WATER POLLUTION CONTROL RESEARCH SERIES • 12120 DlK 12/70
Anaerobic-Aerobic Lagoon
Treatment
for Vegetable Tanning Wastes
ENVIRONMENTAL PROTECTION AGENCY • WATER QUALITY OFFICE
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WATER POLLUTION CONTROL RESEARCH SERIES
The Water Pollution Control Research Reports describe the results
and progress in the control and abatement of pollution of our
Nation's waters. They provide a central source of information
on the research, development and demonstration activities of
the Water Quality Office of the Environmental Protection Agency,
through in-house research and grants and contracts with the
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Inquiries pertaining to Water Pollution Control Research Reports
should be directed to the Head, Project Reports System, Planning
and Resources Office, Research and Development, Water Quality
Office, Environmental Protection Agency, Washington, B.C. 20242.
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ANAEROBIC-AEROBIC LAGOON TREATMENT FOR
VEGETABLE TANNING WASTES
by
Cl inton E. Parker
Assistant Professor
Department of Civil Engineering
Research Laboratories for the
Engineering Sciences
University of Virginia
CharlottesviIle, Virginia 22901
for the
FEDERAL WATER QUALITY ADMINISTRATION
ENVIRONMENTAL PROTECTION AGENCY
Program #12120 DIK
Grant #WPD-I99-01-67
December 1970
For sale by the Superintendent of Documents, U.S. Government Printing Offlce, Washington, D.C. 20402 - Price $1.00
Stock Number 5501-0086
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EPA Reviev Notice
This report has been reviewed by the Water Quality
Office, EPA, and approved for publication. Approval
does not signify that the contents necessarily
reflect the views and policies of the Environmental
Protection Agency, nor does mention of trade names
or commercial products constitute endorsement or
recommendation for use.
ii
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ABSTRACT
A field demonstration lagoon was operated at Virginia Oak Tannery, Inc.,
Luray, Virginia to evaluate the effectiveness of an anaerobic-aerobic
lagoon in treating spent vegetable tannins blended with batepool and
soak waste waters. The enaerobic-aerobFc lagoon system was used to
treat combined waste streams with a BODs concentration of approximately
1000 mg/fc. Aeration and volume of the lagoon were fixed and flow to
the system was varied. The system load varied by increasing the flow
so as to observe five operational phases. Operational phases were
designed to cause the system to go from aerobic conditions to anaerobic-
aerobic. After reaching anaerobic-aerobic conditions, doubling the BOD5
load did not result in a significant decrease in BOD5 removal efficiency.
Efficiency, measured in terms of soluble BODg, at a BOD5 load of 17.3
Ibs/IOOO ft3/day (anaerobic-aerobic condition) was 81 percent compared
to a 92 percent efficiency for a BOD5 load of 4.5 lbs/!000 ftVday
(aerobic conditions). The final load on the system under anaerobic-
aerobic conditions was 1.73 Ibs. of BOD5/IOOO ft3/day/B.hp. During
this loading condition soluble BODs and soluble COD removal efficiencies
of 81 and 58 percent, respectively, were observed.
Although the lagoon system proved successful in removing degradable
organics, co or of the waste water was not reduced by this method of
treatment. Color of spent vegetable tannins is a major problem and will
dictate the most desirable approach to treating this waste water.
A completely mixed aeration unit was used in the laboratory to study the
biological degradation of spent vegetable tannins. Concentrated and
diluted tannins were studied by varying the detention time Tn the
aeration unit. It was found that approximately 60 percent of the COD
of spent vegetable tannins is not biological degradable and the generally
accepted substrate-growth interaction relationship required modification
to take into account the non-degradable fraction of COD. Yield coeffi-
cients, endogenous respiration rate, and specific growth were computed
from the results of the laboratory study.
This report was submitted in fulfillment of Grant No. WPD-I99-OI-67
under the partial sponsorship of the Federal Water Quality Administration.
Key Words: Spent tannins, tannery waste waters, anaerobic-aerobic lagoon,
biological treatment, biological growth units.
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CONTENTS
Section
I CONCLUSIONS I
II RECOMMENDATIONS 3
III INTRODUCTI ON 5
IV TANNERY WASTE WATERS 7
General 7
Tanning and Bating Processes 7
V LAGOON FLOW SYSTEM I I
VI PROCEDURES AND ANALYSES 13
VII LAGOON OPERATIONAL RESULTS 15
General 15
Influent Characteristics 16
Effluent Characteristics 21
VIM DISCUSSION 39
Field Demonstration Lagoon 39
Co I or RemovaI ProbI em 43
IX BACTERIAL GROWTH USING SPENT VEGETABLE TANNINS 45
Genera I 45
Kinetics of Bacterial Cultures: A Brief Review 45
Mathematical Model 46
Spent Vegetable Tannin Analyses 47
Descriptive Parameters 47
Discussion of Results 51
X ACKNOWLEDGMENTS 59
XI REFERENCES 61
XII PUBLICATIONS AND PATENTS 63
XIII NOTATIONS 65
XIV APPENDIX 69
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FIGURES
Number Title Pa
I Schmatic of Vegetable Tanning Process 8
2 Site Plan 12
3 Schematic of Laboratory Apparatus for
Measuring Oxygen Transfer 17
4 Oxygen Transfer: Lagoon Influent 18
5 I. Ultimate BOD: Lagoon Influent 19
6 II. Ultimate BOD: Lagoon Influent 20
7 Average Weekly Flow 22
8 Typical Influent pH 25
9 Effluent BOD5 and COD: Phase I 28
10 Effluent BOD5 and COD: Phase II 29
II Effluent BOD5 and COD: Phase III 30
12 Effluent BOD5 and COD: Phase IV 31
13 Effluent BOD5 and COD: Phase V 32
14 Typical Effluent pH ' 34
15 Lagoon BODs and COD Removal 41
16 Ultimate BOD for Concentrated Tannins 49
17 Flow Diagram for Completely Mixed Continuous Flow
System 50
18 Typical Progressive BODsRemoval and Suspended
Solids Production 52
19 Typical Progressive COD Removal 53
20 Yield and Organism Decay Rate for Diluted Tannins 55
21 Yield and Organism Decay Rate for Concentrated
Tannins 55
vi
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FIGURES (Continued)
Number Title Pages
22 Growth Rate: Michaelis-Menten Enzyme-Substrate
Interaction 56
23 Growth Rate: Relationship Suggested by Hetling
and Washington 56
vi ii
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TABLES
Number Title Page
I Summary Data for Blended Batepool, Tannins
(with Bleach Water) and Soak Water Influent 23
2 Summary Data for Blended Batepool and Tannin
Influent 24
3 Lagoon Influent and Effluent Color 26
4 Effluent Summary Data: Phase I-V 27
5 Effluent Dissolved Oxygen 35
6 Lagoon Dissolved Oxygen Profiles 36
7 Sludge Deposits 37
8 Average Monthly Lagoon Influent and Effluent
Temperatures 38
9 Comparison Summary of Operational Phases 40
10 Spent Vegetable Tannin Analyses 48
II COD and Suspended Solid Changes for Diluted Tannins 54
12 COD and Suspended Solid Changes for Concentrated
Tannins 54
ix
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SECTION I
CONCLUSIONS
I. Spent vegetable tannins and spent vegetable tannins blended with
soak and hairwasher waste water, and batepool waste water are biolog-
ical ly degradable. However, only about 40 percent of the COD of spent
vegetable tannins can be removed by biological treatment. Biological
treatment of waste water that contains spent vegetable tannins will not
reduce color of the waste water.
2. A deep lagoon operated under anaerobic-aerobic conditions can be used
to treat spent vegetable tannins that have been blended with batepool
waste water. An anaerobic-aerobic lagoon 15 feet deep, aerated at the
surface with mechanical aerators, can receive batepool waste water and
spent vegetable tannins in a ratio of 8:1 and provide soluble B005
removal of 81 percent and soluble COD removal of 58 percent when the
load on the system is 1.73 Ibs of BOD5/1000 ft3/day/B.hp and 7.00 Ibs
of COD/1000 ft3/day/B.hp. No appreciable solid build up will occur in
the lagoon system.
3. The most difficult problem that must be dealt with by a tannery in
treating spent vegetable tannins is color removal; therefore, the most
desirable method of treating spent vegetable tannins will depend upon
the approach to color removal.
4. Spent vegetable tannins diluted to approximately 1000 mg/£ of COD
and fed into an aerobic system will result in an organism decay rate
between 0.041 and 0.045 hours"1, and yield coefficients of
0.62 m9 S and 0.78 m9 S. An organism decay rate of 0.061 hours-1
mg LUU mg LOU .. _~ '
and a yield coefficient of 0.91 m9 oor, will result when concentrated
mg LOU
vegetable tannins with COD concentrations between 11,860 mg/£ and
32,800 mg/SL are used as feed.
5. The Michae I is-Menten expression for substrate (or nutrient)-enzyme
interaction will not describe dilute spent vegetable tannins when
substrate is measured in terms of COD. The equation
si ~ A
u = y •= — 7—5- provides an adequate relationship between COD and growth
for diluted spent vegetable tannins. For tannins diluted to 1000 mg/£
of COD and fed into an aerobic system, p = 0.21 hours"1, A = 590 mg/£
of COD and B = -491 mg/A of COD.
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SECTION I I
RECOMMENDATIONS
Design of systems to treat spent vegetable tannins should be based on
pilot studies of the waste at each tannery under consideration. These
studies will be required to insure the adequacy of the system in meeting
the needs of the particular tannery and water quality standards. The
importance of color removal should be recognized in the design of both
pilot and prototype. The approach to color removal will greatly
influence design of the treatment process and operation of the constructed
faclIity.
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SECTION I I I
INTRODUCTION
The tannery industry recognized the need for sound technological develop-
ments in tannery waste treatment and in 1965 the Tanners' CounciI of
America retained Dr. J. David Eye of the University of Cincinnati, a
waste management consultant, to make a detailed field investigation of
the tanning industry. Dr. Eye found that no tannery had a treatment
procedure that was entirely satisfactory. Indications were that the
design engineers lacked sufficient knowledge of the waste characteristics
and its treatability to properly design effective treatment units.
Apparently, the effect of tannery waste was not understood and conventional
treatment methods had failed to provide adequate treatment. As a result,
suitable treatment methods had not been employed and progress in this
area lagged.
During the summer of 1966 a waste water study was made at Virginia Oak
Tannery, Incorporated, Luray, Virginia. This project was sponsored by
Virginia Oak Tannery, Incorporated, and was under the direction of Dr.
Clinton E. Parker. Data from this waste study and bench scale pilot
plant, and the results of a study at the University of Cincinnati by
Lin (I) were the basis for this investigation.
The purpose of this study was to evaluate and derive data for biological
treatment of spent vegetable tannins blended with other tannery waste
streams, except lime and unhairlng waste water. This work was to study
in the field the characteristics of an anaerobic-aerobic system in
treating these waste waters and to evaluate the effectiveness of the
system in meeting the need of a low cost treatment system capable of
producing an effluent that meets pollution abatement standards.
Tanning is the process of converting the fibers of the hide to leather.
Vegetable tannin is the aqueous extract of certain forms of plant life
such as barks, woods, leaves, twigs, fruit pods and roots. Spent vegetable
tannins are highly colored and account for 5 to 10 percent of the total
waste flow and 25 to 30 percent of the total BOD5 from the tanning
processes.
Soak waste waters result from the process of removing salt used to pack
the hides during storage and shipment. This process also removes dirt,
blood, manure, and non-fibrous proteins. The soak waste water is high
In solids and Is 10 to 15 percent of the total tannery waste water
discharge and 15 to 20 percent of the BOD5.
Bating Is the term which applies to the process of preparing the hide
for tanning after hair removal. The bate solution Is usually made up
of ammonia salts and a mixture of commercially prepared enzymes. This
solution Is used in basins which are referred to as batepools. Batepool
waste water Is usually about 40 percent of the total tannery waste water
flow and 15 percent of the BOD5.
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Initially spent tannins (with bleach waste water) were blended with
batepool and soak waste water and fed into the field lagoon. This was
followed by observations of spent tannins blended with batepool waste
water and fed into a lagoon system constructed at Virginia Oak Tannery,
Inc., Luray, Virginia. Aeration was held constant and total flow was
varied between 15 gpm and 127 gpm. Analyses were made of the influent
and effluent waste waters.
A laboratory aeration unit was used to study biological treatment of
spent vegetable tannins. Studies were carried out using concentrated
and diluted tannins. Results from these studies were used to describe
organism growth parameters when the only substrate available was the
spent tannins.
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SECTION IV
TANNERY WASTE WATERS
General
Tanning is as much of an "art" as a science. For a complete understanding
of the composition and chemistry of tanning waste one must learn why the
tanner uses the processes he does, the role of the chemicals used and
the waste contribution that can be attributed to hide substance. Basic
flow diagrams of tanneries using the same method of tanning are similar,
but unit processes and unit operations vary and reflect the experience
of the particular tannery.
The conversion of animal hides, primarily cattle, into leather is generally
comprised to ten separate physiochemica I or biological processes [21], [33.
The tanning step is the actual conversion of the fibers in the hide to
leather. In present practice two primary methods of tanning are vegetable
tanning and chrome tanning. For vegetable tanning an aqueous extraction
from certain forms of plant life is used as the tan solution. The hides
are immersed in a weak extract and move through an increase in concen-
tration, ranging from 0.3 to 6.0 percent tanning extract. Preliminary
tanning is in rocker vats and takes about three weeks. This is followed
by tanning in layer vats with a 6.0 percent tanning extract for another
3 weeks. Although tan solution is reused as much as the "art" will
allow and is small in volume, the spent vegetable tannins are quite
strong.
Tanning and Bating Processes
Virginia Oak Tannery, Inc. (VOTAN) processes cattle hides and employs
both vegetable tanning and chrome tanning, however, between 70 and 80
percent of its production is by vegetable tanning. Although there is
some variation, the processes employed at VOTAN are similar to those
of other tanneries. The animal skins are received "cured" (packed in
salt with a reduced moisture content). Tanning is accomplished by
separate batch physiochemical or biological processes that are adequately
described by others [23, [33. The flow diagram in Figure I indicates
the steps in the vegetable tanning process.
During this study VOTAN processed branded and native steer hides with an
average green prefleshed weight of 54 pounds each. The average hides
processed were I 100 per day with 75 percent of the hide being vegetable
tanned (excludes bellies). Vegetable tanned leather yield was 87
percent of the green prefleshed weight. The finished product contained
35 percent tannin extract on a dry weight basis or 32 percent tannin
extract on a moist basis. Vegetable tanned leather yield was 38,800
pounds per day, equivalent of 825 hides/day. Dry tannins were dissolved
and blended on the premises and no leaching or evaporation was employed.
The tannin extract blend was 55 percent quebracho, 20 percent wattle,
15 percent chestnut and 10 percent myrtan. The extract contained 67.2
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Received at Tannery
Green Pre-Fleshed
Packed in Salt
Tannin
Vats & Drums
I
Wash
Bleach
Wri nger
Wash Dry
Rol t
And Finish
Chrome Re-Tan
(If Desired)
FIGURE I SCHEMATIC OF VEGETABLE TANNING PROCESS
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percent tannins and the tannery used 118,511 pounds of the extract
blend per week. The source of tannin waste water was the tannin yard,
rinse liquor from sole leather and speciality leathers. All I 100
hides per day were soaked and washed, limed, and bated and delimed.
Oropan XXS2 (product of Rohm Haas Co.) was used in the bating operation.
Thirty-five hundred pounds of Oropan was used per week. Batepool waste
water consisted of water from the bating and deliming process.
Total flow from the tannery during this study was 640,000 gpd of which
260,000 gpd was batepool waste water and 32,000 gpd was concentrated
spent vegetable tannins.
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SECTION V
LAGOON AND FLOW SYSTEM
Figure 2 shows the actual constructed site plan of the lagoon system
and the positioning of the aerators. Water surface dimensions were
136 feet by 68 feet and the average depth was 14.5 feet. The inside
bank slope was 2 to I for the first four feet and then I to I to the
lagoon bottom. Water volume of the lagoon was 770,000 gallons. The
influent pipe extended 32 feet into the lagoon and was positioned
6.0 feet from the lagoon bottom. Construction of the facilities and
installation of pumps, pipes, tanks, and aeration equipment was
completed in April 1968. The aeration equipment consists of two
5-horsepower aerators (model FLTM-5), Welles Products Corporation).
The oxygen transfer rate given by the manufacturer was 3.2 Ibs of
02 per nameplate horseplate per hour at standard conditions (water
with zero dissolved solids, 20°C and at one atmosphere). An anti-
erosion assembly was used on the aerator nearest the effluent but was
not placed on the aerator nearest the influent. Advantage was taken
of the aerator draft depth at the influent by positioning the aerator
over the end of the influent pipe to immediately mix fresh waste
entering the lagoon. Positioning the aerator directly over the influent
was an attempt to minimize any shock load that may have occurred.
Flow to the lagoon system was proportioned to correspond with actual
24-hour plant waste water flow. (In-plant changes from time to time
caused some variation in both waste water characteristics and flows).
Initially the flow scheme was as shown in Figure 2, however, after
starting up and experiencing some difficulty with pump clogging the
soak hair and bleach water were diverted to another system. Since
flow from the plant required pumping, flow measurements were made at
the effluent with a V-notch weir and a Stevens recorder. Evaporation
and seepage losses from the lagoon were estimated by observing
lagoon water surface elevation change with zero influent. These losses
were obsecured by the accuracy of the flow measurements, estimated to
be ± 10 percent. In addition to flow from the lagoon system, flow
measurements were made of the spent tannins, batepool and total plant
waste water discharge.
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TANNING(I)
WASTE WATER-
(W/BLEACH WATER)"
•EQUALIZING BASIN
-WATER SURFACE DIMENSIONS 136* K 68*
AVERAGE DEPTH 14.5 FT.
(BATING
WASTE WATER
[MIXING BASIN
INFLUENT
-SOAKllJ
WASTE WATER
*• 32' -4*-
64'
40'
EFFLUENT
EQUALIZING
BASIN
water and soak waste water were
diverted to another facility after
experiencing pump difficulties.
AERATOR WITHOUT ANTIEROSION ASSEMBLY
AERATOR WITH ANTIEROSION ASSEMBLY
FIGURE 2 SITE PLAN
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SECTION VI
PROCEDURES AND ANALYSES
The following laboratory analyses were made on the waste waters (see
Section XII! for notations):
Biochemical Oxygen Demand Suspended Solids
Chemical Oxygen Demand Fixed Suspended Solids
Organic Nitrogen Volatile Suspended Solids
Ammonia Nitrogen Settleable Solids
Total Kjeldahl Nitrogen Hydrogen ion Concentration
Total Sot ids Total SuI fides
Total Fixed Solids Total Phosphorus
Total Volatile Sol ids Color
All laboratory analyses were made In accordance with Standard Methods
for the Exam?nation of Water and Waste Water M with the exception of
total phosphorus. Total phosphorus was determined in accordance with
a wet oxidation procedure in Official Methods of Analysis of the
Association of Official Agricultural CherrIsts [5J and the method of
Paris 'and Guthrie [6]. Phosphorus recovery by this method was 99 percent.
The modified method for determining total phosphorus is presented in
the Appendix. All BOD determinations (except effluent) were made with
dilution water seeded with iagoon effluent. Both ultimate BOD and BOD5
were made at 20°C.
In addition to laboratory analyses, field analyses of dissolved oxygen
(DO), pH, and temperature were made. A model 54 RC YSI DO meter was
used for field oxygen measurements and model 30 pH recorder (Analytical
Measurements, Inc.) was used for continuous pH measurement.
13
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SECTION VI I
LAGOON OPERATIONAL RESULTS
Genera I
The lagoon system became operative in April 1968 and flow to the system
was increased systematically during the period of study from 15 April
1968 through 18 September 1969. Operation of the system was divided
into five phases which were designed to go from an aerobic condition
to an anaerobic condition. The following dates delinate the operative
phases:
I. 15 April 1968 - 15 August 1968 — During this period the
lagoon was filled and allowed to reach a steady-state condition.
The influent consisted of batepool, soak waste water and tannins
(with bleach waste water) proportioned at a ratio of 6 to 2 to I,
respectively. Operations diminished beginning the last week
of June and returned to normal the first week in July because
of a vacation period observed by the tannery. This resulted
in 10 days of zero flow. The flow rate into the lagoon during
this phase was 15 gpm.
I 1. 15 August 1968 - II December 1968 ~ An attempt was made
to increase the flow to the system, however, the pumping
system required modification before this could be accomplished.
Therefore, since it was desireable to extend the data at low
flow to include filtered effluent samples, a low flow of 20
gpm was observed. This period provided additional data on
soluble and insoluble effluent fractions at an extremely low
flow. The waste streams and flow ratios remained the same as
in the above operational phase.
III. II December 1968 - 19 March 1969 — Flow to the lagoon
system was increased to an average flow of 33 gpm. Because
of problems with freezing, hair clopping pumps, and in-plant
changes, after 8 January 1969 soak and bleach waste waters
were not pumped into the system. From 8 January 1969 to the
end of the study only batepool and tannin waste waters were
proportioned during the 5-day work week at a batepool to
tannins ratio of 8:1 and pumped into the lagoon. In addition,
batepool waste water was a I lowed to enter the lagoon on a
7-day basis. Examination of the weekend batepool flow revealed
that it was essentially potable water and did not contribute
to the waste load. This weekend flow was necessary to prevent
pipes and pumps from freezing.
IV. 19 March 1969 - 26 June 1969 — Flow to tha lagoon averaged
69 gpm and consisted of a batepool to tannins ratio of 8:1.
Beginning the end of April and through part of May in-plant
15
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changes were made which required frequent diversion of the
tannins. From the end of May through 26 June the flows
were norma I.
V. 26 June 1969 - 18 September 1969 — Average flow into
the lagoon was 127 gpm. The last week in June and the first
week in July were affected by the tannery closing for vacation.
During this operational phase the flows remained in the same
proportion as the previous phase (batepool to tannins of 8:1).
Influent Characteristics
In addition to routine analyses, uItimate BOD and oxygen transfer measure-
ments were made in the laboratory. Figure 3 shows the arrangement used
to measure oxygen transfer to water and waste water. The DO probe
position, stirrer speed, aeration vessel size, aeration bubble size
and air flow rate were the same for all measurements. Data from these
analyses are given in Table A-I of the Appendix and results from the
plot of
C - C
log 'r-TTr' = -\f
s o
are shown in Figure 4. The data indicate an alpha value of 0.72 for
the influent waste water which consisted of a batepool to tannins ratio
of 8:1. It should be noted that these data were obtained by a comparison
of the waste water with distilled water. Dissolved oxygen of distilled
water was depleted by using enough sodium sulfite catalyzed with cobalt
to lower the dissolved oxygen. Since the dissolved oxygen of the waste
water was low enough to measure oxygen transfer, sodium sulfite and
cobalt were not added to the waste water to reduce the dissolved oxygen.
Long term BOD data was obtained on different samples at 20°C. Figure 5
and Figure 6 show the results of both observed and theoretical values
for different samples with different ultimate BODs. These data indicate
a velocity constant (log to the base 10) of 0.22 day"1. Calculated BOD
values shown on the figures were obtained by using the indicated first
stage ultimate BOD values and the first stage velocity constant. Data
from which these figures were obtained are included in Table A-2 of the
Appendix.
During the first phase of operation flow recording equipment was not
available, therefore measurements were made periodically to determine
the flow. At low flow problems were frequently encountered with pumping
because of hair, therefore, the low flow of 15 gallons per minute is
a best estimate during this period.
Influent flow arrangements were such that it was impossible to obtain
an accurate influent flow rate, hence effluent flows were measured
throughout the study. To obtain an accurate estimate of influent flow
the evaporation and seepage rates were measured. This was accomplished
by shutting off flow to the lagoon, measuring the effluent flow, and
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Thermometer
Compressed
Air ^,-
Reaction Vessel
Magnetic Stirrer
Diffuser
Air Flow Meter
FIGURE 3 SCHEMATIC OF LABORATORY APPARATUS FOR MEASURING
OXYGEN TRANSFER
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c -c
c -c
s o
1.0
0.9
0.8
0.7
0.6
0.5
0.4
0.3
0.2
0. I
• OBS. PT.
a 3 common OBS.PT.
O 2 common OBS.PT
C^ 6.0 ng/£
K = 0.153 min.'
K = 0. I 18 min.'
For: T = 26°C
X OBS.PT.
C = 6.6 mg/£
K|, = 0.136 min
26
K = 0.I 18 min
K0, = 0.190 min
2o
K = 0.165 min"
.0
2.0
3.0
4.0
5.0
Time, Minutes
FIGURE 4 OXYGEN TRANSFER; LAGOON INFLUENT
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2500
T 1 1 1 1 1 1 1 1 T
2000
1500
1000
500
—1 1 1 1 1"
• CBS. L0 = 2020
KOBS. L == 1350
o
ACalc. K = 0.22 (Base 10)
1 T
2nd Stage
Temp. = 20°C
' ' ' I L
I I I L
I I I
J L
0 2.0 4.0 6.0 8.0
10.0 12.0
Time, Days
FIGURES I. ULTIMATE BOD: LAGOON INFLUENT
14.0 16.0 18.0 20.0
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2500
O)
Q
a
2000 _
1500 -
1000
500 -
6.0 8.0 10.0 12.0
Time, Davs
14.0 16.1
FIGURES II. ULTIMATE BOD: LAGOON INFLUENT
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recording the change in lagoon surface elevation. From these measurements
a water balance was struck. The losses were not detectable with the flow
recorder, therefore, the effluent flow was a reasonable measurement of
the influent flow.
Results of flow measurements during the periods in which accurate
measurements were made is shown in Figure 7. These data show weekly
average flows and the average flow for the individual phases III, IV
and V. The change from a five day flow arrangement to a seven day flow
arrangement is noted. It should be understood that the switch to flow
during the weekends resulted in an essentially clear water flowing into
the lagoon for two days - i.e., BOD5 during weekends was 3 mg/fc. The
weekly average flow values are also given in Table A-3 of the Appendix.
During the period of study the influent flow consisted of two different
combinations of in-plant waste stream flows. The first combination of
batepool, soak, and tanning (with bleach water) waste waters is presented
in Table A-4 of the Appendix and summarized in Table I. Table 2 Is a
summary of the influent data presented in Table A-5 of the Appendix.
This last set of data is for the lagoon influent when it consisted of
batepool and tanning. It should be noted that the most significant
difference between these two flow arrangements was the solids content.
Since the tanning process is a batch process pH can be expected to vary
during the day. Figure 8 i lustrates the variation in the influent pH
that was observed.
Color in the waste took on an orange-red hue as is indicated in Table 3.
Although these data were collected in accordance with Standard Methods
[4H, they do not indicate the severity of the color problem. Color of
the waste water on the platinum-cobalt scale was estimated by diluting
with distilled water. This method of measurement indicated that the
color was about 5000 units.
Effluent Characteristics
Results from lagoon effluent analyses are presented in a form compatible
with the five phases previously described. These data are presented in
Table A-6, Table A-7, Table A-8, Table A-9, and Table A-IO of the
Appendix. Table 4 summarizes the average effluent data for the five
operational phases. The BODs and COD for each phase are shown graphically.
Figure 9 is a plot of the BOD5 and COD values for the first phase, showing
the progression to steady-state. This figure shows the change in total
BOD5 and total COD through August 15, 1968. Total BOD5 and total COD,
and soluble BOD5 and soluble COD for the other four phases are shown
separately. Results from flows of 20 gpm, 33 gpm, 69 gpm, and 127 gpm
are shown in Figure 10, Figure II, Figure 12, and Figure 13, respectively.
It should be noted that Figure 12 reflects in-plants changes that resulted
in the diversion of tannings from the end of April through part of May.
In addition, the variation of the effluent in August shown in Figure 13
should be noted. The reason for this variation is uncertain, but it is
believed to have resulted from in-plant changes also.
21
-------
150
125
100
75
50
25
J T
Ave. Weekly Flow
Ave. Flow
With soak and Bleach;
5 - Day Flows
127 gpm
-^•Without soak water
7 - Day Flows
69 gpm
33 gpm
I
I
10 15
15 Dec. 68
20 25 30 35
Weeks in Operation
FIGURE 7 AVERAGE WEEKLY FLOW
40
45 51
20 Sept. 69
-------
TABLE I SUMMARY DATA FOR BLENDED BATEPOOL, TANNINS (WITH
BLEACH WATER) AND SOAK WATER INFLUENT(')>(2)
Ana 1 ys ! s
BOD 5
COD
ORG-N
NH3-N
TKN
TS
TFS
TVS
SS
FSS
VSS
Set. S
pH
T. Suit.
TP
Maximum
1850
6616
48.3
66.3
102.4
15,845
13,675
4427
975
182
975
122
8.6
1.8
8.37
Minimum
725
1937
23.3
23.8
62.6
5051
3435
1143
350
0
350
O.I
3.2
1.0
4.46
Average
1043
4470
40.6
47.1
87.8
9190
6500
2710
539
48
582
15.1
6.0
1.5
6.83
(lResults In mg/A except pH and SS. SS In ml/I
(2)
Based on composite samples with the exception of total suit ides.
Total suit Ides based on grab samples.
23
-------
TABLE 2 SUMMARY DATA FOR BLENDED BATEPOOL AND TANNIN INFLUENT('}'(2>
Analysis
BOD5
COD
ORG-N
NH3-N
TKN
TS
TFS
TVS
Set. S
pH
T.Sulf
TP
Maximum
2050
7340
109.4
99.6
209.0
7579
3410
4169
> 40
9.6
1.2
8.80
Mint mum
725
2349
26.8
33.1
63.0
2556
660
1384
0.5
5.8
0.4
5.61
Average
1170
4730
47.2
59.3
106.5
4392
1850
2542
-
6.8
0.7
7.33
(lResults In mg/Z except pH and SS. SS in mi/i
(2)
Based on composite samples with the exception of total suI fides.
Total suI fides based on grab samples
24
-------
'
-
2.0 --.-rr
7.0-
I2'°oooo
/
r-"-
:'- ---
1200
2.0
'-" - ' v=f— . - . . • -rf^^l— i -
pH ZO-K
.
- ' -^
. .
-*•
* ---- --r==
I4OO
iSOO J8OO 2COO
1600
HOUR
(24-HR. pH, APRIL £4, !968)
220C
24OO
FIGURE 8 TYPICAL INFLUENT pH
-------
TABLE 3 LAGOON INFLUENT AND EFFLUENT COLOR(I)(2)
(pH Adjusted to 7.6)
Inf luent:
dominant wavelength, mu
hue(3)
luminance, %
purity,?
Effluent:
dominant wavelength, mu
hue
luminance, %
purity, %
8/13/68
592
0
25
74
586
Y-0
30
71
8/20/68
583
Y-0
48
55
583
Y-0
48
55
DATE
3/5/69
590
0
26
68
594
0
13
92
3/20/69
588
0
26
70
604
0-R
15
96
6/17/69
590
0
26
76
598
0-R
10
96
Using dilutions, all results compare with about 5000 platinum-cobalt units.
(2)Spectronic 20; 10 ordinates; and spectral band width 20 mu.
3)0 = orange; Y-0 = yellow-orange; R = red and 0-R = orange-red.
26
-------
TABLE 4 EFFLUENT SUMMARY DATA: PHASE I-V
(I)(2)
Ana lys is
BOD 5
F-BODS
COD
F-COD
ORG-N
F-ORG-N
NH3-N
F-NN3-N
TKN
F-TKN
TS
TFS
TVS
SS
FSS
VSS
Set. S.
pH
T. Sulf.
TP
Q=I5 gpm
25
-
1083
-
17.5
-
36.2
-
43.7
-
6130
5270
850
495
1 17
378
25
7.1
0.0
2.36
0=20 gpm
45
17
1549
462
31.6
6.2
29.0
27.7
60.6
33.9
7380
6300
1080
890
250
747
32
6.9
0.0
7.67
AVERAGE
0=33 gpm
132
64
I960
1362
27.7
6.7
24.8
23.7
52.5
30.4
2330
1383
947
435
150
283
2
7.4
0.0
5.6
0=69 gpm
274
145
2113
1328
16.7
5.5
17.8
16.8
34.5
223
2532
992
1540
503
100
402
1
7.1
0.0
5.8
0=127 gpm
313
159
2114
,431
23.9
11.3
41.5
35.2
65.4
46.5
2255
1038
1217
459
98
362
2
6.9
0.3
3.6
(2)
Results in mg/Jl except pH and SS. SS in mi/i.
Only for data after steady state
27
-------
400
r 4C
300
ro
oo
o>
••
«o
200
100
30
QAVE= l59Pm
JUNE FT JULY
31 19 II
TIME, DAYS
FIGURE 9 EFFLUENT BOD5 AND COD: PHASE I
AUGUST
31
15
-------
8
50C
400
30C
200
100
r 5000
4000
3000
1
O
- 8 2000
1000
0
X BOD5
OF- BOD5
^ COD
OF- COD
0 =20 gpm
ave
.^A^-"""
A—— — ~"
x —x— x ^-^o^^^r^g *
" o- ~~° ; r—o i
September October November December
30 Time, days 31 30
FIGURE 10 EFFLUENT BOD5 AND COD: PHASE II
-------
400
4000
X BOD5
OF- 30D5
A COD
n F _ COD
0 = 33 qpm
ave
300
3000
.
20C
2000
100-
1000 -
March
FIGURE II EFFLUENT BOD5 AND COD: PHASE III
-------
400
300
100
400C
3000 -
- a 2000 -
-
1000 -
X BOD5
Op- BOD5
A COD
Dp- COD
0 =69 gpm
ave
FIGURE 12 EFFLUENT BOD5 AND COD: PHASE IV
-------
400_
4000-
300
3000-
200
O) 2000
E
100
1000-
Time, Days
FIGURE 13 EFFLUENT BOD5 AND COD:
,1. September
PHASE V
-------
Effluent pH varied very little. It was observed that the variation
between the phases was relatively small and the daily variation
insignificant. Figure 14 shows a recording of the typical effluent
pH.
Dissolved oxygen measurements were made of the lagoon effluent and in
the lagoon, and samples were taken from bottom deposits. Resulting
from effluent dissolved oxygen and dissolved oxygen in the lagoon are
presented in Table 5 and Table 6, respectively. Sludge deposit data
are presented in Table 7.
Temperature measurements were made of both the influent and effluent.
(The effluent temperatures also represent the condition found in the
lagoon.) Average monthly water temperatures for the influent and
ef-fluent are presented In Table 8. These data represent monthly averages
as obtained from daily measurements made between the hours of 7:30 a.m.
and 3:30 p.m.
33
-------
2.0
—--— —__^_
;: F s -
12.0
oooo
0200
040O
O600
HOUR
08OO
IOOO
I2OO
pH 7.0
-
- H- -
:
— ' T-H
-P
m
1
12.0
- t
V
^•i.J--v" _? ,j _j _-;" °~' __1_|_
•
'".-" _-
1200
1400
1600 1800
HOUR
(24-HR pH, AUGUST 14, 1968)
2000
2200
2400
FIGURE 14 TYPICAL EFFLUENT pH
-------
TABLE 5 EFFLUENT DISSOLVED OXYGEN
DATE
8/8/68
8/19/68
1 1 /22/68
3/5/69
6/19/69
6/25/69
7/2/69
7/28/69
8/4/69
8/15/69
8/20/69
9/10/69
9/17/69
Dissolved Oxygen
mg/Jl
3.7
3.8
9.6
3.3
0.8
1.6
0
0
2.8
0
2.2
0.8
0.5
Temperature
°C
27
27
7
7
22
25
25
25
25
27
27
22
22
Flow
gp™
15
15
20
30
68
70
11.0
130
120
1 10
130
145
165
35
-------
TABLE 6 LAGOON DISSOLVED OXYGEN PROFILES
(I)
STATION,
DATE
Sta. 1
8/ 1 9/68
11/22/68
3/5/69
6/19/69
9/ 1 7/69
Sta. 2
8/19/68
6/19/69
9/ 1 7/69
Sta. 3
8/19/68
11/22/68
3/5/69
6/69/69
9/17/69
Depth.
0
4.0
9.6
3.0
1.0
0.6
4.2
0.7
0.7
4.0
9.6
4.2
1.2
0.8
1
4.0
9.6
3.0
0.0
0.0
4.2
0.0
0.5
4.0
9.6
3.6
0.3
0.3
2
4.0
9.6
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.5
0.0
0.0
3
4.0
9.6
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.4
0.0
0.0
4
4.0
9.6
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.3
0.0
0.0
5
4.0
9.6
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.5
0.0
0.0
feet
6
4.0
9.2
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.5
0.0
0.0
7
4.0
-
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.5
0.0
0.0
8
4.0
3.0
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.5
0.0
0.0
9
4.0
-
3.0
0.0
0.0
4.2
0.0
0.0
4.0
9.6
3.5
0.0
0.0
10
3.2
-
3.0
0.0
0.0
4.3
0.0
0.0
3.6
-
3.5
0.0
0.0
II
-
-
3.0
0.0
0.0
4.4
0.0
0.0
0.0
2.2
2.5
0.0
0^0
12
0.0
0.0
0.0
0.0
4.4
0.0
0.0
0.0
0.0
2.5
0.0
0.0
(I)
Station I at influent end, station 2 at center and station 3 at effluent end.
36
-------
TABLE 7 SLUDGE DEPOSITS
(I)
Date
8/19/68
11/22/68
3/5/69
6/19/69
9/17/69
Station
1
2
3
1
3
1
3
1
2
3
1
2
3
Sludge Depth,
Feet
1.5
0.3
1.5
1.5
1.5
1.5
1.5
1.3
0.5
2.5
1.5
0.5
1.5
Volati le Sol ids,
Liquid
1 nterface
_
-
-
79.8
78.3
-
-
82.6
76.6
72.8
72.1
69.2(mixed)
58.3(mixed)
percent
Bottom
_
-
-
81.9
71.2
-
-
75.3
70.7
67.9
-
-
—
Samples taken with core type sampler.
37
-------
TABLE 8 AVERAGE MONTHLY LAGOON INFLUENT AND EFFLUENT TEMPERATURES
MONTH
January 1969
February 1969
March 1969
April 1969
May 1969
June 1969
July 1969
August 1969
September 1968 & 1969
October I 968
November 1968
December 1968
Average Temperature, °C
Influent Effluent
16
15
15
17
19
21
24
23
20
19
17
17
5
6
8
15
19
22
24
24
22
17
9
5
38
-------
SECTION VI I I
DISCUSSION
Field Demonstration Lagoon
Although the influent pH varied significantly due to the batch operations
at the tannery, the effluent remained at a pH of 7.0 ± 0.5. Dissolved
oxygen in the system varied with temperature changes and waste load.
The lagoon system was completely aerobic for operational phases one,
two, and three (except at the sludge interface at the bottom of the
lagoon). For the fourth operational phase (69 gpm) the lagoon surface
carried a dissolved oxygen content of 1.0 mg/£ and one foot below the
surface the dissolved oxygen was zero. During the fifth operational
phase only trace amounts of dissolved oxygen could be found at the
lagoon surface. The different temperatures at which the operational
phases were observed varied significantly. The average temperatures
for the operational phases (each had a duration time of at least 12
weeks) were 24, 17, 7, 18 and 24°C for phases I through V, respectively.
The alpha value for the waste water at 20°C was 0.72 and the BOD
velocity constant (base 10) was 0.22 day"1. For phases I and II the
N:BOD5, P:BOD5, N:COD and P:COD ratios were 0.084, 0.0065, 0.020, and
0.0015, respectively. During phases III through V these same parameters
were 0.091, 0.0063, 0.023, and 0.0016, respectively.
Since the aerators provided a lagoon turnover rate of once every 3
hours, the lagoon went from aerobic to what may be considered facultative
rather than anaerobic-aerobic. The lagoon system became anaerobic-
aerobic during the fourth operational phase (69 gpm) and remained
anaerobic-aerobic through the fifth operational phase (127 gpm).
Anaerobic conditions were observed in the bottom deposits which
accumulated to an average depth less than 2.0 feet during the initial
operation of the system and remained at that depth throughout the study
period.
Results from the operation of the system are compared in Table 9 and the
efficiencies are presented graphically in Figure 15. These data indicate
that while the system was anaerobic-aerobic, doubling the load did not
substantially change the lagoon characteristics, including the removal
efficiency. Results from the system while aerobic are comparable to
those observed for a laboratory completely mixed unit without recycle.
Diluted tannins (diluted to 1000 mg/£ of COD) fed a laboratory system
with detention times of 12 to 49 hours resulted in soluble BOD5 removal
efficiencies from 60 to 75 percent and soluble COD removal efficiencies
from 18 to 36 percent.
The system was sufficiently turbulent to consider the application of
E = |00 K+
I + Kt
(R = BOD5 removal rate, t = time and E = efficiency) to the data during
39
-------
TABLE 9 COMPARISON SUMMARY OF OPERATIONAL PHASES
(I)
Analysis
Inf luent:
Flow, gpd
Dot. Time (Ave), days
BOD5 load, Ibs/day
COD load, Ibs/day
BOD5 load, Ibs/IOOO ft 3/day
COD load, Ibs/IOOO ft 3/day
Effluent:
Ave. temp., °C
BOD5, Ibs/day
F-BOD5, Ibs/day
COD, Ibs/day
F-COD, Ibs/day
BOD5 red, %
F-BOD5 red, %
COD red, %
F-COD, red, %
F-BODs red, .bs/day/B.hp
F-COD, red, lbs/day/B.hp(2)
SS, Ibs/day
VSS, Ibs/day
F-BOD5 red. to SS
F-COD red. to SS
F-BOD5 red. to VSS
F-COD red. to VSS
Operational Phase
1
21,600
49.6
188
807
1.8
7.9
24
5
<'
195
-
97
99
76
-
13
-
89
68
2.10
-
2.75
-
II
28,800
37.4
251
1,072
2.4
10.4
17
II
4
371
111
96
98
65
90
18
69
213
179
1.22
4.50
1.38
5.37
III
47,500
16.2
463
1,870
4.5
18.2
7
73
36
1,086
754
84
92
42
60
31
80
242
157
1.76
4.60
2.72
7.10
IV
99,300
7.8
969
3,920
9.4
38.1
18
318
168
2,440
1,540
67
83
38
61
57
170
584
467
1.37
4.07
1.72
5.10
V
183,000
4.2
1,785
7,220
17.3
70.0
24
670
341
4,580
3,060
63
81
37
58
103
297
982
772
1.47
4.24
1.87
5.38
(I)
(2)
Total tannery flow: Batepool = 260,000 gpd and spent vegetable tannins = 32,000 gpd.
Converted to 7-day week rate; other data on 5-day work week basis except detention
time averaged through 7-day week.
40
-------
100 r
80
Q
UJ
UJ
a:
60
840
UJ
Q.
20
o BOD
AF-BOD
a COD
« F-COD
0 10 20 30
DETENTION TIME, DAYS
40
50
FIGURE 15 COD AND BOD5 REMOVAL
i
-------
aerobic conditions [7], This assumes the lagoon acted as an aerobic
stablization basjn and a first order reaction rate. Results from this
work indicate a K (corrected to 20°C) of 1.49 day1, 1.42 day-1 and
1.82 day"1 for phases I, II, and III, respectively. The fluctuation
shown in phase III was probably due to temperature averaging.
The aerobic system should have approached the concept of total oxidation,
therefore,
aL = b Sa
should be applicable [7]. In this equation a = synthesis to sludge ratio,
b = rate of auto-oxidation (fraction/day), l_r = BOD removed (Ibs/day)
and Sa = average mixed liquor suspended solids (Ibs). The data obtained
in this work are not sufficient for the calculation of a and b, however,
the ratio of a/b can be calculated from the field data. Since total
oxidation implies an oxygen requirement equivalent to the ultimate BOD,
an oxygen balance can be made for the aerobic phases. For phase III,
taken at-an average temperature of 7°C, the calculated dissolved oxygen
in the lagoon was 2.6 mg/£ compared to a measured dissolved oxygen
concentration of approximately 3.2 mg/£.
Operational characteristics of aerated aerobic lagoons, anaerobic-aerobic
lagoons and anaerobic contact processes are usually reported in terms
of BOD5 loads. It has been reported that BOD5 removal efficiencies of
80 percent or more were achieved from aerated aerobic lagoons, anaerobic-
aerobic lagoons and anaerobic contact units with BOD5 loading ranges of
I to 8, 8 to 15, and 100 to 300 Ibs/IOOO ft3/day, respectively L~8], [9],
[10], [II], [12]. Sawyer [8] has noted that loadings above 5 Ibs/IOOO
ft3/day for anaerobic-aerobic lagoons are impractical because of the
oxygen requirement. The lagoon system was loaded close to the above
ranges reported for lagoons and the removal efficiencies were within
the ranges that have been experienced; however, it appears that
considerable amounts of the waste components, measured as COD, are
not removed during biological treatment.
The anaerobic-aerobic system load may be better indicated in terms of
Ibs of BOD5/IOOO ft3/day/B.hp. Data from this work indicate loads of
0.94 and 1.73 Ibs of BOD5/IOOO ftVday/B.hp for phases IV and V,
respectively.
Although the soluble BODs removal efficiency was 80 percent or better, it
is believed, from the waste characteristics and the operation of the lagoon
system, that anaerobic-aerobic treatment in the same unit would be more
efficient if the anaerobic and aerobic zones could be distinctly separated.
Because of the toxic effects of oxygen on the anaerobic process and
mixing between the anaerobic and aerobic zones, it is difficult to
enhance both aerobic and anaerobic conditions in a lagoon. It may be
more desirable to operate an anerobic contact system with special
design considerations for providing an aerobic zone. The work of Steffen
and Bedker [10], Gates, Smith, Lin and Ris [II], and McCarty D2] offer
42
-------
interesting approaches to the anaerobic contact process and an anaerobic-
aerobic system. A variation of the anaerobic systems reported by these
investigators may have application in tannery waste treatment.
Co I or RemovaI ProbI em
In addition to reporting results from the observed biological systems
it is significant to note the problem of color. Color was not reduced
by biological treatment. Although the color of the diluted tannins
could not be matched with platinum-cobalt units, the color of the diluted
spent vegetable tannins used in the lagoon study was estimated to be
5000 color units. It was observed that color of the influent and effluent
could be reduced by blending with lime waste waters or by coagulating
with a common chemical coagulant. Influent precipitation resulted in
a bulked stringy sludge with poor settling characteristics with sludge
volumes between 50 and 90 percent of total liquid volume. Removal of
color from the lagoon effluent (best results from highly stabilized
effluent) was more successful since the sludge volume produced was 20
to 30 percent of the total volume and color removal was between 90 and
95 percent. However, sludge produced from the colored effluent raises
a serious question on treatment methods. The sludge volume resulting
from the effluent indicates that it is about equal in volume to the
total volume of concentrated spent vegetable tannins that originally
caused the color. (In addition, lime waste water is high in sulfides
which must be considered in its disposal.) Color removal is a significant
consideration in selecting the proper method of treating spent vegetable
tannins and must be thoroughly evaluated if a high degree of treatment
is to be accompIished.
43
-------
SECTION IX
BACTERIAL GROWTH USING SPENT VEGETABLE TANNINS
Genera I
The need for putting tannery waste water treatment on a sound basis and
providing a systematic approach to treatment of tannery waste waters in
a biological system requires evaluation of biological data that is useful
in design concepts that are technologically sound. Modeling of contin-
uous bacterial cultures and the use of this concept in waste design
has been recognized and is receiving more attention by designers.
Therefore, spent vegetable tannins were used as the substrate in a
completely mixed aerobic growth unit and the results were put In
terms of bacterial growth kinetic parameters.
Kinetics of Bacterial Cultures; A Brief Review
It has been recognized that waste treatment facilities are designed
on some correlation between operational variables and performance.
This has been necessary because of various waste characteristics
that are encountered and the unknown composition of the medium. Al-
though chemical oxygen demand parameters (or biochemical oxygen demand)
do not provide fundamental relations for kinetics of substrate utiliza-
tion by bacterial cultures, the sanitary engineer has to rely upon these
parameters in modeling waste treatment processes. Limitations on the
use of these parameters in bacterial growth kinetics must be recognized
and the fundamentals of enzyme-substrate interactions must be understood
by those responsible for design of biological waste treatment systems.
All engineers interested in kinetic descriptions of biological processes
using waste as a substrate should recognize that COD and BOD are
operational parameters and are not an actual measurement of substrate
[13].
A lot of attention has been directed to kinetic equations that can be
used in analysis and design of biological waste treatment systems.
Studies have been made using one substrate, multiple substrate, and
synthetic waste for kinetic description of continuous flow systems and
batch systems with mixed and pure bacterial cultures. Concepts and
theories have been well defined and the literature does indicate
sufficient agreement on kinetic models of biological oxidation for its
application to be put on a sound technological basis [143. It is not
the purpose of this work to evaluate the many theories and kinetic
models; however, it is essential that disagreement among Investigators
be pointed out.
There are two views that are expressed in regard to effective yield, Y.
One view is that the relationship between synthesis and nature of the
compound (substrate) is fixed and independent of the nature of the organic
matter being assimilated and the other Is that cell yield varies with
the chemical nature of the substrate [15], [163, [173, [183. Hetling,
45
-------
Washington, and Rao [I9H indicate that yield varies with substrate,
organisms, and detention time. In addition, these investigators con-
cluded that mixed cultures give higher yield than pure cultures and,
also, complex media give higher yield than simple media. Although
evidence indicates otherwise, the concept of constant yield for a
specific substrate has been used with some degree of success [14], [20],
[21].
Controversy exists about the variability of endogenous respiration rate,
ke. (Endogenous respiration is defined as the utilization of cellular
material by the microorganism for the energy needed to replace protoplasm.
Specific organism decay rate, k^, will be used here for the organism
decay rate due to a decrease in cellular mass.) It has not been clearly
resolved as to whether the rate of organism decay varies with substrate;
however, within limits, the "engineering concept" of a constant organism
decay rate has apparently met with some success [213.
The simple relationship between growth rate, u, of microorganisms and
substrate concentration (or nutrient),
y = y i-e-r-R-
s'
developed by Monod [223 has been very successful and is widely accepted.
This expression is the same as the generally accepted Michaelis-Menten
relationship for enzyme-substrate interaction. Other relationships have
been developed that fit growth kinetic data. Hetling and Washington
[233 studied the relationship of substrate concentration to growth rate
where substrate was measured as COD. These investigators found that a
function, ,
- A
(2)
y = y
Si t B
similar to the Michaelis-Menten equation adequately represented the
relationship.
Mathematical Mode!
A number of mathematical models have been developed for kinetic descrip-
tion of biological systems and the translation of growth kinetic param-
eter to waste treatment technology [14], [203, [2l3, [24], [253. Sound
models of continuous and batch cultures have been developed from the
following relationships (see Section XIII for notations):
y = y
dX
[KS + s]
dx . v~]
-rr = k X
dt e J
i \/ i *•" * i \/ i / ^ \
dt = kdX 'or ~ = k-x I <5)
46
-------
and
dX
dt
dS_
dt
(6)
Both continuous flow growth units and batch growth units have been used
to evaluate Y, k,j Cor kQ), u, and KS. A material balance,
A eel Is, _ A eel Is,
Ireactorj [growth
A ceI Is
organism decay
SPA cells I
leffluent lossj '
and substrate balance,
A substrate,
reactor
A substrate
influent
A substrate,
organism growth
A substrate
effluent loss
for a completely mixed continuous flow reactor (growth unit) without
recycle of suspended solids lead to a set of equations,
S0 -
x;
+1
Y
and
K
I + k .6
d
(7)
(8)
useful for determining descriptive parameters from laboratory data.
When equation 2 is used for the relationship between growth rate and
substrate, measured as COD, equation 8 becomes
6 = A + B l~ I I J_
I + 6k. -> Si - A
d vi L1 J v
Spent Vegetable Tannin Analyses
(9)
Spent vegetable tannins were obtained from Virginia Oak Tannery, Inc.,
Luray, Virginia as needed and as near the same hour of day as possible.
The tannin operation, a batch process, produces an effluent that varies
in strength during the day as well as from day to day. Table 10 is a
summary of analyses that were made on spent vegetable tannins collected
over a period of approximately six months. (The complete data is given
in Table A-ll of the Appendix.) Figure 16 shows the BOD exerted for
two different samples of tannins.
Descriptive Parameters
A continuous flow completely mixed aerobic laboratory growth unit as
shown in Figure 17 was fed spent vegetable tannins that were: (I)
diluted to a COD concentration of 1000 mg/Jl with deionized water and
(2) same strength as collected. The waste was used as collected and
no attempt was made to alter nutrient concentration or eliminate any
toxic substance that may have been present. Hence the results presented
47
-------
TABLE 10 SPENT VEGETABLE TANNIN ANALYSES
Maximum
COD, mg/A
BOD, mg/A
Total Solids, mg/i
Total Volatile Solids, mg/i
Organic Nitrogen, mg/A
Ammonia Nitrogen, mg/fc
Total Phosphorus, mg/fc
pH
|st stage BOD velocity constant (k.) at 208C, day '-
Oxygen Transfer ratio, alpha
Color:
(as collected)
dominant wavelength, mu
hue
luminance, %
purity, %
(pH adjusted to 7.6)
dominant wavelength, mu
hue
luminance, %
purity, %
Minimum
44,790
9,200
22,280
16,822
63.7
20.2
21.5
5.1
. , -1
13,380
2,500
7,940
6,788
24.4
7.6
4.8
4.6
26,500
4,648
13,639
10,984
54.6
12.0
13.1
-
A 1
0.5
60!
orange red
5.9
100
645
red
2.8
100
48
-------
12000
: -
-
10000 -
8000 -
--•-
i
6000 .
4000 -
2000 -
O DBS. BOD
X CALC. BOD
K = 0.17 day
Temp. = 20°C
Ultimate BOD = 10400 mg/JL
Ultimate BOD - 5800 mg/S
4.0 5.0
T i me, Day's
FIGURE 16 ULTIMATE BOD FOR CONCENTRATED TANNINS
-------
Pump
Reactor
Settling Basin
Substrate
Feed Storage
(Refrigeration)
Flow Meter
Air Pressure
Regulator
Compressed Air Supply
Masting
FIGURE 17 FLOW DIAGRAM OF COMPLETELY MIXED CONTINUOUS FLOW SYSTEM
-------
here represent unaltered spent tannins, except for dilution. These
data are given in Table A- 1 I and Table A-12 of the Appendix. Changes
in BOD5and suspended solids and COD with aeration time until steady-
state is reached are shown in Figure 18 and Figure 19, respectively.
Results for diluted tannins are presented in Table II in the form used
for graphical solution of equation 7. Figure 20 shows the graphical
solution for X measured as MLSS and MLVSS. Table 12 and Figure 21
show data resulting from the feed of concentrated spent vegetable tannins.
Values of kd and Y for the diluted waste were 0.045 hr"1 and
0.62 m9 for X as MLVSS, and 0.041 hr'1 and 0.78 for X as
mg COD mg uuu
MLSS. The concentrated waste indicates a k
-------
T
•
•
IxlO
Q = 8.25 A/day
0 - 17.5 Hrs.
X MLSS
A BOD5
OF- SODC
D MLVSS
Change in Cone, of
I nfIuent
\
40
200
240
I 20 I 60
Aeration time, hrs.
FIGURE 18 TYPICAL PROGRESSIVE BOD REMOVAL AND SUSPENDED SOLIDS PRODUCTION
-K -
_G
_o
280
-------
4xlOtt
-
o
a
E
Q = 8.25 A/day
0 = 17.5 Hrs.
Change in Cone, of
I nfIuent
80
I 20 I 60
Aeration Time, hrs.
200
240
280
FIGURE 19 TYPICAL PROGRESSIVE COD REMOVAL
-------
TABLE II COD AND SUSPENDED SOLID CHANGES FOR DILUTED TANNINS
9, Hrs. S , COD, mg/4 S(, COD, mg/£ X(, MLSS, mg/A 'x^ MLVSS, mg/£
49.0
24.4
16.2
12.1
996
936
910
890
636
644
696
728
92
112
96
84
70
90
74
65
TABLE 12 COD AND SUSPENDED SOLID CHANGES FOR CONCENTRATED WASTE
6, Hrs. S , COO, mg/2, S|f COD, mg/X, X(, MLSS, mg/X, 'x(, MLVSS, mg/£
46,0
22.2
22.2
17.5
17.5
12.2
12.2
5.2
5.2
11,860
32,800
24,800
27,880
21,360
19,742
20,192
17,200
12,280
6,652
7,766
6,980
9,050
9,050
12,840
13,552
16,160
11,540
1280
8892
7785
8003
6084
3638
4195
(WASHOUT)
(WASHOUT)
1060
7746
7141
7703
4682
3170
3975
-
-
54
-------
6.0
5.0
to
o
3.0
2.0
A MLVSS
O MLSS
Y = 0.62
k = 0.045 hr"
0
Y = 0.78
k = 0.041 hr'
d
i
10.0
40.0
20.0 30.0
e, HOURS
FIGURE 20 YIELD AND ORGANISM DECAY RATE FOR DILUTED TANNINS
50.0
'.)
in
;,,
6.0 -
5.0
4.0
3.0
X
~ 2.0
CO
1.0
0Di luted Waste
A Concentrated Waste
— _Di luted Waste Only
Core . Waste Only
k = 0.061 hr
d
I
I
I
10,0
40.0
20.0 30.0
6, HOURS
FIGURE 21 YIELD AND ORGANISM DECAY RATE FOR CONCENTRATED TANNINS
50.0
55
-------
16.0
15.0
10.0
-1:1
5.0
7^
'
i
05 0.0010 0.00015 0.002
]_
Sl
FIGURE 22 GROWTH RATE: MICHAELIS-MENTEN ENZYME-SUBSTRATE
INTERACTION
16.0
15.0
10.0
^
+
-I
5.0
A = 590
B = -499
V = 0.21 hr"
I
J
.005
.01
.015
.02 0.025
FIGURE 23 GROWTH RATE:
RELATIONSHIP SUGGESTED BY HETLING AND
WASHINGTON [16]
56
-------
exercised in the selection of these parameters. If biological waste
treatment design is to be technologically sound, laboratory Investiga-
tions may not only be desirable but necessary, even for like wastes
with different strengths.
Obviously, since a negative growth rate would result, the Michaelis-
Menten expression for substrate-growth interaction, using COD as
substrate, does not apply for this waste. The equation,
Si -
adequately represents the data with substrate measured
as COD. Although use of this type of expression may be regarded by some
as curve fitting, it does provide a means of evaluating a relationship
between growth and COD for an industrial waste.
Five-day BOD analyses were made on all samples but it was found that
COD results provided a better fit of the data. While BOD5 may be used
as an operational parameter and for the translation of descriptive
parameters to biological waste treatment, COD was found to be more
applicable in this investigation.
57
-------
SECTION X
ACKNOWLEDGMENTS
The support of Mr. Stephan J. Blaut and Mr. A. Nollert of Virginia Oak
Tannery, Inc. is acknowledged with sincere thanks. Mr. P. Cubbage of
Virginia Oak Tannery, Inc. provided valuable assistance during operation
of the faci tity.
An expression of gratitude is directed to Mr. David Cottrell and Mr.
Indu Thaker who performed the analytical work.
The support of the project by the Federal Water Quality Administration
and the assistance provided by Mr. Harold J. Snyder, Jr., Project
Officer, is acknowledged.
59
-------
SECTION XI
REFERENCES
I. Lin, S., "LagoonIng of Tannery Waste into Anaerobic-Aerobic Lagoons,"
M.S. Thesis, University of Cincinnati, Cincinnati (1964).
2. The Cost of Clean Water. Vol. Ill, Industrial Waste Profile No. 7,
Leather Tanning and Finishing, U. S. Department of Interior (FWPCA),
Washington, D. C., September 1967.
3. Masselli, J. W., Masselli, N. W., and Burford, M. G., "Tannery Wastes:
Pollution Sources and Methods of Treatment," New England Interstate
Water Pollution Control Commission, Boston, June 1958.
4. Standard Methods for the Examination of Water and Waste Water, 12th
Ed., Am. Pub. Health Assoc., New York (1965).
5. Official Methods of Analyses of the Association of Official Agricul-
tural Chemists, IOth Ed., 11(d)(1965).
6. Pons, W. A., Jr. and Guthrie, J. D., "Determination of Inorganic
Phosphorus in Plant Materials," Anal. Ed., Ind. Eng. Chem., 18,
184 (1946).
7. Eckenfelder, W. W., Jr., and O'Connor, D. J ., Biologica I Waste Treat-
ment, Pergamon Press, New York (196!).
8. Sawyer, C. N., "New Concepts in Aerated Lagoon Design and Operation,"
Advances in Water Qua Iity Improvement, (edited by Gloyna, E. F.
and Eckenfelder, W. W., Jr.), U. of Texas Press, Austin (1968).
9. Steffen, A. J., "Waste Treatment in the Meat Processing Industry,"
Advances in Water Quality Improvement, (edited by Gloyna, E. F. and
Eckenfelder, W. W., Jr.), U. of Texas Press, Austin (1968).
10. Steffen, A. J., and Bedker, M., "Operation of Full-Scale Anaerobic
Contact Treatment Plant for Meat Packing Wastes," Proc. 16th
Ind. Waste Conf., Purdue University, 423, 1961.
II. Gates, W. E., Smith, J. H., Lin, S., and Ris, C. H., Ill, "A
Rational Model for the Anaerobic Contact Process," J. Water Pol I.
Cont. Fed., 39, 1951 (1967).
12. McCarty, P. L., "Anaerobic Treatment of Soluble Wastes," Advances
in Water Quality Improvement (edited by Gloyna, E. F. and Eckenfelder,.
W. W., Jr.), U. of Texas Press, Austin (1968).
13. Stumm-ZolIinger, Elisabeth, Busch, P. L., and Stumm, W., discussion
of "Kinetics of Aerobic Removal of Organic Wastes," by K. Keshavan,
V. C. Behn, and W. F. Ames, Jour. San. Engineering Div., Proceedings
of A.S.C.E., 90_, SA4, 107 (1964).
61
-------
14. Pearson, E. A., "Kinetics of Biological Treatment," Advances in
Water Qua Iity Improvement (edited by Gloyna, E. F. and Eckenfelder,
W. W., Jr.), U. of Texas Press, Austin (1968).
15. Henkelekian, H., Oxford, H. E. and Manganelli, R., "Factors Affecting
the Quantity of Sludge Production in Activated Sludge Process," Sew.
and Ind. W. Jour., 23, 945 (1951).
16. McKinney, R. E., "Mathematics of Complete-Mixing Activated Sludge,"
Journ. San. Engineering Div., Proceedings of A.S.C.E., 88, SA3,
87 (1962).
17. Placak, 0. R. and Rochhoft, C. G., "The Utilization of Organic Sub-
strate by Activated Sludge," Sew. Works Jour., J_9, 423 (1947).
18. McCabe, B. J. and Eckenfelder, W. W., "Process Design of Biological
Oxidation for Industrial Waste Treatment." Waste Treatment, Pergamon
Press, London, I960.
19. Met]ing, L. J., Washington, D. R., and Rao, S. S., "Kinetics of the
Steady-State Bacterial Culture II. Variation in Synthesis,"
Proc. of the 19th Ind. Waste Conf., Purdue University, 687, 1964.
20. Reynolds, T. D., and Yang, J. T., "Model of the Completely-Mixed
Activated Sludge Process," Proc. of the 21st Ind. Waste Conf.,
Purdue University, 696, 1966.
21. Middlebrooks, E. J., and Garland, C. F., "Kinetics of Model and Field
Extended-Aeration Waste Water Treatment Units," Jour. Water Pol I.
Control Fed., 40_, 586 (1968).
22. Monod, J., The Growth of Bacterial Cultures," Ann. Rev. M i rcob ? oI.,
3, 371 (1949).
23. Hetling, L. J. and Washington, D. R., "Kinetics of the Steady-State
Bacterial Culture III. Growth Rate," Proc. of the 20th Ind. Waste
Conf., Purdue University, 254, 1965.
24. Martin, E. J. and Washington, D. R., "Kinetics of the Steady-State
Bacterial Culture. I. Mathematical Model," Proc. of the 19th Ind.
Waste Conf., Purdue University, 724, 1964.
25. Herbert, D., Elsworth, R. and Telling, R. C., "The Continuous Culture
of Bacteria; A Theoretical and Experimental Study," Jour. Gen.
Mlcrobiol., 14, 601 (1956).
62
-------
SECTION XI I
PUBLICATIONS AND PATENTS
No patent has been produced as a result of this work.
The following publications have been produced as a result of this project:
(I) Parker, C. E. and Thaker, I. H., "A Study of Kinetic Parameters
Using Spent Vegetable Tannins," Proc. of the 3rd Mid-Atlantic Ind. Waste
Conf., University of Maryland, November 1969.
(2) Parker, C. E., "Biological Treatment of Spent Vegetable Tannins,"
Proc. of the 25th Ind. Waste Conf., Purdue University, May 1970.
63
-------
SECTION XI I I
NOTATIONS
A = constant in Hetling-Washington expression
a = synthesis to sludge ratio
B = constant in Hetling-Washington expression
b = rate of auto-oxidation
B.hp = brake horsepower
BOD5 = 5-day biochemical oxygen demand at 20°C
C = initial DO at beginning of an observation
C = DO saturation
C, = DO after time, t
COD = chemical oxygen demand
DO = dissolved oxygen
E = efficiency
F-prefix = analysis of the filtrate (soluble fraction)
FSS = fixed suspended solids
K BOD velocity constant (common log)
K = BOD5 observed removaI rate
k, = specific organism decay rate hours"1
k = endogenous respiration, hours"1
6
K. = oxygen transfer coefficient
K = constant in Michaelis-Menten expression
L = BOD removed
MLSS = suspended solids in aeration unit
MLVSS = volatile suspended solids in aeration unit
N:BOD5 = nitrogen to BOD5 ratio
65
-------
N:COD = nitrogen to COD ratio
NHs-N = ammonia nitrogen
ORG-N = organic nitrogen
P:BOD5 = phosphorus to BOD5 ratio
P:COD = phosphorus to COD ratio
pH = hydrogen ion concentration
Q = flow rate
S = substrate in aeration unit in terms of influent substrate
S = average mixed liquor suspended solids
a
Si = waste concentration in aeration unit as COD, mg/£
S0 = waste concentration of aeration unit influent as COD, mg/fc
Set. S. = settleable solids
SS = suspended solids
T = temperature, °C
t = time
TKN = total Kjeldahl nitrogen
TFS = total fixed solids
TP = total phosphorus
TS = totaI so I!ds
T. Sulf. = total suI fides
TVS = total volatile solids
VOTAN = Virginia Oak Tannery, Inc.
VSS = volatile suspended solids
X = cell concentration
Xi = MLSS as measure of cell concentration, mg/Jl
'Xj = MLVSS as measure of cell concentration, mg/A
66
-------
= yield coefficient, mg MLSS or MLVSS per tng COD (for
fundamental relationship: mg cells per mg substrate),
= aeration unit retention time, hours
= observed specific growth rate, hours"1
= maximum specific growth rate, hours"1
67
-------
SECTfON XIV
APPENDIX
Page
Determination of Total Phosphorus . 70
Table A-l: Oxygen Transfer: Lagoon Influent 72
Table A-2: Ultimate BOD: Lagoon Influent 73
Table A-3: Average Weekly Flow 74
Table A-4: Influent Data: Batepool, Soak and 75
Tannins with Bleach 75
Table A-5: Influent Data: Batepool and Tannins 76
Table A-6: Effluent Data: Phase I 77
Table A-7: Effluent Data: Phase II 7
Table A-8: Effluent Data: Phase III 78
Table A-9: Effluent Data: Phase IV 79
Table A-10: Effluent Data: Phase V 79
Table A-l I: Concentrated Vegetable Tannin Analyses 80
Table A-12: Reactor Data for Diluted Tannins 80
Table A-13: Reactor Effluent for Cone. Tannins:
5.2 HR. D.T 8!
Table A-14: Reactor Effluent for Cone. Tannins:
12.2 HR. D.T 81
Table A-15: Reactor Effluent for Cone. Tannins:
17.5 HR. D.T 82
Table A-l6: Reactor Effluent for Cone. Tannins:
22.2 HR. D.T 83
Table A-17: Reactor Effluent for Cone. Tannins:
46.0 HR. D.T 84
69
-------
DETERMINATION OF TOTAL PHOSPHORUS
Reagents
Sulfuric acid, H^Oij, concentrated reagent grade
Sodium nitrate, NaNOa, reagent grade
Sodi urn hydroxide, NaOH, concentrated (approximately 15 N)
Phenol phtha lei n indicator
Molybdate reagent. Dissolve 50 gm of (NHit)6Mo702it. 4H20, in 400 ml of
10 N_ su If uric acid and 500 ml of water, make up to I liter, and store
in a paraffin-lined bottle.
Sulfuric acid, (Approximately Ni) Dilute 114 ml of cone, sulfuric acid
to 4 I iters.
Stannous chloride stock so In., 10 gm SnCI2-6H20 or 7.5 gm SnCI2-2H20
in 25 ml of cone. HCI. Store in a small glass-stoppered brown bottle.
Stannous chloride dilute soln. Di lute I ml of stock soln. to 200 ml
with approximately N sulfuric acid just before use.
I sobuty I Alcohol . Comm. grade, with a boiling range 106° to IIO°C.
Ethyl Alcohol . 95%.
Standard phosphate soln. Recrystal I ize A.C.S. grade monobasic potassium
phosphate 3 times from water, dry at MO°C, and store in a desiccator
over concentrated sulfuric acid. Dissolve 4.3929 gm of the dry salt
in 300 ml of water and 200 ml of approximately N sulfuric acid. Add
a few drops of 0. I N potassium permanganate as preservative and make up
to I liter with water. This stock soln., 1.0 mg of P per ml \s
stable. Dilute as needed.
Analytical Procedure
Place 100 ml of the sample (or suitable aliquot) in an 500 ml Kjeldahl
flask and add 20 ml cone. H2SOit. Heat to boi ling and add about 1.5 gm
NaNC^. Be careful of extreme foaming. Boil down to cone. acid.
(Solution may not be clear.) Add a small amount of NaNOs anc' solution
should become clear. Cool, add 40 ml water, and boil for 2-3 minutes.
Cool and neutralize to faint pink phenolphtha lein color with cone.
NaOH (about 1.5 N). Be very careful of splattering. (White solid
may form.) Transfer to 200 or 250 ml volumetric flask. Rinse Kjeldahl
flask thoroughly with small amounts of water until correct volume is
reached. (White solid should dissolve.) Transfer 15 ml of diluted
solution to separatory funnel and add 5 ml of molybdate solution. Add
10 ml butyl alcohol and shake for 30 sec., removing aqueous layer.
70
-------
Add 10 mi of approximately I N sulfuric acid and shake for 30 sec.,
removing aqueous layer. Add 16 m2, of stannous chloride solution and
shake for 30 sec., removing aqueous layer after the blue color separates.
Transfer blue alcoholic layer to 50 m£ volumetric flask, rinse funnel
with ethanol, and dilute to 50 mH with ethanol. Let color develop for
I hr 15 min. Record percent transmittance at 630 m£ against a blank
of 15 mSL distilled water treated as the waste sample. Read mg
phosphorus off calibration curve made from standard phosphorus solution
curve. Make correction to find mg/i, in original sample of 100 mfc.
71
-------
TABLE A-I OXYGEN TRANSFER: LAGOON INFLUENT
LAGOON INFLUENT DI STILLED WATER
T=3I°C, Cs=6.0mg/* T=26°C,C =6.6mg/A T=26°C,C =7.
Dissolved
Oxygen, mg/t tlme,mln. tlme,mln. i\me,m\n. tlme,mln. tlme,m!n.
1.0 0 0 0 0 0
1.5 0.3 0.3 0.3 0 0.2
2.0 0.6 0.7 0.7 0.4 0.4
2.5 1.0 I.I I.I 0.8 0.7
3.0 1.5 1.5 1.4 I.I 0.9
3.5 2.1 2.1 2.0 1.6 I.I
4.0 2.6 2.7 2.6 2.1 1.4
4.5 3.4 3.6 3.5 2.8 1.8
5.0 4.2 4.6 4.5 3.6 2.1
5.5 6.4 - 6.8 5.0 2.6
6.0 - 3.2
6.5 - 4.3
7.0 - 5.8
72
-------
TABLE A-2 ULTIMATE BOD: LAGOON INFLUENT
Biochemical Oxygen Demand, mg/l (T = 20°C )
(By Date Collected)
Time, Days 7/11/68 7/16/68 8/8/68 9/18/69
0.5 - 270
1.0 - 619 550 590
2.0 - 903
3.0 1600 1062 918 980
4.0 - 1170
5.0 1850 1250 1100 1230
7.0 2000 1462 - 1475
9.0 - 1600 - 1725
11.0 - 1800 - 1825
13.0 - 1875
14.0 - 1650
15.0 - 1700
17.0 - 1700 - -
20.0 - 1700
73
-------
TABLE A-3 AVERAGE WEEKLY FLOW
DATE
15-21 Dec. 68
22-28
29 Dec. 68-4 Jan. 69
4-11 Jan. 69
12-18
19-25
26 Jan.-l Feb.
2-8 Feb.
9-15
16-22
23 Feb. -I Mar.
2-8 Mar.
9-15
16-22
23-29
30 Mar.- 5 Apr.
6-12 Apr.
13-19
20-26
27 Apr.- 3 May
Flow, gpm
30*
25*
36*
31*
40
41
32
34
36
41
29
3(»
29
24
35
24
80*
60
65
72
DATE
4-10 May
11-17
18-24
25-31
1-7 Jun
8-14
15-21
22-28
29 Jun. -5 Jul.
6-12 Jul.
13-19
20-26
27 Jul.- 2 Aug.
3-9 Aug.
10-16
17-23
24-30
31 Aug.- 6 Sept.
7-13 Sept.
14-20 Sept. 69
F 1 ow , gpm
65
65
60
68*
60
58
92
70
80
125
143
147
115
120
115
125
120
105
134
145
5-day flow, all others 7-day flow.
74
-------
TABLE A-4 INFLUENT DATA: BATEPOOL, SOAK AND TANNINS WITH BLEACH
(I)
ui
Date
4/30/68<:1
5/7/66 (2)
5/14/68
5/20-21/68
5/28-29/68
6/4-5/68
6/11-12/66
(2) (3)
6/l8-l9/68U '
7/1 1-12/68
7/15-16/68
7/17-18/68
7/22-23/68
7/24-25/68
7/30-31/68
8/1-2/66
8/6-7/68
8/8-9/68
B/ 12- 13/68
8/ 14- 15/68
8/20-21/68
8/27-28/68
9/J-4/68
9/10-11/68
9/17.18/68
9/24-25/68
10/1-2/68
10/8-9/68
10/22-23/68
10/29- 30/68* *'
11/21-22/68
(2/3-4/68
I2/II/68(2''15)
I2/I9.20/6812'
1/7-8/69
BOD 5 COO
4400
2300
1200
800
925
1825 5629
1150 5380
ORG-N
..
,
-
-
-
44.2
48.3
725 3640 47.8
NH3N
_
-
-
-
-
51.0
44.0
32.3
TOi
.
-
-
-
-
95.2
92.5
80.1
1850 -
1250 5663
1213 5352
975 4352
775 5951
800 4275
775 3353
IZ50 5711
1100 5128
.
763
5129
775 2642
_
950
998 2701
1018
846 1937
950 2714
1075 6616
850 547
950 2879
725 3757
5100 >7640
750 3826
1190 5769
'"RMultf In «9/I
"W sa»l.
38.0
37.0
32.9
39.5
33.4
35.1
47.3
32.6
„
_
40.6
.
.
_
_
45.3
..
S5.3
38.8
31.0
40.3
28.3
2.2
64.4
74.7
•xoapt
46.8
53.2
66.3
40.5
51.5
59.4
52.1
46.4
.
.
40.2
_
_
.
„
36.1
r
62.7
23.8
48.7
40.3
58.2
5.9
26.6
2T.7
pH and SS.
84.8
90.2
99.2
90.0
84.9
94.5
99.4
79.0
_
_
80. B
_
_
w
.
61.4
_
98. a
62.6
79.7
80.6
86.!
8.1
101. 0
102.4
SS In
TS
21635
1432ft
9835
8856
652'3
11031
10612
41 16
10168
7584
595S
7856
9856
6892
6781
11835
7IB4
7773
.
.
,
10004
10691
_
IOIII
7963
5051
13307
12907
-
6931
23044
5708
(5845
m/i
TF<
10623
993S
6893
6858
6024
6888
7156
1728
6490
4355
3860
5144
6647
4349
4743
8438
3935
5731
_
.
.
7567
8955
.
7486
6820
3435
8880
8680
-
5206
1874
3595
13675
TVS s; FSS
11012
4388
2942
2008
2498
4143
3456
2388 566 2
3678
3229 643 182
3138 463
2712 376
3209 350 0
2543 460 75
2038 392
3397 975 0
3249 282
2042 882 30
-
.
-
2437
I7J6
.
2625
1143
1616
4427
4227
-
1725
21170
2113
2170
vss S*t-
_
-
-
-
-
-
_
564 1.0
_
461 0.2
0.3
0.6
350 0.2
385 0.2
0.3
975 122.0
0,5
852 5.5
-
1,0
1.0
8.0
4.0
-
70
0.5
0,6
85
5Q
15
0.1
0.0
1.0
0.5
Total Total
pH Sulfide Phosphorus
.
-
-
-
-
.
6.2
3.4
5.7
5.7
5.5
6.2
5.6
5.2 I.72
6.6
4.6
5.4
7.3 I.82 4.46
6.0 0.3 8.47
7.6 - 7.67
6.8 1.0
8.6
6.0
4.0
3.2
6.9
6.5
3,5
9.3
7.5
7.0
4.5
6.8
7.2
(3)No soak Mstewater
I4)No tannins
'"T.I<1.!»5 only
-------
TABLE A-5 INFLUENT DATA: BATEPOOL AND TANNINS
(I)
Date
1/14-15/69
2/1 1-12/69
2/18-19/69
3/4-5/69
3/18-19/69
4/8-9/69
4/24-25/69
5/7-8/69<2>
5/20-2l/69(2>
6/3-4/69
6/17-18/69
6/1 9-20/69 (3)
6/25-26/69
7/16-17-69
7/23-24/69
7/29-30/69
8/5-6/69
8/14-15/69
8/20-21/69
8/27-28/69
9/10-11/69
9/17-18/69
BOD5
1000
1850
H75
1000
1000
725
1125
475
350
850
2000
775
1600
850
1050
900
750
1200
1000
1250
2050
1215
Results
COD
2349
7775
4720
5860
3980
4660
4490
2000
1920
5540
7340
6120
4421
4660
3760
2520
3666
3820
6700
3980
3720
in mg/1
ORG-N
^
26.8
49.0
65.5
29.4
65.2
24.7
27.4
28.8
51.5
-
52.7
35.5
37.8
29.3
52.4
-
109.4
-
except
NH3-N
.
53.8
66.4
69.4
73.3
40.4
39.8
39.8
34.2
33.1
-
36.9
66.1
59.1
92.2
65.8
-
99,6
-
pH and SS.
TKN
.
80.6
115.4
134.9
102.7
105.6
64.5
67.2
63.0
84.6
-
89.6
101.6
96.9
121.5
118.2
-
209. Q
-
SS In
TS
—
4730
4733
5637
3664
-
3805
1848
1625
5042
2556
4904
2902
3119
3092
2920
5050
4108
5975
7579
6034
mi/i
TFS
_
2350
2320
2990
1865
-
1024
958
850
1702
660
1622
900
946
1267
1536
2211
2074
2245
34IQ
2363
TVS
.
2380
2313
2647
1799
.
2781
890
775
3340
1896
3286
2002
2173
1825
1384
1839.
2034
3730
4169
3671
Set.
S.
>40
1.5
1.0
2.5
r.s
2.0
1.5
0.5
0.5
0.5
7.5
8.0
6.0
7.5
15
>40
18
10
6.0
5.Q
5.0.
pH
9.6
6.6
6.5
7.6
6.4
6.5
6.5
6.9
6.8
6.2
6.7
6.2
5.8
6.5
6.5
6.9
7.8
7.3
6.3
6.3
7.U
fi.9
Total Total
bulfide Phosphorus
.. •
• _
_ .
8.80
_
\ \
.
7.60
-
-
-
1,2
-
0.4
-
-
0.4 5.61
-
No tanntns : • - •
(3)
Aerator near effluent end off.
-------
TABLE A-6 EFFLUENT DATA: PHASE I (Q = 15 GPM)
(I)
ANALYSIS
Data
4/30/68 ^
5/7/68^'
5/14/68
5/20-21/68
5/28-29/68
6/4-5/68
6/1 1-12/68
6/18-19/68
7/1 1-12/68
7/l5-l6/68*2)
7/17-18/68
7/22-23/68 (21
7/24-25/68
(21
7/30-3 1/681""
8/,-W2)(3>
8/6-7/68t2)
8/8-9/68
(2)
8/ 1 2-1 3/68^
8/14-15/68
BOD5
400
ISO
130
100
97
8.5
53
27
50
48
50
39
II
32
21
29
30
25
24
COD
.
-
-
-
-
2256
1341
1426
_
838
891
1202
H77
1205
710
1157
832
-
-
ORG-N
.
-
-
-
-
37.1
20.9
22.8
-
21.0
14.3
17.9
16.9
19.0
11.7
20.4
U.2
-
-
NH3N
,
-
-
-
-
36.0
29.0
30.1
-
18.2
19.6
23.0
23.4
25.2
25.8
26.9
25.8
-
•
TKN
_
-
-
-
-
73.1
49.9
52.9
-
39.2
33.9
40.9
40.3
44.2
37.5
47.3
40.0
-
—
TS
5507
6045
6480
6809
7361
7609
7208
7104
6156
6106
6272
6274
6110
6053
5615
6057
5854
6077
••
TFS
3767
4180
4709
5474
5988
5947
6202
6042
5460
6369
5636
5339
5314
5073
5032
5115
5175
5155
—
TVS
1730
1865
1771
1335
1372
1662
1006
1062
696
737
636
935
796
980
583
932
679
922
~
SS
-
-
-
-
-
-
673
-
221
183
311
198
469
-
629
-
502
^•wwamv
FSS
.
-
-
-
-
-
-
242
-
60
86
15
12
125
-
152
-
61
VSS
_
-
-
-
-
-
-
431
-
161
97
296
186
344
-
477
-
441
Set.
S.
.
-
-
-
-
-
-
39.0
-
6.5
2.0
13.0
16.0
22.0
-
27.0
-
23.0
24.0
Total
pH Sulflde
.
-
-
-
-
-
7.4
7.2
6.9
7.2
7.0
7.0
7.0
6.9 0
7.1
7.0
7.2
7.3 0
(2)
7.1 0
Total
Phosphorus
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
2.22
2.45
(I)
(2)
(3)
Results tn mg/j except pH and SS. SS In m}Ji
Grab sample
Aerator off for I hr. prior to sample collection
-------
TABLE A-7 EFFLUENT DATA: PHASE II (Q = 20 GFrM)
(I)
oo
DATE BOD5 F-BOD5 COD
8/20-21/68
8/27-28/68
9/3-4/66(2>
9/10- 11/68
9/17-18/68
9/24-25/68
10/1-2/68
10/8-9/68
10/22-23/68
10/29-30/68
11/21-22/68
12/3-4/68
749
35 - 1042
42
37
43
48 26 1243
41 16 1330
42 20 1545
43 14 1720
1 708
51 10 1748
F-COO
-
-
382
352
461
484
532
562
'"Results in ng/t except pH
ORG-N F-ORG-N NH3-N F-NH3-N TKN
23.3
28.8
-
35.6
44.1
21.6
23.4
36.1
and SS.
TABLE A- 8
Date
12/10-1 1/68
12/19-20/68
1 /7-S/69
1/14-15/69
2/1 1-12/69
2/18-19/69
3/4-5/69
3'I8-I9/69C2>
BOD5 F-60D5 COO
66 23 1 704
773 47 1548
169 774 2012
161 79 2101
114 50 1 936
130 87 1760
122 38 2038
155 68 2408
25.9
23.3
-
7.4 30.2
5.0 28.5
4.0 28.5
8.9 25.8
5.6 37.8
SS in nlfl
EFFLUENT
49.2
52.1
-
25.2 65.8
27.3 72.6
27.6 50.1
24.3 49.2
33.9 73.9
F-TKN
-
-
-
32.6
32.3
31.6
33.2
39,5
TS TfS
7196 6505
6996 6315
7631 6829
7787 6687
7533 6531
7682 6586
7615 6480
-
6312 5222
TVS SS
691
681
802
1100 613
1 002 926
1096 -
1 135 -
-
1090 937
FSS
-
-
146
180
-
-
-
425
Set.
VSS S.
- 28.0
- IO..Q
- 25.0
- 40.0
667 48.0
746 48.0
896 31.0
915 24.0
- 20. Q
512 1 1.0
Tota 1 Tota 1
pH Sulfi.de Phosphorus
7.6 - 7.67
7.2 0
7.4
7.2
7.0
6.3
6.9
6.7
6.9
7.2
7.2
7.3
Sampled after long weekend holiday
DATA:
F-COO ORG-N F-ORG-N NH3-N F-NH3-N TKN
712
1372
1328
141 1
1376
1416
1248
1528
3.8
33.1
35.0
-
39.0
35.6
35.9
49.8
7.8 35.7
12.9 42.0
6.1 41.7
-
9.3 31.6
9.0 30.5
8,1 37.8
16.8 32.2
20.7 39.5
33.9 80.1
40.6 76.7
-
30.5 70.6
28.3 66.1
36.1 73.7
30.0 82.0
PHASE
F-TKN
28.5
46.8
46.7
-
39.9
37.3
44.2
46.8
III (Q=
TS TFS
6761 5693
6157 5219
5304 4334
-
2190 1295
2 1 87 1 285
2621 1575
3180 1555
33 GPM)
TVS SS
1068 1567
938 1 030
970 681
-
895 330
902 327
1046 650
1625 770
(1)
FSS
910
638
276
-
95
74
279
••
Set.
VSS S.
657 11.0
392 14.0
435 0.5
3.5
235 1.5
243 4.0
371 0.7
0.7
Tota 1 Tota 1
pH Su If ides Phosphorus
7.9
7.0
7.3
7.3
7.4
7.3
7.5
7.4 0 5.6
(2)
Results In mg/£ except pH and SS. SS in mt/i.
Aerator near effluent off.
-------
TABLE A-9 EFFLUENT DATA: PHASE IV (Q = 69 GPM)
(I )
DATE
4/3-9/69
4/24-25/69
5/7-8/69
5/20-21/69
6/3-4/69
6/17-1 8/69
6/19-20/69
6/25-26/69
DATA
7/16-1 7/69
7/23-24/69
7/29-30/69
8/5-6/69
8/14-15/69
8/20-21/69
8/27-28/69
9/10-1 1/69
9/17-18/69
BOD5 F-B005 COO F-COD ORG-N F-ORO-N NH3-N F-NH3-N TKN F-TKN TS T
400 230 3876 2480 49.8 17.9 33.3 30.5 83
260 120 2408 1472 -
85 50 1600 992 -
90 70 1576 1008 15.3 5.3 19.9 15.7 35
248 155 (738 123? 19.3 5.6 17.9 17.1 37
276 118 2192 1375 14.0 5.3 17.6 16.5 31
•PS TVS SS FSS VSS
.1 48.4 ------
3017 1418 1599 358 78 280
1370 640 730 395 91 304
.? 21.0 1685 615 1070 430 70 360
.2 22.7 2027 805 1222 422 93 329
.6 21.8 2614 818 1795 664 65 599
345 170 - - - - - - - - ------
240 160
(1)
BOD5
420
410
253
175
240
250
260
390
410
Resu 1 ts
F-BOD5
260
275
103
60
85
60
130
210
250
in mg/fc
38.0 75.8 77.7 20.7 65
except pH and SS. SS in nl/i
TABLE A- 10 EFFLUENT DATA:
COD F-COD ORG-N F-ORG-N NH3-N F-NH3-N TKN
2520
2552
1632
1352
2104
2088
2040
2392
2335
1848 -
2042 38.6 27.9 31.6 25.5 70.2
1296 11.5 7.0 44.2 34.2 55.7
784 10.3 6.7 42.0 31.6 52.3
1240 35.9 7.0 41.7 40.0 77.6
1352 30.5 4.1 44.0 42.6 74.5
1016 -----
1592 16.8 15.4 45.1 36.7 61.9
1705 - - -
.2 46.0 7A
PHASE V
FTKN TS
2082
53.4 2184
41.2 1933
48.3 1797
47.0 2397
46.7 2399
2481
52.1 2307
2752
73
(Q
TFS
879
971
788
867
1054
1245
1 195
1 110
1230
024 1549 56R 165 403
-I
TVS
1203
1213
1145
930
1343
1 154
1288
1097
1522
27 GPM)M)
SS FSS VSS
510 214 296
572 273 299
399 2 397
494 0 494
537 0 537
304 0 304
414 104 310
429 58 37 1
477 230 247
Set. Total Total
S. pH Suit ides Phosphorus
0.8 6.8
1.0 7.3
0.8 7.2
0.3 7.1
0.2 7.0
0.5 7.0 0 5.8
2.0 7.1
2.5 6.9
Set. Total Total F-PhoS'
S. pH Sulfide Phosphorus phorus
3.0 7.0 - -
3.5 7.0 - -
1.5 7.1 0.5
0.8 6.8 - -
1.5 7..0 0.4
3.0 6.8 -
1.5 6.7 - -
1.0 6.8 0.0 3.6 2.9
1.8 6.9 -
(I)
Results in mg/t except pH and SS. SS in ml/!..
-------
TABLE A-ll CONCENTRATED VEGETABLE TANNIN ANALYSES('*'(2)
oo
o
Date
4/10/69
4/20/69
5/11/69
5/15/69
6/6/69
6/17/69
6/22/69
6/30/69
7/18/69
7/25/69
7/31/69
8/21/69
BOD5 F-BOD5 COD
5900 3400 44790
34640
3300 2300 25600
4000 2450 24992
3000 2200 20860
4150 2600 27680
9000 6300 37996
9200 6550 28160
3450 2300 20480
2500 1950 13380
1975 1650 13850
1 1250 7580 57865
Data In mg/l except
Grab samples
6 P
49 2.94
STEADYSTATE
24.4 5.9
STEADYSTATE
16.2 8.9
STEADYSTATE
12.0 12.0
STEADYSTATE
F-COO TS
32800 20494
24800
19742 II 81 6
20192 12430
14600 10194
21585 11050
27880 22000
21360 22280
17200 10222
1 1 920 7960
1 1 860 7940
43580 25880
TFS
3672
-
1470
1710
1520
1510
5668
7300
1582
960
1152
7460
temperature and pH.
TABLE
A- 12
Time F-BODs
0
142
0
162
0
168
• o
144
230
70
220
55
215
75
212
85
TVS SS FSS VSS Temp.
16822 4222
-
10346 2226
10720 2570
8674 1 868
9540 2100
16332 1384
14980 2560
8640 1 906
7000 1230
6780 640
18420 3220
308
-
220
286
278
218
228
498
342
138
152
390
3914 24
24
2006 24
2234 24
1 590 24
1882 24
1 1 56 24
2062 24
1564 24
1092 24
588 24
2830 24
pH
4.7
4.8
5. 1
4.7
4.9
4.6
4.8
5.0
4.7
4.8
5.1
4.9
TKN
78.4
-
58.3
-
74.8
-
68.3
83.40
69.44
-
31.92
-
F-TKN NH3-N F-NH3-N ORG-N F-ORGN
59.4 15.7
-
35.8 7.8
-
55.4 13.8
-
51.6 8.4
67.2 20 J 6
56.56 10.08
-
23.5 7.6
-
13.4 62.7 45.9
-
5.6 50.4 30.2
.
11.9 61.0 43.5
_
5.6 59.9 46.0
15.68 63.2 51.5
8.J2 59.4 48.4
-
6.2 24.4 17.4
-
TP F-TP
20.1 14.1
-
8.3 6.0
-
14.8 11.7
-
16.00 14.2
21.5 16.8
6.4 5.3
-
4.8 3.9
-
Temperature In °6
REACTOR
F-COD
996
636
936
644
910
696
890
728
DATA
TS
588
886
544
848
568
646
610
760
FOR Dl
TFS
248
264
223
223
230
158
258
210
LUTED
TANNINS(I)
TVS SS
340
622
321
625
338
488
352
550
58
92
64
112
72
96
66
84
FSS VSS
28 30
48 69
24 40
22 90
32 40
24 72
34 32
18 66
Temp. pH
5.2
24 6.4
5.4
25 6.5
5. 1
24 6.2
5.3
25 6. 1
(I)
9 in hours, 0 in I/day, time in hours and temp in "C. All others in mg/i except pH.
-------
TABLE A-13 REACTOR EFFLUENT FOR CONC. TANNINS: 5.2 HR. D.T.(I)'(2)
Time
00
Date
7/18/69
BOD5
3450
F-BOD5
2300
COD
20480
F-COD
17200
TS
10222
TFS
1582
TVS
8640
SS
1906
FSS VSS
342 1 564
Temp.
-
pH TKN F-TKN NH3-N F-NH3-N ORG-N F-ORGN TP
4.7 69.4 56.6 10. 1 8.1 59.3 48.5 6.4
F-TP
5.3
(INFLUENT)
40
90
134
00
7/20/69
7/22/69
7/24/69
7/25/69
3050
2550
2350
2500
1850
1450
1425
1950
18480
18280
17880
13380
16720
16440
16160
11920
10332
10440
10564
7960
1522
1568
1420
960
8810
8892
9140
7000
1432
1788
1750
1230
1 94 1 238
346 1442
192 1558
133 1092
26
24
24
-
5.8 - - - -
5.9 -
5.8
4.8 -
r
-
-
-
(INFLUENT)
208
256
306
7/27/69
7/29/69
7/31/69
2150
1975
1950
1350
1300
1238
13280
13560
13440
12280
1 1680
11540
9640
9760
9840
1160
1120
1040
8480
8640
8800
1450
1040
1024
122 1328
1 25 915
164 860
24
24
23
5.6
6.0 -
5.9 65.0 58.2 3.4 1.7 61.6 56.5 4.1
-
-
3.8
Time In hours and temperature in °C; Other data in tng/t excebt Date and pH
CO (2)
— J « 27.6 Vday
TABLE A-14 REACTOR EFFLUENT FOR CONC. TANNINS: 12.2 HR. D.T.(I)'(2)
Time Oat« BOOS F-B005 COD F-COO TS TFS TVS SS FSS VSS Temp. pH TKN F-TKN NH3-N F-NH3-N ORG-N F-ORGN TP F-TP
00 5/11/69 3300 2300 25600 19742 I 1816 1470 10346 2226 220 2006 - 5.1 58.2 35.8 7.8 5.6 50.4 30.2 8.3 6.0
INFLUENT)
49 5/13/69 1800 950 20000 13360 11052 1638 9414 3012 482 2630 25 6.3 - -
97 5/15/69 1850 825 18960 12840 12238 1624 10614 3638 468 3170 25 6.4 - -
00 5/15/69 4000 2450 24992 20192 12430 1710 10720 2570 286 2284 -4.7--- - - -
(INFLUENT)
147 5/17/69 1950 837 20112 10776 13010 1766 11244 4058 266 3792 24 6.4 - -
190 5/19/69 2000 975 20200 13600 12344 2100 10244 4198 274 3924 24 6.7 - -
262 5/22/69 1950 1025 I7SOO 13552 12991 2450 10541 4195 220 3975 24 6.8 56.5 33.7 4.5 3.4 52.0 30.3 8.0 3.8
rime in hours and temperature in °C; Other data in mqfl except Date and RH
-------
TABLE A-15 REACTOR EFFLUENT FOR CONC. TANNINS: 17.5 HR. D.T.
(I),(2)
Time
00
Date
6/22/69
BOD 5
9000
F-BOD5
6300
COD
37996
F-COD
27880
TS
22000
TFS
5668
TVS SS
16332 1384
FSS
228
VSS
1 156
Temo.
„
DH TKN F-TKN NH3-N F-NH3-N ORG-N
4.8 68.32 51.6 8.4 5.6 59.92
F-ORGN TP F-TP
46.00 16.00 142
(INFLUENT)
20
46
70
42
8 l63
187
00
6/23/69
6/24/69
6/25/69
6/27/69
6/29/69
6/30/69
6/30/69
6050
3600
3400
3400
3350
3325
9200
4950
3200
2300
2320
2200
21 10
6555
26960
24080
23750
23360
23760
23550
28160
20920
15120
13180
1 1400
9040
9050
21360
21610
22468
22466
22628
20496
21528
22280
5456
6560
7722
4040
3806
3540
7300
16154 2500
15908 5678
14744 5854
18588 6878
1 6690 8026
17938 8003
14980 2560
278
674
1462
420
398
300
498
2222
5004
4392
6458
7628
7703
2062
24
28
27
30.0
28.5
29.0
28.0
5.8 - - - -
6.6 -
7.2 - - - -
6.5 - -
6.7 -
6.6 - - - - -
5.0 83.4 67.2 20.16 15.68 63.24
.
.
.
-
: : ;
51.52 21.5 16.8
( INFLUENT)
235
283
7/2/69
7/4/69
3350
3450
2162
2225
23550
23840
8280
9050
22465
23420
7200
7124
15265 6015
16296 6084
1 150
1402
4865
4682
26.5
27.0
6.6 - - -
6.7 68.40 56.6 7.8 6.8 60.6
-
49.8 15.8 14.2
(I)
(2)
Time in hours and temoerature in °C; Other data in ng/£ except Date and pH
0 = 8.25 i/day
-------
TABLE A-16 REACTOR EFFLUENT FOR CONC. TANNINS: 22.2 HR. D.T.
CO
Time
00
Date
4/10/69
BOD5
5900
F-B005
3400
COD
44790
F-COD
32800
TS
20494
TFS
3672
TVS
16822
SS
4222
FSS
308
vss
3914
Temo.
-
pH TKN F-TKN NH3-N F-NH3-N ORG-N F-ORGN TP
4.7 78.4 59.4 15.7 13.4 62.7 45.9 20.1
F-TP
14.1
(INFLUENT)
26
43
53
92
117
141
164
189
209
00
C''.r
256
306
330
4/11/69
4/12/69
4/13/69
4/14/69
4/ 1 5/69
4/16/69
4/17/69
4/I8/6Q
4/1' o9
./20/69
L.UENT)
4/21/69
4/23/69
4/24/69
5600
4300
-
2900
2850
2800
2400
2400
2375
-
-
-
-
2475
1775
-
1100
950
1050
MuU
1250
1250
-
-
-
31800
30720
28320
28810
26885
•^6760
26000
26480
24965
34640
18080
18240
(8400
25800
23800
18920
14721
10240
920C
10080
7798
7766
24800
6680
6960
«980
-
-
-
-
201 18
19798
20132
20496
20198
-
19868
•9456
9500
-
-
-
-
3312
3352
3660
4326
4148
-
4060
3571
3504
-
-
-
-
16806
16446
16472
16170
16050
-
15806
15885
15996
1336
3100
4210
7000
7236
8128
8998
8896
8892
-
7768
7788
7785
112
750
600
300
1210
976
1396
1208
1 146
-
760
688
644
1224
2350
3610
6700
8026
7152
7602
7688
7746
-
7008
7100
7141
25
25
25
25
25
26
25.5
25
23
-
24
23
24
5.5 - -
6.2 - -
6.5 - -
6.6 -
6.7 -
6.7 - -
6.9 - -
6.8---- --
6.8 76,2 56.0 4.5 2.3 70.3 53.8 10.8
4.8 -
6.8 -
e.: - -
6.1 -
-
-
-
-
-
-
-
-
13.6
-
-
-
-
(2)
Time in hours and temperature in "C; Other data in ng/£ excent Date and t>H
Q = 6.5 t, ~ -y
-------
TABLE A-17 REACTOR EFFLUENT FOR CONC. TANNINS: 46 HR. D.T,(I)'(2)
Time
00
Date
7/31/69
B005
1875
F-B005
1650
COD
J3850
F-COD
11860
TS
7940
TFS
1152
TVS
6788
SS
740
FSS
152
VSS
588
Temp.
.
pH TKN F-TKN NH3-N F-NH3-N ORG-N F-ORGN
5.1 31.92 23.5 7.6 6.2 24.3 17.3
TP F-TP
4.8 3.9
(INFLUENT)
00
Ja.
46
116
198
258
306
8/2/69
8/5/69
8/8/69
8/ 1 f /69
8/13/69
10-00.
-
:
675
550
-
:
300
42360
11040
9160
9995
10200
II 200
8200
6840
6680
6652
5520
5820
5376
5856
6480
1212
1296
1040
1692
1698
4305
4524
4336
4164
4782
946
1052
1080
1 156
1280
164
208
248
266
226
782
844
832
890
1060
25
25
25
24
25
6.4 »
6.5 - -
6.6 - -
6.7 -
6.7 27.4 17.3 3.3 2.2 24.1 15.1
T ~
-
: ;
3.4 2.9
(I)
(2)
Time in hours and temperature in °C; Other data in mg/t except Date and
-------
1
5
Accession Number
r\ Subject Field & Group
5-D
SELECTED WATER RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
Organization
University of Virginia. Dent, of Civil Engineering.
Charlottesville, Virginia
Title
Anaerobic-Aerobic Lagoon Treatment for Vegetable Tanning Wastes
Authors)
Clinton E. Parker
16
Project Designation
FWQA Project WPD-199
21
Note
22
Citation
Date: June 1970
No. pp.: 84
No. tables: 29
No. Fig.: 23
No. Ref.: 25
No. appendix: 1
23
Descriptors (Starred First)
Biological treatment, oxidation lagoons, lignins, aerobic conditions,
anaerobic conditions.
25
Identifiers (Starred First)
Spent tannins, tannery waste waters, anaerobic-aerobic lagoon,
biological treatment, biological growth units.
27
Abstract
A field demonstration lagoon was operated at Virginia Oak Tannery, Inc.,
Luray, Virginia to evaluate the effectiveness of an anaerobic-aerobic lagoon in
treating spent vegetable tannins blended with batepool and soak waste waters. The
anaerobic-aerobic lagoon system was used to treat combined waste streams with a BOD5
concentration of approximately lOOOmg/8,. Operational phases were designed to cause
the system to go from aerobic conditions to anaerobic-aerobic. After reaching
anaerobic-aerobic conditions, doubling the BOD5 load did not result in a significant
decrease in BODs removal efficiency. Efficiency, measured in terms of soluble 6005,
at a BOD5 load of 17.3 lbs/1000 ft3/day (anaerobic-aerobic condition) was 81 percent
compared to a 92 percent efficiency for a BODs load of 4.5 lbs/1000 ft3/day
(aerobic conditions).
Although the lagoon system proved successful in removing degradable organics,
color of the waste water was not reduced by this method of treatment. Color of
spent vegetable tannins is a major problem and will dictate the most desirable
approach to treating this waste water.
A completely mixed aeration unit was used in the laboratory to study the
biological degradation of spent Vegetable tannins. It was found that approximately
60 percent of the CO) of spent vegetable tannins is not biological degradable and the
generally accepted substrate-growth interaction relationship required modification
fn faka infn arrnnnf- t-hp nnn-rTpra^ablp frar<"t"*l "f ^ntV
Abstractor
C. E. Parker
Institution
University of Virginia
WR:102 (REV. JULY 1969)
WRSIC
SEND TO: WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U.S. DEPARTMENT OF THE INTERIOR
WASHINGTON, O. C. 20240
* ttPO! 1969-359-339
------- |