EPA-660/2-74-012
May 1974
Environmental Protection Technology Series
Treatment of Cheese Processing
Wastewaters In Aerated Lagoons
Office of Research and Development
U.S. Environmental Protection Agency
Washington, D.C. 20460
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RESEARCH REPORTING SERIES
Research reports of the Office of Research and
Monitoring, Environmental Protection Agency, have
been grouped into five series. These five broad
categories were established to, facilitate further
development and application, 'of environmental
technology. Elimination of traditional grouping
was consciously planned to foster technology
transfer and a maximum interface in related
fields. The five series are:
1. Environmental Health Effects Research
2. Environmental Protection Technology
3. Ecological Research
U. Environmental Monitoring
5. Socioeconomic Environmental Studies
This report has been assigned to the ENVIRONMENTAL
PROTECTION TECHNOLOGY series. This series
describes research performed to develop and
demonstrate instrumentation, equipment and
methodology to repair or prevent environmental
degradation from point and non-point sources of
pollution. This work provides the new .or .improved
technology required for the control and treatment
of pollution sources to meet environmental quality
standards.
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EPA-660/2-74-012
May 1974
TREATMENT OF CHEESE PROCESSING WASTEWATERS
IN AERATED LAGOONS
By
Francis R. Daul
Project 12060 EKQ
Program Element 1BB037
Roap/Task 21 BAD 26
Project Officer
Max W. Cochrane
Environmental Protection Agency
National Environmental Research Center
Corvallis, Oregon 97330
Prepared for
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON, D.C. 20460
For sale by the Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402 - Prico $1.50
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EPA Review Notice
This report has been reviewed by the Environmental Protection Agency
and approved for publication. Approval does not signify that the
contents necessarily reflect the views and-policies of the Environmental
Protection Agency, nor does mention of trade names or commercial products
constitute endorsement or recommendation,, for use.
ii
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ABSTRACT
The treatment of cheese processing wastewaters in two-stage aerated
lagoons was evaluated over a one year period. Aeration was provided
by Polcon Corporation subsurface aerators (Helixors). The aeration
system provided an average standard transfer rate of 4.0 Ibs oxygen
per kilowatt-hour at 20*C and 0.0 dissolved oxygen in tap water.
Oxygen dispersion throughout the primary lagoon was normally adequate
at a power input of 8.5 horsepower per million gallons. During the
spring, however, dissolved oxygen concentrations in the primary lagoon
were zero probably due to the solubilization of benthal deposits
accumulated but not stabilized during the winter months. There was not
sufficient power, however, to prevent suspended solids deposition.
Horizontal velocity components varied from 1.0 fps within the central
portion of the lagoon to less than 0.1 fps in the sloped peripheral
zones. Over the one year period of this study, sludge accumulations
ranged from 0 to 2 inches depending upon location.
The lagoon system performance during the one year period was correlated
with temperature. The average total BOD removal was 97 percent producing
an effluent BOD concentration of 52 mg/1. During the summer months
secondary lagoon effluents were less than 20 mg/1, 70 percent of the
time. Approximately 50 percent of the total effluent BOD was soluble.
Effluent suspended solids were high, averaging 108 mg/1. Greater
than 90 percent of the suspended solids were volatile. Total and
fecal coliform reductions were normally greater than 99.9 percent
throughout the study period.
During the early spring primary lagoon dissolved oxygen concentrations
dropped to zero and remained below 0.1 mg/1 until mid July. Benthal
deposits, accumulated during the winter period, were believed to
account for the unusually high oxygen demands during this period.
Demands in excess of three times greater than predicted by the BOD
load to the lagoon were noted.
Costs for lagoon operation, maintenance, and amortization were estimated
to be $13,377 per year, $2.15 per 1000 gallons, $0.14 per Ib of BOD
applied, and $0.0033 per Ib cheese produced.
This report was submitted in fulfillment of project 12060EKQ under the
partial sponsorship of the Environmental Protection Agency.
iii
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TABLE OF CONTENTS
Section Page
I Conclusions 1
II Recommendations 3
III Introduction 4
IV Experimental System 5
V Procedures 10
VI Results and Discussion 15
a. Aerator Performance 15
b. Lagoon Performance 27
c. Costs 50
VII Acknowledgements 52
VIII References 53
IX Glossary of Terms 55
X Appendix 57
iv
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LIST OF FIGURES
Number Title Page
1 Kent Cheese Wastewater Lagoons 6
2 Aerial Photograph of Lagoon System 9
3 Sources of Cheese Plant Wastewater 11
4 Primary Lagoon Grid 16
5 Velocity Profile at one foot below surface -
1 compressor 23
6 Velocity Profile at one foot below surface -
2 compressors 24
7 Aerated Lagoon No. 1 - Solid Deposition 25
8 Influent Wastewater Characteristics 28
9 Influent Hourly Flow Variation 29
10 Primary Lagoon Performance - D.O., Temperature
and Load 30
11 Lagoon Performance - BOD 33
12 Effluent BOD Probability - Primary 35
13 Effluent BOD Probability - Final 36
14 Lagoon Performance - Suspended Solids 41
15 Effluent Suspended Solids Probability - Primary 42
16 Effluent Suspended Solids Probability - Final 43
17 Effluent BOD versus VSS - Primary Lagoon 44
18 Effluent BOD versus VSS - Secondary Lagoon 45
19 Lagoon Performance - Total Coliform 48
20 Lagoon Performance - Fecal Coliform 49
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LIST OF TABLES
Number Title Page
1 Sampling Schedule 12
2 Oxygen Uptake Rates - Primary Lagoon 17
3 Oxygen Transfer Data - Primary Lagoon 18
4 Dissolved Oxygen Concentrations - Primary Lagoon 21
5 Velocity Distribution in Primary Lagoon 22
6 Average BOD Analyses 34
7 Lagoon Loading Parameters Summary 38
8 Average Suspended Solids Analyses 40
9 Nitrogen and Phosphorus 47
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SECTION I
CONCLUSIONS
The conclusions summarized below were the result of the analysis of
data collected over a one year period from the two-stage aerated
lagoons treating cheese processing wastewaters for the Kent Cheese
Company.
Each of the two lagoons were of equal volume and provided detention
times of from 50 to 82 days each during the first year of study. The
average flow to the lagoons was approximately 17,000 gpd, ranging from
7,300 gpd to 35,500 gpd. Raw influent BOD loading averaged 285 Ibs/d
ranging from less than 15 Ib/d to 554 Ib/d resulting in a primary
lagoon loading of from 0.117 to 4.34 Ib BOD/1000 cu ft/d.
1. Aerator Performance
a. The oxygen transfer efficiency of the Polcon Corporation
Helixors in the primary lagoon was 4.0 Ibs oxygen/kw-hr
or 3.0 Ibs oxygen/hp-hr, for standard conditions (20°C,
tap water, zero dissolved oxygen) at an air flow rate of
14.8 scfm per unit.
/
b. An increase of the air flow rate by a factor of two per
unit substantially reduced the oxygen transfer efficiency.
c. The dispersion of oxygen in the primary lagoon at a power
input of 8.5 hp/MG was nearly uniform.
d. At the power input of 8.5 hp/MG, there was a tendency for
suspended solids to accumulate in the peripheral regions
where horizontal velocity components were normally less than
0.1 fps. The one year study was not long enough to evaluate
the rate of solids accumulation within the lagoon.
e. The relative oxygen transfer coefficient in the primary
lagoon was approximately 81 percent of that expected in
tap water. The oxygen saturation value in the primary
lagoon content was approximately 98 percent of that in
pure water.
2. Lagoon Performance
a. An average of 97 percent removal of BOD was achieved in
the two stage aerated lagoon system with the poorest
performance (95 percent) occurring during the winter
season. The average final effluent BOD concentration was
52 mg/1 of which 27 mg/1 was soluble. Probability distribu-
tions for treatment performance were prepared for the one
year study.
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b. Temperature had an important effect on lagoon performance.
c. Suspended solids removals in the primary lagoon were sporadic.
The overall average removal of suspended solids in the lagoon
system was 82 percent with an average concentration of
108 mg/1 in the final effluent. Over 90 percent of the
suspended solids were volatile.
d. Approximately 29Z of the volatile suspended solids in the
final effluent contributed to the effluent BOD. A similar
relationship for the primary effluent suspended solids indicated
that 46 percent of the volatile suspended solids contributed
to the BOD .
e. High oxygen uptake rates occurring in the early spring
resulted in zero D.O. concentrations in the primary lagoon.
These high uptake rates are likely due to the solubilization
of solids deposited during the winter months. The cycling
of sludge accumulation during the cold periods and active
biological stabilization of the benthal deposits during the
warmer months will result in dynamic fluctuations in oxygen
requirements and sludge deposits. Aerator sizing to account
for these fluctuations must be provided. In this study
oxygen demands in excess of three times the influent BOD
were measured during the early spring.
f. The staging of the wastewater treatment lagoons provided
considerable attenuation of the fluctuating BOD and solids
concentrations in the primary lagoon effluent.
g. Total and fecal coliform reductions exceeded 99.9 percent
in the two stage lagoon system without disinfection.
h. Nitrogen concentrations in the raw wastewater were low
with respect to carbon. The BOD to Nitrogen ratio was
100:0.7 indicating a substantial deficiency in nitrogen.
Phosphorus concentrations were high resulting in a BOD:P
ratio of 100:2.2.
i. Total phosphorus removals of 52 percent observed during the
one year study may be misleading insofar as a steady state with
respect to phosphorus transformations has probably not been
established. Total organic nitrogen removal of 47 percent were
observed. Nitrate concentrations in the final effluent were
highest during the warm summer months but were less than 0.4 mg/1
during the rest of the year.
3. Costs
The cost for wastewater treatment Including operation, maintenance,
& capital cost amortization during the first year of operation was
$2.15 per 1000 gal., $0.14 per Ib BOD applied, and $0.0033 per Ib
of cheese produced.
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SECTION II
RECOMMENDATIONS
Based on the operation of the two stage cheese processing wastewater
lagoons at Kent, Illinois, the following recommendations have been
proposed:
1. Efforts should be made to further reduce the settleable solids
input to the lagoons. These solids cause clogging problems at
the inverted siphon, interfere with flow measurement and sampling
at the primary lagoon, and result in increased BOD loading to the
primary lagoon. Insofar as solubilization of settleable solids
during the warm months has resulted in severe depressions in
dissolved oxygen concentrations in the primary lagoon, every
measure taken to reduce influent settleable solids will help to
alleviate that problem. It is suggested that a settling tank or
imhoff tank be provided ahead of the primary lagoon for this
purpose.
2. The high air pressures observed during dual compressor operation
suggests that the air headers and inlet orifices are undersized for
the increased air flow rates. Since oxygen uptake rates during the
spring and early summer exceed current oxygen transfer rates, it
is recommended that investigations be made to determine the
necessity for enlarging existing air piping or providing additional
Helixors in the primary lagoon.
3. The increased oxygen uptake rates in facultative aerated lagoons
during the spring have been reported by a number of investigators.
Further investigation should be conducted to provide a quantitative
estimate of this increased demand. Such a study would require
data collection over a number of years at the existing aerated
lagoon site.
4. Nitrogen deficiencies in the raw wastewater will normally result
in poorer performance of the biological system. It is recommended
that additional nitrogen be added as ammonia or urea to more
closely approximate the BOD to Nitrogen ratio of 100 to 5.
Comparisons in lagoon performance should be noted during this
period (at least one full year) so as to evaluate the value of
this suppllmentation.
5. The secondary lagoon effluent structure consists of only an
upturned 4 inch cast iron pipe elbow. It is recommended that this
effluent structure be modified so as to provide some baffling to
eliminate gross solids and scum entrainment.
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SECTION III
INTRODUCTION
The evaluations and findings reported herein were supported by EPA
Project No. 12060 ERQ for post-construction studies over a 12-month
period to demonstrate and evaluate the use of aerated lagoons for
the treatment of cheese wastes. Initially the objectives of the
study included the evaluation and demonstration of the effectiveness
of reverse osmosis for the reduction of BOD of cheese whey wastes.
The decision was made that the reverse osmosis method would
not be included in this study.
The authors of this report were not engaged to design or size the
system employed, select equipment utilized or were consulted regarding
the process flowsheet applicable to this wastewater treatment scheme.
The authors were retained to conduct the post construction study,
direct frequency of sampling, recommend analyses to be performed,
and evaluate and present findings of the performance of the aerated
lagoon systems for the wastes received at the treatment site under the
limitations of the existing budget.
The principal objectives of this study were to demonstrate the
performance of a staged aerated lagoon treatment plant utilizing the
Helixor* type of submerged aeration system treating cheese processing
wastes over a 12 month period of operation. Part of the evaluation
was directed to the performance of the aeration equipment employed
wherein mixing effectiveness in terms of liquid velocities produced,
uniformity of dissolved oxygen levels and sludge accumulations could
be ascertained under the conditions of operation and geometric
configuration of the lagoons employed. In addition the oxygen transfer
efficiency of the aeration system employed was evaluated under field
conditions. A major part of this study was to determine the BOD
removal rate functions for each stage of aerated lagoon treatment
noting the influence of BOD loadings, temperature and seasonal
variations in loading and performance obtained for this type of
biological treatment. The theoretical, and applied concepts of biological
treatment related to low-solids aerated lagoon systems were employed
to evaluate the treatment system. Lastly, the performance of this
type of treatment was evaluated in terms of costs associated with the
wastewater characteristics and the pounds of cheese produced.
*subsurface aeration unit manufactured by Polcon Corporation, Montreal,
Canada
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SECTION IV
EXPERIMENTAL SYSTEM
The wastewater treatment system consisted of two equal volume aerated
lagoons with a staged flowsheet wherein the effluent from Lagoon No. 1
is passed to Lagoon No. 2 before final discharge of the treated
effluent. The lagoons had earth embankments with side slopes of
3 horizontal to 1 vertical, a water depth of 12 feet at the lowest
central portion of the lagoon, and a length-width measurement of
157 feet by 123 feet at the water line for a volume of 955,000 gallons
each (Figure 1). The first lagoon was provided with thirteen 6 foot
long 18 inch diameter Helixors arranged in a pattern of 2 rows of
4 units equally spaced along the intersection of the flat bottom
and side slopes of the long dimension of the lagoon. Five additional
units were added to this lagoon between the 2 rows of four units
such that 4 of the five units were equally spaced in 2 rows between
the 1st and 2nd and 2nd and 3rd aeration units., The fifth
additional aerator was equally spaced between the third and fourth
unit of the initial eight unit arrangement (Figure 1). The second
lagoon was provided with three aeration units arranged in a triangular
pattern close to the inlet end of the lagoon in the lowest central
section of the lagoon.
A separate blower building with two rated 240 cfm Gardner Denver rotary
blowers (one standby), Model 3CDL5, provided the air supply to both
lagoons. Usual operating conditions required only one compressor to
be operative and it was assumed that the air flow was distributed
between the two aerated ponds with an estimated 80% of the airflow
supplied to Lagoon No. 1 and the remainder to Lagoon No. 2. The air
flow regulation and distribution was effected by the number and size of
air orifices providing air directly to each Helixor. The air header
piping and valving was arranged to permit the control of air to a pair
of aeration units in most instances; however, several aeration headers
supplied air to a single unit. The valving in the aeration headers
were used only for fully open or closed conditions wherein the inlet
orifices controlled the distribution of air flow.
It appeared that the recommendation of the Polcon Corporation Specifica-
tions on concrete weights for holding down the air lines and Helixors
was inadequate. An inspection of the air lines and Helixors after the
initial start up period was performed in the spring of 1970 by a scuba
diver determining the location of the air lines, Helixors, and concrete
weights in reference to the bottom of the lagoon. It was noted that
not all of the Helixors were positioned on the bottom of the lagoon.
Rather, some were 18" - 24" above the bottom. Approximately 500 pounds
of extra concrete weights were added to each individual lateral.
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KENT CHEESE WASTEWATER LAGOONS
inverted
siphon
ON
I
Sampling
Station I
INTERMITTENT STREAM
4"CI
„ I55'x 123'x 12'depth
ST* CI
• • • •
• •
Helixors •
4"CI
PRIMARY
I55'x 123' x 12' depth
Helixors
•
Sampling
Station 3
SECONDARY
I j Blower house
FIGURE |
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Six additional Hellxors were installed as per Polcon Corporation
specifications utilizing 250 pound concrete weights under each
additional Helixor . These six Helixors and lines remained in their
original positions.
The wastewater was conveyed to the treatment lagoons through about
3000 ft. of 8 inch transite pipe, passes through a 4 inch inverted
siphon to a Snyder-Teague sampling station and thence is discharged
through a 4" cast iron pipe to a point of entry to Lagoon No. 1 at
approximately mid-depth. The effluent from Lagoon No. 1 passed
through a submerged 4 inch cast iron pipe to the secondary lagoon.
The water surface elevation in both lagoons was controlled by the
placement of 4 inch cast iron riser pipe with the inlet to this
pipe, or overflow from the lagoons, at a fixed elevation to maintain
the 12 foot water depth. The effluent from the secondary lagoon
passed through another Snyder-Teague sampling station.
The sampling stations provided flow measurements and flow composited
samples for the raw waste water and treated effluents. Serious
operating difficulties resulted in the raw waste sampling station
due to the accumulation of cheese solids upstream from the flow
measuring control section. The sampling device operated on the basis
of taking a fixed volume aliquot on the discharge side of the flow
measuring weir. The sampling device was activated by the water depth
on the upstream side of the flow measuring weir; consequently, when
the upstream float was supported by accumulated solids in the absence
of influent flow, the sampling device was activated but no wastewater
aliquot could be collected for the composite sample at these times.
Thus, the composited sample for quality determination was considered
to be reliable, whereas the flow measurements required correction.
The accumulation of solids resulted in inaccurate flow measurements.
The control section was modified somewhat but proved to present difficulties
throughout the period of the study. In order to obtain reliable measure-
ments of flow, it was necessary to meter water use at the cheese processing
plant and to determine boiler feedwater requirements and the extent of
infiltration of the conveying sewerage system for reliable flow
information. Routine measurements of water pumped at the cheese
processing plant were made throughout the post construction study. The
well pumps were calibrated and clocks were employed to record total
water used. Boiler feed water was also monitored routinely. Only after
considerable effort had been exerted to correct the installed flowmeters
at the lagoon site was it determined that corrected water use data would
have to be employed for flow estimates to the lagoons. At that time
infiltration studies were conducted over two weekends, Dec. 4-5 and
Dec. 18-19, 1971, to provide an estimate of this flow contribution.
During these two periods infiltration rates of approximately 690 and 900
gal/d were measured. The pipeline conveying the cheese process waters
to the lagoon system was constructed in 1969 and employed a 12 inch
diameter Armco truss pipe with chemical band joint. The manufacturer
estimates a maximum infiltration rate with this type of construction
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of 100 gal/inch diameter/day. This would result in a value of 875 gal/day
based on 3,860 ft of 12 inch pipe. An average of 800 gal/d correction
was employed to all water use data recognizing that this value would
undoubtedly fluctuate with season. The corrections that were employed
are tabulated in Appendix C.
A sampling station was not provided between the primary and secondary
lagoons; thus, grab samples of the primary lagoon contents were taken
near the effluent discharge pipe. Because of the long detention times
experienced in each lagoon, 45-75 days, this procedure was deemed
acceptable.
An aerial photograph of the wastewater treatment system appears in
Figure 2.
8
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FIGURE 2
AERIAL PHOTOGRAPH OF LAGOON SYSTEM
-9-
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SECTION V
PROCEDURES
The treatment system handled the wastewater from a cheese making
Industry specializing principally in products of Ricotta, Parmesan,
Romano, and Mozzarella cheese. The sources of wastewater were
primarily from rinses and washes associated with the storage of milk,
transmission lines, vats and pasteurizer with a limited amount of
wastes of domestic origin. The by-product whey was collected and
transported to another site for recovery and only whey wastes associated
with washing and rinsing were discharged to this treatment system.
The sources of wastewater treated by the aerated lagoon system are
shown in Figure 3. The quantity or quality of rinsewater from each
operation was not determined in this study, but rather the collective
properties of the total discharge to the lagoon system were determined.
Certain measurements were made daily for operation of the treatment
works such as D.O., pH, alkalinity, settleable solids, temperature,
and flow quantity whereas more detailed analyses for evaluating the
performance of the treatment system were obtained for raw wastewater
influent, primary lagoon contents near effluent structure, and secondary
lagoon effluent on an eight day sampling frequency. This permitted
each day of the weekly operation to be sampled every 56 days through-
out the one year study commencing on January 14, 1971. A sampling
schedule is outlined in Table 1. All the analyses indicated in
Table 1 were performed by Corning Laboratories, Inc., Cedar Falls,
Iowa. After sample collection, appropriate volumes of well mixed
sample were placed in separate sample bottles for coliform determination,
for nitrogen and phosphorus analysis, and for BOD and solids analysis.
Nitrogen and phosphorus samples were preserved with mercuric chlorides
as prescribed by Methods of Chemical Analyses (1). Samples were shipped
immediately after collection to the Corning Laboratories, Inc. where
analyses were initiated no more than 10 to 12 hours after collection.
The lagoon system had been in operation approximately eight months
prior to initiating the sampling program; thus, the data presented
does not represent start-up conditions, but there were indications
that the performance did not reach steady state in all respects
particularly regarding seasonal variations.
10
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FIGURE 3
SOURCES OF CHEESE PLANT WASTEWATER
Cheese
R-W-R
R-W-R
R-W-R
R-W-R
R-W-R
R-W-R
R-W-R
T
3-tanks
2- 37,000 over the road tankers
// 2" S.S. CIP Lines and pump
2 - 6,000 Gallon __ . .
1 - 10,000 Gallon Storage tanks
/ / 2" S.S. CIP Lines and pump
/ / Pasteurizer - Clarifier pump
/ / 2" S.S. CIP Lines
/~~/ 5 - 12,000 Pound vats
3 - 6,000 Pound vats
r
RWR / / Ricotta, Romano
Mozzarella, Parmesan
I
RWR / / Hoops-Press
RWR / / Whey collection tanks
RWR / / Cheese drainage tables
RWR / / Packaging tables
RWR / / Plant floor
RWR / / Cooler Floor
RWR / / 2" S.S. CIP trans lines
HW / / Separator
HW // 2" S.S. lines
RWR / / Storage Tanks
& HW T~
RWR / / 2" S.S. CIP lines
/ / 0/R tankers to whey
processing plant
RWR = Rinse - Wash - Rinse
HW - Hand Wash
CIP - Cleaned - in - Place
0/R - Over the road tanker
Water Supply » 1/2" diameter hose
60 psi Pressure
Hot Water « Supply provided by steam/water
mixers - air flow 25 GPM
/ / Domestic Waste
| 20 employees
/ / Company Residents
11
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TABLE 1
SAMPLING SCHEDULE*
Sampling
Frequency Parameter or Determination
8 days BOD 5 day 20° C Total
8 days BOD 5 day 20° Soluble**
8 days Total Suspended Solids
8 days Total Volatile Suspended Solids
8 days Total Coliforms
8 days Fecal Coliforms
30 days Total Phosphorus
30 days Total Kjeldahl Nitrogen
30 days Nitrate Nitrogen
Sampling Points
Raw
X
X
X
X
X
X
X
X
X
Primary
Effluent
X
X
X
X
Secondary
Effluent
X
X
X
X
X
X
X
X
X
*Analyses performed according to Methods of Chemical Analysis (1)
**Analysis performed on sample filtrates (Whatman #42 filter paper)
12
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Additional operating and performance evaluations were performed
during the experimental period including the following items:
1. D.O. measurements with respect to horizontal and vertical
control in the primary lagoon,
2. measurements of velocity in the horizontal plane at various
locations and depths within the primary lagoon,
3. measurement of oxygen uptake of the treatment lagoon contents,
4. determination of the oxygen transfer coefficients of a and B
to enable the evaluation of the aeration system employed.
Various other operating conditions and observations were recorded on
a routine basis to assist in the overall evaluation of the performance
of this treatment system (Appendix C).
Special measurement techniques employed for the purpose of evaluating
the aeration system employed a grid established in the primary lagoon
above the water surface to provide a measuring base for horizontal
control. At the time oxygen transfer was evaluated, it was necessary
to have a measureable D.O. in the lagoon and evidence that the D.O.
was maintained at a uniform or steady state condition. The oxygen
uptake or demand of the lagoon contents were determined by taking a
number of representative samples of the mixture under aeration and
placing them in bottles capable of excluding further oxygen transfer
from the atmosphere and wherein the decrease in D.O. concentration
was measured with respect to time with a Yellow Springs Instrument
D.O. probe. In order to evaluate the influence of photosynthetic
plankton on the oxygen transfer in the lagoon, oxygen uptake measure-
ments were made both on rates observed under light and dark conditions.
There was no discernible difference in the rates observed which
indicated that oxygen transfer or supply from this source was
negligible during the test periods.
Aerator efficiency was determined on the basis of line to water for
the complete aeration system wherein power input was metered in each
instance for amperage and voltage drawn. The results were presented
in terms of pounds oxygen transferred per kw-hr. Thus, the reported
efficiency included oxygen transferred from the atmosphere as well as
oxygen transferred by virtue of the aeration system employed.
Aeration efficiencies were corrected to standard conditions of zero
dissolved oxygen and 20° C with appropriate corrections for a and 3 .
Representative samples of the lagoon contents were tested in Madison
laboratories in a simulated diffused air system to compare transfer
capacities (a) for the waste mixture against tap water for two
replicate samples. The value a was obtained as an average of the ratio
of the transfer rates in the wastewater and tap water. The value 3 was
13
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determined on the basis of the highest D.O. obtained in the aerated
lagoon contents for a given temperature, checked by the Winkler D.O.
method, against the D.O. at saturation for tap water at the same
temperature.
The velocity profiles in the aerated lagoon were made with the use of
a Gurley Current Meter which was fixed in the horizontal plane by
attachment to a vertical rod. The current meter was rotated in the
horizontal plane at a predetermined depth and the maximum velocity
and direction were noted to obtain a vectorial representation of the
water movement in the lagoon. The velocity was observed in four
directions parallel to the sides of the lagoon in the central portion
of the aerated lagoon where a single maximum velocity component was
not observed due to the highly undirected flow patterns evident within
the area bounded by the aeration devices. An attempt was made to
measure the vertical velocity component immediately above the discharge
of the aeration device but the variation in fluid density as a result
of high levels of air entrainment caused on the measurements to be
somewhat erratic. Measurements were made one foot below the surface,
mid-depth and one foot from the bottom.
14
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SECTION VI
RESULTS AND DISCUSSION
Aerator Performance
The performance of the Polcon Corporation subsurface aerators (Helixors)
was evaluated over the one year period in the primary lagoon only.
As indicated earlier, the lagoon was sampled at a number of points on
a grid (Figure 4) at selected depths to determine the oxygen uptake
rates, dissolved oxygen concentration, and temperature. Tests were
repeated five times over the grant period in order to evaluate perform-
ance under different waste loading and environmental conditions.
Oxygen Uptake Rates - The average oxygen uptake rates recorded in the
primary lagoon over the one year study period are presented in Table 2.
The values reported represent the average uptake measured at a number
of selected points within the lagoon (see Appendix A). Normally, the
uptake rates measured on any given day were within 10 percent of each other.
The uptake rates reported were not converted to specific uptake rates
(mg O-XgVSS/day) since the volatile solids fraction measured in this
lagoon was not well correlated with the active biomass during the
study period. Large amounts of suspended volatile matter non-biological
in origin associated with the wastewater contributed significantly to
the total volatile fraction measured. The influence of algal cells on
the oxygen uptake rates in the primary lagoon were negligible as
measured by both dark and light bottle uptake rates.
Examination of the uptake rates presented in Table 2 suggest that the
biological activity in the primary lagoon was comparable to other aerated
lagoon systems (2). The analysis obtained in May, 1971, occurred during
the anaerobic period and indicates that the lagoon was extremely
active. As discussed later, this high rate of oxygen consumption was
believed to be due to the rapid solubilization of organic matter and
synthesized cells which had settled in the lagoon and had subsequently
been stored over the cold winter months.
Oxygen Transfer Capacity - The values of the oxygen transfer capacity
of the primary lagoon contents, as measured by the ratio of the oxygen
transfer coefficients in the waste to that in tap water, are reported in
Table 3 as alpha. These values represent the average values obtained from
several points within the lagoon. Alpha appeared to fluctuate seasonally
being highest during the summer months. There was not sufficient data
to establish any reliable correlations between alpha and lagoon BOD
solids or temperature, but it is reasonable to assume that changes in
the metabolic activity within the lagoon would result in changes in the
oxygen transfer relationships.
15
-------
INLET
n
N
~U
t
"u
^
"»
J
•)
•>
•
i
f
htn' m.
V
X
c_ ^
PRIMARY LAGOON GRID
*f>> . ^ •.-• - . ..' -
1
LAG
2
3
^.
'\ uj
4
DON NO. 1
5
6
. —
FIGURE 4
•"
7
8
9
— -* —
i 1 11 r
« 2| r
• •
10
II
12
~ —
i II1 r
JL^
13
14
15
^ — — ^
1- static
-*- OUTLET
m numbers
-------
TABLE 2
OXYGEN UPTAKE RATES
PRIMARY LAGOON
(Average Values)
DATE
11-19-70
5-23-71
7-21-71
8-26-71
10-7-71
TEMP.
•c
6.3
17.0
24.0
23.5
16.5
D.O.
mg/1
2.8(43)
0.0(43)
4.4(39)
4.4(27)
2.3(41)
UPTAKE RATE
mg/l/hr Ib/hr
2.1 (5) 16.7
5.6 (5) 44.6
1.2 (4) 9.55
0.8 (4) 6.4
1.5 (3) 12.0
( ) - Number of samples analyzed (see Appendix A & Table 4)
17
-------
TABLE 3
OXYGEN TRANSFER DATA
PRIMARY LAGOON
DATE
11-19-70
5-23-71
7-21-71
8-26-71
10-7-71
TEMP.
°C
6.3
17.0
24.0
23.5
16.5
D.O.
mg/1
2.8
0.0
4.4
4.4
2.3
a
0.75
0.88
0.90
0.94
0.70
3
0.96
0.96
0.98
0.98
0.98
STD.
Ib/kw-hr
5.25
3.18
0.98
3.45
TRANSFER
Ib/hp-hr
3.91
2.47
0.73
2.59
Overall Average
0.81
0.97
3.96
2.98
1 - 20*C, D.O. « 0.0, Tap water - see Appendix B
2 - Excluding 8-26-71 data for reason on page 19.
18
-------
The solubility of oxygen was only slightly affected by the wastewater
characteristics within the primary lagoon. Normally values of beta
in long detention-type processes such as the one studied here approach
1.0.
Aeration Efficiency - The aeration efficiency of the Polcon Corporation
Helixors are presented in Table 3 for five test days. The
aeration efficiencies were computed by employing the measured oxygen
uptake rates, dissolved oxygen concentration, alpha, beta, and temperature.
Power was metered during the test period. The value of the aeration
efficiency was corrected to standard conditions of 20°C, tap water (alpha
and beta equal 1.0), and a dissolved oxygen concentration of 0.0 mg/1.
The approximate saturation value for oxygen for the 12 foot lagoon depth
was estimated by using the relationship given by Oldshue(3):
where Cg is the oxygen saturation value corresponding to the average
partial pressure of oxygen in the gas stream entering and leaving the
aerator, C is the oxygen saturation value of water at atmospheric
pressure, P^ is the absolute pressure in psi at depth, d and Ot is the
percent concentration of oxygen in the air leaving the lagoon. A
sample calculation appears in Appendix B.
The overall aeration efficiencies in the primary lagoon were estimated
by assuming that 80% of the air provided by the blower was directed to
the primary lagoon, since 13 of the 16 helixors were located in the
primary lagoon. During August 26, 1971, test, both blowers were in
operation resulting in a doubling of the power input to the aerators.
Yet the actual measureable oxygen transfer rate was not appreciably
higher than for other test periods. It has been well documented in the
literature (4,5) that aeration efficiency decreases with increased air
flow rates and this analysis tends to verify that fact. In addition,
however, it was determined that, during the operation of both compressors,
the line pressures increased very significantly requiring the bleeding
of air from one of the headers. This was practiced by the use of a
"blow-off" or "by-pass" Helixor in the secondary lagoon. Thus, the
poor transfer rates for August 26 were not included in the overall average
for aeration efficiency.
The measured transfer efficiencies of the Helixor units were lower than
the expected performance claimed by the manufacturer (6). Whether this
was due to undersizing of the air headers, the geometry of the Helixor-basin
configuration, or was, in fact, the actual field expectation for these
units has not been determined but it suggests that caution must be
exercised in sizing aerators for lagoon systems. An additional factor to
be considered was the oxygen uptake occurring in the benthai deposit. No
effort was made to ascertain what this contribution was, but significant
uptake from this source would substantially increase the aeration efficiencies
reported herein.
19
-------
Oxygen Dispersion - An important function of aeration devices in
biological processes is the dispersion of oxygen throughout the basin
contents. Normally, rule of thumb criteria recommend that at least
6 to 10 horsepower per million gallons (hp/MG) be supplied to insure
adequate oxygen dispersion (7). For the primary lagoon, 8.5 hp/MG were
provided during the single blower operation. The results of dissolved
oxygen analyses in the primary lagoon for the five field surveys are
presented in Table 4. Examination of this data indicates that oxygen
was well dispersed throughout the primary lagoon.
Mixing and Solids Suspension - The D.O. parameter is indicative of the
dispersion of substances in the dissolved state such as soluble B.O.D.
However, the distribution of particulate matter such as biological floe
would be a function of the velocity distribution and the velocities necessary
to keep the particulate matter in suspension. Normally in aeration tanks
in wastewater treatment, velocities along the bottoms of these units would
range from 1.0 to 2.0 fps depending upon the geometry of the aeration system
employed. Velocity measurements within the lagoon can serve only to
show flow regimes developed within the lagoon with the given aeration
equipment for the placement arrangements employed and the geometry of
the lagoon. Effectiveness of the system in terms of keeping particulate
solids in suspension can be evaluated in a qualitative way by determining
the location and extent of solids deposition on bottom surfaces of the
lagoon.
The maximum velocities observed in the primary lagoon at the various depths
are reported in Table 5 for one blower, 192 cfm, and two blowers, 384 cfm.
These airflow rates correspond to 2.3 cfm per lineal foot and 4.6 cfm
per lineal foot respectively along the longest bottom dimension of the
lagoon. The vectorial representations of the resulting surface velocities
are shown in Figures 5 and 6 for the single and dual blower operation.
An estimated surface wind of less than 5 mph as indicated on the diagram may
have influenced the resulting velocity measurements. Because of the upward
vertical velocity components in the immediate vicinity of the inlet and
outlet of the Helixors and the necessary compensating downward movement of
water between adjacent aeration units, no definitive flow pattern is
discernible. However, in zones peripheral to the aeration section, where
the bottom of the lagoon is sloped to intersect the water surface, horizontal
velocities were measured near the water surface indicating a general
circulation pattern towards the periphery of the aerated lagoon with
velocities ranging from less than 0.1 to 0.8 fps. Likewise, to compensate
for the outward movement of water toward the periphery of the lagoon
near the surface, water movement must be in the opposite direction near
the bottom of the lagoon, the measurements and magnitude of which was
less discernible. Thus, a circulatory pattern of flow developed, in
the outer prism shaped sections similar to that which is depicted in
Figure 7.
20
-------
Is}
TABLE 4
DISSOLVED OXYGEN CONCENTRATIONS*
PRIMARY LAGOON
Date
11/19/70
1 blower
5/14/71
1 blower
7/21/71
1 blower
8/26/71
2 blowers
10/7/71
1 blower
1
2.7
2.7
—
0.1
0.1
— -
4.4
4.3
—
4.1
3.9
—
2.2
2.0
2.1
2
2.9
2.8
2.8
0.1
0.1
0.1
4.4
4.2
4.2
4.3
4.6
3.0
2.2
2.1
2.0
3
2.9
2.9
2.7
0
0
0
4.4
4.3
__
4.7
—
—
2.7
2.7
—
4
2.7
2.7
2.7
0
0
0
4.3
4.3
3.0
4.3
4.3
4.4
2.3
2.4
2.3
5
3.1
3.0
3.0
0.3
0.2
0.2
4.3
4.3
4.3
4.4
4.4
4.5
2.3
2.3
2.3
Station Number
678
2.9
2.9
2.9
0.1
0.1
0
4.4
4.3
4.2
4.7
4.7
4.7
2.4
2.4
2.4
3.0
2.9
2.9
0
0
0
4.6
4.7
4.7
__
—
—
2.3
2.3
2.3
2.8
2.8
2.8
0.3
0.2
0.1
. 4.7
4.7
4.5
4.7
4.6
4.6
2.4
2.2
2.2
9
2.8
2.8
2.7
0.1
0.1
0
4.2
4.2
4.2
__
—
—
2.3
2.3
2.3
10
2.8
2.8
2.8
0.1
0.1
—
4.8
4.7
4.7
^^>
—
—
2.3
2.3
2.3
11
2.8
2.7
2.7
0.3
0.3
0.3
4.4
4.4
4.3
4.4
4.4
4.5
2.1
2.1
2.1
12
2.7
2.7
2.7
0
0
0
4.3
4.2
— —
__
—.
—
2.3
2.3
2.3
13
2.8
2.7
2.6
0
0
0
4.9
4.8
—
4.4
4.4
__
2.4
2.3
2.3
14
2.7
2.7
2.7
0.1
0.1
0.1
4.7
4.7
—
4.5
4.5
4.5
3.0
2.6
2.5
15
2.6
2.5
--
0.1
0
0
4.4
4.4
— —
4.5
—
—
_-
—
—
*D.O. values In mg/1 at 1 ft
3 ft
5 ft below water surface
-------
TABLE 5
VELOCITY DISTRIBUTIONS IN PRIMARY LAGOON
November 7, 1971
One Compressor
Two Compressors
Station
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
Surface*
0.1
0.1-0.2
0.0-0.1
0.4
0.2-0.5
0.1
0.2
0.5-0.8
0.1
0.0
0.3
0.1
0.2
0.2
0.0
Mid Depth
0.0
0.0
0.0-0.1
0.1
0.2-0.3
0.0
0.0
0.2
0.0
0.2
0.2
0.0
0.0
0.1
0.0
Bottom
0.0
0.0
0.0
0.0
0.1
0.0
0.0
0.2
0.1
0.0
0.1
0.1
0.0
0.0
0.0
Surfacl^
0.0-0/2
0.1-0.2
0.2-.0.3
0.6-0.8
0.2-0.6
0.0-0.2
0.4-0.5
0.8
0.2
0.4-0.5
0.3
0.1
0.2
0.2
0.1
Mid Depth
0.0-0.2
0.0-0.1
0.2-0.3
0.3-0.4
0.2-0.3
0.0-0.2
0.0-0.2
0.2
0.1
0.0-0.1
0.2
0.1
0.0
0.0
0.0
Bottom**
0.0
0.1-0.2
0.0-0.1
0.1=0.2
0.0-0.2
0.0-0.1
0.0-0.1
0.2
0.1
0.0
0.1-0.2
0.0
0.0
0.1
0.0
All values of velocity in ft/sec.
* One foot below
**0ne foot above
22
-------
to
to
VELOCITY PROFILE AT ONE FOOT BELOW SURFACE
one compressor
INLET
^^
0.lfps=l/8" •
p«— •».«—
\
O.I
0.1-0.2
X
?
0.0-0.1
<—————-
»f vector
•
0.4
0.4
0.5
. — -
0.5
0.2
O.I
—
FIGURE 5
• n..
0.2
\
V0.l
• ,
0,0
^0.3
>^
0.5-0.8
s.,
— \
0.2
*0.2
0.0
' '
Date Nov
-*— OUTLET
r. 7, 1971
-------
INLET
^^
^4f§p
$$P&*
is*
O.I fps = I/
\
0.0-0.2
0.1-0.2
0.1-O.Z X
0.1-0.2
0.2-0.3
<~~~ • • ' —
8" of vectc
VELOCITY
tv
0.6-0.8
0.5
0.4
•r
PROFILE AT 0
to compressors
g^^^1^ ^mni^^^—t~~^^*m
0.6
0.2
0.0-0.2
- '
FIGURE 6
ME Fi
I 1
- «.
0.4-0.5
/
\
s«
DOT BEL
— »
0.4-0.5
/
[
^0.3
^0.8
O.I
.OW SL
••"^^N
02
/
*0.2
k
O.I
— — -— - •
Date
IRFACE
-»~ OUTLET
Nov. 7, 1971
-------
INLET
AERATED LAGOON NO. I - SOLIDS DEPOSITION
Ol
O
Q
o o o
0 ° OUTLET
Q G>
•*•»*• —
o
O O O
Q Q Q
WATER MOVEMENT PROFILE
TTTTTTT
FIGURE 7
NOVEMBER 8, 1971
O AERATOR
SOLIDS ACCUMULATION
Q- i"
Q-
-------
Perhaps a more meaningful observation that was made to ascertain the
ability of the aeration system to keep solids in suspension was to
estimate the accumulation of solids on the lagoon bottom. Utilizing
a D.O. probe* a crude estimate of the sludge accumulation was made by
lowering the probe to an elevation where the 0.0. decreased to zero.
This elevation was compared with that where a weight would come to rest,
a point which was presumed to be at the bottom of the lagoon. The
results were plotted qualitatively by the graphical representations
for deposit as shown in Figure 7. It is noted that the greatest
accumulation reported on November 8, 1971, almost two years after lagoon
operation, occurred in the non-aerated zones of the lagoon corresponding
to the tapered prism sections representing sloped sections of the lagoon
nearest the intersection of the two adjacent sloped bottom sections. The
least discernible deposits of solids occurred in the central aeration
zone which may be due either to the higher levels of fluid turbulence
to keep the solids in suspension or due to the greater diffusion of
oxygen In the lighter accumulations of sludge at these points. For
longer periods of treatment plant operation, it is likely that greater
accumulations will occur. However, at the time the determinations were
made, it would appear that the accumulation of solids would not present
a serious problem for this system.
Aeration System Operation - Maintenance of low ambient temperature in
the compressor building during the months of July and August required
the installation of a fan to maintain an equilibrium temperature between
the inside and the outside of the building. During the extreme cold
months of the winter, when the temperature of the water drops to
approximately 4 degrees Centigrade, the brake horsepower of the fifteen
horsepower motor climbed to 18-19 brake horsepower. This problem was
corrected by utilizing the six extra Helixors that were initially installed
to discharge the air whenever two compressors were required to be in
operation in order to maintain residual dissolved oxygen in the springtime.
This problem of increased brake power could also be handled by replacing
the fifteen horsepower motors with twenty horsepower motors in this
particular situation.
The recommendations of Polcon Corporation for stainless steel clamps with
the ends bent over has proven to be inadequate. Since January, 1971, three
Helixors have floated to the top because of the stainless steel clamp
vibrating loose. A type of bolt-nut clamp with the threads damaged after
the connections have been made would prevent the nuts from vibrating
off the bolts.
26
-------
Lagoon Performance
The performance of the staged lagoon system was interpreted in terms
of several measured parameters: BOD (total and soluble), suspended
solids, nitrogen, phosphorus, colifonus (total and fecal). The
results reported herein are subdivided in accordance with these
parameters. Tabulated results of lagoon performance appear in Appendix C.
The loading to the lagoon system is summarized for the one year study
in Figure 8. It is apparent from this figure that flow and organic
load to the lagoon is quite variable over the one year period. Hourly
flows over a typical 24 hour period are presented in Figure 9 for two
days, January 24 and 25, 1972. Analysis of this data indicates that
the ratio of maximum to average flow for the day was 1.9. The average
flow rate over the 12 month study was approximately 17,000 gallons per
day including Sundays.
The apparent cyclic variation in BOD and solids loading to the lagoons
(Figure 8) are due to the sampling schedule employed. As noted in Table 1,
samples were collected every 8 days in order to obtain data over the
entire week. The flows and pollutant loads noted, therefore, represent
weekly cycles. Therefore, a trend line was difficult to describe.
Average BOD loading over the 12 month study was 285 Ib/day and suspended
solids loading was 85 Ib/day. An average of 13,000 Ib cheese were
produced per day (excluding Sunday) requiring approximately 1.3 gallons
of water per Ib of cheese and resulting in 22 Ibs of BOD and 6.5 Ib
of suspended solids per 1000 Ib of cheese produced.
Biochemical Oxygen Demand - The performance of the lagoon system in
removing biodegradable organic matter was measured by the five day BOD
determination. Both total and filtered analyses were performed in
order to reflect the influence of the pond system on actual biochemical
stabilization as compared with physical separation of particulate
organic matter. No long-term ultimate BOD analyses were performed nor
were COD or Total Carbon Analyses; thus, the interpretation of the data
in terms of mass balances of oxygen demanding materials through the
system was limited.
Although the BOD load to the lagoons varied widely over the one year
period of study, the most apparent influence on lagoon performance
was temperature. In Figure 10, BOD load and temperature are plotted
along with the primary lagoon dissolved oxygen (D.O.) concentrations.
It is immediately apparent that D.O. rapidly disappeared in the spring
along with rising temperatures. In fact, D.O. reached 0.0 on April 10
and did not reappear until July 19. During the remainder of July, six
of thirteen days the lagoon was devoid of oxygen. Also, 11 of 31 days
in August, 15 of 30 days in September, 19 of 31 days in October,
6 of 30 days in November, and 2 of 31 days in December D.O. values
were less than 1.0 mg/1.
27
-------
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971 - 1972
00
Lb 20
CHEESE
PRODUCED|0
x IO"3
0
50
40
FLOW
gpd 30
Xl° 20
10
500
BOD
Lb/doy
TSS
300
100
0
200
•• * * * f*
" V^ •„- • V^V.V^V^Vnr v%/^
v -wywc v^.v */•**.....•••.".•••• •%***.«.*•:•;••• -•-• *
.. -..••• •' ' • ' "•-••..•• •*•••••./
INFLUENT CHARACTERISTICS
monthly average
- o
o o o
o o
o ° o
o o o
o
o
o
Lb/day ,00
oo ^ o
0°°
O 00
°o o°
ooo
°o0
o0o
o o
O t
O I
c
JAN FEB MAR APR MAY JUNE JULY AUG SEPT OCT NOV DEC JAN
FIGURE 8
-------
CHEESE PROCESS WASTEWATER FLOWS
JAN
1972
20
INFLUENT HOURLY FLOW
VARIATION
15
co
o
o
x
O
Ul
1/24/72
mox hr
1/25/72
max hr
ave hr
= 1.87
MID
AM
12
TIME OF DAY
MID
PM
FIGURE 9
29
-------
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971 - 1972
u>
o
BOD
LOAD
1 he
LD8.
day
TEMR
°C
D.O.
mg/l
ouvs
500
*f\f\f
400
300
200
100
20
10
6
4
n
PRIMARY •
LAGOON PERFORMANCE . •
• • • •
• */\ • * • *
°>^^ ^/* \ * s~ — «^^^°^^ ^*" — V • •
• \ ^^ ' ^ "" £ * ^^
• jr • imjnfhly average **0
•
• •
o
o ° °o 00° weekly
o o° °° °°°oo0 o averages
o o o
o o
°0°rtrt00o0 °°oo
4
• •
' • t daily values
• »" *'•.."."'• •
* • t • ••«••*•• « „•••«••
*• • • • . • * * . • • • .• •
. •••. ' - • •
w • • ** • ** • •• ••* •*•••
• * »• • •
•
• • « •* * •••*»•••
• * • • •
"" * **• • » • • t •».-
•• •*«• » • •
• * * •• «** • * * •
1 1 1 • 1 1 1 1.' •' 1 •-•••*•• t •••.."•. 1 -." 1 'J • /
FIGURE 10
-------
It might be assumed that this increased demand for oxygen during the
spring was due to the increased biological activities brought about
by the warmer temperatures. However, examination of the BOD load just
preceding this period would indicate that the demands measured during
this period could not be accounted for by the applied load.
For example, if one assumes that the ultimate oxygen demand is 1.47 times
the 5 day value (deoxygenation constant, k. = O.I/day), the oxygen
demand for a 5 day BOD load of 285 Ib/day would be 419 Ib/day. The
oxygen demand measured in May, during the oxygen deficient period, was
1165 Ibs/day, 746 Ibs in excess of that predicted above. Furthermore,
if one computes the oxygen supplied during this period based on a standard
transfer rate of 4.0 Ibs 02 per Kw hr., approximately 600 Ibs of oxygen
are transferred per day by this system at 20°C and zero D.O.
Therefore, it is reasonable to assume that significant amounts of
biodegradable organics are being solubilized from the benthal deposits.
During the cold months, anaerobic decomposition of the settled organic
matter slows down resulting in accumulations of this material. As
the temperature increases, biological activity also increases and
solubilization of the benthal deposits begin to appreciably contribute
to the organic load of the lagoon. This solubilization increases to
a maximum value and then remains constant over the summer months. It
may be assumed that this cyclic effect will continue, stabilizing the
settled organic solids during the warmer periods and*continue to
produce both gas and soluble organic compounds.
The high oxygen demands occurring during the spring in waste stabiliza-
tion lagoons has been attributed to benthal digestion by a number of
investigators. Marais and Capri (8) have attempted to estimate
the benthal demand in aerated lagoons. In a dynamic simulation of
data collected for domestic wastewater lagoons, they showed that the
rate of benthal decomposition was highly temperature dependent with
an estimated value of the temperature coefficient theta of 1.35. They
found that approximately 40 percent of the settled organic matter was
resolubilized for the domestic waste.
The one year period of this study was insufficient to adequately quantify
the benthal contribution to the lagoon organic load. The study period
was too brief to evaluate the effectiveness of the anaerobic digestion
in reducing accumulated sludge deposits. Steady state (or rather a
quasi-steady state) may occur only after a number of years. Yet, based
on this and other studies (2,8,9), it is reasonable to report that oxygen
demands during the spring may exceed three times the applied BOD load.
Dissolved oxygen concentrations in the secondary lagoon were normally
greater than 2.0 mg/1 even during the April-July period of anaerobiosis
in the primary lagoon. Only during two weeks in late June did dissolved
oxygen levels drop below 2.0 -mg/1 and there was never a time when a
value of zero D.O. was recorded. Dissolved oxygen concentrations
were highest during the winter months, decreasing as oxygen uptakes
increased in the spring and summer months.
31
-------
The results of BOD analyses in the two lagoons appear in Figure 11 and
average BOD-analyses by quarter are presented in Table 6. The removal
of BOD was strongly correlated with lagoon temperatures and concomitant
biological activity reaching a maximum late in the summer and early fall.
Average BOD removal through both lagoons was 97.3 percent with the poorest
performance occurring in the winter quarter with a value of 94.5 percent.
During the 4 1/2 month period, July 1 through November 15, the effluent
soluble BOD did not exceed 30 mg/1 and was*20 mg/1 70 percent of the time.
Examination of the probability plots for total and soluble BOD in the
primary and secondary lagoon effluents (Figures 12 and 13) indicates
that the distributions of effluent BOD are skewed, being bounded at the
lower end by the presence of organic matter relatively resistant to
biological degradation. Considerable scatter of effluent BOD is demonstrated
above the 50 percentile suggesting that, even with very long detention
times, the reliability of the system to produce effluent BOD concentration
less than 25 mg/1 at all times is very improbable.
It is of interest to note that the soluble fraction of the effluent BOD
represents on an average 50 percent of the total, with the highest values
occurring during the spring and summer quarters.
«
Lagoon Modelling for BOD Removal - The mathematical modelling of biological
wastewater treatment systems has become a popular method for compacting
design data into a simple and useable form. Unfortunately, the biochemical,
chemical, and physical reactions taking place in biological waste treatment
processes are only poorly understood and the techniques of mathematical
modelling normally become curve fitting processes (10). Most popular
models currently in use for biological systems include the Monod
equation (11, 12, 13, 14) and first order reaction models (15, 16).
Defining the appropriate model parameters for these mathematical models
requires careful experimental design in order to examine the model over
a rather broad range of the independent variables. In addition, the
modeler must be aware of all independent variables which will influence
the outcome of the reaction.
The study conducted and reported herein was not designed to provide this
kind of Information. The lagoons were designed to accept the flow and
pollutant load that occurred and little or no control was available.
Furthermore, funds were inadequate to make meaningful measurements of
both dependent and independent variables. Therefore, it would seem
inappropriate to try to develop any type of sophisticated model for this
system. Furthermore, until one is able to define with considerable
confidence, the independent variables which will provide a model with
sufficient rigor to extrapolate process performance from one system to
another, there is considerable hazard in presenting any type of mathematical
expression which might be used in an effort to describe another system.
Thus, by use of dynamic modelling, one may employ the data appearing in
Appendix C to write a model for the experimental system described herein.
Yet, use of this model to describe performance of any other similar
32
-------
CHEESE PROCESS WASTE WATER LAGOONS
LO
JAN 1971 - 1972
o
o
CD
3500
3000
2500
2000
1500
1000
500
<
300
200
100
LAGOON PERFORMANCE
row wostewater
.•
DO = 0.0 mg/l
Primary Lagoon
o o
2 o°
o o«o
u> to in
Ji
o o
o o
x o
*
primary lagoon effluent
«".•,". ". * . ° 0°0° o o
X x x *
X X
secondary lagoon effluent
X * * * t
xx. .xxx ixx5
X X
-------
w
TABLE 6
AVERAGE BOD ANALYSES
Quarter
1971
Jan-Mar
Apr-June
July- Sept.
Oct-Dec.
Avg.
Influent
Total
1940
2040
1530
2100
1910
Soluble
1060
1110
870
1420
1140
Primary Effluent
Total
224
204
122
274
209
Soluble
49
45
37
42
43
% R.*
(Total)
88.5
90.0
92.0
87.0
89.0
Secondary Effluent
Total
106
61
21
31
52
Soluble
51
32
13
14
27
% Overall R.*
(Total)
94.5
97.0
98.5
98.5
97.3
All values of BOD in mg/1
*BOD Removal based on total BOD
-------
CHEESE PROCESS WASTEWATER LAGOONS
U)
Ln ^
O
E
I
Q
o
CD
600
500
400
300
200
JAN 1971-1972
PRIMARY POND EFFLUENT
100
* *
J 1 I I I I
±
_L
O.I
0.5 I 2
10
20 30 40 50 60 70 80 90 95 98
PERCENT TIME EQUAL TO OR LESS THAN VALUE
FIGURE 12
-------
160
CHEESE PROtESS WASTEWATER LAGOONS
JAN 1971-1972.
FINAL EFFLUENT
140
120
100
u>
I
O
O
m
80
60
* * * » *
40
X**
20-
X XVMXXX
»n *********
J I
I I
O.I 0.5 I 2 5 10 20 30 40 50 60 70 80 90
PERCENT TIME EQUAL TO OR LESS THAN VALUE
FIGURE 13
95
98
-------
system may be inappropriate unless the significant independent variables
have been described.
The design parameters most often used for aerated lagoon design include
BOD loading per unit volume, detention time, and BOD removal rate
(usually expressed as a zero or first order kinetic parameter). For reasons
stated above, a simplistic analysis of design parameters is provided.
Table 7 summarizes by quarter the three design parameters most often
associated with aerated lagoons.
Examination of Tables 6 and 7 suggests that BOD loadings, although increasing
slightly during the summer months, are relatively uniform based on
quarterly analysis. Day to day variations are of little importance in
overall lagoon performance owing to the long detention periods. Note
the significant. increase in flow during the third quarter (July-Sept)
resulting in a reduction in detention time of approximately 15 percent
from the average.
The estimation of the first-order removal rate constant is of academic
interest only. The assumption of completely-stirred conditions is probably
reasonable for the soluble BOD fraction based on oxygen dispersion measure-
ments, but total BOD undoubtedly is greatly influenced by the mixing
patterns in the lagoon. No measurements were made to ascertain quantitatively
the mixing properties of the lagoon system. A first-order reaction is also
assumed, although there was no measurement . made in this study to confirm
it. First-order kinetics are commonly applied to lagoon systems (8,9,16).
The magnitude of the removal rate constants are reasonable for this type
of system. The seasonal influence on these rates are difficult to
separate from the effects of increased flow rates. In any event, a
temperature coefficient 0 > defined by the relationship
was estimated for the primary lagoon employing the quarterly data presented
in Table 7. By solving equation (2) for Q , an average value for 9 for
soluble BOD in the primary lagoon was 1.015 whereas a similar value for
the total BOD was 1.012. These values are substantially lower than
those normally reported for aerated lagoon systems (2, 16). Efforts to
calculate 0 for the secondary lagoon were unsuccessful owing to the
variation of the first-order rates calculated. It is important to note
that the influence of temperature on biological processes is related
primarily to changes in biochemical reaction rates. This can normally be
detected through analysis of oxygen uptake rates, dehydrogenose activity,
and other biochemical analyses. As stated earlier, volatile solids measure
ments in this study were meaningless indicators of biological activity
owing to the high volatile solids of an inert nature occurring in the
raw wastewater.
37
-------
TABLE 7
LAGOON LOADING PARAMETERS SUMMARY*
00
Quarter Flow
1971 (gal/ day)
Jan-Mar 14,900
Apr-June 17 , 300
July-Sept 20,000
Oct-Dec 15,200
Ave. 16,900
1 BOD Loading
(Total/Soluble)
Inf. Prim. Sec.
Eff. Eff.
(Ib/day)
270 31.2 14.2
143 6.7 7.2
285 35.9 10.7
159 7.2 5.2
300 26.9 4.6
169 8.4 2.8
284 35.7 4.2
191 8.5 8,3
285 32.4 8.4
166 7.7 5.9
Volumetric
Load
Prim. Sec.
(lb/d/1000ft3
2.12 0.24
1.12 0.05
2.24 0.28
1.25 0.06
2.35 0.21
1.33 0.07
2.22 0.28
1.50 0.07
2.24 0.25
1.30 0.06
Hydraulic
Detention Time
Prim. Sec.
) (Days)
64 64
55 55
48 48
63 63
57 57
First-Order**
BOD Removal
Prim. teSec.
(Days'1)
0.12 0.019
0.30
0.13 0.042
0.39 0.007
0.21 0.100
0.40 0.041
0.11 0.119
0.34 0.0003
0.14 0.05
0.36 0.005
Temp.
Prim. Sec.
(°C)
2.2 1.0
17.8+ 17.8+
21.7 21.7
9.5 9.5
"•"" ™~
*all values averaged from Appendix C
**k « Lo-Le , based on BOD assuming first-order kinetics, CSTR,
LeO
+Estlmated, based on estimated temperature for May of 20°C
-------
Suspended Solids - The performance of the lagoon system with respect
to suspended solids is considerably more difficult to quantify than
BOD. Influent suspended solids were high (Table 8) and contained
a large fraction of organic matter. Adequate data was not available on the
settling properties of the influent solids and it is apparent from
Figure 14 that suspended solids removals in the primary lagoon were
very sporadic. During the oxygen deficient periodj primary effluent
solids often exceeded the influent solids level.
Again the advantage of staged lagoon operation is evident in Figure 14
where it is noted that final effluent suspended solids were considerably
more attenuated. The probability plots (Figures 15 and 16) indicate
that the effluent suspended solids are not distributed normally, being
rather widely scattered at the high end of the distribution. The lowest
values of final effluent suspended solids occurred during the period
July 1 through September 19. In this period, suspended solids
concentrations were less than 50 mg/1, 60 percent of the time. The
average suspended solids concentration in the final effluent was 108 mg/1
of which 91% was volatile matter (Table 8). It is interesting to note
that the solids discharged were predominately volatile, especially
during the July through December period. Furthermore, lowest effluent
solids occurred during the period when greatest algal growth was evident.
The effluent discharge structure, as noted previously, was a vertical
standpipe with no baffling. This discharge pipe was used to control
lagoon elevation. Although no data was available, it is reasonable to
assume that baffles may more significantly reduce suspended solids
discharges.
Solids Contributions to Effluent BOD - The data presented above suggests
that suspended solids play a significant role in the bio-degradable
organic matter discharged from the lagoons. A simple mathematical
expression for this contribution is:
L (total) - L (soluble) + C S , (3)
where S is the concentration of volatile suspended solids in mg/1, and
L is tne total or soluble BOD in mg/1 and C is the fraction of the
volatile solids contributing to the BOD (total).
Plots of effluent insoluble BOD versus volatile suspended solids (VSS)
for both primary and secondary lagoons are presented in Figures 17 and
18. Although not well correlated, there is an indication that approximately
46 percent of the VSS contribute to the total BOD in the primary lagoon.
This value is high indicating that the primary lagoon solids are not
well stabilized. The contribution of VSS to the final effluent BOD is
also quite variable, the average value of GV being 0.29.
39
-------
TABLE 8
AVERAGE SUSPENDED SOLIDS ANALYSES
Quarter
Jan-Mar
Apr-June
July- Sept
Oct-Dec
Average
Influent
Total Volatile
658
600
547
595
602
614
569
520
565
567
Primary Effluent
Total Volatile % *
(Total)
403
477
239
445
395
335
390
197
377
328
38.6
20.5
56.3
25.2
34.4
Total
155
119
43
111
108
Secondary
Volatile
143
103
43
110
98
Effluent
% Overall*
(Total)
73.4
80.1
92.1
81.3
82.0
All values of suspended solids in mg/1
*Percent removal based on total suspended solids
-------
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971-1972
1200
- 1000
o»
LAGOON PERFORMANCE
• raw wastewater
o primary lagoon effluent
x secondary lagoon effluent
V)
o
o
UJ
o
V)
<
800
600
400
200
0
0
• 0
0
o o
x 0
.,
DO = 0.0 mg/l
• • •
Primary Lagoon o
0
«
°
oo
xx
xxxx*x
x o x x o
y
x |
JAN FEB MAR APR MAY JUNE JULY AUG SEPT OCT NOV DEC JAN
FIGURE 14
-------
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971-1972
^
e
i
CO
0
_J
*. o
s> CO
o
UJ
o
z
UJ
a.
CO
=>
CO
0 W
600
700
600
500
400
300
200
100
0
•
PRIMARY EFFLUENT
-
Jf
•
•
X
« *
' »» *
-
•
9
t
-
• *
• •
**
• » • *
— • X
* * Jf
x^ **
^^ ***
^ * *
•••' «•*"" ^
*** -•&/
'."
-------
CHEESE PROCESS WASTEWATER LAGOONS
400
JAN 1971 - 1972
300
I
w
o
-j
o
CO
O
tu
o
z
UJ
1
200
FINAL EFFLUENT
* VOLATILE FRACTION ~ 90%
O.I
0.5 I
10
20 30 40 50 60 70 60 90 95 98
PERCENT TIME EQUAL TO OR
FIGURE 16
LESS THAN VALUC
-------
400
300
o
O
ID
I
O
O
§200
t
ui
o
o
100
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971-1972
EFFLUENT BOD vs VSS
PRIMARY LAGOON
0.46
Standard error
of estimate = 86.45
® - D.O. - 0.0 mg/l
_L
100 200 300 400 500 600
PRIMARY LAGOON EFFLUENT VSS - mg/l
FIGURE 17
700
-------
in
70
60
8 50
CD
i
o
I 40
I-
Ul
S 30
8
in
to
I0
,90
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971 - 1972
EFFLUENT BOD vs VSS
SECONDARY LAGOON
0.29
Stondard error of
estimate = 22.36
i ^
100
SECONDARY LAGOON VSS - mg/l
fl!5
•
•-266
200
FIGURE I?
-------
Nutrient Levels - The nutrients, nitrogen and phosphorus were determined
monthly on 24 hour composite samples collected from the raw wastewater
stream and the secondary lagoon. The results of these analyses appear
in Table 9. Examination of Table 8 indicates that total phosphorus levels
are high owing to the use of phosphate base cleaners. A substantial
amount of phosphorus was removed in the pond system. It should be
emphasized, however, that removal is the result of sedimentation of the
phosphorus and that eventually substantial amounts of phosphorus may be
resolubulized and be discharged in the final effluent. Thus, during the
one year period, it is doubtful that a steady state with respect to
phosphorus transformations has been achieved and, likely, effluent levels
may rise significantly over those presently reported.
No data was available on the ammonia nitrogen levels in the system, but
it is apparent that total Kjeldahl nitrogen is very low with respect to
carbon. The BOD to Nitrogen ratio for the raw wastewater averaged
100:0.7, well below that normally required for adequate biological growth
(100:5). The substantial removals of total Kjeldahl nitrogen through
the pond system is indicative of both cell synthesis and sedimentation.
It is expected that nitrogen recycle would play an Important role in
the biological system in these lagoons. Nitrate nitrogen in the final
effluent was normally low, but warmer temperatures did result in
significant nitrification between May and September. An examination of
lagoon temperature during these months (Figure 10) indicate that when
temperatures exceeded 20°C the rates of nitrification did increase.
Coliform and Fecal Coliform - The sanitary wastewaters from the cheese
processing plant were discharged to the process sewers, thereby
requiring the installation of chlorination equipment for disinfection
of the final effluent. Both total and fecal coliforms were determined
from 24 hour flow composited samples of the raw wastewater and final
effluent preceding disinfection. Results of these analyses appear in
Figures 19 and 20. During this study, no chlorination of the effluent
was practiced.
Examination of Figures 19 and 20 Indicate that better than 99.9 percent
removal of the total coliforms and fecal coliforms was achieved in the
lagoons. Temperature did not appear to significantly influence coliform
disappearance in the lagoons during the survey period, although there
was considerable variation in effluent coliform numbers.
Other Measurements - Values of pH and alkalinity were measured routinely
throughout the one year study (Appendix C). Raw wastewater pH values
were highest during January through May, averaging approximately 6.5,
and then decreasing and leveling off to 6.2 for the remainder of the study.
Similarly alkalinities of the raw wastewater averaged 330 mg/1 during
the January through April period and then continuously decreased to
approximately 230 mg/1 in September. It is possible that process changes
of raw water quality accounted for these changes.
46
-------
TABLE 9
NITROGEN AND PHOSPHORUS
Primary Lagoon Influent
Secondary Lagoon Effluent
Date
1971 Day
1-22 F
2-23 Tu
3-19 F
4-12 M
5-14 F
6-15 Tu
7-9 F
8-10 Tu
9-11 Sa
10-13 W
11-14 Su
12-16 Th
Total
Phosphorus
mg/1 Ib/d*
37.0= 8.5
35.0 4.1
41.3 4.9
7.4 0.7
32.5 5.4
76.9 13.2
15.5 3.1
33.0 5.8
68.4 14.0
55.7 8.2
04.6 14.4
42.6 5.7
Total
Kjeldahl
mg/1
7.5
9.2
10.8
10.2
5.3
16.0
12.2
3.6
12.1
2.0
26.2
7.7
Nitrogen
Ib/d*
1.7
1.1
1.3
1.0
0.9
2.7
2.4
0.6
2.5
0.3
3.9
1.0
Nitrate
Nitrogen
mg/1
0.1
1.0
0.1
0.4
0.4
4.4
0.1
0.1
0.1
0.1
0.1
2.7
BOD:N:P** Total Total Kjel- Nitrate
Phosphorus dahl Nitrogen Nitrogen
mg/1 Ib/d* mg/1 Ib/d* mg/1
100:0.6:0.3 35.0 8.0 4.0 0.9 0.3
100:0.3:1.1 27.5 3.3 5.9 0.7 0.5
100:0.5:2.1 26.4 3.1 5.5 0.7 0.2
100:6.8:4.9 28.0 2.8 6.0 0.6 0.4
100:0.5:3.2 26.8 4.5 10.6 1.8 1.9
100:1.0:5.0 10.7 1.8 4.2 0.7 24.4
100:0.8:1.0 14.8 2.9 1.5 0.3 3.4
100:0.2:1.6 11.6 2.0 1.0 0.2 4.0
100:0.7:3.8 8.4 1.7 1.1 0.2 1.4
100:1.1:2.2 14.8 2.2 0.2 0.0 0.4
100:0.7:2.6 23.1 3.5 1.8 0.3 0.4
100:0.5:2.7 31.6 4.3 4.2 0.6 0.2
Avg.
45.0
7.3
10.2
1.6
100:0.7:2.2 21.6 3.3
3.8 0.6
*lb/d - Calculated by using flow rates on day parameter was measured
** BOD:N:P - ratio of weights (or concentrations) of each component on day of analysis
-------
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971 - 1972
8
10
10*
I06-
CO
E
O
O
oc
Ul
Q.
QL
2
J2 10'
e
I03-
LAGOON PERFORMANCE • •
INFLUENT
<- less than value
SECONDARY EFFLUENT
ftAA -t.
J I I I L
J I L
J L
JAN FEB MAR APR MAY JUN JUL AU6 SEPT OCT NOV DEC JAN
FIGURE 19
-------
CHEESE PROCESS WASTEWATER LAGOONS
JAN 1971-1972
to'
io6
E
o 10
o
VO
o:
ui
o.
S
ce
o
8
o
tu
u.
10'
10
10
LAGOON PERFORMANCE
X x
X *
I ' ' I
f
'
f
1
X X
i x __ L
• INFLUENT
• X EFFLUENT
< - less than value
• .«
JAN FEB MAR APR MAY KJUN JUL AUG SEPT
FIGURE 20
OCT NOV DEC JAN
-------
The lagoons exhibited pH values of approximately 7.4 during the first
one half of the year (January through June), which then sharply decreased
to a value of about 7.2 for the remainder of the study. Alkalinlties
ranged from about 310 mg/1 to as high as 540 mg/1 during the year. No
correlation was noted between pH and measured alkalinity and there was
no particular trend in alkalinity values during the year. No correlation
was noted between pH and measured alkalinity and there was no particular
trend in alkalinity values during the year. It is assumed that changes
in algal activities and microorganism respiration Influenced these
variations, but no data was available on algal activities to document
these variations.
Settleable solids were monitored daily on the raw wastewater and on the
primary and secondary lagoon effluents (Appendix C). Settleable solidsx
in the raw wastewater ranged between 0.1 and 5 ml/liter during the one year
study* normally being less than 1.0. Secondary lagoon effluents never
demonstrated significant amounts of settleable solids, but the primary
lagoon effluent was high in settleable solids from mid-May through
mid-July. Values as high as 120 ml/liter were recorded during this period
when dissolved oxygen concentrations were zero. Floating mats of solids
and rising sludge was noted throughout this period. Once dissolved
oxygen was maintained in this lagoon, the settleable solids decreased to
an immeasureable amount.
Costs
The estimated annual capital costs for wastewater treatment at Kent Cheese
Co. are based on an Interest rate of 7 1/2 percent for mechanical and
equipment amortized over a five year period and costs for lagoon
construction over a 30 year period. Whereas the estimated annual costs
for operation and maintenance are based on costs associated with operating
labor, electric power, repairs and replacements, supplies and administration,
The annual costs presented do not include those costs associated with the
post construction studies that are not representative of normal operating
expenses. A summary of the costs related to annual operation for the
period January 18, 1971,to January- 17, 1972, of these treatment facilities
are presented below.
50
-------
Construction Costs
Annual Costs
Contract 29,097.42
Engineering
Preconstruction Report 500.00
Preparation of Plans 3,387.14
Construction Supervision 916.00
sub total $33,900.56
(i - 7.5% 30 yr) $ 2,870.40
Mechanical Equipment 15,592.82
(i » 7.5% 5 yr) 3.853.99
sub total $ 6,724.39
Operating and Maintenance Costs
Operator labor $ 1,364.83
Electric Power (2.676<:/kwm
x 92575 kwhr) 2,477.71
Repairs and Replacement 1,725.43
Supplies (expendable) 347.47
Administration 144.62
sub total 6,060.06 $ 6,060.06
Total Annual Costs $12,784.45
The estimated costs associated with the treatment of wastewaters for the
period January 18, 1971, through January 17, 1972, are based on the
interest rates and amortization periods selected for fixed costs, whereas
the operating and maintenance costs are those costs actually incurred for
the period of operation indicated. One item in the Repairs and Replacement
costs category; that is the replacement of a single blower with associated
costs, accounted for all but $134.55 of the $1,725.43 indicated in this
category. Normally one would expect a longer period of performance for
this type of equipment.
The costs prorated to pounds of BOD applied or 1000 gallons of wastewater
treated are $0.134 per pound of BOD and $2.05 per 1000 gallons respectively.
Based on cheese produced, the estimated cost is $0.0032 per pound.
51
-------
SECTION VII
ACKNOWLEDGMENTS
This study was supported by the United States Environmental Protection
Agency, Office of Research and Monitoring,and Kent Cheese Company, Inc.,
Kent, Illinois.
William C. Boyle, Ph.D., and Lawrence B. Polkowski, Ph.D., were contracted
as research consultants and authors after the treatment plant was in
operation and thereafter were responsible for the interpretation of data
collected during the post-construction studies and for writing this report.
Lorpe Gramms,Ph.D., Tom Jensen, E.I.T., and Jack Quigley, P.E., were
employed as part-time assistants to the project.
Mr. Allen Fehr, P.E., Freeport, Illinois, designed and supervised construction
of the treatment plant.
E.P.A. Representatives included William J. Lacy, H. 6. Keeler, Robert
Bum, and Max Cochrane.
Laboratory analysis were performed by Robert Corning, Chief Chemist, and
Mrs. Susan Kelly, Laboratory Supervisor, Corning Laboratories, Cedar
Falls, Iowa.
The Assistant Operator, plant operator, was Michael Green, Kent Cheese
Company, Kent, Illinois.
Mrs. Kathy Watson and Mrs. Barbara Daul, Lena, Illinois, served as
administrative assistants.
52
-------
SECTION VIII
REFERENCES
!• Methods for Chemical Analyses of Water and Wastes, U.S. EPA, National
Environmental Research Center, Analytical Control Laboratory,
Cincinnati, Ohio (1971).
2. SERCO Laboratories, Minnesota Aerated Lagoon Study, pp 101, Minnesota
Pollution Control Agency, Minneapolis, Minn. (Aug. 1970).
3. Oldshue, J.Y., "Aeration of Biological Systems Using Mixing Impellers",
Biological Treatment of Sewage and Industrial Wastes, (Ed. J. McCabe
and W.W. Eckenfelder, Jr.), Reinhold Publishing Corp., 231 (1956).
4. West, R.W. and Paulson, W. L., "Jet Aeration in Activated Sludge
Systems", J. Water Pollution Control Federation, 41, 1726 (1969).
5. Bewtra, J.K. and Nicholas, W.R., "Oxygenation from Diffused Air in
Aeration Tanks", J. Water Pollution Control Federation, 36, 1195 (1964).
6. Polcon Corp., Technical Bulletin, Teanech, N.J. (undated).
7. Eckenfelder, W.W. Jr., and Ford, D.L., "Engineering Aspects of Surface
Aeration Design", Proc. 22nd Industrial Waste Conf., Purdue University,
Engr. Ext. Series No. 129, 279 (1967).
8. Marias and Capri, M.J., "A Simplified Kinetic Theory for Aerated
Lagoons", Second International Symposium for Waste Treatment Lagoons,
Kansas City, Missouri, 299 (June 1970).
9. Pohl, E.F., "A Rational Approach to the Design of Aerated Lagoons",
Second International Symposium for Waste Treatment Lagoons, Kansas City,
Missouri, 231 (June 1970).
10. W. C. Boyle and P.M. Berthouex, "Biological Wastewater Treatment Model
Building - Fits and Misfits", Proc. International Conference Toward
a Unified Concept of Biological Waste Treatment Design, Atlanta, Ga. (Oct 1972)
11. Monod, J., "Researches sur la Croissance des Cultures Boetenennes",
Ann. Inst. Pasteur J79_, 390 (1942).
12. Lawrence, A.W. and McCarty,^P.L., "Unified Bases for Biological Treatment
Design and Operations", J. San. Engr. Div., A.S.C.E., 96, 757 (1970).
13. Pearson, E.A.,"Kinetics of Biological Treatment", Advances in Water
Quality Improvement, (E.F. Gloyna , & W. W. Eckenfelder, Jr., ed). Univ.
of Texas Press, Austin, Texas, 381 (1968.
14. Ramanathan, M. & Gandy, A.F., Jr., "Steady-State Model for Activated
Sludge with Constant Recycle Sludge Concentration", Biotech. Bioeng.
J.3, 125 (1971).
53
-------
15. McKinney, R.E., "Mathematics of Complete Mixing Activated Sludge",
Trans. ASCE, 128, 497 (1963).
16. Eckenfelder, W.W., Jr., Industrial Water Pollution Control, McGraw-
Hill, New York (1966).
17. Conway, R.A. & Kumke, G.W., "Field Techniques for Evaluating Aerators",
J. San. Eng.Div. A.S.C.E. 92, SA2, 21 (1966).
18. Technical Practice Committee - Subcommittee on Aeration in Wastewater
Treatment, "Aeration in Wastewater Treatment - Manual of Practice
No. 5", J. Water Pollution Control Federation, 41, 1863 (1969).
54
-------
Alpha, a
Beta, $
BOD
C
Cs
Cv
CIP
cu ft
d
DO
ft
fps
gal
hp
k
kl
kw
kw-hr
Lo
Le
SECTION IX
GLOSSARY OF TERMS
Ratio of overall oxygen mass transfer coefficients in
waste to tap water
Ratio of oxygen saturation value in waste to tap water
Biochemical Oxygen Demand, Five-day, 20°C
Oxygen concentration in water, mg/1
Oxygen saturation concentration in water, mg/1
Fraction of VSS contributing to BOD
Clean-in-place
Cubic foot
Day
Dissolved oxygen concentration
Feet
Feet per second
Gallon
Gallons per day
Horsepower
First order removal rate of BOD, I/days
BOD deoxygenation constant
Kilowatt
Kilowatt-hour
Five-day 20°C BOD of influent, mg/1
Five-day 20°C BOD of effluent, mg/1
55
-------
Ib pound
MG Million gallons
mg/1 Milligrams per liter
N Nitrogen
Nf Field oxygen transfer efficiency, Ib 02
kw-hr
NS Standard oxygen transfer efficiency at 20°C, zero D.O. in
tap water, Ib Q£
kw-hr
0/R Over-the-road trucking
0 Percent concentration of oxygen in air leaving lagoon, %
P Phosphorus
2
Pfe Absolute pressure at point of air release, Ib/in
Q Flow rate, MGD
R Percent removal of pollutional constituent
S VSS Concentration
SS Suspended solids
Sec Second
Scfm Standard cubic foot per minute
9 Detention time, V/Q, days
Q. Temperature correction coefficient
T Temperature, °C
v Volts
V Volume
VSS Volatile suspended solids
56
-------
SECTION X
APPENDICES
57
-------
APPENDIX A
OXYGEN UPTAKE RATES
Primary Lagoon
Date Station Depth
(Figure 4) from water surface
(ft)
11-19-70 1 5 6.3
3 5 6.3
5 5 6.2
13 5 6.2
14 5 6.3
5-23-71 1 1 17.1
1 5 17.1
5 1 17.1
5 6 17.0
14 2 17.1
7-21-71 1 6 24.0
5 6 24.1
8 6 24.0
13 6 24.0
8-26-71 3 6 23.5
56 —
12 6 23.5
14 6 23.5
10-7-71 1 2 16.5
14 6 16.5
8 6 16.5
Uptake Rate
(mg/l/hr)
1.9
2.3
2.1
2.0
1.9
5.0
5.8
6.3
6.0
4.9
1.2
1.2
1.3
1.1
0.9
1.0
0.8
0.6
1.6
1.4
1.6
58
-------
APPENDIX B
Calculation of Oxygen Transfer Rate
November 19, 1970
Lagoon No. 1 (Primary Lagoon)
Average Oxygen Uptake Rate =2.1 mg/l/hr =16.7 Ib/hr
Lagoon Temp. - 6.3°C
Dissolved Oxygen » 2.9 mg/1
1 compressor - 30 amps at 220 v - 6.6 kw
Air Distribution to Primary Lagoon - 80% estimated
Field Transfer: (17, 18)
-16.7 Ib/hr
f 6.6 kwx 0.8 " '
Standard Transfer:
N = N- Cs T-20
8 f (Ca -C)9
s
C at 20°C « 9.2( Pb + °t )
(29.4 42 )
« Q •> ,14.7 + 12/2.3 + 18.3.*
9'2 ( 2974 ^42~)
C - 9.2 (0.68 +0.5)
20°
- 10.8 mg/1
C - 14.8 mg/1 <§ 12' depth
S6.3°C
a • 0.75, 3 - 0.96, 9 = 1.02(19)
Ns - 3.16 f
]_0.
10>8
b*J
_
75(0.96 x 14.8 - 2.8) 1.02
N - 5.25 Ib/kw-hr
N - 3.91 Ib/hp-hr
S
*where depth " 12* and estimated transfer efficiency is estimated at 10%
59
-------
APPENDIX C
Lagoon Data
60
-------
WEEKLY DAT*
DATE
DAY
LAGOON
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APPENDIX D
Cost Estimates
Annuity whose present value is 1
* « • / X ^ **V *^ ** • -*
Mechanical Equipment - $15,592.82
n - Syr i - 0.075 (7 1/2%) 0.24716472 x $15,592.82 =• 3853.99
Construction - $33,900.56
n - 30 yr i - 0.075 ( 7 1/2%) 0.08467124 x 33,900.56 - 2870.40
where
A
nji present value of annuity for unit periodic payment
at interest rate i
i » rate of interest
n = number of conversion periods
v » present value (at compound interest) for unit principal,
- (1 + i)"1
S • Amount (at compound interest) for unit principal = (1 + i)n
76
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APPENDIX E
Pictures
77
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Primary Lagoon - Summer
-------
I
\ \
Primary Lagoon - Winter
-------
CD
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PLAN SHOWING LIQUID FLOW
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POLCON CORP.
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SELECTED WATER . i. Report NO.
RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
2. 3. Accession No.
4. Title Treatment of Cheese Processing Wastewaters 5- Deport Date
in Aerated Lagoons s.
8. Performing Organization
7. Author Pranrifi R> Dault Qr
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