WATER POLLUTION CONTROL RESEARCH SERIES 1212O
Treatment of Sole Leather
Vegetable Tannery Wastes
U.S. DEPARTMENT OF THE INTERIOR FEDERAL, WATER QUALITY ADMINISTRATION
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WA R POLLUTION CONTROL RESEARCH SERIES
The Water Pollution Control Research Reports describe
the results and progress in the control and abatement
of pollution in our Nations waters. They provide a central
source of information on the research, developnent, and
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Reports should be directed to the Head, Project Reports
System, Planning and Resources Office, Office of Research
and Development, Department of the Interior, Federal Water
Quality Administration, Room llO , Washington, D. C. 20242.
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"TREATMENT OF SOLE LEATHER
VEGETABLE TANNERY WASTES"
SEPARATION/ PRETREATMENT, AND BLENDING
OF THE WASTE FRACTIONS FROM A SOLE LEATHER
TANNERY FOR FINAL TREATMENT IN A STRATIFIED
ANAEROBIC-AEROBIC LAGOON SYSTEM
FEDERAL WATER POLLUTION CONTROL ADMINISTRATION
DEPARTMENT OF INTERIOR
BY
DR, J, DAVID EYE
PROFESSOR OF ENVIRONMENTAL HEALTH ENGINEERING
UNIVERSITY OF CINCINNATI
PROGRAM NUMBER 12120
GRANT NUMBER WPD-185
SEPTEMBER, 1970
For solo by tho Superintendent of Documents, U S Government Printing Ofllco
Washington, D C 20402 - Price $1 25
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FWPCA Review Notice
This report has been reviewed by the Federal
Water Pollution Control Administration and
approved for publication. Approval does not
signify that the contents necessarily reflect
the views and policies of the Federal Water
Pollution Control Administration.
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Abstract
Four major studies, two pilot scale and two full
scale, were carried out during the period of this investi-
gation. The basic objective of the studies was to find a
technically feasible and economical procedure for treat-
ing the wastes from a sole leather vegetable tannery. A
detailed identification of the sources of all wastes as
well as a comprehensive characterization of each waste
fraction was made for the International Shoe Company
Tannery located at Marlinton, West Virginia.
It was found that a large percentage of the pollutants
initially were contained in a relatively small fraction of
the total waste volume. The treatment scheme consisted of
separation and pretreatment of the individual waste streams
followed by mixing all waste streams for additional treat-
ment in an anaerobic-aerobic lagoon system.
The lime bearing wastes from the beamhouse were
screened, treated with polyelectrolytes, and then clari-
fied. The lime sludge was used for landfill. The system
was designed to treat one million gallons of waste per
week. BOD was reduced 85-95 percent and the suspended
solids reduction was in excess of 95 percent. Installed
cost of the total system was approximately $40,000 and it
is estimated that the operating cost will be about $15,000
per year or 7 cents per hide processed.
This report was submitted in fulfillment of Research
and Development Grant Number WPD-l85 between the Federal
Water Pollution Control Administration and the University
of Cincinnati.
Key Words:
Tannery
Pilot Plants
Prototype Plants
Waste Treatment
Industrial Wastes
Clarification
anaerobic-Aerobic Lagoons
111
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TABLE OF CONTENTS
Page No .
ABSTRACT
SECTION 1. Conclusions and Recommendations 1
SECTION 2. Introduction 5
SECTION 3. Experimental and Operational Findings 11
Research Plan 11
Removal of Suspended Lime 11
Design and Construction of the
Full-Scale Clarification System 15
Performance of the Clarifier 20
Characteristics of the Lime Sludge 25
Biological Treatment 27
Pilot Plant Studies on Beamhouse
Wastes 28
Design of Stratified Anaerobic-
Aerobic Lagoons 30
Operating and Performance
Characteristics of Lagoons 31
Pilot Plant Treatment of the Total
Tannery Wastes 42
Treatment of Total Tannery Wastes 45
Effect of Effluent on the
Receiving Stream 67
Removal of Color 83
SECTION 4. Acknowledgements 85
SECTION 5. References 87
SECTION 6. Appendix 89
V
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LIST OF FIGURES
Figure No. Title Page No .
1. Sources of Major Wastes 8
2. Settling Curves for Lime-Bearing
Wastes 14
3. Settling Rates for Lime Sludge 16
4. Sewerage System Serving Beamhouse 17
5. Upflow Clarifier Details 19
6. Clarifier Performance 21
7. Overflow Rate vs Suspended Solids
emova1 24
8. Polyelectrolyte Dose vs Fixed
Suspended Solids Removal 26
9. Lagoon System at Plant Site 32
10. COD of Effluents from L-1 and L-2 35
11. Oxygen Buildup and Uptake 41
12. BOD vs Time 46
13. Oxygen Buildup and Uptake 47
14. Oxygen Buildup and Uptake 48
15. Layout and Approximate Dimensions
of Lagoon System 50
16. Reduction in BOD in Biological
System 66
17. Effluent BOD vs Time 70
18. Long-Term BOD Values 71
19. Oxygen Build-up and Uptake 75
20. Dissolved Oxygen Levels in
Receiving Stream 81
21. Dissolved Oxygen Levels in
Receiving Stream 82
vii
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LIST OF TABLES
Table No. Title Page No .
1. Characteristics of Tannery Waste
Fractions 7
2. Flocculation of Beamhouse Waste
Fractions by an Anionic
Polyelectrolyte 12
3. Results of Pilot Plant Clarification 13
4. Performance of Clarification System 22
5. Sludge Drying Characteristics 27
6. Influent and Effluent Characteristics
of the Biological Units 30
7. Design Criteria for Stratified
Lagoons 31
8. Dissolved Oxygen Concentration in
Lagoon 2 36
9. Alkalinity and Hardness of Influent
and Effluent of Lagoon 2 38
10. Dissolved Oxygen Concentration in
Lagoon 2 39
11. BOD and COD Removals in Lagoon 2 39
12. Performance Characteristics of
Anaerobic-Aerobic Pilot Unit 43
13. BOD Values and Rate Constants 42
14. Performance of Full-Scale Biological
System 52
15. Sludge Accumulation in Lagoons 57
16. Performance of Biological System 59
17. Performance of Full-Scale Biological
Treatment System 61
lx
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LIST OF TABLES
(Continued)
Table No. Title Page No .
18. Long-Term BOD Values for Lagoons 68
19. Organic Loading and Flow to
Lagoons 72
20. Dissolved Oxygen Levels and Water
Temperature at Water Surface around
Periphery of Lagoons 76
21. Dissolved Oxygen Levels in Lagoons 79
A-i Performance of Clarification System 90
A-2 Performance of Clarification System 92
A-3 Performance Characteristics of
Anaerobic-Aerobic Pilot Unit 98
A4 Performance Characteristics of
Anaerobic-Aerobic Pilot Unit 109
C
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Section 1
Conclusions and Recommendations:
The investigation described in this report was con-
ducted for the express purpose of developing and evaluating
a procedure for treating the wastes from a sole leather
tannery. The study plan included the characterization,
separation, and pretreatment of the various waste fractions
followed by a blending of all waste streams for final puri-
fication. Pilot plant scale studies were used to provide
design and operational data for a full-scale waste treat-
ment system which was constructed and operated as a part of
the demonstration grant.
The lime-bearing wastes from the beamhouse were
screened, treated with an anionic polyelectrolyte and
clarified prior to being mixed with the other beamhouse
waste fractions (also screened). The pretreated bearnhouse
wastes then were subjected to biological treatment in
stratified anaerobic-aerobic lagoons equipped with floating
aerators. After the lagoons had been operated for several
months on beamhouse wastes, the spent vegetable tan liquors
were added and the total wastes treated biologically.
The data derived from the pilot plant and full scale
treatment procedure over a period of approximately three
years lead to the following specific conclusions and
recommendations:
1. A detailed study of the total tanning operations
is a required first step in formulating a feasible waste
treatment procedure. Specifically the sources of all wastes
must be identified and each waste stream must be completely
characterized. The volume, discharge pattern and con-
stituents of each waste fraction must be determined accu-
rately and related to specific tanning operations.
2. A waste reduction program through conservation,
reuse, and process changes is feasible for a sole leather
tannery. Such a program can.be effective only if the plant
operating personnel are fully informed of the objectives to
be achieved and the role that they play in the total plan.
3. About 70 percent of the total pollutional load dis-
charged from a sole leather tannery initially is contained
in three or four waste streams which comprise only about 30
percent of the total volume of wastes discharged. Segre-
gation and pretreatment of the individual waste fractions,
therefore, is necessary if an economical waste treatment
procedure is to be achieved.
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4. Separation of waste streams can be facilitated by
use of self-priming and submersible pumps coupled to plastic
piping run overhead rather than underground. It is
important that segregation procedures not interfere unduly
with normal tanning operations or require undue maintenance.
5. Excess hair, fleshings and grease should be removed
from the waste streams at an early point in the waste
management procedure as these materials clog pumps and
generally interfere with any mechanical handling of the
wastes. Mechanically cleaned screens with openings as small
as 20 mesh provide excellent control of coarse suspended
solids and require little maintenance.
6. Feasible pretreatment methods for the individual
waste streams can be determined by laboratory and pilot
plant studies. For example it was found that the lime-
bearing waste fractions from the beamhouse containing a con-
siderable quantity of suspended lime could be clarified
readily by use of an anionic polyelectrolyte followed by
quiescent settling. By contrast, without polyelectrolyte,
little clarification was achieved. It was noted also that
the suspended lime could not be removed effectively when
all of the beamhouse waste streams were mixed prior to
adding the polyelectrolyte. The data obtained from the
laboratory and pilot plant studies were used for designing
the fullscale separation, pretreatment and clarification
system.
7. In the full scale system an anionic polyelectrolyte
at a dosage of 10 mg/i provided optimum removal of the
suspended lime particles from the lime waters. Removal
efficiencies in excess of 90 percent were achieved routinely
at clarifier overflow rates of 1600 gallons per day per
squarefoot of clarifier surface area. Even at overflow
rates of 2,000 2,500 gpd/ft 2 , removal efficiencies of 80
90 percent were quite common.
8. The sludge obtained from the lime-water clarif i-
cation operation was pumped from the bottom of the clarifier
and used for land-fill. The solids content of the sludge
as pumped from the clarifier ranged from 8 to 30 percent
with an average of 15 percent. The volume of sludge pro-
duced averaged about 3 percent of the total volume of lime-
water clarified.
The lime sludge when placed on porous drying beds
could be dried sufficiently in three days to permit it to
be handled as a dry solid.
2
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9. After pretreatment all of the waste streams from
the beamhouse were blended and pumped to a lagoon system
for biological treatment. The pH of the blended beamhouse
wastes ranged from 11.5-12.5. Neutralization of the excess
alkalinity and reduction of the pH to a suitable range for
biological treatment was accomplished by adding spent
bleach acid to the lagoons.
10. The combination of spent bleach acid and beamhouse
wastes produced an extremely voluminous precipitate which
reduced the effective capacity of the lagoons significantly.
It was found, however, that once the lagoons became
operative sufficient carbon dioxide and organic acids were
formed to automatically control the pH of the system.
Further neutralization, therefore, was unnecessary.
11. Severe odor problems were encountered when
operating the anaerobic-aerobic lagoons on beamhouse wastes
only. The addition of the spent vegetable tan liquors
eliminated the odors completely.
12. Foaming of the aerated lagoons occurred periodi-
cally and was severe enough to prohibit the location of
such a system near residential or commercial areas. High
pressure water jets were effective in controlling the foam
when air temperatures were above freezing but could not be
used during the winter months.
13. Loading intensities as high as 20-25 pounds of
BOD per day per 1,000 cubic feet of lagoon capacity were
employed in the pilot plant studies. The loading intensity
for the full-scale system ranged from 2 to 20 pounds per
day per 1000 ft 3 . The reduction in BOD through both the
pilot and full scale units normally ranged from 8095
percent. During cold weather when the water temperature in
the full-scale lagoon dropped to 33-34°F. for an extended
period of time BOD reductions of 65 to 75 percent were
obtained.
14. Little reduction in colbr of the spent tan liquors
was achieved in the biological system. It was found that
the color could be precipitated either before or after
biological treatment by raising the pH of the wastes to
11.5 or greater with lime. The resulting precipitates,
however, were voluminous and settled poorly. In some cases
settling was improved by use of polyelectrolytes.
15. The final effluent from the full scale lagoon
system contained from 100-200 mg/l of suspended solids.
The settleable solids level, however, was near zero through-
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out the period of study.
16. Large numbers of bacteria were present in the
final effluent. Adequate disinfection was achieved with
chlorine at a dosage of about 30 mg/i and a 15-minute con-
tact period. The treated waste exerted an extremely high
chlorine demand but the reaction was sufficiently slow to
permit high bacterial kills before the chlorine disap-
peared.
17. The installed cost of the Narlinton system was
approximately $40,000. The operating costs are estimated
at about $15,000 per year or $0.07/hide processed based
on a production level of 800 hides per day.
18. Further research is needed to provide additional
operational and performance data for the anaerobic-aerobic
lagoons during the winter months.
19. A further definition of the bacteriological
characteristics of tannery wastes is needed along with
more refined studies on disinfection requirements and pro-
cedures.
20. Studies on the combined treatment of domestic
sewage and sole leather tannery wastes in anaerobic-aerobic
lagoons are needed. Most of the sole leather tanneries
remaining in operation are located near communities where
joint treatment would be physically possible.
21. More research work is needed on the removal of
the color from spent vegetable tan liquors. It is likely
that such information would be of value in the treatment
of other types of wastes containing vegetable extracts.
4
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Section 2
Introduction
The tanning industry long has been recognized as a
major contributor to water pollution because of the high
concentrations of organic and inorganic substances present
in untreated tannery effluents. The overall volume of
tannery wastes in the United States, however, amounts to
only about 16 billion gallons per year with the sole
leather tanneries contributing approximately 10 percent of
this volume. On a national basis, therefore, the wastes
from sole leather tanneries are relatively insignificant
whereas on a local or regional basis they often are of a
major concern.
It is of interest to note that some of the earliest
work on industrial waste treatment in the United States
was devoted to finding acceptable means for treating
tannery wastes. The annual reports of the Massachusetts
State Board of Health describe laboratory and pilot plant
studies on tannery waste treatment from 1850 to about 1910.
The Public Health Service performed extensive waste treat-
rnent studies at various tanneri s in the period from 1912-
1914 (1). Following the Public Health Service work, in-
vestigators for the tanning industry, both in the United
States and abroad, conducted many studies on the treatment
of tannery wastes alone and in combination with domestic
wastes (2,3,4,5,6,7,8,9,10,11 and 12).
While the research effort has been extensive, few
full scale treatment plants have been built for handling
tannery wastes. A detailed investigation of the tanning
industry in the United States in 1965-66 revealed that
while a number of tanneries were served by various treat-
ment procedures no tannery had acquired a treatment
system that was completely satisfactory. Operational data
gathered during the survey indicated that most of the
systems had been improperly designed from the standpoint
of the effects of specific constituents of tannery wastes
on conventional waste treatment processes.
The tanning industry, however, recognized the need
for finding acceptable means of waste treatment which
might be employed throughout the industry. In 1965 the
Tanners Council of America retained the Author as a
consultant on waste management. During 1966 a laboratory-
pilot plant study on the treatment of beamhouse wastes
5
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from a sole leather tannery was carried out at the Inter-
national Shoe Company Tannery located at Marlinton, West
Virginia. This study was sponsored jointly by the Tanners
Council of America, the Water Resources Commission of West
Virginia and the University of Cincinnati. The data
derived from the pilot plant study formed the basis for
the Demonstration Project described in this report. This
Demonstration Project supported by the Federal Water
Pollution Control Administration also was conducted at the
Marlinton Tannery.
Approximately 160 persons are employed at the Tannery
and about 800 heavy steer hides are processed into sole
leather on each of the five working days per week. While
many individual steps are required for converting the
hides into leather they can be grouped under two major
operations, beamhouse and tan yard. In the beamhouse
operations the hides are prepared for tanning and in the
tan yard the skins are converted into sole leather. Salt
cured hides are used.
In the beamhouse operations, the hides are initia].ly
washed and soaked to remove curing salt, extraneous dirt,
blood, and manure and to soften the hides. After the hides
are washed and soaked, they are immersed in a lime-sulfide
solution in still vats or pits. The lime and suif ides
dissolve the unwanted hide substance and loosen the hair.
After the hides are removed from the lime vats, they are
rinsed to remove excess chemicals, unhaired, fleshed, and
sent on to the bating process. Bating consists of washing
the hides in a solution containing wetting agents, enzymes,
and arnmonium salts to remove excess lime and to further
prepare the hides for tanning.
In the tanning operation the hides are gently rocked
for a period of several weeks in a solution made from veg-
etable extracts. The vegetable extracts react with the
collagen fibers to produce leather. Following the tanning
step, the leather is run through a bleaching process to
remove excess tannin and to give the desired color control.
Final finishing operations for sole leather are mainly
mechanical in nature and are designed to impart specific
characteristics to the leather.
The major parameters used for characterizing sole
leather tannery wastes are pH, chlorides, BOD, COD, chlorine
demand, total solids, suspended solids, ammonia, organic
nitrogen, alkalinity, sulfides, and color. Most of the
pollutants stemming from sole leather tanning processes are
found in the initial wash and soak waters, the spent lime
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liquors and the spent vegetable tanning solutions.
The beamhouse wastes have a high concentration of BOD,
COD, suspended solids, ammonia, organic nitrogen, suif ides,
chlorides, and alkalinity. The p 1-I of the total beamhouse
wastes ranges from 11.5 - 12.5. The major pollutants found
in the beamhouse wastes initially are contained in
relatively small batch volumes of waste.
The spent tan liquors are extremely high in color and
COD and moderately high in BOD. The pH averages about 4.5
and the acidity is sufficient to reduce the pH of the total
tannery wastes to about 9.5 when all waste streams are
mixed.
The major waste fractions stemming from the tanning
operations are illustrated in Figure 1. Some of the more
important characteristics of the individual waste streams
are tabulated in Table 1.
Table 1: Characteristics of Tannery
Waste Fractions
Waste Fraction Flow COD Suspended pH
Solids
(tgpd) (mg/i) (mg/l)
Wash Water 25 2100 1300 6.8
Soak Water 10 2200 1000 7.8
Lime Water 10 11900 30300 12.3
Rinse Water 20 2500 4900 12.3
Hair Water 15 2500 3100 12.3
Fleshing Water 5 3600 4900 12.3
Bate Water 55 1700 1000 9.0
Spent Tan Liquors 60 10000 500 4.5
Note: 1 tgpd = 3785 liters per day tgpd - 1,000 gal/day
As shown in Table 1, the lime vat, rinse vat, and hair
washer waters contain moderate to high concentrations of
COD and suspended solids (mostly Ca(OH) 2 ) and have a high
pH; yet they make up only 32 percent of the beamhouse waste
water volume. The wash, soak, and bating waters represent
64 percent of the waste volume, but are moderate to low in
COD and suspended solids and near neutral in pH.
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KEY:
HIDES
WASTES
LEATHER
Ill
Cu RED
TANNING
HIDES
BEA1 HO USE
FIGURE 1.
SOURCES OF MAJOR WASTES
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When the concentrated waste fractions are mixed with
the large volumes of wash waters and other less concen-
trated wastes, the resulting or final bearnhouse waste
stream is large in volume and still grossly polluted. For
example, lime while soluble to a rathar limited extent in
water will continue to dissolve as the liquors containing
high concentrations of suspended lime are mixed with non-
lime bearing wastes thereby increasing the hardness,
alkalinity, and pH of the combined waste streams.
The spent tan liquors when mixed with the beamhouse
waste streams containing lime yield a voluminous precipi-
tate which is difficult to separate from the liquid phase.
In addition the colored compounds present in the spent
tan liquors are sufficiently concentrated to impart an
extremely intense color to the total tannery wastes.
In general, small volumes of concentrated wastes are
easier and more economical to treat than large volumes of
a more dilute waste. Also in many cases it is easier to
remove the pollutants from the individual waste streams
than from the combined wastes.
It was determined, therefore, that the basic approach
to be used for the Narlinton project would be that of re-
moving the pollutants from the individual waste streams
when feasible. Waste streams were to be mixed only after
pretreatment or when such mixing could be justified in
terms of economy or ease of treatment.
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Section 3
Experimental and Operational Findings
Research Plan :
The basic plan utilized in this investigation con-
sisted of separating the beamhouse waste streams, removing
the excess suspended lime, and blending all waste streams
for final treatment by biological means. Pilot plant
studies were used to provide design data for the full scale
system. In general, each unit or treatment process was
constructed and evaluated before the next downstream unit
was constructed. This step-by-step procedure provided a
desired degree of flexibility to the design of the total
system and allowed for easy modification when changes had
to be made in the basic plan.
Removal of Suspended Lime :
A review of the literature showed that many investi-
gators believe that the excess suspended lime is the major
complicating factor in the treatment of bearnhouse wastes
because of its tendency to form calcium carbonate scale on
the surfaces of conduits, containers and mechanical equip-
ment. The high pH resulting from the lime also precludes
any form of biological treatment for reduction of the BOD
of the wastes unless the waste is partially neutralized.
Neutralization of the excess lime with acid is costly and
leaves the waste with a high calcium content. Also
neutralization with acid must be controlled carefully be-
cause of the danger of liberating hydrogen sulfide from
the sulfides contained in the waste. Flue gas sometimes
is used to neutralize the excess alkalinity.
Ceamis (13), Jansky (14), Rosenthal (15), Guerree
(16) and Eye and Graef (17) have shown that the combined
tannery wastes are ameanable to biological treatment if
the suspended lime is removed as a pretreatment measure.
Ceamis (13), Jansky (14) and Domanski (18) investigated
the use of iron salts as coagulants for the limebearing
waste fractions. Sproul (19), Scholz (20) and Eye and
Graef (17) have reported on the use of polyelectrolytes in
tannery waste treatment.
A laboratory study was conducted to determine the
effectiveness of polyelectrolytes as a flocculant for the
lime-bearing beamhouse effluents. From correspondence
with several manufacturers it was learned that the beam-
house waste water characteristics, i.e. high pH, colloidal
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lime and soluble protein, dictated the use of anionic,
rather than cationic or non-ionic polyelectrolytes. This
information was substantiated later in the study.
Jar tests, performed to determine which waste
fractions could be flocculated by an anionic polyelectro-
lyte, showed that the lime-bearing waters (i.e. lime vat,
rinse vat, and hair washer waters) could be treated
readily. Table 2 contains the jar test data.
Table 2: Flocculation of Beamhouse Waste Fractions
by an Anionic Polyeiectrolyte
Waste Fraction
Results
Dosage
Wash Water
NF
-
Soak Water
NP
-
Lime Water
EF
6
mg/i
Rinse Water
EF
6
mg/i
Hair Water
EF
10
mg/i
Fleshing Water
NF
-
Bate Water
NF
-
Note: NF = No flocculation
EF = Excellent flocculation
Jar tests were performed to determine the optimum
dosage of anionic polyelectrolytes. Dosages of 0-60 mg/i
of polymer were evaluated using rapidity in settling,
density of floc and clarity of supernatant as criteria.
Dosages of 8-60 mg/i gave satisfactory removal of the
suspended lime, but there was only minor improvement in re-
movals at dosages above 20 mg/i.
A small pilot plant was constructed and operated on a
batch basis to further define the settling characteristics
of the suspended lime particles. Polyelectrolyte dosages
from 0 to 50 mg/i were investigated. Little improvement in
the rate or degree of clarification was noted at dosages
above 10 mg/i. It also was found that 5 mg/i gave approxi-
mately the same removal of suspended solids as 10 mg/i.
The rate of settling at the 10 mg/i dosage, however, was
twice as great as for 5 mg/i and a dosage of 10 mg/i was
used for design purposes.
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Typical results obtained from the pilot plant studies
at a polyelectrolyte dosage of 10 mg/i are presented in
Table 3 and illustrated in Figure 2.
Table 3. Results
of Pilot
Plant
Clarification
Waste
Suspended Solids
mg/i %Reduction
mg/i
COD Alkalinity
%Reduction %Reduction
Lime 6,000
Clar. Lime 1,650 72.5 66.7
Lime 9,700
Clar. Lime 2,400 75.3
Lime 4,900
Clar. Lime 1,550 68.4 60.0
Lime 11,200 4,100
Clar. Lime 1,650 85.1 2,750 33.0 77.4
Lime 18,500 4,200
Clar. Lime 3,500 81.1 2,650 37.0 85.6
Lime 15,400 4,600
Clar. Lime 4,000 74.1 2,150 53.0 84.3
Lime 16,700 2,850
Clar. Lime 2,100 87.4 1,750 38.5 81.7
Lime 12,350 3,140
Clar. Lime 3,400 72.5 2,320 26.0 80.5
Lime 12,750 3,040
Clar. Lime 1,950 84.7 1,890 38.0 87.2
The data derived from the small scale pilot unit were
used to design a larger pilot plant which was constructed
adjacent to the bearnhouse and operated on a continuous f low-
through basis. The results obtained from the larger pilot
unit verified the optimum polyelectrolyte dosage of 10 mg/i
as well as the necessity of separating the lime-bearing
wastes from the other beamhouse waste fractions. From the
data obtained from the pilot plant clarifier it was con-
cluded that suspended solids removals of 90 percent and 70
percent could be achieved at overflow rates of 2,000 gpd/ft 2 ,
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100
7
a _ o
0
0
0
WASTE WITHOUT
POLYELECTROLYTE
-I
LU
C,)
C /)
LU
LU
C /)
=,
C,,
2.
10 MG/L
POLYELECTROLYTE
0
SETTLING TIME - MINUTES
FIGURE 2.
SETTLING CURVES FOR LIME BEARING WASTES
-------
and 3,000 gpd/ft 2 respectively.
Settling tests conducted in a settling cylinder re-
vealed that the polyelectrolyte treated lime waters ex-
hibited flocculent settling for a short period of time
followed by hindered settling. Settling curves for two
concentrations of suspended solids are shown in Figure 3.
Analysis of the settling curve data indicated that for
quiescent settling overflow rates as high as 3500 gpd/ft 2
could be utilized. By contrast without polyelectrolytes
the maximum calculated overflow rate was less than
100 gpd/ft 2 .
The success achieved in the pilot plant studies
prompted a decision to design and construct a full-scale
system to clarify the total lime-bearing wastes discharged
from the beamhouse. A preliminary plan for separating
the waste fractions was developed and the clarification
unit complete with polyelectrolyte feeding equipment was
designed.
Design and Construction of the Full-Scale Clarification
System :
The layout of the process units and the sewer system
at the start of the project is illustrated in Figure 4.
The wastes discharged from the 10 initial soak vats and
the 30 lime-sulfide and rinse vats were carried in a
common sewer located beneath the battery of vats. Con-
struction of an auxiliary sewer underground to serve the
soak vats independently of the lime vats would have been
extremely difficult and expensive. It was decided, there-
fore, to empty the soak vats by use of a pump and an
overhead piping system.
A self-priming non-clog pump was connected to a main
header pipe which in turn was connected to a riser pipe
in each of the ten soak vats. Each riser pipe was
equipped with a fast acting, manually operated valve.
When a vat is to be drained, the pump is started and the
appropriate valve is opened. The pump switch is controlled
by an adjustable timer which automatically stops the pump
after a predetermined time interval which is just
sufficient to allow a vat to be emptied. This arrangement
was inexpensive, easy to construct, and has presented few
operational problems.
The initial wash waters were re-routed to a sump
along with the initial soak waters. A float actuated pump
15
-------
20
16
12
S
4
00
LU
L)
LL
LU
LL
=
LE
LU
=
Co = 29 000 MG/L
Co = 18 000 NG/L
2 4 6 8 10 12 14
SETTLING TIME - MINUTES
FIGURE 3.
SETTLING RATES FOR LIME SLUDGE
-------
WASH SOAK LIME
ORIGINAL SYSTEM
BEAI9HOUSE
SUMP
REVISED SYSTEM
CLARIFIER
FIGURE LI. SEWERAGE SYSTEM SERVING BEAMHOUSE
-------
delivers the wash and soak waters to a 20 mesh, 30 inch
diameter vibratory screen for removal of hair and other
extraneous matter derived from the initial processing of
the hides. After screening this waste stream is dis-
charged into the main sump serving the entire beamhouse.
The revised flow diagram for the bearnhouse sewerage
system also is illustrated in Figure 4. Since the lime
bearing wastes are discharged intermittently over an
eight hour period on each working day, it was determined
that a holding sump would be advantageous from the stand-
point of clarifier operation. A sump with a capacity of
about 2,000 gallons was constructed near the end of the
lime liquor discharge channel and the lime liquors di-
verted to the sump. A float actuated pump was installed
in the sump to pump the lime bearing wastes to the
clarifier. Provision was made to inject the polyelectro-
lyte solution into the discharge line from the sump pump
by means of a small gear pump which operates only when
the main pump is running. The discharges of the sump
pump and the chemical feed pump can be adjusted to
accomodate flows in excess of 100,000 gallons in an eight
hour period.
The clarifier was designed to provide a detention
time of 30 minutes and an overflc w rate of 2,000 gpd/ft 2
at a feed rate of 150 gpm. A cylindrical steel tank 12
feet in diameter and 11 feet deep was selected. These
dimensions met the design requirements and more
importantly permitted the tank to be fabricated at the
factory and transported to the site by truck. The cost
of factory fabrication was approximately 50 percent less
than for field construction of a similar unit.
Mixing and flocculation of the lime-liquor poiy-
electrolyte mixture was accomplished by constructing a
baffled inclined feed trough leading to the center feed
column which also was equipped with baffles. The feed
trough and center feed column were fabricated from steel
barrels welded together end to end. The clarifier,
therefore, was constructed to function as an upf low unit.
Sludge is withdrawn through a perforated steel pipe
placed on the bottom of the clarifier and connected to a
sludge pump. The details of the clarification system
are shown in Figure 5.
18
-------
MIXI NG H
SLUDGE
REMOVAL
PIPE
FIGURE 5
UPFLOW CLARIFIER DETAILS
SLUDGE
OUT
19
-------
Performance of the Clarifier :
The performance of the clarifier was evaluated during
the early part of the study period by measuring the re-
duction in suspended solids, alkalinity, and chemical
oxygen demand through the unit, Table A-i and Figure 6.
The data show that wide variations in removal efficiency
occurred even at relatively low overflow rates. Factors
found to be contributing to the poor removals included:
1) the total suspended solids removals were adversely
affected by the volatile solids composed of grease and
hair which did not settle; 2) the influent samples were
not reflecting the actual suspended solids concentration
present because of clogging of the sampling device by
grease and hair; 3) there was evidence of solids wash-
out from the clarifier resulting from too great an accumu-
lation of sludge in the unit and 4) the soluble portion
of the total alkalinity showed considerable variation
from day to day.
A revision in the sampling and operational schedule
for the clarifier during March, 1968 improved the percent
removals of suspended solids. The chemical oxygen demand
data accumulated during this period indicated that some
reduction in organics was being achieved in the clarifier
although the percent reduction varied widely from day to
day. The data for the month of May, Table 4, show that
increasing the dosage of polyelectrolyte to 15 mg/i had
little effect on the clarifier performance. During June
and July even closer attention was given to maintaining
a constant overflow rate as well as to preventing too
great an accumulation of sludge in the clarifier.
The data presented in Table A-2 show the pronounced
effect of close operational control of the clarifier on
the performance. The data likewise show that the fixed
suspended solids were being removed about as predicted
by the pilot plant studies. Subsequent experiments on
prolonged operation of the clarifier at overflow rates
generally in excess of 2000 gpd/ft 2 and at polyelectro-
lyte dosages below 10 mg/i indicated that reasonable
removals of fixed suspended solids can be achieved, Table
A-2.
The data shown in Figure 7 iLlustrate the effective-
ness of removal of suspended solids at two overflow rates
for a polyelectrolyte dosage of about 10 mg/i. In general
20
-------
0
0 0
TOTAL ALKALINITY
POLYELECTROLYTE
DOSAGE --- 8-13 MG/L
0
0
0
0
0
0
0
0
0
I I I I ,0
L100
600
1000
- GPD/FT 2
1200
1400
0
o 00
0O
000
0
00
0
0
i oo
I
FIGURE 6. CLARIFIER PERFORMANCE
.LUU
SUSPENDED SOLIDS
S
S
S
S
S
S
1. 5
80
60
40-
-J
uJ
L)
uJ
0
0
0
800
OVERFLOW RATE
-------
Table 4:
Performance of Clarification System
5/20/68 3840
21 3620
400 89.6
340 90.6
3334 2168 35.0
4008 1494 62.6
15.3
14.5
1590
1590
Date Suspended
Solids
Inf.
Eff.
Removal
mci/i
mci/i
%
COD
Inf. Eff.
Removal
%
Dosage
A_10*
mg/i
Overflow
Rate
qpd/ft 2
9
2900
540
81.4
4012
2247
44.0
10.4
1610
10
3480
240
93.1
4086
1835
55.2
10.4
1610
11
3040
440
85.5
3898
1965
49.6
9.6
1610
12
2720
420
84.6
3271
2775
15.2
9.9
1610
4/15/68
3960
520
86.9
3444
2084
39.5
10.9
1560
16
3960
620
84.3
4488
2947
34.4
10.2
1580
17
6000
560
90.7
4972
2591
47.7
9.9
1610
18
4120
560
86.4
4582
2609
43.2
9.8
1590
19
4800
1020
79.8
5524
3039
45.0
9.9
1590
22
6180
700
88.7
5530
2974
46.2
10.0
1590
4/23/68
3620
660
81.8
4820
3150
34.6
10.0
1590
24
3420
160
95.3
4428
2767
37.5
10.0
1590
25
5600
620
88.9
4968
2863
42.4
10.9
1590
26
5480
800
85.4
4253
2405
43.3
16.6
1590
29
4720
200
95.8
3479
2578
25.9
16.6
1590
5/13/68
3920
840
78.6
4806
2607
45.7
15.3
1590
14
3520
560
84.1
2654
1669
37.1
15.1
1590
15
3740
460
87.7
2815
1743
38.2
15.8
1590
16
4260
220
94.8
3616
1800
50.2
14.4
1590
17
5200
500
90.4
4913
2085
57.6
14.1
1590
*Rohm and Haas
-------
Table 4:
Performance of Clarification System
Suspended
Inf. Eff.
mg/i mg/i
Solids
Removal
COD
Inf. Eff. Removal
Dosage
A-lO
mg/i
Overflow
Rate
gpd/ft 2
Date
5/22/68
3600
540
85.0
3414
1870
45.6
14.8
1590
23
5060
380
92.5
4001
1924
51.7
15.4
1590
24
3400
520
84.7
3574
1989
44.4
14.4
1590
27
5000
500
90.0
4760
2483
47.7
15.1
1590
28
4480
280
93.8
3508
1912
45.5
15.1
1590
29
4140
560
86.5
3388
1686
50.1
16.0
1590
31
3460
180
94.8
3266
1856
43.1
15.7
1590
6/3/68
4080
400
90.2
4282
2164
49.3
15.0
1590
-------
9O
0-
I I
10 20 30 140 50 60 70 80
O.R 1 = 1600 GPD/FT 2
° °° O.R = 2450 GPD/F1 2
A-lU DOSAGE 8 7 - 1O 8 MG/L
PERCENT OF OBSERVATIONS =
I I I I
90 95 98 99 ,5
FIGURE 7,
0 0
.0 0
0 o_-
85
80
75
70
65
60
C D
uJ
C)
J
C D
C)
L J
cL
C)
C )
0
1
5
OVERFLOW RATE VS SUSPENDED SOLIDS REMOVAL
-------
he removal of suspended solids exceeded 80 percent even
at the higher overflow rates. The effect of polyelectro-
lyte dosage on fixed suspended solids removal is
illustrated in Figure 8. The average removal was about
8 percent greater at polyelectrolyte dosages of 7-11 mg/i
than at 4-7 mg/l for the same range of overflow rates.
The dosage of polyelectrolyte used in this system was
higher than normally considered economical in water and
waste treatment. Only the lime bearing waste fractions
which represented about 30 percent of the beamhouse flow,
however, required treatment and the actual weight of
polyelectrolyte used each day was relatively small.
The annual operating costs for the separation and
clarification system are estimated to be:
Electrical power $ 200
Truck for sludge 500
Polyelectrolyte 800
Repair and Maintenance --- 500
Labor 3,000
$5,000
Characteristics of the Lime Sludge :
The sludge was withdrawn from the clarifier through a
perforated pipe on the bottom of the unit and pumped to a
1000 gallon tank mounted on a truck chassis. The sludge
was used for landfill without further dewatering. The
average volume of sludge produced per week (5-working days)
was about 10,000 gallons or about 3 percent of the volume
of lime-bearing wastes clarified. The solids content of
the sludge as removed from the clarifier ranged from a low
of 7.2 percent to a high of 29.8 percent. The average
solids content of the sludge was 14.1 percent. Only ten
loads out of a total of 237 had a solids content less than
10 percent and eleven loads exceeded 20 percent. The
usual variation in solids content, therefore, was
relatively small.
The sludge exhibited excellent drying characteristics.
A number of experiments on dewatering the sludge on beds of
flyash revealed that the sludge drained readily even during
periods of cold, wet weather. In general the sludge
cracked and could be removed from the drying beds in two to
three days. The dried sludge was flaky and did not exhibit
any tendency to accumulate additional water from rain or
melting snow.
25
-------
100
/
/ 0
ob 0
/
I I I
20
140
60
A-1O DOSAGE 7-11 MG!L
0- o- - A-lU DOSAGE 14-7 MG/L
0 1 R. = 2300 - 2700 GPD/FT 2
OPERATING PERIOD: 10-1-68 - 2-28-69
I I
80 100
PERCENT OF OBSERVATIONS =<
FIGURE 8.
POLYELECTROLYTE DOSE VS FIXED SUSPENDED SOLIDS REMOVAL
go -
.
S
.-,--
80
a- 0 0
-J
LU
( 1)
-J
C,)
LU
LU
C,)
=,
( /)
LU
><
-l
U-
0
o
0
9-
0
-
0
0
000
1
70-
60 d
-------
The results of one drying experiment in which the
sludge was placed on flyash beds four feet square are pre-
sented in Table 5.
Table 5:
Time
Days #1
Sludge
#2
Drying
#3
Charact
#4
eristics
Weather
Type
Temp.
0
2
4
6
8
Clear
25°F.
1
1/4
1/2
11/4
2
Cloudy
28°F
2
1/4
1/2
11/4
2
Snow
22°F.
This aspect of the study is of particular importance be-
cause lime sludge normally is difficult to dewater
effectively. The dried lime sludge can be used for land-
fill or for certain agricultural purposes.
Biological Treatment :
Separation and pretreatment of the various waste
fractions while effective in removing the inert suspended
solids effected only a limited reduction in the total
organics contained in the wastes. The BOD (5-day, 20°C)
of the pretreated and blended waste streams from the beam-
house ranged from 1000 - 1500 mg/i and the COD from 2000 -
3000 mg/l. The total tannery wastes after pretreatment
and blending had a BOD of 1500 - 3000 mg/i and a COD of
4000 8000 mg/i. The total Kjeidahi nitrogen concentrations
in the beamhouse wastes and the total tannery waste averaged
about 200 and 150 mg/i respectively.
It was decided that the use of a biological system for
removing organics would be investigated. The economic
position of the sole leather industry dictated that the
treatment system selected for reducing the organics have a
low capital and maintenance cost and be relatively easy to
operate and maintain. Another important consideration in
the selection of a system for removing the organic s was
that the production of sludge be minimal so that extensive
drying facilities would not be required.
27
-------
A combination of anaerobic and aerobic biological
units appeared to meet the basic requirements established
for the system, particularly if they could be combined in
a lagoon or series of lagoons. Ivanof (21) and Toyoda
(22) reported on the successful treatment of sole leather
tannery wastes by anaerobic means. Gates and Lin (23)
conducted laboratory and pilot plant studies on a
stratified anaerobic-aerobic lagoon process and found it
applicable to treating tannery wastes.
A decision was made to explore the feasibility of
combining an anaerobic and an aerobic biological process
in a deep lagoon to achieve the desired removal of
organics. A deep lagoon equipped with a floating aerator
arranged to aerate only the upper zone of the wastes being
treated offered the potential advantages of: 1) low
construction cost where soil conditions were favorable;
2) small land area requirements; 3) low volume of sludge
accumulated; 4) reduced air requirements for the aerobic
system since some organics would be eliminated in the
anaerobic zone; and 5) heat conservation during winter
operation. The large volume of wastes undergoing bio-
logical breakdown also would tend to protect the biolog-
ical system against shock loads which are always possible
from batch operations in a sole leather tannery. This
concept was evaluated in pilot plant and full scale
studies.
Pilot Plant Studies on Beamhouse Wastes :
Samples of pretreated beamhouse waste fractions were
blended in proportion to their respective volumes
discharged from the tanning operations. The mixed wastes
with the pH adjusted to about 8.5 were used as the feed
to the anaerobic unit. The anaerobic feed volume was five
liters per day, five days per week. The five liters were
introduced continuously over a period of 15-30 minutes,
while simultaneously five liters were withdrawn and dosed
to the aerobic unit. An overflow siphon was attached to
the aerobic tank in such a manner that a volume of ten
liters was always maintained. Therefore, as five liters
were added to the unit five liters were discharged as
effluent.
The anaerobic unit was acclimated to the pretreated
tannery waste water initially by adding one liter of
partially digested primary sludge from a domestic sewage
treatment plant and one liter of composted beamhouse
sludge to the 35-liter anaerobic unit. The container was
28
-------
then filled to the 35-liter mark with raw sewage from a
municipal outfall. On the second or following day one
liter of the neutralized, blended tannery waste water and
four liters of raw domestic sewage were added to the tank.
The five liters added caused the displacement of five
liters of the previous contents of the tank. On the third
day, two liters of tannery waste water and three liters of
raw domestic sewage were added to the unit. On each
subsequent day the tannery sewage addition was increased
by one liter, while the raw domestic sewage addition was
decreased one liter. After six days the unit was consid-
ered acclimated. The anaerobic unit was then fed with
five liters of the neutralized blend on five days per
week. The operational data for the anaerobic unit are
listed below:
Volume = 1.2 cubic feet
Influent COD = 1000-2500 mg/i Avg. 1550 mg/l
Effluent COD = 500-1500 mg/l Avg. 780 mg/i
% Removal = 50%
Loading Intensity = 15 lb COD/bOO cu.ft./day
Detention Time = 1.4 weeks = 9.8 days
Temperature Range = 25-38°C. Avg. 30°C.
The aerobic unit was acclimated by starting with ten
liters of raw domestic sewage and then adding five liters
of anaerobic effluent each day thereafter. The operating
characteristics of the aerobic unit are tabulated below:
Volume = 0.34 cubic feet
Influent COD = 500-1500 mg/i Avg. 780 mg/i
Effluent COD = 150-500 mg/i Avg. 275 mg/i
Removal, % = 65
Loading Intensity = 25 lb COD/bOO cu.ft./day
Detention Time 0.4 week - 2.8 days
Temperature Range = 20-38°C. Avg. 30°C.
A summary of the performance of the biological system
is shown in Table 6 on the following page.
In the anaerobic zone the pH was reduced and the
total sulfide concentration was increased. The pH re-
duction can be attributed to the organic acids and carbon
dioxide liberated by the anaerobic bacteria. The increase
in total sulfides was a result of the conversion of the
29
-------
Table 6: Influent and Effluent Characteristics
of the Pilot Biological Units
Waste Anaerobic Anaerobic Aerobic
Parameter Influent Effluent Effluent
COD
1,550
mg/i
780
mg/i
275
mg/i
Total solids
12,500
mg/i
10,900
mg/i
10,300
mg/i
Dissolved solids
10,800
mg/i
10,000
mg/i
9,500
mg/i
Suspended solids
1,700
mg/i
900
mg/i
800
mg/i
Total sulfides
75
mg/i
300
mg/i
5
mg/i
pH
8.59.0
7.8
8.0
sulfate and organic sulfur to sulfide by anaerobic orga-
nisms. The net reduction of COD, therefore, is not
indicative of the total stabilization achieved in the
anaerobic unit because the sulfates reduced to suif ides
would register as additional COD in the effluent.
Considerable reductions in COD and sulfides were
achieved through aerobic treatment of the anaerobic
effluent. The solids levels, how ver, remained relatively
unchanged. The data obtained from the pilot unit proved
conclusively that the pretreated beamhouse wastes were
ameanable to biological treatment. It was shown also that
a stratified anaerobicaerobic unit would meet the con-
ditions specified for an acceptable system for reducing the
organic components of the waste to ΰn acceptable level.
Design of Stratified Anaerobic-Aerobic Lagoons :
The data obtained from the pilot plant study indicated
that a full scale lagoon providing a detention time of 8
10 days would yield satisfactory reduction in the organics
of the beamhouse wastes as measured by the COD. The
criteria used to design a unit capable of treating the
total beainhouse flow are listed in Table 7 on the following
page.
The capacity of the aeration equipment needed to meet
the oxygen requirements of the wastes in the aerobic zone
of the lagoons was difficult to predict. Laboratory
studies indicated that the soiubility of oxygen in untreated
beamhouse wastes was considerably lower than in ordinary
tap water. Furthermore, no reliable data on oxygen
transfer capability of floating aerators operating in
30
-------
Table 7: Design Criteria for Stratified Lagoons
Flow: - 150,000 gpd - 750,000 gals/week
COD: 2,500 lb/day 12,500 lb/week
BOD: 1,200 lb/day 6,000 lb/week
Det. Time (Theoretical)
Anaerobic zone: 5 days
Aerobic zone: 3 days
Number of units: 2
Dimensions of each unit: lOOxlOOxl2 deep
Effective volume: 160,000 cu.ft.
Loading intensity: 16 lb/COD/bOO cu.f t./
day
tannery wastes were available. In addition considerable
BOD would be contributed by the spent tan liquors if and
when they were mixed with the bearnhouse wastes for bio-
logical treatment.
The design of the aerators to accomodate the total
wastes was based on the following assumptions:
Oxygen required per week 10,000 lb.
Oxygen transferred per hour per H.P. -- 2 lb.
Total horsepower required 30
Operating and Performance Characteristics of Lagoons :
The lagoons were constructed late in 1967 but were
not placed in operation until the summer of 1968. Three
floating aerators, a 5 H.P., a 10 H.P., and a 15 H.P.
were purchased and installed in the lagoons. The 5 H.P.
unit was operated continuously for about five months
while the pH of the lagoon was maintained at 12.0 or
greater to evaluate the possibility of foaming and scaling
problems. The layout of the lagoon system is illustrated
in Figure 9.
During the late spring and early summer of 1968,
spent bleach acid was mixed with the clarified beamhouse
wastes to give partial neutralization of the residual
caustic alkalinity. In July, 1968 sufficient concentrated
sulfuric acid was added to the lagoons to reduce the pH to
approximately 9.0. The aerators were started and almost
immediately there was evidence of biological activity.
31
-------
BYPASS ROUTE
BEAMHOUSE
TO RIVER
SPENT TANS TO OFFSITE STORAGE
LAGOON SYSTEM AT PLANT SITE
FIGURE 9.
-------
The pH of the lagoons started dropping and it became
apparent that continued neutralization of the caustic
alkalinity with spent bleach acid was unnecessary. The COD
of the effluent from the secondary lagoon (L-2) which was
already on the decline following the reduction in pH
dropped rapidly. After approximately one week, the COD of
the primary lagoon (L-l) also showed a marked decline. The
dissolved oxygen content of both lagoons was only about
one mg/l at the surface and near zero at a depth of four
feet.
Pronounced odors emanated from the lagoon system and
efforts to control the odors by use of odor counteractants
were unsuccessful. The odors were particularly critical
as the lagoons were located in close proximity to a number
of residences. At no time, however, was there any evidence
of hydrogen sulfide being released from the operating
lagoons.
The effluent from L-2 was passed through a small
earthen clarifier equipped with vacuum sludge return lines.
While the amount of settleable solids in the effluent was
negligible 20-40 percent of the flow was re-cycled through
L-2 for the purpose of adding an acclimated bacterial
population to the incoming wastes. The effluent from the
clarifier was discharged into two existing lagoons which
contained a heavy accumulation of lime sludge. Soon aftei
startup of the biological system, a heavy growth of algae
was observed in the old lagoons which were receiving the
effluent from L-2. Microscopic examination revealed the
presence of a single species of motile algae plus many types
of protozoa. The treatment achieved in the lagoon system,
therefore, rendered the wastes suitable for supporting a
variety of microscopic organisms.
Over a period of several weeks the algae became so
dense that the dissolved oxygen was completely depleted
during night time and hydrogen sulfide was released from
the bottom deposits. Thus, while hydrogen sulfide was no
problem in the operating lagoon, it became a serious
problem in the lagoon which received the treated effluent.
Some ten houses adjacent to the old lagoon showed severe
darkening of the paint and reimbursement of the owners by
the insurance company was necessary.
A survey of the operating lagoons revealed a sludge
blanket approximately six feet in thickness in L-l and
from a few inches up to two feet in L-2. The sludge re-
sulted from the precipitates that formed upon neutraliza-
tion of the clarified lime liquors with the spent bleach
33
-------
acid. After operating both lagoons for about three weeks
it became apparent that the rate of oxygen utilization
exceeded the capacity for re-aeration with the 30 H.P. of
available aeration equipment.
It also was found that large quantities of lime and
soda ash were needed to keep the pH above 8.0 which was
deemed to be the lowest permissible level because of the
soluble sodium sulfide in the wastes. Consequently after
about one month of operation, L-l was rendered inactive by
increasing the pH to about 12.0. All of the aerators were
transferred to L-2 which had a volumetric capacity of about
0.6 million gallons.
The COD of the effluent from L-2 continued to decrease
until it reached a value of about 900 mg/i, Figure 10. At
this time a mixture of domestic sewage and river water was
added to L-2 so as to achieve a more balanced biological
population. Low D.O. values continued as did the odors
although the odors could be controlled by the addition of
ammonium nitrate. The control of pH was extremely
difficult requiring the addition of several hundred pounds
of soda ash each day. Much of the lime sludge removed
from the clarifier also was added to L-2. This extra
alkalinity coupled with a caustic alkalinity of 300800
mg/i in the influent to L-2 mainta 1 ined the pH at about 8.0-
8.2.
Dissolved oxygen values observed for L-2 are listed in
Table 8. The data listed in Table 9 show the alkalinity
and hardness relationship between the influent and effluent
from L-2.
The data indicate that little bicarbonate alkalinity
existed in the influent whereas the total alkalinity of
the effluent was in bicarbonate form. The decrease in the
hardness values in L-2 probably resulted from the precipi-
tation of calcium carbonate.
About mid-September auxilliary pumps were installed
so that the feed rate to L-2 could be maintained at a con-
stant rate. Prior to this time the feed rate fluctuated
widely because all of the beamhouse wastes (about 150,000
gallons per day) were discharged over a 10-12 hour period.
By reducing the flow rate to L-2 to about 75,000 gallons/
day and increasing the detention time, the dissolved
oxygen levels improved, Table 10. The remainder of the
beamhouse waste was bypassed through an existing settling
pond and then discharged to the receiving stream.
34
-------
-o
_Qpq
0
L-1 EFFLUENT
L-2 EFFLUENT
I I L (
LO
C 4 O r1 C
U U I I
o_) O
Lfl r- r C -J
I I I I
00 00 00 00
NOTE:
EFFLUENT L-1
Is
INFLUENT TO L-2
WEEK OF
FIGURE 1O
COD OF EFFLUENTS FROM L-1 AND L-2
2500
2000
-J
()
(-)
F-
LU
-J
U-
LL
LU
LU
I
c
F-
C,)
C)1
1500
1000
500
C,)
c
F-
LU
*
I I I
c J a
. 1 C ( J
I I I
N N. N.
-------
Table 8:
Dissolved Oxygen Concentration
in Lagoon 2
12 .11
1 10
19 22
2 9
18
.20 21 8
.
4 5 6. 7
Date Station
Depth
Temperature
D.O.
Sketch
ft.
°C
mg/i
8/16/68
1
0
23.2
1.2
4
0
24.8
0.5
18
0
23.2
4.8
18
4
23.2
0.1
18
8
23.2
0.1
8/19/68
1
4
7
8
10
12
18
18
0
0
0
0
0
0
0
4
25.0
25.0
25.1
25.0
25.0
25.0
25.0
25.0
1.2
2.6
1.2
1.1
0.6
1.0
0.7
0.5
8/21/68
1
4
5
7
8
10
11
18
18
0
0
0
0
0
0
0
0
4
25.4
25.5
25.4
25.4
25.4
25.3
25.4
25.5
25.1
1.4
1.9
1.5
1.7
2.4
1.4
2.4
3.2
0.9
8/22/68
4
0
26.2
1.5
4
6
7
9
10
4
0
0
0
0
26.2
26.2
26.2
26.2
26.2
0.6
1.4
1.3
1.4
11
36
-------
Table 8: Dissolved Oxygen Concentration
in Lagoon 2
Station D.O.
Sketch ing/l
12 0 26.2 3.0
18 0 26.2 2.2
18 4 26.2 0.1
1 0 25.2 1.5
3 0 25.1 1.4
4 0 25.1 1.2
6 0 25.1 1.2
7 0 25.0 1.1
9 0 25.1 1.5
10 0 25.0 1.3
12 0 25.2 1.5
18 0 25.1 0.6
18 4 25.0 0.4
18 8 25.0 0.4
20 0 25.0 0.7
20 4 25.0 0.4
20 8 25.0 0.2
22 0 25.0 0.7
29 4 25.0 0.3
22 8 25.0 0.1
4 0 19.9 2.5
4 4 19.2 1.6
8 0 19.2 1.1
8 4 19.1 0.6
8 8 19.1 0.5
12 0 20.0 0.6
12 4 19.1 0.2
12 8 19.1 0.1
18 0 19.1 0.8
18 4 19.1 0.5
18 8 19.1 0.2
20 8 19.2 0.8
21 0 19.2 1.0
21 4 19.1 0.9
21 8 19.1 0.7
Date
Depth
ft.
Temperature
OC
8/2 2/6 8
8/2 4/6 8
8/29/68
37
-------
Table 9: Alkalinity and Hardness of Influent
and Effluent of Lagoon 2
Date Alkalinity Hardness
Influent Effluent Influent Effluent
Total Phth Total Phth mg/i mg/i
mg/i mg/i mg/i mg/i
8/20/68 696 296 624 0
21 612 264 596 0
22 672 324 632 0
23 568 300 756 0
26 604 220 1140 0 844 240
27 798 560 544 0 1048 1048
28 544 160 612 0 588 492
29 914 600 592 0 914 512
30 876 544 548 0 1162 518
31 808 496 552 0 1172 488
9/1/68 940 564 600 0 1137 538
2 824 476 612 0 1202 526
3 872 434 654 0 1192 500
4 1028 716 510 0 1209 781
9 1200 880 536 0 1440 438
10 1560 1220 518 0 1469 439
ii 1612 1316 424 0 1830 460
15 716 348 604 0 716 582
16 720 382 546 0 1062 648
20 906 600 630 0 1220 748
23 832 544 672 0 1220 712
24 496 0 624
25 472 0 542
Note: All values as mg/i CaCO 3
The odors disappeared completely and the pH remained at
about 8.0 without addition of extra lime or soda ash.
Only limited BOD data were gathered during the start-
up phase of the biological system because of limitations
in laboratory facilities. A few BOD determinations made
during September and October indicated that the BOD was
being reduced by 80-85% as measured by the change from the
influent to the effluent values, Table 11.
The BOD reduction probably is somewhat misleading be-
cause of the unknown contribution of biodegradable
materials from the anaerobic sludge zone. The increase in
38
-------
Table 10: Dissolved Oxygen Concentration
in Lagoon 2
Station
Sketch
D.O.
mg / 1
Table
Date
I
11: BOD and COD Removals in Lagoon 2
BOD-mg/l COD
nfluent Effluent Influent Effluent
9/17/68
1084 191 2016 861
18
1059 198 2377 934
20
905 2011 873
23
114 1978 952
24
195 808
24
270 (10day)
30
960 272 1951 934
10/2/68
900 221 2067 1419
7
1060 273 2107 1036
9
1310 190 1992 1063
14
690 110 2034 747
16
1878 686
Date
Depth
ft.
Temperature
OC
9/23/68
1
0
17.5
3.0
2
0
17.5
2.5
3
0
17.5
2.5
4
0
17.0
2.7
6
0
17.1
3.0
8
0
17.2
1.8
10
0
17.2
1.5
9/24/68
1
2
3
4
5
7
8
9
11
12
0
0
0
0
0
0
0
0
0
0
18.2
18.0
18.2
18.2
18.0
18.0
18.0
18.1
18.1
18.1
3.0
4.0
3.7
4.7
4.1
4.4
4.7
4.8
2.0
3.6
39
-------
the effluent values for L-2 at the end of September and the
first few days of October probably can be attributed to
reduced biological activity with decreasing temperatures in
the lagoon. Laboratory studies on the effluent from L-2
indicated an oxygen uptake rate of 10-30 mg/i/hr.
The total Kjeldahl nitrogen level of the waste which
averaged about 200 mg/l for the entire period was reduced
by about 50 percent. No reduction in sulfides was observed
and no measurable settleable solids ever appeared in the
effluent although the suspended solids averaged about 200
mg/i. Bacterial studies on the effluent from L-2 showed a
very high bacterial population although at no time was
there any tendency toward agglomeration or flocculation of
the bacteria. The sludge in L-2 decreased in thickness
and had the appearance of well digested sludge indicating
that anaerobic decomposition was reducing the sludge at a
greater rate than it was being added to the unit.
Foaming was another severe problem encountered in
operating the lagoon. At times a layer of foam 5-6 feet thick
would accumulate over the entire surface of the lagoon.
High pressure water jets were partially effective in con-
trolling the foam but presented difficult operational
problems when the air temperature was below freezing.
The combination of the odor and foam problems prompted
a decision to construct new lagoons on a more isolated
site. The study, however, did prove conclusively that the
pretreated beamhouse wastes were ameanable to biological
treatment without adjustment of the pH or without addition
of extra nutrients. These studies also provided more ex-
plicit design values for the new system, namely that a
detention time of at least 16 days would be required and
that the loading intensity should not exceed about 10 lb.
of COD/day/l000 cu.ft.
Another important characteristic of tannery wastes
demonstrated in this study was the fact that tannery wastes
even after treatment exhibited a rapid loss in dissolved
oxygen, Figure 11. It could not be deermined if this
particular characteristic was caused by a chemical oxygen
demand or reflected a lower saturation value for the
tannery wastes. Wastes that had been sterilized tended to
lose oxygen more slowly than non-sterilized waste.
40
-------
TIME MINUTES
TEMP-20°C-22° C
AT START;25°C
AT END OF TEST
BOILED
DISTILLED WATER
N
I -
AUTO C LAVED
L-2 EFFLUENT
L-2 EFFLUENT
0 5 10 15
20
25
30
35
FIGURE 11.
OXYGEN BUILDUP AND UPTAKE
-------
Pilot Plant Treatment of the Total Tannery Wastes :
The construction of the new lagoon system was started
in late autumn 1968 but was not completed until April,
1969. During this period of time pilot plant studies were
conducted to obtain operational data which would be appli-
cable to the system for treating the combined tannery
wastes.
The data presented in Table A-3 indicate that the
total tannery wastes (beamhouse plus spent vegetable tan
liquors) are ameanable to biological treatment. The pH of
the system remained remarkably constant even though the
pH of the feed varied considerably. The C02 and organic
acids produced in the anaerobic unit effectively neutral-
ized the excess lime carried in the beamhouse waste
fraction. The effluent from the aerobic unit contained
only bicarbonate alkalinity throughout the entire study.
Significant reductions in the COD and suspended solids
were achieved.
The total Kjeldahl nitrogen levels were reduced 30-
50%, but the ammonia content of the effluent remained
high throughout the study, Table A-4. Determinations for
the other forms of nitrogen could not be made because of
the intense color imparted to th total wastes by the
spent tan liquors. No reduction in total sulfides was
observed.
The BOD of the total tannery wastes was reduced by
80-90 percent, Table 12. The effluent BOD values were in
the same general range as observed for the fullscale
lagoon system which had been operated on beamhouse wastes.
A few BOD values and rate constants for the total wastes
are shown in Table 13.
Table 13: BOD Values and Rate Constants
Date Sample
1-Day 2-Days 3-Days 4-Days 5-Day
3/18/69 Inf. 1008 1568 1882 2150 2442
K 1 .18 .17 .14 .13
Eff. 76 128 165 199 232
K 1 .13 .11 .08 .07
3/19/69 Inf. 694 1120 1568 1680 1770
K 1 .18 .17 .29 .24
Eff. 75 119 147 170 191
K .18 .17 .14 .12
42
-------
Date
Table 12:
5-Day, 20°C BOD
Inf. Eff.
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date
5-Day, 20°C BOD
Inf. Eff.
Feed: Bearnhouse Wastes Only
Det. Time - 10 Days
Feed: 3 Parts Beaithouse
1 Part Spent Tan Liquors-Det.
Waste
Time - 10 Days
10/7/68
8
9
10
1060
1181
1212
1172
273
687
196
95
11/2 6/6 8
27
Feed: 3 Parts Beamhouse Waste
1 Part Spent Tan Liquors
Det. Time - 10 Days
1775
2140
Feed: 3 Parts Bearrthouse
1 Part Spent Tan Liquors -
Det. Time 15 Days
12/2/6 8
3
11/4/6 8
5
7
12
14
14
690
110
9
15
37
10
22
1267
118
11
24
1525
167
12
29
915
117
31
1980
1470
2135
2957
2010
2127
130
134
186
259
236
250
16
17
18
19
24
26
19
2395
213
20
2220
180
21
2215
181
233
225
Waste
1 L Sewage
285
188
144
139
81
79
157
195
245
243
170
160
1472
2232
1520
1270
1475
1215
1205
1335
2030
2195
2032
1510
Feed: Beamhouse Wastes Only
Det. Time - 10 Days
1/6/6 9
1580
459
244
7
1632
-------
Date
Table 12:
5-Day, 20°C BOD
Inf. Eff .
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date
17
18
19
5-Day, 20°C BOD
Inf. Eff.
1330
2315
1645
291
248
180
A
A
Feed: Beamhouse Wastes Only
Feed: 2
Parts
Beamhouse
Waste
Det. Time - 10 Days
1 Part
Spent
Tan
Liquors
-
0.9 L
1/8/69 1547 138
2/6/69
1177
163
9 2018 128
3/6/69
1042
129
13 1250 334
7
863
168
14 1267 363
10
1075
158
15 1590 117
11
1915
168
16 1160 99
12
1215
161
Feed: 2 Parts Beamhouse Waste
1 Part Spent Tan Liquors
0.9 L Sewage: Det.Time-20 Days
Sewage
1/20/69
1460
176
3/25/69
1781
113
21
1340
179
26
2195
138
23
1740
143
4/1/69
1702
170
24
1530
155
2
1232
178
27
2260
301
8
1973
258
28
2240
194
9
2242
207
29
2285
191
15
1977
183
30
1470
210
16
2071
181
2/3/69
1155
184
4
1435
220
5
1422
162
-------
While the BOD data plot as smooth curves, Figure 12, the
Ki values show considerable variation from day to day.
There was little evidence of an initial lag phase in the
BOD reaction.
Domestic sewage was added to the feed to the pilot
unit during a portion of the study. In general the
performance was improved somewhat when sewage was added.
Bacteriological and microscopic examination of the con-
tents of the aerobic zone revealed a relatively low
bacterial population and large numbers of protozoa. In
all probability, the sewage served to reseed the system
more effectively than recirculated effluent from the
aerobic zone which had a relatively low bacterial
population.
Studies on the oxygen buildup and uptake rates of
the wastes from both the anaerobic and aerobic zones of
the pilot unit were made. The data presented in Figures
13 and 14 indicate that the saturation value for oxygen
in the tannery wastes is appreciably less than that of
pure water. As shown in Figure 13 the waste in the
anaerobic zone exerted a rapid oxygen uptake. The waste
from the aerobic zone by contrast exhibited a low uptake
rate indicating that the wastes were well stabilized.
Treatment of Total Tannery Wastes :
In the initial phases of the investigation it was
assumed that the entire waste treatment system could be
constructed and operated on the tannery site (see
Figure 9). Problems of odor and foaming of the ana-
erobic-aerobic lagoons dictated that a new site be
selected for the biological treatment units. The company
owned land about 7,000 feet from the tannery which was
suitable for the new units. The land had been used for
storing spent vegetable tan liquors during periods of low
stream flow. The tan liquor was pumped through a 3-inch
diameter plastic pipeline from the tannery to the holding
basins. The rate at which waste water could be pumped
through the pipeline was limited to about 55 gpm (whereas
the total tannery waste flow amounted to about 120 gpm)
because the maximum pressure that the pipe could with-
stand was about 40 psi.
Detailed hydraulic studies showed that the rate of
pressure drop varied considerably for the various
sections of the pipeline under constant flow conditions.
It was determined that the installation of two pumps in
45
-------
S
I-
LU
=
-J
LL
LL
LU
-J
-S- - S
c1
280
240
200
160
120
80
40
0
0
800
400
000
1600
LU
=
-J
LL
5
-J
-S--S
cD
1200
1 2 3 14 5 6 7
800
I00
TIME-DAYS
FIGURE 12. BOD VS TIME
-------
8
6
-J
4
NOTE:
SAMPLE FROM ANAEROBIC ZONE
OF PILOT UNIT
TEMPERATURE - 20°C
2
k
00
-0 O0--0--O
AUTOC VED SAMPLE
8
SAMPLE-NOT AUTOCLAVED
TIME - MINUTES
FIGURE 13.
OXYGEN BUILDUP AND UPTAKE
-------
8
-J
(D
,14
NOTE: SAMPLE FROM AEROBIC ZONE
OF PILOT UNIT
TEMPERATURE - 20°C
2
--
KEY:* S
0
8
SAMPLE NOT
0- --O---0
16
AUTOC L.AV ED
AUTOCLAVED
24
SAMPLE
TIME - MINUTES
32
64
FIGURE 114. OXYGEN BUILDUP AND UPTAKE
-------
series in the pipeline would boost the flow to the desired
range without exceeding the pressure limitation on the
pipeline. Two 5-HP close coupled pumps were installed at
distances of 2500 feet and 4000 feet from the plant site.
The pumps actuated by pressure switches delivered 115 gpm
which was sufficient to pump the total tannery wastes to
the new treatment site.
The decision to construct the new anaerobic-aerobic
lagoons at a site about one mile from the tannery allowed
the lagoons at the tannery site to be used for clarif i-
cation of the lime-bearing wastes. The clarifier was
taken out of operation at the beginning of March to
ascertain if the suspended lime could be removed effec-
tively by plain settling in the existing lagoon system.
It was found that with the detention time of about three
weeks provided in the lagoons the suspended solids con-
centration in the effluent as discharged to the receiving
stream was essentially the same as when the lime bearing
wastes were treated with polyelectrolyte and passed
through the clarifier. The separation and pretreatment
procedures other than mechanical screening for the beam-
house wastes were discontinued in March, 1969.
Construction of the new anaerobic-aerobic lagoons was
completed in May, 1969. The new lagoons, Figure 15, pro-
vided a surface area of about 60,000 ft 2 and a volumetric
capacity of about 2.3 million gallons. The new lagoons
had a depth of only six feet and provided a detention
time of about 16 days for the total flow. A deeper lagoon
would have been preferred but construction difficulties
limited the depth to about six feet.
In May, 1969 the lagoons were filled with clarified
beamhouse wastes and the aerators were started. No effort
was made to reduce the pH of the wastes prior to startup
of the biological system and the wastes were not seeded
with domestic sewage. Within two days the pH had fallen
to about 9.5 and it was apparent that biological activity
was underway.
The units were operated for approximately two months
on beamhouse wastes. Odors were apparent in the vicinity
of the lagoons and severe foaming occured intermittently.
On July 12 and 13 , 500,000 gallons of spent tan liquor
were added to the system. An immediate increase in the
effluent BOD was noted. The odors disappeared completely
and foaming was not nearly so severe. Small amounts of
tan liquors were added intermittently from July 13 through
49
-------
EFFLUENT
RECORDER
FIGURE 15.
LAYOUT AND APPROXIMATE DIMENSIONS
OF LAGOON SYSTEM
300
VOL. = 258 OOO FT 3
70
VOL.=23 2OOFT 3
0
0
15 HP
0
10 HP
5 HP
SLUDGE RETURN
-------
August 20 with little apparent effect on the performance
of the lagoons as measured by the COD and BOD of the
effluent.
From August 22 through September 22 all of the tan
liquors were added to the system. The spent tan liquors,
however, were not mixed with the beamhouse wastes prior
to introduction to the biological system. Each waste
fraction was pumped separately to the treatment site
through the same pipeline. After September 22, the spent
tan liquors and beamhouse wastes were mixed prior to
being pumped to the treatment system.
The performance data for the anaerobic-aerobic
lagoon system in terms of the pH, alkalinity, COD and
suspended solids for the period from May 22 through
October 24 are listed in Table 14. The pH of the effluent
remained remarkably stable even though the influent values
varied considerably. The reduction in total alkalinity
during the period when only beamhouse wastes were added
indicates that calcium carbonate was being precipitated.
Near the end of the observation period there was little
reduction in alkalinity. The spent tan liquors effected
a slight reduction in the pH of the influent but did not
change the total alkalinity significantly.
The reduction in COD ranged from about 30-80 percent.
The spent tan liquors when added without prior mixing
with beamhouse wastes greatly increased the COD and
volatile suspended solids of the total influent. By con-
trast, the mixing of the two waste streams followed by
settling, effected a significant reduction in the organic
load imposed on the biological system. A large volume of
sludge resulted from the blending of the two waste streams.
It is probable, therefore, that the cost of handling th.e
excess sludge would more than offset the gains made in
reducing the organic load to the biological units.
When the spent tan liquors were pumped to the treat-
ment site separately and added to the lagoons which had
a pH below 9.0, no marked precipitation occurred. A
detailed survey of sludge deposits in the anaerobic-
aerobic lagoons after about five months of operation
showed only a small accumulation of sludge, Table 15. The
deposited sludge appeared to be decomposing readily hence
it is believed that sludge accumulation will not be a
problem in operating the system. The suspended solids in
the effluent from the final lagoon ranged from 20 to as
high as 400 mg/i while the settleable solids remained
51
-------
Table 14:
Performance of Full-Scale Biological System
pH
Inf. Eff.
COD
Inf. Eff.
Fixed
Inf. Eff.
Volatile
Inf. Eff.
Date
Total
Alkalinity
Inf. Eff.
Suspended Solids
C. 1
5/22/69
12.0
7.7
848
368
2450
814
240
0
140
20
23
11.9
7.7
940
380
2470
822
380
0
240
20
26
12.0
7.6
1216
400
2582
645
340
0
500
10
27
12.1
7.5
1220
424
2218
683
120
0
140
10
28
11.5
7.8
748
436
2038
609
240
0
280
10
29
11.0
7.5
556
456
2133
663
120
25
120
95
6/2/69
11.7
7.7
632
516
1623
472
160
20
200
85
3
11.5
7.9
600
484
1535
386
200
0
220
40
4
11.6
7.9
536
484
1666
495
160
15
100
25
5
11.7
7.9
764
476
1738
377
80
10
120
40
6
11.7
7.8
784
464
1770
361
80
25
30
35
9
11.5
7.9
728
412
1786
413
200
40
400
90
10
11.1
7.9
516
496
1627
409
240
30
260
120
11
10.7
7.8
676
472
1596
400
130
15
370
95
12
11.7
7.8
704
440
1800
384
160
10
240
60
13
11.8
7.8
900
436
1497
370
110
30
210
30
16
11.8
7.8
784
496
1610
390
60
10
130
40
17
11.8
7.8
768
504
1537
369
120
40
280
80
18
11.7
7.8
624
444
1576
341
180
10
140
15
19
11.7
7.7
756
436
1631
361
190
10
190
25
20
11.4
7.8
624
484
1631
381
200
10
160
0
23
11.5
8.0
860
552
1550
402
170
10
190
90
24
11.4
8.0
844
600
1581
421
150
20
160
115
-------
Table 14:
Performance of FullScale Biological System
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
Date pH Total
Alkalinity
Inf. Eff. Inf.
Eff.
COD
Inf. Eff.
6/25/69
11.2
7.9
844
532
2195
416 160
30
240
75
26
11.6
7.8
836
564
1952
512 100
16
280
124
27
11.5
7.9
796
556
2113
399 26
26
194
45
30
11.0
7.9
796
420
1963
517 120
25
40
85
7/1/69
10.8
7.8
708
504
2113
611(427) 230
15
170
45
2
10.9
7.9
824
584
2307
620 110
30
100
15
3
11.2
7.9
844
556
2433
687(432) 110
40
180
30
7
10.9
7.9
822
586
1925
545 100
20
80
20
8
11.0
7.9
696
544
2113
552(496) 150
15
170
10
9
11.1
8.0
636
520
1954
503 160
20
60
0
10
11.2
8.0
728
488
2088
594(446) 210
35
140
0
11
11.1
8.0
766
524
1865
564 280
35
140
0
14
11.0
7.8
920
504
1967
1231 220
40
170
40
15
11.1
7.8
844
524
1604
1238(987) 180
40
20
55
16
11.0
7.7
776
504
2442
1542 260
74
220
46
17
11.1
7.7
808
528
2096
1561(1398)250
90
260
40
18
11.1
7.7
816
528
1956
1522 290
110
180
40
7/21/69
11.2
7.7
884
536
1788
1201 225
25
275
70
22
11.2
7.7
596
616
1642
922(881) 215
35
265
75
23
11.4
7.9
720
612
1941
953 270
30
50
70
24
11.4
7.7
652
608
1809
894(797) 180
40
210
20
25
11.4
7.8
852
624
1798
818 250
30
30
50
COD values in (
are for filtered samples.
-------
Table 14: Performance of Full-Scale Biological System
Suspended Solids
Fixed Volatile
Irif. Eff. Inf . Eff.
Date pH
Inf. Eff.
Total
Alkalinity
Inf. Eff.
COD
Inf. Eff.
Qi
7/28/69
11.4
7.8
804
536
2046
885(719)
180
40
220
30
29
11.5
7.8
950
584
2160
711
140
30
20
30
30
11.4
7.8
784
568
1951
704(634)
200
20
130
10
31
11.3
7.8
772
572
1902
617
120
10
40
50
8/1/69
11.3
7.8
884
556
1933
660(578)
300
25
100
25
4
11.8
8.0
940
576
1969
690
220
20
360
60
5
11.6
7.9
884
488
1820
490(459)
400
25
110
35
6
11.5
7.9
856
504
1816
518
260
35
240
45
7
11.0
7.9
836
476
1863
483(410)
250
10
310
65
8
11.3
7.9
812
568
1880
441
240
20
260
50
11
11.6
8.0
836
664
1917
437
230
30
180
35
12
11.4
8.0
816
672
2019
383(343)
230
20
90
50
13
11.4
7.9
648
484
1781
475
250
15
250
55
14
11.5
7.9
676
464
1879
494(438)
360
20
190
60
15
11.4
7.9
736
492
1752
339
230
20
290
70
18
11.4
7.9
580
456
1874
339(290)
280
20
60
80
19
11.8
8.0
676
396
1851
304
160
15
220
50
20
11.6
7.9
644
464
1691
335
200
40
260
50
21
11.8
8.0
688
444
1582
320
280
20
200
50
22
11.6
8.0
744
468
2930
316(313)
330
30
260
25
25
10.2
8.0
760
424
1487
512
260
25
220
30
26
10.1
7.9
640
464
2822
602
290
20
330
40
COD values in (
) are for filtered samples.
-------
Table 14: Performance of Full-Scale Biological System
Total COD
Alkalinity
Inf. Eff. Inf. Eff.
Date pH
Inf. Eff.
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
01
8/27/69
8.5
7.9
484
460
3138
510
220
15
560
55
28
8.9
7.9
496
444
2844
525(400)
220
30
410
64
29
9.3
7.8
520
456
2760
555(508)
300
40
90
60
9/2/69
9.7
7.9
510
496
3050
820
260
30
420
70
3
8.9
7.9
532
504
3754
838(570)
220
25
440
70
4
8.3
7.9
556
496
2780
780
195
30
585
90
5
9.5
7.8
596
544
260
40
460
50
8
592
568
4344
706
9
616
536
3759
709
10
7.9
944
580
3363
817
11
7.9
596
532
2571
674
12
644
552
3693
801
15
7.8
7.9
556
504
6185
1187
300
75
720
315
16
576
560
6382
1119
17
9.1
7.9
644
556
5140
1720
350
82
710
353
18
572
528
5100
1728
22
7.8
7.9
724
404
1797
1293
310
90
380
260
23
11.5
8.0
836
624
1759
1224
270
70
370
370
24
11.5
7.9
792
598
1769
1046
240
100
240
260
25
11.4
7.9
812
572
2038
1085
220
80
210
270
26
11.5
7.9
800
568
1908
1033
230
90
340
270
29
11.3
8.0
916
600
2262
882
240
50
130
110
30
11.4
8.0
932
620
2376
806
250
80
430
130
10/1/69
2168
778
2
11.4
7.9
924
604
2093
733
190
40
190
3
11.4
7.9
896
576
2218
732
240
40
110
160
COD values in C )
are for filtered samples.
-------
Table 14:
Performance of Full-Scale Biological System
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
Date pH
Inf. Eff.
Total
Alkalinity
Inf. Eff.
COD
Inf. Eff.
10/6/69
7
8
9
10
10.0
10.0
9.8
9.8
9.8
7.9
7.9
7.9
7.9
7.9
656
660
736
712
696
644
644
656
636
648
2274
2004
1930
1918
1996
725
816
831
816
857
180
190
160
130
140
40
70
30
40
40
300
410
150
70
60
100
90
100
120
80
13
14
15
16
17
9.5
9.6
9.4
9.4
9.7
7.9
7.9
7.9
7.9
7.9
620
592
604
724
720
684
692
700
696
684
1999
1992
1935
2073
1943
951
925
944
937
892
150
100
110
100
120
30
80
40
60
60
90
70
50
20
80
7C
80
60
20
40
20
21
22
23
24
9.8
10.0
10.1
10.6
10.8
7.9
8.0
7.9
7.9
7.9
704
712
736
718
700
692
656
632
1915
1830
1862
1949
1927
850
913
916
938
934
100
100
90
60
50
50
70
50
40
30
40
60
50
60
90
70
90
50
40
30
-------
Table 15: Sludge Accumulation in Lagoons
.28 27
4 12 20 2l 29
Ll 22 26
18. L2
2 6 1:1 l 23. L-3 25
1. 15 16
8
Station Water Sludge Station Water Sludge
No. Depth Depth No. Depth Depth
Inches Inches Inches Inches
1 66 0 16 75 5
2 66 4 17 72 3
3 63 6 18 73 0
4 69 3 19 72 0
5 66 4 20 69 0
6 72 0 21 66 0
7 66 1 22 69 0
8 60 6 23 66 2
9 66 5 24 66 0
10 72 2 25 48 1
11 66 4 26 63 0
12 69 0 27 69 3
13 69 2 28 60 0
14 69 3 29 78 0
15 66 5
57
-------
essentially zero for the entire period of study.
The nitrogen data presented in Table 16 show extensive
reductions in the organic nitrogen content of the tannery
wastes. The ammonia content of the effluent remained high
throughout the period of observation. Laboratory
determinations for nitrites and nitrates could not be
made because of the high color of the treated effluent.
It is not known, therefore, if any denitrification was
achieved. The change in nitrogen levels observed in the
anaerobic-aerobic lagoon was substantially the same as
observed in the pilot plant operation.
The data on total sulfides indicate that the sulfides
were unchanged in passage through the anaerobic-aerobic
lagoons. This same characteristic was observed in the
pilot plant studies. At no time was there evidence of
hydrogen sulfide evolution from the operating system even
though the pH of the effluent remained in the range of 7.7
to 8.0. Also when the spent tan liquors which had a pH of
about 4.5 were mixed with the sulfide bearing wastes no
hydrogen sulfide could be detected from an odor standpoint
or by chemical means.
It is possible that the high dissolved salt content
of tannery wastes prevents the formation and liberation of
hydrogen sulfide at pH values above about 7.5. The sulfide
concentration, however, does increase the chemical oxygen
demand and will interfere with disinfection of the effluent.
The BOD data that were obtained* for the lagoon system
show that reductions of 75-95 percent were obtained as
measured by the influent and effluent values, Table 17 and
Figure 16. Because of the long detention time, the vari-
ability of the BOD in the influent, and the mixing caused
by the aerators, only approximate values for BOD removal
can be given. The total removal of BOD obtained through
the clarification and biological treatment steps, however,
exceeded 90 percent. The limited number of BOD determi-
nations made on filtered effluent samples indicates that
most of the residual BOD was in dissolved form. Thus while
the effluent at tj.mes contained appreciable volatile
suspended solids these apparently were of little signifi-
cance in terms of oxygen utilization.
While the 5-day, 20°C BOD values are used in most
waste characterization and treatment studies, long term
*All BOD determinations made with a Manometric Analyzer manu-
factured by the Hach Chemical Company, Ames, Iowa.
58
-------
Table 16: Performance of Biological System
Date TKN Ammonia Organic Total
Nitrogen Nitrogen Sulfides
Inf. Eff. Inf. Eff. Inf. Eff. Inf. Eff.
5/26/69 206 92 85 48 122 45 16 8
28 171 97 37 55 135 42 17 10
6/2/69 15 9
4 216 108 116 71 99 38 15 7
6 176 110 59 72 116 38 14 9
9 202 113 73 77 129 36 11 10
11 272 109 41 75 231 34 13 8
13 158 103 39 72 119 31 12 8
16 162 105 46 75 115 30 15 8
18 147 110 29 78 118 30 19 9
20 131 113 18 80 113 32 13 9
23 145 109 34 79 111 29 10 9
25 144 109 38 80 106 30 16 11
27 148 114 35 82 113 32 15 10
30 147 118 28 85 119 33 16 10
7/2/69 135 116 27 88 108 28
7 132 112 24 84 108 28 18 14
9 137 113 27 88 112 25 17 11
11 149 108 39 83 110 25 13 13
14 188 109 76 80 112 29 25 17
15 153 113 35 80 118 33 19 16
18 142 111 29 77 113 34 20 18
21 114 104 46 71 68 33 17 15
23 158 109 48 76 110 33 20 12
25 153 114 38 77 115 37 17 8
28 148 106 31 67 117 39 14 13
30 144 98 28 60 116 38
8/1/69 161 102 52 71 109 31 15 16
4 148 96 40 71 108 25 19 16
6 149 95 47 68 102 27 11 15
8 137 87 29 67 108 20 14 13
11 156 86 52 68 104 18 15 14
13 161 104 55 83 106 21 17 14
15 154 88 48 70 106 18
*TKN -- Total Kjeldahl Nitrogen
59
-------
Table 16; Performance of Biological System
Date
TKN Axnnionia
Nitrogen
Inf. Eff. Inf. Eff.
Organic
Nitrogen
Inf. Eff.
Total
Suif ides
Inf. Eff.
8/18/69
145
91
44
71
101
20
20
133
94
30
73
103
21
20
13
22
94
90
45
70
49
20
21
15
25
147
90
56
66
91
24
20
16
27
137
87
50
64
87
23
15
15
29
140
89
54
62
86
27
19
14
9/3/69
143
84
52
59
91
25
20
15
5
128
79
44
55
84
24
19
13
11
140
71
52
48
88
23
16
135
85
45
57
90
28
18
14
17
143
85
50
56
93
29
22
142
77
46
44
96
33
19
16
24
153
69
59
43
94
26
19
15
26
147
95
54
58
93
37
18
14
29
152
83
63
46
89
37
19
14
10/1/69
149
82
57
47
92
35
19
15
3
148
79
58
44
90
35
19
15
6
135
92
46
50
79
42
18
14
8
130
91
59
49
71
42
19
16
10
125
94
56
48
69
46
10/13/69
109
97
53
52
56
45
19
14
15
133
95
57
50
76
45
19
15
17
133
93
56
50
77
43
19
15
20
116
95
54
52
62
43
21
14
22
117
96
50
52
67
44
20
14
24
126
96
53
51
73
45
18
14
60
-------
Table 17: Performance of Full Scale Biological
Treatment System
20°C BOD by Days in mg/l
Date Sample 1 2 3 4 5 6 7
5/22/69 Influent 952 1024 1084 1155
Effluent 181 204 230 254
5/23/69 Influent 940 1024 1120 1155
Effluent 168 194 228 246
6/3/69 Influent 441 788 1192 1241 1289
Effluent 68 84 141 157 170
6/4/69 Influent 429 800 1192 1278 1338
Effluent 63 79 133 147 162
6/10/69 Influent 418 739 998 1132 1205
Effluent 65 86 128 139 147
6/11/69 Influent 455 764 1047 1132 1205
Effluent 50 65 94 115 131
6/17/69 Influent 280 661 952 1098 1131
Effluent 55 71 115 144 152
6/18/69 Influent 213 672 952 1064 1142
Effluent 63 79 118 133 136
6/25/69 Influent 355 937 972 1045 1179 1206
Effluent 52 81 97 -105 141
6/26/69 Influent 243 873 934 984 1080 1106
Effluent 55 92 105 118 136 138
-------
Table 17: Performance of Full Scale Biological
Treatment System
200 C BOD by Days in mg/i
Date Sample 1 2 3 4 5 6 7
7/3/69 Influent 521 693 929 1127 1236
Effluent 26 33 39 42 55
7/11/69 Influent 333 630 804 1002 1199
Effluent 26 38 50 52 76
*Effluent 16 24 31 37 63
7/12/69 Influent 336 853 188 1159 1336
Effluent 92 115 131 160 173 204
7/14/69 Influent 392 644 821 853 928 1047
Effluent 102 160 183 208 249 274
7/18/69 Influent 504 779 923 1016 1118 1215
Effluent 84 149 173 201 221 256
7/21/69 Influent 573 1165 1335 1643 1790 2089
Effluent 111 157 191 220 241 262
*Eff luent 88 141 170 199 222 238
7/28/69 Influent 465 722 870 965 1163
Effluent 76 115 144 165 191
7/29/69 Influent 452 868 808 978 1126 1150
Effluent 73 97 123 162 170 181
*Eff luent 71 92 118 141 165 170
*Filtered Sample
-------
Table 17: Performance of Full Scale Biological
Treatment System
200 C BOO by Days in mg/i
Date Sample 1 2 3 4 5 6 7
8/4/69 Influent 490 823 984 1157 1230 1329 1415
Effluent 68 89 102 113 131 136 144
8/12/69 Influent 432 730 902 1000 1037 1093
Effluent 33 39 55 65 73 79
8/15/69 Influent 419 680 878 989
Effluent 24 37 42 50
8/18/69 Influent 433 730 890 951 1038
Effluent 26 39 50 63 65
*Eff luent 24 31 37 42 50
8/22/69 Influent 308 605 928 1201 1375 1498 1597
Effluent 26 39 52 55 60 68 71
8/23/69 Influerit 490 871 1010 1107 1157 1243
Effluent 73 89 97 115 118 120
*Eff luent 65 79 89 102 107 111
8/28/69 Influent 580 866 1002 1125 1211 1235 1259
Effluent 26 31 44 60 71 79 81
8/29/69 Influent 519 941 1139 1361 1597 1732 1856
Effluent 31 44 52 63 76 89 99
*Eff luent 21 24 34 47 55 71 71
*Fjltered Sample
-------
Table 17: Performance of Full Scale Biological
Treatment System
20°C SOD by Days in mg/l
Date Sample 1 2 3 4 5 6 7
9/3/69 Influent 245 506 728 870 1037 1173
Effluent 26 29 34 44 50 58
9/4/69 Influent 258 543 778 1013 1186 1335
Effluent 31 42 52 68 79 81
9/10/69 Influent 202 331 491 539 713 811
Effluent 26 34 39 42 50 55
9/11/69 Influent 208 306 466 502 688 986
Effluent 34 44 63 71 79 89
C )
9/17/69 Influent 493 688 958 1091 1202 1299 1384
Effluent 50 99 126 165 181 196 217
9/18/69 Influent 469 738 983 1130 1239 1349 1459
Effluent 39 76 113 147 160 183 201
9/19/69 Influent 589 793 927 1025 1120 1142 1176
Effluent 71 107 123 144 191 222 238
9/22/69 Influent 501 781 865 950 1021 1067 1128
Effluent 76 141 165 183 220 249 272
9/29/69 Influent 630 964 1120 1167 1338 1484 1595
Effluent 52 94 118 133 170 201 235
-------
Table 17: Performance of Full Scale Bio3ogical
Treatment System
20°C DOD by Days in mg/l
Date Sample 1 2 3 4 5 6 7
9/30/69 Influent 605 852 1167 1167 1238 1310 1346
Effluent 42 63 115 139 162 194 209
10/6/69 Influent 477 859 1051 1183 1329 1362 1398
Effluent 72 110 170 212 251 290 301
10/7/69 Influent 490 777 927 1126 1217 1274 1310
Effluent 68 118 183 238 273 306 327
10/8/69 Influent 556 881 1049 1205 1236 1285 1320
Effluent 65 118 173 225 274 304 319
10/20/69 Influent 564 782 966 1037 1109 1143 1177
Effluent 71 105 131 157 201 243 288
10/21/69 Influent 514 758 817 938 985 1081 1190
Effluent 79 126 154 186 209 241 267
-------
BEAMHOUSE WASTES
J Af1HOUSE WASTES +
PART SPENT TANS
i TOTAL i
WASTES
PRETREATMENT FOR
COLOR REMOVAL
: 1 INFLUENT
EFFLUENT
a]
5
I.
I
II
89
1
I
1 i
13 14
WEEKS AFTER STARTUP OF UNITS
FIGURE 16. REDUCTION IN BUD IN BIOLOGICAL SYSTEM
-J
Ά
0
>-
1400
1200
1000
800
600
1400
200
0
7
>-
10 11
15 17
-I
F-
-------
data often are significant from a design and operational
standpoint. A number of long term BOD determinations were
made to determine the relationship between the 5-day values
and the corresponding 20-day values. The data presented
in Table 18 and in Figures 17 and 18 show that for the
effluent samples the 5day BOD represented a major fraction
of the ultimate BOD. This was somewhat surprising because
of the relatively high ammonia concentration in the effluent
from the lagoons.
Some of the long term BOD values for the influent
samples were considerably higher than the 5-day values. In
the selection of aeration equipment for a lagoon with a
detention time greatly in excess of five days, long term
BOD data must be given serious consideration. The
calculated loading intensity for the system, Table 19,
ranged from 1.9 to 7.0 pounds of 5-day, 20°C. BOD/day/
1000 cu.ft.
The actual aeration requirements probably were con-
siderably higher, since the detention time in the aerobic
portion of the system was 10-12 days. This factor coupled
with the rapid loss of oxygen from tannery wastes, Figure
19, probably accounts for the low dissolved oxygen levels
observed in the aerated lagoons throughout the period of
operation.
Dissolved oxygen measurements made almost daily at
the water surface around the periphery of the lagoons re-
vealed a very low oxygen concentration, Table 20. A
detailed study made on September 18 showed that dissolved
oxygen was present in the aerated lagoons to a depth of
about 44 inches, Table 21. Since the total water depth
ranged from 5 to 6 feet, a large portion of the system was
aerobic.
Effect of Effluent on the Receiving Stream :
The effluent became highly colored soon after spent
tan liquors were added to the biological units. A survey
of the receiving stream revealed that the effluent reduced
the D.O. in a narrow segment of the stream immediately
below the point of discharge, Figures 20 and 21. This
segment of the stream also was highly colored but aquatic
life was abundant. The discoloration persisted for at
least one mile downstream. It is believed that dispersal
of the wastes across the entire width of the stream would
reduce the color to a more acceptable range although the
entire stream would be slightly discolored during periods
67
-------
Table 18:
Long-Term BOD Values For Lagoons
Time
Days
Dates
72 96 9
Inf. Eff.
On Which Samples Were Composited
Inf. Eff.
1 452 73 580 26
82869 82969 91969
Inf. Eff.
Inf .
589
793
927
1025
1120
1142
1176
1213
1224
1225
1225
1225
1225
1225
Eff .
71
107
123
144
191
222
238
264
272
277
277
277
277
277
519
31
2
686
97
866
31
941
44
3
808
123
1002
44
1139
52
4
978
162
1125
60
1361
63
5
1211
71
1597
76
6
1126
170
1235
79
1732
89
7
1149
181
1259
81
1856
99
8
1160
194
1259
81
1905
99
9
1210
196
1283
89
1942
105
10
1222
199
1295
97
1979
107
11
1222
207
1300
99
2028
115
12
1222
207
1318
105
2074
118
13
1222
209
1324
105
2074
120
14
1222
209
1324
105
2079
120
15
1222
209
1324
105
2079
120
16
1222
209
1324
105
2079
120
17
1233
209
1324
107
2079
120
18
1233
209
1330
107
2114
126
19
1233
209
1330
107
2138
128
20
1233
209
1341
114
2200
133
21
1354
115
2212
133
68
-------
Table 18: Long-Term BOD Values for Lagoons
Time Dates On Which Samples Were Composited
Days 10669 10769
Inf. Eff. Inf. Eff.
1 477 72 490 68
2 859 110 777 118
3 1051 170 927 183
4 1183 212 1126 238
5 1328 251 1216 273
6 1362 290 1274 306
7 1398 301 1311 327
8 1370 308 1312 353
9 1429 314 1342 369
10 1440 324 1378 385
11 1451 348 1388 395
12 1451 366 1418 406
13 1451 379 1418 416
14 1451 392 1555 4-19
15 1451 403 1555 419
16 1451 408 1555 421
17 1451 416 1555 424
18 1451 416 1555 424
19 1451 416 1555 424
20 1451 416 1555 424
21 1451 416 1555 424
69
-------
8
UNF I LTERED
O a a G-
0 -0
FILTERED
10
TIME - DAYS
SAMPLE COMPOSITED: 8/29/69
12
14
16
FIGURE 17
EFFLUENT BUD VS TIME
120
go
-J
L)
0
c-.J
60
30
/
0
2
4
6
-------
, -
/ ,-
7/
1/
/1
/ /
1
Ii
INFLU NT -
-
- a- a- - - a -o o - -
9 0
SAMPLES COLLECTED
o 7-29-69
8-29-69
EFFLUENT
0--- M 0 0 0 0 o o o
0 £
I
I
i
I
I
I
I
6 8 10
TIME - DAYS
12 iLl 16 18
FIGURE 18. LONG TERM BUD VALUES
1LIOO
1200
1000
800
600
400
200
J
(D
0
c. 4
/
-U 2
-------
Table 19:
Organic Loading and Flow to Lagoons
Applied Load
COD BOD
#/day #/day
Intensity
BOD
#/dav/l000ft 3
Date Flow
gpd
Lagoon Loading
COD
#/dav/10 OOft3
6/12/69
117,300
1760
5.7
13
129,400
1610
5.1
16
98,000
1310
4.3
18
140,800
1940
1180
6.4
3.9
19
161,800
2200
7.2
20
153,300
2080
6.8
27
164,700
2890
9.4
30
156,900
2560
8.4
7/1/69
64,450
1130
3.7
2
153,300
2960
9.7
3
151,650
3060
1520
9.9
4.9
8
92,750
1630
5.3
7/9/69
161,500
2640
8.6
10
165,300
2880
9.4
11
167,750
2610
1535
8.5
5.0
15
87,750
1170
3.9
16
150,150
3060
9.9
17
149,500
2600
8.5
18
150,250
2450
1400
7.9
4.5
7/21/69
143,000
2150
2140
7.0
7.0
22
84,350
1160
3.7
23
164,900
2660
8.6
24
166,100
2510
8.2
25
155,400
2330
7.6
28
157,900
2690
1400
8.8
4.5
29
86,900
1565
760
5.0
2.5
30
147,750
2410
7.8
31
146,500
2320
7.6
8/1/69
4
146,100
164,650
2360
2700
1690
7.7
8.7
5.4
5
81,500
1230
4.0
6
143,250
2180
7.0
7
142,500
2210
7.2
8
143,000
2240
7.3
11
143,600
2290
7.4
12
66,000
1110
570
3.6
1.9
13
148,950
2210
7.2
14
149,300
2340
7.6
15
156,250
2280
1370
7.4
4.5
18
156,500
2450
1360
8.0
4.4
72
-------
Table 19:
Organic Loading and Flow to Lagoons
Date Flow
gpd
Applied
Load
Lagoon Loading
Intensity
COD
BOD
COD
BOD
#/day
#/day
#/day/l000ft 3
#/day/l000ft 3
8/19/69
111,750
1730
5.6
20
166,500
2350
7.7
21
161,350
2140
6.9
22
147,900
2020
1690
6.6
5.5
25
116,600
1460
1120
4.8
3.6
26
71,350
1680
5.5
27
77,250
2020
6.6
28
120,250
2900
1240
9.4
4.0
29
126,500
2920
1680
9.5
5.5
9/2/69
151,500
3860
12.4
3
100,300
3110
900
10.1
2.9
4
156,100
3620
1530
11.7
5.0
8
142,500
5160
16.7
9
89,000
2790
9.0
10
144,650
4080
860
13.2
2.8
11
151,700
3260
872
10.5
2.8
12
157,150
4850
15.7
15
112,900
5800
18.8
16
141,000
7500
24.3
17
160,500
6880
1610
22.2
5.2
18
168,500
7160
1740
23.2
5.6
19
160,350
1500
4.9
22
167,380
2510
1430
8.1
4.6
23
157,000
2300
7.5
24
162,750
2400
7.8
25
153,250
2610
8.4
26
157,500
2510
8.1
29
156,800
2960
1750
9.6
5.7
10/1/69
143,500
2590
8.4
2
166,750
2900
9.4
3
165,250
3060
9.9
6
166,500
3160
1845
10.2
6.0
7
165,000
2760
1670
8.9
5.4
8
171,000
2750
1760
8.9
5.7
9
166,500
2660
8.6
10
164,100
2730
8.9
73
-------
Table 19:
Organic Loading and Flow to Lagoons
Applied Load
COD BOD
#/dav #/dav
Date Flow
gpd
Lagoon Loading
COD
#/dav/lO 0 Oft 3
Intensity
BOD
#7 day/i 00 Oft 3
10/13/69
162,200
2710
8.8
14
84,000
1400
4.5
15
105,500
1700
5.5
16
125,500
2160
7.0
17
135,750
2200
7.1
20
87,750
1400
810
4.5
21
89,300
1360
734
4.4
22
150,500
2340
7.6
23
111,200
1810
5.8
2.6
2.4
74
-------
8
140
FIGURE 19. OXYGEN BUILD-UP AND UPTAKE
AIR ON
6
1
14
2
SAMPLES FROM
LAGOON: 8-28-69
TEMPI 22-214°C
EFFLUENT
s.
- - - -
INFLUENT
00
20
TIME - MINUTES
-------
Table 20: Dissolved Oxygen Levels and Water Temperature
at Water Surface Around Periphery of Lagoons
Date
L-l
D.O.
Temp.
D.O.
Temp. DO. Temp.
mq/l
°C
mg/i
°C rn g/1 °C
L-2 L-3
6/16/69
5.26.5
22.0
2.8
220
0.60.8
21.6
17
1.02.0
20.6
4.7
20.5
0.52.0
20.4
18
0.62.0
20.0
2.54.0
20.0
0.50.7
20.0
19
0.81.2
20.0
0.81.2
20.0
0.40.6
20.0
20
0.82.0
21.0
1.01.5
21.0
0.81.0
21.0
23
0.61.0
22.0
0.81.0
21.5
0.60.8
21.5
6/24/69
0.50.8
22.0
0.81.0
22.0
0.40.6
22.0
26
0.41.0
22.5
0.61.0
22.5
0.30.5
22.5
27
0.40.9
22.5
0.51.2
22.5
0.40.6
22.5
30
0.81.5
23.0
1.52.4
23.0
0.60.8
23.0
7/1/69
1.01.8
22.0
2.23.2
22.0
0.40.6
22.0
2
1.01.2
23.0
1.72.1
23.0
0.50.8
23.0
3
0.40.8
24.0
0.50.9
24.0
0.40.6
24.0
7
1.02.4
25.0
1.52.8
25.0
0.40.8
25.0
8
0.81.5
24.0
24.0
0.42.6
24.0
10
0.51.5
22.0
0.50.6
22.0
0.30.4
22.0
11
0.60.8
21.0
0.61.0
21.0
0.30.5
21.0
14
1.02.2
23.5
1.02.0
23.5
0.50.6
23.5
15
0.61.0
23.5
0.81.0
23.5
0.30.5
24.0
16
0.50.8
24.0
0.61.0
24.0
0.30.4
24.0
17
0.60.9
24.0
0.81.0
24.0
0.30.4
24.0
18
0.40.8
24.0
0.60.8
24.0
0.20.4
24.0
-------
Table 20: Dissolved Oxygen Levels and Water Temperature
at Water Surface Around Periphery of Lagoons
L-2
Date
L-l
D.O. Temp. D.O.
Temp. D.O.
Temp.
mg/i mg/i
mg/i
°C
L- 3
1
7/21/69
1.21.8
25.0
2.03.5
25.0
0.20.4
25.0
22
0.81.0
25.0
1.01.5
25.0
0.20.5
25.0
23
0.61.0
25.0
0.50.8
25.0
0.10.4
24.5
24
0.61.2
25.0
0.5i.2
25.0
0.30.7
25.0
25
0.50.8
25.0
0.60.9
25.0
0.30.5
25.0
28
1.82.6
25.0
2.23.1
25.0
0.81.4
25.0
29
0.81.0
24.0
1.61.9
24.0
0.60.8
24.0
30
0.81.0
23.0
1.01.2
23.0
0.40.6
23.0
31
0.60.8
23.0
0.81.0
23.0
0.30.6
23.0
8/1/69
0.50.8
24.0
0.81.0
24.0
0.20.4
24.0
4
1.42.4
23.0
2.03.4
23.0
1.01.4
23.0
5
1.01.5
23.0
1.21.6
23.0
0.60.8
23.0
7
0.91.1
24.0
0.81.0
23.5
0.40.6
23.5
8
0.60.9
24.0
0.81.0
23.5
0.40.6
23.5
11
2.43.6
22.0
3.13.8
22.0
1.01.6
22.0
12
2.13.0
22.0
2.52.9
22.0
1.21.6
22.0
13
1.41.8
22.0
1.82.0
22.0
0.50.8
22.0
14
0.61.0
22.0
2.02.8
22.0
0.40.5
22.0
15
0.81.2
23.0
1.61.8
23.0
0.50.6
23.0
18
2.73.1
24.0
3.23.8
24.0
1.61.9
24.0
19
2.22.6
24.0
2.62.9
24.0
0.91.2
24.0
20
1.62.0
24.0
1.82.0
24.0
0.40.6
24.0
21
0.91.2
24.0
1.83.2
24.0
0.30.6
24.0
25
1.31.8
22.0
1.52.0
22.0
0.61.0
22.0
26
1.42.1
21.0
1.82.5
21.0
0.50.8
21.0
27
1.21.4
21.0
1.41.6
21.0
0.40.8
21.0
-------
Table 20: Dissolved Oxygen Levels and Water Temperature
at Water Surface Around Periphery of Lagoons
L2 L-3
Date
L- 1
D.O. Temp.
D.O.
Temp.
D.O.
Temp.
mg/1
mg/i
°C
mg/i
1
8/29/69
0.60.9
21.0
0.81.0
21.0
0.40.6
21.0
9/2/69
1.01.5
23.0
1.82.6
23.0
1.01.8
24.0
3
1.01.2
23.0
1.61.8
23.0
0.51.0
23.0
4
0.40.6
24.0
0.60.8
24.0
0.20.5
24.0
10
1.01.2
24.0
1.21.4
24.0
0.40.5
24.0
*22
0.61.2
23.0
0.40.5
23.0
1.01.4
23.0
*24
0.81.0
23.0
0.30.5
23.0
0.81.0
23.0
26
0.50.8
24.0
0.81.2
24.0
0.40.6
24.0
29
0.60.8
23.0
0.81.0
23.0
0.40.6
23.0
10/1/69
0.50.7
24.0
0.60.9
24.0
0.30.4
24.0
2
0.50.8
24.0
0.50.6
24.0
0.20.4
24.0
6
0.40.7
22.0
0.40.8
22.0
0.20.4
22.0
8
0.50.8
23.0
0.70.9
23.0
0.20.5
23.0
10
0.60.8
22.0
0.81.0
22.0
0.20.4
22.0
13
0.60.9
22.0
0.61.0
22.0
0.20.4
22.0
16
0.81.0
21.0
0.60.8
21.0
0.20.5
21.0
*5 H.P. Aerator moved from L-2 to L-3.
-------
Table 21:
Dissolved Oxygen Levels
In :agoons
10, 11
3. 4 17
9 16
L1
l2 J
5. I
2.
8
13
1. 6. 7. I
14
I
18
19
20
I
Station
No.
Depth Temp. D.O.
In. mg/i
Station
No.
Depth Temp. D.O.
In. mq/1
2 21 0.6
22 21 0.3
44 21 0.0
6 2 21 0.6
22 21 0.3
44 21 0.1
2
21
0.5
7
2
21
0.5
22
21
0.3
22
21
0.2
44
21
0.2
44
21
0.0
2
21
0.4
8
2
21
1.0
22
21
0.2
22
21
0.4
44
21
0.2
44
21
0.3
2
21
0.5
9
2
21
1.0
22
21
0.2
22
21
0.6
44
21
0.2
44
21
0.3
2
21
0.8
10
2
21
0.5
22
21
0.5
22
21
0.2
44
21
0.3
44
21
0.0
L-2
15
21
.28 27
L- 3
22
26
.
24 25
. I
1
2
3
4
5
79
-------
Table 21: Dissolved Oxygen Levels
In Lagoons
Station Depth Temp. D.O. Station Depth Temp. D.O.
No. In. °C mg/i No. In. mg/i
11 2 21 0.6 20 2 21 0.5
22 21 0.3 22 21 0.2
44 21 0.0 44 21 0.0
12 2 21 0.9 21 2 20.8 1.0
22 21 0.5 22 20.8 0.8
44 21 0.3 44 20.8 0.5
13 2 21 0.5 22 2 20.8 0.9
22 21 0.3 22 20.8 0.6
44 21 0.1 44 20.8 0.5
14 2 21 0.5 23 2 20.8 0.7
22 21 0.2 22 20.8 0.4
44 21 0.1 44 20.8 0.2
15 2 21 0.6 24 2 20.8 1.0
22 21 0.3 22 20.8 0.6
44 21 0.1 44 20.8 0.4
16 2 21 0.8 25 2 20.8 1.0
22 21 0.4 22 20.8 0.6
44 21 0.3 44 20.8 0.5
17 2 21 0.8 26 2 20.8 1.2
22 21 0.4 22 20.8 0.8
44 21 0.2 44 20.8 0.8
18 2 21 0.6 27 2 20.8 1.2
22 21 0.2 22 20.8 0.9
44 21 0.0 44 20.8 0.8
19 2 21 0.5 28 2 20.8 1.2
22 21 0.2 22 20.8 0.8
44 21 0.1 44 20.8 0.6
80
-------
EFFLUENT FEET DOWNSTREAM FROM POINT OF WASTE DISCHARGE
IN
510 1 O 2 O 350 790 1 i pn ]L 11
BROWN
5 DARK 11.2 COLORED ZONE 5.0 LIGHT BROWN
107 LIMIT OF COLORED ZONE
U-
j 200 NOTES:
WATER TEMPERATURE: 19-26°C
___ WEATHER: CLEARSUNNY
TIME: 1-3 P.M. ON 9-16-69
250 -
WEST BANK OF STREAM
FIGURE 20. DISSOLVED OXYGEN LEVELS IN RECEIVING STREAM
-------
0
25
EFFLUENT
IN 59
225 NOTES:
WATER
_____ WATER
TIME:
FEET DOWNSTREAM FROM POINT OF DISCHARGE
100 150 250
65
DEPTH: O 5-2.5
TEMPERATURE: 13.0-13.2°C
6-7 A,M . ON 10-6-69
ANKOFSTREA
6.3
500
2.5
I
C,)
L
I-
LL
1111)0
2.6
COLORED ZONE
6.5
4.8
---- --- --
2.6 2.8
6.7
14,7
14.7
4.8
LIMIT OF COLORED ZONE
6.7
250
-
FIGURE 21.
DISSOLVED OXYGEN LEVELS IN RECEIVING STREAM
-------
of low stream flow.
Removal of Color :
After having determined that the total tannery wastes
could be treated effectively in an anaerobic-aerobic bio-
logical system, it was decided that efforts should he made
to remove the residual color from the lagoon effluent.
Detailed laboratory and pilot plant studies demonstrated
that the residual color in the lagoon effluent could be
precipitated effectively by adding lime tc. bring the pH to
about 12.0. The addition of an anionic polyelectrolyte
(NALCO-675) at a dosage of 2-5 mg/l produced rapid
settling of the precipitated color compounds leaving the
effluent with only a pale yellow tinge.
A reduction in color of at least 90 percent was
achieved (estimated by dilution with river water) and the
volume of sludge produced was small. The dosage of lime
required to increase the pH of the effluent to 12.0, how-
ever, was in excess of 2,000 mg/i. This fact coupled with
the necessity of reducing the pH to 10.0 or less before
final discharge rendered the process uneconomical.
The studies then were directed toward precipitating
the color before biological treatment. It was found that
by mixing the spent tan liquors with the highly alkaline
beamhouse waste fractions, the colored materials were pre-
cipitated when the pH was maintained above 11.5. In the
laboratory and pilot plant studies, the mixture of the two
waste fractions produced a large volume of sludge that
settled poorly. Efforts to overcome the sludge problem
by use of poiyelectrolytes (in a reasonable dosage range)
were unsuccessful.
It was decided, however, to conduct a full scale
experiment in mixing the two wastes prior to discharging
them to the biological treatment unit. The two waste
fractions were mixed in a small lagoon and allowed to pass
through several larger lagoons before reaching the bio-
logical unit. The reduction in color was dramatic and
the resulting precipitates settled rapidly and appeared to
compact readily. This finding is quite surprising in
light of the laboratory and pilot plant experience.
Continuous operation of the color removal process has
shown that unless the total waste volume is maintained at
a pH of 10.5 or greater, color will be released from the
precipitated materials. It appears also that complete
83
-------
color removal will not be achieved unless the p1-I of the two
waste fractions is above 11.5 after mixing. It is likely,
therefore, that a more sophisticated mixing, clarification
and sludge handling system which can be controlled closely
will be required.
84
-------
Section 4
Acknowledgements
Many individuals and organizations were involved in
the total project. The initial laboratory and pilot plant
studies were sponsored jointly by the Tanners Council of
America, The University of Cincinnati, The West Virginia
Water Resources Commission and The International Shoe
Company. The full scale studies were supported jointly by
the Federal Water Pollution Control Administration and The
International Shoe Company.
Individuals who have participated directly in the
project and their major role are as follows:
Mr. Stephen Graef, Mr. Stephen Lackey, Mr. John
Aldous and Mr. Lawrence Liu, Graduate Students from The
University of Cincinnati served as Project Engineers at
various times during the study. Mr. J. C. Burchinal,
Professor of Sanitary Engineering, West Virginia Univer-
sity and Mr. Edgar Henry, Director of the West Virginia
Water Resources Commission, served as consultants and
advisors on the Project. Mr. Stevan Pierce and Mr. Frederic
Lamoureux, Graduate Students from The University of Cincin-
nati, conducted specialized studies relating to the major
project. The late Mr. Richard Jones, former Superintendant
of The International Shoe Company Tannery and Mr. Thomas
Morrison, Superintendant of The International Shoe Company
Tannery, provided technical, financial and mechanical
assistance in all phases of the study. Mr. Harold E.
Cutup, of the International Shoe Company, served as
Assistant Project Engineer for the field studies and is
now in direct charge of the total project.
The support and guidance of: Dr. Riley N. Kinman,
formerly Project Officer, and Mr. Eugene Harris, current
Project Officer for the Federal Water Pollution Control
Administration; and Mr. William T. Roddy, Director of The
Tanners Council Research Laboratory of The University of
Cincinnati, are gratefully acknowledged.
85
-------
Section 5
References
1. Hommon, H.B., Public Health Bulletin No. 110 (1919).
2. Alsop, E.C., J. Am. Leather Chemists Assoc. 7, 72
(1912)
3. Bonsib, R.S. What Tanners Should Know about Sewage
Disposal, Tanners Council of America, New York
(1920)
4. Howalt, W., and Cavett, E.S., Proc. Am. Soc. Civil
Engrs., 1675 (1927).
5. Eldridge, E.F., Mich. State Coil. Exp. Sta. Bull.
Nos. 5, 82, and 83 (1938).
6. Maskey, D.F., J. Am. Leather Chemists Assoc. 36, 121
(1941)
7. Watson, K.S., Purdue Univ. Eng. Bull. Rxt. Ser. No.
68 (Vol. 33, No. 4) (1949).
8. McKee, J.E., and Camp, T.R., Sewage and Industrial
Wastes, 803 (1950).
9. Harnly, J.W., J. Am. Leather Chemists Assoc. 46, 170
(1951)
10. Redlich, H.H. , J. Am. Leather ChemistsAssoc. 48, 422,
(1953)
11. Spiers, C.H., Disposal md. Waste Materials Conference,
Sheffield, 219 (1956)
12. Haseltine, R.R., Sewage and md. Wastes, 30, 65 (1958).
13. Ceamis, M., Noxiousness and Purification of Tannery
Waste Waters, Irid. usoara (Bucharest) 2, 208-15
(1955). Abstracted from (CA:535717g)
14. Jansky, K., Tannery Waste Water Disposal, Kozarstvi,
11, 32729, 35560 (1961) . Abstracted from
(JALCA:57-282)
15. Rosenthal, B.L., Treatment of Tannery Waste Sewage
Mixture on Trickling Filters, Leather Mfg., 74, No.
12, 20 (1957).
87
-------
16. Guerree, H., Purification of Tannery Waste Water, Bull.
Assoc. Franc. Ingrs. Chimistes Techniciens m c i. Cuir
Doc. Inferm Centre Tech. Cuir, 26, 95-97 (1964).
Abstracted from (JALCA:59-709)
17. Eye, J.D. and Graef, S.P., Pilot Plant Studies on the
Treatment of Beainhouse Wastes from a Sole Leather
Tan nery, J. Am. Leather Chemists Assoc. Vol. 63,
No. 6, June, 1968.
18. Domanski, J., Sedimentation of Suspension in Coagu-
lation of Sewage from Tanning Industry, Gaz. Woda
Tech. Sanit. 38, 27982 (1964). (Pol.) Abstracted
from (CA:6215897D) U
19. Sproul, O.J., Keshavan, K., and Hunter, R.E., Extreme
Removals of Suspended Solids and BOD in Tannery
Wastes by Coagulation with Chrome Dump Liquor, Purdue
Univ. Ext. Ser., No. 121, Vol. L, No. 2 (1966)
20. Scholz, H.G., Modern Effluent Water Disposal in the
Leather Industry-Effects and Cost, Lectures during
the 8th Congress of the International Union of
Leather Chemists Societies, 95-125, (1963)
21. Ivanof, G.I., Anaerobic Purification of Tannery Waste,
Kozh. Obuvn. Prom., 4, No. 7, 3033 (1962).
22. Toyoda, H., Yarisawa, T., Futami, A., and Kikkawa, M.
Studies on the Treatment of Tannery Wastes, Nihon
Hikaku Gijutsu KyokaiShi, 8, 79-92 (1963).
23. Gates, W.E., and Lin, S., Pilot Plant Studies on the
Anaerobic Treatment of Tannery Effluents, J. Am.
Leather Chemists Assoc., 61, 10 (1966).
88
-------
Section 6
Appendix
89
-------
Table A-i:
Performance of Clarification System
o
Overflow
Rate
gpd/ft 2
Date
Suspended
Solids Total
COD
A-i0
Inf.
mg/i
Eff.
mg/l
Red. Inf.
% mg/l
Eff.
mg/i
Red.
%
Inf.
mg/i
Eff.
mq/1
Red.
%
Dose
mg/i
11. 2
10. 0
None
9.9
9.6
9.6
9.8
9.6
9.8
12.0
11. 2
10. 1
11. 9
13.2
10. 2
11.3
9.4
9.8
9.5
10. 3
1/3/68
5420
480
91.0
7560
3176
58.0
885
4
5000
460
90.8
6750
2913
56.8
885
5
3220
2920
9.3
5546
4798
13.5
1090
8
2820
600
78.7
4464
2960
33.7
1060
9
4140
540
87.0
6720
2544
60.6
1520
10
3760
400
89.4
6008
2864
51.7
860
1/11/68
2640
500
81.0
3136
2448
21.9
1220
12
3360
460
86.3
5704
2624
53.8
1400
15
3680
520
85.9
3584
2504
30.1
1560
16
3800
440
88.4
6744
2480
63.2
1410
17
3540
480
86.5
5776
1712
70.3
1220
18
3860
600
84.5
5880
2304
60.7
1200
19
3800
400
89.5
6208
2464
60.3
775
1/22/68
3380
320
90.5
5312
2160
59.3
2910
1888
35.2
380
23
2580
280
89.2
4240
1936
54.4
3425
1616
52.7
625
24
3360
320
90.5
4728
2288
51.7
3304
1898
42.5
505
25
3180
500
84.3
4792
2488
48.2
3646
2383
34.7
1290
26
2220
600
73.0
4296
2440
43.2
3328
2403
27.8
1240
29
3040
500
83.6
1870
1220
34.8
2812
2404
14.5
1390
30
3420
420
87.7
5600
2496
55.4
3775
2195
41.8
1430
31
3460
620
82.0
4664
1680
64.0
3311
2286
31.0
1450
2/1/68
3980
960
76.0
5776
3312
42.7
3868
2415
37.6
7.1
1410
2
3520
2600
26.2
5200
4864
6.5
3524
3221
8.6
6.8
1390
5
4420
920
79.2
6832
3168
53.6
3911
2767
29.3
5.7
1400
6
4360
1660
61.9
6984
4008
42.6
3954
2775
29.8
-------
Table A-i:
Performance of Clarification System
Date
Suspended
Solids
Total
Alkalinity
COD
A-109
Overflow
Inf.
mg/i
Eff.
mg/i
Red.
%
Inf.
mg/i
Eff.
mg/i
Red.
%
Inf.
mg/i
Eff.
mg/i
Red.
%
Dose
mg/i
Rate
gpd/ft 2
2/7/68
4060
840
79.3
6304
4136
34.4
3802
2283
39.9
3.7
1410
8
5360
720
86.6
7480
2800
62.6
4512
2427
46.3
3.7
1410
9
4760
800
83.2
7280
3088
57.6
3910
2336
40.2
10.3
1540
15
5780
480
91.7
7944
2656
66.6
5041
2327
53.7
10.1
1500
16
4500
800
82.2
7264
2872
60.3
4214
2304
45.2
9.6
1390
19
4680
680
85.5
5944
2560
57.0
3999
2297
42.6
7.9
1520
20
3920
360
90.8
4952
2880
41.7
3917
2398
38.7
9.7
1520
21
3120
600
80.8
4576
2880
37.2
3929
2340
40.3
9.3
1540
22
4640
880
81.1
6544
3168
51.5
3081
2692
12.6
8.0
1540
23
3880
580
85.0
5376
2704
49.8
5400
2347
56.5
8.0
1550
26
6040
2120
65.0
7264
4320
40.6
7040
3688
47.6
7.4
1550
27
3700
680
81.6
7.9
1550
28
3340
360
89.2
5208
2624
49.6
4465
2575
42.3
8.1
1550
29
3160
400
87.3
8.0
1520
3/1/68
4220
3240
23.2
5740
5548
3.4
5896
3775
36.0
8.2
1500
4
3460
700
79.8
4707
3040
35.3
4183
2887
31.0
8.4
1580
ii
3800
920
75.8
4416
3200
27.5
3764
2801
25.6
6.1
1640
12
3660
660
82.0
8.8
1620
13
3360
560
83.3
4624
2608
43.4
4559
2872
36.9
8.8
1590
14
3680
680
81.5
8.8
1590
15
3998
560
86.2
5248
2704
48.6
4713
2386
49.3
9.4
1590
18
3220
560
82.6
4192
2520
40.0
4209
2414
42.6
9.3
1590
19
5680
1040
81.7
10.3
1590
20
5060
700
87.2
6216
2424
61.0
9.0
1600
21
3900
580
85.1
7.8
1600
22
4980
500
90.0
5024
2672
46.8
7.9
1600
4/1/68
2680
220
91.8
4624
2952
36.2
8.8
1520
2
3980
440
88.9
8.3
1590
3
5960
420
92.8
7616
3080
59.4
9.6
1610
-------
Table A-2:
Performance of Clarification System
Inf.
TSS FSS
Eff.
TSS FSS
Removal
TSS FSS VSS
A-b
Dose
mg/i
Overflow
Rate
gpd/ft 2
Date
6/11/68
7620
6840
180
100
97.6
98.5
89.7
8.6
1600
12
7400
6100
580
320
92.2
94.6
80.0
10.2
1600
13
4620
2640
420
80
90.9
96.8
82.8
10.6
1600
14
4760
2540
540
280
88.7
89.0
88.4
9.8
1600
17
3660
1620
560
180
84.7
89.0
81.4
9.4
1600
18
7100
6180
720
400
89.9
93.6
65.3
9.1
1600
19
3400
3200
380
180
88.8
95.0
0.0
10.2
1600
20
5600
3280
540
180
90.4
94.5
85.5
10.8
1600
21
3700
2640
380
220
89.7
91.7
85.0
10.3
1600
24
1760
860
320
80
81.8
90.8
73.3
10.0
1600
25
5120
4100
520
200
89.8
95.2
68.0
10.6
1600
26
4720
3800
680
260
85.6
93.2
54.4
10.2
1600
7/15/68
3220
1640
340
80
89.4
95.2
83.5
8.8
1600
16
6940
6160
560
320
91.9
94.7
69.3
9.7
1600
17
7200
6020
380
220
96.4
96.4
86.5
9.9
1600
18
4760
2300
500
100
89.5
95.6
83.7
9.5
1600
19
4240
2980
320
160
97.2
94.6
87.3
8.7
1600
22
4720
4020
600
320
87.3
92.8
60.0
10.2
1600
23
5110
3240
360
180
92.9
94.4
90.5
9.5
1600
24
4200
1800
320
140
92.4
92.3
92.3
9.8
1600
25
2760
920
700
200
74.6
78.2
72.8
410
20003000
26
5980
4500
920
500
84.6
88.9
71.6
410
20003000
29
5800
3140
1080
560
81.4
82.1
80.4
410
20003000
30
6220
5580
720
500
88.4
91.1
65.6
410
20003000
31
5600
3480
520
200
90.7
94.3
84.7
410
20003000
-------
Table A-2:
Performance of Clarification System
Date Influent Effluent Removal - A-b Overflow
Dose Rate
TSS FSS TSS FSS TSS FSS vss mg/i gpd/ft 2
8/1/68 5540 4600 480 420 91.4 90.7 93.7 410 20003000
2 3720 2060 380 140 89.8 93.2 85.5 410 20003000
5 6400 5200 1880 760 70.6 85.2 6.7 410 20003000
6 5160 4340 340 160 93.4 96.4 78.0 410 20003000
7 6260 5760 880 140 85.9 97.6 410 20003000
8 11580 11120 460 180 96.0 98.3 39.1 410 20003000
9 3960 2400 340 140 91.4 94.2 91.0 410 20003000
12 7100 3700 340 40 95.2 99.0 91.1 410 20003000
13 4300 2620 2480 1160 42.3 58.0 21.4 410 20003000
14 4580 3560 120 97.4 410 20003000
15 6600 4380 200 40 97.0 99.1 92.8 410 20003000
16 5680 2760 280 80 95.1 410 20003000
19 5100 4180 740 360 85.5 78.0 410 20003000
20 2980 3780 0 20003000
21 2580 980 2720 1100 0 20003000
22 3420 1920 1300 940 32.7 21.9 61.8 0 20003000
23 2320 1640 540 160 76.7 58.5 8.0 20003000
26 2880 1740 1820 640 36.8 34.5 0 20003000
27 2880 1740 1660 1000 42.3 34.5 34.0 8.2 3460
28 2320 1000 920 380 60.3 8.0 3460
9/3/68 3380 2160 880 400 74.0 81.5 60.6 7.4 3460
4 2060 940 860 400 58.3 57.5 58.8 6.8 3460
9 2380 800 3840 2480 45.1 0
10 3540 2160 8740 2200 36.5 0
11 5220 2640 1860 1140 64.4 56.7 72.2 410
-------
Table A2:
Performance of Clarification System
Date
Influent
TSS FSS
Effluent
TSS FSS
Removal
TSS FSS VSS
A-b
Dose
mg/i
Overflow
Rate
gpd/ft 2
2980 1580
6660 6140
900 520
1240 640
2740
2420
9/12/68
17
18
19
20
23
24
25
2280
5900
2320
4180
2300
2900
6460
2720
1380
2860
1820
2880
1080
1840
4920
1800
920
500
480
1200
560
1760
1000
1020
240
220
240
380
380
1420
21.1
84.4
78.5
88.5
47.8
80.7
72.8
63.2
34.8
91.6
87.8
91.7
64.8
79.3
71.0
23.5
77.5
44.0
81.6
32.8
83.0
78.0
410
410
410
12.0
5.0
2000
2200
2520
2520
2520
2520
2670
26
27
69.8
81.4
67.0
91.2
72.8
7.0
8.2
10/1/68
3
4
8
10
11
4760
6480
10180
3740
3500
3740
2980
4380
9220
2580
3220
1760
1180
940
1480
1160
660
820
600
320
880
400
240
340
75.2
85.5
85.5
69.0
81.1
78.0
80.0
95.0
90.5
84.4
92.5
80.6
67.5
70.4
37.6
34.5
75.8
7.4
7.5
6.9
6.2
6.2
5.6
2700
2460
2420
2450
2460
2660
11/11/68
12
13
14
15
6760
7220
5300
4660
4320
5080
5340
2700
3860
2060
1400
1460
1460
1200
1780
680
520
580
760
700
79.3
79.8
72.5
74.2
58.8
86.7
90.2
78.5
80.4
66.0
57.2
50.0
69.6
45.0
52.2
5.9
4.7
6.1
6.5
7.0
2720
2660
2610
2480
2000
18
19
20
3840
5960
5520
2360
5300
4740
680
1400
780
320
900
560
82.3
76.5
85.9
86.5
79.2
88.4
75.6
24.2
71.8
8.7
4.9
6.7
2020
1940
2340
-------
Table A-2: Performance of Clarification System
A-b Overflow
Dose Rate
mg/i gpd/ft 2
Date
Influent
Effluent
Removal - %
TSS
FSS
TSS
FSS
TSS
FSS VSS
C ;
11/21/68
6900
6100
1080
640
84.4
89.6
45.0
4.4
2260
22
6640
4520
1400
600
78.9
86.7
62.4
6.3
2290
26
4680
2440
1020
360
78.2
85.2
70.5
6.9
2290
27
4640
3700
1640
820
64.7
77.8
12.8
5.6
2340
29
4160
2920
1640
780
60.6
73.4
30.6
3.7
2450
12/2/68
4240
2040
1240
500
70.8
75.4
66.4
5.8
2470
3
3520
2240
1420
600
59.7
73.2
36.0
5.6
2530
4
4980
2720
2440
840
51.0
67.6
29.2
5.8
2460
5
3780
2680
600
320
89.4
88.0
74.5
6.7
2290
6
4240
2580
1240
420
70.6
83.6
50.6
8.5
1930
12/9/68
3420
2480
600
280
-82.5
88.6
66.0
9.5
1840
10
6160
4840
2740
1660
55.5
65.7
16.7
6.1
2740
11
3200
2200
1340
740
58.1
66.4
40.0
6.6
2600
12
4400
3060
2720
1340
38.1
56.2
5.9
2720
13
3780
1680
1320
560
65.1
66.6
63.8
4.3
2680
17
4720
3400
1260
580
73.3
82.9
49.0
4.8
2720
18
4240
3300
1860
1080
56.1
66.7
17.0
6.2
2620
19
5120
3480
1120
680
78.1
80.6
73.2
6.5
2260
20
4440
2840
1200
540
73.0
81.0
58.7
4.8
2460
12/23/68
6220
4160
1860
800
70.1
80.6
48.5
4.5
2500
24
3660
2080
560
220
84.7
89.5
78.3
14.9
2630
26
3280
2040
1280
420
70.0
79.5
30.6
8.8
2580
27
5760
4360
1240
840
78.5
80.7
71.4
9.8
2580
30
6120
3760
1240
400
79.7
89.3
64.5
9.6
2660
-------
Table A-2: Performance of Clarification System
Removal %
TSS FSS VSS
A-lU
Dose
mg/i
Overflow
Rate
gpd/ft 2
Date Influent Effluent
TSS FSS TSS FSS
12/31/68
3660
1000
880
280
76.0
72.0
77.5
10.9
2610
1/2/69
3
6
7
8
9
10
4400
6220
5000
5680
4640
6280
3500
3620
3500
4540
4560
3380
5400
2380
1140
620
1080
920
920
1320
940
400
200
380
420
240
540
580
74.1
90.0
78.4
83.8
80.2
79.0
73.1
89.0
94.3
91.7
90.6
92.8
90.0
75.7
5.1
84.4
55.4
46.0
11.4
67.8
11.1
8.5
8.9
9.2
8.1
5.2
7.3
2580
2640
2500
2530
2640
2460
2540
13
14
15
16
17
3260
3960
4640
4340
3140
1720
2480
3860
3160
1440
1220
1380
740
1080
1260
460
520
340
340
440
62.6
65.2
84.1
75.1
59.9
73.3
79.0
91.6
89.1
69.5
50.7
41.8
48.7
37.3
51.8
6.1
8.5
5.8
7.0
9.3
2600
2480
2470
2460
2420
20
21
22
23
24
6020
4960
4260
5680
7500
4660
3920
3020
4360
4240
620
780
820
760
600
220
380
380
260
160
89.7
87.5
80.8
86.6
92.0
95.1
90.4
86.8
93.8
96.2
71.8
61.6
64.5
62.2
65.1
9.4
7.1
6.3
8.2
8.6
2480
2420
2690
2570
2560
27
28
29
30
9780
6140
4960
4800
8780
5320
3760
3560
600
1180
1840
780
220
500
780
240
93.9
80.8
62.9
83.8
97.7
90.6
79.2
93.2
62.0
17.1
11.7
56.5
10.6
11.0
10.1
10.1
2420
2420
2420
2440
-------
Table A-2:
Performance of Clarification System
Date
Influent
Effluent Removal - % A-b
Dose
Overflow
Rate
TSS
FSS
TSS
FSS TSS
FSS VSS mg/i
gpd/ft 2
2/1/69
3
4
5
6
7
5220
7220
3760
7200
4760
4300
2820
5780
2600
5820
1920
2640
440
980
1340
1160
1540
620
200
340
740
540
460
240
91.6
86.4
64.4
83.9
67.7
85.6
93.0
94.0
69.2
90.7
76.0
90.8
90.0
55.6
48.3
55.0
62.0
77.0
9.0
8.7
8.3
7.7
8.3
8.4
2450
2500
2460
2450
2450
2410
2/10/69
11
12
13
14
4220
4800
3480
4020
3820
3300
4340
2000
2840
2040
1000
1040
1200
1160
440
600
480
200
580
200
76.3
78.3
65.5
71.1
88.5
81.7
89.1
90.0
79.5
90.2
56.5
32.4
42.3
86.6
8.1
8.5
8.3
8.5
9.2
2440
2420
2440
2420
2420
17
18
19
20
21
6980
2720
5580
4620
7680
5760
1380
4200
3600
6080
500
980
740
800
1260
180
380
400
480
540
92.8
64.0
86.7
82.7
83.5
96.7
72.4
90.5
86.7
91.1
73.7
55.2
75.3
68.6
55.0
9.5
9.2
8.2
10.5
10.7
2460
2420
2460
2380
2450
24
25
26
27
28
3480
5420
4180
6400
3900
1640
4740
3300
5600
2680
780
580
340
880
680
240
240
140
440
400
77.6
89.3
91.9
83.3
82.6
85.3
95.0
95.7
92.3
88.3
70.7
50.0
77.3
40.0
81.6
9.5
10.0
9.8
9.3
8.6
2390
2430
2430
2520
2500
-------
Table A3: Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Suspend-id
Fixed
Inf. Eff.
Solids
Vol at i 1 e
Inf. Eff.
Feed: Beamhouse Wastes Only:
9.3 8.1
8.9 8.2
30 10.4 8.2
31
Det. Time - 10 days
20 2280
20 140
60 1860 160
Date
pH
Inf. Eff.
Total
Alkalinity
Inf. Eff .
COD
Inf. Eff.
10/1/68
2
12.0
8.0
4
11.8
8.2
7
11.8
8.2
c -c
582
568
650
468
1510
696
2147
2150
2316
2627
1 Part
10 days
8
9
10
11
10/14/6 8
15
17
21
22
23
24
25
28
29
866
1079
687
494
Spent Tan Liquors:
11.9 8.2
12.0 8.2
Feed: 3 Parts Beamhouse Waste:
Det. Time -
8.9 8.1
310
8.8 8.2
8.9 8.1 360
8.7 8.2 502
9.4 8.2 764
385
3778
385
5543
643
524
2183
705
120
520
2597
721
140
516
260
-
380
392
528
80
1540
520
700
20 920
40 1140
20 1320
5650 874
2456 1084
140
100
100
0
40
5499 859
-------
Table A-3:
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
Date
pH Total
Alkalinity
Inf. Eff . Inf. Eff.
COD
Inf. Eff.
Feed: 3 Parts Beamhouse
Waste:
1 Part Spent Tan Liquors:
Det.
Time
- 10 days
11/1/68
10.8
8.2
560
20
680
20
4
9.2
8.0
544
604
4896
1267
260
20
920
40
5
9.6
8.2
5973
1058
220
20
1300
40
6
9.9
8.2
1044
476
6115
733
400
20
2000
60
7
10.0
8.2
6025
874
420
20
1440
20
8
10.3
8.1
1264
496
5039
923
520
20
1340
140
11
11.8
8.1
2844
524
7494
886
880
60
2400
80
12
10.0
8.2
4932
822
360
60
1580
140
13
9.8
8.1
816
464
3913
880
240
40
1400
180
14
9.4
8.2
6460
866
200
40
1360
320
15
11.8
8.2
1084
484
2789
1050
200
160
540
100
18
6.8
8.2
80
496
1064
20
140
260
480
19
9.7
8.3
4924
796
200
0
1120
40
20
9.9
8.3
952
404
5768
804
400
60
1420
260
21
9.7
8.3
6444
806
340
40
1500
40
22
9.9
8.3
1104
416
6360
932
380
60
1380
40
26
9.8
8.3
5073
914
220
40
1620
220
27
10.1
8.2
1064
456
5691
873
140
60
2320
220
29
9.9
8.0
1124
404
5334
1034
-------
Table A-3:
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
pH
Inf. Eff.
Fixed
Inf. Eff.
Volatile
Inf. Eff.
21
22
Feed: 3 Parts Beamhouse Waste: 1 Part Spent
1 L Sewage: Det. Time - 15 days
Tan Liquors:
Date
Total
Alkalinity
Inf. Eff.
COD
Inf. Eff.
Suspended Solids
12/2/68
11.4
8.2
1056
560
2703
1042
160
60
680
200
3
9.4
8.2
6089
1059
240
40
1940
240
4
9.6
8.2
800
476
5926
1148
320
80
1460
280
5
9.4
8.1
5230
1053
280
40
1420
180
6
9.9
8.1
972
482
4788
1142
360
120
1400
200
7
10.0
8.2
6414
1153
440
0
1940
180
8
9.9
8.2
6255
1146
580
40
2140
320
9
9.6
8.3
884
520
7048
1182
360
20
2300
380
10
10.8
8.3
4670
1203
380
80
1140
420
11
11.1
8.2
1200
412
4249
1283
280
20
1300
340
12
10.2
8.2
3722
1305
400
320
1020
200
13
9.8
8.2
5946
1184
540
240
2080
200
14
9.4
8.2
6918
1088
560
40
2300
320
15
9.1
8.2
16,344
1103
880
40
5480
260
16
9.2
8.2
4770
1306
360
40
1260
320
17
9.4
8.1
6701
1614
380
160
2220
460
18
9.3
8.1
7196
1551
420
60
2020
500
19
10.1
8.1
7706
1788
700
140
2880
600
20
11.2
8.2
1444
620
6922
1763
660
120
2420
500
9.8
10.2
8.1
10.2
1020
1040
636
608
6114
6092
1813
1656
520
840
160
840
2360
1580
740
1580
-------
Table A-3:
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
Feed: 3 Parts Bearrthouse Waste: 1 Part Spent
1 L Sewage: Det. Time - 15 days
Tan Liquors:
Date pH
Inf. Eff.
Total COD
Alkalinity
Inf.
Eff. Inf. Eff.
12/23/68
10.1
8.2
856
612 5312
1711
420
220
1560
480
24
10.4
10.4
7898
1662
600
80
2100
160
25
9.8
8.1
796
712 5051
1969
320
200
1460
360
26
9.5
8.2
5600
1859
360
160
1780
500
27
10.4
8.2
1764
592 7286
1315
380
240
2140
480
Anaerobic
Zone Thoroughly
on 12/27/68
Mixed
28
10.0
8.1
1240
1316 6795
3248
540
700
2440
1560
29
11.7
8.1
1316
2152 5496
5259
520
1780
2140
2980
30
8.3
8.2
780
1280 8824
3318
2560
800
4320
1860
31
8.9
8.2
5333
5584
220
1660
2000
3740
Feed:
Beamhouse
Wastes - Det.
Time
10
Days
1/2/69
11.4
8.1
4345
5282
400
780
1040
2660
3
11.8
8.1
1200
976 7093
4130
400
540
1280
1920
6
11.6
8.1
1228
952 4097
4306
380
580
1200
2140
7
8.6
8.2
5992
3152
560
280
1340
1020
8
10.3
8.1
952
576 4031
2322
360
260
1160
760
9
8.2
8.1
7539
1800
340
200
2260
620
10
8.3
8.1
564
520 4523
1800
240
160
1320
560
-------
Table A-3: Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Suspended Solids
Va 1 at lie
Inf. Eff.
28
29
9.7 8.0
9.7 8.0
976 608
1316 636
6314 1898
8824 1843
480 180
560 200
900
880
800
820
860
500
580
2060 460
2440 640
Date
pH Total
Alkalinity
Inf. Eff. Inf. Eff. Inf.
COD
Fixed
Eff. Inf. Eff.
Feed: Bearnhouse Wastes
- Det.
Time 10 Days
1/11/69
10.0
8.0 1500 516 7907
1751 560 140
2060
620
12
10.5
8.0 2728 576 12279
2165 1000 80
4240
740
13
10.7
8.0 940 696 3361
1977 280 140
1280
740
14
10.5
8.0 3678
2041 240 180
1320
620
15
9.8
8.0 1488 740 7830
2258 700 140
2780
840
16
10.1
8.0 6704
2358 600 260
2180
800
17
10.3
8.0 1440 764 6674
2388 600 280
2220
820
18
9.6
8.0 1416 732 8962
2091 420 200
2900
900
19
9.2
8.1 596 744 5494
2375 260 240
1640
1080
20
9.8
8.1 764 756 5055
2153 240 180
1500
900
Feed:
2 Parts Bearnhouse Waste: 1 Part Spent Tan Liquors
0.9 L Sewage: Det. Time - 20 Days
21
9.9
8.0 964 740 5460
2307 340 240
2940
22
9.6
8.0 1204 712 7051
2235 600 240
2400
23
9.8
8.0 1368 692 7815
2222 680 260
2460
24
8.0 1568 696 9260
2252 680 240
3260
25
9.9
8.0 1104 720 7509
2174 520 220
2540
26
10.0
8.0 1240 664 6560
1778 440 140
2120
27
10.5
8.0 1248 620 6363
1818
-------
Table A-3:
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
pH
Inf. Eff.
Total
Alkalinity
Inf . Eff.
COD
Inf. Eff.
Fixed
Inf. Eff.
Volatile
Inf. Eff.
Feed: 2 Parts Bearnhouse Waste: 1 Part Spent Tan Liquors
0.9 L Sewage: Det. Time - 20 Days
Feed: 2 Parts Beanthouse Waste: 1 Part Spent
Det. Time - 20 Days
Date
Suspended Solids
31 9.1
8.0 1080 1096 8992 2311
2/1/69
900
2
856
3
964
4
900
5
936
6
1192
7
532
340 260
400 120
1620 960
2260 860
8.9
8.0
704
10679
2532
320
120
3040
880
8.4
8.0
756
19960
2804
680
160
10720
1380
10.2
8.0
700
6951
2827
300
220
1900
1160
9.2
8.0
700
6948
3334
400
200
2600
1540
9.3
8.0
680
8315
3176
580
360
2840
1360
10.1
8.0
696
6881
2859
600
340
2220
1220
7.9
8.1
700
8192
3117
240
120
1580
1260
8
8.7
8.0
420
684
4157
2557
320
120
1440
1120
9
9.7
8.1
632
668
4353
2635
360
220
1300
1100
10
10.2
8.1
664
600
3020
2247
260
140
1200
460
11
10.1
8.1
972
632
4733
2090
360
200
1680
560
12
9.6
8.1
668
568
7139
1908
480
160
4580
620
13
9.4
8.1
980
572
8006
1785
340
140
2660
480
14
9.5
8.1
960
556
7089
1656
400
80
2160
440
2/15/69
9.2
8.0
928
564
8276
1497
280
100
2540
400
16
8.6
8.0
784
572
15840
1394
620
160
5980
240
Tan Liquors
-------
Table A-3:
Performance Characteristics of
AnaerobicAerobic Pilot Unit
Date pH
Inf. Eff.
Total COD
Alkalinity
Inf. Eff. Inf. Eff.
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
Feed: 2 Parts
Bearrthouse Waste: 1 Part Spent
Det. Time - 20 Days
Tan Liquors
Feed: 2 Parts Beainhouse Waste: 1 Part
0.9 L Sewage: Det. Time -
Spent Tan
20 Days
5392 3021
6904 2777
Liquors
340 240
380 180
2100 1120
1900 960
2/17/69
18
19
20
21
10.1
9.1
9.1
9.8
8.5
8.0
8.0
8.1
8.1
8.1
888
744
940
668
460
596
680
736
664
640
6772
7438
8821
9660
7883
1798
2833
2758
2344
380
400
240
360
240
200
260
400
280
220
1500
2600
2620
1500
1560
440
1120
1040
780
740
22
23
24
25
26
27
28
7.9
7.7
9.6
8.0
9.0
9.0
9.0
8.1
8.1
8.1
8.1
8.1
8.1
8.1
502
504
828
696
804
840
804
664
648
682
636
668
660
644
6141
6257
5854
J0752
6112
10280
8630
2314
2065
2284
2430
2679
2671
2664
220
200
380
320
220
360
440
200
200
280
180
260
220
240
1440
1560
2020
2480
1140
2080
2280
780
640
1000
920
940
900
1040
8.8
8.9
9.5
4.2
8.1
8.1
8.1
8.1
876
796
868
716
740
740
680
9798
7385
10566
6730
2749
2881
2969
2753
320
380
380
120
300
240
220
160
2280
2100
3640
1320
1060
1260
1200
860
3/1/6 9
2
3
4
3/5/69
6
9.5 8.1
9.4 8.1
700
760
700
620
-------
Table A-3:
Performance Characteristics of
AnaerobicAerobic Pilot Unit
Total
Alkalinity
Inf. Eff.
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
Date pH
Inf. Eff.
COD
Inf. Eff.
Feed: 2 Parts Bearrthouse Waste:
).9 L Sewage: Det.
1 Part Spent Tan
Time - 20 Days
Liquors
3/7/69
6.6
8.1
280
720
5923
2981
120
220
1200
1220
8
8.8
8.2
644
600
5770
2960
200
160
1580
1280
9
5.4
8.3
96
580
6344
2408
380
140
2000
760
10
9.8
8.3
828
600
4946
2408
80
160
1420
1040
11
9.3
8.2
1228
588
10269
2480
640
160
3540
1080
12
9.4
8.2
788
564
6820
2573
460
160
1440
1000
13
9.9
8.2
1024
560
5770
2339
560
160
1840
820
14
7.2
8.2
508
612
5308
2623
200
160
800
1100
15
6.5
8.2
480
644
6980
2452
80
240
1240
1260
16
7.1
8.2
500
564
6753
2083
100
140
2200
640
17
8.3
8.2
428
636
4263
2496
220
260
1100
1160
18
7.1
8.2
604
600
7634
2635
60
180
1140
960
19
6.9
8.2
584
588
4942
2452
40
200
560
800
20
7.9
8.2
340
560
6263
2452
60
100
960
820
21
6.2
8.2
220
540
5352
2342
60
100
820
700
22
6.5
8.2
236
760
12866
2364
420
480
5640
2680
23
6.3
8.2
364
540
6355
2403
80
80
1640
580
24
5.8
8.1
164
520
8870
2004
240
120
3280
1000
25
9.8
8.0
836
484
6415
2051
360
140
1680
500
26
8.3
8.0
600
536
7765
2565
320
260
1880
2040
27
8.1
8.1
884
472
17608
2298
880
180
7120
460
28
6.8
8.0
540
516
7040
2137
140
60
1240
780
-------
Table A-3 Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date pH
Inf. Eff.
Total
A 1k a 1 in i ty
Inf. Eff.
COD
Inf. Eff.
Suspended
Fixed
Inf. Eff.
Solids
Vol at i le
Inf. Eff.
0
C )
120
120
400
560
140
200
100
180
120
360
Feed: 2 Parts Beanthouse Waste:
0.9 L Sewage: Det.
1 Part
Time
Spent Tan
20 Days
Liquors
Spent
Tan
Liquors
280
120
440
480
560
4/1/69
2
3
4
5
5.7
7.4
9.4
7.5
11.1
8.0
8.1
8.1
8.1
8.0
216
360
800
480
1036
524 7192
516 5394
464 7038
496 16186
600 5410
2678
2566
2408
2390
2761
1280
1200
1920
6820
1680
1160
740
860
760
1960
7
8
9
10
11
5.6
3.5
9.6
8.7
9.5
8.0
8.0
8.0
7.9
7.9
164
0
1020
660
1120
656 3769
516 7114
492 10578
472 8880
524 6972
2798
2812
2794
3027
2734
1240
1520
4380
1520
2000
720
1350
740
1540
760
12
13
14
9.3
5.8
9.6
8.0
8.0
8.0
1372
148
1216
572 11048
664 8332
644 14498
3175
3377
3267
3200
1320
5060
1560
1980
920
Feed:
2
Parts
Bearrthouse Waste:
Det. Time - 20
1 Part
Days
15
16
17
18
19
8.4
9.8
9.9
9.8
10.0
8.1
8.1
8.1
8.1
8.1
524
964
1136
1000
1260
620 7410
628 7788
624 7488
616 8699
684 8528
3176
2911
2624
2881
3570
240
440
440
100
260
180
180
320
2300
2340
2060
1120
500
840
780
2020
200
200
140
240
200
560
320
960
240
260
220
-------
Table A-3:
Total
Alkalinity
Inf. Eff.
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Suspended Solids
Fixed Volatile
Inf. Eff. - Inf. Eff .
Feed: 2 Parts
Beamhouse Waste: 1 Part
Det. Time - 20 Days
Spent Tan Liquors
Date pH
Inf. Eff.
COD
Inf. Eff.
4/20/69
9.8
8.1
1084
960
7104
3370
540
340
2620
1500
21
5.5
8.1
204
828
7797
3042
480
220
2520
840
22
7.9
8.1
576
676
18757
2724
640
120
6940
720
23
10.4
8.1
1364
768
8586
2896
780
320
2560
1140
24
7.7
8.1
524
724
8306
3780
380
200
2220
1180
25
10.1
8.1
1256
764
8137
4136
480
280
2300
1520
26
9.1
7.8
1200
940
8535
4412
560
480
2640
2680
27
4.8
7.9
104
744
18967
3896
400
240
7560
1640
28
8.5
8.0
376
744
2824
3979
140
420
300
1740
29
9.0
7.8
804
744
7545
4185
540
440
1820
1800
30
9.1
7.8
1000
644
9481
3327
440
180
2360
1080
5/1/69
9.0
7.7
1284
752
11560
5073
720
240
3760
2240
2
10.6
7.8
1128
720
4408
3061
540
200
1500
1040
3
10.1
7.8
1140
920
5271
4607
720
580
1780
2180
4
9.7
7.8
1368
860
8289
2917
1000
480
3620
1780
5
8.3
7.9
748
696
13207
2979
640
240
4380
1320
6
7.8
7.9
652
972
7750
3812
220
520
1560
2480
7
6.3
7.8
476
684
8095
2869
160
220
1040
1100
8
6.8
7.8
784
652
11631
3340
180
240
1660
980
9
9.3
7.8
820
648
5870
3405
300
200
1700
1140
10
8.0
7.8
682
976
7938
4903
400
500
2260
2220
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Table A-3:
Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
pH Total
Alkalinity
Inf. Eff. Inf. EU. Inf. Eff.
Date
COD
Feed: 2 Parts Beamhouse Waste: 1 Part Spent Tan Liquors
Det. Time - 20 Days
Suspended Solids
Fixed Volatile
Inf. Eff. Inf. Eff.
5/11/69
8.1
7.8
480
964
6459
4222
360
240
2020
2110
12
9.3
7.9
752
736
8778
3327
540
360
2080
1220
13
7.7
7.8
556
664
9018
2906
320
120
2260
1500
14
6.2
7.8
320
620
7766
2636
180
40
1280
400
15
6.8
7.9
376
624
8813
2938
160
140
1240
980
16
7.0
7.9
404
636
6288
3064
160
120
1420
920
17
7.2
7.8
684
664
8660
3242
280
200
2240
1200
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Table A-4: Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date TKN M monia Organic Total
Nitrogen Nitrogen Sulf ides
Inf. Eff. Inf. Eff. Inf. Eff. Inf. Eff.
Feed: 3 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
Det. Time - 10 days
10/22/68 273 160 179 127 94 34 15 9
24 222 163 121 126 102 38 13 6
29 207 159 111 121 96 38 18 15
31 321 114 187 106 134
11/5/68 216 132 105 99 ill 33
7 221 128 104 101 117 27 16 13
12 217 128 107 95 110 33 14 13
14 202 128 94 94 108 34 12 15
19 211 122 95 88 116 34 12 11
21 221 112 101 83 121 29 16 13
26 188 116 70 78 118 39 16 10
Feed: 3 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
1 L Sewage: Det. Time 15 Days
12/3/68 237 112 114 76 124 37 16 13
5 204 114 98 73 106 41 17 12
10 237 118 116 73 122 45 17 12
12 245 115 109 73 137 43 16 10
17 220 126 103 74 118 53 13 11
19 255 140 126 81 129 59 17 11
26 267 138 139 80 129 59 9 10
31 200 266 83 85 117 182 14 12
Feed: Bearnhouse Wastes Only
Det. Time - 10 Days
1/2/69 190 229 67 75 123 154 14 10
7 195 146 90 75 105 70 13 7
9 251 141 119 75 132 66 10 6
14 241 155 124 83 117 73 8 6
16 253 167 125 85 128 82 10 7
109
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Table A-4: Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date TKN Ammonia Organic Total
Nitrogen Nitrogen Sulfides
Inf. Eff. Inf. Eff. Inf. Eff. Inf. Eff.
Feed: 2 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
0.9 L Sewage: Det. Time - 20 Days
1/21/69 220 161 108 84 112 77 11 8
23 256 153 135 82 121 71 16 11
1/28/69 233 141 123 81 110 60 9 10
30 218 155 117 80 101 75
2/4/69 231 166 102 75 129 91
6 259 160 128 78 131 82
11 183 136 84 81 99 55
Feed: 2 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
Det. Time - 20 Days
2/13/69 207 126 113 78 95 47
18 233 144 110 70 123 73
20 223 136 102 71 122 64
25 180 149 84 71 96 69 12 12
27 234 133 125 69 108 64 10 8
3/4/69 196 142 87 69 109 73 10 11
Feed: 2 Parts Bearnhouse Waste: 1 Part Spent Tan Liquors:
0.9 L Sewage: Det. Time - 20 Days
3/6/69 232 135 116 65 116 70 9 6
9 208 120 101 68 108 52 8 6
10 225 129 113 60 113 69
11 241 136 113 64 129 71
12 236 126 107 60 130 66 12 7
13 217 137 104 69 113 69
14 150 130 41 67 109 63 9 6
15 165 147 51 67 110 80
16 180 105 63 58 117 47
17 197 137 96 59 101 78 7 7
18 137 133 63 58 73 75
19 154 125 56 57 98 68 10 6
20 150 125 36 55 113 70
21 147 110 38 52 109 58 15 8
110
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Table A-4: Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date TKN Ammonia Organic Total
Nitrogen Nitrogen Sulf ides
Inf. Eff. Inf. Eff. Inf. Eff. Inf. Eff.
Feed: 2 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
0.9 L Sewage: Det. Time - 20 Days
3/22/69 177 111 38 50 139 60
23 101 132 52 49 49 63
24 142 115 27 49 115 66 10 6
25 238 87 97 43 142 43
26 258 118 130 43 127 76 9 7
27 252 101 129 43 123 58
28 257 106 134 46 122 60 9 6
29 145 138 48 48 97 90
30 195 123 96 49 99 74
31 223 138 89 48 134 90 10 6
4/1/69 194 105 109 47 85 58
2 105 118 49 49 56 69 12 10
3 225 118 99 50 126 68
4 245 115 117 52 128 63 12 12
5 242 155 114 54 128 101
7 252 117 114 53 138 64 9 8
8 151 123 31 55 120 68
9 281 121 138 53 143 68 11 8
10 320 125 141 53 179 72
11 274 123 140 53 134 70 8 8
12 308 123 171 55 137 68
13 245 125 109 55 136 70
14 309 124 147 55 162 69 13 8
Feed: 2 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
Det. Time - 20 Days
15 254 128 118 56 136 72
16 252 130 131 57 121 73 12 10
17 331 133 170 58 161 75
18 288 141 150 60 138 81 14 12
19 261 145 137 62 124 83
20 269 135 139 63 130 72
21 283 137 144 64 139 73 8 10
111
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Table A4: Performance Characteristics of
Anaerobic-Aerobic Pilot Unit
Date TKN Ammonia Organic Total
Nitrogen Nitrogen Suif ides
Inf. Eff. Inf. Eff. Inf. Eff. Inf. Eff.
Feed: 2 Parts Beamhouse Waste: 1 Part Spent Tan Liquors:
Det. Time - 20 Days
4/22/69 271 137 139 64 132 73
23 262 144 122 64 140 80 15 10
24 238 152 104 62 134 90
25 267 155 138 61 129 94 12 9
26 307 150 165 62 142 88
27 84 136 47 65 37 71
28 65 201 27 95 38 106 10 11
29 243 168 132 62 111 106
30 269 147 144 61 125 86 10 7
5/1/69 312 181 139 57 173 124
2 195 178 86 60 109 118 13 7
3 178 172 71 59 107 113
4 240 163 84 59 156 104
5 196 146 59 59 137 87 12 10
6 203 150 81 59 122 91
7 196 138 79 57 117 81 12 11
8 245 136 134 53 111 83
9 220 125 111 49 109 76 12 11
10 229 116 115 48 114 68
11 170 116 62 48 108 68
12 214 131 93 48 121 83 14 6
13 217 122 102 53 115 69
14 209 114 106 54 103 60 7 9
15 224 160 118 58 106 72
16 247 132 133 57 114 75 8 7
17 255 142 145 61 110 81
112
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1 I Acce ion Number I 2 I Subject re id & Group
SELECTED WATER RESOURCES ABSTRACTS
05D INPUT TRANSACTION FORM
5 Organ i7atzon
University of Cincinnati
Cincinnati, Ohio
T r ite
Treatment of Sole Leather Vegetable Tannery Wastes
J_9J Author(s)
Dr. J. David Eye
Project Designation
FWQA Grant WPDl85
Note
Problem #12120--
Citation
.32J Descriptors (Starred P irsi)
Tannery Industrial Wastes
Pilot Plants Clarification
Prototype Plants AnaerobicAerobic Lagoons
Waste Treatment
25 Identifiers (Started First)
.2zi Abstract Four major studies, two pilot scale and two full scale, were carried out
during the period of this investigation. The basic objective of the studies was
to find a technically feasible and economical procedure for treating the wastes from
a sole leather vegetable tannery. A detailed identification of the sources of all
wastes as well as a comprehensive characterization of each waste fraction was made
for the International Shoe Company Tannery located at Marlinton, West Virflnaa. It
was found that a large percentage of the pollutants initially were contained in a
relatively small fraction of the total waste volume. The treatment scheme consisted
of separation and pretreatment of the individual waste streams followed by mixing all
waste streams I or additional treatment in an anaercbicaerobic lagoon system. The
lime bearing wastes from the beamhouse were screened, treated with polyelectrolytes,
and then clarified, The lime sludge was used for landfill. The system was designed
to treat one million gallcns of waste per week. W)D was reduced 8595 percent and the
suspended solids reduction was in excess of 95 percent. Installed cost of the total
system was approximately $40,000 and it is estimated that the operating cost will be
about $15,000 per year or 7 cents per hide processed.
SEND TO WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U S DEPARTMENT OF THE INTERIOR
WASHINGTON 0 C 20240
GPO 196 53 59.330
CR 102 (REv JU L Y lOSS )
CR SI C
Abstraclor Instltut aon
Dr. J. David Eye University of Cincinnati
* I t S GOVERNMENT FS tThG orrrcc [ 971 0 413.720
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