mills 2, 3 and 4 estimates obtained from respective mills
'- d. Mills 1-4 estimates made by Project Staff
e. Includes contingency reserve, normal capital improvements, and debt service retirement (20 yrs. -7%)
-------
funds will be available to meet fluctuations in operating costs . The
allocation for normal annual capital improvements would be utilized for
improvements and additions to the system above the normal maintenance
items.
Based upon this final cost estimate, the joint treatment venture would
require an estimated capital expenditure of $31, 127, 000, $3, 087, 000 in
annual operating costs and $6, 792, 000 in total annual costs. If each of
the participants were to construct their own facilities, the estimated
capital costs would be $37, 796, 000, annual operating costs would be
$4, 496, 000, and total annual costs would be $8, 992, 000. Therefore,
the joint venture would result in an accrued savings of approximately
$6,669,000 in capital costs, $791,000 in annual operating costs, and
$2, 200, 000 in total annual costs.
The percentage distribution of the estimated construction costs is
shown in Table 38. Note that the aeration equipment and basins, and
solids handling facilities make up an estimated 51% of the total
construction cost.
The Mills evaluated the factors involved in becoming a part of this joint
venture and gave their decision to the GBMSD on July 1, 1970. Mills 1
and 2 will become participants in the joint venture; Mills 3 and 4 elected
to provide their own facilities to treat their wastes.
242
-------
DISTRIBUTION OF ESTIMATED TREATMENT
PLANT CONSTRUCTION COSTS
Item Percent of Total Construction Cost*
Influent Pumping Facilities 10.9
Screening and Grit Removal 3. 0
Primary Clarification (Metro Only) 3.9
Aeration Equipment and Basins 18.9
Return Activated Sludge Facilities 2.1
Final Clarification 9. 1
Chemical Feeding Facilities 3.3
Solids Handling Facilities 32.2
Electrical and Instrumentation 7.4
Sitew ork 7.2
Administration and Control Buildings -2. 0
100.0
* Administration, engineering and contingencies are not included.
Table38 Page 243
-------
SOLIDS HANDLING UNIT PROCESS STUDIES
An extensive solids handling unit process study was conducted between
September and December, 1969- The unit processes studied were:
Centrifugation Low pressure oxidation
Dissolved air flotation Pressure filtration
Gravity thickening Vacuum filtration
Heat treatment
A summary of the unit processes which were analyzed, test equipment
which was used and the manufacturers participating in the studies is
presented in Table 39. The testing schedule which was followed is shown
in Figure 46. The tests related to each unit process being studied were
conducted in accordance with the procedures developed by the respective
manufacturers.
The objectives of this study were as follows:
1. Provide each participating manufacturer with the necessary
laboratory data required to prepare accurate unit process
performance and cost estimates.
Z. Determine the characteristics of sidestreams from the solids
handling unit processes which would be returned to the secondary
treatment system.
3. Evaluate the applicability of each unit process to this particular
combination of waste sludges .
The laboratory analyses conducted on the samples from each unit process
study are summarized in Table 40. (The laboratory data obtained from
these studies are presented in Appendix E. Chemical aids were used in
some of the studies conducted; those unit processes and tests in which
chemicals were used are listed in this Appendix.)
A summary of the minimum and maximum total suspended solids and
BOD values obtained during the unit process studies is presented in
Table 41. It is important to note that these data are for a sludge which
is primarily waste activated in nature. The approximate volume ratio
for the composite sludge samples analyzed was 13 parts of waste activated
sludge to 1 part of primary clarifier sludge. This composition was used
for all tests except the dissolved air flotation tests by Rex Chainbelt,
Inc. and the Eimco Corporation,and the gravity thickening and filter leaf
245
-------
SOLIDS HANDLING PROCESS STUDIES
Unit Process
Centrifugation
Dissolved Air
Flotation
Gravity Thickening
Company
Test Site*
Heat Treatment
Low Pressure
Oxidation
Pressure Filtration
Vacuum Filtration
FEMicroscreening
Sharpies Equipment
Division
Rex Chainbelt, Inc.
The Eimco Corp.
Dorr Oliver, Inc.
The Eimco Corp.
Walker Process
Equipment
BSP Corporation
Dorr Oliver, Inc.
Zimpro, Inc.
Zimpro, Inc.
Salt Lake City,
Utah
Colorado Springs,
Colo.
Stamford, Conn.
Rothschild, Wis.
Rothschild, Wis.
B eloit -Pa s s avant
Corporation
The Eimco Corp.
Walker Process Equip.
Beloit Passavant Corp.
Crane-Glenfield, Inc.
Southwestern Engr. Co.
Equipment Utilized
Sharpies Solid Bowl Unit,
Fletcher Basket Unit
Bench Scale Pressure
Cylinder Unit
Manufacturer's Batch
Equipment (a)
1-liter stirred cylinder
1-liter stirred cylinder
3-1/2" dia. x 12' SWD
cylinder, 7-1/2" dia.
x 14' SWD cylinder,
1-liter cylinder (all
units had stirrers).
Manufacturer's Batch
Equipment (b)
(c)
(d)
(d)
Portable "Bomb" Pressure
Filter Unit
Filter Leaf Apparatus
Filter Leaf Apparatus
Modified Filter Leaf App.
Field Test Kit
18" Production Unit
(a) A 10-gallon sample was analyzed.
(b) A 15-gallon and a 20-gallon sample were analyzed.
(c) A 5-gallon and a 10-liter sample were analyzed.
(d) A total of two 150-gallon samples were analyzed in the two processes,
* All tests conducted at Green Bay except as noted.
Table 39 Page 247
-------
SPECIAL STUDIES SCHEDULE - PHASE Iff - 1969
COMPANY - UNIT PROCESS
SEPTEMBER
OCTOBER
NOVEMBER
DECEMBER
CD
C
33
m
O)
2
CD
m
ro
-&
ID
BELOIT-PASSAVANT CORP. FE MICR OSCREENING
-PRESSURE FILTRATION
BSP CORPORATION PORTEOUS HEAT TREATMENT
-VACUUM FILTRATION
DORR-OLIVER, INC. GRAVITY THICKENING
-FARRAR HEAT TREATMENT
EIMCO CORPORATION AIR FLOTATION
- GRAVITY THICKENING
-VACUUM FILTRATION |
CRANE-GLENFIELD, INC. -FE MICROSCREENING
REX CHAINBELT, INC. AIR FLOTATION
SHARPLES EQUIPMENT DIVISION CENTRIFUGATION
SOUTHWESTERN ENGR. CO.- FE MICROSCREENING
WALKER PROCESS EQUIP.--- GRAVITY THICKENING
- VACUUM FILTRATION
ZIMPRO INC. - HEAT TREATMENT
- LOW PRESSURE OXIDATION
11
PROJECT SPECIAL STUDIES
OXYGEN UPTAKE 8 TRANSFER
CHLORINE DOSAGE vs COLIFORM KILL
SLUDGE PRODUCTION RATES
STORM FLOW AND METRO -I-MILLS 1,2,4
I I
I I
-------
SAMPLE ANALYSES SCHEDULE
Unit Process
Thickening
Conditioning
Dewatering
FE Microscreening
Footnote
a, b, c
c
b
b
b
a
a
d
d
d
a, e, f
a
e, £
a, e, f
Sample Source
Raw Feed Sludge
Supernatant
Pressurized Flow
Combined Flow
Subnatant
Centrate
Cake
Raw Feed Sludge
Decant
Decant Sludge
Feed Sludge
Centrate
Filtrate
Cake
Raw Final Effluent
Filtrate
Solids A
TS
X
X
TVS
X
X
nalvsis
TSS
X
X
X
X
X
X
X
X
X
X
X
X
X
X
VSS
X
X
X
X
X
X
X
X
X
X
X
X
X
X
pH
X
X
X
X
X
X
X
X
X
X
X
X
X
X
BOD
X
X
X
X
X
X
X
X
X
Nutrient Analvsis
NH^
X
X
X
X
X
X
X
X
X
X
X
X
O.P.
X
X
X
X
X
X
X
X
X
X
X
X
T,P,
X
X
X
X
X
X
X
X
X
X
X
X
%
Moist
X
X
a. Centrifugation d. Heat Treatment and Low Pressure Oxidation
b. Dissolved Air Flotation e. Pressure Filtration
c. Gravity Thickening f. Vacuum Filtration
-------
SOLIDS HANDLING UNIT PROCESS STUDIES
Minimum and Maximum Data*
Sample Source
TSS
BOD
(Data is as mg/1 except as indicated)
Gravity Thickening
Feed Sludge
Supernatant
Thickened Sludge
Dissolved Air Flotation
Feed Sludge
Subnatant
Float Concentration
Centrifigation
Solid Bowl
Feed Sludge
Centrate
Cake (TS)
Basket
Feed Sludge
Centrate
Skimmed Cake (TS)
Bowl Cake (TS)
Heat Treatment
Feed Sludge
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake (TS)
Low Pressure Oxidation
Feed Sludge
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake (TS)
Vacuum Filtration
Feed Sludge
Filtrate
Cake (TS)
Pressure Filtration
Raw Feed Sludge
Filtrate
Cake (TS)
Min.
2676
84
3.0%
10044
104
1.7%
29708
330
8.1%
14888
904
6.2%
10.2%
29392
7400
106
4.19%
266
25.0%
29994
10400
200
5.83%
350
31.7%
22280
124
11.4%
28688
7
29.4%
Max.
16864
313
4.2%
12364
320
6.9%
30148
2200
11.0%
17956
2492
9.8%'
13.8%
34416
19920
300
7.75%
1970
38.0%
30588
11400
6.78%
730
33.4%
36680
1240
19.0%
34304
73
51.1%
Min. Max.
60 335
255 589
1170 1875
338 975
7000 8520
4000 13200
4300 7500
5700 6000
5600 5700
870 1575
600 2310
* All values mg/1 except as noted
Table 41 Page 253
-------
tests by Walker Process Equipment. In these latter tests the samples
analyzed were straight WAS.
Summary of the Solids Handling Unit Process Studies
Based upon the data obtained during the solids handling studies on this
particular combination of sludges, the following general conclusions
were made:
1 . Gravity thickening of the composite sludge is not economically
feasible.
2. Thickening of the waste activated sludge by air flotation was
not enhanced by using flotation aids .
3. Large coagulant dosages would be required to utilize centrifuges
for thickening the composite sludge.
4. Conditioning of the composite sludge by chemicals prior to
dewatering is not economically feasible.
5. Conditioning of the sludge by the heat treatment and low pressure
oxidation systems resulted in significant BOD and nutrient
concentrations in the sidestreams from these processes.
6. Conditioning of sludge by use of ash required a higher than
expected ash to solids ratio.
Sidestreams from solids handling unit processes have usually been
ignored in the past when the applicability of a unit process to a particular
solids handling problem was being analyzed. In this study, many tests
were conducted to characterize the individual sidestreams from each
process. It was found that there were considerable variations in the
characteristics of the sidestreams, (BOD, suspended solids, and
nutrient content), which could significantly alter the design of the
secondary system and the unit process under consideration. Since
these sidestreams can be both a benefit (source of nutrients for a
nutrient-deficient waste) and a detriment ( added BOD and TSS load on
treatment units), it is necessary to know the characteristics of the
sidestreams to select the most efficient and economical sludge handling
schematic .
In addition to these studies, thickening of the waste activated sludge by
returning it to the primary clarifier was also investigated. See the
section entitled "Primary Clarification".
254
-------
Estimates of capital costs were obtained from the respective manufacturers
and were utilized in the final cost estimates. Based on the data supplied
a sludge handling capital cost of approximately $10, 000, 000 (including
allowance for administration, engineering, contingencies and inflation
during construction) was utilized. Further analyses of costs for
alternative sludge handling processes is beyond the scope of this report.
A more comprehensive study will be made during final plant design.
255
-------
BTU VALUE OF SLUDGES
Two sets of eleven sludge composite samples were sent to an outside
laboratory for Btu determinations .
The daily grab samples were dried at 105°C and composited with
previously dried samples. Approximately 25 grams of each sample
were sent to the testing laboratory where the Btu analyses were conducted
according to Manual #130, Bomb Calorimetry, published by the Parr
Instrument Company. Volatile solids analyses were conducted on the
second set of samples in the GBMSD laboratory.
The sample compositions were as follows:
Sample Number Composition
1-4 Grab sample of primary clarifier sludge
mixed with a grab sample of WAS in volume
ratio of 1:6 (primary sludge to WAS).
5 Grab sample of pilot clarifier sludge (which
contained WAS).
6 Grab sample of pilot clarifier sludge (which
contained WAS) mixed with digested pilot
clarifier sludge (Digester No. 2) in volume
ratio of 1:3 (pilot clarifier sludge to digested
sludge).
7-10 Grab sample of WAS.
11 Grab sample of primary clarifier sludge.
The results of the tests on samples composited between May 1-15 and
May 16-31, 1969 are shown in Table 42. The Btu value of 9600 Btu per
pound of TVS was assumed for sludge cake going to an incinerator when
developing the final cost estimates. This was based on the average of
9679 Btu/lb of TVS for the two sets of primary clarifier sludge plus WAS
samples .
257
-------
BTU VALUE OF SLUDGES
Table -
•4^.
CM
tl
P
TO
ffl
CM
Ul
vO
Sample
Number
1
2
3
4
5
6
7
8
9
10
11
* Estimates
Sample Description
CS-V Primary Clarifier Sludge plus WAS
CS-C Primary Clarifier Sludge plus WAS
K-V Primary Clarifier Sludge plus WAS
K-C Primary Clarifier Sludge plus WAS
K-C Pilot Clarifier Sludge (including WAS)
K-C Pilot Clarifier Sludge (including WAS)
plus Digested Sludge
CS-V WAS
CS-C WAS
K-V WAS
\
K-C WAS
Primary Clarifier Sludge
May 1-1
BTU/lb TS
7732
7857
7514
7532
8235
7496
7821
7911
7911
7514
7550
5, 1969
BTU/lb TVS*
9487
9664
9323
9769
10807
10678
10053
10368
10261
10237
8977
Mav 16-31,
% Volatile BTU/lb
81.5
81.3
80.6
77. 1
76.2
70.2
77.8
76.3
77. .1
73.4
84.1
7893
7893
7929
7676
7803
7586
7676
7694
8145
7676
7730
1969
TS BTU/lb TVS
9685
9708
9837
9956
10240
10806
9866
10084
10564
10458
9191
based on % Volatile values for samples collected May 16-31.
-------
OXIDATION OF SULFIDES IN
PRIMARY CLARIFIER EFFLUENT
Sulfide Oxidation By Chlorine Addition
Studies on chlorine addition to pilot plant primary effluent (PP-PE) were
made on November 11 and December 19, 1968. The objective was to
determine the quantity of chlorine necessary to reduce the total sulfide
concentration to a negligible amount and thus control the growth of
filamentous sulfur bacteria.
One milliliter of household bleach was diluted to 1000 mis with distilled
water and this solution (A) was added to 100 mis of pilot plant primary
effluent. The equipment used was a Beckman Zeromatic II pH meter,
an Orion Sulfide Electrode Model 94-16, a single junction reference
electrode and a Magnastirrer.
The pH of the sample was measured before the first and after the last
addition of solution A to the sample. The pH of the PP-PE was 6. 55 in
each case; therefore a constant pH was assumed during the test. Since
the testing required approximately one hour, there was the possibility
of sulfide oxidation due to surface aeration of the sample. Therefore,
a control sample was set up and tested; 100 mis of PP-PE was stirred
for one hour at a similar rate as the test sample. There was no
appreciable decrease in sulfide concentration due to the stirring.
Therefore, any change in sulfide concentration in the original sample
was assumed to be due to the addition of chlorine.
A graph of chlorine dosage versus total sulfide concentration is shown
in Figure 47. The graph shows that a dosage of 20-25 mg/1 of chlorine
is required to reduce the sulfide content in the primary clarifier effluent
to an insignificant amount.
Sulfide Oxidation By Preaeration
Tests to determine the effectiveness of preaeration as a method of
reducing the total sulfide concentration were conducted January 17, 1969.
The test conditions were as follows: (Air was used as an oxygen source.)
Sample Volume Time of Aeration pH Dissolved
Liters Hours Oxygen
Initial Final mg/1
A 3 1-1/2 6.70 7.05 4.0+
B 3 2 6.75 7.95 8.0+
261
-------
PRIMARY EFFLUENT TOTAL, SUUFIOE CONTENT
versus
CHLORINE DOSAGE
TO"
c
(D
^
OP
N
0s
U)
1-4
w>
g
.
H
W
H
0
O
W
§
w
E-i
0
H
W
0.
1U
fi
10° -3
lO"1 -
ID'2 -
10-3 .
10-4 -
10-5 .
10-6 _
10-7 .
10'8 -
10-9 -
10-10-
•
* •
A * . /— 11/7/68
A • /
A /
A * X
A ••
12/19/68 — / *•
**A
* A
*
*
*
•
A*
A
*
A •
1 1 1 1 1 1 V 1 1 I 1 I 1 1 1 1 1 1 1
0 2 4 6 8 10 12 13 14 15 16 17 18 19 20 21 22 23 24
CHLORINE DOSAGE, mg/1
-------
The results of this study are presented in Figure 48. Based on these
curves it would require approximately 30-45 minutes to reduce the
total sulfide content to a negligible amount. The higher dissolved
oxygen content did not appear to be beneficial in this test.
In summary, both pre-chlorination and pre-aeration were effective in
reducing the total sulfide content. An economic comparison plus
evaluation of the detriment or benefit of the two methods of sulfide
oxidation would be required to determine the best procedure. However,
in this particular research project it was later determined that RAS-
chlorination was much more effective for controlling the filamentous
sulfur bacteria.
264
-------
TO
C
TJ
f"
TO
(I)
00
6
H
fc
W
O
u
w
9
H
O
H
W
PH
1/17/69
DQ. @
4.0 mg/1
10
PRIMARY EFFLUENT TOTAL SULFIDE CONTENT
versus
TIME OF PREAERATION
1/17/69
DO. @
8.0 mg/1
T
T
1.0
1
1.5 2.0 2.5
TIME OF PREAERATION, Hours
3.0
3.5
—1—
4.0
—1
4.5
-------
FINAL EFFLUENT CHLORINATION
Chlorine dosage versus chlorine residual studies were made on the final
effluents of the four plants during Phase III on June 3 and 13, 1969. The
results of these tests are presented in Tables 43 and 44. The chlorine
dosage ranged between 10 and 17 mg/1 to maintain a 0. 5 mg/1 total
chlorine residual in the effluent after 15 minutes detention time.
During October and November, 1969, arrangements were made with
the City of Green Bay Health Department Laboratory to jointly conduct
coliform count and chlorine residual studies on the pilot plant effluents.
Grab samples of pilot plant final effluents were obtained and split into
two equal portions (A and B ). Aliquot A, analyzed by the Health
Department, was divided into five equal volumes; each volume was
dosed with zero, 5, 10, 15, and 20 mg/1 of chlorine respectively.
After 15 minutes contact time, any remaining chlorine in each of the
samples was inactivated by adding a small amount of a 10% solution of
sodium thiosulfate. Samples from the dosed final effluents were then
properly diluted into sterile, buffered, distilled water blanks. Total
coliform counts were made by the Membrane Filter Technique, using
DIFCO Endo Broth as media. The incubation period was between 18
and 20 hours .
Aliquot B was analyzed for total and volatile suspended solids by the
GBMSD laboratory. It was then divided into five equal volumes; each
volume was dosedwith zero, 5, 10, 15 and 20 mg/1 of chlorine
respectively. After 15 minutes contact time, the total residual
chlorine was measured by the amperometric titration method.
The results of the chlorine - coliform studies are presented in Table 45.
Based upon the studies in June and the studies presented in this Table,
the values of 10 and 15 mg/1 were chosen respectively as the average
and maximum chlorine dosage rates required to maintain the total
coliform count at a value less than 5000 per 100 mis of sample.
267
-------
FINAL EFFLUENT CHLORINATION
Date Plant 24-Hour Chlorine Added Total Chlorine Chlorine Addition
Composite Analyses To Grab Sample Residual After To Maintain
of Final Effluent 15 Minutes 0. 5 mg/1 Residual
mg/1 After 15 Minutes
BOD TSS mg/1 mg/1 mg/1
6/3 CS-Variable 39 52 2.43 0 14
6/3 CS-Control 48 70 12.13 0.5 12
6/3 K-Variable 30 16 12.13 0.3 14
H
&>
cr
i—"
£ 6/3 K-Control 24 26 12.13 0.2 17
(jO
V
p
OQ
fl>
M
CT^
NO
2.43
12.13
14.55
16.98
19.40
24.25
12.13
13.34
14.55
16.98
12. 13
14.55
16.98
19.40
21.83
24.25
12.13
14.55
16.98
19.40
21.83
24.25
0
0.4
0.5
0.7
1.3
1.1
0.5
0.9
1.2
1.8
0.3
0.6
0.9
1.2
1.4
1.7
0.2
0.4
0.4
0.7
0.9
1.6
-------
FINAL, EFFLUENT CHLORINATION
Date Plant 24-Hour Chlorine Added Total Chlorine Chlorine Addition
Composite Analyses To Grab Sample Residual After To Maintain
of Final Effluent 15 Minutes 0. 5 mg /I Residual
1969 mg/1 After 15 Minutes
BOD TSS mg/1 mg/1 mg/1
6/13 CS-Variable 48 20 9.57 0.2 12
11.96 0.4
14.36 0.8
16.75 1.2
6/13 CS-Control 50 54 9.57 0.3 11
11.96 0.8
14.36 1.5
6/13 K-Variable 74 38 9.57 0.4 11
11.96 0.7
14.36 1.1
16.75 1.9
6/13 K-Control 70 32 9.57 0.4 10
11.96 0.9
14.36 1.7
TO
CD
ts)
-si
-------
TOTAL, COLIFORM IN FINAL EFFLUENT
-o
H
S-
r— 1
«
nt
P
10-2
10-9
10-23
11-6
11-13
* Total
TRC -
d
i— <
PH
t>
•i-i
OH
B
C
D
C
D
g
to"
to
H
19
44
36
39
68
Coliform
Total
00
g
to"
g
15
30
--
36
24
per
Residual
rt
.S
Vi ^
*. J2 ?
S u ^
225,000* 190,000*
150,000 7,000
590,000 7,900
1,490,000 1,000
220,000 150,000
100 mis of sample
Chlorine
toO
g
U
S
0
0
1.8
1.8
. 1
00
C g
tiuO
g 0
o g
0
2700* 1.0
5820 3.7
600 5.5
8500 .8
-
bo
g
in
1300*
100
90
1420
SuD
g
U
H
0.6
2.5
9-1
8.8
1.4
^
bo
g
0
500*
100
40
1290
bo
g
O
H
0.9
4. 1
13.8
12.0
2.2
Ul
OP
(B
to
-------
TOTAL CARBON CORRELATIONS
The procedures for BOD, COD, TSS and total carbon (TC) analyses are
presented in the section entitled "Laboratory Staff, Equipment, Procedures
and Data Reduction. " The following information also pertains to the
measurement of total carbon (TC).
1. A 25 microliter, No. 702-N Hamilton syringe was used for the
manual injections.
2. The carbonaceous analyzer was fitted with a manual-injection
glass tee adapter and rubber septum.
3. Standardization Procedure:
A. Each standards injection equaled 19 microliters.
B. 500 ppm total carbon standard equaled the midscale value
of the recorder.
4. Sample temperature: Approximately 68°F.
5. Sample size:
0 - 800 mg/1 TC: 19 microliters
800 - 1800 mg/1 TC: 9.5 microliters
> 1800 mg/1 TC: sample diluted with CO2 - free
water; 19 microliter sample used
6. Between sample injections, the syringe was rinsed in distilled
water several times .
The laboratory technician ran two TC tests on a given sample: if the two
values were within 10 mg/1 of each other, the values were accepted as
reliable; if the values disagreed by more than 10 mg/1, a third test was
run. The third value normally agreed within 10 mg/1 of one of the first
two analyses. These two values were then averaged and the average
value reported on the lab data sheet.
The purpose of the total carbon correlation studies was to determine if
the BOD of a given sample could be accurately predicted with a known
degree of confidence and deviation.
275
-------
The following samples were utilized in the correlation studies:
1. Pilot Plant Primary Influent (BOD, TC, TSS)
2. Pilot Plant Primary Effluent (BOD, COD, TC, TSS)
3. Metro Influent (BOD, TC, TSS)
4. Mills 1, 2, 3, and 4 storage contents (BOD, TC, TSS)
The values in parentheses are those tests used in the correlation
for that particular sample.
The mathematical model used in these correlation studies was as follows:
Y = Bo + B X + e, where
X = dependent variable
BQ. B, = constants
e = estimate of error
With the assistance of Dr. Watts(2°), the laboratory data for BOD, COD,
TC and TSS were utilized in a computer program to develop the following
models:
1. BOD = f(TC) 4. BOD=f(TSS)
2. COD = f(TC) 5. COD = f (TSS)
3. BOD = f (COD) 6. TC =f(TSS)
The average, maximum, minimum and standard deviation values for the
laboratory data utilized in the correlation studies and the BOD/TC ratios
developed from the laboratory data are presented in Table 46. The
average BOD/TC ratio varied from 0.81 ( 1969-Mill 4) to 1.24(1968 -
Mill 3).
A summary of the important terms developed in the statistical correlation
studies is presented in Tables 47 and 48. A definition of the terms in
the Tables is as follows:
BO & Bj Regression coefficients
BQR & BJR- Half-magnitude of the 95% confidence
interval of respective regression
coefficient
Coefficient of Determination - (Multiple correlation coefficient)^
vStandard Error Estimate Estimate of "e" in model
X Average value of independent variable
276
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
BOD AND TOTAL CARBON MODELS
Parameter
Deo. Ind.
H
cr
H- '
(D
is
1?
OQ
ffi
Cs>
-J
PP-PI -
BOD
BOD
TC
PP-PI -
BOD
BOD
TC
PP-PE
BOD
COD
BOD
COD
TC
BOD
PP-PE
BOD
COD
BOD
COD
TC
BOD
METRO
BOD
BOD
TC
METRO
BOD
BOD
TC
68
TC
TSS
TSS
69
TC
TSS
TSS
- 68
TC
TC
TSS
TSS
TSS
COD
- 69
TC
TC
TSS
TSS
TSS
COD
- 68
TC
TSS
TSS
- 69
TC
TSS
TSS
BO
148.2
418.7
473.3
155. 1
401.5
437.6
160.6
391.3
447.8
1258.6
486.1
103.6
57.6
14.5
374.9
815.2
416. 1
247.6
48.0
123.2
167.9
21.0
66.9
130.6
BOR
45.1
49.1
48.6
37.4
19.1
13.4
33.5
83.8
21.6
57.5
19.9
25.2
30. 1
118.7
16.8
58.9
12.5
14.6
35.4
24.0
14.8
15.4
14.5
10.9
Bl
0.77
0.53
0. 16
0.68
0.42
0.28
0.72
1.96
0.58
0.91
0. 14
0.31
0.83
2.28
0. 54
1.99
0.45
0.19
1.41
0.74
0.33
0.96
0.82
0.48
BIR
0.09
0.21
0.21
0.07
0.08
0.06
0.07
0.16
0.16
0.41
0. 14
0.12
0.06
0.24
O.M
0.37
0.08
0.01
0.14
0.09
0.06
0.06
0.06
0.05
Coef.
of
Det.
0.54
0.09
0.01
0.23
0.08
0.07
0.41
0.45
0.08
0.03
0.01
0.63
0.38
0.24
0.08
0.09
0. 10
0.44
0.59
0.46
0.31
0.44
0.37
0.26
Std.
Err.
Est.
71.4
100.1
99.1
83.1
90.5
63.7
66.9
167.2
83.9
222.8
77.3
53.4
66.4
261.7
81.2
285.3
60.5
63.5
52.2
59.6
36.7
63.1
67.3
50.6
X
Average
509
229
229
499
221
221
504
504
133
133
133
1379
484
484
152
152
152
1118
248
243
243
237
219
219
± % t %
Y About Average About Average
540
541
509
494
494
499
525
1379
525
1379
504
526
457
1117
457
1117
484
458
398
302
248
249
247
235
3. 1
4.4
4.7
2.0
2.2
1.4
1.9
1.8
2.5
2.4
4.2
1.5
1.8
2.7
2.0
3.0
1.4
1.5
3.0
4.6
3.6
2.8
5.3
2.6
25.9
36.4
27.9
32.2
35.0
24.4
24.4
23.2
30.7
31.0
29.6
19-4
27.8
44.9
33.9
14. 1
112.6
26.4
25.6
38.4
29.0
48.6
52.2
41.3
-------
BOD AND TOTAL, CARBON MODELS
Parameter
Dep. Ind.
H
£
-------
Y Predicted value of dependent variable
based upon average value of X
GI Half-magnitude of the 95% confidence
interval at the mean for the regression
line
G£ Half-magnitude of the 95% confidence
interval at the mean for a future
predicted value
In evaluating the models, the following information was obtained:
1. The correlation for the model BOD =f(COD) was better than for
the model BOD = f(TC) in the two cases of direct comparison,
PP-PE 68 and PP-PE 69.
2. The correlation of BOD, COD and TC with TSS was poor for all
samples except Metro and Mill 1.
3. The 95% confidence intervals about the mean for the regression
lines vary between t 1. 4% and ± 31. 6%.
4. The 95% confidence intervals about the mean for the future
predicted values vary between t 14.1% and t 105.3%.
5. The Mill samples are much more variable than the Metro
samples or the combination of Metro and Mill samples.
Due to the large amount of data utilized in the studies, a very narrow
95% confidence interval results for the regression lines. However, due
to the high variability of the individual data, wide 95% confidence
intervals resulted for the future predicted values.
In conclusion, these studies showed that using a carbonaceous analyzer to
predict BOD values for these samples would be of questionable value.
However, should the parameter of total carbon replace BOD in the environ-
mental control field at some future date, there would be less variation
in the data from similar research projects. For the studies reported
herein, the ratio of standard deviation to average value for the TC tests
was normally less than for the BOD tests.
(A similar study was conducted by R. B. Schaffer, etal, and is presented
in an article entitled, "Application of a Carbon Analyzer in Waste Treatment'
Journal Water Pollution Control Federation, November, 1965.)
282
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ACKNOWLEDGEMENTS
The project was governed by a Steering Committee composed of the
following members:
Green Bay Metropolitan Sewerage District
Mr. David W. Martin
Pulp and Paper Mills
American Can Company Mr. Bruce B. Robertson
Charmin Paper Products Company Mr. Clyde R. Faulkender
Fort Howard Paper Company Mr. David F. Pagel
Green Bay Packaging Inc. Mr. William R. Nelson
Donohue & Associates, Inc., Engineering Consultants
---Mr. William O. White
University of Wisconsin, Special Consultant
Dr. L. B. Polkowski
Wisconsin Department of Natural Resources
Mr. Carl G. Blabaum
Those persons responsible for the daily administration and operation of
the research project were Mr. Karl G. Voelkel - Research Director,
Mr. Robert W. Deering - Laboratory Director, Mr. Larry R. Wilms -
Project Engineer, Mrs. Betty Liebman - Project Accountant, Mr.
Willard DeBauche, Jr. - Special Studies Technician, Miss Lynda
Bentley - Microbiologist, and Miss Kathleen Nowicki - Secretary. In
addition, Mr. Dean Burns - Laboratory Technician and Mr. James
Zimmer - Microbiologist were associated with the initial development
of the research program. Mr. Voelkel and Mr. Wilms were associated
with Donohue & Associates, Inc. The remaining persons were members
of the GBMSD staff.
The assistance of the staff of the Green Bay Metropolitan Sewerage
District is gratefully acknowledged. Mr. Martin is the Engineer-Manager
in charge of the operations of the GBMSD. Mr. Robert Thompson -
Superintendent, Mr. Welcome Hendrickson - Assistant Superintendent,
and Mr. Roman Vannes - Chief Electrician, along with the GBMSD
maintenance personnel, were primarily responsible for the construction
and maintenance of the pilot plants.
285
-------
The efforts of the pilot plant operators and laboratory technicians on
the project staff contributed to the successful research program. The
GBMSD plant operators were responsible for the operation of the pilot
plants during the 4 P. M. to 8 A. M. period.
The services of Dr. L. B. Polkowski and Dr. W. C. Boyle, Polkowski,
Boyle and Associates, who were directly involved in the conduct and
evaluation of the research project, is gratefully acknowledged. The
assistance of the Special Consultants noted in this report was also
appreciated.
This project was funded 75% by the Federal Water Pollution Control
Administration. The assistance of Mr. Charles L,. Swanson, FWQA
Grant Project Officer and Mr. George R. Webster, FWQA Grant Project
Manager is acknowledged with appreciation.
286
-------
REFERENCES
1. Faulkender, C. R., Byrd, J. F., and Martin, D. W. , "Green Bay,
Wisconsin - Joint Treatment of Pulp Mill and Municipal Wastes",
J. Water Pollution Control Federation. 42, No. 3, p. 361 (1970).
2. Polkowski, L. B., andBoyle.W. C., "Investigation on the Treatment
of Charmin Yeast Processing Wastes Alone and In Combination With
Green Bay Domestic Sewage", (Unpublished Report for Proctor and
Gamble Co. - 1965).
3. Polkowski, L. B. andBoyle.W. C., "Pilot Plant Investigations On
the Biological Treatment of Charmin Yeast Processing Wastes in
Combination With Green Bay Municipal Sewage", (Unpublished
Report for Proctor and Gamble Co. - 1966).
4. Standard Methods for the Examination of Water and Wastewater.
12th Edition, American Public Health Assn. , New York (1966).
5. "Joint Municipal and Semichemical Pulping Waste Treatment",
Water Pollution Control Research Series, ORD-1, FWQA, U. S.
Dept. of the Interior.
6. Personal Correspondence, Crabtree, K. T., Assoc. Professor,
Dept. of Bacteriology, University of Wisconsin, Wausau, Wisconsin.
7. "The Determination of Orthophosphate, Hydrolyzable Phosphate and
Total Phosphate in Surface Waters1,' Subcommittee on Phosphates,
Technical Advisory Committee, AASGP, Inc., (1958).
8. Sanning, D. E. , "Phosphate Determination -A Method Evaluation",
Water and Sewage Works, 114, No. 4, p. 131-133.
9. Personal Correspondence, Wiersma, J. H. , Asst. Professor, Dept.
of Chemistry, University of Wisconsin, Green Bay, Wisconsin.
10. Hahn, D. J., "Filterability Index and Its Application", M.S.
Dissertation, University of Wisconsin, Madison, Wisconsin (1967).
11. Coackley, P., McCabe, Br. J. and Eckenfelder, W. W. Jr.,
Biological Treatment of Sewage and Industrial Wastes, Volume 2,
Chapter 3-2, Laboratory Scale Filtration Experiments and Their
Application to Sewage Sludge Dewatering, New York, Reinhold
Publishing Company (1958).
287
-------
REFERENCES (Cont'd)
12. Personal Correspondence, Lee, G. F., Professor, Dept. of Water
Chemistry, University of Wisconsin, Madison, Wisconsin.
13. Farquhar, G. J., "Filamentous Microorganisms in Activated
Sludge", Ph.D. Dissertation, University of Wisconsin, Madison,
Wis. (1968).
14. Farquhar, G. J. , "A Report On The Conditions Of Two Experimental
Activated Sludges For The Green Bay Metropolitan Sewerage
District, Industrial-Municipal Research Project", (Unpublished
Report for GBMSD-1968).
15. Heukelekian, H. and Weisberg, E., "Bound Water and Activated
Sludge Bulking", Sewage and Industrial Wastes, 28, No. 4, p. 558
(1956).
16. Farquhar, G. J., "Identification and Classification of Filamentous
Microorganisms In Activated Sludge", (Unpublished Report for
GBMSD-1968).
17. Personal Correspondence, Hunter, W. G., Professor, Department
of Statistics, University of Wisconsin, Madison, Wisconsin.
18. Watts, D. G., "Statistical Analyses of Research Data - Summary
Report"; (Unpublished Report for GBMSD-1969).
19. "Report on Financial Requirements and Cost of Service for the
Green Bay Metropolitan Sewerage District, Green Bay, Wisconsin",
Black and Veatch Consulting Engineers, Kansas City, Missouri,
(Unpublished Report for GBMSD-1970).
20. Personal Correspondence, Watts, D. G. , Professor, Dept. of
Statistics, University of Wisconsin, Madison, Wisconsin.
288
-------
APPENDICES
Appendix Page
A. Pilot Plant Facilities 291
1. Pilot Plant As-Built Drawing
B. Laboratory Procedures and Data Reduction 295
1. Micro-Kjeldahl Nitrogen Analyses
2. Ortho and Total Phosphorus Analyses
3. Color Analyses
4. Oxygen Uptake Procedure
5. Special Study - Oxygen Uptake - Process B
6. Special Study - Oxygen Uptake - Process D
7. Oxygen Transfer Procedure
8. Sulfide Analyses
9. Microbiological Analyses
10. Final Clarification - Laboratory Procedure - Phase II
11. Gravity Thickening - Laboratory Procedure - Phase III, IV
12. Air Flotation - Laboratory Procedures - Phase II, III, IV
13. Sludge Production Calculations - Phase II, III, IV
14. Computer Data Sheets and Data Graphs
C. Quantity and Characteristics of Municipal and Pulp Mill
Effluents ., 345
D. Experimental Data 355
1. Pilot Plant Laboratory Data - Phase IV
E. Solids Handling Studies - Laboratory Data 371
F. Full-Scale Design Parameters 393
1. Design Parameters Developed From Laboratory Data
2. Alternate Design Parameters Used in Cost Estimates
3. Parameters For Capital and Operating Cost Estimates and
Design Scale-Up Factors
289
-------
APPENDIX A
PILOT PLANT FACILITIES
291
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
APPENDIX B
LABORATORY PROCEDURES
AND
DATA REDUCTION
295
-------
MICRO KJELDAHL NITROGEN ANALYSES
Equipment Required
Complete Micro Kjeldahl Nitrogen Apparatus (Keeney Still), including
side arm flasks and receiving flasks; 0.2 g. Hach Spoon.
Procedure
A. Ammonia - N
1. Place a 10 ml. sample (or aliquot size sample diluted to 10
mis.) in a side arm flask.
2. Add approximately 0.2 g. of magnesium oxide to the flask,
swirl to mix, stopper, and place on distillation apparatus.
3. Pipet 5 mis of boric acid indicating solution into a receiving
flask and place in position.
4. Close steam bypass and begin distillation.
5. When there is approximately 35 mis. of distillate in the
receiving flask open the steam bypass again.
6. Titrate the distillate with 0.005 NH2SO4 titrant. The &nd
point is a pink-red color, a change from green.
B. Nitrate - N
1. Using the same sample size as for ammonia - N, add 0.2 g.
magnesium oxide and swirl.
2. Add 1 ml. of sulfamic acid solution, (to destroy nitrite) and
swirl.
3. Distill off approximately 30 mis to remove ammonia. (This
can be titrated and used for ammonia - N as above.)
4. Open steam bypass. Then add 0.2 g of Devarda's Alloy to
the sample.
5. Stopper the flask, close the steam bypass and collect 35 mis
of distillate in another receiving flask containing 5 mis of
boric acid indicating solution.
6. Titrate as in Step A-6.
C. Nitrite - N
1. Place a 10 ml (or aliquot size) sample in a side arm flask.
2. Add 0.2 g magnesium oxide and 0.2 g of Devarda's Alloy and
distill as normal. This distillate will yield ammonia +
nitrite + nitrate.
3. Titrate as in Step A-6.
4. Place another 10 mis of the same sample into another side
arm flask.
296
-------
5. Add approximately 0.2 g magnesium oxide and 1 ml of
sulfamic acid. Swirl to mix. Allow to stand for about one
minute to insure nitrite destruction.
6. Add 0.2 g Devarda's Alloy and distill. This distillation
yields ammonia + nitrate.
7. Titrate as in Step A-6.
8. Determine nitrite by difference.
Calculations
A curve of nitrogen standards, prepared on rectangular graph paper,
should be made by distilling known concentrations of ammonia-N and
titrating the distillates. The curve is made by plotting concentration
(mg/1 as N) versus volume of titrant (0.005 NH2SO4) used to titrate the
distillates. The slope of the line is then determined and an equation is
derived so that the concentration of nitrogen can be calculated by
inserting the volume of titrant into the equation.
Reagents
Boric Acid Indicator Solution - Prepared according to Section 2.2 -
Reagents, part 2, page 3 of Bremner, J. M. and D. R. Keeney, 1966,
Soil Sci. Soc. Amer. Proc. Report.
Sulfuric Acid, 0.005 N - Prepared from a 1 N stock solution.
Nitrogen Standard ^olutions - Prepared by dissolving 3.819 g NH^Cl in
one liter of ammonia-free H2O. From this stock solution various
dilutions are made and used to plot the nitrogen standard curve. (Stock
solution: 1 ml = 1.0 mg N.)
Magnesium Oxide .
~ j i AH Purchased from Chemical Companies.
Devarda's Alloy r
297
-------
MICRO KJELDAHL APPARATUS
§ 10/30
5 19/38
STEAM
TO WASTE
PAGE 299
-------
ORTHO AND TOTAL PHOSPHORUS ANALYSES
The lab procedure used for determining phosphates is an adaptation of
that presented in an Association of American Soap and Glycerine Producers
report "Determination of Orthophosphate, Hydrolyzable Phosphate, and
Total Phosphate in Surface Waters" in the American Water Works Assoc-
iation Journal, December, 1958.
A. Apparatus
All glassware must be carefully washed with phosphate-free soap
(Liqui-Nox), rinsed well with tap water, and then rinsed at least
three (3) times with distilled water.
1. Spectrophotometer or electrophotometer, red filter, wave-
length approximately 620-630 mu, optical cells with light
path of 20-25 mm.
2. Automatic pipet, calibrated, 50-ml capacity, with reservoir.
3. Pipets, calibrated, 25 ml, 10 mg, 5 ml, 1 ml. Safety
aspirator, (the safety aspirator used in these tests was the
"Propipet" manufactured by Will Corp., Rochester, N.Y.).
4. Graduated extraction cylinder, 100 ml, with well-fitting
ground-glass stoppers.
5. Volumetric flasks, 50 ml.
6. Beakers, 250 ml.
7. Graduated cylinders, 100ml.
8. Glass beads or Hengar granules, 1-2 mm diameter.
9. Hotplate, rheostat-controlled.
B. Reagents
1. Potassium persulfate, ACS reagent grade.
2. Potassium phosphate, monobasic, anhydrous, ACS (American
Chemical Society) reagent grade. Dry at 110° C for one hour.
Cool in a desiccator prior to weighing.
300
-------
3. Sulfuric acid, 8 N. ; Dilute 222 ml of concentrated H2SO4, (ACS
reagent grade, sp.gr. -1.84) to one liter with distilled water.
4. Ammonium molybdate solution, neutral, 10 per cent. Dissolve
100 g of (NH4) 6 Mo?O24-4H2O, ACS reagent grade and dilute
to one liter with distilled water. Store in brown, stoppered
bottle.
5. Acidic molybdate reagent. Equal volumes of 8 N sulfuric acid
and ammonium molybdate solution (see reagent number 4) are
mixed. Store in stoppered bottles.
6. Benzene-isobutanol solvent. Equal volumes of benzene and
isobutanol, both ACS reagent grade, are mixed.
7. Stock stannous chloride solution. Ten grams of SnCL? • 2H2O
are dissolved in 25 ml of concentrated HC1, both ACS reagent
grade. Solution should be freshly prepared every (2) weeks
and stored in a dark, stoppered bottle.
8. Sulfuric acid, IN. Dilute 27.7 ml of concentrated H2SC»4 (ACS
reagent grade, sp.gr-1.84) to one liter with distilled water.
9. Diluted stannous chloride solution. Add 0.5 ml of stannous
chloride solution (reagent number 7) to 100 ml sulfuric acid
(reagent number 8). Prepare daily.
10. Methyl alcohol, ACS reagent grade.
11. Alcoholic sulfuric acid: Mix 20 ml of concentrated H2SO4 (ACS
reagent grade, sp.gr. -1.84) with 980 ml of methyl alcohol, with
adequate stirring.
C. Procedure
1. Ortho Phosphate
Preparation of calibration curve. Dissolve 0.1917 g KtL^PO^ in
one liter of distilled water. This standard solution (Std. 1) contains
0.1 mg (100 ug) P2°5 per milliliter. Dilute 50 ml of this solution
to one liter to obtain standard solution (Std. 2) which contains
0.005 mg (5 ug) P2O5 per milliliter. Pipet 5, 10, 20, and 30 ml
aliquots of standard solution (Std. 2) into separate 100-ml graduated
extraction cylinders and dilute to 40 ml with distilled water. Add
301
-------
exactly 50 ml of the benzene-isobutanol mixture from an automatic
pipet. Measure 15 ml (t 0.1 ml) of the acidic molybdate reagent
in a 25-ml graduate, pour it into the 100-ml graduated extraction
cylinder containing the sample and the organic solvent, close
immediately, and shake vigorously without delay for exactly 15
seconds. (The time must be watched carefully when analyzing
mixtures of orthophosphates and condensed phosphates. Considerable
error could be caused by hydrolysis of condensed phosphates.)
Remove the stopper of the graduated extraction cylinder and, as soon
as the layers have separated, withdraw a 25 ml aliquot of the
supernatant organic solvent with a calibrated 25-ml pipet, using a
safety aspirator. Transfer the aliquot into a 50-ml volumetric
flask, add about 15 ml alcoholic sulfuric acid, and swirl. Add 1 ml
diluted stannous chloride solution, swirl, and make to the mark
with alcoholic sulfuric acid. Mix well and allow to stand 10 minutes
before reading percentage transmission at 620 mu. Measure within
30 minutes against the blank. Set up the calibration curve by
plotting micrograms of PZ^S against the percentage transmission.
2. Total Phosphate
Analysis for total P^Oc plus orthophosphate &2®5' Add 0.5 grams
of potassium persulfate and 8 ml of 8N sulfuric acid to an appropriate
aliquot and dilute to 48 ml with distilled water in a 150-ml beaker.
Add two Hengar granules, or several glass beads, to avoid bumping,
cover with a close-fitting, non-ribbed watch glass, and boil gently
for 40 minutes. Do not evaporate to dryness. Add 8 ml of 8N
sulfuric acid plus potassium persulfate and dilute to 48 ml with -
distilled water in another 150-ml beaker and carry it through the
whole procedure as a blank. After cooling, transfer the acid
solution into a 100-ml graduated extraction cylinder and rinse the
beaker and granules, or beads, with a few milliliters of water.
Make up to 48 ml with distilled water. Add exactly 50 ml benzene-
isobutyl alcohol mixture and 8 ml neutral (10 per cent) ammonium
molybdate solution. Stopper the cylinder and shake vigorously for
at least 15 seconds. In this procedure, extension of the shaking
period does not affect the result since all reversion of the hydro-
lyzable P2Og has been completed in the preceding hydrolysis step.
The analysis is completed as described in Sec. C-l -- Ortho
Phosphate Analyses.
302
-------
D. Calculations
1. Orthophosphate P2O5 (mg/1) = P2°5 from calibration curve (ug)
sample (ml)
2. Total PzOs (mg/1) = p2Qci from calibration curve (ug)
sample (ml)
3. Amount of PO4 (mg/1) = P2O5 (mg/l)x 1.34
4. Amount of P (mg/1) = P2O5 (mg/1) x .437
Note: All results are normally reported as P
303
-------
COLOR ANALYSES
Equipment Required
Spectronic 20
Bauch & Lomb Inc.
Cat. No. 33-29-61-62
1/2" I.D. Test Tubes
1/2" I.D. Test Tube Receiver for Spec. 20
Wavelength Range: 340-700 millimicrons
Method of Analysis
1. Filter all samples through Whatman #5 filter paper.
2. Just prior to analysis, the pH of the sample should be adjusted to
7. 6 by adding H£SO4 or NAOH as required.
3. Place the sample to be analyzed into a 1/2" I.D. test tube. The
sample should be at room temperature. If not, moisture will
develop on the outside of the test tube and interfere with the
transmittance reading on the Spec. 20.
4. Set the Spec. 20 at 375 mu wavelength and allow 1/2 hour warm up
time. Span the "% transmittance scale" as follows:
A) Adjusting the left dial, set needle at 0% transmittance.
B) Using distilled t^O as a blank (0 color units), place test tube
into receiver. Adjust the right dial until the needle reads
100% transmittance. Remove test tube and recheck the 0%
transmittance setting. If necessary, readjust, and then
recheck 100% transmittance until both limits are set.
5. Insert test tubes with samples and read % transmittance.
6. To determine the sample's color unit value, read the transmittance
value on the "Curve of Platinum -Cobalt Standards".
304
-------
350
100
90
80
70
60
50
CURVE OF PLATINUM COBALT STANDARDS
Percent Transmittance vs Color Units
Color Units
300
250
200
150
100
50
en
rt
o
40
30
20
10
9
8
7
6
s
in
"rt
u
d
nJ
-P
C
oi
0)
u
0)
700
650
600
550 500
Color Units
450
400
350
PAGE 305
-------
OXYGEN UPTAKE PROCEDURE
Equipment Required
Dissolved oxygen meter with automatic temperature compensation and
direct readout of dissolved oxygen in mg/1.
BOD bottles
Magnetic stirrer
Graph paper - rectangular grid
Introduction
Two basic procedures were utilized for oxygen uptake analyses; studies
were conducted on subreactors and also by utilizing the contents of the
pilot plant aeration tanks directly.
The subreactor study is outlined in the section of this procedure entitled
"Contact Stabilization-Control Process (B)"; this is the report of
analyses conducted May 21, 1969. This report illustrates how two
separate subreactors were used to obtain the total oxygen required for
the reaeration section and the contact section and the total BOD removed
in the contact section.
Oxygen uptakes conducted in-plant, September 15, 1969, are illustrated
in the section of this procedure entitled "Contact Stabilization Process-
Plant D-Oxygen Uptake Study."
The assumptions in a subreactor study are that, by utilizing the return
activated sludge and fresh primary effluent for a specific plant, the
conditions of aeration are fixed with regard to detention time, oxygen
level and solids concentration. Therefore, specific values can be
obtained for the quantity of oxygen required per pound of BOD removed.
The assumptions for in-plant oxygen uptake studies are that in a
continuous flow system the conditions under which the tests are conducted
are more realistic. The oxygen uptake analyses for the selected points
in the aeration tank are conducted in sequence as rapidly as possible.
Assuming a constant flow through the aeration tanks during the period
of testing, oxygen uptake rates, as a function of location (detention time)
in the tanks, can be obtained.
The procedure used to specifically measure the oxygen uptake in each
case is presented; the methods used to calculate the pounds of oxygen
306
-------
required per pound of BOD removed are detailed for each of the four
flow schematics. These procedures are applicable to either a subreactor
study or an in-plant study.
The number of Q£ uptake tests to be run on a subreactor is a function of
the theoretical detention time of the contact section of the process being
studied and the shape of the C>2 uptake rate versus time curve. The
tests should be continued beyond the theoretical detention time and an
adequate number of analyses should be made to accurately define the
shape of the curve.
In the case of in-plant studies, the tests should be conducted as quickly
as possible to minimize the ratio of total time of studies for the contact
or reaeration section to the theoretical detention time in the respective
section.
Procedure
1. Obtain approximately 500 ml of mixed liquor either from the sub-
reactor or the desired section of the aeration tank.
2. Aerate the 500 ml sample with pure ©2 to obtain about 10-15 mg/1
dissolved oxygen in the sample.
3. Immediately pour about 300 mis of the aerated sample into a BOD
bottle; insert a magnetic stirrer bar and place the dissolved oxygen
probe in the top of the bottle. Be sure the bottle is sufficiently full
so that oxygen bubbles are not entrained beneath the probe.
4. Place the bottle on a Magnastir. Maintain a constant Magnastir speed
during the entire study.
5. When the dissolved oxygen meter reading has steadied, read the
initial D.O. (Time: 0).
6. Continue to read the dissolved oxygen content a minimum of every
minute for approximately 10 minutes or until the D.O. content
becomes less than 0.5 mg/1.
7. Plot the measured dissolved oxygen content (mg/1), (on the ordinate)
versus Time (minutes), (on the abcissa) on rectangular-grid graph
paper.
307
-------
8. The slope of the line in Step 7 is the oxygen uptake rate in mg D.O. /
liter/minute. Convert this rate to mg D.O. /liter /hour.
9. Run total suspended and volatile suspended solids analyses on a
portion of the sample.
10. Allow the approximately 200 mis of sample remaining from Step 3
to settle for 30 minutes; withdraw a portion of the settled supernatnat
for BOD analysis.
11. Plot on rectangular -grid graph paper the QZ uptake rate (mg/l/hr)
(on the ordinate) from Step 8 versus time (hrs) (on the abscissa)
elapsed since combining the raw sewage and RAS.
12. Plot on rectangular -grid graph paper the BOD remaining (mg/1)
(on the ordinate) from Step 10 versus time (hrs) (on the abscissa)
elapsed since combining the raw sewage and RAS.
The following methods were used to calculate the pounds of Oxygen
required per pound of BOD removed:
A. Conventional Activated Sludge Process
On the graph of Q£ uptake rate versus time, draw a vertical line at
the theoretical detention time of the aeration section. Planimeter
the area between T0 and T (theoretical detention time) beneath the
curve. Record this value as total mg O2/liter used for the given
detention time.
The initial calculated BOD is obtained as follows:
Initial Calculated BOD = Influent Q x Influent BOD + RAS Q x RAS Supt. BOD
Influent Q + RAS Q
The BOD removed is the difference between the initial calculated
BOD, (mg/1) and the BOD of the FE at the theoretical detention
time. The FE BOD value is obtained from the BOD remaining versus
time curve for the chosen detention time.
The total C>2 used (mg O2/1) divided by the total BOD removed (mg
BOD/1) for the chosen detention time gives total milligrams (or
pounds) O2 required per milligram (or pound) of BOD removed.
308
-------
B. Step Aeration Activated Sludge Process
As in the conventional process, the theoretical detention time for
each zone of aeration is marked sequentially on the C>2 uptake rate
versus time curve. The areas for each zone of aeration beneath
the curve are planimetered. The areas determined are then
multiplied by the respective volume for each zone of aeration to
obtain a mass weight of Q£ used. The total C>2 requirement (mg)
is obtained by summating the O2 used in each zone.
The BOD removed for each zone of aeration is the value of the
initial calculated BOD minus the FE BOD for that zone. The BOD
removed times the respective volume of the zone of aeration were
summated to obtain the total BOD (mg) removed for all zones. The
pounds of ©2 required per pound of BOD removed was then obtained
as for the conventional process.
C. Contact Stabilization Activated Sludge Process
A vertical line marking the theoretical detention time of the contact
section is drawn on the Q? uptake rate versus time curve for the
contact and reaeration sections. The area beneath each curve was
then planimetered and reported as mg O2/1. The volume of each
section is then multiplied by the respective mg O2/1 value; the mass
of ©2 for each section is then summated to obtain the total ©2 used
during the theoretical detention time of the contact section. The
total BOD removed (mg/1) is the initial calculated BOD minus the
FE BOD of the contact section at the theoretical detention time of
the contact section. This value must be multiplied by the volume of
the contact section to obtain the mass weight of BOD removed. The
pounds of QZ required per pound of BOD removed is then calculated
the same as for the step aeration process.
D. Kraus Activated Sludge Process
The procedure to obtain pounds of 0% required per pound of BOD
removed is identical to that for the contact stabilization process;
the nitrifying section was treated in the same manner as the
reaeration section of the contact stabilization process.
309
-------
SPECIAL, STUDY - OXYGEN UPTAKE
Contact Stabilization
Control Process (B)
May 21, 1969
This study was conducted using a grab sample of fresh RAS placed
in a 3-liter reactor identified as CS-Reaeration Section. Chlorine at the
rate of 10.7 mg/1 was added to the RAS to simulate actual conditions in the
pilot plant.
A second reactor identified as CS-Contact Section, was set up using
an R/Q value of 0.50. The actual volumes used were 3 liters of sludge
from cell 5 (last cell of reaeration section) and 6 liters of primary effluent.
To best represent the actual conditions in the pilot plant, nutrient addition
was also included. (137 ml of nutrient solution was added to 6 liters of
primary effluent. In actual operation the pilot plant added 1 ml of nutrient
solution for each 44 ml forward flow of primary effluent.)
CS Reaeration Section
Time Hours MLTSS MLVSS % Vol. O? Uptake BOD
mg/1 mg/1 mg/l/hr mg O?./g mlvss*/hr mg/1
09:15
10:15
11:15
13:15
15:15
0
1
2
4
6
09:15
09:45
10:15
10:45
11:15
12:00
13:15
14:15
15:15
0
1/2
1
1-1/2
2
2-3/4
4
5
6
11440
11460
1712
2116
9608 84.0
9696 84.6
CS- Contact
1512 88.3
1800 85.1
81
60
60
52
45
Section
96
76
48
41
36
24
30
29
23
Primary Effluent
Cell 5 4832
4220 87.3
8.4
6.2
6.2
5.4
4.7
58.0
45.9
29.0
24.8
21.
14.
18.
17.
7
,5
1
5
13.9
(Supernatant)
345
240
188
144
115
109
117
105
96
615
80
0.80 #O2 Required/#BOD removed for 3.27 hr. detention time.
d^.
Based on average of MLVSS determinations: 9.652 g for CS-reaeration sec.
1.656 g for CS-contact section
310
-------
100
80
M 60
6
s
H
o
20
0
O3 UPTAKE vs TIME
Contact Stabilization-Control
Contact Section
Subreactor
R/Q = 0.50
MLTSS 1914 mg/1
MLVSS 1656 mg/1
Date 5/21/69
153 mg/1 Oxygen Required in 3.27 Hours
3.27 Hours - Calculated Detention
Time of Contact Section
234
Aeration Time, Hours
-------
100
O UPTAKE vs TIME
OJ
t—>
UJ
M
-s.
&JO
>N
X
O
80
60
40
20
Contact Stabilization-Control
Reaeration Section
Subreactor
R/Q 0.50
MLTSS 11450 mg/1
MLVSS 9652 mg /1
Date
5/21/69
191 mg/1 Oxygen Required in 3.27 Hours
3.27 Hours - Calculated Detention
Time of Contact Section
234
Aeration Time, Hours
-------
480
Ul
400
320
240
Q
O
160
Initial Calculated BOD = 437 mg/1
BOD vs TIME
Contact Stabilization-Control
Contact Section
Subreactor
R/Q = 0.50
MLTSS 1914 mg/1
MLVSS 1656 mg /1
Date 5/21/69
335 mg/1 BOD Removed in 3.27 Hoars
234
Aeration Time, Hours
-------
SPECIAL STUDY - OXYGEN UPTAKE
Contact Stabilization
Process D
September 8, 1969
This study was conducted by grabbing samples directly from the
pilot plant reaeration and contact section cells. In an attempt to insure
the use of accurate detention time in plotting the curves of "C>2 Uptake
vs. Time", samples were taken from the initial point of entry to the cells
and from mid-depth in the cells. The results tend to show that, due to
thorough mixing within the cells, the values for the mid-cell analyses
would be the best in plotting the various curves.
The flows of RAS, nutrient addition and chlorine addition into the
pilot plant were measured at the time of the study. The Q£ value and the
mixed liquor solids determinations were taken from the daily calculations,
Cell and total detention times were based upon the flow data for the pilot
plant at the time the tests were conducted.
The location of the samples, A-J, are shown in the sketch below.
1
RAS Qf,
Cl2 Primary
Nutrients Effluent
A
B
^
^^
f
D
l
C
J
\
E
1
F
1 V.
^-^
(
i
G
J
\
H
i
^
J
1
I
J
To
*• Final
Clarifier
Cell 5 Cell 6 Cell 7 Cell 8 Cell 9 Cell 10
317
-------
SPECIAL STUDY - OXYGEN UPTAKE
PROCESS D
September 8, 1969
Sample Time
Cell Detention Time, Hours
Total Detention Time, Hours
MLTSS
MLVSS
% Volatile
O Uptake - Mid Cell Value; mg/l/hr
BOD - Mid Cell Value; mg/1
REAERATION
Cell Cell
5 6
12:30
1.82
1.82
60
12:45
1.82
3.64
10140
8924
88.0
48
CONTACT
Cell Cell Cell Cell
7 8 9 10
1:10
0.60
0.60
75
102
1:20
0.60
1.20
54
68
1:30
0.60
1.80
42
53
1:40
0.60
2.40
3728
3368
90.3
39
42
Qf - 4552 L/D Nutrient Solution - 67.7 L/D
RAS- 2131 L/D C12 Solution - 50.4 L/D
Based on attached data, 0. 67 pounds of O2 are required (total amount for reaeration plus contact sections)
per pound of BOD removed in the Contact section.
Note: Cells 1-4 were not being used at the time of this study.
-------
100
uo
N)
80
60
a
C
0)
40
20
Surface-Cell 7
Mid Cell 7
Cell 9
Mid Cell 10
Surface-Cell 10
Q2 UPTAKE vs TIME
Process D
Contact Section
MLTSS 3728 mg/1
MLVSS 3368 mg/1
Date 9/8/69
123 mg/1 Oxygen Required in 2.40 Hours
•* 2.40 Hours - Calculated Detention Time of
Contact Section
2 3 4
Aeration Time, Hours
-------
oo
N
OJ
100
80
00 60
0)
X
rt
OJD
>>
«
O
40
20
Surface-Cell 5
O-, UPTAKE vs TIME
Process D
Mid Cell 6
Reaeration Section
MLTSS 10140
MLVSS 8924
Date 9/8/69
_mg/l
_mg/l
/Surface-Cell 6
©
136 mg/1 Oxygen Required in 2.40 Hours
2.40 Hours - Calculated Detention Time of
Contact Section
234
Aeration Time, Hours
-------
250
Q
O
200
150
100
Initial Calculated BOD = 326 mg/1
Surface-Cell 7
Mid Cell 7
Mid Cell 8
Mid Cell 9
Mid Cell 10
Surface-Cell 10
BOD vs TIME
Process D
Contact Section
MLTSS 3728 mg/i
MLVSS 3368 mg f\
Date 9/8/69
284 mg/1 BOD Removed in 2.40 Hours
234
Aeration Time, Hours
-------
02 TRANSFER PROCEDURE
LABORATORY APPARATUS - FIGURE I.
\
D
10
.£X
0. METEF
(ft
.MUM*
/
~S
Pi A DD ADC
r-DIFFUSERS
^ijS
AIR
FLOW
RATER
•AIR SUPPLY
DRAIN
1. Place tap H20 (temperature adjusted to that of the
sample to be run) in container (approximately 2 liter
cylinder).
2. Strip any ©2 present in F^O with N2 gas.
3. Aerate at a constant air flow rate.
4. Measure D.O. at various time intervals.
5. Plot a curve of D.O. vs. aeration time on 10 x 10
rectangular graph paper.
FIGURE 2
to
9
z
U
O
>-
X
o 4
UJ
o
TAP H20
2 34 56789 10
AERATION TIME, MINUTES
327
-------
6. Drain H^ (Do not change position of D.O. probe
or diffusers.)
7. Place sample in container.
8. Strip 02 with N2 gas.
9=. Aerate at the same air flow rate as used with the
tap H20.
10. Measure D.O. at various time intervals.
11. Plot a curve of D.O. vs. aeration time on 10 x 10
FIGURE 3. rectangular graph paper.
12 34 56789 10
AERATION TIME, MINUTES
12. Determine the slopes of tangents drawn to the
curves at several points along the curve, (avoid
using the ends of the curves).
12 34 5678 9 10
AERATION TIME, MINUTES
328
-------
13. Plot dc/dt vs. D.O. concentration for the tap 1^0 and
for the waste sample.
Figure 5.
10
9
8
7
6
. 5
4
3
2
14,
15,
16,
17.
TAP H20
I 23456789
DISSOLVED OXYGEN Mg/L
10
u
•o
10
9
8
7
6
5
4
3
2
I
0
SAMPLE
2345
8
DISSOLVED OXYGEN Mg/L
Determine the slope of the lines plotted in Figure 5.
Alpha* equals the slope of the waste sample curve
(K^A-Waste) divided by the slope of the tap ^0 curve
(KxA-Tap Water).
By extending the line plotted in Figure 5 until it
intersects the axis of D.O. concentration, the 02
saturation value of the sample can be determined.
Beta is the 02 saturation value of the Waste (Cs-Waste)
divided by 02 saturation value of the tap ^0 (Cs-Tap
Water).
10
*Alpha = KjA Waste
KjA Tap Water
329
-------
SULFIDE ANALYSES
Equipment: Model 404 Orion Specific Ion Meter; Sulfide Probe Model
94-16; Orion Double Junction Reference Electrode Model 90-02.
The calibration curve for the measurement of sulfide ion is a plot of
millivolt reading vs. the log of the activity of the sulfide ion in moles/
liter. A 20 x 20 cycle rectangular graph paper is used for this plot.
A low point and a high point are determined for this graph and a straight
line is then plotted through the two points.
The low point for the graph is found by the following procedure:
1. Saturate a 0.1 Molar HC1 solution with t^S gas for approximately
10 minutes.
2. With the Orion sulfide probe and double junction reference
electrode installed on the Model 404 Orion Specific Ion meter,
and the control knob placed in the millivolt mode, insert the
probes in the HCl-t^S solution and read and record the milli-
volt reading.
3. The known activity for this solution is 1.8 x 10~19 moles/liter.
Knowing the millivolt reading and the activity for this solution,
the low point can then be plotted on the graph.
The high calibration point is found as follows:
4. Make a . 1 Molar solution of Na2S. 91^0 in t^O rather than in
1 Molar NaOH as specified in the instruction book.
5. Dilute the solution from Step 4 accurately to 1:1 with a buffer
solution to lower the pH to between 7. 6 and 8.0. If necessary,
a few drops of concentrated HC1 may also be added to bring
the pH to the desired range.
6. Place the solution from Step 5 in a beaker and insert the sulfide
reference probes (see Step 2). Read and record the millivolt
reading. The millivolt reading should be approximately 680-
690 millivolts. Measure the pH of the solution.
7. To determine the total sulfide concentration (Ct), titrate 25 ml
of the solution from Step 5 with 0. 1 Molar silver nitrate (AgNO3)
using the sulfide probe and meter to determine the end point by
330
-------
titrating through zero millivolts. The resulting concentration
of the sodium sulfide should be about .05 Molar.
8. The formula, Ct = f x Ag = , can now be used to obtain the value
for As = . The value for C^. is obtained in Step 7. The value
for f is a function of the pH of the solution and can be obtained
from a chart in a sulfide probe instruction manual. Knowing C
and f, the value for As= can be determined. Having the value
of As = and the millivolt reading for the given solution, this
point can then be plotted on the calibration curve.
9. Draw a straight line between the two points on the graph. The
slope of the line should be such that there is about 29.6 milli-
volt change for a tenfold change in concentration.
To measure sulfides in an unknown solution;
1. Determine millivolt reading of solution.
2. Measure pH of solution and obtain value for "f",
3. Obtain Ac= from calibration curve.
O
4. Knowing f and Ag= calculate C^..
Ct = f x As =
331
-------
MICROBIOLOGICAL ANALYSES
Microbiological analyses on activated sludge samples were conducted
routinely every two days unless some unusual condition required closer
and more frequent observations. Grab samples were taken from Cell
10 of each of the four plants for these analyses. Grab samples of mill
wastes were analyzed about once a month.
All analyses were made using an American Optical Series 10 Phasestar
microscope equipped with a Polaroid camera. Photographs of Cell 10
observations were taken once a week. In addition, any unusual or
excessive condition was photographed at the time of occurrence.
Maximum magnification with this microscope and 20 X eyepiece was
2000X, with a maximum Polaroid print magnification of 1500X.
All samples were first observed on low power (200 X) for filament
extent, floe dispension, and bridging of floe. The presence of higher
biological forms and of non-biological forms was noted. Samples
were then observed on high power (900X). The types of biological life
were reported and any filaments were examined for presence of
granules.
If the number of filaments was sufficiently great, filament identification
was attempted according to the procedure developed by Dr. Farquhar""'
The microphotograph form is shown on the next page.
332
-------
MICRO PHOTOGRAPH FORM
Sample Picture No. Date
Magnif. 75 150 338 750
Trans. Set 4.5 5.0 5.5 6.5 7.5
Expos. Time 1/1 1/2 1/5 1/10 1/25 1/50 1/125
Mount — Wet, Dry; Dry — Air, Heat; Coverglass, Yes No
Stain - Yes No: 1 2 3 4 5 6 7
Phase — Yes No; Contrast — Bright, Dark
Objective lOx 20x 45x lOOx
Condenser A B C D O
Illuminator Filter — Yes, No; Others — Yes, No
REMARKS:
Initials
333
-------
FINAL CLARIFICATION-LABORATORY PROCEDURE - PHASE II
The samples used for the final clarification studies during Phase II were
Cell 10 (last aeration cell) mixed liquor (at the existing concentration)
from each pilot plant.
The equipment utilized was a 3-1/2 inch internal diameter x 12-feet
sidewater-depth clear acrylic settling tube. The column contained a
mechanical stirrer operating at a peripheral speed of about 1.0 feet
per minute. An acrylic block was used as the base for the column and
was supported above the floor by an angle iron frame with adjustable
legs. A pipe tee was tapped into the bottom of the acrylic block to
permit dual valving for filling and draining the column. This bottom-
fill technique was employed to minimize the formation of air bubbles
and to keep the column contents homogeneously mixed until the column
was filled.
The position of the solids-liquid interface was recorded every 5 minutes
for the first half hour, every 10 minutes for the next half hour, every
15 minutes for the next three hours, and every 30-60 minutes thereafter
until there was no change in the interface height for at least three
successive readings or until the test was arbitrarily stopped. The
resulting settling curve was analyzed by the Kynch Method to determine
the time of concentration (Tc) to obtain a 1.0% sludge underflow
concentration. Based upon the initial portion of the settling curve,
corresponding clarification rates (C.R.) were calculated in terms of
gallons per day per square foot of surface area.
This column was also used for the gravity settling column tests
discussed in the section of this report entitled, "Primary Clarification".
Removable taps, which projected 1/2 the radius into the tube, were
inserted at the 2, 4, 6, 8, 10 and 12-feet levels above the bottom of
the column. The tube was slowly filled from the bottom with the sample.
The taps were sampled sequentially from the top to the bottom each 15
minute interval, for 90 minutes; approximately 50 mis of liquid were
first wasted from each tap to insure that a representative sample was
obtained. Based upon the initial and sequential total suspended solids
analyses, the percent removal at each depth for each time period was
calculated.
334
-------
GRAVITY THICKENING-LABORATORY PROCEDURE - PHASE III, IV
During Phase III and IV of the research project, fresh WAS and combined
fresh WAS and primary clarifier sludge were used as sludge sources
for the gravity thickening tests. During Phase III the samples were
used as obtained; during Phase IV both undiluted and diluted (with final
effluent) samples were used.
X
The equipment utilized consisted of one-liter graduated glass cylinders
equipped with mechanical stirring mechanisms which operated at a
peripheral speed of approximately 0. 05 fpm. The pickets were three
small-diameter rods, extending the full length of the cylinder, which
were rigidly positioned in a triangular pattern approximately one inch
on a side.
Solids-liquid interface readings were taken every 5 minutes for the
first half hour, every 10 minutes for the next half hour and every 30
minutes for each hour thereafter until there was no change in the inter-
face height for at least three successive readings, or until the test
was arbitrarily stopped. These data were plotted on rectangular graph
paper and the resulting curves were analyzed to obtain the desired
design parameters.
335
-------
AIR FLOTATION-LABORATORY PROCEDURE - PHASE II. III. IV
All air flotation tests were conducted according to test procedures
developed by Rex Chainbelt, Inc. The equipment consisted of a small
clear acrylic pressure cylinder and one-liter graduated cylinders.
For Phase II, the air flotation tests were run on diluted samples of
Cell 10 mixed liquor and WAS respectively, rather than utilizing the
existing solids concentration of the given sample. The sample was
diluted with final effluent to approximately the same concentration as
the lowest sample concentration of the four pilot plants. For Phase III
and IV, the samples were used as obtained and were not diluted with
final effluent.
The solids-liquid interface was plotted versus time to determine the
point at which compaction of the floating solids blanket began. This
compaction point was used to determine the rate of ascent (or rise
rate) in feet/minute.
Two flotation-thickening parameters for each pilot plant sample, the
rate of ascent and the calculated float concentration, were each ranked
1, 2, 3, or 4 for the four samples. These values were then summated
to yield a composite ranked value for each pilot plant.
336
-------
SLUDGE PRODUCTION CALCULATIONS - PHASE II. III. IV
Sludge production calculations were based on the last 7 days of data
for each statistical experimental design condition during Phase II.
Seven-day intervals were also used during Phase III. Sludge production
calculations during Phase IV were based on intervals ranging from 15
to 27 days.
Factors considered were:
1. The total amount of WAS (TSS, grams) generated during the
study period.
2. The discharge of solids (TSS, grams) from the process, via
the final effluent, during the study period.
3. The change in inventory of solids (TSS, grams) under aeration
between the first and last day of the study period.
4. The change in inventory of solids (TSS, grams) in the final
clarifier between the first and last day of the study period.
The equation is as follows:
Total Sludge Production =
WAS + TSS in FE + A TSS in Aeration Tank +A TSS in FC.
Seven-day averages of primary effluent and final effluent BOD were used
during Phase II to determine the grams of BOD removed during the
interval. Both filtered and unfiltered BOD removals were determined
and corresponding sludge production rates were calculated. (Filtered
BOD values were obtained using Whatman No. 5 filter paper.) A
summation of daily BOD removal values was used for Phase III and
IV solids production rate calculations.
337
-------
04
69
PRIMARY CLARIF1ER
FLOW DATA LITER
HILLS
DAY DATE
01
02
03
04
05
06
07
08
09
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
1
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1699
1621
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
2
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1776
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
1853
3
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3487
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
3892
/ DAY
4
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0830
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
0926
USD
0004819
0005088
0005205
0006208
0005731
0005830
0008415
0010482
0010130
0008919
0008843
0008022
0006610
0008044
0008030
0007363
0007468
0006981
0007582
0006935
0006564
0007745
0011152
0011466
0007495
0009513
0009933
0010209
0009081
0009623
TOTAL
13343
13612
13729
14732
14255
14354
16939
19006
18654
17443
17367
16546
15134
16568
16554
15656
15259
15505
16106
15459
15088
16269
19676
19990
16019
18037
18457
18733
17605
18147
FORM Al
I
PH
6.5
6.8
6.6
6.4
6.4
6.6
6.7
6.7
6.9
6.8
6.8
6.8
6.7
6.7
6.8
6.7
6.8
6.7
6.7
6.8
6.4
6.7
6.8
6.7
6.8
6.7
6.6
6.8
6.7
6.8
N F
TSS
252
212
248
176
492
116
188
192
184
124
196
184
092
200
204
184
216
180
132
136
272
204
308
116
252
192
168
252
200
244
L U E
VSS
240
144
160
156
480
096
160
172
180
160
080
136
156
156
140
120
124
192
196
224
064
220
192
144
212
180
212
N T
BOD S =
0615
0650
0550
0510
0521
0561
0439
0370
0535
0495
0645
0533
0606
0584
0530
0490
O525
0510
0578
0572
0593
0590
1230
0515
0500
0476
0442
0458
0520
0725
**************************************************************************************************************
TOTAL 055204 055513 0116355 027684 0239486 00494242 200.9 06116 04696 016868
AVG
MAX
1840
1853
1850
1853
3879
3892
923
0926
7983
0011466
16475
19990
6.7
6.9
204
492
174
480
562 .00
1230
1621
1776
I) 004819
13343
04
PRIMARY CLARIFIER
EFFLUENT
TSS P/CNT
BOD P/CNT
EFFLUENT
BOO ' COLOR
DAY DATE
TSS
VSS
RED
RED
UNITS
*****:
TOTAL
AVG
MAX
MIN
01
02
03
04
05
06
07
08
09
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
3O
*****
6.3
6.9
6.7
6.3
6.4
6.4
6.7
6.7
6.8
6.9
6.8
6.9
6.7
6.9
6.9
6.9
6.7
6.8
6.7
6.8
6.5
6.8
6.6
6.8
6.9
6.8
6.7
6.8
6.8
6.8
********>
201.7
6.7
6.9
6.3
064
132
240
136
152
116
112
136
120
112
124
128
080
152
160
140
100
140
140
112
176
124
168
088
184
112
120
172
116
168
k*******i
04024
00134
240
064
100
160
128
148
112
104
136
120
116
072
108
128
108
096
104
080
132
112
120
040
044
092
152
104
128
*********
02744
00110
160
040
74.6
37.7
3.2
22.7
69.1
.0
40.4
29.2
34.8
9.7
36.7
30.4
13.0
24.0
21.6
23.9
53.7
22.2
17.6
35.3
39.2
45.5
24.1
27.0
41.7
28.6
31.7
42.0
31.1
********
34.3
74.6
.0
630
620
545
525
572
538
417
380
435
570
540
482
487
507
435
420
495
400
567
493
530
535
540
385
470
459
408
408
495
505
*********
14793
00493
630
380
4.6
.9
4.1
5.0
18.7
16.3
9.6
19.6
13.2
17.9
14.3
5.7
21.6
1.9
13.8
10.6
9.3
56.1
25.2
6.0
3.6
7.7
10.9
4.8
30.3
********
12.3
56.1
.9
1728
1681
1594
1464
1446
1430
1267
1099
1000
1199
1356
1432
1470
1417
1426
1652
1280
1402
1417
1424
1591
1560
1433
1216
1285
1293
1245
1245
1282
1339
'********«
041673
001389
1728
1000
570
540
510
470
510
510
470
420
410
460
490
505
515
490
450
470
460
495
500
460
535
535
490
450
455
440
445
445
480
460
!*******<
14440
00481
570
410
1.11
1.15
1.07
1.12
1.12
1.05
.89
.90
1.06
1.24
1.10
.95
.95
1.03
.97
.89
1.08
.81 318
1.13
1.07
.99 318
1.00
1.10
.86
1.03
1.04
.92
.92
1.03
1.10 323
t***************** ******
30.68 00959
1.02 00320 .00
1.24 323
.81 318
338!
-------
OJ
OJ
(S)
04 69
i, 55T5« BffSi 5177 HIS JS53 ttl S555J 5755? KT5 SI
0! 0»16B 07111 *>.« !•.;> »6«4 »>.* 6*«H S*6Ju «!.i 01
0. 0W» , U770» ?5.» 5l!S .311 .5.6 CJ6JJ OaUo JJ.l . p«. ,.
06 0927* 07946 89.6 SC56 4374 86.5 096?6. 06344 86.7 06
OB 10036 OB720 86.9 4060 418D 89.7 1O28B 09004 87.9 08
10 09728 00392 86.3 4172 4136 66.7 0958 H 06412 87. 10
H 59421 08312 aa.; 4944 4T73 sO BTO oRTI SKJ ii
09120 0793? 87.2 9^30 4530 88. ! 09824 OB*)1* 6T75 13
14 08732 07612 87.2 5468 4832 88.4 C9B96 08484 «5. 14
16 09680 OB6B4 89.7 9064 4904 BB.9 10460 09*32 86.3 16
IB IQIQQ 0*768 04.8 459? 4060 88.4 «J14(I OB950 *T.T J*
20 10376 09030 67.1 4,92 4286 86.* 11046 09760 88.4 20
2? II24S 04824 RT.I 91«« 4670 09. 1 11756 10176 U. 3 22
51 r?524 noil 577? 4751 MIS TO I3T64 TTTR 1T75 n
* 1168 B 10140 86. B 452C 3920 86.7 11472 10043 8t.6 25
it, ll?40 04704 06. 2 47?* 4160 66.0 11172 0975? BT.3 26
28 10174 08672 85.7 3852 3276 89.0 08924 0766* 64.1 28
tvu
04
616641 661702 86.7 004421 0042FS 86.9" OlG*« UoViT8"~BT72 ' JVC OOfrOOft 001
13437 116BO 8«.7 9H24 4964 89.1 13164 11574 64.2 MAX
ttHAttOH tAM itXIOS MdCftt~'JT " H!ffS 55
L/D US P£ 10 30 30 MIN ilUDGE
0950 55so — 537?* 4i 7"
0990 0830 00162 41
'
C BOO
s vss ••••- —
n 751
1 .34
09)0 0760 OOI5S 4l" .36 .32 ~ ~
0880 0700 00143 00 .34 .31
090C C6?C CD (JO 00 .15 .44
CBOO 0620 00k 29 00 .37 .35
0006 0*00 00091 00 .34 .)6
0900 035O OOO69 00
1 .27
OHO 0)20 00070 00 .3) .27
04 TO 0)60 00069 00
6455 0216 : 86699 BQ 7
5 .14
0 .32
3 .3! -
4 .34
0390 0260 00096 00 .3 .29
0490 030O OOO63 00 .32 .3)
0310 0210 00099 00 .40 .37
05JO 0240 00050' 00 .34 .75 _— —
unrc oweo m — mrrcoo ni — PDKTI — CTOJUB — BOTTO ITOKI m ^r — — —
0980 0910 00169 49 .40 .44
OVPftSS *CT ACT R/0 ACT CMN» / D»Y TSS LOW p/CNT P/CNT P/CNT P/CNI
0? OOOO D03403 3715 1.09 07.1 000742 000639 27.2 02 132 068 46.9 100 040 60.0 620 098 84.2
04 OOOO 0036B3 3283 .89 56.8 000947 000463 25.1 04 136 106 20.6 128 OS* 34.4 525 106 79.8
05 OOOO 001564 3024 ,85 60.6 0009 55 OO0476 24. 1 05 152 05
06 OOOO 003589 3024 .84 4S.4 000437 000379 23.5 06 116 Ol
84.5 112 538 054 90.0
9 OOOO (J04A64 3454 . 74 60. 1 000451 000577 26.7 09 1 20 030 75.0 435 696 87. 1
0 OOOO 004361 3494 .79 49.2 000472 000414 26.2 , 10 112 O32 71.4 570 038 93.3 398 050 87.4
) OOOO 007704 7341 .66 79.7 OOOT44 000645 25. 6 13 080 02
4 OOOO 004142 3226 .78 J7.9 000379 000322 28.3 14 152 04
19 OOOO 004139 2822 .68 98.4 001098 OOO936 25.6 19 160 03
16 OOOO 003V14 2)92 .66 87.1 000911 000804 23.1 16 140 O2
7 OOOO 003B15 2650 .69 48.1 0006 75 00099* Zt.l ' 17 too' 01
B OOOO 003876 2650 .68 T1.9 000730 OO0640 21.0 18 140 02
0 OOOO 003865 ?592 .67 37.9 000419 000370 22.4 20 112 04
22 OOOO O04067 2016 .90 75.7 000890 OOOTS5 22.1 22 124 O3
4 OOOO O04998 ? 160 .43 113.6 001376 001206 23.3 24 088 06
5 OOOU O040Q5 2246 .56 102.2 001172 001027 19.8 25 184 02
27 OOOO 004614 2189 .47 102.2 001027 OO0891 20.5 27 1 20 02
28 OODO 004683 1024 .65 102.2 000912 OOOt89 20.8 28 172 O5
30 OOOO C045J7 J2?6 .71 24*5 00029) 000241 ??.9 30 168 05
TOTAL
68.6 072 Ot3 6l. 6 487 64S 46.8
72.4 1Q8 027 79.0 507 054 89.3
F "B3.0 4« 032 «.5 413 615 *6.4
BO.O 096 Ot 7 82.3 400 02« 91.1
59. B 080 037 93,8 493 032 93.5
72.d 112 028 75.0 S3S 064 8B.O
9.1 040 072 389 Q3B 90.1 28* 014 95.1
86.6 459 032 93.0
UNITS S-
235
299
215
282
1.6
305
?77
240
6B.6 15? 092 69.8 406 098 85.8 7.5
70.2 128 040 68.8 905 040 92.1
HlN OOOo 0633)6 Z0l6 .43 22.7 000206 1100 17* 14.8 H!N 0«4 61* 4.1 040 till 34.4 Jfl3 0*6 W.S ?94 01) SA.S
0
NM3 - N H03 N OR
T H 0 CELL 10
PE DS PEF PI PC PEP N »
TCTAL
MX
02 01
04 .4 03 1.1
06 17.0 29.1 ' 6.4 . 2.4 05
06 .9 07
10 09 .9
12 9.2 IT. 2 10.2 " 1.3 11
4 2-2 13
6 15 .5
18 10.2 21.3 9.8 .B 17
19 18 .3
20 19
22 21 .5
4 11.8 19.8 11.0 1.9 23
6 1.6 25
B 27 .3
C I>f0 18.8 .11.1 .6 29
4.7 3.4 3.9
5.0 4.1 6.5
9.8 2.1
4.4 4.2 4.1
5.1 4.2 3.4
9.5 2.2
5.7 4.1 4.0
10.3 2.1
5.4 3.8 1.5
T.6 1.9
073 — "WoTffl JT79 ' — TT72 771 T7J ' 173 "" ToT*C 673 46V5 SSTT 5571 . ~ ~4«.J ~ 9.T "
17.0 29.1 ... 22.3 . 2.6 (.4 »VG .6 0000 4.7 ... 3. J.6 .0 ».Z 1.9
MIN .1
1.0 1. 1-5 7.8 1.5
240
.3 02432
.6 305
.4 "215 •'
PEF BOD N.P.
N P
4.B .9
>.) 1.1
J.6 .9
4.7 1.2
*.2 1.1
6.2 1.3
49.3 R73
4.9 1.0
3.6 .6
-------
CM
•b
o
04
" 61
02
' OJ
64
0*
4?
04
-
-
If
K_
24
H
26
3*
H_
30
TOIAL
MAX
o?
04
04
1?
ff
i?
H
24
24
-w...il
PJ
04
OB
to
12
»4
14
IB
20
24
26
«
IvC
MAX
it
TH
'""Hi**
07»3?
' 67*11
0*4i2
0*1)4
A**}*
11094
' '1164*
10411
loll!
10)10
t&US
10*71
UT00
U344
Eo9lfl
10904
IU»4
1139*
lliii
11004
300994
1170B
•'Mil
9000
oooo
H9
MW
P90°
MOO
oooo
WW
oooo
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oooo
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6*
17.0
9.Z
10.2
11.0
1370-
I .0
AfAATIW TAUC 501101 HKttl I FMH M
*NM4f J0M IK. «MiU JH. UTIMV AW
NA1TE SLUDOC
" 0*0*6" li.4 ' 4414 ' 1T44 14. » OU*4 Oil** 01.0
94911 «).0 49*2 3*OB 13.1 077Z0 04460 11. T
' Still 14.1 *T*4 4414 ll.4 0*111 OUT*"" 14.4
0739* 13.0 4920 4110 «).0 04776 01284 04.7
oioti fti.f 9til 4Ul I4l4 044U 0(1 U M.I
07010 14.4 4*60 41*4 13.5 09770 0(172 fll.7
00*91 84.2 4796 1040 10.9 11004 09320 04.0
- 6*76* W.I ~4400 IMC"1' 14.0 11104 0«« H.I
09011 01.9 4411 3120 !*.* 1099* 04008 83.1
fiUW—1 Illl— - ««— ' IT4I ill* Holt 0*441 IT. 4
0*160 B6.4 4304 9740 17.) 10734 09420 87.7
60J94 84.4 4414 1146 IT.O 10904 A»U If.*
few '11.4 '4oU IMF If.6 • 10904 •' 6«lfll 11.4
&il» U.8 4sU • ma (»;!" ' 11044 omo H.T
09900 16.7 4412 30*1 10.2 I152B fl'*46 «• T
Mil 14.4 4141 1906 I*. J bUll 01111 11.1
0412* 14. * 4070 339* 17.4 04531 0116* 87.7
o*»U ii.l 1411 35)1 11.6 OU4B 01410 IT.l
0*420 19.0 3461 1114 14*8 11904 09*20 B*!s
64TT1 16.0 4111 1114 II.* 1UH 16101 16.6
099 J 2 04.0 4300 3988 B3. OITZO 074BO 09 .0
OWIZ B4.7 19411 )4M SI U11Z O43*B 04.4
oMlfl 1S.1 44!1 SITi IT — 18711 TJUV8 M.B
09412 09.3 3076 3140 B6 1107* 04537 84.1
2*411 J 130940 112480 306042 2*4512
101 1* B0.2 975* 4*04 || 11*76 10100 81.4
0 *Ai HAS 101. t.*STED f.C.
»CT ACT »/0 ACT CRAMS / OAV TIS LOAD
003*14 4444 1.J4 >o.S BflMJ4 OOOI«~ -J4.4 '
99MSJ 1nif }l" ">-0 000410 000341 21.9
J9iy? !11° *!* *3'S <»>9'« 000502 23.5
p03«9 19*] *fJ2 90% 000*61 000874 tl'.l
004H4 iM .49 J6.) flOOSOS 0081*1- 11.5"
004792 2914 .93 96. 0 000629 000310 24.9
0046*4 Hi4 .94 Io*.fl MUTT OUlOOt l!.l
J0434I 2JJ4. .38 «4.« 000*94 OOOB52 21.3
004341 ?30* ;$} ti5.fr 661 it 6 661141 14.1
004 1J7 2246 .34 US.* 001220 001070 19.3
00i*l4 int. .)4 11S.4 Collii o616*l 10.'
004142 2016 .4* *4.4 000*72 000982 19.3
AD413* Mil .31 4S.4 000444 066441 IT. ft
— *»B — Btt — ^H — ti:: BBB B»B — $3
99397* >J72 .8 90.4 OOU34 000984 17.8
0040 Z7 tlli" ".4? 104.1 BOTOT! HRWr! TttH
0038*9 172B . ) 102.2 00097) 000099 16.0
004067 201* . a Ai.l 000711 . 00040* 13.3
064*19 SoU . 1 U.t 6^6441 A603B4 11. a
0049«8 11*0 . » ,*.i 00039t OOO3S9 l*-4
004603 20*4 . 2 64.4 006T3± 000691 1». 1
004909 20T4 . 6 96.0 000499 000413 19.9
004614 2074 .44 ' *6.6 000402 660914 19.3
0046B3 >?18 47 60.* 00067) 000977 19.1
io44oi JHe lie -T!lT -ftoollT OooTol }6.T
y*****ty«**«»«**iT*w»Tna***t**^»yi*TTrm*w'*^r«tniO»*i*****»T»
113)43 07IOB4 17.91 1271.4 023194 020194 600.1
004998 44*4 U14 113^6 001240 001101 29.Q
MufKitht 6*1* Hueis' - 0 • - raw
N 1 7 M 0 e E N
"t»3 - H H03 - N
is nt HI nr f t-lb HT
.6
10.0 11. 8 i.|
I.I
17.0 10,2 .7
21.0 10.0 ., .9
20.1 4.* 1.4
1.4
19.3 .2.3 .4
ooooo JT.^ ran ^B m rzr —
10.0 22.0 . 1.7 2.2
oictutR sutttMAUtat • i rr~ —
S*
04
OS
jf
»?
\i
i?
24
2B
10
TOTAL
MAX
04
0*
!9
t*
14
tf-
— K-
20
2*
24
?8
*
134
lit
H*
ize
w.
112
f"
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112
1T2
83t
09*
041
016
004
Oil
018
-^
Oil
037
064
044
090
VWT
«-r
90.0
63.0
73.9
94.4
B3.4
79.0
77.*
72.3
«•?
J7.3
40.7
47.7
• — —K-fji'S'ii'fS* »**"***"***'« *'W*lt**~i'f*SJ
HAX
il ' ' 04
01
62
w
66
•
09
11
1!
11
19
tb
19
21
21
19
24
27
— H-
— - — nmrc
AVG
HIN
66134
240
69
PI
.1
,
.3
.9
.,
*.J
.4
,1
TWIT
090
OS
DODO
T1.4
94.4
T K 0
PfF
4.7
4.J
1.0
S.I
5.2
IT?
»!T
3.2
4/0 »** « 10 JO 30 JUN SlUOSf FC BOP
0983 MU 6oH* £[ .14 .1!
0990 0960 002 10 32 .26 . 32
C*BO 0960 00221 32 .26 23
0990 0440 00212 « .'« |?
«« ««0 0"» " -23 20
0*90 0460 00218 27 .23 19
00 . 12 24
0960 0890 01)243 00 .31 31
0990 0840 00234 00 .30 26
0980 0490 00221 00 .24 29
09*0 0410 002 36 IB .27 24
09*0 0910 00240 52 .27 30
29)70 74240 05)94 1094 7.73 7 80
m »i7 ».<
n m — nn SFT — nra — 44.4 " — — — .
000 075 68. B 491 093 89.
112 03) 6».« 3J9 080 B3.
040 060 liS 07« 79, 289 02§ 90.2 29S
459 093 79.
112 074 91.3 400 069 83. 7.6
06114 00016 6B.4 OC4«) 6oW~1Kl Ofll»C"~'OOg7 9tt T7J StSTn 7m
160 074 85.0 630 112 9). 424 016 93.9 7.T 31)
CEIL 10 PEF BOD N.P.
3.4 3.4 3.9 1.1
4.1 6.5 3.Z 1.1
9.6 2.3
4.Z - *.l - — ' 1.! .9
4.2 3.4 4.7 1.1
9.3 2.2
2.8 2.) 5.5 1.1
4.1 4.0 5.0 1.0
*-2 2.0
1.8 1.) 6.1 1.3
10.2 1.5
l.B 3.6 .0 9.6 2.1 bio l'.0
1.2 1.5 9.2 1.5 1.5 .6
-------
or
04
DAY DATE
01
03
06
2R_
17
19
21
23
29
is-
10
r*rm*m
TLTftL
H*
04
• -"i.AV DAN
01
01
OS
07
It
iT-
16
17
FT
it
69
1SS
1446*
16170—
it:;;
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11484
1CT64 "'
-HHJ-
AERttlON
SEC.
P/WT
79.4
«o-o
DOT*. 12190 BO. •
11720 11012 BO. 4
I*2O0
16044
16980
606H
14644
17252
16312
19)88—
1723*
1739*
"1HI4"
69
ffiC
0000
0000
0000
oft on
0060
000-0
0660
0000
0666
0000
0000
OQOO--
oood
B6W-
}
4500 81. B
482B (La
:ta u::
— :m— a*
1716 82. i
4004 82.9
4024 11.4
4120 81 !*
4B78 62.?
4412- 04to
4140 81.6
47T6 85.2
4240 84. a
5420 84.9
— us-— m
1720 82.'
110996
5948 89.1
C
REfiJRN
WASTE S
16440
it 912
— HW-
— ms-
172*4
16672
12828
20624
16924
— 1»««
iflw
r>9'44
21060
20900
21824
— Hrfr
1*376
10496
ilftlkltTii
521046
v5i
1*684
13)00
14728
13920
I056a
1 72 96
14268
1)722
OSSS
H424-
— rsTft
16484
{9*04
17464
10228
14896
14040
-4$J
15192
of 69 ' AtkAflON |AM sOilM «M(Si C. PbAH bl
L/D TSS PE 10 30 )0 N1N SLUDGE TC BOO
01 11*52 96. 001124 2 5 0950 0870 00158 42 26 10
BO 9 04 15)96 82. 001261 2 S 0960 0860 00191 41 ?3 25
fll.2 06 15)56 90. 001)93 S 41 26 27
3ltl ^07 tS320 BS45 ?2*6 967 — 661613 It 6W3 UTR 5UTW « Zfl H
• ,['Z — — 55 [57J5 5555 «TT5 ^75 661019 " — T~J 5?55 — "' 6718 tfofil ft6 !T !i '
Ofllr 10 10724 B). OOCB95 1 0960 0750 00152 00 |9 36
82.4 12 1166 6B40 7141 99. 001100 Z 0050 0500 0009B 00 26 25
a) i 14 U6« 85, OOC992 1 C990 0950 00141 15 26 27
•i ft i& i!*9 56. COC1I4 1 0960 0900 00159 00 26 73
.4.6 18 0857 9296 1969 97. C00494 0980 0910 001*3 00 76 21
84.4 22 09944 60. 000577 1 0960 0900 001B) 00 27 27
84.9 24 06148 4516 1770 94. OOC33* 0810 0900 00122 10 26 23
84.2 26 06148 46.1 00028) 0980 0840 OO2O9 )3 27 28
84.7 28 0808a T9.2 000b41 0980 0940 00100 24 12 29
«To J9 oTOIi OTB KTCTW B DWD «5B TOT*! K JI !Z
82.1 TOTAL 320076 062456 21311 2250.7 025T69 91 Z4700 21460 04001 0511 T 96 • 09
4)))00 MAI 16 a 20 8640 21TO 96. S OOUI3 4 Q990 0970 002O9 49 32 3*
21624 2022(
C
ACT
L/6
00)))*
0341?
00)683
04
1.3
2.2
1.9
2.3
TSS tOAO P/CNT P/CNT P/CNT P/CNT UNITS S'
19.1 02 132 040 69.7 100 024 76. C 620 074 88.1
19.6 04 136 066 51.) 128 056 56.3 523 098 81.3
19.) 06 116 032 72.4 112 538 036 93.3 316
20.8 08 1)6 040 70.6 1)6 380 058 84.7
21.5 10 112 022 H0.4 570 0)8 93.3 398 037 92.0
21.9 12 12B OZ6 79.7 11* 02) 80.2 482 048 90.0 318
27. 7 14 152 O19 74.1 1O9 078 74.1 907 060 88.2 7.7
«•« 16 140 026 «1.4 108 01? 82.4 470 03B 91.0
21.4 IB 140 038 72.9 09* 027 71.9 400 032 92.0 298
19. B 20 11J 044 *0.7 OBO 0?9 63.8 49) 032 91.5
18.) 22 124 094 24.2 112 084 25.0 5)9 108 /9.8
19. 3 24 088 244 040 385 120 68.8 285 046 83.9 261
16.4 26 112 142 110 459 138 69.9
77.9 za 172 094 45.) 152 076 50. C 4DB 089 78.? 7.0
20. 7 30 168 056 66.7 178 018 70.3 905 054 89.1 252
678.9 TOTAL 04024 01779 02844 00958 14793 2123 01*>200I13 37.5 O2629
27.7 MAX 240 244/ 05.6 160 110 82.8 630 152 93.5 424 046 96.6 7.7 312
N 0 ft T H 0 CELL 10 PEF BOD N.P.
PE DS PtF PI PE W N P N P
01 ^
« L. 227 7.4 3.4 3.9 * ' 6.4 1.4
04
06 .1 341 0.7 1.2 1. 6.2 1.6
09 .9 323 7.5 4.1 6.5 6.1 1.7
.* 14
15 .5 127 3.) 4.2 3.4 5.4 .8
1.4 17 8.8 2.0
19
?1 .5 1)1 2.6 4.1 4.0 *.7 .1
.9 Z) 8.4 1,4
75
l.t 26
27 .3 092 1.5 3.8 1.5 %."i .4
.9 J9 9.2 1.4
rly — rcTAi *n T6T9 -*r.i 7— — WTT IS.T - . • U.T 9.2 SJ.T a.r
2.4> *«, .'6 0168 4.1 .3 3.8 3.6 .0 73. T 8.7 1.8 5.4 .9
HIM .1 0*1 1.2 .1 1.2 1.5 8.9 a. 4 1.4 t.J .3
-------
f\J
04
U*Y L)*U
U
Oi
' M
10
ll
H_
J*
is
it
i"
X
K-
24
26
*°
mm
01
04
08
10
ll_
H-
?0
H-
24
16
I*
10TJL
02
0*
06
08
12
1*
15
is
18
2C
2?
23
2*
24
26
2f
28
10
TOIiL
A VI.
MAX
"
»5S
12992
'$816
HlSi
1)192
fills
14* 9ft
12592
12800
11616
[3040
1161*
15508
11000
114*8
tUKAf |6*
vi5
1614*
10900
10*88
Ill80
10*71
jmo
10792
10*68
09*76
10792
1 111
-4K«-
10764
0992*
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-------
APPENDIX C
QUANTITY AND CHARACTERISTICS
OF
MUNICIPAL AND PULP MILL
EFFLUENTS
345
-------
QUANTITY AND CHARACTERISTICS OF
MUNICIPAL AND PULP MILL WASTES
The proposed quantities of flow from these five major sources were
revised several times during the project. A schedule of the flows used
to proportionately composite the five wastes for use in the laboratory
reactors and the pilot plants is presented on page 347.
The characteristics of the Mill and Metro wastes are presented on page
349; the following facts apply to this Table:
1. Between June, 1967 and February, 1968 mill waste grab
samples were delivered to the GBMSD laboratories in small
containers.
2. Between February 16, 1968, when the first tank-trailer load of
waste was received, and April 16, 1968, the samples used for
laboratory analyses were obtained directly from the tank-trailer.
After April 16, 1968, all samples of mill wastes were taken
from the respective storage tanks after they were filled. This
change in sampling procedure was made to obtain the characteris-
tics of the mixture of old and fresh wastes in each of the storage
tanks actually being fed to the pilot plants rather than the
individual characteristics of each mill waste as it was delivered
to the pilot plant site.
3. Data on Mill 1 waste characteristics are restricted to the
periods of June 8, 1967 through February 15, 1968 and
September 3, 1968 through August 22, 1969; mill waste loads
obtained outside these time intervals were not representative
due to inadequate mixing of mill storage tank contents prior to
discharge into the tank-trailer.
4. The limited number of ammonia, nitrate, ortho phosphorus and
total phosphorus analyses presented were obtained between
June 16, 1969 and August 12, 1969, with the exception of Mill 2
ammonia analyses and Metro total phosphorus analyses which
were obtained uniformly between the dates showin in the Table.
5. The Metropolitan waste characteristics are taken from the
monthly data sheets maintained by the GBMSD.
Information on the temperature of the wastes is presented on page 351.
346
-------
HYDRAULIC FLOWS UTILIZED IN STUDIES, MGD
Date
June 1, 1967
February 6, 1968
February 24, 1969
March 26, 1969
June 23, 1969
August 13, 1969
Sept. 16, 1969
October 20, 1969
Dec. 15, 1969
Mill
1
4.0
4.0
5.0
5.0
5.0
5.0
5.0
5.0
5. 0
2
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
3
7. 0
7.0
10. 5
10.5
10.5
10.5
13.25
13.25
13.25
4
3. 0
2.25
2.3
2.5
0.6
0.6
0.6
0.6
0.6
Metro
20. 0
20.0
23. 5
23.5
23.5
30.0
30.0
23. 5
23. 5
Total
39. 00
38.25
46.30
46. 50
44.60
51. 10
53.85
47.35
47.35
OJ
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
TEMPERATURES OF MILL AND METRO WASTES
Source
Mill 1
Mill 2
Mill 3
Mill 4
Metro
1965
1966
1967
1968
1969
Temperature
Summer
120
116-122
July
High 1 1 3
Low 102
Avg. 107
140
Max. 76
(August)
Max. 78
(Sept.)
Max. 76
(Sept.)
Max. 78
(August)
Max. 78
(August)
, °F
Winter
80
85-95
January
High 96
Low 79
Avg. 90
140
Min. 45
(March)
Min. 45
(Feb.)
Min. 47
(March)
Min. 47
(January)
Min. 50
(January)
Remarks
Estimated values based on limited measurements.
Estimated values based on limited measurements.
Temperature changes would be gradual.
Measured values. Hourly variations small due to
equalization effect of lagoons . Daily variation of
5° in summer and 15° in winter could be expected.
Temperature is controlled to a constant value.
These are trickling filter effluent values. Studies
made prior to this project indicate that the
primary influent temperature averages approxi-
mate^ 3° higher than the trickling filter effluent
temperature.
-------
MINERAL ANALYSES OF MILL, AND METRO WASTES
Source
Mill 1
Mill 2
Mill 3
Mill 4
Metro
Percent by Weight
P
<0.0013
<0.0013
<0.0013
<0.0013
<0.0013
K
-CO. 0050
<0.0050
<0.0050
<0.0050
<0.0050
Ca
0.0240
0.0075
0.0130
0.0047
0.0047
Mg
0.0018
0.0016
<0.0005
0.0009
0.0018
Na
0.0009
0.0014
0.0230
0.04ZO
0.0140
Mg/1 as
Al
1;40
0.77
23.00
5.80
1.30
Element
Ba
<10.10
<0.10
<0.10
0.21
<0.10
Source
Mill 1
Mill 2
Mill 3
Mill 4
Metro
Fe
2.
0.
1.
3.
1.
5
5
1
3
8
Sr
0
0
0
0
0
.36
.36
.36
.36
.67
Mg/1
B
<0.05
<0.05
0.48
0.08
0.19
as Element
Cu
<0.05
-------
Grab samples of the five wastes (the mill samples were taken from the
storage tanks) were analyzed for mineral content in August, 1969- The
results of these tests are presented on page 352. The values shown
must be considered only as indicative of the range expected for the given
parameter as they are based on one sample.
Miscellaneous analyses conducted on single grab samples are presented
as follows. These values must also be considered only as indicative
of the range expected for the given parameter as they are based on one
sample.
MISCELLANEOUS ANALYSES ON MILL AND METRO WASTES
Date
Source
Mill 1
Mill 2
Mill 3
Mill 4
Metro
6/8/67
Total
Organic
Nitrogen
mg/1 as N
3.0
5.4
11.6
9.9
6/8/67
Volatile
Acids
mg/1 as acetic
759
157
169
381
PH
3.7
6.0
9.7
6.7
7.0
8/28/69
Methyl
Orange
Alkalinity
mgAas CaCO3
0
200
400
720
248
Chloride
mgA as Cl
105
87
247
40
274
9/24/69
Sulfate
mg/1 as SO^.
2645
2048
377
53
596
353
-------
APPENDIX D
EXPERIMENTAL DATA
355
-------
PILOT PLANT LABORATORY DATA - PHASE IV
The following comments apppy to the laboratory data sheets:
1. The data are presented in the vertical order of average value,
maximum value, minimum value.
2. All total and volatile suspended solids are expressed as mg/1.
3. The final clarifier sludge level is expressed in inches.
4. The cellular nitrogen and phosphorus values are expressed as
percent by weight.
5. The settled sludge volume is expressed in milliliters.
6. All nitrogen analyses are reported in mg/1 as N.
7. All phosphorus analyses are reported in mg/1 as P.
8. PEF = primary effluent fortified; this is the primary effluent
after nutrient addition.
9. BOD is reported as mg/1.
356
-------
GBMSD Industrial-Municipal Research Project
Primary Clarifier
Month
Aug.
Sept.
Oct.
Nov.
Dec.
w
in
Year
69
69
69
69
69
Primary Influent Flow
Liters/Day
Mills
1
1917
1933
1450
1263
1266
1200
1440
1843
1200
1843
1843
1843
1805
1843
1267
2
1797
1933
0
1263
1266
1200
1440
1843
1200
1843
1843
1843
1597
1843
0
3
4025
4058
3043
2682
3180
2658
3770
4896
3180
4896
4896
4896
4794
4896
3366
4
229
231
173
152
152
144
173
223
144
223
223
223
218
223
153
MSD
8718
11555
5452
8367
10912
6392
8163
11109
5257
7138
10193
2233
5188
7714
3602
Total
16687
19710
11568
13727
16254
11734
14987
19914
11515
15943
18998
11038
13602
14676
10981
Influent
pH
6.7
7.1
6.4
6.8
7.1
6.5
6.8
7.0
6.4
6.8
7.1
5.2
6.7
6.9
6.4
me/1
TSS
220
232
148
206
352
100
192
492
112
253
372
124
250
404
104
VSS
192
264
124
169
312
84
151
372
104
192
284
88
189
312
88
BOD
481
600
323
434
565
295
457
600
325
480
612
346
540
670
340
Effluent
pH
6.6
7.1
6.4
6.8
7.0
6.5
6.8
7.0
6.4
6.7
7.1
6.5
6.7
7.1
6.3
mg/1
TSS
160
220
96
126
200
56
124
192
72
1-51
224
92
203
588
100
VSS
142
200
104
104
180
40
100
152
52
114
160
60
156
432
76
Red.
TSS
27.3
46.4
0
38.8
68.2
8.0
35.4
61.0
0
40.3
66.7
11.8
18.8
50.8
0
mg/1
BOD
457
548
330
401
510
285
434
550
340
466
629
300
492
600
326
Red.
BOD
5.0
15.7
0
7.6
27.3
0
5.0
20.7
0
2.9
27.4
0
8.9
18.8
0
mg/1
COD
1023
1374
672
830
1168
566
813
1187
605
1029
1225
790
1229
1568
908
TC
513
590
425
485
560
410
455
560
390
476
870
300
499
570
400
BOD
TC
.89
1.07
.62
.83
1.07
.62
.96
1.28
.67
1.01
1.94
.68
.97
1.18
.80
Color
Units
256
332
54
256
332
175
243
342
163
248
337
170
276
373
220
-------
in
00
GBMSD Industrial-Municipal Research Project
Process A
Month
8
9
10
11
12
IH
nt
«)
><
69
69
69
69
69
ReaerationSec.
Contact Sec.
Return and
Waste Sludge
mg/1
TSS
12475
16452
9836
12338
15000
9972
13024
15940
9740
15585
20048
11912
15635
18516
14124
VSS
10921
14612
8528
10983
13376
8900
11543
14364
8656
12871
16384
9772
13104
15484
11744
%
87.5
89.1
85.3
89.0
91.7
86.3
88.6
91.7
86.2
82.6
87.1
79.1
83.8
85.6
81.3
TSS
4293
4888
3472
3750
4280
2756
4083
4920
3028
4451
5680
3616
4203
5180
3204
VSS
3776
4252
3164
3370
3848
2488
3662
4500
2784
3718
4764
3012
3542
4312
2728
%
88.0
91.3
85.2
89.9
94.6
84.0
89.7
94.1
86.6
83.5
87.9
80.4
84.3
86.6
82,0
TSS
12764
16012
9740
13228
15544
10396
13874
17068
10776
16456
19440
13692
15357
16920
12788
VSS
11191
14116
8384
11823
13996
9236
12354
15288
9492
13650
16076
11232
12902
14076
10664
<7o
87.7
89.1
85.5
89.4
90.8
87.7
89.0
91.5
85.9
82.9
85.7
79.4
84.0
85.8
77.0
Digester Supernatant
mg/1
TSS
VSS
BOD
L/D
added
grains
TSS
added
DS-TSS
PE-TSS
Set SI.
Volume
10
Min.
924
980
640
794
980
400
348
520
210
375
465
270
379
570
260
30
Min.
736
930
360
587
930
300
264
375
170
281
350
200
282
380
200
30
Min.
SVI
173
234
85
155
252
75
64
87
47
64
75
53
66
84
55
Clar.
sludge
level
0
6
0
0
0
0
0
0
0
0
0
0
0
0
0
F/M Ratio
TC
VSS
.34
.45
.25
.37
.43
.26
.32
.43
.23
.28
.44
.17
.25
.28
.16
BOD
VSS
.31
.38
.20
.28
.40
.14
.25
.38
.09
.27
.37
.16
.24
.32
.13
-------
GBMSD Industrial-Municipal Research Project
Process B
Month
8
9
10
11
12
UJ
NO
rt
4)
I*
69
69
69
69
69
Reaeration Sec.
Contact Sec.
Return and
Waste Sludge
mg/1
TSS
9290
11708
6900
10584
13356
6452
13718
15348
11076
13967
16332
11804
14569
17140
12740
VSS
8108
10004
6156
9193
11604
5744
12006
13636
9728
12087
14112
10248
12125
14096
10704
%
87.3
89.2
84.6
86.9
89.8
.4
.5
.8
.4
.5
.5
.1
.2
.4
.1
TSS
4065
5012
2980
4178
4824
3192
4235
5248
3644
4161
4840
3536
4295
4904
3616
VSS
3547
4300
2592
3647
4224
2848
3728
4696
3200
3619
4312
3040
3603
4040
3048
%
87.3
90.8
84.1
87.3
91.1
82.5
88.0
91.3
80.3
87.0
90.0
82.8
83.9
85.5
82.4
TSS
9648
11764
7770
11568
13888
7592
14578
16456
11344
15240
18868
9332
16344
18900
13100
VSS
8455
9968
6822
10079
12072
6604
12801
14492
10080
13079
15984
7964
13676
16528
11012
%
87.6
89.4
84.7
87.1
88.6
86.0
87.8
93.5
86.0
86.0
88.3
83.5
83.7
87.4
82.4
Digester Supernatant
mg/1
TSS
X
VSS
BOD
L/D
added
grams
TSS
added
DS-TSS
PE-TSS
Set SI.
Volume
10
Min.
891
995
230
646
950
260
322
460
220
396
750
225
781
940
400
30
Min.
790
990
180
426
800
200
240
340
170
282
505
170
605
840
300
30
Min.
SVI
190
247
60
101
189
63
57
75
40
68
104
47
140
193
69
Clar.
sludge
level
12
56
0
0
0
0
0
0
0
0
0
0
0
0
0
F/M Ratio
TC
VSS
.38
.62
.20
.40
.71
.26
.31
.40
.24
.29
.47
.18
.26
.31
. 17
BOD
VSS
.34
.57
.16
.34
.52
.22
.29
.39
.23
.28
.38
.18
.25
.34
.14
-------
GBMSD Industrial-Municipal Research Project
Process C
1 Month
8
9
10
11
12
LI
Rt
0)
>H
69
69
69
69
69
ReaerationSec.
Contact Sec.
Return and
Waste Sludge
mg/1
TSS
11765
16132
8436
11391
14188
9040
12890
16588
10044
14144
15932
1185?
14233
15948
11156
VSS
10384
14040
7628
10113
13088
8144
11006
13836
8544
11852
13708
9872
12107
14932
9312
%
88.3
90.6
86.4
88.8
92.2
84.8
85.4
88.3
76.1
83.8
87.1
78.7
85.1
94.7
83.0
TSS
4243
5288
1996
4055
6080
2044
4455
5628
1296
4307
5640
1684
4280
4796
3336
VSS
3763
4668
1792
3583
4736
1800
3906
5112
1244
3620
4796
1408
3608
4108
2768
%
88.7
91.3
85.4
88.4
92.1
77.9
87.7
96.7
84.4
84.0
88.2
75.9
84.3
85.7
82.9
TSS
12293
16488
9636
12724
19208
10356
15312
21128
10520
14869
19324
9060
14317
15912
11584
VSS
10896
14448
8620
11309
16992
9148
13193
18424
9056
12545
16184
7544
12095
13264
9752
%
88.6
90.4
86.6
88.9
98.9
86.6
86.2
88.0
83.4
84.4
86.8
81.7
84.5
85.4
83.4
Digester Supernatant
mg/1
TSS
VSS
BOD
L/D
added
grams
TSS
added
DS-TSS
PE-TSS
Set SI.
Volume
10
Min.
948
995
440
878
985
300
844
980
300
532
955
300
783
960
360
30
Min.
908
975
310
789
970
230
712
960
230
381
880
220
605
850
270
30
Min.
SVI
218
298
103
194
260
89
164
340
69
91
249
53
140
191
74
Clar.
sludge
level
49
68
23
8
43
0
0
0
0
0
0
0
0
0
0
F/M Ratio
TC
VSS
.36
.54
.23
.38
.50
.29
.32
.43
.23
.29
.46
.19
.26
.35
.20
BOD
VSS
.32
.51
.18
.32
.52
.20
.31
.44
.23
.29
.40
.18
.26
.38
.16
-------
GBMSD Industrial-Municipal Research Project
Process D
Month 1
8
9
10
11
12
w
O1-
LI
nt
V
>
69
69
69
69
69
ReaerationSec.
Contact Sec.
Return, and
Waste Sludge
mg/1
TSS
9880
12468
6784
9939
13440
6376
12343
14240
9532
13807
16688
11488
13202
14864
11932
VSS
8690
10904
6228
8315
11892
5580
10747
12508
8484
11489
14296
9692
10971
12284
9912
%
88.0
91.8
81.9
89.0
91.7
86.9
87.1
91.7
83.4
83.2
)1.5
79.4
83.1
85.1
82.1
TSS
4056
5180
2692
3756
4496
2668
4218
5456
3728
4444
5384
3760
4356
5100
3296
VSS
3596
4580
2468
3355
3980
2428
3718
4832
3188
3716
4420
3132
3647
4236
2756
%
88.7
94.9
81.0
89.3
94.6
80.9
88.1
96.8
83.4
83.6
89.4
79.4
83.7
85.9
80.7
TSS
10773
13204
6676
10180
14152
6860
13242
15260
10428
14630
17444
9416
13176
16588
7664
VSS
9529
11868
6136
9110
12672
6116
11540
13248
9268
12205
14428
7624
11077
13936
6460
%
88.5
93.7
85.7
89.5
95.6
85.9
87.1
92.6
84.7
83.4
94.1
81.0
84.1
88.5
82.3
Digester Supernatant
mg/1
TSS
VSS
BOD
L/D
added
grams
TSS
added
DS-TSS
PE-TSS
Set SI.
Volume
10
Min.
962
990
880
756
980
260
468
930
230
530
920
350
398
600
190
30
Min.
898
965
750
593
920
200
357
810
180
351
490
260
278
350
140
30
Min.
SVI
224
306
182
160
261
54
84
188
44
79
100
63
63
78
42
Clar.
sludge
level
14
69
0
1
10
0
0
0
0
0
0
0
0
0
0
F/M Ratio
TC
VSS
.35
.67
.17
.44
.60
.31
.33
.42
.24
.30
.54
.17
.27
.32
.18
BOD
VSS
.32
.54
.13
.36
.53
.23
.32
.46
.23
.29
.41
.17
.27
.34
.15
-------
GBMSD Industrial-Municipal Research Project
Process A
1 Month
8
9
10
11
12
M
n)
V
!H
69
69
69
69
69
Supplemental Ope rat in
Feed
bypass
L/D
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Q
L/D
4216
4928
3501
4642
5701
3806
6311
11989
3516
3986
4750
2760
3401
3669
2745
RAS
L/D
1632
2448
950
1325
1507
1066
1861
2549
1152
1195
1444
1037
1117
1212
1049
R/Q
Ratio
.39
.66
,.22
.29
.38
.22
.31
.41
.19
.30
.42
.26
.33
.43
.29
WAS
L/D
61.2
102.2
0
45.8
121.1
0
41.2
147.6
0
70.4
166.6
15.1
78.5
117.3
34.1
r Data
Sol. Wasted
grains /day
TSS
785
1293
0
623
1649
0
609
2519
0
1146
2712
294
1215
1699
436
vss
688
1151
0
556
1453
0
543
2257
0
949
2222
240
1025
1458
364
F.C.
TSS
load
#/sf/d
17.7
21.7
12.1
15.7
19.8
10.5
23.5
42.2
13.5
16.2
21.5
10.9
13.3
16.5
10.7
Final Effluent
mg/1
Total
Sus. Solids
PE
160
220
96
138
232
62
128
372
50
151
224
92
203
588
100
FK
39
114
4
64
144
24
59
138
19
81
160
24
71
112
32
%red
75.6
97.6
44.1
53.6
86.5
0
53.9
82.3
0
46.4
83.8
0
65.0
85.0
37.1
Volatile
Sus. Solids
PE
142
200
104
122
212
66
106
308
48
114
160
60
156
432
76
FE
35
96
21
53
110
22
50
106
14
58
156
20
50
84
16
%red
75.4
86.7
42.9
56.6
84.7
0
52.8
79.7
0
49.1
75.0
0
67.9
83.3
32.7
Unfiltered
BOD
PE
457
548
330
369
518
213
362
530
150
466
629
300
492
600
326
VE
31
51
10
62
225
10
58
143
30
45
75
18
68
153
34
%red
93.2
97.4
90.2
83.2
95.3
34.8
84.0
93.2
56.1
90.3
95.3
84.4
86.2
92.3
74.5
Filtered
BOD
PE
352
413
308
308
368
278
290
417
158
427
476
409
484
484
484
FE
15
25
10
29
41
16
18
23
14
24
29
17
%red
95.7
96.9
93.9
90.6
94.4
86.3
93.8
95.3
89.9
94.4
95.9
92.9
PH
7.6
7.7
7.5
7.6
7.7
7.2
7.6
7.7
7.5
7.4
7.5
7.2
7.5
7.6
7.4
Color
Uijiits
FE
225
396
40
216
232
130
190
275
113
238
340
170
262
305
180
-------
GBMSD Industrial-Municipal Research Project
Process B
Supplemental Operating Data
1 Month
8
9
10
11
12
ri
(U
69
69
69
69
69
10
10
Feed
bypass
L/D
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Q
L/D
4203
4928
3501
4576
5418
3911
4476
5713
3516
3986
4750
2760
3401
3669
2745
RAS
L/D
2486
3197
1872
2028
3099
1537
1379
1495
1276
1230
1385
1094
1152
1213
1082
R/Q
Ratio
.59
.85
.42
.44
.62
.32
.31
.39
.23
.31
.46
.25
.34
.39
.29
WAS
L/D
41.6
121.1
0
20.2
128.7
0
52.0
128.7
0
63.1
140.1
7.6
64.5
140.1
24.6
Sol. Wasted
grams/day
TSS
409
1356
0
249
1638
0
763
2090
0
963
2304
121
1048
2027
427
VSS
359
1170
0
216
1419
0
670
1844
0
826
1924
104
875
1679
357
F.C.
TSS
load
#/sf/d
19.1
25.6
13.5
19.3
22.9
15.2
17.4
22.0
13.3
15.2
18.4
10.4
13.7
15.7
11.3
Final Effluent
mg/1
Total
Sus. Solids
PE
160
220
96
126
200
56
124
192
72
151
224
92
203
538
100
FE
74
134
13
31
80
11
37
102
13
44
94
8
101
376
18
%red
53.8
90.4
25.8
75.4
91.7
31.0
70.2
87.0
31.1
70.9
91.3
24.0
50.2
86.4
0
Volatile
Sus. Solids
PE
142
200
104
104
180
40
100
152
52
114
160
60
156
432
76
FE
63
114
7
26
•46
8
30
65
10
31
78
2
70
182
6
%red
55.6
94.2
28.8
75.0
93.3
42.5
70.0
89.1
32.3
72.8
96.9
45.0
55.1
94.4
0
Unfiltered
BOD
PE
457
548
330
401
510
285
434
550
340
466
629
300
492
600
326
FE
47
82
11
35
62
19
42
69
14
41
66
10
88
174
30
%red
89.7
96.7
81.0
91.3
94.5
85.4
90.3
96.4
82.1
91.2
97.3
81.7
82.1
93.3
71.0
Filtered
BOD
PE
352
413
308
352
432
304
344
417
248
427
476
409
484
484
484
FE
15
23
10
16
22
10
16
20
12
17
20
11
%red
95.7
97.2
94.4
95.5
97.0
92.8
95.3
96.6
91.9
96.0
97.3
95.6
PH
7.6
7.8
7.5
7.7
7.8
7.4
7.8
7.9
7.7
7.7
7.8
7.5
7.7
7.8
7.6
Color
Units
FE
210
318
43
197
293
153
191
232
175
215
230
138
212
275
153
-------
w
GBMSD Industrial-Municipal Research Project
Process C
Supplemental Operatin
1 Month
8
9
10
11
12
ti
(4
V
{H
69
69
69
69
69
Feed
bypass
L/D
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Q
L/D
4Z03
4928
3501
4576
5418
3911
4476
5713
3516
3986
4750
2760
3401
3669
2745
RAS
L/D
2100
2724
1267
1792
2196
1330
1550
1805
1252
1160
1556
998
1084
1220
997
R/Q
Ratio
.50
.66
.27
.39
.50
.25
.35
.46
.27
.30
.41
.23
.32
.39
.30
WAS
L/D
74.5
212.0
0
49.6
196.8
3.8
52.5
132.5
0
64.7
143.8
0
60.4
106.0
7.6
I Data
Sol. Wasted
grams /day
TSS
899
2400
0
619
2528
45
844
2578
0
939
2108
0
876
1445
93
VSS
797
2145
0
551
2254
40
729
2258
0
790
1772
0
740
1204
79
F.C.
TSS
load
#/sf/d
18.7
24.4
9.5
18.0
26.7
9.7
18.8
25.4
5.1
15.5
20.6
6.6
13.5
15.6
8.9
Final Effluent
mg/1
Total
Sus. Solids
PE
160
220
96
126
200
56
124
192
72
151
224
92
203
588
100
FE
58
168
14
58
144
16
44
112
17
40
88
15
58
144
18
%red
63.8
88.7
12.5
54.0
87.5
0
64.5
85.7
0
73.5
89.9
37.1
71.4
89.5
10.0
Volatile
Sus. Solids
PE
142
200
104
104
180
40
100
152
52
114
160
60
156
432
76
FE
53
148
10
52
128
10
36
92
16
30
60
112
41
126
10
%red
62.7
91.4
20.2
50.0
87.1
0
64.0
85.0
0
73.7
87.5
37.5
73.7
90.7
14.9
Unfiltered
BOD
PF,
457
548
330
401
510
285
434
550
340
466
629
300
492
600
326
FE
39
120
10
46
112
24
48
93
20
36
58
14
51
92
23
%red
91.5
97.4
77.7
88.5
93.3
74.5
88.9
95.4
76.8
92.3
96.6
80.7
89.6
94.8
84.7
Filtered
BOD
PE
352
413
308
352
432
304
344
417
248
427
476
409
484
484
484
FE
20.
28
10
23
31
16
14
19
8
11
13
8
29
29
29
%red
94.3
96.8
92.5
93.5
95.3
90.6
95.9
98.1
92.3
97.4
98.3
96.8
94.0
94.0
94.0
PH
7.7
7.8
7.6
7.7
7.8
7.6
7.7
7.8
7.6
7.7
7.8
7.5
7.7
7.8
7.6
Color
Units
^H«^M«M
FE
208
358
40
219
315
165
204
260
180
221
317
163
262
305
185
-------
GBMSD Industrial-Municipal Research Project
Process D
Supplemental Operatin
1 Month
8
9
10
11
12
n)
o>
69
69
69
69
69
S
Feed
bypass
L/D
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Q
L/D
4203
4928
3501
4576
5418
3911
4476
5713
3516
3986
4750
2760
3401
3669
2745
RAS
L/D
2217
3341
1382
2176
2874
1670
1651
2128
1282
1109
1326
998
1034
1133
945
R/Q
Ratio
.53
.75
.36
.48
.70
.32
.37
.49
.28
.28
.39
.24
.30
.39
.26
WAS
L/D
54.8
166.6
0
19.1
83.3
0
42.9
87.1
0
56.8
136.3
0
66.9
117.3
26.5
; Data
Sol. Wasted
grams/day
TSS
615
2094
0
218
1074
0
573
1297
0
841
2086
0
876
1531
360
VSS
548
1963
0
195
947
0
499
1140
0
700
1704
0
737
1291
297
F.C.
TSS
load
#/sf/d
18.3
24.9
13.2
17.7
21.7
13.1
18.1
23.5
14.3
15.9
18.7
11.1
13.5
16.0
10.2
Final Effluent
mg/1
Total
Sus. Solids
PE
160
220
96
126
200
56
124
192
72
151
224
92
203
588
100
FE
43
101
10
87
236
22
51
144
14
28
54
8
35
88
14
%red
73.1
93.4
48.5
31.0
77.0
0
58.9
88.9
22.9
81.5
93.9
60.3
82.8
95.2
45.0
Volatile
Sus. Solids
PE
142
200
104
104
180
40
100
152
52
114
160
60
156
432
76
FE
39
80
16
74
168
10
44
100
20
20
42
4
26
72
7
%red
72.5
87.5
52.4
28.8
86.1
0
56.0
85.7
26.7
82.5
95.3
64.3
83.3
92.9
51.4
Unfiltered
BOD
PE
457
548
330
401
510
285
434
550
340
466
629
300
492
600
326
FE
41
72
10
70
228
25
45
82
19
31
48
10
21
36
9
%red
91.0
97.4
82.2
82.5
94.0
48.2
89.6
95.1
79.3
93.3
97.3
84.0
95.7
98.2
92.0
Filtered
BOD
PE
352
413
308
352
432
304
344
417
248
427
476
409
484
484
484
FE
21
30
11
31
39
24
15
20
8
12
14
10
9
9
9
%red
94.0
96.9
90.6
91.2
94.4
87.8
95.6
97.8
92.7
97.2
97.7
96.6
98.1
98.1
98.1
PH
7.6
7.7
7.5
7.7
7.8
7.5
7.7
7.8
7.7
7.6
7.7
7.6
7.7
7.8
7.6
Color
Units
FE
201
332
33
217
323
125
206
275
190
218
305
163
251
290
180
-------
GBMSD Industrial-Municipal Research Project
Process A
Nutrient Data
Month
8
9
10
11
12
Year
69
69
69
69
69
NH3 - N
mg/1 as N
PE
16.5
25.6
4.8
22.5
27.3
16.2
15.6
25.5
7.2
30.6
49.3
10.7
12.7
19.3
1.8
PEF
17.7
25.6
4.8
22.5
27.3
16.2
19.3
34.1
7.2
37.2
55.9
16.3
20.7
29.8
8.5
DS
RT
9.0
19.7
2.6
13.7
25.2
1.4
7.9
21.9
.7
25.9
44.3
15.1
20.9
31.8
11.1
NO3 - N
mg/1 as N
C-10
2.0
4.4
.4
1.7
3.7
.1
1.0
4.3
0
2.8
18.7
0
0
0
0
RT
1.5
2.6
.4
1.4
3.7
.1
1.0
4.7
0
1.2
2.5
0
.6
1.8
0
Ortho-P
mg/1 as P
PE
1.7
2.8
.5
4.5
5.3
3.6
1.7
5.0
.6
1.6
3.7
.2
1.5
2.7
.5
PEF
2.4
3.4
1.3
4.7
5.7
4.0
2.0
5.0
.6
1.8
2.4
1.6
4.9
8.3
1.0
DS
PEF
BOD:N:P
BOD=100
N
3.8
5.4
1.5
6.2
11.1
3.6
5.3
8.4
2.8
8.5
14.2
3.5
4.4
6.0
1.9
P
.5
.8
.3
1.3
2.3
.8
.6
1.8
.2
.4
.7
.1
1.0
1.7
.2
Cell 10
Cellular
%N
9.3
11.7
7.7
9.7
10.0
9.4
10.0
13.2
8.7
6.4
9.4
4.4
7.4
8.9
5.9
% P
2.3
2.8
1.9
2.5
2.9
2.2
2.3
3.0
2.1
1.8
2.4
1.4
2.1
2.4
1.7
OO
-------
GBMSD Industrial-Municipal Research Project
Process B
Nutrient Data
Month
8
9
10
11
12
Year
69
69
69
69
69
NH3 - N
mg/1 as N
PE
16.5
25.6
4.8
19.1
23.7
15.3
15.6
18.0
14.4
30.6
49.3
10.7
12.7
19.3
1.8
PEF
17.7
25.6
4.8
23.7
27.6
19.4
23.0
49.9
17.3
37.5
56.8
16.8
20.8
31.3
9.2
DS
RT
5.9
15.0
1.7
2.9
6.8
1.1
4.1
16.2
.7
22.7
28.9
14.4
18.5
36.1
3.4
NO3 - N
mg/1 as N
C-10
1.8
3.3
.7
2.3
5.0
1.1
1.4
4.7
0
3.2
19.1
.4
.5
1.4
0
RT
1.6
2.9
.7
4.3
15.8
0
3.2
12.6
0
3.3
12.9
0
1.2
2.9
0
Ortho-P
mg/1 as P
PE :
1.7
2.8
.5
2.9
3.8
2.2
1.7
2.8
.8
1.6
3.7
.2
1.5
2.7
.5
PEF
2.5
3.4
1.4
3.2
3.8
2.2
1.7
2.8
1.0
1.9
2.8
.5
3.7
6.7
.9
DS
PEF
BOD:N:P
BOD=100
N
3.8
5.4
1.5
5.8
8.1
4.4
5.2
11.7
3.2
8.5
14.0
3.6
4.4
6.7
1.6
P
.5
.8
.3
.8
.9
.7
.4
.5
.3
.4
.7
.1
.8
1.3
.2
Cell 10
Cellular
%N
8.8
9.6
7.1
9.0
9.4
8.7
9.6
12.2
8.3
6.7
9.1
5.2
6.7
8.1
5.2
%P
2.3
2.7
1.8
2.3
2.6
2.2
2.3
2.4
2.2
1.9
2.9
1.3
1.9
2.3
1.4
-------
GBMSD Industrial-Municipal Research Project
Process C
Nutrient Data
Month
8
9
10
11
12
Year
69
69
69
69
69
NH3 - N
mg/1 as N
PE
16.5
25.6
4.8
19.1
23.7
15.3
15.6
18.0
14.4
30.6
49.3
10.7
12.7
19.3
1.8
PEF
19.8
28.0
4.8
23.7
28.2
20.3
22.7
41.4
18.0
39.1
56.0
16.3
20.8
29.4
8.9
DS
RT
12.5
50.4
1.1
21.8
41.7
12.2
7.2
41.7
.4
24.1
27.1
18.3
19.6
29.6
6.4
NO3 - N
mg/1 as N
C-10
1.7
2.2
.3
1.7
3.6
.7
.8
3.6
0
1.2
3.6
0
.4
1.4
0
RT
1.6
3.3
0
1.1
2.6
. 1
1.0
2.9
0
1.1
7.1
0
.6
1.1
0
Ortho-P
mg/1 as P
PE
1.7
2.8
.5
2.9
3.8
2.2
1.7
2.8
.8
1.6
3.7
.2
1.5
2.7
.5
PEF
2.7
3.7
1.4
4.7
6.0
3.5
2.5
4.2
1.7
4.7
7.8
1.6
5.0
9.0
1.1
DS
PEF
BOD:N:P
BOD=100
N
4.3
9.9
1.5
5.8
8.3
4.3
5.2
9.7
3.3
8.9
14.7
3.5
4.4
5.9
2.0
P
.6
.9
.3
1.2
1.7
.7
.6
.8
.4
1.1
1.9
.3
1.0
1.7
.2
Cell 10
Cellular
%N
10.0
11.8
8.9
11.3
15.7
9.6
8.8
10.4
7.8
7.0
8.4
5.7
7.5
7.8
6.1
% P
2.2
2.9
1.8
2.5
3.4
2.1
2.6
2.7
2,3
2.6
2.8
2.3
2.5
2.9
2.1
oo
-------
GBMSD Industrial-Municipal Research Project
Process D
Nutrient Data
Month
8
9
10
11
12
Year
69
69
69
69
69
NH3 - N
mg/1 as N
PE
16.5
25.6
4.8
19.1
23.7
15.3
15.6
18.0
14.4
30.6
49.3
10.7
12.7
19.3
1.8
PEF
19.9
28.4
4.8
23.7
27.8
20.3
22.2
40.5
17.3
39.1
56.0
17.6
22.0
31.4
8.7
DS
RT
9.4
26.3
1.5
15.5
23.0
6.1
7.0
18.3
.7
23.0
25.7
20:i
21.2
31.1
6.4
NO3 - N
mg/1 as N
C-10
1.7
4.0
.4
1.3
3,3
.7
.7
1.8
0
1.5
7.1
0
1.4
2.9
0
RT
1.7
4.0
.7
1.3
4.4
0
1.4
11.2
0
2.7
20.7
0
2.6
5.0
.4
Ortho-P
mg/1 as P
PE
1.7
2.8
.5
2.9
3.8
2.2
1.7
2.8
.8
1.6
3.7
.2
1.5
2.7
.5
PEF
2.8
3.8
1.4
4.7
6.0
3.4
2.5
4.0
1.6
4.5
6.9
2.6
6.0
8.3
4.3
DS
PEF
BOD:N:P
BOD=100
N
4.3
7.0
1.5
5.8
8.1
4.2
5.1
9.5
3.3
8.9
14.7
3.7
4.6
6.7
1.9
P
.6
.9
.3
1.2
1.6
.7
.5
.7
.4
1.0
1.9
.5
1.2
1.6
.7
Cell 10
Cellular
%N
9.5
9.8
9-1
9.5
10.0
8.6
9.3
9.8
8.3
6.6
7.8
4.7
7.3
9.0
5.5
% P
2.4
2.9
1.9
2.2
2.7
1.9
2.6
2.9
2.2
2.9
3.5
2.5
3.0
3.3
2.7
xO
-------
APPENDIX E
SOLIDS HANDLING STUDIES
LABORATORY DATA
371
-------
SOLIDS HANDLING STUDIES - LAB DATA - INDEX
Centrifugation
Solid Bowl
Basket
Dissolved Air Flotation
Gravity Thickening
Heat Treatment
Low Pressure Oxidation
Pressure Filtration
Vacuum Filtration
FE Microscreening
Sharpies Equipment Division
Rex Chainbelt, Inc.
The Eimco Corporation
Dorr-Oliver, Inc.
The Eimco Corporation
Walker Process Equipment
BSP Corporation
Dorr-Oliver, Inc.
Zimpro, Inc.
Zimpro, Inc.
Beloit-Passavant Corporation
The Eimco Corporation
Walker Process Equipment
Beloit-Passavant Corporation
Crane-Glenfield, Inc.
Southwestern Engr. Co.
37Z
-------
SOLIDS HANDLING STUDIES - LAB DATA - FOOTNOTES
a. "S" and "T" denotes "Sampled By" and "Tested By", respectively;
We = GBMSD; They = Manufacturer
b. 5-day BOD
c. Ammonia nitrogen as N
d. Total ortho phosphorus as P
e. Total phosphorus as P
E. Estimated value
f . "(13:1)" represents the ratio of WAS to primary clarifier sludge,
by volume
g. Suffix "C" indicates the use of chemical admixtures; the chemicals
and feed rates used are listed on page 374.
h. Sample analyses lost (--*)
i . "Skimmed Cake" is the normal sludge cake discharged by the unit
j . "Bowl Cake" is the residual cake in the bowl that is periodically
removed from centrifuge
k. "Combined Flow" represents analyses of the combined volumes of
waste activated sludge and pressurized flow
m. Two (2) dilutions of raw sludge feed were tested during each run;
pilot plant final effluent was used for dilution
n. Sample Nos. T-3C and T-9C represents the use of Walker Process
Equipment's Pilot Poly-Thickener Unit (7-1/2" dia. x 14' SWD).
Sample No. T-8C represents use of the research project's pilot
settling column (3-1/2" dia. x 12' SWD).
p. O.P. values are soluble orthophosphorus as P
q. T.P. values are total soluble phosphorus as P
373
-------
SOLIDS HANDLING STUDIES - CHEMICAL ADMIXTURES
Unit Process
Centrifugation
Sharpies Equipment Div.
Dissolved Air Flotation
Rex Chainbelt, Inc.
Sample Number
The Eimco Corp.
Gravity Thickening
Walker Process Equip.
Pressure Filtration
Beloit-Passavant Corp.
Vacuum Filtration
The Eimco Corp.
Walker Process Equip.
Rex 35C
Rex 6C, 9C
Rex 38C
Rex 25C
E-4, E-5, E-6
All
All
All
All
All
Selected
All
All
Chemical Admixture
Reten 210
Dow C-7
Dow C-31
Gendriv 1 62
Nalco 603
Dow C-31
Nalco 610
Fly Ash
Lime
FeCl3
Lime (as CaO)
Magnafloc 521-C
Fed,
Lime (as Ca(OH)2)
* By weight means dry weight of chemical to dry weight of total solids.
Chemical Feed Rates
Unavailable
0.5-10 Ibs./ton D.S.
2-40 Ibs. /ton D.S.
5-20 Ibs. /ton D.S.
15-40 Ibs./ton D.S.
2-10 mg/1 based on
forward flow to unit
(recycle excluded)
10 mg/1 based on flow
to unit
1:1-3:1 by weight*
0. 1:1 - 0.2:1 by weight
0-8% , by weight
4 - 23%, by weight
0 - 20%, by weight
0 - 11%, by weight
10 - 23%, by weight
-------
SOLIDS'HANDLING STUDIES
Unit Process Centrifugation
Company
Sample- Source
Sharpies Equipment Division
Solid Bowl Centrifuge
Raw Feed Sludge (13:l)f
Centrate
Centrate
Raw Feed Sludge (13:1)
Centrate
Cake
Centrate
Cake
Centrate
Cake
Centrate
Cake
Centrate
Cake
Centrate
Cake
Centrate
Cake
Centrate
Cake
Centrate
Cake
Sample
No.
Run 1
1
1-C8
Run 2
IE
IS
2EC
2SC
3EC
3SC
4E
4S
SEC
5SC
6EC
6SC
7E
7S
SEC
8SC
9EC
9SC
We
Ca)
S,T
S,T
S,T
T
T
S,T
T
S,T
T
S,T
T
S,T
T
S,T
T
S,T
T
S,T
T
S,T
T
S,T
They
(a)
S
S
S
S
S
S
S
S
S
S
S
S
TS
8.1
11.0
9.9
10.0
9.. 2
10.8
8.1
9.4
9.0
TVS
Vol.
TSS
mg/1
30148
10936
630
29708
17000
340
380
21610
1870
2200
10950
330
1300
VSS
mg/1
24944
7932
470
24492
13892
*h
*
17425
1400
1670
8760
*
990
Vol.
82.7
72.5
74.6
82.4
81.7
80.6
74.9
75.9
80.0
76.2
PH
6.5
LI. 3
9.8
6.2
6.9
7.1
7.0
7.0
7.2
7.2
BODb
mg/1
1440
1265
1670
1875
1170
1480
Nutrient Anal.
mg/1
13.5
57.9
30.4
173
167
119
115
132
144
109
126
O.P.d
mg/1
179
106
3.1
185
4.5
4.4
9.1
10.9
4.2
8.0
T.P.e
mg/1
691
267
10.0
664
20.9
13.8
32.8
40.0
12.5
22.9
u>
-------
SOLIDS'HANDLING STUDIES
Unit Process Centrifugation (Continued)
Company
Sample- Source
Fletcher Centrifuge
Raw Feed Sludge (13:1)
Centrate
j
Skimmed Cake1
Bowl CakeJ
Centrate
Centrate
Raw Feed Sludge (13:1)
Centrate
Skimmed Cake
Bowl Cake
Raw Feed Sludge (13:1)
Centrate
Skimmed Cake
Bowl Cake
Raw Feed Sludge (13:1)
Centrate Composite
Skimmed Cake
Bowl Cake
Raw Feed Sludge (13:1)
Centrate Composite
Skimmed Cake
Bowl Cake
Raw Feed Sludge (13:1)
Centrate Composite
Skimmed Cake
Bowl Cake
Sample
No.
FF-1
1-E1
1-S1
1-S2
1-E2
1-E3
FF-2
2-E1
2-S1
2-S2
FF-3
3-E1
3-S1
3-S2
FF-4
4-E1
4-S1
4-S2
FF-5
5-E1
5-S1
5-S2
FF-6
6-E1
6-S1
6-S2
We
Ca)
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
They
(a)
S
S
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s
s-
s
TS
7 .2
10.5
8.1
11. 3
6.2
L0.2
9.8
L3.8
8.2
L3.2
7.3
L3.5
TVS
Vol.
TSS
mg/1
14888
1292
1520
8348
15124
904
15564
2492
17956
1484
17744
1564
16616
2196
VSS
mg/1
12404
1172
1220
6816
12644
740
12960
2112
14924
1152
14712
1156
13940
1772
Vol.
83.3
90.7
80.3
81.6
83.6
81.9
83.3
84.8
83.1
77.6
82.9
73.9
83.9
80.7
pH
6.7
7 .3
7.1
6.6
7 .2
6.5
7 .1
6. 7
7.0
6.8
6.9
BODb
mg/1
413
600
338
900
675
825
975
Nutrient Anal.
mg/1
19.6
13.6
14.3
22.5
13.9
16.4
11.4
7.9
18.6
9.3
10.0
O.P.d
mg/1
65.6
10.4
12.7
75.6
9 .6
58.6
16.5
9.4
7.0
10.3
6.7
T.P.e
mg/1
369
35.4
42.8
341
39.8
350
66.0
31.0
304
33.2
48.5
-------
SOLIDS HANDLING STUDIES
Unit Process
Dissolved Air Flotation
Company
Sample Source
Rex Chainbelt, Inc.
Raw WAS Feed
Combined Flow
Subnatant
"Combined Flow
Subnatant
Raw WAS Feed
Combined Flow
Combined Flow
Raw WAS Feed
Combined Flow
Subnatant
Combined Flow
Subnatant
Pressurized Flow
Raw WAS Feed
Combined Flow
Subnatant
Combined Flow
Subnatant
Combined Flow
Subnatant
Sample
No.
Run 1
7
7
6-C8
6-cB
Run 2
8
9-C
Run 3
20
20
25-C
25-C
Run 4
Run 4
30
30
35-C
35-C
38-C
We
Ca)
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
They
(a)
TS
TVS
Vol.
TSS
mg/1
11044
3480E
220
3480E
124
12364
4228
4028
11772
3672E
200
3672
216
300
11472
3701E
320
3700E
172
3683
104
VSS
mg/1
9860
3150E
200
3150E
92
10636
3560
3520
10060
3110E
116
3110
128
216
9604
3126E
216
3114E
132
3113
80
Vol.
89.3
90.5
90.9
90.5
74.2
86.0
84.0
87.4
85.5
84.7
58.0
84.7
59.3
72,0
83.7
84.5
67.5
84.2
76.7
84.5
76.9
pH
6.7
6.8
7.1
6.7
6.8
6.7
6.9
7.1
6.3
6.6
6.6
6.6
6.9
BODb
mg/1
385
310
371
335
589
305
340
255
Nutrient Anal.
NH3c
m /I
42.1
29.1
17.3
19.4
16.2
15,5
19.3
12.5
15.0
13.2
12.9
mg/1
45.9
5". 7
3.9
59 .4
2.1
2.6
5.3
39 . 8
4.0
4.3
3.8
T.P.e
mg/1
240
10.5
8.1
262
6.6
7.4
13.2
240
9.8
11.5
8.8
-------
SOLIDS HANDLING STUDIES
Unit
Dissolved Air Flotation
Company
Sample Source
The Eirnco Corporation
Raw WAS Feed
Subnatant
Float Concentration
Subnatant
Float Concentration
Subnatant
Float Concentration
Subnatant
Float Concentration
Subnatant
Float Concentration
Subnatant
Float Concentration
Sample
No.
E-l
E-l
•E-2
E-2
E-3
E-3
E-4C
E-4C
E-5C
E-5C
E-6C
E-6C
We
(a)
S,T
They
(a)
S,T
S,T
S,T
S,T
S, T
S,T
S,T
S.T
S,T
S, T
S,T
S, T
TS
%
3.39
2.99
3.77
3.38
3.50
3.53
TVS
%
%
Vol.
TSS
mg/1
12, 792
180
551
224
190
340
241
VSS
mg/1
10,484
%
Vol.
82.0
pH
BODb
mg/1
Nutrient Anal.
NH3C
mg/1
O.P.d
mg/1
T.P.e
mg/1
OJ
-0
00
-------
SOLIDS HANDLING STUDIES
Unit Process
Gravity Thickening
Company
Sample Source
Dorr-Oliver, Inc.
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Sample
No.
Run lm
ti
Run !"»
ii
Run 2
it
Run 2
ii
Run 3
ii
Run 3
ii
Run 4
ii
Run 4
it
We
Ca)
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,I
S,T
They
(a)
TS
%
TVS
%
%
Vol.
TSS
mg/1
4408
210
8520
170
4052
160
7772
152
3324
142
6516
160
2676
136
6104
232
vss
mg/1
3876
180
7432
150
3408
128
6748
120
2812
100
5520
108
2300
104
5144
148
%
Vol.
87.9
85.7
87.2
88.2
84.1
80.0
86.8
78.9
84.6
70.4
84.7
67.5
85.9
76.5
84.3
63.8
PH
7.0
7.0
7.0
6.9
6.9
7 .0
6.7
7.0
7 .5
7.3
7.5
7.3
7.0
7.2
7.0
7.1
BODb
mg/1
264
276
130
160
75
105
60
110
Nutrient Anal.
NH3c
mg/1
18.7
19.1
21.6
19.8
5.0
1.5
7.6
4.0
7.1
3.6
16.1
6.4
5.0
3.9
4.3
2.9
O.P.d
mg/1
20.1
5.4
35.0
7.2
16.6
1.7
32.8
2.3
18.2
2.3
37.1
2.7
9.2
2.3
21.9
2.8
T.P.e
mg/1
78.7
9.2
168
11.4
72.1
51
160
6.0
44.8
4.2
168
6.4
45.9
5.1
103
7,5
SO
-------
SOLIDS'HANDLING STUDIES
Unit Process Gravity Thickening
w
00
o
Company
Sample Source
Eimco Corporation
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Raw Sludge Feed (13:1)
Supernatant
Sample
No.
Run 1
it
Run 2
it
Run 3
ii
Run 4
ii
We
Ca)
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
They
(a)
TS
%
TVS
%
%
Vol.
TSS
mg/1
14248
313
16864
142
14160
276
15068
288
VSS
mg/1
12460
227
14344
142
13228
192
12568
196
%
Vol.
72.5
85.1
93.4
69.6
83.4
68.1
PH
6.4
7.0
6.8
6.8
6.7
6.7
6.5
7.0
BODb
mg/1
335
145
240
165
Nutrient Anal.
NH3c
mg/1
29.3
20.9
21.6
4.7
41.4
7.6
11.1
2.9
O.P.d
mg/1
50.3
10.2
78. 7
3.2
76.9
3.6
51.1
2.4
T.P.e
mg/1
240
18.1
323
5.9
240
7.6
245
7.9
-------
SOLIDS'HANDLING STUDIES
Unit Process Gravity Thickening
Company
Sample Source
Walker Process Equipment Co,
Raw WAS Feed11
Supernatant
Raw WAS Feed +Fen
Supernatant
Raw WAS Feed +Fen
Supernatant
Sample
No.
T-3C8
ii
T-8C
ii
T-9C
II
We
Ca)
S,T
S ,T
S,T
S,T
S,T
S,T
They
(a)
TS
%
TVS
%
%
Vol.
TSS
mg/1
12732
84
9860
111
7708
143
VSS
mg/1
10564
8028
6388
143
%
Vol.
83.0
81.4
82.9
PH
7.0
7 .0
6.9
7 .0
6.9
7 .1
BODb
mg/1
345
68
68
Nutrient Anal.
NH3c
mg/1
70.3
31.8
22.9
18.9
33.6
15.0
O.P.d
mg/1
69.9
3.4
61.2
5.0
48.1
3.6
T.P.e
mg/1
110
6.3
179
10.7
184
8.4
oo
oo
-------
SOLIDS'HANDLING STUDIES
Unit Process Heat Treatment
Company
Sample Source
Dorr-Oliver, Inc.
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Cooked Sludge
Cooked Sludge
Decant
Cooked Sludge
Decant
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Sample
No.
3
1
1-A
1-B
1-C
It
1-D
it
2
2
2-A
ti
We
Ca)
S,T
T
T
S,T
T
They
(a)
S,T
S,T
S,T
S,T
S
S,T
S
S,T
S,T
S
TS
TVS
Vol.
TSS
mg/1
30840
30710
19920
17050
17680
16948
17090
8164
30580
32660
18660
180
VSS
mg/1
26368
26270
16400
14970
12990
12844
12390
6312
25472
27100
13840
60
%
Vol.
82.3
87.8
73.4
75.8
72.5
77.3
83.3
83.0
74.2
33.0
PH
6.4
5.4
5.0
4.9
5.0
5.4
5.0
5.4
6.8
5.0
BODb
mg/1
7950
8520
8210
12600
8000
13200
2809
8470
11400
Nutrient Anal.
mg/1
187
421
506
80.0
355
O.P.o
mg/1
238
68.2
74.7
190
13.1
T.P.e
mg/1
756
140
153
511
61.2
OJ
00
-------
SOLIDS HANDLING STUDIES
Unit Process Heat Treatment
Company
Sample Source
BSP Corporation
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake
Sample
No.
1-2
1-2
1-2
1-2
1-2
1-2
1-2
3
3
3
3
3
3
3
We
Ca)
S,T
S,T
They
(a)
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
TS
3.11
3.11
7.75
26.5
3.30
1.58
4.19
25,0
TVS
2.54
2.07
4.92
17.6
2.37
1.09
2.51
Vol.
81.8
66.5
63.5
66.5
71.7
69.0
60.0
TSS
mg/1
30840
194
266
29392
106
508
VSS
mg/1
26368
174
218
24836
68
336
Vol.
85.5
89.7
82.0
84.5
64.2
66.1
PH
6.4
5.9
5.4
5.4
5.4
6.4
6.4
5.7
5.6
5.6
BODb
mg/1
5330
6340
16000
7000
4000
5500
Nutrient Anal.
NH3c
mg/1
187
305
343
155
98
154
162
146
O.P.d
mg/1
238
36. 5P
48. 9P
119
7.2P
24. 3P
24. 3P
f\
74. 5P
T.P.e
mg/1
756
24. 5q
39. lq
642
9.5q
18. 3q
18. lq
55. 5q
w
00
-------
SOLIDS HANDLING STUDIES
Unit Process Heat Treatment
Company
Sample Source
Zimpro, Inc.
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake
Raw Sludge Feed (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant
Decant Sludge
Filtrate
Cake
Sample
No.
B-2
#36
ti
ti
ii
tt
ii
B-3
#37
n
tt
ti
ii
ii
B-2
#41
ii
ii
it
it
ii
B-3
#42
ii
ii
ii
ii
M
We
Ca)
S,T
S,T
S,T
S,T
They
(a)
S,T
S,T
S,T
S,T
S ,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T
S,T,
S,T
S,.T
TS
%
3.71
2.68
1.53
7.02
1.36
38.0
3.46
2.92
1.44
6.31
1.25
35.0
3.21
2.08
7.61
.99
32.8
3.34
1.45
5.89
0.73
34.7
TVS
%
3.07
2.15
1.38
5.12
1.24
26.9
2.87
2.40
1.30
4.95
1.14
26.6
2.59
1.64
5.35
.90
22.3
2.68
1.13
4.14
0.66
23.6
%
Vol.
82.7
80.2
90.2
72.9
91.2
70.8
82.9
82.2
90.3
78.4
91.2
76.1
80.7
78.8
70.3
90.9
68.0
80.2
77.9
70.3
90.4
67.9
TSS
mg/1
34416
13400
300
59800
300E
33104
17100
300
52800
30996
11300
76400
1970E
30580
7400
53450
890E
VSS
mg/1
29632
9200
300
41600
300E
28412
12900
300
40000
25504
8100
54700
1467E
25472
4800
36600
530E
%
Vol.
86.1
68 .7
69.6
85.8
75.4
75.8
82.3
71.7
71.6
74.5
83.3
64.9
68.5
59.6
PH
5.9
5.9
6.0
6.2
5.8
6.7
5.4
5.7
6.8
6.1
5.4
BODb
mg/1
7900
7500
7090E
6560E
5700
4300
Nutrient Anal.
NH3c
mg/1
122
370
440
470
450
129
410
390
400
146
400
330
350
80.0
360
260
280
O.P.a
mg /I
192
11
7
131
14
9
214
22
9
190
97
8
T.P.e
mg/1
691
700
520
50
60
673
570
460
70
489
320
310
30
511
360
150
20
UJ
oo
-------
SOLIDS'HANDLING STUDIES
Unit Process Low Pressure Oxidation
u> -
oo
m
Company
Sample Source
Zimpro, Inc.
WAS & P.C. Mixture (16.6:1]
Raw Sludge as Tested
Cooked Sludge
Decant Liquor
Decant Sludge
Filtrate Liquor
Cake
WAS & P.C. Mixture (13:1)
Raw Sludge as Tested
Cooked Sludge
Decant Liquor
Decant Sludge
Filtrate Liquor
Cake
Sample
No.
B-l
#35
it
it
ii
it
M
B-l
#40
ii
ti
ii
ii
ii
We
Ca)
S,T
S,T
They
(a)
S,T
S,T
S ,T
S,T
S,T
S,T
S,T
S,T
S,T
S ,T
S,T
S,T
TS
%
3.18
2. 31
1.24
6.74
1.19
33.4
3.21
2.09
1.02
7.66
1.06
31,7
TVS
%
2.60
1.82
1.08
4.81
1.04
2.56
1.59
0.92
5.36
0.91
%
Vol.
69.4
67.7
TSS
mg/1
30588
11400
200
58270
350E
29994
10400
67800
730E
VSS
mg/1
25836
7900
200
40070
350E
24624
6900
46300
730E
%
Vol.
84.5
82.2
PH
6.2
6.0
4.7
5.0
6.5
5.2
4.6
4.8
BODb
mg/1
6000
5700
5700
5600
Nutrient Anal.
NH3c
mg/1
122
470
470
520
480
73.2
320
450
470
450
O.P.d
mg/1
188
13
18
114
31
11
T.P.e
mg/1
656
220
200
30
30
236
370
290
30
30
-------
SOLIDS HANDLING STUDIES
Unit Process Pressure Filtration
Company
Sample Source
Beloit-Passavant Corp.
Raw Sludge Feed (13:1)
Filtrate
Cake
Raw Sludge Feed (13:1)
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Raw Sludge Feed (13:1)
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Sample
No.
Prelim
"-CS
"-C
1
1-C.
R1C
2-C
R2C
3-C
R3C
4-C
R4C
5-C
R5C
6-C
R6C
1
1-C
R1C
2-C
R2C
3-C
R3C
4-C
We
Ca)
S,T
T
T
S,T
T
T
T
T
T
T
T
T
T
T
T
T
S,T
T
T
T
T
T
T
T
They
(a)
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
S
TS
40.8
33.5
51.1
42.7
29.4
40.7
30.0
50.0
46.9
48.0
TVS
16.9
13.0
17.3
16.5
12.9
13.7
12.6
14.8
14.6
16.4
Vol.
41.5
38.7
33.8
38.7
44.0
33.7
42.1
29.6
31.2
34.2
TSS
mg/1
34304
73
32084
7
198
566
24
13
54
28688
23
28
46
61
VSS
mg/1
29304
20
27592
— *
16
109
20
11
20
24188
18
22
42
48
Vol.
85,4
27.4
86.0
8.1
19.3
83.3
84.6
37.0
84.3
78.3
78.6
91.3
78.7
PH
L2.1
6.4
8.9
7.3
7.9
7.9
6.1
8.1
7.4
7.9
7.5
BODb
mg/1
2310
600
1005
1230
945
1020
930
908
1080
1095
1005
Nutrient Anal.
NH3c
mg/1
230
184
104
50
76
62
72
75
71
118E
61
78
71
67
O.P.d
mg/1
245
0.1
175
0.3
0.1
2.2
0.6
0.9
0.8
139
0.2
0.6
0.4
1.1
T.P.e
mg/1
752
8,7
791
2,2
5.5;
16.4
4.7
4.5
5.7
599
1.4
1.9
1.7
3.6
w
oo
-------
SOLIDS'HANDLING STUDIES
Unit Process Vacuum Filtration (,Raw Sludge)
Company
Sample- Source
Eimco Corporation
Raw Sludge Feed (13:1)
Filtrate
Cake
Filtrate
Cake
Raw Sludge Feed (13:1)
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Raw Sludge Feed (13:1)
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Raw Sludge Feed (13:1)
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
1
Sample
No.
Run 1
T-6C8
ii
T-7C
||
Run 2
T-1C
it
T-3C
II
T-4C
ii
T-5C
ii
T-6C
II
Run 3
T-1C
ii
T-3C
ii
T-4C
ii
T-5C
ii
Run 4
T-1C
ii
T-2C
ii
T-3C
it
We
Ca)
S ,T
S,T
S ,T
w 9
S ,T
S ,T
S ,T
S ,T
S,T
S,T
S,T
S ,T
S,T
S ,T
S ,T
S ,T
S ,T
S ,T
S ,T
S ,T
S,T
S ,T
S ,T
S ,T
S ,T
S,T
S,T
S ,T
S ,T
S,T
S,T
S,T
S,T
They
(a)
TS
%
13.0
14. 6
17 . 2
16. 5
L5.5
L9.0
15. 3
L4.0
L2. 7
L4.4
LI. 4
15. 3
L7.0
L4.7
TVS
%
%
Vol.
TSS
mg/1
22280
1053
1240
34188
376
372
472
496
288
32136
300
306
360
472
29840
408
900
736
VSS
mg/1
18940
560
720
28504
220
200
296
276
130
27404
156
148
164
384
24836
180
488
380
%
Vol.
85.0
53.2
58.1
83.4
58.5
53.8
62.7
55.6
45.1
85.3
52.0
48.4
45.6
81.4
83.2
44.1
54.2
51.6
PH
6.G
11.7
11.7
6.0
12.1
12.1
12.1
12. 1
12.1
6.6
12.3
L2.2
LI. 9
7.0
7 .2
LI. 9
L2.0
L2.0
BODb
mg/1
990
1080
1020
930
870
960
990
1575
1050
900
1020
960
1050
1110
Nutrient Anal.
NH3c
mg/1
121
77,3
66,9
52.2
36.7
37.4
38.5
40.3
28.1
69.1
76.6
61.5
50.7
96.4
168
58.6
59.6
51.1
O.P.d
mg /I
94
2.8
3.5
153
1.0
1.4
1.4
1.6
0.8
124
0.8
0.8
1.0
7.0
50. 3
0.9
4.4
2.7
T.P.e
mg/1
410
15.3
18.1
586
6.6
5.1
6.3
7.6
3.6
581
3.5
4.5
4.4
17.9
586
6.1
16.8
11.6
UJ
oo
-------
SOLIDS HANDLING STUDIES
Unit Process Vacuum Filtration (continued)
Company
Sample- Source
Eimco Corporation
Filtrate
Cake
Filtrate
Cake
Filtrate
Cake
Sample
No.
Run 4
T-4C
it
T-5C
it
T-6C
u
We
Ca)
S,T
S,T
S,T
S,T
S,T
S,T
They
(a)
TS
%
15.4
16.6
15.4
TVS
%
%
Vol.
TSS
rag /I
568
580
524
VSS
mg/1
224
272
240
%
Vol.
39.4
46.9
45.8
PH
11.6
11.8
11.7
BODb
mg/1
960
900
930
Nutrient Anal.
NH3c
mg/1
51.4
50.0
65.7
O.P.d
mg/1
2.0
2.3
3.4
T.P.e
mg/1
6.1
7.4
12.0
00
oo
-------
SOLIDS'HANDLING STUDIES
Unit Process Vacuum Filtration
Company
Sample Source
Walker Process Equipment
Raw Sludge Feed (13:1)
Filtrate
Cake
Cake
Cake
Sample
No.
5-WI
5-WC8
ii
3-WC
7-WC
We
(a)
T
T
T
T
T
They
(a)
S
S
S
S
S
TS
%
14.4
15.7
12.:
TVS
%
10.4
11.5
9.1
%
Vol.
72.1
73.5
73.9
TSS
mg/1
36680
124
VSS
mg/1
23748
60
%
Vol.
64.7
48.4
PH
9.7
10.!
BODb
mg/1
1035
Nutrient Anal.
NH3c
mg/1
59.6
O.P.d
mg/1
0.6
T.P.e
mg/1
8.6
OJ
oo
-------
SOLIDS HANDLING STUDIES
Unit Prnross
Micfoscreening
Company
Sample Source
Beloit-Passavant Corp.
Raw Final Effluent
10 M Filtrate
3 M Filtrate
Raw Final Effluent
10 M Filtrate
3 M Filtrate
Raw Final Effluent
10 M Filtrate
3 M Filtrate
Raw Final Effluent
10 M Filtrate
3 M Filtrate
Note: M = Micron
Sample
No.
BP-1
BP-1AB
BP-5AB
BP-2
BP-2AB
We
'a)
S,T
S,T
S, T
S,T
S,T
BP-6ABJS.T
BP-3JS.T
BP-3B
BP-7AB
BP-4
BP-4AB
BP-8AB
S,T
S,T
S,T
S,T
S,T
I
They
(a)
TS
%
TVS
%
%
Vol.
TSS
mg/1
76
45
42
95
65
57
52
18
11
20
15
2
vss
mg/1
56
33
30
72
48
41
49
__*
__*
15
9
__*
%
Vol.
73.7
73.3
71.4
75.8
73.8
71.9
94.2
75.0
60.0
PH
BODb
mg/1
Nut
NH3C
mg/1
ient Anal.
O.P.d
mg/1
T.P.e
mg/1
-------
SOLIDS HANDLING STUDIES
Unit Process FE Microstraining
Company
Sample- Source
Crane -Glenfield, Inc.
Raw Final Effluent
Filtrate
Raw Final Effluent
Filtrate
Raw Final Effluent
Filtrate
Raw Final Effluent
Filtrate
Sample
No.
A
A-12
B
B-12
C
C-12
D
D-12
We
Ca)
T
T
T
T
T
T
T
T
They
(a)
S
S
S
S
S
S
S
S
TS
%
-
TVS
%
%
Vol.
TSS
mg/1
94
68
116
84
62
27
27
7
VSS
mg/1
84
66
108
82
__*
__*
__*
__*
%
Vol.
89.4
97.1
93.1
97.6
PH
7.0
7.2
7.4
7.4
7.4
7.4
7.2
7.4
BODb
mg/1
138
41
86
39
78
69
18
13
Nutrient Anal.
NH3C
mg/1
o.p.a
mg/1
T.P.e
mg/1
CO
-------
SOLIDS HANDLING STUDIES
Unit Process FE Microscreening
Company
Sample Source
Southwestern Engr. Co.
Raw Final Effluent
Filtrate
Filtrate
Filtrate
Note: M = Mesh
Sample
No.
A-D
100M
ZOOM
325M
We
Ca)
T
T
T
T
They
(a)
S
S
S
S
TS
%
TVS
%
%
Vol.
TSS
mg/1
42
29
30
32
VSS
mg/1
*
*
#
#
%
Vol.
PH
7.2
BODb
mg/1
59
58
52
54
Nutrient Anal.
NH3c
mg/1
O.P.d
mg/1
T.P.e
mg/1
OO
O
to
-------
APPENDIX F
FULL-SCALE DESIGN PARAMETERS
393
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
PARAMETERS FOR CAPITAL AND OPERATING COST ESTIMATES
Design
Year
Source
Mill 1'
Mill 2
Mill 3
Mill 4
Metro
Total
PHASE II
1980
Flow
MGD
4.0
5.0
7.0
1.25
27.0
44.25
BOD
TON/D
15.0
20.0
20.5
7.75
29.0
92.25
TSS
TON/D
2.5
3.0
5.2
1.5
32.4
44.6
PHASE III
1983
Flow
MGD
5.0
5.0
10.5
0.6
30.0
51.1
BOD
TON/D
30.0
15.0
25.0
7.0
29.5
106.5
TSS
TON/D
5.0
2.0
5.0
2.5
23.0
37.5
PHASE IV
1983
Flow
MGD
5.0
5.0
13.25
0.6
30.0
53.85
BOD
TON/D
30.0
15.0
33.2
7.0
29.5
114.7
TSS
TON/D
5.0
2.0
6.6
2.5
23.0
39.1
DESIGN SCALE-UP FACTORS
Design Parameter
Peak Flow
Primary Clarifier
Sludge Volume
Recirculation
03 Supply
WAS Volume
TV 4. J Cl A
juigesteci tDiudge
•P>' C D 4-
uig. oup. ±\eturn
Nutrient Feed:
N and P
PI
C
Metro, M3-250%
Ml, 2, 4 --150%
150%
R/Qa = 1.25
150%.
25% Qa
"""*"""
140%
1ASE II
CS
Same
Same
R/Qa=1.0
Same
Same
140%
K
Same
Same
Rn=150%
Rc/Qa=1.0
Same
Same
1 50%
JL -f \J /U
1 ?^°1n
± L* J /V
PHASE
CS
Metro-412%
Mills -125%
150%
R/Qm=1.0
150%
25%Qa
200%
III
K
Same
Same
R/Qm = 1.0
Same
Same
150%
_L ^ \J /{J
125%
J. « *J /\]
PHASE IV
CS
Metro - 400%
Mills - 125%
140%
R/Qm=1.0
170%
25%Qa
*""*""""
200%
Qa = Q average; Qm = Q maximum
-------
ABBREVIATIONS
add. added
BOD Five-day biochemical oxygen demand
BOD:N:P-- biochemical oxygen demand to nitrogen (as N) to phosphorus
(as P) ratio, by weight
C conventional process
cap. capacity
CF cubic feet
cf/lb cubic feet per pound
COD chemical oxygen demand
cone. concentration
CS contact stabilization
D. digester supernatant
dc/dt rate of change of concentration with respect to time --oxygen
uptake studies
Dest. destroyed
Dig. sup.--digester supernatant
D.O. dissolved oxygen
D.S. dried solids
D£ detention time
eff. effluent
F-BOD biochemical oxygen demand of sample filtered through
Whatman #5 filter paper
FC final clarifier
FE final effluent
F.I. filter ability index
F/M food to microorganism ratio; pounds of BOD daily fed to the
aeration tanks divided by the pounds of volatile suspended
solids under aeration in the contact and reaeration sections
inf. influent
K Kraus
lbs/1000 CF/day - pounds per 1000 cubic feet per day
Ibs/D as N-pounds per day as nitrogen
Ibs/D as P-pounds per day as phosphorous
Libs TSS/SF/Day - pounds of total suspended solids per square foot per day
Lbs VSS/CF/Day - pounds of volatile suspended solids per cubic foot per
day
L/D liters per day
mg/gm milligrams per gram
mg/1 O2/MLVSS/hr. - milligrams per liter of oxygen per milligram of
mixed liquor volatile suspended solids per hour
M.L. mixed liquor - the mixture of biological organisms and
liquor undergoing aeration in the aeration tanks
MLTSS mixed liquor total suspended solids
409
-------
ABBREVIATIONS (Gont'd)
MLVSS mixed liquor volatile suspended solid s
mu. millimicrons
N.A. no analysis
O. R. overflow rate
p phosphorous
PE primary effluent
PEF primary effluent fortified - PE after nutrient addition
Phos O + C as P - ortho plus condensed phosphorous as P
PI primary influent
PP-PE pilot plant primary effluent
Q quantity of raw sewage to be treated, = Qf
Qa Q average
Q£ Q forward, = Q
Qm Q minimum
R quantity of return activated sludge
RAS return activated sludge
RAS-S= sulfide ion concentration in return activated sludge
R --quantity of RAS returned to contact section of process
Reaer reaeration
Rn ' quantity of RAS returned to nitrifying section of process
R/Q ratio of return activated sludge divided by total forward flow
SA step aeration
Sa't MLVSS concentration (mg/1) in contact section times the
detention time (hours) in the contact section
S.D. standard deviation
SFR specific filtration resistance
S. U. standard units
sup. supernatant
SVI sludge volume index
SWD sidewater depth
T time
TC total carbon
To time at start of experiment
T.O. total organic nitrogen
TRC total residual chlorine
TS total solids
TSS total suspended solids
U-BOD BOD of unfiltered sample
Ug micrograms
vol. volume
voL A volatile acid
VS/1000 CF/D - pounds of volatile solids added per 1000 cubic feet per day
VSS volatile suspended solids
WAS waste activated sludge
# pounds
410
-------
1
Accession Number
w
5
Q Subject Field & Group
05D
SELECTED WATER RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
Organization
Green Bay, Wisconsin
Title
Joint Treatment of Municipal Sewerage and Pulp Mill Effluents
10
Authors)
Voelkel, K. Go
Deering, R. W.
Wilms, L. Ro
16
Project Designation
Grant #WPRD 60-01-6? (Program #12130 EDX)
21
Note
22
Citation
23
Descriptors (Starred First)
Pulp Wastes, Municipal Wastes, Waste Treatment, Activated Sludge,
Pilot Plant, Sludge Disposal, Capital Costs.
25
Identifiers (Starred First)
27
Abstract
influent from the Green Bay Metropolitan Sewerage District was treated in
combination with the weak effluents from pulping sections of four local paper mills,
American Can Company, Charmin Paper Products Company, Fort Howard Paper Company and
Green Bay Packaging, Inc. Four activated sludge processes (conventional, step aeration,
contact stabilization, and Kraus) were studied in parallel using 1-gpm pilot plants 0
Contact stabilization was selected as the most promising process and units were
operated for five months to obtain refined design and operating parameters for a full-
scale treatment plant. Initially, the pilot plants became infested with filamentous
organisms identified as the bacterial genus Thjpthrix. Chlorination of the return
activated sludge successfully controlled the growth of these organisms,, It was also
necessary to add nutrients to achieve the desired BOD:N:P ratios.
The operation of the pilot plant units during the last study phase gave BOD
removals of 91# and TSS removals of 78$. Extensive solids-handling unit process studies
were conducted at the pilot plant site and in the cooperating manufacturer's labora-
tories. The capital costs to the individual participants, based on becoming a part
of the joint venture or providing separate facilities, are presented. American Can
Company and Charmin Paper Products Company are joining with the Green Bay Metropolitan
Sewerage District in a joint treatment plant program.
Abstractor
K. G. Voelkel
Institution
Green Bay Metropolitan Sewerage District
WR:102 (REV. JULY 1969)
WRSIC
SEND. WITH COPY OF DOCUMENT. TO: WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U.S. DEPARTMENT OF THE INTERIOR
WASHINGTON, D. C. 20240
•fcUS. GOVERNMENT PRINTING OFFICE: 1572 O—453-779
------- |