WATER POLLUTION CONTROL RESEARCH SERIES
12060—10/70
Treatment of
Citrus Processing 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
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For sale by the Superintendent of Documents, U.S. Government Printing OfUcc
Waefilni'tnn. TXC. 20402 - Price $2.75
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Treatment of Citrus Processing Wastes
by
THE COCA-COLA. COMPANY FOODS DIVISION
Orlando, Florida 32802
for the
ENVIRONMENTAL PROTECTION ACENCY
WATER QUALITY OFFICE
Program 12060 10/70
WPRD 38-01-67
October 1970
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EPA Review Notice
This report has been reviewed by the Water Quality Office,
EPA, and approved for publication. Approval does not signi-
fy that the contents necessarily reflect the views and poli-
cies of the Environmental Protection Agency, nor does mention
of trade names or commercial products constitute endorsement
or recommendation for use.
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ABSTRACT
Plant scale studies were performed to determine operational and treatment
parameters for citrus processing wastewaters. Part I discusses treatment of concentrated
citrus processing wastewaters combined with domestic sewage using a modified activated
sludge process; namely, extended aeration. Part II discusses treatment of weak processing
wastewaters using a system which functioned as an aerated lagoon.
Extended aeration yielded 94 to 95 percent BOD removal; however, difficulties
concerning positive control of the treatment process were encountered. Variations in mixed
liquor suspended solids concentrations, sludge volume indices, sludge recirculation rates, and
hydraulic loading were considered principal causes adversely affecting the treatment process.
Excess sludge buildup amounted to approximately 0.5 pounds per pound of
influent BOD and sludge wastage accounted for the greater portion of overall nutrient
removal from the system.
The aerated lagoon process afforded 91 percent BOD removals when daily average
hydraulic and organic loadings were controlled at 6.4 mgd and 6,770 pounds, respectively
(detention time 7.9 days).
Kinetic studies yielded a BOD removal rate coefficient for citrus processing
wastewaters of 1.46 and an average temperature coefficient of 1.05.
Ecological studies indicated that BOD:N:P ratios of the order of 150:5:1 were
adequate for supporting the population of organisms required for effective bio-oxidation.
Organic nutrient removal studies using hyacinths indicated a minimum of 5 days'
detention would be required to afford substantial nutrient reduction. Significant organic
loading reductions (BOD, COD) were also attained by the hyacinth plant system during the
5-day detention period.
It was found that dried hyacinth plants were similar in food value to alfalfa hay
and could be used as a supplement in cattle feed.
This report was submitted in fulfillment of Demonstration Grant No. WPRD
38—01—67 between the Federal Water Quality Administration and The Coca-Cola
Company, Foods Division.
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CONCLUSIONS AND RECOMMENDATIONS
LEESBURG - PART I
1. The extended aeration modification of the activated sludge process is capable of a
high degree of secondary treatment for combined citrus processing and municipal
wastewaters. Organic removals averaging 94 percent were afforded even though
loading levels exceeded design capacity by an average of 52 percent (4,000
pounds) during weekday operation. Mixed liquor suspended solids concentrations
varied generally from 3,000 mg/1 to greater than 5,000 mg/1. BOD reductions
varied generally between 90 and 98 percent. A slight correlation was suggested
between higher mixed liquor suspended solids levels and higher BOD removals.
This was accomplished despite inexperience of operators and several difficulties
enumerated below.
2. The Leesburg plant was designed for a daily biochemical oxygen demand (BOD)
loading of 8,000 pounds, and constructed for about $500,000. Based on
long-term data, it afforded an average BOD reduction of 95.6 percent at an
average daily loading of 6,810 pounds, and 94.2 percent BOD reduction at an
average weekday loading of 12,200 pounds. Underdesign of the clarifiers and
inadequate sludge removal faculties significantly deterred continuous optimum
daily operations.
3. Principal difficulties with the treatment process involved positive control of
following factors:
A. Highly variable BOD loads prevented practicable control of mixed
liquor suspended solids (MLSS) at design ratio of 10 pounds MLSS per
pound of BOD applied;
B. High sludge volume indicies (SVI) caused by filamentous organisms,
sphaerotilius, due to high carbohydrate concentrations characteristic of
citrus wastewaters;
C. Sludge recirculation rates were extremely variable due to erratic
wastewater flow patterns; and
D. Hydraulic loadings were subject to considerable variation due to erratic
citrus wastewater flow patterns.
4. Treatment process control and efficiency would be enhanced significantly by:
A. Design Parameters
1. Equalization of citrus process wastewater loadings; and
2. Minimization of flow surges by means of a holding pond.
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B. Operational Parameters
1. Maintain a MLSS concentration of about 4,500 mg/1 or about
14 pounds of MLSS under aeration per pound of influent
BOD per day; and
2. Maintain a sludge recirculation rate of less than 100 percent
of plant influent flow.
5. Clarification was affected significantly by sludge bulking due to poor SVI control
and flow surges. Solids carryover in clarifier effluent was almost a daily occurance
during the height of the citrus processing season.
6. Based on very rough estimates, some 0.4 to 0.6 pounds of waste sludge solids
were provided per pound of influent BOD. This was significantly higher than
anticipated for domestic waste alone by extended aeration.
7. Facilities for disposing of waste sludge were inadequate. Further studies are
required to determine most economical improvements. However, the current
disposal problems could be minimized by controlling MLSS concentration to
about 4,500 mg/1 by daily wastage from clarifier at highest practical solids
content
8. BOD reductions of better than 90 percent were afforded with no supplemental
nutrients, despite a relatively high BOD: Nitrogen ratio of about 30:1 in the
combined raw wastewater. The addition of supplemental nutrients produced no
observable change in BOD removal efficiencies.
9. Average nitrogen and phosphorous removals of the order of 70 and 90 percent,
respectively, were largely accounted for in waste sludge removal from the system.
These removals appeared to be independent of MLSS levels. Oxygen transfer
levels were not studied.
10. The oxidation pond was quite effective in compensating for deficiencies in
treatment process control. The pond contributed significantly to overall BOD
reductions during periods of excessive solids carryover from the clarifiers. On an
average the pond achieved 14 percent out of the 94 percent total average BOD
removal.
11. The oxidation pond following the activated sludge process did not provide
substantial nitrogen or phosphorous reductions, probably because of the large
amount of solids released to the pond over the clarifier weirs.
12. Clarifiers for service conditions at Leesburg probably should be designed for lower
overflow ratio than 750 gpd per square foot The sludge blanket frequently
approached the weir level because of consistently high SVI values. Sludge was
sensitive to turbulence during high flow rates and solids carryover resulted.
Further studies should be conducted to determine a more suitable design overflow
rate.
VI
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13. Lower costs probably do not justify the use of vertical turbine pumps
recirculating sludge under conditions at Leesburg. Excessive outages were
experienced due to stringy solids such as hair which fouled impellers and bearings.
AUBURNDALE - PART H
1. The Aubumdale plant was designed for a daily biological oxygen demand (BOD)
loading of 18,500 pounds and hydraulic loadings of 30 mgd. Construction costs
were approximately $485,000.
2. The existing facility will not operate as an extended aeration system due to the
inadequacy of the sludge collection system. During the period of attempted
operation as an extended aeration plant BOD removals averaged 62 percent and
mixed liquor suspended solids (MLSS) concentrations averaged only 67 mg/1,
despite a wide variety of operating procedures. Therefore, the majority of original
grant objectives could not be satisfied.
3. Modification of the existing facility to operate as an extended aeration plant
would require:
A. Two 200 foot diameter clarifiers;
B. A sludge recirculation system; and
C. Sludge wastage and treatment facilities.
4. Additional studies during the 1968—1969 citrus processing season indicated that
the existing facility would afford adequate BOD removals when operated as an
aerated lagoon system. BOD removals of 91 percent were attained at daily average
hydraulic and organic (BOD) loadings of 6.4 mgd and 6,770 pounds, respectively.
5. Modification of the existing facility to operate as an aerated lagoon system would
entail:
A. Approximately 40 additional acres of aeration basins with mechanical
aerators;
B. Six additional 75 horsepower mechanical aerators; and
C. Relocating three aerators from the existing aeration pond to the settling
pond.
6. Kinetic studies conducted at Aubumdale yielded an average BOD removal rate
coefficent (K20°C w^ nutrients) of 1.46 and an average temperature coefficent
(O) of 1.05 (see Appendix 5).
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7. Ecological studies confirmed that BOD:N:P ratios of 150:5:1 provided a well
balanced system (nutritionwise) that was capable of supporting the variety of
organisms required for effective bio—oxidation.
8. The hyacinth study indicated that:
A. A minimum of five days' detention was required to attain a substantial
nutrient removal which was most significant at dissolved oxygen
concentrations below 0.5 mg/1.
B. Hyacinth plants appeared to be comparable to alfalfa hay in
composition;
C. A substantial quantity of wastewater and nutrient was released when
the hyacinth plants were squeezed during a drying process (one acre of
hyacinths would yield 34,000 gallons of pressed liquor containing 63
mg/1 PO4-P and 335 mg/1 total-N.
D. Existing feed mill equipment would require modification in order to
incorporate hyacinth plant processing with present feed mill operations;
E. Microbiota attached to the hyacinth plant roots produced substantial
biological and chemical oxygen demand removals (averaging 70 and 47
percent, respectively);
F Large scale harvesting operations could be accomplished by means of
mechanical devices now available for aquatic vegetation control.
9. Principal difficulties with the treatment process included:
A. Sludge recirculation could not be accomplished due to an inadequate
sludge collection system.
B. Mixed liquor suspended solids concentrations could not be increased
above a maximum monthly average of 103 mg/1 due to low sludge
concentration of recirculated sludge.
C. Organic (BOD) and hydraulic loadings increased significantly due to
increased processing levels at both The Coca—Cola Company and
Adams Packing Company. Statistical studies conducted during the
1966—1967 citrus processing season indicated daily average hydraulic
and organic (BOD) loadings of 17.9 mgd and 18,400 pounds,
respectively. Studies during the 1968—1969 citrus processing season
indicated daily average hydraulic and organic loadings of 30 mgd and
32,500 pounds, respectively. This represents a hydraulic loading
increase of 67 percent and an organic loading increase of 77 percent.
Vlll
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10. Inadequacies in plant equipment were found in:
A. Sludge collection system prevented implementing design concept
involving the extended aeration process. Sludge collection area was too
large and slopes too gentle (15°) to effectively move sludge to the
gravity pickups without mechanical devices. A minimum slope of about
60° is recommended.
B. Aerator flotation devices were constructed of fiber glass and were not
properly tested by the manufacturer prior to delivery. Apparently 75
horsepower aerators created more stress than the fiber glass floats could
withstand causing fatigue cracks and the floats were no longer
watertight. This adversly affected the level of aerator submergence.
C. High volume, low head lift pumps were used to provide a low cost lift
station. The lift pumps were sensitive to small head variations and when
all pumps were running simutaneously, discharge rates were somewhat
lower than rated capacities.
D. A low cost metering system was provided to measure flows between 5
and 50 mgd. However, due to intermittent pumping and
subatmospheric pressures when two or more transfer pumps were
operating, air frequently became trapped in the transmitter lines. Daily
manual venting of the air bleed-off valves was required.
11. Polishing ponds afforded biological oxygen demand (BOD) reductions of
approximately 14 percent. Nitrogen concentrations exhibited reductions of 21
percent and phosphate concentrations decreased about 26 percent. Further
studies are required to determine whether the nitrogen and phosphorus are
soluble forms or are associated with the particulate (suspended solids) matter.
12. Chemical oxygen demand (COD) analyses should be used as an operational
control parameter since citrus processing wastewaters inherently contain materials
that are toxic, and therefore affect biological oxygen demand (BOD) results. Also
the 5-day incubation period required for BOD tests renders the tests useless for
operational purposes; whereas, COD tests can be performed in less than one
hour's time and operational procedures can be adjusted accordingly.
13. Treatment plant effluent contained about 30 mg/1 BOD. However, it could be
used for cooling water with little or no additional treatment. At present, pumping
costs involved to return effluent water about a half mile to the process plant do
not make reuse of treatment plant effluent economically attractive.
14. COD/BOD ratios on the influent stream averaged 1.73. Treatment plant effluent
stream COD/BOD ratios averaged 3.34. Influent organic loadings could be
estimated by multiplying influent COD loadings by 0.578.
IX
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IS. Due to the variety of mechanical and operational problems inherent during the
first year's operation of a new waste treatment facility, detailed research and
plant evaluation studies should be delayed until these difficulites are corrected. At
least one years' time should be allowed between completion of construction and
beginning of research. This would allow sufficient time to acquaint operators with
the treatment process and waste characteristics.
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TABLE OF CONTENTS
PART I
ABSTRACT
CONCLUSIONS AND RECOMMENDATIONS
Leesburg
Auburndale
Page Number
iii
v — x
V
vii
SECTION 1 INTRODUCTION
SECTION 2 SCOPE AND OBJECTIVES
SECTION 3 GENERAL DESCRIPTION OF WASTEWATERS
3.01 The Coca—Cok Company Foods Division
3.02 City of Leesburg Sewage
SECTION 4 WASTEWATER TREATMENT PLANT
4.01 General Description
4.02 Design Criteria and Characteristics
SECTION 5 PLAN OF INVESTIGATION
SECTION 6 PLANT OPERATION
6.01 Startup (1966-1967) Citrus
Processing Season
6.02 1967-1968 Citrus Processing Season
SECTION 7 SAMPLING AND TESTING
7.01 Sampling
7.02 Testing
SECTION 8 RESULTS
8.01 General Conditions
8.02 Flow Data
1-2
3
5-6
5
6
7-8
7
8
9
11-13
11
11
15
15
15
17-19
17
17
XI
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TABLE OF CONTENTS
PART I
(continued)
Section 8 — continued
8.03 Daily BOD Loadings
8.04 Suspended Solids
8.05 Dissolved Oxygen
8.06 pH Values
8.07 Temperature
8.08 Sludge Recirculation
8.09 BOD Removal
8.10 Suspended Solids Removal
8.11 Sludge Volume Index
8.12 Waste Sludge
8.13 Nitrogen and Phosphorous Analyses
SECTION 9 DISCUSSION OF RESULTS
9.01 Flow Data
9.02 BOD Loadings and Removals
9.03 Wastewater Suspended Solids and Removal
9.04 Mixed Liquor Suspended Solids (MLSS)
9.05 Sludge Wastage
9.06 Sludge Recirculation and Sludge Volume
Index (SVI)
9.07 Dissolved Oxygen Levels
9.08 pH Value and Temperature
9.09 Nutrient Removal
9.10 Plant Equipment
9.11 Cost of Treatment
SECTION 10 ECOLOGICAL STUDY
10.01 General
10.02 Leesburg Extended Aeration System
Page Number
17
18
18
18
18
18
19
19
19
19
19
21 -27
21
22
23
23
24
24
25
25
25
26
27
29-30
29
29
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TABLES
PARTI
Page Number
Table 1 Characteristics of Treatment Plant Facilities T — 1
Table 2 City of Leesburg Sewage Treatment Plant
Operating Data During 1966—67 Citrus Processing
Season
Minute Maid Company — Leesburg, Florida T - 5
Table 3 Characteristics of Typical Wastewaters T — 6
Table 4 Nutrient Levels and Removals T — 7
Table 5 Analyses for Nitrogen and Phosphorus T — 9
Table 6 Leesburg Biota — Extended Aeration
The Coca—Cola Company Foods Division T — 10
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FIGURES
PART I
Page Number
Figure 1 Location Map — The Coca—Cola Company
Leesburg, Florida F — 1
Figure 2 Vicinity Map — The Coca—Cola Company
Leesburg, Florida F — 2
Figure 3 Wastewater Sources — Typical Citrus
Concentrate Plant F — 3
Figure 4 City of Leesburg — Wastewater Treatment
Facilities F - 4
Figure 5 Daily Operation Record F — 5
Figure 6 Weekly Average Wastewater Flows - F — 6
Figure 7 Weekly Average BOD Loadings F — 7
Figure 8 Weekly Average Combined Wastewater
BOD Concentration F - 8
Figure 9 Weekly Average MLSS Concentrations F - 9
Figure 10 Weekly Average Clarifier Effluent Suspended
Solids F - 10
Figure 11 Weekly Average D.O. Concentration — Aeration
Basin No. 1 F - 11
Figure 12 Weekly Average D.O. Concentration — Aeration
Basin No. 2 F - 12
Figure 13 Weekly Average D.O. Concentration Oxidation
Pond Effluent F - 13
Figure 14 Typical Weekly pH Record Citrus Wastewater F — 14
Figure 15 Weekly Average Effluent Temperatures F — 15
xv
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FIGURES
PART I
(continued)
Pace Number
Figure 16 Weekly Average Sludge Recirculation F — 16
Figure 17 Weekly Average BOD Removals F —17
Figure 18 Weekly Average Suspended Solids Removals F — 18
Figure 19 Weekly Average Sludge Volume Indices F -19
Figure 20 Weekly Average Sludge Wastage F - 20
Figure 21 Weekly Average D.O. Concentrations F - 21
Figure 22 Weekly Average MLSS Concentrations - BOD
Removals F - 22
Figure 23 Weekly Average MLSS Concentrations — Sludge
Wastage F - 23
Figure 24 Weekly Average MLSS Concentrations — Sludge
Recirculation — Sludge Volume Indices F — 24
Figure 25 Weekly Average MLSS Concentrations — Sludge
Volume Indices F — 25
Figure 26 Weekly Average Sludge Recirculation — Sludge
Volume Indices — Clarifier Effluent Suspended
Solids F - 26
xvi
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APPENDIX
PARTI
Page Number
Appendix 1 Laboratory Studies, 1966-67 Citrus Processing
Season A - 1
TABLE OF CONTENTS
FOR PART II
FOLLOWS PARTITION PAGE
AT THE END OF PART I
xvii
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SECTION 1
INTRODUCTION
Citrus production, processing, and marketing comprises a $2 billion industry in
Florida alone. More than 800,000 acres of the peninsula, extending some 250 miles from
north to south, are planted in citrus trees. This area yields about 75 percent of oranges and
80 percent of grapefruit grown in the United States. The total Florida citrus crop for the
1967-1968 season amounted to about 9.0 million tons. For comparison, the United States
produced 3.3 million tons of apples, 1.8 million tons of peaches, and 12.1 million tons of
potatoes in 1964. Since about one-third of orange acreage had not attained bearing age by
the 1966-67 season, and since citrus acreage is constantly expanding, a steady increase in
production is anticipated for years to come. Thus, the citrus industry is a very important
factor hi the economy of Florida.
The majority of Florida citrus is subjected to processing within the State to
produce single-strength or concentrated juice for marketing in containers. A survey in 1965
revealed a total of 52 citrus processing plants in the State. These processed about 82 percent
of the 1965-1966 crop. It is understandable that operations of such magnitude yield great
quantities of waste materials to be dealt with. The industry has made substantial progress in
disposing of wastes through recovery of valuable by-products. For example, Florida plants
produced 350,000 tons of cattle feed and 48,000 tons of citrus molasses during the
1965-1966 season. Cattle feed production in 1966-1967 amounted to about 573,000 tons.
The above mentioned survey indicated, however, that some 130 million gallons per day
(mgd) of wastewater, with a 5-day biochemical oxygen demand (BOD) loading of the order
of 319,000 pounds per day, were discharged from Florida plants. The Bureau of Sanitary
Engineering of the Florida State Board of Health is vigorously proposing treatment of
wastewaters from the industry.
There are no standard design parameters for citrus processing plant wastewater
treatment. It is generally recognized that plant location is an important factor in
determining treatment requirements and planning treatment facilities. For example, The
Coca-Cola Company, Foods Division plant at Leesburg, Florida (Figure 1) is located on
limited space within the city limits. Prior to 1967, raw wastewater from the plant and
primary treated sewage from the nearby Leesburg sewage treatment plant were discharged
separately into Lake Griffin (Figure 2). It was determined earlier by the Bureau of Sanitary
Engineering, Florida State Board of Health, that secondary treatment of both wastewaters
was required for adequate protection of receiving waters. In this particular case, it appeared
mutually advantageous for the citrus processing plant and the City to provide treatment
facilities for the combined wastewaters. Based on results of laboratory and pilot plant
studies covering a two-year period, a treatment plant of the extended aeration type was
installed to accommodate the combined wastewaters. This plant was placed in service during
1966-1967 citrus season, and it is the first large-scale facility of its type in the citrus
processing industry.
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Although the plant was provided primarily for BOD reduction, it was recognized
by the design engineers (Black, Crow and Eidsness, Inc.), that accelerated eutrophication in
receiving waters is a problem that must be faced in the future. It was seen also that the
facilities afford an opportunity for investigation of nutrient removal, as well as for further
studies regarding factors affecting organics removal.
The Coca-Cola Company Foods Division was known as Minute Maid Company
during the first part of this study. The latter designation appears on some of the material
presented herein to describe results of the study.
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SECTION 2
SCOPE AND OBJECTIVES
The general purpose of this study was to investigate treatment of combined citrus
processing and municipal wastewaters afforded by the City of Leesburg Wastewater
Treatment Plant. More specific objectives included investigation of operating parameters,
determination of suitable control limits, and evaluation of plant design criteria. Examination
of nitrogen and phosphorous removal in the treatment system was also included in the scope
of work.
The primary objective of plant operations at all times is to fulfill an obligation to
the public by satisfying the established need for a high degree of treatment of all
wastewaters entering the plant. Operational restrictions imposed by this service requirement
were seen to place significant limitations on the latitude of investigative work. In view of
these restrictions and design capabilities of the plant, it was anticipated that principal
operational variables subject to some degree of control for study purposes are mixed liquor
suspended solids (MLSS) concentration, phosphorous concentration, and sludge
recirculation rate. Investigation of effects of these controlled variables on treatment were
prime objectives of the study.
As the plant stands, such variables as dissolved oxygen concentration and nutrient
removal are not subject to operational control. Analyses of operating data to relate these
variables to other treatment factors were included as study objectives.
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SECTION 3
GENERAL DESCRIPTION OF WASTEWATERS
3.01 The Coca-Cola Company Foods Division
Citrus processing plants are operated on a seasonal basis. Some early varieties of
fruit mature by September or October, but a succession of others reach maturity later.
Inasmuch as oranges may stay on the tree in mature condition for two to five months,
considerable control is exercised over the harvesting and processing season, which may
extend over eight to ten months.
The principal processing season at the Leesburg plant usually extends from early
December into June. Processing is usually discontinued or slackened about midseason
between crops of early and late maturing fruit. This lull may extend from a few days to a
few weeks, depending upon crop conditions. During the off season, plant facilities are used
sporadically for processing lemons and limes and for repacking operations. These off-season
activities yield relatively light wastewater loadings.
Wastewater sources in a typical citrus concentrate plant are indicated in Figure 3.
The major source of high-strength wastewater is the juice extractor and finisher area, where
relatively large volumes of water are used during frequent clean-up periods. Other
high-strength wastewaters result from less frequent cleaning of juice storage, evaporator,
blend tank, chiller, and packaging areas. All of these wastewaters at the Leesburg plant are
screened to remove pulp, peel, seeds, and other suspended solids.
Fruit unloading and preparation operations and barometric condensers yield large
volumes of low-strength wastewaters. The former are screened at the Leesburg plant to
remove gross solids.
In general, citrus processing wastewaters may be considered as dilute solutions of
citrus juice. The pH value is variable. Citric acid content of the juice tends to yield mildly
acid values. However, periodic discharges of alkaline agents during clean-up operations result
in high pH values. Total solids are comprised largely of sugars, which are readily
biodegradable. Other constituents include peptizing agents, which interfere with gravity
clarification, and peel oils, which may act as bacteriostatic agents. The wastewaters are
usually deficient in nitrogen and/or phosphorous compounds required for optimum
treatment by biological processes. Wastewater volume and strength may be subject to
considerable fluctuation, depending upon the nature of processing operations.
Total citrus wastewater flow at Leesburg is of the order of 12 mgd. Wastewaters
are segregated within the plant into low and high strength fractions. The former, amounting
to some 95 percent of the total flow and exhibiting BOD of the order of 30 milligrams per
liter (mg/1), is discharged directly to Lake Griffin. The latter are discharged to the City of
Leesburg wastewater treatment facilities.
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The citrus processing plant at Leesbuig operates on a 24-hour per day basis during
the principal crop season. It is usually shut down on weekends and holidays. The shutdown
period is variable and dependent upon processing requirements.
3.02 City of Leesburg Sewage
The population of Leesbuig in 1960 was 11,172. A population of 22,000 is
anticipated during the 1980's. The Coca-Cola Company Foods Division citrus processing
plant is by far the largest industry in the City.
Existing sewerage serves approximately 80 percent of the population. Average
daily sewage flow is of the order of 1.15 mgd. The sewage flows to the treatment facilities in
a relatively fresh condition and exhibits an average BOD of the order of 145 mg/1.
6
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SECTION 4
WASTEWATER TREATMENT PLANT
4.01 General Description
The plant is a modification of the activated sludge type designed for extended
aeration of unclarified wastewaters with completely mixed recycled sludge. A shallow
oxidation pond was provided for further polishing of the effluent prior to ultimate
discharge. A schematic flow diagram is presented in Figure 4.
The plant includes elements of an older primary plant provided for City of
Leesburg sewage. Additional secondary treatment facilities were constructed on an adjoining
site to accommodate combined sewage and citrus processing plant wastewaters. Elements of
the above mentioned primary plant are indicated in the upper portion of Figure 4. Certain
of these, including the comminutor, degritter parshall flume and wet well still accommodate
City sewage alone. The thickener indicated in Figure 4 is actually the old primary plant
clarifier, with no modifications. Remaining elements of the primary plant are the two
digesters and sludge drying beds indicated in the figure.
Citrus processing wastewaters are delivered to the treatment site by a pumping
station located at the citrus plant. Facilities were included at the treatment plant for adding
supplemental phosphorus, in the form of phosphoric acid, to the citrus waste. Citrus
wastewater, raw sewage and recirculated sludge are blended in a head box, which is the first
element of the new treatment facilities. The mixture is apportioned by mud valves in the
bottom of the head box to two aeration basins. These are lined earthen basins, and each was
provided with two 60 horsepower, mechanical aerators mounted on piers. Aeration basin
effluent is combined in common gravity piping and then divided into two suction type
clarifiers. Clarified wastewater is recombined in common gravity piping, chlorinated, and
discharged to a shallow, earthen pond. Pond effluent is discharged to Lake Griffin (Figure
2).
Provisions were made for wasting sludge from the two clarifiers to the clarifier of
the old primary plant, described in Figure 4 as a thickener. It was anticipated that this
clarifier and the digesters would be adequate for storage and thickening of sludge prior to
further dewatering on the drying beds and/or ultimate disposal by hauling.
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4.02 Design Criteria and Characteristics
Plant design criteria are summarized as follows:
City Citrus
Sewage Processing Total
Daily Wastewater flow, mgd:
Average 2.50 0.85 3.35
Maximum 6.25 1.15 7.40
BOD concentration, mg/1 144 706 287
BOD (5-day) load, Ibs/day 3,000 5,000 8,000
Recirculated sludge, mgd 3.35
BODlbs/Mcf 18.3
Extended aeration:
Mixed liquor suspended solids (MLSS)
Under aeration, Ibs/lb BOD 10
Concentration, mg/1 2,937
Detention, hours 24
Clarifier surface overflow rate, gpd/sq. ft 730
BOD reduction, % 90+
Design flow and BOD load for city sewage were based on projected conditions for
1975. Actual sewage flow and BOD load averaged 1.15 mgd and 1,400 pounds per day,
respectively, in 1964. According to The Coca-Cola Company Foods Division management
personnel, above design flow and BOD load for citrus processing waste, which were based on
1964 conditions, should suffice for projected 1975 conditions.
Further details of plant facilities are described in Table 1.
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SECTION 5
PLAN OF INVESTIGATION
The general plan of experimentation involved the few variables that were
anticipated to be subject to reasonable operational control. These were mixed liquor
suspended solids (MLSS), phosphorous concentration, and sludge recirculation rate. It was
planned to vary one of these variables at a time in series of tests covering one citrus season.
Routine data indicated in Figure 5 would be collected throughout the season.
Supplementary routine analyses for nitrogen and phosphorous concentrations in combined
wastewater and in clarifier and pond effluents were provided for.
It was proposed to operate under each set experimental conditions for about one
month to assure collection of a reasonable average data under equilibrium conditions. Since
the duration of the citrus processing season is usually about six months, a rather limited
program was planned. This program is summarized as follows:
Controlled Variable Test
Recirc. BOD:P Ratio MLSS duration,
Condition Sludge, % (Combined Waste) mg/1 months
1 100 100:1 3,000 1
2 100 100:1 4,000 1
3 100 100:1 5,000 1
4 100 As received Optimum 1
5 100 Midway above Optimum 1
6 50 Optimum Optimum 1
Total 6
Analysis of all data was proposed to afford evaluation of nutrient removal,
treatment efficiency, and plant design.
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SECTION 6
PLANT OPERATION
6.01 Startup (1966-1967) Citrus Processing Season
Plant construction was far from completion at the beginning of the 1966-1967
citrus processing season, during which it was originally proposed to initiate the investigation.
Insistence from City officials resulted in acceptance of citrus wastewaters at the plant early
in December, 1966, before any of the secondary treatment units were operable. Citrus
wastewaters were routed through one aeration basin, in which the mechanical aerators were
inoperable, and remaining facilities were by-passed with a temporary arrangement. Separate
operation of the old primary plant was continued for treatment of City sewage in
accordance with prior practice. As anticipated, premature acceptance of citrus wastewaters
resulted in a variety of significant problems, including objectionable odors, hindered orderly
completion of facilities, and multiplied difficulties usually encountered during plant
startups.
It was not until February 24, 1967, that plant construction was reasonably
complete, and City sewage was diverted to the new facilities. Remainder of the season was
devoted largely to training of plant personnel, who were totally inexperienced in operation
of secondary treatment facilities; solving usual startup problems with mechanical
equipment, instrumentation, etc.; and establishing treatment control, sampling, and
analytical procedures to be employed during the investigation.
Reasonable satisfactory operation of the plant was established by mid-April,
1967. Phosphoric acid was added to yield a BOD:P ratio of about 80:1 in raw combined
wastewater based on average requirements indicated during pilot plant studies preceding
design. Operating data obtained during the last two months of the citrus season are
summarized in Table 2. Sludge wastage was insignificant during this period, and the
uncontrolled MLSS concentration ranged to values of 6,000 to 7,000 mg/1. Citrus
wastewater BOD loadings were significantly higher than the design loading 92 percent of the
time, due probably to a bumper crop of fruit and associated problems within the citrus
plant. Despite an average weekday BOD loading of 12,200 pounds per day, amounting to an
overload of 53 percent of the design loading, BOD reductions were consistently higher than
anticipated and averaged 94.2 percent until an aerator reduction gear failure on June 3,
1967. Principal problems of process control involved MLSS concentration and solids
carryover from the clarifiers.
6.02 1967-1968 Citrus Processing Season
The detailed program of investigation described earlier was initiated at the outset
of the 1967-1968 season. Improvements were made to sampling facilities just prior to the
season to assure more dependable data during the studies. These consisted of automatic
proportional samplers for raw sewage, raw citrus wastewater, and clarifier effluent, as well as
sample pumps for continuous delivery of aerator basin effluent and recirculated sludge. A
pH recorder was provided for raw citrus wastewater. These improvements are indicated in
Figure 4. Analyses for nitrogen and phosphorous compounds in the wastewaters were
initiated in December, 1967.
11
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Average MLSS concentration during the week of November 12, 1967, was about
6,500 mg/1. It was reduced to about 3,000 mg/1 by the end of the month and maintained at
weekly average'values of about 3,100 to 3,750 mg/1 until the week of January 14, 1968, in
accordance with condition 1 of our program. This was accomplished by wasting some
1,430,000 gallons of sludge at an average rate of 30,500 gpd and ranging to 168,000 gpd.
Sludge was wasted by pumping to the thickener and digesters; settling; drawing
off supernatant, which was returned to the sewage wet well; and discharging to a tank truck
or sludge drying beds. Since the capacity of the drying beds was no more than about 7,500
gpd, the majority was hauled away to the City's solids disposal area. Limited tests indicated
that waste sludge could be thickened to about 3.2 percent solids during the procedure. The
thickened sludge dewatered well on the drying beds with little odor, comparable with
anaerobically digested sludge.
Reasonable control was maintained over sludge recirculation during the initial
study condition. Average recirculation amounted to about 80 percent.
Phosphorous levels in the combined raw wastewaters were considerably higher
than anticipated from preliminary laboratory and pilot plant studies preceding design of the
plant. BOD:P ratios averaged about 57:1 over the season. Addition of phosphoric acid
during the initial study condition resulted in an average BOD:P ratio of about 53:1 rather
than 100:1 as indicated in our program. This ratio was maintained, approximately, through
March, 1968, to minimize effects of the variable on subsequent studies. Addition of
phosphoric acid was discontinued on April 2, 1968, and BOD:P ratios averaged about 70:1
in combined raw wastewaters throughout the remainder of the season.
Operating personnel were requested on January 12, 1968, to maintain a MLSS
concentration of about 4,000 mg/1 in accordance with condition 2 of our program. This
concentration was maintained reasonably well for about two weeks. It was then purposely
decreased to about 3,100 mg/1, through wasting sludge, by plant personnel on the advice of
Florida State Board of Health personnel in an effort to control a considerable clarifier
carryover problem. Thus, the average MLSS concentration for the planned period of study
amounted to no more than 3,400 mg/1, or roughly the same as that of the initial period.
Sludge recirculation was increased from about 80 percent to about 130 percent by plant
personnel in a further effort to control clarifier carryover.
Plant and regulatory agency personnel were quite reluctant to increase MLSS
concentration in accordance with our program to 5,000 mg/1 despite satisfactory operation
at concentrations of more than 6,000 mg/1 during the previous season. In view of this and
the previous abundant data at higher solids loadings, it was agreed that treatment would be
controlled as nearly as possible to design conditions for the remainder of the season. The
program involving deliberate variations of treatment factors was abandoned in favor of
greater emphasis on collection and analysis of operating data. As it turned out, the season
afforded a very wide variety of operating conditions for study. For example, weekly average
MLSS concentrations varied from about 2,000 to 4,750 mg/1, and sludge recirculation varied
from about 70 to about 185 percent.
12
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BOD loadings were generally within the design value throughout the season,
although one weekly average amounted to some 11,300 pounds per day and four others
ranged from 8,300 to 9,200 pounds per day. Principal process control problems involved
MLSS concentration and clarifier carryover due to sludge bulking. As a result of
inexperience, there was a pronounced reluctance on the part of operators to experiment in
solving problems. A variety of problems are certain to arise in unique wastewater treatment
systems such as that at Leesburg, and operating personnel with adequate education and
training in this discipline are requisite to proper end results.
13
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SECTION 7
SAMPLING AND TESTING
7.01 Sampling
Routine sampling of the raw sewage, raw citrus waste, and clarifier effluent was
accomplished by means of Chicago Pump Company, "Tru—Test" samplers. Locations are
indicated in Figure 4. The sampling systems provided composite samples automatically in
direct proportion to flow. Samples were collected over 24-hour periods in 2-gallon
polyethylene containers, and were maintained at 40°F. in the refrigerated compartment of
the sampler throughout the sampling period.
Since there was no suitable sampling point for collection of combined wastewater
samples, these were constructed from composited raw sewage citrus waste samples in
proportion to their respective daily flows. A simple nomograph was provided the treatment
plant operator to facilitate manual preparation of the samples.
Daily composite samples of the oxidation pond effluent were constructed from
periodic grab samples collected over a 24-hour period. These were also maintained at
approximately 4CrF. in a standard laboratory refrigerator. Aeration basin effluents and
recirculated sludge samples were grab samples taken and tested once each 8-hour shift.
7.02 Testing
Routine tests conducted at the plant are indicated in Figure 5.
Semiweekly composite samples of combined wastewater, clarifier effluent, and
oxidation pond effluent were analyzed for total nitrogen and phosphorous content. Total
nitrogen was determined from analyses for ammonia, organic nitrogen, nitrate, and nitrite.
All testing procedures were in accordance with "Standard Methods for
Examination of Water and Wastewater," 12th Edition, APHA, AWWA, WPCF (1965).
Routine sampling and analyses were accomplished by the operating personnel of
the City of Leesburg wastewater treatment plant. Training and supervision were provided by
Black, Crow and Eidsness, Inc. Nitrogen and phosphorous determinations were made by L &
S Laboratory, Winter Haven, Florida. Samples were transported to this laboratory in a
refrigerated shipping container by bus. A schedule for handling samples was arranged to
permit analysis within a few hours after collection.
15
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SECTION 8
RESULTS
8.01 General Conditions
Data were collected and reviewed for purposes of this investigation from April 19,
1967, through June 30, 1968, covering a total of some 62 weeks. The 1966-1967 citrus
processing season was represented by data for April 19 - June 3,1967. An aerator reduction
gear failure on the latter date resulted in bypassing of citrus wastewaters on June 16,1967.
This wastewater stream was returned to the treatment system on July 4, 1968, after the
closing of the processing season. The aerator was returned to service on July 6. Citrus
wastewaters from this date to early December, 1968, resulted principally from sporadic
processing of lemons and limes and for repacking operations. The main 1967-1968
processing season was represented by data collected from December, 1967, through June,
1968.
Typical analytical data pertaining to the wastewaters are shown in Table 3.
8.02 Flow Data
Flows of raw sewage, raw citrus wastewater, and recirculated sludge were
measured by Kennison nozzles located as indicated in Figure 4. These were arranged with
B-I-F instrumentation to indicate, record and totalize flow of each stream. Clarifier effluent
flow was measured by a Parshall flume as shown in Figure 4, also arranged for indicating,
recording and totalizing the flow.
Flow data collected during the period of investigation are summarized in Figure 6.
Daily sewage flows ranged from 0.723 to 2.02 mgd and averaged 1.106 mgd. Daily citrus
wastewater flows during the portion of the 1966-1967 season covered by the investigation
ranged to 1.122 mgd and averaged 0.935 mgd. During the 1967-1968 season they ranged to
1.631 mgd and averaged 0.528 mgd. It is seen from Figure 6 that offseason flows were
considerable.
8.03 Daily BOD Loadings
Daily BOD loadings are summarized in Figure 7. Combined wastewater BOD
loading ranged to 31,400 pounds per day and averaged 12,200 during the last few weeks of
the 1966-1967 season. During the 1967-1968 season, maximum and average loadings were
22,300 and 6,810 pounds per day, respectively.
Whereas citrus wastewater BOD loading ranged to 29,900 pounds per day and
averaged 11,200 during the latter part of the 1966-1967 season, maximum and average
loadings during the subsequent season were 20,200 and 5,050 pounds per day, respectively.
Daily BOD loading contributed by City sewage during the entire period of the
study averaged 1,315 pounds per day and ranged to 5,840 pounds per day.
17
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Combined wastewater BOD concentrations during the 1967-1968 season are
summarized in Figure 8.
8.04 Suspended Solids
Suspended solids concentration in citrus wastewater and sewage averaged 182 and
162 mg/1, respectively, during the period of study.
MLSS concentrations are summarized in Figure 9. Weekly average concentrations
ranged between 1,630 and 6,550 mg/1 during the period of study.
Clarifier effluent suspended solids concentrations are summarized in Figure 10.
Concentrations varied between 0 and 779 mg/1 and averaged 78 mg/1 during the period of
study.
Pond effluent suspended solids varied from 6 to 160 mg/1 and averaged 32 mg/1.
8.05 Dissolved Oxygen
Dissolved oxygen concentrations in aeration basins 1 (south) and 2 (north) are
summarized in Figures 11 and 12, respectively. Concentration in basin 1 varied from 0.1 to
9.0 mg/1 and averaged 2.8 mg/1 during the study. That in basin 2 varied from 0.1 to 8.4 mg/1
and averaged 2.3 mg/1.
Dissolved oxygen concentrations in the oxidation pond are summarized in Figure
13. These were found to vary considerably with weather conditions, algae blooms, etc., and
ranged from 0.2 mg/1 to 31 mg/1. The average concentration was 9.3 mg/1.
8.06 pH Values
Citrus wastewater pH values were monitored and recorded continuously by means
of a Beckman Model 729 Process Flow Chamber located as indicated in Figure 4. Values
ranged from 4.2 to 11.8 and averaged 7.5. A typical weekly pH record is shown in Figure
14. pH values for sewage clarifier effluent and oxidation pond were determined on
composited samples. These were quite uniform and averaged about 8.0. Values ranged from
7.0 to 10.1.
8.07 Temperature
Temperatures were comparable in aeration basin and oxidation pond effluents
and varied from 17°C. to 31°C., depending upon the ambient temperature. Temperatures
for the entire study period are summarized in Figure 15.
8.08 Sludge Recirculation
Data pertaining to sludge recirculation are summarized in Figure 16. Weekly
average flows ranged from 42 percent to 184 percent of plant influent flow.
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8.09 BOD Removal
Data pertaining to overall BOD removal in the plant are summarized in Figure 17.
Despite an average BOD loading some S3 percent in excess of the design loading during the
latter part of the 1966-1967 season, the average removal amounted to some 94.2 percent
until the aerator failure of June 3, 1967. This failure resulted in decreased removals
indicated in Figure 17 from the week of June 4 through the week of July 9,1967.
Weekly average BOD removals for the 1967-1968 season ranged from 89.0 to 99.0
percent and averaged 95.6 percent.
Despite the aerator failure and subsequent aerator shutdowns to replace reduction
gears in all units, average BOD removal for the period of study amounted to 94 percent.
8.10 Suspended Solids Removal
Sparse data pertaining to suspended solids removals were accumulated and are
presented in Figure 18. Weekly average removals ranged from 54 percent to 96 percent and
averaged 81 percent during the period of study.
8.11 Sludge Volume Index
Sludge volume indices were variable, ranging from a low of 67 to a high of 507
during the period of study. The average SVI value was 263. The data are summarized in
Figure 19.
8.12 Waste Sludge
Data pertaining to waste sludge are summarized in Figure 20. Sludge was wasted
in insignificant amounts until the week of November 26, 1967, at the start of the
1967-1968 season. Sludge wastage during this season ranged to 165,000 gpd and averaged
20,100 gpd.
8.13 Nitrogen and Phosphorous Analyses
Nitrogen and phosphorous determinations were made to determine: 1) if
sufficient quantities of nutrient were available in the influent for efficient bio-oxidation;
and 2) removal of these nutrients during treatment. All data in this regard were collected
during the 1967-1968 season, and these are summarized in Tables 4 and 5.
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SECTION 9
DISCUSSION OF RESULTS
9.01 Flow Data
Figure 6 illustrates that combined wastewater flows were well below the design
average of 3.35 mgd. The maximum weekly average flow was 2.38 mgd, and the maximum
daily flow of record was 3.24 mgd. The average daily citrus wastewater flow of 0.935 mgd
during the latter part of the 1966-1967 season exceeded the design average of 0.85, but the
average flow of 0.528 mgd during the more normal 1967-1968 season was significantly less
than design conditions.
As indicated in Figure 6, daily citrus wastewater flow were subject to considerable
variation. The erratic flow pattern, in conjunction with high and variable BOD loadings,
contributed significantly to difficulties in controlling MLSS concentration and sludge
recirculation rate.
Daily peak flow of sewage was of the order of 3.0 mgd, although occasional peaks
ranged higher. Variable speed drives on the two 3.0 mgd pumps afforded reasonably smooth
and predictable flows throughout the day. Typical weekday citrus plant operations during
the season resulted in cyclical surging of citrus wastewatef flow rates between about 0.5
mgd and 1.25 to 1.40 mgd. The lower rate corresponded to operation of one 350 gpm wet
well pump, while the larger rate resulted from operation of the 1,000 gpm pump. During
weekend or other plant shutdowns, wastewater flow rate usually varied from 0 to less than
0.5 mgd.
The usual operating procedure resulted in cyclical surging of recirculated sludge
between minimum flow rates of about 0 to 0.75 mgd and maxima of 2.0 to 3.5 mgd.
Surging of citrus wastewater and recirculated sludge probably contributed to a
significant problem of solids carryover from the clarifiers. Based on an average sludge
recirculation rate of the order of 1.0 mgd, an estimated maximum momentary flow rate of
7.9 mgd to the head box (Figure 4) would tend to result in a momentary clarifier surface
overflow rate of the order of 1,500 gpd per square foot. The actual effect of such condition
on the overflow rate depends, of course, on the flow rate dampening effect afforded by the
oxidation ponds.
Indicated measures to minimize difficulties associated with flow surges include:
1. Equalization of citrus wastewater flows by means of a suitable surge
pond and variable special pumps,
2. Proper adjustment of sludge recirculation rate controls to minimize
surgings,
3. Increased clarifier capacity, and/or,
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4. Provisions for better flow rate equalization in aeration basins.
9.02 BOD Loadings and Removals
Daily BOD loadings were highly variable, as indicated in Figures 7 and 8 and in
Table 2. These data show that the variability was due mainly to citrus wastewaters. It is seen
further that design loadings were exceeded rather extensively. A revealing summary in this
regard is as follows:
Average Dafly
BOD Loading, Ibs.
Design Actual
Percent of Time
Design Loading
Was Exceeded
City sewage
Citrus wastewater
1966-1967 season(1)
1967-1968 season(2)
Combined wastewater
3,000
5,000
5,000
1,315
11,200
5,050
92
40
1966-1967 season1'"
1967-1968 season(2)
8,000
8,000
12,200
6,810
61
20
Partial, April 19-June 9,1967, only.
<2> December 1,1967 - June 30,1968.
Above described loading characteristics subjected the treatment process to severe
"shocking," which promoted sludge bulking. This phenomenon contributed largely to
frequent difficulties with MLSS concentration control and solids carryover from the
clarifiers.
The effect was often well demonstrated early in the week. In these cases the
treatment process was upset by resumption of citrus processing, following weekend
curtailment. Towards the latter part of the week the sludge evidently became acclimatized
to the loading, and evidence of bulking became less pronounced.
Indicated means for minimizing difficulties resulting from the highly variable
BOD loads involve equalization of citrus wastewater discharges to the plant throughout the
week. Some type of holding tank is the most obvious solution, but potential problem
conditions within such a tank receiving raw concentrated citrus wastes should be
anticipated. Laboratory studies showed that aeration may cause the raw waste to gel
(probably because of high dissolved sugar concentrations) and produce odors, but no
aeration may lead to anaerobic conditions with even more severe odor problems.
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Despite above described loading characteristics, the treatment system afforded
excellent BOD reduction, as attested to by data shown in Figure 17. The oxidation pond
played a significant part in overall BOD reduction during period of excessive solids carryover
from the clarifiers. For example, contributions by the pond to monthly average overall BOD
reductions ranged from 0 to 14.7 percent and averaged 3.0 percent during the 1967-1968
season. During prolonged period of optimum treatment, the pond played a very minor role
in BOD reduction. At times BOD values actually increased somewhat through the pond, due
evidently to carryover of dead algae cells, etc.
Decreased BOD removals indicated in Figure 17 for weeks of June 4 - July 19,
1967, resulted from an aerator failure. Average BOD reductions amounted to 94.2 and 95.6
percent for the 1966-1967 and the 1967-1968 seasons, respectively.
9.03 Wastewater Suspended Solids and Removal
Suspended solids content of raw sewage and citrus wastewater were of the same
general order of magnitude (Table 3). Overall removals described in Figure 18 were affected
significantly by copious quantities of algae cells discharged continuously from the oxidation
pond. Apparent removals of 80 percent or more occurred 59 percent of the time.
As indicated in Figure 10, suspended solids content of clarifier effluent was
variable. Erratic clarification was due to effects of sludge bulking and flow surges mentioned
earlier. The data show that the oxidation pond was of significant benefit in compensating
for poor clarifier performance.
9.04 Mixed Liquor Suspended Solids (MLSS)
The quantity of MLSS under aeration is of prime concern in activated sludge
processes. The design criteria of 10 pounds of MLSS under aeration per pound of daily
influent BOD is a generally accepted level for the extended aeration modification of the
process. To realize this level with the plant design BOD load of 8,000 pounds per day,
would require maintaining a MLSS concentration of 3,000 mg/1 in accordance with the
design control.
In practice the concentration would be adjusted in accordance with actual BOD
loading to maintain the above described 10:1 ratio. The highly variable BOD loads indicated
in Figure 7 made such control so difficult that it could not be accomplished reasonably.
Comparison shown in Figure 22 indicates a trend towards a direct relationship
between BOD removal and MLSS concentration, particularly when MLSS concentration
exceeded 3,000 mg/1. By including Figure 7 in the comparison, it appears that a MLSS
concentration of 4,000 to 4,500 resulted in better BOD removals with BOD loads near or
exceeding the plant design load. On this basis, it is concluded that some 14 pounds of MLSS
under aeration per pound of daily influent BOD is appropriate for conditions at the
Leesburg plant. Equalization of citrus wastewater discharges to the plant would facilitate
MLSS control.
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9.05 Sludge Wastage
Average sludge wastage of 20,100 gpd for the 1967-1968 season was for the
purpose of maintaining a MLSS concentration of 3,000 mg/1 over all but about two weeks
of the season. As shown in Figure 9 such wastage was insufficient to fully satisfy this
objective. Conditions were too erratic for collection of reliable data concerning waste sludge
solids produced per pound of influent BOD. Based on very rough estimates in regard to
average waste sludge solids concentration and solids carryover from the clarifiers, this could
have amounted to some 0.4 to 0.6 pounds per pound of BOD during the 1967-1968 season.
Comparisons in Figure 23 indicate that quantity of waste sludge solids produced
during citrus processing varies inversely with MLSS concentration. Thus, control of MLSS
concentration to a range of the order of 4,500 mg/1 as suggested above would tend to
minimize the solids handling and disposal problem.
Waste sludge disposal facilities were obviously inadequate for long term operation.
The anaerobic digester was too small for the large volumes of sludge produced. The interim
solution adopted was periodic hauling of sludge in tank trucks to a land fill for disposal. It
was recognized at the outset that improvements would be advisable as soon as problems
peculiar to the unique treatment system were clearly defined and evaluated.
9.06 Sludge Recirculation and Sludge Volume Index (SVI)
Sludge recirculation rate must be varied directly as SVI in controlling MLSS to a
fixed level. The relationships are illustrated by comparison of data for weeks of November
26, 1967 through March 31, 1968 in Figure 24. MLSS was controlled within a relatively
narrow range during most of this period, while sludge recirculation rate and SVI gradually
increased.
SVI is dependent to a large extent on factors associated with the particular
wastewater. Citrus wastewaters contain large amounts of carbohydrates. Such compounds
are notorious for promoting growth of filamentous organisms, such as sphaerotilus, during
treatment by activated sludge processes. These organisms yield light, bulky sludges that do
not settle well and thus promote relatively high sludge volume indices. In view of the
relationship between SVI and recirculation rate described above, citrus wastewaters may be
expected to require higher than usual recirculation rates during activated sludge treatment.
These factors are believed largely responsible for solids carryover from the clarifiers
illustrated in Figure 10.
Comparisons in Figure 25 yield some evidence that SVI varies inversely with
MLSS concentration. Thus, positive control of MLSS concentration within the above
suggested range of 4,000 to 4,500 mg/1 could benefit clarification. Comparisons in Figure 26
afford evidence that bulking and solids carryover from the clarifiers might be minimized by
positive control of sludge recirculation rate to an absolute minimum. In general, lower
sludge volume indices accompanied sludge recirculation rates of less than 100 percent of
influent flow.
Equalization of flows and BOD loading would facilitate better control of MLSS
concentration, sludge recirculation and SVI.
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9.07 Dissolved Oxygen Levels
Inspection of Figure 21 shows that dissolved oxygen levels were generally higher
in aeration basin No. 1 (south) than in No. 2 (north). From the week of September 24,
1967, through the week of March 31, 1968, dissolved oxygen concentrations were
consistently higher in No. 1. This was accounted for by short circuiting in the head box
(Figure 4). Due to the arrangement of Kennison nozzles and the two mud valves serving the
basins, basin No. 2 received a disproportionate amount of recirculated sludge. This
condition was alleviated by baffling late in March, 1968.
Comparison of Figures 6, 7 and 21 shows that dissolved oxygen concentration in
the aeration basins varied inversely with flow and BOD load, as would be expected.
From Figures 10 and 13, it is seen that dissolved oxygen concentration in the
oxidation pond appeared to be affected in varying degrees by solids carryover from the
clarifiers. Weather conditions and algae blooms were probably of more overall consequence.
9.08 pH Value and Temperature
Despite wide variations in citrus wastewater pH value, as indicated by Figure 14,
average pH value of this stream was about 7.5. Buffering capacities of City sewage and
mixed liquor were sufficient to yield relatively uniform pH values of the order of 7.5 to 8.0
in the aeration basins.
Although citrus wastewaters were quite warm, temperature of mixed-liquor was
relatively uniform and followed seasonal patterns.
9.09 Nutrient Removal
The treatment would be expected to yield a final effluent containing little
ammonia and organic nitrogen. Nitrate concentration would be expected to increase during
treatment A review of Table 5 shows that such expected results were obtained. Comparison
of data in Table 5 for the period of January 17 through May 24, 1968, shows a direct
relationship between clarifier effluent suspended solids (bulking) and organic nitrogen in the
effluent It is indicated that the effect of bulking extended through the oxidation pond,
where there was a substantial increase in ammonia nitrogen as well as in organic nitrogen.
It is seen in Table 4 that average nitrogen removal through the clarifiers amounted
to about 69 percent. There was an indicated additional removal of about 7 percent in the
oxidation pond. This is not regarded to be of particular significance, in view of the
variability in analytical results.
: From Table 4, average phosphorous removal amounted to about 53 percent, and
the oxidation pond afforded no additional removal. Average removals through the clarifiers
and pond during the period of phosphoric acid addition were 70 and 61 percent,
respectively, as compared to 34 and 31 percent after phosphoric acid addition was
discontinued. During these respective periods BOD:phosphorous ratios were 53:1 and 70:1.
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Since an average daily volume of waste sludge amounting to some 20,100 gallons
was removed from the system during the 1967-1968 season an attempt was made to
determine the effect on overall removals reported in Table 4. A very limited amount of
analytical data was obtained on the sludge. These data indicated that nutrients were
removed largely in the waste sludge. Although the data pertaining to nitrogen were rather
inconsistent, they show that practically all nitrogen removal was accounted for in the
sludge. It was indicated that phosphorus removed in waste sludge amounted to about 94
percent of the overall removal reported in Table 4.
It is generally accepted that BOD:nitrogen ratios of the order of 15:1 to 20:1 and
BOD:phosphorus ratios of the order of 80:1 to 100:1 are required for optimum biological
treatment of wastewaters. Extensive analytical data collected during laboratory and pilot
plant studies preceding plant design indicated that raw combined wastewaters would contain
ample nitrogen, but that they would be deficient hi phosphorus. Data in Table 4 indicate
opposite conditions hi regard to raw wastewater nutrient levels. Although some
consideration might be given to feeding of a nitrogen compound rather than phosphoric
acid, excellent BOD reductions were obtained despite the indicated nitrogen deficiency.
9.10 Plant Equipment
Principal inadequacies in plant equipment were found to deal with waste sludge
disposal, sludge recirculation pumps, clarifiers, and citrus wastewater flow control.
Inadequacies in waste sludge disposal facilities were mentioned above under
"Sludge Wastage." Improvements to be considered might include digestion facilities, either
aerobic or anaerobic. However, observed dewatering characteristics of undigested waste
sludge appeared good. Further studies might indicate economic advantages for unproved
thickening facilities for undigested sludge to be used in conjunction with vacuum filtration,
centrifugal filtration, or increased drying bed capacity. In any case, operating procedures
should be improved to include daily wastage of sludge from clarifiers at highest practical
solids content.
It was assured by the manufacturer that vertical turbine pumps would afford
satisfactory service for anticipated recirculated sludge. With this assurance, such pumps were
selected as an economic measure. Excessive outages were experienced as a result of solids
characteristics. Undegraded gross solids were found to foul impellers and bearings. Stringy
solids such as hair were particularly troublesome in fouling bearings. It is possible that such
difficulties could have been minimized by different bearing materials, such as Teflon.
As mentioned previously, flow surges and bulking of sludge resulted in
clarification problems. It was apparent that clarification of the high SVI solids characteristic
of citrus wastewaters was quite sensitive to turbulence in the clarifiers. High sludge levels
prevailed because of the relatively high sludge volume indices. Under such conditions, cross
members and other obstructions hi the upper portion of the clarifiers contributed to
intolerable velocities, particularly at high flow rates, that caused solids to carry over the
wiers. Further studies are required to determine a more suitable design overflow rate.
Apparently this rate should be substantially less than the design value of 750 gpd per square
foot that was employed, although the latter is considered conservative in usual design
practice.
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As mentioned previously, equalization facilities for citrus
wastewaters would afford better control of such variables as MLSS and
sludge recirculation rate. Clarification would benefit as a result of
improved sludge volume indices and reduction of flow surges.
9.11 Cost of Treatment
For the 1969-70 season the Leesburg Plant processed ...
6,785,000 boxes of fruit and sent 996,000# BOD to the city treatment
plant for treatment.
Cost of Treatment $9,442.00
Waste Load - #BOD 996,000#
Fruit Processed - Boxes 6.785X106
Treatment Cost
$/#BOD $.0095
$/Box Fruit $.0014
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SECTION 10
ECOLOGICAL STUDY
10.01 GENERAL
A detailed ecological survey of the Leesburg wastewater treatment facility was
made by Dr. James B. Lackey to characterize biota associated with the treatment process.
At the time of the facility to characterize biota associated with the treatment process. At
the time of the survey the plant was operating effectively and BOD removal averaged better
than 95 percent.
10.02 LEESBURG EXTENDED AERATION SYSTEM
Over a period of several years, intermittent observation of the Leesburg situation
exhibited that: (1) a high degree of BOD removal had not been achieved; (2) combinations
of citrus waste and domestic sewage produced a varied biota in a pilot plant trickling filter
experimentally operated; (3) large quantities of citrus waste solids entered the canal which
extended out to Lake Griffin; (4) a great deal of gassing occurred in this canal and that
sludge banks had formed therein; (5) in this canal containing the combined waste, a large
and heterogeneous population of algae and protozoa was found,
On March 10, 1969, microbiota at the Leesburg plant were studied. A qualitative
examination of the sludge floes in the aeration chambers, of the growths on the clarifier
walls, of the rising sludge in the polishing pond, and of the polishing pond (final) effluent
was made and the results are exhibited in Table 6. Mixed liquor in the aeration basins was a
light brown mixture of debris, bacteria, and animals. No photosynthetic organisms were
present in the mixture. Bacteria were predominant and typical of biota developed on a
complex organic substrate, actively carrying on conversion to a simple substrate. Free living
bacteria were scarce; however, bacterial masses, typical colonies of Zooglea, unidentified
filamentous forms and Sphaerotilus were present in vast quantities. As shown in column 1
of Table 6, the remaining organisms (except forAcineta) were consumers of bacteria. They
totaled 7,575 per ml and 7,067 of these were Vorticella, Opercularia, and Epistylis. With
such a predator population, the bacteria should be kept at a high reproductive working level.
The floe in the clarifiers appeared to have excellent settling properties, and the
supernatant (clarifier effluent) was free of suspended solids. Growth on the clarifier walls
was composed of the same organisms found in the aeration basins with an additional five
photosynthetic genera. Three were blue—green algae with Euglena gracilis which is indicative
of simpler organic compounds available for uptake. Navicida, the dominant one of these five
is probably more dependent upon nitrogen and phosphorus.
The polishing pond was green in color, with a visibility of about two feet. Its
effluent was of excellent clarity and free of odor. Its biota contained 11 photosynthetic
species to 9 colorless species. However, green algae were predominant and a small
29
-------
filamentous green (unrecognized) was the most abundant. Three Volvoades and one
Euglena indicated a good uptake of soluble organic matter, but the remaining seven species
are known to utilize nitrogen and phosphorus. The numbers present indicate considerable
uptake.
The algal population should insure good oxygenation despite an indication that
substantial quantities of organic matter remain in the clarifier effluent and exert a high
oxygen demand. This is supported by the fact that Trepomonas, Hexamitus, and
Gastronauta, which tolerate low oxygen tensions, were found in the sludge which floats up
from the bottom of the oxidation pond.
The Leesburg plant was operating successfully and had a balanced biota; however,
the balance between efficient and inefficient performance is delicate. A sudden change such
as a large slug of peel oil or alkali could adversely affect the treatment process.
Organisms in the oxidation pond effluent that are contributed to Lake Griffin are
acceptable species. Together with the biota presently existing in the lake, they should be
able to mineralize the increased fertilization. Since the biota concerned is a balanced one,
and of the type desirable in lake water of good quality, it is beneficial to the lake.
30
-------
TABLES
-------
TABLE 1
CHARACTERISTICS OF TREATMENT PLANT FACILITIES
Sewage Facilities:
Comminutor
Capacity, mgd 6.0
Degritter
Type Air
Capacity, mgd 6.0
Wet well pumps
Number 2
Drive Variable speed
Capacity (each), gpm 2,100
Head, ft. 40
Citrus Wastewater Facilities
Wet well pumps (at citrus plant)
Low service
Number 2
Type Non clog wet pit
Capacity (each), gpm 350
Head, ft. 15
High service
Number 1
Type Non clog wet pit
Capacity, gpm 1,000
Head, ft. 36
T-l
-------
TABLE 1
(continued)
CHARACTERISTICS OF TREATMENT PLANT FACILITIES
Phosphoric acid feeding equipment
Storage tank capacity, gal
Feed pumps
Number
Type
Combined Wastewater Facilities
Aeration basins
Number
Capacity (total), MMG
Detention (design), hours
Aerators
Number
Type
Horsepower (each)
Clarifiers
Number
Type
Diameter, ft
Detention (design), hours
Surface overflow rate (design) gpd/sq. ft
Weir overflow rate (design), gpd/lin. ft
Sludge recirculation pumps
Number
Type
1,500
Wallace & Tiernan A747
single head metering
2
3.26
24
Mechanical
60
Suction (Eimco)
55
2.5
750
10,000
Vertical turbine
T-2
-------
TABLE 1
(continued)
CHARACTERISTICS OF TREATMENT PLANT FACILITIES
Sludge recirculation pumps - (continued)
Capacity (each), gpm
Head, ft
Waste sludge pumps
Number
Type
Capacity (each), gpm
Head, ft
Chlorination equipment
Chlorine storage
Feeder capacity, lbs/24 hours
Oxidation Pond
Depth (approx.), ft
Area (approx.), acres
Capacity (approx.), MMG
Detention (design), hours
Thickener
Diameter, ft
Capacity, gallons
Digesters
Large
Type
Diameter, ft
Capacity, gallons
1,400
25
Non clog wet pit
150
25
1-ton containers
1,000
3
5
4.40
31.5
50
157,000
Floating cover-unheated
50
150,000
T-3
-------
TABLE 1
(continued)
CHARACTERISTICS OF TREATMENT PLANT FACILITIES
Digesters - (continued)
Small
Type Fixed cover-unheated
Diameter, ft. 25.5
Capacity, gallons 76,000
Sludge drying beds
Area, sq. ft. 8,590
T- 4
-------
TABLE 2
cn
CITY OF LEESBURG SZWAGE TREATMENT PLANT
MINUTE MAID COMPANY
Federal W
Date
1 467
Apr.l
19
21
24
25
26
27
28
29
30
May
1
2
3
4
S
6
7
8
9
10
11
12
13
14
16
17
IB
19
20
21
22
23
24
25
26
27
28
29
30
31
June
1
2
3
4
5
6
7
a
9
10
11
12
13
14
Wee
W
F
M
T
W
T
F
5
S
M
T
W
T
F
S
S
M
T
W
T
F
S
S
M
T
W
T
F
5
S
M
T
W
T
F
S
S
M
T
W
T
F
5
S
M
T
W
T
F
S
S
M
T
W
ID
(2)
(3)
ln!lu<
m Flow, M Gal.
f Minute
k Maid Cily
900
919
922
72
980
961
1 ,017
914
48
685
1,026
1,048
983
1,015
1,021
88
101
1,106
1,089
692
1,080
991
48
45
1,017
1,017
1,029
994
933
155
722
312
R64
962
880
861
82
1,008
. 963
1,01 1
1,023
248
961
1,004
1,038
1,041
1,122
1,099
897
488
1,0?5
Not inc
Sludge
1,020
1 ,013
919
1 ,087
1,051
1,018
907
841
962
956
976
972
967
978
913
1,023
942
965
1,024
1,024
978
886
1,071
970
966
976
950
926
870
1,042
1,042
980
982
959
961
890
983
948
905
929
896
792
960
949
882
911
909
848
772
953
902
luding was
(1)
1,920
1,932
991
2,067
^,032
2,055
1,621
889
1,648
1,982
2,024
1,955
1,982
1,999
1,001
1,124
2,046
2,054
1,716
2, 104
1,969
934
1, 116
1,987
) ,985
2,005
1,944
1,861
1,025
1,764
1,354
1,844
1,944
1,839
1,B22
972
2,045
1,956
1,868
1,940
1,919
1,040
1,921
1,953
1,920
1,952
2,031
1,947
1,669
1,441
1 ,927
S
MGD
660
«.
770
994
1,267
1,182
1,597
1,034
866
1,451
1,477
1,310
1,256
1,321
1,348
1, 342
1,108
,716
,482
,426
,545
,239
, 194
,530
,563
, 181
959
1,079
985
932
518
643
1,027
1,428
1,556
1,225
1,420
1,382
1,455
1,483
1,345
1, 142
,235
,246
,352
,407
,306
,369
,404
,335
1,611
u d
Perce
34. 4
8. 0
1. 1
7. 7
8. 1
62.4
67.3
87. 7
lib
52.5
73. 2
73. 0
6 '.0
63. 4
66. 1
135
119
54. 1
83. 5
86. 4
67. 8
78.5
133
107
77.0
78. 7
58.9
49.3
58.0
96. 1
52. B
36. 3
34.9
52.8
77. 7
85. 4
126
69.4
70. 7
82.6
77. 9
76. 4
70. 1
110
64.3
63. a
70. 4
72. 1
64.3
70. 3
84. 1
92.6
83 6
Su.per
r,l (3) Liquor
1 ,710
2,980
3,440
3,400
3,630
3,710
3,520
thickener
3,810
I, 500 gal. 3 ,810
4,080
4,730
6, 160
4, 130
3,000 gal 4, 760
5, 100
5, 110
5, 170
5,730
5,710
1,875 gal. 5, 170
5,730
5,890
5,820
6,360
6,380
3,000 gal. 5,980
6, 110
5,900
6, 140
6,360
6,000
5,920
5,860
5,880
6,220
7,020
4, 800 gal. 6,540
6,280
6,500
6,680
6,300
5,240
5,300
5,700
5,620
5,760
5,600
5, 600 gal.
5,840
5,760
5,440
— Tr-s
de d Sol
Clanfx
EfHue,,
17
13
1 1
34
11
14
16
43
667
18
53
13
217
29
46
48
70
19
65
206
36
23
44
14
20
180
132
168
44
30
162
18
60
24
96
0
546
202
78
60
1 ID
78
256
66
278
420
144
86
114
..umPv
i d i ma
Effluen
56
22
28
38
43
24
59
31
37
52
44
40
42
36
55
48
48
45
19
22
39
5
0
7
6
4
70
64
42
66
78
40
10
10
50
82
58
48
64
66
62
54
70
74
B2
82
90
/' 5 - Day BOD
combined
t Maid
4, QUO
1,200
1,117
416
1,467
2,550
884
978
1,213
1,650
299
2,400
1 ,685
1, 142
1,750
1,200
2,150
367
1,113
771
1,033
975
197
383
820
1,100
927
1, 167
1,394
800
1,433
1,233
1,000
1,367
2,000
1,238
1,666
1,433
1,186
1,300
1,800
2,750
1,875
2,200
1,800
City
164
174
47
300
130
285
96
46
75
68
195
210
147
92
70
69
70
80
179
91
83
100
118
158
142
79
110
LOB
105
225
89
40
20
127
141
143
269
56
32
129
103
132
113
42
(5)
1,960
1,077
S87
309
765
1,290
477
516
687
862
201
1, 120
944
736
915
648
253
L06
683
452
664
541
105
128
497
633
514
651
297
390
503
625
515
664
286
711
928
818
639
693
528
1,430
1,028
1,241
980
«• in
RW
- LEESBURG, FLORIDA
C 1 Ad t
m R / 1
Clarilier
Effluent
14
38
5
21
54
26
315
42
37
30
120
32
30
49
94
10
27
86
22
26
8
7
a
3
1
8
1
41
26
239
76
72
87
101
288
257
Effluen
21
20
19
22
40
31
18
23
25
24
23
22
16
16
17
25
36
35
23
17
19
20
21
19
21
19
19
23
20
28
22
10
17
26
26
28
30
47
122
(5)
(6)
(7)
(8)
t % Liquor
98.9 1.0
1. 1
97.0
96.6
92 9 1.0
94.8 0.8
97.6 0.8
96.2 1.3
95.5 5 0
96.4
88. 1
97. 1 4. 3
97.7 0.6
97.5 0.7
98. 3
97.4
90. 1 1. 6
66.0 0.4
94,9 0.3
94.7 0.3
97. 4
96. S
81.0 1.6
83.6 1.5
96.2
96.7 0.7
96.3
97. 1
92. 3
94.9 0.5
94.4 5.0
96.5
96.9
97.4
90.9
96.3 1.3
97.0 0,9
96-3
87.4
0. 2
0. 2
87.6
0,2
0. 1
6 -day BOD values
4-day BOD value*
Effluent Effluent
0.05 22.5
03 28 4
0.5 25 8
0.4 19.4
0.9 8.5
1.6 7.5
3.5 5.5
4.0 9.0
0. 5 14. 3
0.7 5 . .7
0.5 12.4
0. 4 19. 3
0.4 19.2
0.2 6.2
1.3 6.8
1.7 5.0
0.5 25.8
0.5 9-0
3.6 7.3
0.9 75.0
0.9 56.9
0.3 12.4
0.2 9. 7
0.3 0.3
0.1 2.8
Maid
29,970
9,430
9 ,730
250
1 1 ,990
19,740
7,230
8,450
11, 170
12 .svn
120
13.700
14,410
9,980
14,331
10,150
1,580
309
10,260
7,000
5,960
8.780
79
143
6,946
9,330
7,950
9,670
1,800
4,820
3,730
8,880
8,020
10,020
1,370
10,960
13,990
9,910
9,520
10,950
3,720
22,030
15,690
19,030
15,620
City
1 .400
1 .470
402
2,300
1 , 180
2,780
841
390
593
514
1 , 370
1,665
1, 180
749
567
556
532
682
1,400
731
1 ,060
709
738
1,050
1,280
1, 140
642
871
783
912
1,950
727
327
160
943
1,160
1,130
2,080
423
248
855
824
1,040
831
319
45 P.M.
Tutal
31 , iTO
10,900
10, 130
2,550
1 J, 170
22,520
8,070
8,840
1 1, 760
13 ,OBO
1,490
15.390
15.590
10,730
14,900
10,710
2, 110
991
11,660
7,730
7,020
9,490
817
1, 190
8,230
10,470
8,590
10, 540
2, 540
5, 730
5,680
9,610
8,350
10, 180
2,313
12,120
15, 120
11,990
9,940
11,200
4,580
22,850
16, 730
19,860
15,940
R.-marks
(6)
(?)
(6)
(8)
-------
TABLE 3
CHARACTERISTICS OF TYPICAL WASTEWATERS
Citrus Wastewater
Combined
Wastewater
Constituent
BOD (5-day), mg/1
Solids:
Suspended, mg/1
Settleable, ml/1
Nutrients, mg/1:
Nitrogen (total)
Phosphorus (total)
BOD: Nutrient Ratio:
Nitrogen
Phosphorus
pH value
City 1966-67 1967-68 1966-67 1967-68
Sewage Season Season Season Season
139 1470 1044 782 409
149 144 196 148 183
6 60 20 21 8
17.2
7.9
31:1
57:1
8.2 8.4^ 8.0^ *) 8.0 7.9
Subject to extreme variation.
T-6
-------
TABLE 4
NUTRIENT LEVELS AND REMOVALS
BOD.-Nutrient Ratio
Sample
Date
1967
Dec 14
16
20
23
27
29
1968
Jan 3
5
10
12
17
19
24
26
31
Feb 2
7
12
14
16
22
24
28
Raw Combined
Wastewater
Nitrogen
39:1
31
33
33
16
39
33
34
25
30
37
24
42
33
42
43
46
-
27
30
36
30
28
Phosphorus
26:1
17
66
60
29
78
53
62
30
63
75
71
77
63
88
80
88
-
49
61
56
69
65
Dosed(1)
Wastewater
Phosphorus
97:1
79
45
44
23
55
46
53
27
52
61
55
60
51
71
66
72
-
40
51
46
53
47
Removal. %
Nitro
Clarifier
89
92
92
95
94
92
95
93
94
94
85
70
-
72
12
60
69
67
64
87
-
13
22
gen
Pond
79
90
91
94
93
91
93
92
94
95
93
95
86
85
90
87
76
82
77
85
69
74
66
Phosphorus'"*)
Clarifier
63
66
40
39
71
40
84
86
83
85
84
41
-
76
41
71
75
45
63
67
7
4
39
Pond
61
49
44
48
62
59
70
75
89
79
86
75
68
60
75
74
65
72
65
65
54
36
37
T-7
-------
TABLE 4
(continued)
NUTRIENT LEVELS AND REMOVALS
BOD : Nutrient Ratio
Raw Combined Dosed
Removal, %
Sample
Date
1968 -
Mar 1
6
8
13
Apr 3
5
10
12
17
26
May 3
17
24
Average
Wastewater Wastewater
Nitrogen
(continued)
30
25
14
14
29
33
-
31
23
33
26
31
40
31:1
Phosphorus Phosphorus
84 65
61 54
25 24
47 41
75
89
-
53
49
65
62
76
94
57:1<2) 53:1
Nitr
Clarifier
44
90
86
13
-
82
20
71
64
60
70
76
60
69
og en
Pond
74
79
75
50
-
39
61
32
49
57
55
52
51
76
Phosphorus
Clarifier
-
85
83
37
-
21
20
-
41
25
80
34
15
53
(3)
Pond
41
48
58
34
21
26
40
6
41
14
54
34
39
53
Raw combined wastewater dosed with phosphoric acid through April 2, 1968.
Average through March 13, 1 968 only, 59:1.
Based on dosed wastewater from December 14, 1967 - May 24, 1968.
T-8
-------
TABLE 5
ANALYSES FOR NITROGEN AND PHOSPHORUS
(Results in mg/1)
R_a«r Combined Wast«w_ate_r CU_rifier Effluent _Qxidation Pond Effluent
„ , Nitrogen, as ~ BQD Nitrogen, as_N BOD Nitrogen, as K BOD
oTte NH3 Org. ~NO3~ Phos.lU SS<2> May NHj Org. NOj_ Pho..tD SS
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
FIGURES
-------
FIGURE
0
-------
FIGURE 2
TTl
LXD^af0<^TN<7
L4K§JMl££ILid£
B ' ?.^I3 SB
-^ ^^^= F^V'
Lake
IA COMPANY
f Florido
AND EIDSNESS, INC
-------
4 HOUM
oooe
PULP • KB. •V-PmOUGT>
VAPOR •••••••••••
UNCt NOT LAMLE0 Oil STMMUZEO ARC U»EO WATE1I
O
<=
SO
m
CO
-------
cur _
SEIAtE
PARSHALL
FLUME
CITRUS IASTEIATEH _
FROI PlWPinii STATION
AERATION BASINS
"f:gSgi
•<:-S >3~
" > 5 "* ° y "
°*"?>is
:gf= o 3s
"ilz|S«
s > i-
(PHOSPHOAIC \
ACID STORACE j
-OpH RECORDER
HEAD
B01
o
CHLORINE FROI _
I-TOM GOUT*I HERS
SPLITTER
ton
,
:R
CLARIFIERS
(21
1
H.
r
CHLORINE
ESIDUIL
-JESIDU
PtRSHtLL
FLUU
HASTE SLU06E
OIClSItRS
1
© - KENBISON
OUTOIUTIC SAIPLER
(FLOU PIOnillTIONtL)
011 DAT I ON POND
>_TO SLUDGE
OR)INC tltS
_ TO
LAKE
-------
FIGURE 5
DAILY OPERATION
RECORD
City of Leesburg
Sewage Treatment Plant
24-hr, period ending on:
, , 19
Weekday Month Day Year
FLOW DATA (Figures in thousand gallons, as recorded on totalizers.
Readings taken at M each day.)
Raw Minute Maid
(Citrus) Waste
Present Day
Previous Day
Difference
Raw City Sewage
Total Flow
(Clarifier Effluent)
RECIRCULATED SLUDGE
Present Day
Previous Day
Difference
% Of Total Flow
WASTE SLUDGE - (Hours pumping into each)
Head Box
Pump No. 1
Pump No. 2
Total Hours
Pond
Thickener
PHOSPHORIC ACID FED:
Pump #1
Present Day
Previous Day
Difference
Pump Setting
#1 #2
TOTAL:
CHLORINE FED:
Cylinder Weight, Ibs:
Prev. Day
Pres. Day
Difference
Avg. Residual
Chlorine
Maintained
mg/1
TOTAL:
ROUTINE SAMPLING AND TESTING RESULTS
TEST
Sampling
Point
Type of
Sample
Raw Sewage Cent. Composite
Raw Citrus " "
Combined Waste Constructed
grab-
M
Aerator Eff.
Clarifier Eff.
Return Sludge
_M
M
grab-
M
M
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Temp
°C
_E5_
D. Oxy.
5-day BOD
mg/1
-r
3ett. Solids
ml/1
Susp. Solids
Tot, mg/11 % Volatile
REMARKS:
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-------
FIGURE
TYPICAL WEEKLY pH RECORD
CITRUS WSTEUTER
THE COCA-COLA COMPANY
FOODS DIVISION
t««iburg, Florida
BLACK, CROW AND EIDSNESS, INC.
Enfineert
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-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
APPENDIX
-------
LABORATORY STUDIES
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY, FOODS DIVISION
LEESBURG, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
During December 1966, January, and February 1967, a series of laboratory tests
were conducted at the Phelps Research Laboratory. The purposes of these tests were:
1. To develop a biological floe acclimated to a 50-50 mixture of sewage
and citrus waste;
2. To establish the biological oxidation rate (Kj) for citrus waste and for a
50-50 mixture of citrus waste and domestic sewage from the Leesburg
area;
3. To determine the effect of various mixed liquor suspended solids
(MLSS) concentrations on the removal of BOD and the buildup of
sludge mass.
Test No. 1
Purpose: Acclimation of a biological floe.
Procedure:
Twelve liters of a 50-50 mixture of degritted Leesburg sewage and citrus waste
were placed in a 15-liter container. One liter of returned activated sludge from the
University of Florida Campus Sewage Treatment Plant was added and the mixture aerated
for 24 hours.
At the end of 24 hours the air supply was cut off and the mixture allowed to
settle for 30 minutes. Eight liters of the supernatant were decanted from the top, leaving 5
liters of sludge mixture. Eight liters of a 50-50 sewage-citrus waste mixture were added and
the air supply turned on.
This procedure was repeated daily for two and one-half months.
The mixed liquor suspended solids settled rapidly and no odor problems were
experienced.
A-l
-------
In an effort to reduce the amount of travel between Gainesville and Leesburg,
degritted sewage from the campus plant was substituted for the Leesburg sewage at the end
df the first week. No problems were experienced.
Samples of citrus waste were obtained periodically from the head box at the new
Leesburg wastewater treatment plant. Samples were collected in 13-gallon carboys,
transported to Gainesville, and stored at 4°C. until used. The 50-50 mixture was made up
daily.
On several occasions, the pH of the citrus waste was found to range as high as
12.0 to 12.6. After mixing with sewage, the pH was lowered to 7.0 plus or minus, by the
addition of sulfuric acid. No attempt was made to raise the pH if it was on the acid side of
the scale.
Results:
The biological floe developed without difficulty. No odors were experienced and
the floe settled rapidly.
Test No. 2
Purpose: The determination of biological oxidation rates for citrus waste and a 50-50
mixture of domestic sewage and citrus waste.
Procedure:
A sample of Leesburg citrus waste was collected on December 10, 1966. Serial
BOD dilutions were set up and incubated at 20°C. for 1, 2, 3, 4, 5, 6, and 12 days. The
results were as follows:
Time
(Days)
0
1
2
3
4
5
6
12
BOD
(mg/1)
0
95
472
(590)*
650
766
857
907
Calculated BOD
Kj = -0.106 La
0
246
442
592
710
804
877
1081
Values
= 1141
*No dilution within range. Estimated.
A-2
-------
Judging from the difference between the first and second day BODs, a significant
lag appears. This is probably due to the fact that the citrus waste was seeded with normal
domestic sewage and the sewage biota had to be acclimated to the citrus waste.
Using the slope method suggested by Thomas, values for Kj and La were
calculated and found to be as follows:
K! = 0.106
La=1141mg/l
Using these values, the theoretical BOD values were calculated and included in the
above table.
Samples of Leesburg citrus waste and Leesburg domestic sewage were collected on
December 29, 1966. Serial dilutions were set up on a 50-50 mixture and incubated at 20°C.
for 1, 2, 3, 4, 6, and 10 days. The results were as follows:
Time
(Days)
0
1
2
3
4
6
10
BOD
(mg/1)
0
468
736
1446
1544
1792
2312
Calculated BOD
Kj= -0.101 La
0
502
880
1226
1475
1833
2199
Values
= 2438
Using the slope method suggested by Thomas, Kj and La values were calculated
and found to be:
K! = -0.091
La=2623
The graphical method suggested by Thomas and Tsiroglou's daily difference
method were also used to calculate Kj and L&.
A summary of the values is given below:
Method Kj La
Thomas'Slope Method 0.091 2623
Thomas' Graphical Method 0.088 2644
Tsiroglou's Daily Difference
Method 0.125 2048
Average 0.101 2438
A-3
-------
Using the average values for K j and La, the theoretical BODs were calculated.
Test No. 3
Purpose: To determine the effects of various mixed liquor suspended solids (MLSS)
concentrations on the removal of BOD and the buildup of sludge mass.
Procedure:
Four 15-liter containers were filled with 12 liters of a 50-50 mixture of Leesburg
citrus waste and domestic sewage. Varying amounts of an acclimated biological floe were
added to each unit and the units aerated for 24 hours. Samples were withdrawn from each
unit at predetermined time intervals and the BOD and suspended solids determined. A
summary of the results is given below:
Test A Test B Test C Test D
Time 250 ml 500 ml 1000 ml 1500 ml
Hours BOD MLSS BOD MLSS BOD MLSS BOD MLSS
0 1032 1084 1213 1208 899 1240 1088 1268
2 645 1150 599 1160 554 1310 511 1140
4 506 1200 500 1210 432 1290 410 1270
6 398 1180 373 1300 336 1290 329 1260
8 338 1180 286 1170 244 1220 224 1320
12 165 1020 122 1490 117 1340 61 1400
24 115 1110 102 1210 97 1310 79 1300
A-4
-------
TABLE OF CONTENTS
PART 0
SECTION 1 PURPOSE AND SCOPE
SECTION 2 GENERAL DESCRIPTION OF WASTEWATERS
2.01 The Coca—Cola Company Foods Division
2.02 Adams Packing Company
2.03 City of Auburndale
SECTION 3 CITRUS WASTEWATER TREATMENT PLANT
3.01 General Description
3.02 Statistical Study
3.03 Design Criteria
SECTION 4 PLAN OF INVESTIGATION
4.01 General
4.02 Sampling Procedures
4.03 Testing Procedures
SECTION 5 PLANT OPERATION
5.01 Citrus Processing Season, 1968—69
5.02 Problems Encountered
Page Number
1
3-5
3
4
4
7-9
7
8
8
11 -12
11
11
12
13-15
13
14
SECTION 6 HYACINTH STUDY
6.01 General
6.02 Nutrient Uptake
6.03 Hyacinth Plant Characteristics
6.04 Pressed Liquor
17-20
17
17
19
20
SECTION 7 ECOLOGICAL STUDY
7.01 General
7.02 Auburndale Aerated Lagoon System
21 -23
21
21
-------
TABLE OF CONTENTS
PART H
(continued)
SECTION 8
SECTION 9
SECTION 10
KINETIC STUDY
8.01 General
8.02 Laboratory Study
RESULTS
9.01 General
9.02 Hydraulic Loadings
9.03 Organic Loadings
9.04 COD/BOD Ratios
9.05 BOD and COD Removals
9.06 Suspended Solids
9.07 Dissolved Oxygen
9.08 Temperature and pH Values
9.09 Nutrient Removals
9.10 Reuse of Treatment Pknt Effluents in
Citrus Processing Plant
DISCUSSION OF RESULTS
10.01 Hydraulic Loadings
10.02 Organic Loadings and Removals
10.03 COD/BOD Ratios
10.04 Dissolved Oxygen
10.05 Nutrient Removal
10.06 Reuse of Treatment Plant Effluents in
Citrus Processing Plant
10.0? Cost of Treatment
Page Number
25
25
25
27-29
27
27
27
28
28
28
28
28
29
29
31-34
31
31
32
32
33
33
34
11
-------
TABLE OF CONTENTS
PART H
(continued)
Page Number
SECTION 11 AERATED LAGOON DESIGN 35 - 36
11.01 General 35
11.02 Experimental Data 35
11.03 Design Criteria 36
SECTION 12 SUGGESTED DESIGN PARAMETER
EXTENDED AERATION 37 - 38
12.01 General 37
12.02 Preliminary Background Data 37
12.03 Design Parameters 37
HI
-------
TABLES
PART II
Page Number
Table 1 Wastewater Pond Characteristics T - 1
Table 2 Wastewater Flow Data T - 2
Table 3 Daily Area Precipitation T - 9
Table 4 Raw Wastewater Analyses at Weir No. 1 T - 10
Table 5 Raw Wastewater Analyses at Darby Avenue T — 13
Table 6 Raw Wastewater Analyses at Weir No. 2 T - 14
Table 7 Wastewater Pond Characteristics and Equipment T — 15
Table 8 Treatment Plant Characteristics T -16
Table 9 Average Analyses 2.4-Day Detention T - 18
Table 10 Hyacinth Pond Microbiota T -19
Table 11 Average Analysis 5-Day Detention T - 20
Table 12 Pressed Liquor Analyses T — 21
Table 13 Auburndale Biota T - 22
Table 14 Average Weekly Operating Data
1968-69 Citrus Processing Season T - 24
Table 15 Design Characteristics — Aerated Lagoon
System T - 25
Table 16 Summary of Operations 5 MGD Flow Rate T - 26
Table 17 Summary of Operations 10 MGD Flow Rate T - 29
Table 18 Summary of Average Monthly Operations
1968-69 Citrus Processing Season T - 32
Table 19 Summary of Nitrogen and Phosphorous Analyses T — 33
Table 20 Monthly Average Data — Wastewater Treatment
Plant T - 34
-------
FIGURES
PARTH
Page Number
Figure 1 Location Map — The Coca—Cola Company
Auburndale, Florida F — 1
Figure 2 Vicinity and Location Map — The Coca—Cola
Company — Auburndale, Florida F — 2
Figure 3 Wastewater Treatment Plant F — 3
Figure 3a Wastewater Sources - Citrus Concentrate
Plant and Hi "C" Plant F - 3a
Figure 3b Wastewater Sources — Adams Packing Company F — 3b
Figure 4 Daily Average Flow at Weir No. 2
1966-67 Citrus Processing Season F — 4
Figure 5 Daily Peak Flow at Weir No. 2
1966-67 Citrus Processing Season F — 5
Figure 6 Daily Minimum Flow at Weir No. 2
1966—67 Citrus Processing Season F — 6
Figure 7 BOD Load at Weir No. 2
1966-67 Citrus Processing Season F — 7
FigureS BOD:Nitrogen Ratio at Weir No. 2
1966—67 Citrus Processing Season F — 8
Figure 9 BODrPhosphorus Ratio at Weir No. 2
1966—67 Citrus Processing Season F — 9
Figure 10 BOD Removal Rate F - 10
Figure 11 Daily Operation Record F — 11
Vll
-------
APPENDICES
PART II
Appendix 1 Grab Sample Analyses Taken During January
and February
Appendix 2 Kinetic Studies — Auburndale Plant
Appendix 3 Kinetic Studies — Auburndale Plant
Appendix 4 Kinetic Studies — Leesburg Pknt
Appendix 5 Theoretical Considerations — Aerated
Lagoon Design
Page Number
A-l
A-2
A-3
A-4
A-5
IX
-------
SECTION 1
PURPOSE AND SCOPE
The purpose of this study was to investigate treatment of a relatively large
quantity of weak citrus wastes from two processing plants; namely, The Coca—Cola
Company Foods Division and Adams Packing Company, along with the treated effluent
from the domestic waste treatment plant of the City of Auburndale. The investigation
included loading parameters, evaluation of plant design, required nutrient levels, operational
control parameters, and a study of the ecology of the raw waste stream, the entire treatment
process, and finally, of the receiving stream. Kinetic studies and nutrient removal by aquatic
plants were also included in this investigation.
Operational parameters such as minimum dissolved oxygen levels, excess sludge
buildup, and sludge recirculation rates could not be fully investigated as previously
anticipated due to the inadequacy of the sludge collection and return system. Because of
this, the plant could not be effectively operated as an extended aeration plant and had to be
converted to operate as an aerated lagoon system. The scope of this investigation was
broadened to include design parameters to treat weak citrus wastes by means of an aerated
lagoon system.
Further study objectives included the possible use of water hyacinths in cattle
feed and the possible reuse of treated wastewater in the citrus processing plant.
Velocity distribution studies in the lagoons using Rhodamine-B dye as a tracer
were unsuccessful due to adsorption of the dye by high solids concentrations in the lagoon
system.
-------
SECTION 2
GENERAL DESCRIPTION OF WASTEWATERS
2.01 THE COCA-COLA COMPANY FOODS DIVISION
Wastewater characteristics and sources are described generally in the Introduction
to Part I of this report. Specific sources and characteristics of individual waste streams were
not included in the scope of this investigation.
Project location and vicinity maps are shown in Figure 1 and Figure 2,
respectively. Sources of wastewater at the Auburndale plant are shown in Figure 3 a.
Measurements of volumes and strengths of wastes from various processes within the plant
will be begun by The Coca-Cola Company during the 1969-70 citrus processing season.
Some investigative work to trace sources of overload throughout the study period indicated
that wastes from feed mill, juice extractor, Hi C plant, and oil recovery processes
contributed significantly to the total waste load. Some typical COD values from both The
Coca—Cola Company and Adams Packing Company are exhibited in Appendix 1. These
values were on grab samples taken during January and February, 1969, and are by no means
to be construed to be typical for all process plants nor all operating conditions.
The citrus processing season at Auburndale usually extends from December
through July, depending upon crop conditions. Processing is slackened or halted for a short
period in March for the midseason changeover to later maturing fruit. During the changeover
and off season the principal wastes are from the repacking, ades and bases, and beverage
operations. The wastewater loadings and volumes during these operations are relatively light.
Wastewater from the concentrate plant is screened to remove peel, pulp, seeds,
and other suspended material. Gross solids are also removed from wastewater from the fruit
unloading and preparation operations and the barometric condensers. Unlike the Leesburg
processing plant, the two wastewater streams are not segregated; therefore, the processing
wastes yield large volumes of moderately low-strength wastewater.
Wastewater volume and strength vary considerably depending upon processing
operations. Poor operation in the feed mill, pressed liquor and oil recovery systems have a
detrimental effect on the biological treatment process. Peel oil is toxic and acts as a
bacteriostatic agent, greatly affecting both the biological process and the major operational
control parameter; namely, the BOD.
Variations in pH values are caused by discharges of caustic during cleanup
operations. However, due to the large dilution, these variations are slight and pH values
average about 7.0.
In general, the wastewaters are deficient in nitrogen and/or phosphate compounds
required for optimum biological treatment.
-------
Total citrus wastewater flow from The Coca—Cola Company at Auburndale is
approximately 20 mgd. Biological and chemical oxygen demands are of the order of 120
mg/1 and 210 mg/1, respectively. The wastewater is discharged into Lake Lena Run and the
entire creek is taken into the wastewater treatment facility.
The citrus processing plant at Auburndale operates on a 24-hour per day basis
during the crop season. Daily production levels during the 1968—1969 processing season
averaged 50,000 boxes of fruit.
2.02 ADAMS PACKING COMPANY
Wastewater characteristics and sources from Adams are essentially the same as
those of The Coca-Cola Company. However, in addition to the concentrate process, Adams
includes wastewater from a sectioning operation in fruit processing and a single-strength
operation in juice processing which produce about 3 mgd of wastewater and average COD
values of the order of 500 mg/1. Sources of wastewater at the Adams Packing Company are
shown in Figure 3b.
Adams' processing season at Auburndale usually extends from November through
July with a brief slackening during midseason.
Wastewater from the concentrate plant, fruit unloading and preparation
operations, and barometric condensers are not segregated. Gross solids are removed by
screening prior to discharge into Lake Lena Run. The process yields large volumes of
moderately low-strength wastewater deficient in nitrogen and/or phosphate compounds.
Wastewater volume and strength have the same degree of variability as those from
The Coca-Cola Company and for the same general reasons.
Total wastewater flow from Adams at Auburndale is approximately 10 mgd.
Biological and chemical oxygen demands are approximately 190 mg/1 and 290 mg/1,
respectively. pH values average about 7.0.
Adams' processing plant at Auburndale operates on a 24-hour per day basis during
the principal crop season. In slack and off seasons principal wastes are from repackaging
operations which yield relatively light flows and organic loadings. Daily production levels
during the 1968—1969 processing season averaged 60,000 boxes of fruit.
2.03 CITY OF AUBURNDALE
The population of Auburndale in 1969 was 7,030. A population of 11,396 is
expected by 1980. The economy of Auburndale is based almost entirely on the citrus
processing industry.
The City of Auburndale sewage treatment plant receives waste from both
domestic and industrial sources. The average daily flows are of the order of 762,650 gpd and
influent BOD's average 225 mg/1.
-------
Industrial wastes from certain manufacturing complexes contain appreciable
amounts of formaldehyde and other toxic compounds. This greatly affects the efficiency of
the biological process and adds an additional organic load and possibly toxic substances to
the treatment plant effluent. Effluent from the domestic treatment plant is discharged
through an 18-inch outfall extending 2,800 feet below the city treatment plant into Lake
Lena Run above the citrus treatment plant. The effluent from the city treatment plant is
included in the wastewater received by the citrus wastewater treatment facility.
The effluent wastewater exhibits BOD's of approximately 75 mg/1. The flow
averages 762,500 gallons per day and contains appreciable quantities of both nitrogen and
phosphate compounds.
-------
SECTION 3
CITRUS WASTEWATER TREATMENT PLANT
3.01 GENERAL DESCRIPTION
The plant was designed for extended aeration of unclarified wastewater with
completely mixed recycled sludge. Two shallow oxidation ponds (in series) were provided
for further polishing of the effluent before discharge into Lake Lena Run. A schematic flow
diagram is given in Figure 3.
The plant consists of four unlined, earthen ponds covering an area of
approximately 23.6 acres. Citrus processing wastewaters (including the effluent from the
City of Auburndale) are delivered, by gravity, to the treatment site by means of Lake Lena
Run. A weir is provided below the treatment plant intake so that the entire run flows into
the aeration pond. Flow rates exceeding 30 mgd (with 40 percent recirculation) overflow
the weir and that portion of the flow bypasses the treatment plant. The aeration pond
covers 3.15 acres, is 11.7 feet deep, has a capacity of 9.7 million gallons (MMG), and is
equipped with six 75-horsepower floating mechanical aerators/3' A float control in the
aeration pond activates each of three transfer pumps which lift the mixed liquor from the
aeration pond to the second pond. The transfer pumps have a total pumping capacity of 42
mgd. Two pumps are equipped with 50 horsepower motors and one pump is equipped with
a 30 horsepower motor. The two larger pumps each have a pumping capacity of 17 mgd and
the smaller has a capacity of 8 mgd. The mixed liquor from the aeration pond flows through
a vented 42-inch discharge line into a distribution trough in the second earthen pond. This
pond serves as a clarifier and has a dual function; namely, sludge settling and collection. The
settling and collection section of the pond covers approximately 2.72 acres, is 14.2 feet
deep, and has a capacity of 9.2 MMG. The remainder of the pond covers 4.1 acres, is 9.7
feet deep, and has a capacity of 11.6 MMG. Sludge collection and recycling is accomplished
by suction-type sludge pickups into a vented 36-inch gravity line back to the aeration pond.
Metering devices' ' include Dall tubes (installed in both the 42-inch transfer line
and the 36-inch gravity return sludge line), transmitters and continuous flow recorders with
totalizers. Flow measurements on the 42-inch transfer line represent the total flow (plant
influent and recirculated sludge); whereas those measurements on the 36-inch gravity line
represent only the recirculated sludge. The daily plant influent is obtained by difference.
The effluent from the settling pond flows by gravity into a third earthen pond
which serves as an oxidation pond. This pond covers 6.85 acres, is 5.0 feet deep, and has a
capacity of 10.5 MMG. A fourth earthen pond (also an oxidation pond) is gravity fed from
the third pond. An area of 6.85 acres is utilized with an average depth of 4.5 feet and a
capacity of 9.5 MMG. The pond effluent is discharged, without chlorination, into Lake Lena
Run.
a Manufactured by Yeomans Brothers Company, Melrose Park, 111.
Manufactured by B-I-F Division, Providence, R.I.
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Flow control baffles were provided in each of the last three ponds to insure better
mixing within each pond and to prevent short circuiting of the treated effluents.
Facilities were included for adding both aqua ammonia and phosphoric acid as
supplemental nutrients. These are added to the mixed liquor in the aeration pond.
No provisions were made for wasting or treating waste sludge. Sludge carryover
from the settling pond to the oxidation ponds will necessitate periodic dredging of one or
both of these ponds.
A summary of wastewater pond characteristics is presented hi Table 1.
3.02 STATISTICAL STUDY
Weirs, level recorders, and automatic sampling devices were installed at points
indicated in Figure 2 to provide design data for Auburndale citrus wastewater treatment
facilities. Weir No. 1 was located in Lake Lena Run below Adams Packing Company. Wen-
No. 2 was located at Recker Highway and included flows from Adams Packing Company,
The Coca-Cola Company, and the City of Auburndale sewage treatment plant
Flows were measured at the above described weirs throughout the 1966-67 citrus
processing season, and the results are given in Table 2. Area precipitation during the season
is described in Tables 2 and 3. Statistical analyses were made for flows at Weir No. 2 as
shown in Figures 4,5, and 6.
Organic loads (BOD) and nutrient levels at Weir No. 2 were analyzed statistically
as shown in Figures 7,8, and 9.
Composite samples were collected and analyzed routinely at each of the weirs
during the first half of the 1966-67 processing season, and two samples were collected at
Darby Avenue (Figure 2). Results of the analyses are given in Tables 4, 5, and 6.
3.03 DESIGN CRITERIA
Basic design of these faculties involves the activated sludge (extended aeration)
process. Plant design criteria was partially based on a statistical study made during the
1966-67 citrus season. Design parameters were primarily based on a survey of the industry
by Fiske and Gay.^ They reported a combined volume from the two citrus processing plants
of approximately 25.5 mgd with a combined organic loading (COD) of 29,500 pounds.
Using the COD-BOD conversion factor suggested by McNary,2 the 5-day, 20°C. BOD
strength would be of the order of 18,500 pounds per day. Design hydraulic and BOD
loadings of 30 mgd and 18,500 pounds per day, respectively, were assumed.
8
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A relatively inexpensive settling basur0' was substituted for conventional
clarifiers to minimize construction costs. Treatment units were arranged to permit
wastewater transfer and sludge recirculation with a single, low cost pump station. The plant
will accommodate hydraulic loadings of 30 mgd with an additional 40 percent of this flow
as sludge recirculation.
Plant characteristics were as follows:
Plant influent, mgd:
Average 15.6
Maximum 30.0
BOD concentration, mg/1 74
BOD loading, Ibs/day 18,500
Recirculated sludge, mgd 12.0 - 26.4
Extended aeration:
Mixed liquor suspended solids:
Concentration, mg/1 (ave) 2,300
Under aeration,
Ibs/lb BOD 10
Total plant area, acres 23.6
Total detention time, days (ave) 3.2
Further details of pond and treatment plant characteristics are described in Tables
7 and 8.
Actual data collected during the 1968-69 citrus processing season indicated
substantial increases in the organic (BOD) loadings. This was due, in part, to unexpected
changes in processing and increased production at both The Coca-Cola Company and
Adams. Production levels during the 1969-1970 processing season increased by 10,000
boxes of fruit per day and are expected to increase yearly by the same for the next few
years.
0 See Section 5.02, first paragraph.
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SECTION 4
PLAN OF INVESTIGATION
4.01 GENERAL
Principal objectives of plant operation during the 1968—69 citrus processing
season were to demonstrate capabilities of the low cost plant and to determine favorable
operating procedures.
The general plan of experimentation involved the variables that were subject to
operational control. These were loading, nutrient level, and sludge recirculation rate. It was
planned to change one of these variables at a time, under optimum conditions, in a series of
tests covering the 1968—69 citrus processing season. However, despite a wide variety of
operating procedures, the mixed liquor suspended solids (MLSS) concentration could not be
increased above about 200 mg/1. It was concluded prior to midseason that the settling basin
did not afford MLSS control because of an inadequate sludge collection system. Due to this
inadequacy, the plan of investigation had to be altered somewhat from the original plan
since the system was operating as an aerated lagoon system rather than an activated sludge
system. Sludge recirculation rates were maintained at 100 percent of the influent flow and
the only control variables were hydraulic loadings and nutrient levels.
Supplementary routine analyses for nitrogen and phosphorous concentrations in
the wastewater and pond effluents were made.
Kinetic studies were performed to determine BOD removal rate coefficients and
temperature coefficients which are necessary in order to design an aerated lagoon system
(see Appendix 5).
Experimentation included an ecological study throughout the treatment system
and also the use of aquatic plants (hyacinths) for nutrient removal. Aquatic plants were
further studied for nutritional value and possible use in cattle feed.
4.02. SAMPLING PROCEDURES
Routine sampling of the combined citrus wastewater flow was accomplished by
means of a Chicago Pump Company "Tru—Test" sampler. Effluent flows from the settling
pond and Polishing Pond No. 2 were collected routinely by means of portable automatic
samplers. Locations of the sampling stations are indicated in Figure 3. Samples were
collected over 24—hour periods in polyethylene containers. Those samples collected in the
"Tru—Test" sampler were maintained at 40° F. in the refrigerated compartment of the
sampler throughout the 24—hour period. Other samples were kept packed in ice in a
polystyrene cooler throughout the same sampling period.
Grab samples were taken from the aeration pond effluent, Polishing Pond No. 1
effluent, and recirculated sludge return line once each 24—hour shift. Plant influent grab
samples were analyzed once each 8—hour shift for COD concentrations.
11
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Automatic samplers, although convenient, do not take truly representative
samples due to the stringy solids in the waste. On several occasions analyses were made on
grab and automatic samples collected simultaneously. BOD, COD, and suspended solids
results generally were higher on the grab samples by 10 to 20 percent. However, all data
presented in this report were based on the automatic sampling procedures described in the
preceding paragraphs. Since the data are consistent, all efficiencies (ratios) are only slightly
affected; influent data may be slightly low.
4.03 TESTING PROCEDURES
All testing procedures were in accordance with "Standard Methods for
Examination of Water and Wastewater," 12th Edition, APHA, AWWA, WPCF (1965).
Routine sampling and testing were accomplished by the operating personnel of
The Coca-Cola Company Foods Division wastewater treatment plant. A summary of the
tests conducted at the plant is shown in Figure 11. Training and supervision were provided
by Black, Crow and Eidsness, Inc.
Weekly composite samples of the plant influent, settling pond effluent, and
Polishing Pond No. 2 effluent were analyzed for forms of nitrogen and total phosphates.
These samples were preserved with mercuric chloride to prevent changes in the nitrogen
balance due to further biological activity. Nitrogen and phosphorous determinations were
made by Black, Crow and Eidsness personnel on a Technicon AutoAnalyzer, Gainesville,
Florida. Samples were transported to the laboratory within 24 hours after collection.
12
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SECTION 5
PLANT OPERATION
5.01. CITRUS PROCESSING SEASON, 1968-69
Plant construction was completed November, 1968. Processing wastes from
Adams and The Coca-Cola Company were received on November 14 and December 2,1968,
respectively. Although citrus processing wastes were received and a detailed sampling
program initiated at the start of the 1968—69 season, the treatment plant facilities were not
fully operative until January 15, 1969. Between January 17 and 20,1969,60,000 gallons of
waste activated sludge from the Leesburg plant were added to the aeration pond in an effort
to rapidly build up the mixed liquor suspended solids (MLSS). However, despite a wide
variety of operating procedures, the MLSS concentration could not be increased above 200
mg/1. It was concluded in February that the sludge collection system was inadequate and
that existing treatment facilities could not be operated as an extended aeration system. BOD
removals between December, 1968, and February, 1969, averaged about 62 percent and
MLSS concentrations averaged 67 mg/1. See Table 16 for average weekly operating data.
Hydraulic loads during the outset of the processing season were about one—half
the design capacity; however, organic loadings (BOD) were almost twice those anticipated.
During March, 1969, the treatment plant was set up to operate as an aerated
lagoon system as described in "Industrial Water Pollution Control" by W.W. Eckenfelder.3
The principal objectives during the remainder of the processing season were to determine
optimum operating conditions and to collect pertinent background data required for design
of an aerated lagoon system.
The Coca-Cola Company halted operations on March 3,1969, for the mid-season
changeover to Valencias and resumed operations April 15, 1969.
Reasonable control was maintained over influent flows and recirculation rates
during the last phase of the research program. Influent flow rates were maintained at
approximately 5 mgd from May 1 through May 19, and at approximately 10 mgd from May
20 through June 13, 1969. Recirculation rates averaged 4.8 mgd and 10.4 mgd, respectively,
during these periods. BOD removals averaged 94.5 percent and 83.8 percent, respectively, at
the 5 mgd and 10 mgd influent flow rates.
Nitrogen levels in the raw wastewaters were low and were supplemented by the
addition of aqua ammonia. BOD:N ratios during the processing season averaged about 20:1,
which is higher than the 30:1 BOD:N ratio recommended by Helmers in a paper by
Eckenfelder.4 Phosphorous levels in the raw wastewater were variable and when necessary
were supplemented by the addition of phosphoric acid. BOD:P ratios averaged 103:1 for the
entire study period and 148:1 and 99:1, respectively, during the 5 mgd and 10 mgd
controlled flow period. These values compare to phosphate levels recommended in the
literature as being adequate for optimum biological activity. It appears that the
supplemental nutrients are required to promote favorable growth conditions at the startup
13
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of a biological system and become of lesser importance once the system is acclimated.
Phosphorus appeared least important after startup, since supplemental phosphorus was
omitted for long periods of tune with little or no change noted in BOD removals. A
BOD:N:P ratio of 150:5:1 appears to be applicable to citrus wastes.
5.02 PROBLEMS ENCOUNTERED
The major problem was the failure of the sludge collection system to collect
sludge, making it impossible to study the design concept involving the extended aeration
process. The sludge collection area was too large and the slopes were too gentle to
effectively move the sludge to the gravity pickups. (A minimum slope of approximately 60°
is suggested, whereas the slope in the sludge collection section of the settling pond was only
about 15°.) Mechanical scrapers may have aided the collection procedure; however, due to
the size scrapers required, the cost would have been substantial.
Minor difficulties were encountered in the metering transmission system on the
transfer lines between the aeration pond and Pond No. 2 (settling pond). This was caused by
air trapped in the transmission system.
Other inadequacies in plant equipment were found in the flow metering system,
transfer pumps, and flotation devices on the mechanical aerators. The low cost metering
system was provided to cover a range of between 5 and 50 mgd and still deliver reasonable
accuracy. However, the Dall tube designed for this flow range operates at subatmospheric
pressures (negative head) at this installation when two or more pumps are operating. This is
not a serious problem so long as the pressure piping from the flow tube to the transmitter is
airtight. Air trapped in the transmitter lines could lead to minor metering inaccuracies. Daily
manual venting of the ah- bleed-off valves is recommended.
High volume, low head lift pumps of the type used in irrigation of citrus groves
were used to provide a low cost lift station to transfer the mixed liquor from the aeration
pond to the higher elevation of the settling pond. This provided a means for gravity sludge
recirculation, thereby eliminating a second pumping station. The lift pumps are extremely
sensitive to small head variations and when all three pumps are operating simultaneously,
the discharge rates are somewhat lower than the rated capacities indicated by the pump
discharge curves.
Only three of the six floating mechanical aerators were operative when plant
operation began in November-December, 1968, due to a design fault hi the flotation devices.
The fourth aerator was placed in service on December 21, 1968, and the fifth and sixth
aerators were in service by January 15, 1969. In repairing the flotation devices, buoyancy
was increased and it was May, 1969, before aerators could be operated at maximum
efficiency.
The fiber glass flotation devices were not properly tested by the manufacturer
prior to delivery to the plant site. Although similar flotation units equipped with smaller
aerators have been successful at other installations, starting the 75 horsepower aerators
created significantly more stress than the fiber glass floats could withstand. Consequently,
14
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small fatigue cracks developed at points of excessive stress and the floats were no longer
watertight. The level of submergence was adversely affected and the flotation units had to
be removed from the system and repaired by reinforcing and filling the floats with bouyant
material. Unless significant changes in design are made on the fiber glass floats, steel floats
with positive flotation are recommended for future installations involving aerators exceeding
60 horsepower.
Earthern aeration basins should be provided with concrete pads or some sort of
stabilizing material below the mechanical aerators. Poor mixing in the aeration basin was
noted during March, 1969. Investigation of the problem revealed that turbulence from the
mechanical aerators had dug hc'es approximately eight feet in depth below the bottom level
of the aeration basin, greatly affecting mixing patterns.
Several thousands of gallons (approximately 3,500) of pressed liquor (toxic) from
Adams and excessive feed mill wastes (high BOD) from both Adams and The Coca-Cola
Company were discharged into Lake Lena Run and subsequently taken into the waste
treatment plant on January 3 and 4, and again on January 6, 1969. This material grossly
overloaded the system. With only four aerators in operation, the required volume of air for
proper treatment could not be supplied. Consequently, the entire system of ponds
developed anaerobic conditions and had to be drained on January 11, 1969.
It is apparent from this study that a generous variety of problems are inherent
during the first year's operation of a new waste treatment facility. Mechanical equipment
requires frequent adjustment and plant operators in many cases are not familiar with the
plant's capabilities nor the degree of variability of the wastewater. Therefore, detailed
research, plant design, and capability evaluations should not be initiated until plant
operations are stable and operators have a thorough knowledge of the treatment process and
waste characteristics.
15
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SECTION 6
HYACINTH STUDY
6.01 GENERAL
The purpose of this study was to examine nutrient uptake by water hyacinths and
to investigate the possible use of these plants in cattle feed.
A hyacinth pond with a total surface area of 1,130 square feet, an average depth
of six feet, and a total volume of 50,850 gallons was constructed of plywood and lined with
plastic in Polishing Pond No. 1. Influent to the water hyacinth pond was pumped from the
effluent from the settling pond. Influent 5-day BOD's ranged from 22 mg/1 to 56 mg/1
during the period of this study. Nitrogen and phosphorous concentrations were well above
those recommended as being sufficient for bio-oxidation. Average total nitrogen
concentration ranged from 3.58 mg/1 to 5.27 mg/1, and average phosphorous concentrations
ranged from 0.75 mg/1 to 0.76 mg/1.
Hyacinths were harvested from Lake Parker, Lakeland, Florida, and a total of 850
pounds of plants were placed in the hyacinth pond at Auburndale on April 22, 1969. The
plants loosely covered an area of 660 square feet out of a total pond area of 1,130 square
feet. Plant root lengths ranged from 6 to 16 inches and averaged 8 inches. The hyacinth
plants were acclimatized for a one-week period prior to experimentation. The investigative
period extended from April 30 through June 30,1969.
Penfound and Earle conducted studies on hyacinth plants in New Orleans,
Louisiana. They determined that the wet weight of hyacinth plants varied from 120 to 180
tons per acre and would yield 7 to 10 tons of dry plant material. Rate of propagation was
also studied and they concluded that ten plants would cover an area of one acre in one
growing season. Our study confirmed this propagation rate since after a one-week period
each plant had produced three new plants. Penfound and Earle further determined that
hyacinths could withstand temperatures of 33°F. for periods of 12 hours with slight leaf
damage; however, 24-hour exposures at 20°F. killed the plants. Temperatures seldom range
below 33°F. at Auburndale for extended periods; therefore, environmental conditions are
ideal for a long growing season. Other observations by Penfound and Earle were that oxygen
levels below dense mats of hyacinths were less than 0.1 mg/1; under closely growing plants
but without a mat, dissolved oxygen concentrations were 0.5 mg/1; where only 80 percent
of the total surface area was covered, dissolved oxygen levels averaged about 1.5 mg/1.
6.02 NUTRIENT UPTAKE
The first phase of study extended from April 30,1969, through May 28,1969. A
2.4-day detention time with continuous flow conditions was employed. Plant root lengths at
the influent end of the hyacinth pond averaged 12 inches, whereas the roots at the effluent
end remained approximately 8 inches long. A slime covered the roots of the plants at the
influent portion of the pond but was absent from those at the effluent end. Dissolved
17
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oxygen concentrations in the influent and effluent hyacinth pond streams averaged 1.9 mg/1
and 1.0 mg/1, respectively. Chemical oxygen demand (COD) reductions averaged 29.9
percent and biological oxygen demand (BOD) reductions averaged 45.2 percent. Organic
nitrogen exhibited reductions of 25.8 percent and little or no changes were observed in the
remaining forms of nitrogen. Phosphate reductions averaged 14.7 percent. A summary of
the 2.4-day detention period data is given in Table 9.
The last phase of investigation covered the period June 2 through June 30, 1969.
A 5-day detention time with continuous flow conditions was employed. Little change was
observed in root lengths during this period of study. Microbiota attached to the hyacinth
roots at the influent portion of the hyacinth pond were studied. Several forms of bacteria,
blue-green algae, green algae, volvocales, zooflagellates, and ciliates were found. These
organisms account for the substantial biological purification observed across the hyacinth
pond. A summary of microbiota found on the hyacinth plant roots and in the influent and
effluent streams of the hyacinth pond are exhibited in Table 10. Dissolved oxygen
concentrations did not deplete as expected due to the fact that we only had approximately
72 percent of the total surface area covered. Dissolved oxygen levels averaged 1.24 mg/1 in
the influent stream and 1.00 mg/1 in the effluent stream. This agrees with the work done at
Louisiana, since Penfound and Earle reported oxygen levels of 1.5 mg/1 with approximately
80 percent of the water's surface covered by plants. An area of 36 square feet of hyacinths
yielded a wet weight of 140 pounds. This is equivalent to 86 tons of hyacinths per acre and
further indicates that a dense growth had not been attained since Penfound and Earle
commonly found 120 to 180 tons of hyacinth plants per acre. Biological and chemical
oxygen demands were reduced by 69.6 and 47.2 percent, respectively, during this study
period. Organic nitrogen decreased by 59.9 percent and ammonia nitrogen increased by 411
percent. Slight reductions in both nitrite and nitrate nitrogens were observed. Decreases in
organic nitrogen are attributed to the increased biomass on the roots and the sharp decrease
in suspended solids. An increase in ammonia nitrogen is contrary to the findings of Clock.
Although the pressed liquor analyses indicate a greater uptake of ammonia nitrogen (Table
12) during the 5-day detention period, apparently the denitrification process released more
nitrogen as ammonia than the plants could utilize at this detention time. Overall nitrogen
reductions were only slightly higher than at the 2.4-day detention time. Phosphate
reductions were substantially better at the longer detention periods as 35.5 percent of the
phosphate was removed, compared to 14.7 percent at the 2.4-day detention period. Table
11 summarizes the 5-day detention period data.
Based on the above data, the following conclusions were reached:
1. A minimum of 5 days' detention would be required to obtain
significant nutrient reductions.
2. Since the average total detention time in the polishing ponds is only 42
hours, nutrient removal by hyacinths in the present facility is not
applicable.
3. Biological and chemical oxygen demand reductions by the hyacinth
plant system appear to be more promising than nutrient removals.
18
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>~l
Furman and Gilcreas reported serious mosquito breeding problems in a study
near Tampa, Florida, when hyacinths formed dense mats over the-water's surface. This was
not found to be a serious problem at Auburndale, however, our hyacinth pond was
relatively small compared to the lagoon system studied by Furman and Gilcreas.
6.03 HYACINTH PLANT CHARACTERISTICS
Detailed chemical analyses were made on the hyacinth plants at the outset of this
investigation, during the 2.4-day detention period, and during the 5-day detention period.
Air dried samples averaged 95 percent moisture throughout the study period. Protein and
ash concentrations increased significantly with detention time, whereas crude fiber
concentrations remained virtually unchanged. Results of these analyses are shown below.
Average Analyses
Constituent
2
Moisture, percent
Protein, percent
Ash, percent
Crude fiber, percent
Ether extract, percent
Carotene, mg/lb
Xanthophylt, mg/lb
Dicumarol, mg/lb
KNO3, g/g
Oxalate, mg/g
Total PO4 - P, mg/g
Total N, mg/g
Hyacinth Plants
Natural State
95.0
12.26
13.75
15.12
1.99
-
-
-
649
-
0.65
-
2 -Day
Detention
95.0
11.00
16.00
12.05
2.09
0-28
70
35
505
0.4
7.0
112.0
5 -Day
Detention
95.0
19.90
16.80
16.93
1.14
2L6
304
-
367
-
7.7
55.8
* Analyses were made by personnel of University of Florida, Animal Nutrition
Laboratory and personnel of The Coca—Cola Company, Foods Division Research
Laboratory.
"Moisture on air dried samples at 103°C. averaged 10 percent.
19
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Chemical analyses of Alfalfa hay exhibit characteristics similar to the dried
hyacinth plants. Protein values average IS percent, fiber 28 percent, and moisture about 9
percent Bahai grasses average 10 percent protein and 5 percent ash. Based on these
comparative analyses, dried hyacinth plants have good potential as a supplemental feed for
cattle.
An attempt was made to process the hyacinth plants through the existing feed
mill facilities at Auburndale; however, due to the fibrous nature of the hyacinth plant,
fouling of equipment was encountered. It was concluded that hyacinth plants would require
special processing equipment and that present feed mill facilities were inadequate to process
the plants without some capital improvements.
Harvesting of the hyacinth plants could be accomplished on a large scale
operation by means of several mechanical devices now available for aquatic vegetation
control. Harvesting operations during this study were done manually.
6.04 PRESSED LIQUOR
Pressed liquor analyses indicate that significant quantities of nutrient are released
during processing. A summary of pressed liquor analyses is given in Table 12. Nitrogen and
phosphorous concentrations in the pressed liquor increase with detention time. Also, the
volume of wastewater from the squeezing process is considerable.
Based on an average wet weight of 150 tons of plants per acre, of which
approximately 95 percent is water, 34,000 gallons per acre of additional wastewater would
be produced. Assuming an average PO^P concentration of 63 mg/1 and an average total—N
concentration of 335 mg/1 in the pressed liquor, this amounts to an additional 18 pounds
per acre and 95 pounds per acre, respectively, of phosphorus and nitrogen in the wastewater
stream. Gtrus wastewater flows would be increased by some 0.1 percent per acre of plants
processed; however, nitrogen and phosphorous concentrations would be increased
significantly in the normally nutrient deficient process water. During periods of hyacinth
plant processing a small savings in chemical costs for supplemental nutrient would be
realized.
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SECTION 7
ECOLOGICAL STUDY
7.01 GENERAL
A detailed ecological survey was made by Dr. James B. Lackey of the Aubumdale
wastewater treatment plant to characterize types of biota associated with the treatment
process. Aubumdale facilities had recently been converted to operate as an aerated lagoon
system and had not stabilized by the time of the first survey. A second study was made at
Aubumdale after three months' operation as an aerated lagoon system.
7.02. AUBURNDALE AERATED LAGOON SYSTEM
No previous background data were available for the Aubumdale treatment plant
At the first visit conditions throughout the plant were not satisfactory, although BOD
removals averaged about 70 percent. The principal objection was odor. Since the treatment
plant effluent discharges into Lake Lena Run which terminates at Lake Hamilton,
widespread odors could be considered a nuisance and improper treatment could be
detrimental to the lake. Vast improvement was noted on the second visit as BOD removals
averaged better than 80 percent and there were no objectionable odors.
Microbiota at Aubumdale were first studied on March 11,1969. The ponds were
turbid, but not colored. The mixed liquor in the aeration pond did not contain as a great a
quantity of organisms as found at Leesburg, but the biota was roughly the same. A
qualitative examination of the biota in the aeration pond indicated a nontoxic, high organic
content, low carbon, high nitrogen, and high phosphate substrate with a BOD high enough
to be putrescible if not sufficiently mineralized. The high nitrogen and phosphate were due
to supplementary nutrients added as aqua ammonia and phosphoric acid at a BOD:N:P ratio
of roughly 150:5:1.
Some of the organisms were attached to roots or the sides of the aeration pond.
These were filamentous green algae such as Ulothrix, Schizomeris, and Rhizoclomwn,
probably Stigeoclonium as well, and several worms, noticeably chironomid larvae.
Sphaerotilus was the dominant organism hi the mixed liquor (substrate). Colonies of
Zooglea were abundant and the numbers of free swimming bacteria seemed low.
Nevertheless, large numbers of Rotifera, Vorticellids, and Ciliatas indicated a good food
supply. Beggiatoa and large numbers of a Spirillum further indicated a low oxygen content
In addition, photosynthetic algae such as Navicula, Ankistrodesmus, and Euglena were
present.
The concentration of oxygen in the first polishing pond was low, but nutrient
conditions excellent as evidenced by the large variety of organisms shown in Table 13. The
low oxygen is indicated by Trepomonas, Saprodinium, and various facultative organisms
such as Spirillum and Paramecium calkinsi. Ciliates, Oicomonas, and Rotifera are bacterial
21
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consumers. Blue-green algae, the colorless euglenids Peranema, Sphenomonas, and
Spondymonum indicate soluble organic matter, while the various green algae add oxygen
and utilize nitrogen and phosphorous. The second polishing pond was much the same,
microbiota was varied, and there were indications that oxygen concentrations were low. Of
particular interest was that seven green euglenids and Spondylomorum were numerous; in
fact, so numerous as to constitute a bloom. Such a bloom of these organisms is prima facie
evidence of recent organic contaimination, usually fecal. This was probably due to the large
numbers of egrets and other birds that congregate on the flow control baffles and berms of
the polishing pond.
Conditions in Lake Lena Run, downstream from the treatment plant, further
indicate the variety of microbiota in the treatment process. Here, all the organisms found in
the treatment and others were present. At a point about 1.75 miles downstream, there was a
heavy white coating of the colonial vorticellid Zoothamnium on every stick or other solid in
the stream. These were dominant and could be seen from several yards away. In the stream
the colorless flagellate Monas was dominant It is also a consumer of bacteria, but ciliates
were also present in large numbers. Blue-green algae, diatoms, green algae, many euglenids,
desmids (a whole collection of typical stagnant water organisms) were present, such as are
found in a relatively fertile situation.
A sample of unpolluted water from Saddle Creek was also examined at this time.
This sample showed more varied diatoms, euglenids, volvocales, and desmids. The only
group present here and lacking in Lake Lena Run was the Cryptophyceae.
A second ecological survey was made on June 11, 1969. Conditions were
somewhat more favorable. Lake Lena Run above the waste treatment plant revealed
considerable numbers of recently dead organisms. Either oxygen depletion or a slug of toxic
material was implicated. The fact that two green organisms were alive, although few in
number, and that some tolerant flagellates were present in the sludge supports this idea.
Substantial numbers of green organisms, as well as bacteria-consuming ciliates,
were present in the aeration pond. A bloom had already developed of two photosynthetic
algae, namely, Ankistrodesmus falcatus and Chlorellasp.
A steady improvement was noted throughout the plant until the bridge about one
mile below the treatment plant outfall. Here the temperature was 36°C. and dissolved
oxygen was only 0.5 mg/1. This was due to intentional bypassing of part of the untreated
wastewater in order to maintain a controlled influent flow of 10 mgd for a phase of research
in progress at the time of this survey. This caused a noticeable decrease in the number of
bacteria, yeasts, and phycornycetes downstream as seen in Table 13.
The diversity of species was greater and green algae had assumed greater
prominence since the first visit. The odor, prevalent on the first visit, had diminished. The
stream's appearance toward Lake Hamilton was good.
Table 13 summarizes the data from both visits. In addition to the large number of
genera and species present, the organisms found were quite similar to those of a well
functioning domestic treatment plant. The waste was fairly well balanced nutritionwise. The
22
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initial steps in decomposition produce large numbers of bacteria and related organisms.
These, in turn, support a good population of colorless flagellates and ciliates.
Euglenophyceas and Volvocales in the later stations, utilize the partially degraded organic
matter and release enough inorganic nutrients to support a green population, useful in
reaeration.
A buildup of sludge in the bottom of the polishing ponds at Leesburg and
Auburndale could result in anaerobic conditions leading to odors and an increasing rise, due
to gassing, with more solids going out in the effluent. It is suggested that these ponds be
taken out of service periodically, the sludge dried and removed before the pond is put back
in service. This may be necessary as often as every other year, depending on treatment
practices.
23
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SECTION 8
KINETIC STUDY
8.01 GENERAL
o
Kinetic studies were performed as described by Eckenfelder using an acclimated
sludge at various temperatures, with and without nutrients. The purpose of these studies was
to determine BOD removal rate coefficients and temperature coefficients (Appendix 5).
These values are necessary in order to calculate design parameters for an aerated lagoon
system. BOD removal rates exhibited a retardant-type reaction where removal rates
decreased with time and concentration. A typical removal rate curve is presented in Figure
10.
8.02 LABORATORY STUDY
Studies were conducted at Auburndale during May and June, 1969. BOD removal
rates were determined simultaneously at 20°C. and 25°C., with and without nutrients.
Supplemental nutrients were added as ammonium hydroxide and phosphoric acid;
concentrations were 5 mg/1 NH^-N and 1 mg/1 PO^-P. Mixed liquor suspended solids
(MLSS) concentrations ranged from 160 mg/1 to 220 mg/1. The results of these studies are
summarized as follows:
BOD Removal Rate Temperature
Coefficient - k2Q° c. Coefficient - 0
Average 1.46 1.05
Maximum 2.80 1.06
Minimum 0.80 1.04
Variations of the BOD removal rate coefficients were caused by discharges of
pressed liquor into the plant effluent, which is toxic and decreases the biological activity of
the activated sludge. Also, the concentration of mixed liquor suspended solids affects the
removal rate.
A study by Furman during the 1966-67 citrus processing season at Leesburg
reported a BOD removal rate coefficient (k20°C.) of ^'8^' Cample calculations of
Auburndale and Leesburg data are presented in Appendices 2-4.
25
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SECTION 9
RESULTS
9.01 GENERAL
Although the 1968-69 citrus processing season extended from November 14,
1968, through July 25, 1969, only those data collected between December, 1968, and June,
1969, were reviewed for purposes of this investigation. Citrus wastewaters received in
November, 1968, and July, 1969, were principally from sporadic processing operations and
not representative of wastewaters received during the main processing season.
Citrus processing wastewaters were bypassed on several occasions during the
period of this investigation. Prior to January 15, 1969, intentional bypassing was employed
in order to maintain aerobic conditions throughout the treatment plant, as only a portion of
the aeration equipment was operative. During the period May 1 through June 13, 1969,
investigations concerning plant capabilities required that influent flow rates be controlled at
5 mgd and 10 mgd. Therefore, a significant quantity of the wastewater stream was again
intentionally bypassed. Thus, average hydraulic and organic loading values, as shown in this
report, are somewhat lower than actual full-scale operating conditions.
Table 14 summarizes the average weekly data for the 1968-69 processing season
presented in the forthcoming sections.
9.02 HYDRAULIC LOADINGS
Flow measurements were made by Dall tubes as indicated in Figure 3. These were
installed with B—I—F instrumentation to indicate, record, and totalize flows from the
aeration pond (total) and recirculated sludge line. Daily influent wastewater flows were
obtained by difference.
Daily total flows ranged from 11.3 to 31.9 mgd and averaged 20.3 mgd. These
data included daily influent wastewater flows which ranged from 5.5 to 20.5 mgd and
averaged 12.8 mgd, and recirculated sludge flows which ranged from 2.4 to 13.2 mgd and
averaged 7.5 mgd.
9.03 ORGANIC LOADINGS
Since citrus wastewaters contain substances which, at times, are bacteriostatic,
both BOD and COD determinations were made in order to obtain comparative organic
loading values.
Daily BOD loadings ranged from 3,432 to 22,099 pounds per day and averaged
12,256 pounds per day. Citrus processing wastewater 5-day BOD values ranged from 43
mg/1 to 201 mg/1 and averaged 117 mg/1. Daily COD loadings ranged from 8,021 to 52,516
pounds per day and averaged 20,756 pounds per day. COD concentrations in the influent
stream ranged from 99 mg/1 to 297 mg/1 and averaged 190 mg/1.
27
-------
9.04 COD/BOD RATIOS
COD/BOD ratios varied from 1.30 to 2.40 and averaged 1.73 on the untreated
citrus processing wastewater (plant influent) and from 1.43 to 6.50 with an average of 3.34
on the wastewater treatment plant effluent during the study period.
9.05 BOD AND COD REMOVALS
Organic removal was somewhat lower than anticipated due to an inadequate
sludge collection system which prevented operating the treatment facility as an extended
aeration plant BOD removals between December, 1968, and February, 1969, ranged from
6.7 to 85.5 percent and averaged 61.8 percent COD removals were lower and ranged from
14.1 percent to 76.1 percent and averaged 46.7 percent for the 13-week period.
During March the operation was changed to explore the aerated lagoon process.
Controlled flow conditions during May, 1969, and June, 1969, yielded average BOD
removals of 94.5 percent and 83.8 percent, respectively. COD removals during the same
period averaged 76.9 percent and 64.6 percent, respectively.
BOD removals for the entire 1968-69 citrus processing season ranged from 6.7 to
95.3 percent and averaged 70.8 percent COD removals for the study period ranged from
14.1 percent to 79.4 percent and averaged 53.0 percent
9.06 SUSPENDED SOLIDS
Suspended solids concentrations in both the influent stream and treatment plant
effluent ranged from 0 mg/1 to 120 mg/1 and averaged 27 mg/1.
9.07 DISSOLVED OXYGEN
Dissolved oxygen concentrations in the aeration pond ranged from 2.0 to 6.8 mg/1
and averaged 4.3 mg/1. Settling pond (Pond No. 2) dissolved oxygen concentrations ranged
from 0 to 2.6 mg/1 and averaged 1.3 mg/1. Polishing pond dissolved oxygen concentrations
for the study period ranged from 0 to 5.7 mg/1 and averaged 1.5 mg/1.
9.08 TEMPERATURE AND pH VALUES
Influent temperature and pH values averaged 27.4°C. and 7.1, respectively.
Variations in temperature were * 6°C. and pH variations were * 0.2. Effluent temperatures
were affected by climatological conditions and ranged from 19.5°C. to 30.4°C. and
averaged 23.6°C. Effluent stream pH values ranged from 7.1 to 7.7 and averaged 7.2.
28
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9.09 NUTRIENT REMOVALS
Nitrogen and phosphorous determinations were made on the influent wastewater
stream once each week to determine if nutrient concentrations were ample for biological
treatment. Supplemental nitrogen and phosphorus were added to maintain desired nutrient
levels. Effluent wastewaters were likewise analyzed to determine the reduction in nitrogen
and phosphorous concentrations during bio-oxidation of the citrus processing wastewaters.
Reductions were based on dosed influent nitrogen and phosphorous concentration levels.
Influent nitrogen concentrations (undosed) (Table 14) ranged from 1.60 to 5.64
mg/1 and averaged 3.05 mg/1, whereas effluent concentrations varied from 2.01 to 5.12 mg/1
and averaged 3.63 mg/1. Overall nitrogen removals for the study period averaged 36 percent
and ranged from 0 to 70 percent.
Phosphorous concentrations (undosed) (Table 14) ranged between 0.21 and 1.84
mg/1 and averaged 0.81 mg/1 on the influent stream. Effluent stream phosphorous
concentrations varied from 0.58 to 1.88 mg/1 and averaged 1.16 mg/1. Phosphate removals
for the 1968-69 citrus season ranged from 0 to 82 percent and averaged 37 percent.
9.10 REUSE OF TREATMENT PLANT EFFLUENTS IN CITRUS PROCESSING
PLANT
Water uses at the Auburndale citrus processing plant include (1) process; (2)
cooling; and (3) steam generation. Process water must be of potable quality, cooling water
can be of a lower quality, and water for steam generation must have low hardness and other
special requirements.
Analyses of the wastewater treatment plant effluent during the 1968-69 citrus
processing season are exhibited in Table 14, indicating a potential for reuse as cooling water.
29
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SECTION 10
DISCUSSION OF RESULTS
10.01 HYDRAULIC LOADINGS
Average flow measurements of 12.8 mgd as shown in Table 14 are lower than
actual, due to intentional bypassing of a portion of the wastewater stream for control and
research purposes. Observations during the study period indicated that average flows would
approach 25-30 mgd when both The Coca—Cola Company and Adams were in full
production. Studies made prior to and during the 1966-67 citrus processing season further
support this idea. Fiske and Gay reported an average flow from both plants of 25.5 mgd and
our statistical studies indicated average flows of 17.9 mgd.
Results from the controlled flow experiments shown in Tables 16 and 17 and
design characteristics shown in Table 15 indicate that the present facility operating as an
aerated lagoon system would accommodate wastewater flows of 6.4 mgd and achieve 91.3
percent BOD removal.
Production levels during the 1968-69 season from both citrus processing plants
were approximately 110,000 boxes per day. Projected production levels for the 1969-70
season approach 135,000 boxes per day. Unless wastewater volumes are reduced in the
processing plants, it is conceivable that wastewater flows during the next processing season
will average in excess of 36 mgd.
10.02 ORGANIC LOADINGS AND REMOVALS
Many of the organic loadings reported were artifically reduced hi order to study
plant capabilities at lower influent flow rates. The average organic loadings passed through
the treatment plant are consequently somewhat lower than the output of the citrus
processing plants.
Based on flow data and 5-day BOD values obtained during full production, BOD
loadings of the order of 32,500 pounds per day are anticipated during the 1969-70 citrus
processing season.
A detailed summary of average monthly operations is presented in Table 18. Data
for the month of May indicate that BOD loadings of 287 pounds per day per acre (6,789
pounds BOD per day) are optimum for the present facility. Based on kinetic data collected
during this study and projected requirements for the 1969-70 processing season, an
additional 40 acres of aeration space are necessary in order to operate the present facility as
an aerated lagoon system and to obtain the required 90 percent BOD removal (see Section
11). To operate the facility as an extended aeration plant, two 200-foot diameter clarifiers
and waste sludge handling facilities are needed using design criteria set forth in Section 12.
31
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BOD reductions of the order of 57.3 percent were afforded through the aeration
pond and the settling pond during the 1968-69 processing season. Additional aeration in the
settling pond might increase BOD reductions by 5 percent; however, detention time is a
major limiting factor in an aerated lagoon system as seen from data summarized in Table 18.
The polishing ponds contributed significantly to overall BOD reductions during the study
period. BOD removals through the polishing ponds averaged 13.5 percent as shown in Table
14. Operating the existing facility as an aerated lagoon system, with additional aeration in
the settling pond and with hydraulic and BOD loading levels as indicated by this study, a
maximum BOD removal of 75 percent would be estimated.
10.03 COD/BOD RATIOS
Weekly and monthly average COD/BOD ratios were determined and are exhibited
in Tables 14 and 18, respectively. The small differences between the average values is due to
the fact that the monthly averages tend to level out extreme variations more readily than
weekly averages.
COD analyses were performed at the outset of the 1968-69 processing season.
Refluxing times were varied from 10 minutes to 2 hours to determine maximum COD
recovery. Since citrus wastes consist primarily of carbohydrates, they are susceptible to
rapid oxidation. Reflux times of 20 minutes afforded better than 98 percent of the COD
value obtained after two hours' refluxing; therefore, routine COD analyses were refluxed for
a period of 30 minutes to minimize error. COD/BOD ratios of the citrus processing
wastewater at Auburndale averaged 1.76. McNary^ reported an average value of 1.56 during
a pilot plant study.
The COD test plays a significant role in plant operations since organic loadings
can be determined quickly and treatment operations adjusted accordingly. BOD analyses are
not suitable for this purpose because of the 5-day time period required to obtain the results.
Another important factor concerning the COD test is that certain wastes from the
citrus process are toxic and tend to give misleading (low) BOD values. Therefore, once a
COD/BOD factor is determined, more accurate BOD values and organic loadings can be
obtained from COD measurements than from BOD measurements when toxicity is
suspected.
10.04 DISSOLVED OXYGEN
Average dissolved oxygen concentrations (Table 19) in the ponds during the
study period were good. Except for gross overloading during January and February causing
anaerobic conditions, especially in the settling pond and the first polishing pond, oxygen
levels were within the range of 0.6-2.6 mg/1 recommended by Mueller** for maximum
oxygen uptake by bacterial floe. A paper by Eckenfelder described filamentous growths as
obligatory aerobes which flourish in the presence of a readily available carbon source and at
oxygen levels below 0.5 mg/1, oxygen uptakes are low. Since the filamentous growths have a
high surface area to volume ratio, they will consume most of the available oxygen. High
oxygen concentrations tend to favor floe-forming bacteria.
32
-------
Based on the results of this study and the data discussed in the above papers, it is
feasible that additional aeration in the settling basin would afford an increase in BOD
removals; however, an increase of not more than 5 percent would be anticipated.
10.05 NUTRIENT REMOVAL
Nitrogen and phosphorous removals during the study period averaged 36 percent
and 37 percent, respectively. The settling pond afforded nitrogen removals of 14.8 percent
and phosphorous removals of 10.3 percent. Primary nutrient reductions occurred through
the polishing ponds. Nitrogen concentrations exhibited reductions of 21.2 percent and
phosphate concentrations decreased an average of 25.7 percent. Nutrient removals were
based on dosed influent concentrations.
Ecological studies at Auburndale indicated that the treatment process was well
balanced nutritionally and that the microbiota present were favorable for bio-oxidation of
the citrus wastewater. Under aerobic conditions, ammonia nitrogen and organic nitrogen
concentrations would be expected to decrease while nitrate nitrogen concentrations would
be expected to increase. Data presented in Table 19 show that although ammonia nitrogen
concentrations decreased, organic nitrogen increased and nitrate nitrogen remained virtually
unchanged. Settling pond effluent samples indicate a substantial increase (approximately 65
percent) in organic nitrogen over the influent samples. Appreciable quantities of organic
matter (BOD) in the settling pond wastewater probably contributed to further production
of plant biomass. The biomass contains significant quantities of proteinaceous material
which, in turn, contributed to the higher organic nitrogen concentrations experienced in the
settling pond effluent. Organic nitrogen removals of the order of 20 percent were indicated
between the settling pond and the final polishing pond effluent.
Nitrate nitrogen concentrations probably remained low due to the depth of the
settling pond and the long detention time of the treated wastewater in the pond. Since no
additional aeration was provided in this pond, the only oxygenation was due to surface
aeration. Therefore, the settling pond served as a facultative device where aerobic conditions
prevailed at or near the surface and anaerobic conditions, favoring denitrification, prevailed
in the deeper areas of the pond.
Nitrogen and phosphorous analyses were made on ulfiltered samples throughout
this study since this was representative of the actual conditions from pond to pond and in
the treatment plant effluent. Further studies should include duplicate analyses on filtered
and unfiltered samples in order to substantiate the above findings.
10.06 REUSE OF TREATMENT PLANT EFFLUENTS IN CITRUS PROCESSING
PLANT
Chemical analyses indicate substantial quantities of nitrogen (3.63 mg/1) and
phosphorus (0.74 mg/1) in the effluent stream. BOD concentrations average about 30 mg/1
and suspended solids concentrations average 27 mg/1.
33
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Citrus processing water requirements generally fall into
three categories: (1) process; (2) cooling; and (3) steam generation.
Process water should be of potable quality since it comes in contact
with the product. Treatment plant effluent would not be suitable
for use as process water without further treatment. Additional
treatment would also be required for steam generation. Primary water
consumption is for cooling water in the shell and tube exchangers.
Since the average temperature of the treatment plant effluent ap-
proximates that of ground water, it would be applicable for use as
cooling water. The quality of the treatment plant effluent is ac-
ceptable without further treatment; however, due to the nutrient still
remaining in the treated effluent, bacterial slime buildup normally
encountered in the tube exchangers would be accelerated. Therefore,
additional slime control chemicals would be required.
The major disadvantage of reusing the treatment plant ef-
fluent at Auburndale at the present time would be the costs involved
to pump the water back to the process plant.
10.07 Cost of Treatment
The waste load.entering the Auburndale waste treatment plant
for the 1969-70 season was generated from the processing of approximately
16X106 boxes of fruit. The treatment plant treated a total of 3,010,000#
BOD. It should be pointed out that this plant still does not function
properly and that part of the waste loading has frequently been bypassed
around the treatment plant. This is, of course, reflected in a high
cost of treatment based on #BOD.
Total Construction Cost $616,000
Depreciation 145,000
(Based on 5 yr. @ 6%)
Direct Expense 134,000
Annual Treatment Cost 279,000
#BOD Treated 3.01X106#
Boxes Fruit Processed 16X10^
Cost of Treatment
$/#BOD $.0.090
$/Box Fruit $0.017
34
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SECTION 11
AERATED LAGOON DESIGN
11.01 GENERAL
An aerated lagoon is a pond for the treatment of sewage or industrial wastes
which is oxygenated by means of induced surface aeration and by mechanical or diffused
aeration units. The depth of an aerated lagoon varies from 6 to 12 feet. Other factors
affecting treatment in an aerated lagoon system are sunlight, wastewater and ambient
temperatures, nutrient levels, algae, evaporation, percolation, and sedimentation. Mixed
liquor suspended solids in an aerated lagoon system are generally low (100 - 300 mg/1) and
BOD removal is a function of the initial organic load, detention time, and temperature.
Oxygen levels of at least 2.0 mg/1 should be maintained throughout the basin in order to
insure effective biological treatment and to reduce the possibility of odors. Mechanical or
diffused aeration units should be so arranged as to maintain an oxygen level of at least 1.5
mg/1 DO throughout the system. Eckenfelder suggests spacings of 200 feet at power levels
of 0.015 - 0.02 horsepower per 1,000 gallons of basin volume to supply the required oxygen
levels; however, these levels are inadequate to maintain solids in suspension. Both the kinetic
studies and the ecological studies at Auburndale indicate a BOD:N:P ratio of 150:5:1
affords excellent nutrient levels for an effective biological process.
11.02 EXPERIMENTAL DATA
Based on daily operating data, supported by survey data of the 1966-67 citrus
processing season and recent studies at Auburndale, combined wastewaters from The
Coca—Cola Company and Adams at present (in full operation) have the following
characteristics:
Flow, mgd 30
BOD (average) mg/1 130
BOD (average), Ibs/day 32,500
BOD removal rate coefficient (^20°c) * "^
Temperature coefficient ( O ) 1.05
Wastewater temperature, °F. 91.5
Minimum monthly ambient temperature, °F. 59.0
Monthly average data summarized in Table 20 indicate that the present system
operating as an aerated lagoon system will afford average BOD removals of approximately
72 percent. This is significantly lower than the 90 percent organic removal required by the
Florida Air and Water Pollution Control Commission.
Controlled flow rates during May and June, 1969, of 5 mgd and 10 mgd,
respectively, indicate that the present facility is capable of BOD removals of the order of 90
percent at flow rates of not more than 6.4 mgd.
35
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11.03 DESIGN CRITERIA
Based on supporting data collected during the 1968-69 processing season,
laboratory studies at Auburndale and theoretical considerations outlined by Eckenfelder,^
the following design criteria are suggested for 90% BOD removal:
Actual Operation Theoretical
(5 mgd & 10 mgd Studies) (Eckenfelder3)
Average flow, mgd
Influent BOD, mg/1
Effluent BOD, mg/1
Loading:
BOD, Ibs/day
BOD, Ibs/acre (including polishing ponds)
Aeration:
Area, acres
Pond depth, feet
Oxygen required, Ibs/hr
Surface, Ibs/hr
Mechanical, Ibs/hr
Total horsepower
Polishing ponds:
Area, acres
Pond depth, feet
Nutrient requirement:
Nitrogen, Ibs/day
Phosphorus, Ibs/day
Average k2Q°C.
Wastewater temperature, °F.
Temperature coefficient, O
Average ambient temperature (winter),°F.
30
130
12
GIVEN
32,500
550
CALCULATED
51
12
1,584
562
1,022
410
8-15
5.0
1,210
177
1.46
91.5
1.05
59.0
30
130
12
32,500
677
40
12
1,584
440
1,144
460
8-15
5.0
1,210
177
1.46
91.5
1.05
59.0
* Since six aerators of 75 horsepower each are in the existing aeration pond,
additional aerators totalling 450 horsepower would be required in order to be spaced
properly for proper aeration and mixing hi the larger expanded facilities.
A summary of supporting data is presented in Tables 20 and 15 and sample
calculations are given in Appendix 5.
36
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SECTION 12
SUGGESTED DESIGN PARAMETER
EXTENDED AERATION
12.01 GENERAL
The following design parameters are based as much on the engineer's estimates
derived from experience during the course of this research as on actual data obtained during
the investigation.
12.02 PRELIMINARY BACKGROUND DATA
Laboratory and small scale pilot plant studies should be made prior to design.
Process variables, waste characteristics, and basic operating parameters should be studied.
BOD removal rates and variations, oxygen requirements, nutrient levels, excess sludge
production and settling rates should also be determined.
12.03 DESIGN PARAMETERS
Citrus processing wastewaters are extremely variable regarding both hydraulic and
organic loadings. Therefore, average maximum flow and loading rates rather than overall
average rates should be used for design purposes in order to continuously meet minimum
organic removal criteria.
Basic design parameters are as follows:
Aeration
Depth, feet 10-12
Loading, pounds BOD/1,000 cu ft 20
Mechanical aeration, hp/330 Ibs
BOD applied 10
MLSS, pounds/pound BOD applied 10-12
MLSS, mg/1 2,000-6,000
Dissolved oxygen, mg/1 1.5-2.5
Sludge recirculation, percent, variable 0-100
Clarifier overflow, gal/day/ft2 500
Waste sludge, Ibs/lbs BOD applied 0.3-0.4
Sludge digestion Aerobic
Nutrient, BOD:N:P 150:5:1
37
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Relationships between sludge recirculation and sludge settleability, dissolved
oxygen levels, and degree of treatment, along with sludge buildup and sludge wasting,
require further investigation.
38
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TABLES
-------
TABLE 1
WASTEWATER POND CHARACTERISTICS
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Water depth, feet
Bottom dimensions, feet:
Length
Width
Area, acres:
Bottom
Water surface
Capacity, mg:
Over bottom
Over slopes
Total
Capacity (min.), mg
Cross section.
area, s.f.O)
Aeration
Pond
(No. 1)
11.7
380
235
2.05
3.15
7.815
1.889
9.704
8.07
Settling Pond (No. 2)
Sludge
Section
14.2
210
439
2.11
2.72
8.305
0.906
9.211
4,536
Remainder Total
9.7
327 537
439 439
3.29 5.40
4.06 6.78
10.404 18.709
1.153 2.059
11.557 20.768
Polishing
(No. 3)
5.0
576
463
6.12
6.85
9.963
0.583
10.546
Ponds
(No. 4)
4.5
464
581
6.19
6.85
9.074
0.475
9.549
Total
System
19.76
23.63
45.561
5.006
50.567
(l)Over hopper bottom
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TABLE 2
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01 -67
Date
1966
Nov. 4
Nov. 5
Nov. 6
Nov. 7
Nov. 8
Nov. 9
Nov. 10
Nov. 11
Nov. 12
Nov. 13
Nov. 14
Nov. 15
Nov. 16
Nov. 17
Nov. 18
Nov. 19
Nov. 20
Nov. 21
Nov. 22
Nov. 23
Nov. 24
Nov. 25
Nov. 26
Nov. 27
Nov. 28
Nov. 29
Nov. 30
Dec. 1
Dec. 2
Dec. 3
Dec. 4'
Dec. 5
Dec. 6
Dec. 7
Day of
Week
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Weir
Peak
12.1
17.1
18.5
11.4
5.0
9.6
9.6
10.6
10.6
11.4
8.5
7.0
16.7
9.6
9.6
1.6
10.6
15.8
3.2
8.5
7.9
7.6
7.6
6.4
4.2
0.8
4.7
10.6
19.6
No.
MGD
Min.
2.0
2.8
3.0
2.1
0.9
0.2
0.1
0.6
0.3
0.3
1.4
0.3
0.6
0.6
0.6
0.7
0.1
0.0
0.4
0.4
0.0
0.0
0.1
0.3
0.2
1 ' l'
Avg.
6.6
8.5
7.9
5.5
2.8
3.4
4.3
5.2
4.4
4.4
4.4
2.4
5.5
4.2
4.8
0.9
4.2
6.4
2.0
3.6
4.1
4.4
3.4
2.9
1.8
0.8
4.1
5.7
9.8
Weir
Peak
21.5
19.7
12.9
26.2
17.9
23.4
18.9
17.9
21.9
8.1
14.4
15.8
14.8
14.4
25.0
14.4
9.5
17.9
16.1
19.7
5.4
12.8
6.7
10.2
14.8
14.4
13.4
14.4
11.2
3.4
14.4
19.7
23.4
No.
MGD
Min.
1.6
4.4
4.2
4.2
3.2
0.5
1.9
1.6
0.3
0.3
0.3
1.4
0.3
0.8
0.4
0.8
0.3
1.4
4.4
2^>
Avg.
9.5
9.5
8.1
11.2
9.5
9.5
9.5
9.5
6.7
3.2
4.9
6.1
6.7
5.4
7.5
6.7
3.2
8.3
8.1
8.9
1.1
3.8
1.9
; 3.2
4.2
4.7
4.9
4.9
3.8
0.5
4.9
6.7
11.2
Area
Precipitation
Inches (3)
0.05/0.08
/0.08
0.13/0.02
T-2
-------
TABLE 2
(continued)
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1966
Dec. 8
Dec. 9
Dec. 10
Dec. 11
Dec. 12
Dec. 13
Dec. 14
Dec. 15
Dec. 16
Dec. 17
Dec. 18
Dec. 19
Dec. 20
Dec. 21
Dec. 22
Dec. 23
Dec. 24
Dec. 25
Dec. 26
Dec. 27
Dec. 28
Dec. 29
Dec. 30
Dec. 31
1967
Jan. 1
Jan. 2
Jan. 3
Jan. 4
Jan. 5
Jan. 6
Jan. 7
Jan. 8
Jan. 9
Day of
Week
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Weir
Peak
15.8
16.7
12.9
7.0
4.4
8.2
11.4
6.4
16.2
10.6
3.7
12.5
12.1
8.2
9.6
12.1
11.4
13.3
13.3
12.9
4.7
22.5
21.5
10.2
No.
MGD
Min.
6.4
5.8
7.0
0.2
0.3
1.2
4.2
0.9
4.7
2.6
0.8
9.0
0.1
0.0
1.8
0.9
11.4
8.5
4.7
0.1
0.3
9.9
4.7
id)
Avg.
10.6
11.0
10.1
2.4
1.9
5.2
7.6
3.5
8.0
5.8
1.6
6.3
9.1
5.5
6.2
8.0
5.2
12.1
11.4
10.2
1.5
11.2
16.7
6.8
Weir
Peak
17.9
25.4
19.7
6.1
17.2
17.9
21.5
17.9
21.5
21.5
11.2
25.0
27.4
16.1
21.9
6.1
4.2
8.0
12.8
19.7
25.4
22.7
21.5
6.6
27.4
27.4
23.8
18.9
24.2
21.9
14.8
18.2
No.
MGD
Min.
4.7
5.4
8.1
2.6
3.0
11.2
9.5
3.2
8.6
7.2
5.4
6.6
16.1
4.9
5.4
0.8
0.8
2.6
3.2
3.4
14.4
12.8
12.8
0.8
4.2
18.9
13.1
6.1
8.6
14.1
0.5
0.5
2<2>
Avg.
11.8
13.4
13.1
4.9
8.9
14.4
13.4
12.2
15.1
15.1
8.1
14.8
13.4
9.9
12.8
3.4
2.6
4.2
6.6
12.2
18.6
17.2
16.5
3.4
14.8
20.4
18.9
12.5
15.8
16.8
8.9
8.9
Area
Precipitation
Inches (3)
0.02/
0.63/0.85
0.30/0.25
0.02/
0.02/
0.04/0.06
0.07/0.08
n
0.02/
0.31/0.46
0.01/
/0.01
T-3
-------
TABLE 2
(continued)
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1967
Jan. 10
Jan. 11
Jan. 12
Jan. 13
Jan. 14
Jan. IS
Jan. 16
Jan. 17
Jan. 18
Jan. 19
Jan. 20
Jan. 21
Jan. 22
Jan. 23
Jan. 24
Jan. 25
Jan. 26
Jan. 27
Jan. 28
Jan. 29
Jan. 30
Jan. 31
Feb. I
Feb. 2
Feb. 3
Feb. 4
Feb. 5
Feb. 6
Feb. 7
Feb. 8
Feb. 9
Feb. 10
!•<*. 11
Day of
Week
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thuis
Fri
Sat
Sun
Mon
Tues
Wed
Thuis
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Weir
Peak
8.9
9.6
11.0
11.4
9.6
10.2
133
11.0
11.0
93
9.2
8.9
9.6
11.4
12.1
12.1
12.1
10.2
8.5
16.2
12.9
16.2
16.7
11.0
11.4
No.
MGD
Min.
73
7.9
6.7
7.6
1.8
1.6
6.7
7.3
5.8
7.0
6.7
2.0
1.4
8.5
4.2
5.8
8.5
8.5
0.06
10.2
10.2
3.4
2.4
10.2
jd)
Avg.
5.4
83
9.2
9.7
7.1
5.0
9.1
9.4
9.1
7.7
8.2
5.6
5.0
10.2
9.9
93
10.6
9.6
3.0
8.5
12.1
12.1
8.5
5.4
10.6
Weir
Peak
24.2
27.4
29.5
28.7
26.6
25.8
27,4
27.4
24.6
23.8
23.4
23.4
17.9
24.2
25.4
303
23.4
31.6
26.2
19.7
29.9
27.4
29.9
333
34.2
31.6
25.0
31.2
31.6
27.4
31.6
17.5
31.6
No.
MGD
Min.
14.1
16.8
18.6
17.5
175
11.5
10.8
18.7
11.2
14.4
15.8
15.8
9.8
9.8
16.1
17.5
0.9
193
13.4
11.5
11.2
17.9
16.1
19.7
223
20.4
14.1
12.9
21.9
22.3
12.9
8.3
15.1
2<2>
Avg.
18.6
21.9
21.9
21.5
21.5
16.1
19.7
20.4
17.9
17.9
17.9
17.9
13.4
16.1
21.5
22.7
14.4
24.2
19.7
15.1
19.7
22.3
23.4
23.4
26.2
25.4
19.7
21.5
24.2
223
23.4
14.1
23.4
Area
Precipitation
Inches <3)
0.11/0.28
/0.22
0.42/0.12
0.02/
0.03/0.02
/0.10
0.071
0.21/036
0.05/035
235/2.00
0.21 /
T-4
-------
TABLE 2
(continued)
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1967
Feb. 12
Feb. 13
Feb. 14
Feb. 15
Feb. 16
Feb. 17
Feb. 18
Feb. 19
Feb. 20
Feb. 21
Feb. 22
Feb. 23
Feb. 24
Feb. 25
Feb. 26
Feb. 27
Feb. 28
Mar. 1
Mar. 2
Mar. 3
Mar. 4
Mar. 5
Mar. 6
Mar. 7
Mar. 8
Mar. 9
Mar. 10
Mar. 11
Mar. 12
Mar. 13
Mar. 14
Mar. 15
Mar. 16
Mar. 17
Day of
Week
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Weir
Peak
9.6
13.7
14.1
13.3
14.1
14.1
12.9
10.2
13.3
15.4
7.0
10.2
12.9
11.4
12.1
12.9
14.5
14.9
14.1
14.1
10.2
11.4
10.2
19.0
7.6
13.7
12.9
12.1
10.2
6.4
12.1
7.0
7.0
7.0
No.
MGD
Min.
0.1
0.4
12.1
8.5
5.5
7.0
7.9
3.4
4.7
4.2
3.0
1.4
10.2
8.5
3.0
2.0
7.3
8.5
8.5
10.2
5.5
9.9
4.7
7.3
7.9
4.2
6.7
10.2
1.8
6.4
12.1
7.0
7.0
7.0
id)
Avg.
3.0
8.5
10.2
10.9
10.9
12.1
10.9
8.5
8.5
10.2
5.0
4.2
12.1
10.2
7.0
9.3
9.3
12.1
12.1
12.1
8.5
10.2
8.5
9.3
6.1
7.9
9.2
11.0
5.5
3.9
9.2
6.4
5.5
5.5
Weir
Peak
24.6
21.9
25.8
32.5
36.0
36.9
38.2
34.2
37.8
27.4
23.4
28.7
27.8
33.8
27.4
215
25.4
24.2
23.4
26.6
No.
MGD
Min.
7.2
2.2
11.2
21.5
22.3
17.9
22.7
18.2
18.2
19.7
9.5
8.6
20.0
23.4
10.5
7.2
14.4
10.2
10.2
10.2
2 (2)
Avg.
18.9
14.4
18.9
25.0
27.4
27.4
27.4
25.4
27.4
23.4
17.9
19.7
25.4
27.4
19.7
14.4
18.9
16.1
16.1
17.9
Area
Precipitation
Inches (3)
0.09/0.18
0.69/0.48
0.03/
0.02/1.00
1.42/0.29
0.06/
/0.55
0.32/0.08
0.02/
T-5
-------
TABLE 2
(continued)
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1967
Mar. 18
Mar. 19
Mar. 20
Mar. 21
Mar. 22
Mar. 23
Mar. 24
Mar. 25
Mar. 26
Mar. 27
Mar. 28
Mar. 29
Mar. 30
Mar. 31
Apr. 1
Apr. 2
Apr. 3
Apr. 4
Apr. 5
Apr. 6
Apr. 7
Apr. 8
Apr. 9
Apr. 10
Apr. 11
Apr. 12
Apr. 13
Apr. 14
Apr. 15
Apr. 16
Apr. 17
Apr. 18
Apr. 19
Day of
Week
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Weir
Peak
11.0
9.6
4.2
0.2
5.5
14.1
12.1
4.2
3.4
20.0
12.1
12.1
7.9
12.1
3.7
12.1
14.1
19.0
18.5
16.7
21.0
8.5
14.1
14.1
20.0
24.1
24.1
16.2
14.1
19,5
19.0
19.5
No.
MGD
Min.
11.0
9.6
4.2
0.2
5.5
14.1
12.1
4.2
3.4
20.0
12.1
12.1
7.9
4.2
3.7
14.1
10.2
7.0
3.0
2.0
10.2
10.6
13.3
13.3
11.4
13.7
5.0
3.0
10.2
15.4
1(1)
Avg.
8.5
4.2
3.0
4.4
4.2
7.0
10.2
4.2
3.0
3.0
8.5
7.0
7.6
7.0
7.3
3.0
5.5
8.5
16.2
14.1
12.1
11.0
4.2
7.0
12.1
14.9
18.5
16.2
14.9
7.0
14.1
14.9
18.5
Weir
Peak
26.2
14.4
14.8
19.7
25.4
29.5
12.9
21.5
15.4
17.9
29.5
25.4
25.4
23.4
21.5
14.4
17.9
22.7
24.6
24.2
23.8
22.3
10.5
16.1
21.9
23.4
23.4 .
23.4
18.2
16.1
19.6
17.8
25.4
No.
MGD
Min.
12.2
6.7
4.7
12.9
14.1
15.8
27.4
13.4
9.5
5.9
11.8
16.1
16.8
16.1
13.4
9.5
6.7
8.1
19.3
17.9
14.8
11.2
7.5
7.8
19.7
18.9
17.9
17.9
13.4
8.1
6.7
11.2
13.1
2 (2)
Avg.
17.9
10.2
8.6
12.9
18.6
21.5
19.7
17.9
11.2
12.9
19.7
20.8
21.5
21.2
17.9
11.2
12.9
16.1
21.5
21.5
19.7
16.8
8.6
11.8
21.5
21.5
19.7
19.7
15.1
9.5
14.4
12.9
21.5
Area
Precipitation
Inches (3)
/0.17
0.32/0.11
0.23/
T-6
-------
TABLE 2
(continued)
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1967
Apr. 20
Apr. 21
Apr. 22
Apr. 23
Apr. 24
Apr. 25
Apr. 26
Apr. 27
Apr. 28
Apr. 29
Apr. 30
Mayl
May 2
May 3
May 4
May5
May 6
May 7
May 8
May 9
May 10
May 11
May 12
May 13
May 14
May 15
May 16
May 17
May 18
May 19
May 20
May 21
May 22
May 23
Day of
Week
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Weir
Peak
18.5
12.1
8.5
4.2
10.2
12.1
10.2
11.0
12.1
11.4
9.2
12.1
10.2
11.4
11.0
11.0
9.2
10.2
10.2
3.4
10.2
11.0
10.2
12.5
11.7
11.4
26.4
26.4
12.1
No.
MGD
Min.
14.5
9.2
4.2
3.0
2.6
8.5
7.9
4.7
6.1
9.2
1.1
1.1
4.2
2.0
4.4
9.9
3.4
2.1
3.7
1.4
1.1
10.2
2.6
3.0
10.6
3.9
3.0
3.4
4.2
!(D
Avg.
12.1
10.2
5.5
3.0
4.2
10.2
8.5
10.2
10.2
10.2
3.4
5.5
7.0
5.5
8.5
10.2
5.5
8.5
7.0
2.0
4.2
10.2
Weir No. 2 (2) Area
MGD Precipitation
Peak Min. Avg. Inches ' '
25.4 23.4 25.4
f-
0.85/0.54
0.01/
21.5 16.1 17.9
17.9 11.5 14.4
20.4 11.2 16.1
19.3 11.8 16.1
12.2 3.16 6.7
18.7 3.16 11.2
21.1 1.7 18.7
17.9 11.2 14.4 0.10/
1.29/2.26
0.11/0.06
T-7
-------
TABLE 2
(continued)
WASTEWATER FLOW DATA
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1967
May 24
May 25
May 26
May 27
May 28
May 29
May 30
May 31
June 1
June 2
June 3
June 4
JuneS
June 6
June?
JuneS
June 9
June 10
June 11
June 12
June 13
Day of
Week
Wed
Thurs
Fri
Sat
Sun
Mon
Tues
Wed
Thun
Fri
Sat
Sun
Mon
Tues
Wed
Thun
Fri
Sat
Sun
Mon
Tues
Weir
Peak
12.1
14.1
14.1
125
4.7
55
14.1
12.9
16.2
33.8
21.0
7.0
12.1
16.2
16.2
7.0
195
12.1
12.1
4.2
12.1
No.
MGD
Min.
4.2
3.0
6.1
4.2
3.7
3.4
3.0
55
2.0
5.0
4.2
2.4
1.6
4.2
3.0
21.0
11.4
12.1
4.2
3.0
10.2
1<1)
Avg.
8.5
10.2
85
4.2
4.7
4.2
85
10.2
16.2
10.2
4.7
55
8.5
10.2
11.0
12.1
12.1
55
55
11.0
Weir
Peak
215
15.8
18.9
18.9
11.8
11.8
18.9
16.8
42.9
42.9
22.7
175
20.4
20.4
21.2
215
25.4
22.7
19.7
18.6
23.4
No.
MGD
Min.
12.9
95
115
12.2
5.4
5.6
4.0
125
10.8
165
15.4
4.7
5.4
12.9
4.7
13.4
15.4
17.2
12.2
5.6
15.4
2 <2>
Avg.
16.1
11.8
15.1
16.1
8.1
6.7
12.9
14.4
17.9
215
17.9
11.1
12.9
16.8
16.1
17.9
19.7
19.7
16.1
12.9
18.2
Area
Precipitation
Inches (3)
0.10/0.01
3.95/1.72
1.13/0.32
1.97/052
/0-09
0.37/
1.231
10.15
052/0.04
Below Adams Packing Company.
Below Adams Packing Company, The Coca-Cola Company, and City of Auburndale
Sewage Treatment Plant.
Lake Alfred Experiment Station / Winter Haven Stations of U.S. Weather Bureau.
T-8
-------
TABLE 3
DAILY AREA PRECIPITATION
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Date
1966
Nov. 2
Nov. 3
Nov. 28
Dec. 4
Dec.5
Dec. 11
Dec. 12
Dec. 13
Dec. 14
Dec. 17
Dec. 18
Dec. 24
Dec. 29
Dec. 30
1967
Jan. 4
Jan. 5
Jan. 8
Jan. 11
Jan. IS
Jan. 16
Jan. 23
Jan. 25
Jan. 27
Jan. 28
Feb. 7
Feb. 8
Feb. 9
Feb. 10
S t a
Lake Alfred
Exp. Sta
0.05
0.05
0.13
0.02
0.63
0.30
0.02
0.02
0.04
0.07
0.02
0.31
0.01
0.11
0.42
0.02
0.03
0.07
0.21
0.05
2.35
0.21
t i o n
Winter Haven
0.05
0.08
0.08
0.02
0.85
0.25
0.06
0.08
T
0.46
0.01
0.28
0.22
0.12
0.02
0.10
0.36
0.35
2.00
Date
1967
Feb. 12
Feb. 13
Feb. 14
Feb. 21
Feb. 22
Feb. 23
Mar. 7
Mar. 8
Mar. 10
Mar. 28
Mar. 29
Mar. 30
May 6
May8
May 17
May 22
May 23
May 24
Jun. 2
Jun. 3
Jun. 4
Jun. 5
Jun. 6
Jun. 7
Jun. 9
Jun. 10
Jun. 15
Sta
Lake Alfred
Exp. Sta.
0.09
0.69
0.03
0.02
1.42
0.06
0.32
0.02
0.32
0.23
0.85
0.01
0.10
1.29
0.11
0.10
3.95
1.13
1.97
0.37
1.23
0.52
t i o n
Winter Haven
0.18
0.48
1.00
0.29
0.55
0.08
0.17
0.11
0.54
2.26
0.06
0.01
1.72
0.32
0.52
0.09
0.15
0.04
T
(1) From U. S. Weather Bureau Records. Precipitation expressed in inches.
T-9
-------
TABLE 4
RAW WASTEWATER ANALYSES AT WEIR NO. 1
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA(1)
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Dates
1966
Nov.
29-30
Dec.
1-2
6-7
8-9
13-14
15-16
20-21
22-23
27-28
30-31
1967
Jan.
3-4
6-7
10-11
13-14
Days
of
Week
Tu-W
Th-F
Tu-W
Th-F
Tu-W
Th-F
Tu-W
Th-F
Tu-W
F-Sa
Tu-W
F-Sa
Tu-W
F-Sa
Flow
MGD
4.70
2.90
6.50
9.61
7.67
6.06
7.73
8.89
3.71
11.7
8.73
8.01
9.20
T o
mg/1
502
410
455
382
270
305
325
373
300
334
315
360
338
280
S o
t a 1
% Vol.
69
56
89
52
63
65
59
79
67
31
70
63
84
68
1 i
d s
Suspended
mg/1
42
40
42
42
82
72
36
23
17
26
28
24
28
17
% Vol.
48 <
55 <
40 <
31 <
18 <
39 <
97 <
87 <
100
100
93
75
100
100
Sett.
ml/1
:o.i
:o.i
0.1
0.1
:o.i
:o.i
:o.i
:o.i
0.5
0.4
0.3
0.2
0.2
0.1
5-day
BOD
mg/1
118
94
108
78
75
110
120
158
65
80
100
98
98
160
Nit.
(N)
mg/1
1.40
1.12
2.52
0.28
2.41
3.81
2.69
2.97
1.2
0.9
1.8
1.3
0.8
1.7
Phos.
(P)
mg/1
1.60
1.30
1.28
0.40
1.12
1.28
0.58
0.80
0.3
0.9
0.3
0.6
0.03
0.8
Total
Alk.
mg/1
101
108
149
104
143
148
168
146
146
101
100
Temp.
pH °F. Remarks
7.2
6.9
7.0
6.9
7.0
6.9
7.2
6.7
90
91
7.3 93
6.8 88 (2)
6.6 90
-------
TABLE 4
(continued)
RAW WASTEWATER ANALYSES AT WEIR NO. 1
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA (l>
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Dates
1967
Jan.
19-20
20-21
24-25
26-27
Jan. 31-
Feb. 1
Feb.
3-4
7-8
10-11
15-16
17-18
21-22
Feb. 28-
Mar. 1
Mar.
3-4
7-8
Days
of
Week
Th-F
F-Sa
Tu-W
Th-F
Tu-W
F-Sa
Tu-W
F-Sa
W-Th
F-Sa
Tu-W
Tu-W
F-Sa
Tu-W
Flow
MGD
7.20
7.97
9.90
9.90
12.1
10.2
12.1
11.4
5.50
12.1
8.90
7.90
T o
mg/1
466
349
352
300
436
486
308
399
300
552
404
425
882
593
S o
t a 1
% Vol.
72
69
82
84
66
67
97
52
77
90
68
75
80
67
1 i
d s
Suspended
mg/1
51
36
113
22
23
30
21
30
32
40
44
28
58
27
% Vol.
88
86
24
100
78
80
95
87
94
85
82
100
97
96
Sett.
ml/1
0.5
0.1
0.3
0.1
0.5
0.5
0.1
0.2
0.1
0.1
<0.6
0.3
1.1
<0.1
5 -day
BOD
mg/1
150
155
210
115
145
190
70
85
155
84
280
145
370
150
Nit.
(N)
mg/1
0.9
1.3
0.6
0.7
3.2
1.8
0.4
1.5
1.2
1.6
1.1
2.4
1.8
Phos.
(P)
mg/1
1.0
0.5
0.8
0.7
0.8
0.7
0.4
1.1
0.8
1.4
0.7
0.5
1.0
0.7
Total
Alk.
mg/1
88
100
80
993
151
102
98
80
93
152
130
98
95
125
pH
6.9
6.8
7.2
6.9
9.2
7.4
7.3
6.9
7.2
7.6
7.0
6.9
6.4
7.3
Temp.
OF
87
90
89
92
91
91
89
88
90
86
91
90
Remarks
(3)
(4)
(3)
-------
TABLE 4
(continued)
RAW WASTEWATER ANALYSES AT WEIR NO. 1
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 38-01-67
H
1
to
Days
of
Dates Week
Average
Maximum
Minimum
Flow
MGD
8.42
12.1
2.90
T o
mg/1
400
882
270
S o
t a 1
% Vol.
70
97
31
1 i
d s
Suspended Sett.
mg/1
38
113
17
% Vol. ml/1
78 <0.3
100 <1.1
18 <0.1
5-day
BOD
mg/1
135
370
65
Nit.
(N)
mg/1
1.6
3.81
0.4
Phos.
(P)
mg/1
0.8
1.60
0.3
Total
Alk.
mg/1
116
168
80
pH
7.1
9.2
6.4
Temp.
°F. Remarks
90
93
87
"' 24-hour composite samples initiated and terminated at 4-5 PM unless otherwise indicated.
(2) Nitrate nitrogen -1.5 mg/1.
"' Composite composed of three grab samples due to sample pump failure.
W Nitrate nitrogen - 0.00 mg/1.
-------
TABLE 5
RAW WASTEWATER ANALYSES AT DARBY AVENUE*!)
1966-67 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURNDALE, FLORIDA
Federal Water Quality Administration
Grant No. WPRD 3841-67
Dates
1967
Jan. 31 -
Feb. 1
10-11
Days
of
Week
Tu-W
F-Sa
Flow T o
MGD mg/1
330
289
S o
t a 1
% Vol.
63
35
1 i
d s
Suspended
mg/1
23
24
% Vol.
96
92
Sett.
ml/1
0.8
1.0
5-day
BOD
mg/1
120
64
Nit.
(N)
mg/1
2.1
1.0
Phos.
(P)
mg/1
0.6
0.6
Total
Alk.
mg/1 pH
94 7.4
85 7.2
Temp.
°F. Remarks
91 (2)
(3)
Below Adams Packing Company and The Coca-Cola Company.
24-hour composite sample initiated and terminated at 5 PM.
' ' 9-hour composite sample. Nitrate nitrogen - 0.1 mg/1.
-------
TABLE 6
RAW WASTEWATER ANALYSES AT WEIR NO. 2
196647 CITRUS PROCESSING SEASON
THE COCA-COLA COMPANY - AUBURN DALE. FLORIDA1 J)
Federal Water Quality Administration
Grant No. WPRD 38-01-67
Dates
1966
NOT.
29-30
Dec.
1-2
6-7
8-9
13-14
15-16
20-21
22-23
27-28
30-31
1967
faaM
JML
3-4
6-7
10-11
13-14
19-20
20-21
24-25
27
Jan. 31-
Feb.1
Feb.
3-4
7-8
10-11
15-16
17-18
21-22
Feb. 28-
Mar.l
Mar.
3-4
7-8
Average
Maximum
Mmnwm
Days
of
Week
Tu-W
Th-F
Tu-W
Th-F
Tu-W
Th-F
Tu-W
Th-F
Tu-W
F-Sa
Tu-W
F-Sa
Tu-W
F-Sa
Th-F
F-Sa
Tu-W
F
Tu-W
F-Sa
Tu-W
F-Sa
W-Th
F-Sa
Tu-W
Tu-W
F-Sa
Tu-W
Flow
MOD
6.86
6.04
10.7
13.5
14.1
15.3
11.0
10.4
17.6
18.4
16.4
21.3
19.9
17.6
17.6
22.7
25.6
22.4
2S.O
21.3
19.9
26.4
26.4
21.0
19.3
17.9
26.4
6.04
T o
mg/l
1450
450
388
450
J72
272
344
268
340
340
288
352
319
323
414
336
253
259
289
343
259
389
305
434
418
453
504
513
394
1450
253
S o
t a 1
%Vol.
84
49
69
56
65
62
60
63
68
63
66
74
79
73
62
61
70
85
57
68
61
67
75
95
65
75
82
81
69
85
49
1 1
d s
Suspended
mg/l
59
66
59
58
55
86
72
55
20
38
40
50
32
40
48
42
26
26
31
26
18
32
36
31
48
42
34
40
43
86
18
%VoL
61
65
66
38
31
19
89
62
95
100
82
80
100
100
83
83
100
96
94
88
89
94
94
90
83
36
88
90
80
100
19
Sett
ml/1
<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
9-hour composite, 7 AM -4PM.
(*) Nitrate nitrogen - 0.00 mg/l.
ft) Nitrate nitrogen - 0.03 mg/L
T-14
-------
TABLE 7
WASTEWATER POND CHARACTERISTICS & EQUIPMENT
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Aeration Settling Pond ( No. 2 )
Pond Sludge
Polishing Ponds Total
Parameter
(No. 1) Section Remainder Total (No. 3) (No. 4) System
Water depth, feet
Bottom dimensions, feet:
Length
Width
Area, acres:
Bottom
Water surface
Capacity, MMG:
Over bottom
Over slopes
Total
Cross section,
area, sq. ft. '
Aerators:
Number
Type
Horsepower,
(each)
11.7
14.2
9.7
5.0
4.5
380
235
2.05
3.15
7.815
1.889
210
439
2.11
2.72
8.305
0.906
327
439
3.29
4.06
10.404
1.153
537
439
5.40
6.78
18.709
2.059
576
463
6.12
6.85
9.963
0.583
464
581
6.19
6.85
9.074
0.475
19.76
23.63
45.561
5.006
9.704 9.211 11.557 20.768 10.546 9.549 50.567
4,536
6
Mechanical
75
' *' Over hopper bottom
T- 15
-------
TABLE 8
TREATMENT PLANT CHARACTERISTICS
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Pump Combination
Pumping capacity (Name plate), mgd
Rerirculation (about 100%), mgd
Plant influent, mgd:
Peak
Daily:
Average
Maximum
Minimum
BOD load, lbs/day(1)
Aeration Pond (No. 1)
Detention, hours:
Average
Maximum
Minimum
BOD load, Ib/day/hp
Settling Pond (No. 2):
Sludge removal section:
Detention, hours:
Average
Maximum
Minimum
Horizontal Velocity, fpm:
Average
Maximum
Surface Overflow Rate, gpd/s.f.
Average
Maximum
Small
9.33
4.5
4.8
4.5
4.8
<2.0
4,600
51.7
>116
48.5
10.2
49.2
>110
46.1
0.092
0.098
38
40
Large
16.74
8.0
8.7
8.1
8.7
<2.0
8,300
28.7
>116
26.7
18.5
27.3
>110
25.4
0.17
0.18
68
73
Large
Small
26.07
12.0
14.1
12.0
14.1
<2.0
12,300
19.4
>116
16.5
27.3
18.4
>110
15.7
1.25
0.29
101
119
Large
Large
33.48
14.5
19.0
14.5
19.0
<2.0
14,900
16.0
>116
12.2
33.1
15.2
>110
11.6
0.30
0.39
122
160
Large
Large
Small
42.81
15.5
27.3
15.6
27.3
<2.0
16,000
14.9
>116
8.5
34.7
14.2
>110
8.1
0.32
0.56
131
230
T-16
-------
TABLE 8
(continued)
TREATMENT PLANT CHARACTERISTICS
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Pump Combination
Small
Large
Large
Small
Large
Large
Large
Large
Small
Baffle Overflow Rate, gpd/s.f.:
Average
Maximum
Total Basin:
Detention, hours:
Average
Maximum
Minimum
Polishing Pond (No. 3):
Detention, hours:
Average
Maximum
Minimum
Polishing Pond (No. 4):
Detention, hours:
Average
Maximum
Minimum
Total Pond System:
Detention, days:
Average
Maximum
Minimum
BOD load, Ibs/day/acre
10,200 18,500 27,400 33,000 35,600
10,900 19,800 32,200 43,300 62,200
111 61.6 41.6 34.4 32.0
>250 >250 >250 >250 >250
104 57.4 35-4 26.3 18.3
56.3
>127
52.8
31.3
>127
29.1
21.1
>127
18.0
17.5
>127
13.3
16.2
>127
9.3
51.0 28.3 19.1
47.7 26.4 16.2
15.8 14.7
5 >115
12.1 8.4
11.25
>25.3
10.52
6.25
>25.3
5.82
4.22
>25.3
3.59
3.49
>25.3
2.66
3.24
>25.3
1.85
195
350
522
632
678
O) Basis average BOD of 123 mg/1.
T-17
-------
TABLE 9
AVERAGE ANALYSES 2.4-DAY DETENTION
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Hyacinth Pond*1*
Parameter
Temperature, degrees C.
pH
Dissolved oxygen, mg/1
Chemical oxygen demand, mg/1
Biological oxygen demand, mg/1
Total suspended solids, mg/1
Total organic nitrogen, mg/1 - N
Ammonia nitrogen, mg/1 - N
Nitrite nitrogen, mg/1 - N
Nitrate nitrogen, mg/1 - N
Total phosphate, mg/1 - P
Total nitrogen, mg/1 - N
Influent
7.3
1.9
68.3
22.1
33.8
4.46
0.48
0.002
0.33
0.75
5.27
Effluent
26.3
7.2
1.0
47.9
12.1
22.5
3.31
0.52
0.002
0.34
0.64
4.17
Percent Reduction
1.4
47.4
29.9
45.2
33.4
25.8
0
14.7
20.9
' *' Average analysis of nine sampling days.
T-18
-------
TABLE 10
HYACINTH POND MICROBIOTA
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE. FLORIDA
ORGANISMS
HYACINTH PLANT
ROOTS
HYACINTH POND
INFLUENT
HYACINTH POND
EFFLUENT
BACTERIA
FREE FLOATING
CHAIN
SPHAEROTILUS NATtNS
SARCINA
SPIRILLI
BEGGIATOA ALBA
THIOROHDACEAE
BLUE GREEN ALGAE
OSCILLHORIA SP.
450
GREEN ALGAE
ANKISTRODESHUS FALCATUS
AHIUSTRODESMUS TUMIDUS
CHLORELLA SP.
DICTYOSPHAERIUM EHERN.
SCENEDESIUS SP.
12800
9600
40
80
1600
16
1600
4
40
EUGLENOPHYCEAE
EUGLENA PISCIFORMIS
EUGLEHA SP.
PETALOMONAS CARINATA
PETALOUONAS PLAYFAIRI
PERANEMA TRICOPHORUM
TRACHELOMONAS VOLVOCINA
4
700
12
DIATOMS
CYCLOTELLA COMTA
NAY1CULA SP.
(DEAD)
(DEAD)
20
RHIZOPODA
AMOEBA VESPERTILIO
PELOMVXA SP.
ZOOFLAGELLATA
HEXANITUS INFLATUS
MASTIGAMOCHA SP.
NONAS SP.
OICOMONAS TERMO
TETRAMITUS PYRIFORMIS
ZOOFLAGEUATA
160
80
320
1600
640
24
4
CILIATA
CYCLIDIUM SALTANS
CYRTOLOPHOSIS
HALTERIA GRANLINELLA
LEMBUS FUSIFORMIS
METOPUS SP.
OXYTRICHA PELIONELLA
PARAMECIOM CAUDATA
SPIROSTOMUM AMBIGUUM
TRINYEMA SP
OROCENTRUM TORBO
VORTICEUA SP.
CILIATA
0.25
1
0.25
0.5
ROTIFER
(I) NUMBERS, WHERE REPORTED ARE AS ORGANISMS / ml
T-18
-------
TABLE 11
AVERAGE ANALYSIS S-DAY DETENTION
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Hyacinth Pond*1)
Parame ter
Temperature, degrees C
pH
Dissolved oxygen, mg/1
Chemical oxygen demand, mg/1
Biological oxygen demand, mg/1
Total suspended solids
Total organic nitrogen, mg/1 - N
Ammonia nitrogen, mg/1 - N
Nitrite nitrogen, mg/1 - N
Nitrate nitrogen, mg/1 - N
Total phosphate, mg/1 - P
Total nitrogen, mg/1 - N
Influent
6.90
1.24
106
56
21
3.27
0.26
0.002
0.04
0.76
3.58
Effluent
30.3
6.86
1.00
56
17
4
1.31
1.07
0.001
0.03
0.49
2.80
Percent Reduction
19.4
47.2
69.6
80.9
59.9
411<2>
50.0
25.0
35.5
21.8
' ' Average analyses of 5 sampling days. Continuous flow, 5-day detention.
^ ' Increase.
T-20
-------
TABLE 12
PRESSED LIQUOR ANALYSES
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Constituent
April 30
May 15
May 26
May 28
June 5
Average
Total Organic Nitrogen, mg/1— N
H
1 Ammonia Nitrogen, mg/1— N
to
Nitrite Nitrogen, mg/1— N
Nitrate Nitrogen, mg/l-N
Total Nitrogen, mg/l-N
Total Phosphate, mg/1— N
42
2.3
0.01
2.n
46.3
22.8
264
10.6
0.004
274.6
53.0
239
7.6
0
246.6
42.0
484
5.9
0.001
489.9
110.0
532
76
0.21
9.0
617.2
85.0
312
20.5
0.045
5.5
334.9
62.6
Liquid squeezed from hyacinth plants.
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
TABLE 15
DESIGN CHARACTERISTICS
AERATED LAGOON SYSTEM
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
H
1
to
Flow
mgd
11.8">
9.5^
6.4^)
5.3(4)
30.0(5)
BOD
Ibs/day
11,550
11,800
6,780
5,930
32,500
A e
Area, acres
9.93
9.93
9.93
9.93
51.0
ratio
Depth, ft.
11.5
11.5
11.5
11.5
12.0
n Ponds roiisning ronas
Horsepower
450
450
450
450
900
DO, mg/1
4.2
4.9
5.7
6.0
2.0
Area, acres
13.7
13.7
13.7
13.7
8l
Depth, ft
4.75
4.75
4.75
4.75
4.75
JDUU
%rem.
72.3
83.8
91.3
94.5
90.0+
DUU Luaumg
Ibs/day/acre
489
500
287
250
550
(1) Average data 1968-69 processing season
(2) Average-controlled influent flow June 1969
(3) Average-month of May 1969
(4) Average-controlled influent flow May 1969
(5) Required based on 1968-69 processing season
-------
TABLE 16
SUMMARY OF OPERATIONS 5 MGD FLOW RATE
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Total influent flow, MG
Average daily influent flow, MG
Average daily sludge recirculated, MG
Average percent sludge recirculated
Total pounds BOD - influent
Total pounds BOD - effluent
Average daily BOD - influent - mg/1
Average daily BOD - effluent - mg/1
Average BOD removal - percent
Total pounds COD - influent
Total pounds COD - effluent
Average daily COD - influent - mg/1
Average daily COD - effluent - mg/1
Average COD removal - percent
COD/BOD influent - average
COD/BOD effluent - average
Total pounds suspended solids - influent
Total pounds suspended solids - effluent
Average suspended solids - influent - mg/1
Average suspended solids - effluent - mg/1
Average total pounds MLSS (aeration basin)
Average MLSS, mg/1
Average pounds BOD/pound MLSS
Total hours aeration
Total pounds oxygen (3.5 Ibs 02/HP theoretical)
Pounds of oxygen / pounds of BOD applied
BOD load - pounds/day/HP (ave)
COD load - pounds/day/HP (ave)
Pounds of oxygen / pound of COD applied
100.7
5.3
4.8
91.4
112,632
6,156
134
7
94.5
174,610
40,413
208
48
76.9
1.6
6.6
15,117
7,559
18
9
3,964
49
1.5:1
2,520
661,500
5.87
14.3
22.2
3.79
T-26
-------
TABLE 16
(continued)
SUMMARY OF OPERATIONS 5 MOD FLOW RATE
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Detention time - hours (average)
Aeration (9.7 MMG) 43-9
Settling (20.8 MMG) 94.2
Sludge removal section (9.2 MMG) 41-7
Polishing pond No. 1 (10.5 MMG) 47.5
Polishing pond No. 2 (9.5 MMG) 43-0
Total system (days) (50.567 MMG) 9.5
BOD load, pounds/day/acre (approx. 23.6 acres) 251
Average temperature, ° C
Influent 29-6
Effluent 25-9
Average pH
Influent l'\
Pond 2 13
Effluent 7'9
Average dissolved oxygen - mg/1
Aeration pond *~
Settling pond }•'
Polishing pond No. 1 -•*
Polishing pond No. 2 *•*
Return sludge
Nitrogen 3 2
Average influent concentration, mg/1 *•*•
Average dosage added, mg/1
Total influent concentration, mg/1 *™
Total nitrogen - influent - pounds 5 >039
Total nitrogen-effluent-pounds
Nitrogen removed - percent
Total gallons ammonia used '
T-27
-------
TABLE 16
(continued)
SUMMARY OF OPERATIONS 5 MGD FLOW RATE
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Phosphorus
Average influent concentration, mg/1 0.9
Average dosage added, mg/1 0
Total influent concentration, mg/1 0.9
Total phosphorus - influent - pounds 756
Total phosphorus - effluent - pounds 588
Phosphorus removed - percent 22.2
Total gallons H3PO4 used 0
BOD:N 22.3:1
BOD-.P 148:1
BOD:N:P 100:4.5:07
Total rainfall - inches 1-8
T-28
-------
TABLE 17
SUMMARY OF OPERATIONS 10 MGD FLOW RATE
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Total influent flow, MG
Average daily influent flow, MG
Average daily sludge recirculated, MG
Average percent sludge recirculated
Total pounds BOD - influent
Total pounds BOD - effluent
Average daily BOD - influent - mg/1
Average daily BOD - effluent - mg/1
Average BOD removal - percent
Total pounds COD - influent
Total pounds COD - effluent
Average daily COD - influent - mg/1
Average daily COD - effluent - mg/1
Average COD removal - percent
COD/BOD influent - average
COD/BOD effluent - average
Total pounds suspended solids - influent
Total pounds suspended solids - effluent
Average suspended solids - influent - mg/1
Average suspended solids - effluent - mg/1
Average total pounds MLSS (aeration basin)
Average MLSS, mg/1
Average pounds BOD/pound MLSS
Total hours aeration
Total pounds oxygen (3.5 Ibs 02/HP theoretical)
Pounds of oxygen / pounds of BOD applied
BOD load - pounds/day/HP (ave)
COD load - pounds/day/HP (ave)
Pounds of oxygen / pound of COD applied
237.5
9.5
10.4
108.4
295,325
47,800
149
24
83.8
445,300
157,825
225
80
64.6
1.5
3.3
39,615
51,500
20
26
5,500
68
2.1:1
3,473.8
911,873
3.4
27.2
41.0
2.2
T-29
-------
TABLE 17
(continued)
SUMMARY OF OPERATIONS 10 MGD FLOW RATE
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Detention time - hours (average)
Aeration (9.7 MMG) 24.5
Settling (20.8 MMG) 52.5
Sludge removal section (9.2 MMG) 23.2
Polishing pond No. 1 (10.5 MMG) 26.5
Polishing pond No. 2 (9.5 MMG) 24.0
Total system (days) (20.567 MMG) 5.3
BOD load, pounds/day/acre (approx. 23.6 acres) 500
Average temperature, ° C
Influent 33.1
Effluent 28.7
Average pH
Influent 7.0
Pond 2 7.1
Effluent 7.3
Average dissolved oxygen - mg/1
Aeration pond 4.9
Settling pond 1.3
Polishing pond No. 1 1.5
Polishing pond No. 2 1.5
Return sludge 1 -7
Nitrogen
Average influent concentration, mg/1 4.5
Average dosage added, mg/1 2.8
Total influent concentration, mg/1 7.3
Total nitrogen - influent - pounds 14,459
Total nitrogen - effluent - pounds 4,952
Nitrogen removed - percent 65.8
Total gallons ammonia used 2.625
T-30
-------
TABLE 17
(continued)
SUMMARY OF OPERATIONS 10 MGD FLOW RATE
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Phosphorus
Average influent concentration, mg/1 1.48
Average dosage added, mg/1 .02
Total influent concentration, mg/1 1.5
Total phosphorus - influent - pounds 2,971
Total phosphorus - effluent - pounds 792
Phosphorus removed - percent 73.3
Total gallons H3PO4 used 75
BOD:N 20.4:1
BOD:P 99.0:1
BOD:N:P 100:4.9:1.0
Total rainfall - inches 1.6
T-31
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
TABIE 1 9
SUMMARY Of NITROGEN AND PHOSPHOROUS ANALYSES
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
196)
DEC 4
DEC 13
DEC 18
DEC 26
DEC 31
1969
JAN 7
FEB 6
FEB 9
FEB 19
FEB 25
MAR 4
MAR 1 1
MAR 18
MAR 24
MAY 5
MAT 12
MAY 19
HAY 26
JUN 2
JUN 16
JUN 20
JUN 23
AVERAGE
MAXIMUM
MINIMUM
CITRUS KASTEKATER - INFLUENT - ng/l
NITROGEN AS N
HH3
0.24
0.34
0.57
0.79
0.10
O.OB
0
0
0
0
0
o.te
0
0
0
0
0
0
0
0
0. II
3.26
0.29
3.26
0
ORO.
2.98
1.92
1.43
1 .49
2.711
1.30
1.68
1 .86
3.48
2.30
2.97
2.06
2.56
2.66
2.86
3.02
2.43
3.56
4.87
2.68
3.04
2.31
2.66
4.87
1.30
N02
0.001
0.012
0.020
0.018
0.014
0.010
0
0.003
0.002
0.004
0.001
0.012
0.002
0.002
0.004
0.004
0.007
0.001
0.001
0.002
0.003
0.001
0. 006
0.020
0
N03
0.09
0.08
0
0.06
0
0.21
0.07
0. 1 1
0.22
0. 10
O.OB
0.06
0. 19
0.17
0.36
0.51
0.41
0.26
0. 16
0.07
0.09
0.07
0. 15
0. 41
0
NHj
ADDED
1 .43
2.84
2.84
2.84
2.84
2.80
2.84
2.84
2.80
2.80
2.85
2.90
2.83
2.83
2.84
2.84
2.84.
2.84
2.84
2.84
2.84
2.84
2 .77
2.85
1 .43
TOTAL
4.74
5. 19
4.86
5.20
7.00
4.40
4.59
4.81
6.50
5.20
5.90
5.51
5.60
2.83
6.06
6.37
5.69
6.65
7.87
5.59
6.08
8.48
5.68
8.48
2.83
TOTAL PO|)-P
NAT.
1 .84
0.66
0.58
0.60
0.21
0.54
0.40
0.47
0.80
0.63
1 .03
0.94
0.96
0.70
1.14
0.85
0.77
1 .29
0.55
0.73
0.73T
1.34
0.81
1 .84
0.21
DOSED
1 .84
0.66
0.56
1.19
0.80
1.13
1.13
1 .20
1 .40
1 .22
1 .62
1.53
1 .55
0.70
1 .14
0.85
0.77
1 .88
1 . 14
0.73
0.73
1 .34
1 . IE
1 .88
0.58
SETTLING POND EFFLUENT - ng/l
NITROGEN AS N
NHj
2.43
0
0
0.66
0.07
0
0
0.69
0
0
0.59
2.34
0
0.92
0.62
_
1.03
0
0.28
0
0.39
l.ll
0.53
2.43
0
ORG.
10.26
3. 14
4.37
4.48
4.06
4.83
3.75
5.06
4. 18
2.34
4.57
3.15
4.04
3.35
3.50
_
4.64
4.81
2.00
5.05
3.72
3.66 •
4.24
10.26
2.00
N02
0
0.003
0.003
0.002
0.002
0.032
0
0.003
0.001
0
0.001
0
0
0.001
0.002
_
0.003
0.001
0.001
0 -
0.003
0.001'
0.001
0.003
0
N03
0
0.03
0.03
0.05
0
0. 18
0.05
0
0. 1 1
0
0.01
0
0.01
0.04
0.33
_
0.41
0. 14
O.IB
0.03
0,05
0.03
0.06
0.41
0
TOTAL
12.69
3. 17
4.40
5. 19
4. 13
5.01
3.80
5.57
4.29
2.34
5. 17
5.49
4.05
4.31
4.45
.
6.08
4.95
2.1(6
5.08
4. 16
4.80
4.84
12.6 >
2.34
TOTAL PO,-P
4.92
0.63
0.66
0.93
0.23
0.62
0.80
0.87
0.73
0.89
0.93
1 .83
1 .31
1 .00
0.90
.
0.64
O.B3
0.86
0.80
0.70
0.78
1 .04
4.92
0.23
FINAL EFFLUENT - ng/l
NITROGEN AS N
NH3
0
0 .
0
0
0
0
0
0
0
0
0.01
0.53
0
1 .64
0
1.51
0.33
0
0
0
0
0
0.16
1 .64
0
ORG.
2.30
3.46
4. 1 1
4, 15
4.08
4.92
3.56
3.00
3.39
2.09
2,75
3. 17
H.70
3.41
2.31
3.91
2.45
1.89
2.87
4.21
3.85-
3.63
3.37
4.92
1 .89
N02
0.008
0.002
0.002
0.002
0.001
0.005
0
0
0
0
0.001
0
0
0.001
0.005
0.005
0.009
0
0.001
0
0.002
0.001
0.002
0.009
0
N03
0
0.01
0.04
0.03
0
0.22
0.03
0
0. 10
0
0
0
0
0.07
0.31
0.38
0.40
0. 12
0.07
0.01
0.05
0.05
0.09
0.40
0
TOTAL
2.30
3.47
4. 15
4.18
4. 18
5. 14
3.61
3.00
3.49
2.09
2.76
3.70
4.70
5. 12
2.63
5.81
3. 19
2.01
2.94
4,22
3.90
3.68
3.64
5.81
2.CI
TOTAL PO,,-P
1.12
0.65
0.63
0,67
C.2I
0.65
0.73
0.73
0.67
0.57
0.75
1.12
1.48
1.35
0.69
0.94
0.47
0.36
0.53
0.71
0.61
0.66
0.74
1 .48
0.21
-------
TABLE 20
MONTHLY AVERAGE DATA
WASTEWATER TREATMENT PLANT
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
Month
(1968-69)
Nov.'1)
Dec.
Jan.
Feb.
Mar'(3)
Ma>>
June'5)
Average
Maximum' )
Minimum'8)
Flow
mgd
5.8
12.9
14.1
17.9
10.4
6.4
14.8
n.s'7)
26.6
0.8
BOD,
Inf.
106
109
147
120
65
127
133
124
250
14
mg/1
Eff.
12
39
47
39
17
11
34
28.4
126
2
BOD, Ibs/day BOD Removal Temperature, °C
Inf.
5,130
11,700
17,300
17,900
5,640
6,780
16,382
11,547(7)
49,474
782
Eff.
580
4,200
5,530
5,820
1,480
587
4,167
3,195<7)
19,743
38
Percent
88.7
64.2
68.0
67.5
73.8
91.3
74.6
72.3
98.4
20.9
Ambient
!6 8<*>
I'M*6)
15. 2^6)
13.9(6)
15.5(6)
21.3
21.6
17.0
34.2
15.0
Inf.
32.7
33.0
32.9
35.6
27.8
Pondl
22.3
25.4
27.7
25.8
22.4
28.8
31.0
26.2
32.2
20.0
Pond 4
17.2
22.8
22.7
20.6
18.7
25.6
30.4
22.6
32.0
15.0
15 days only
Changeover, BOD values not included
No data collected
Plant influent flow controlled - 5 mgd - May 1-19
Plant influent flow controlled - 10 mgd - May 20 - June 13
Weather bureau data - Lake Alfred
'') Value not absolute due to intentional bypass during research and plant overloads
' ) Maximum and minimum values are from daily operations during 1968-69 citrus processing season
-------
FIGURES
-------
FIGURE 1
AUBURNDAL
LOCATION MAP
THE COCA-COLA COMPANY
FOODS DIVISION
Auburndole, Florida
BLACK, CROW AND EIDSNESS, INC
Engineers
-------
FIGURE 2
PROJ LOCATION
F-2
-------
AUTOMATIC SAMPLER
(PROPORTIONAL FLOW)
Auburndal*, Florida
BLACK, CROW AND EIDSNESS, »
Enfineers
CITY EFFLUENT
® = DALL TUBES
AQUA AMMONIA
a
rL_____ AUTOMATIC SAMPLERS
L © = rPflRTlRIFt
PHOSPHORIC 1 1 I
ACID "" "*" _^^
RAW
WASTE
M01JM3AO
UJ
^ C3
>« x
t— e»
2: o-
WASTENATER TREATMENT PL
THE COCA-COLA COMPANY
FOODS DIVISION
• IFRITRR'! ffit VS/~ > . -. ^/7\ --,
yy Hunniuna \.\> ) SETTLING ^^~"~ •• — *\J/
— ®- 5 5? 5- Y BASIM
r * ~* * * _J"™""™T
~ LEVEL 1 i
® AERATION CONTROLl 1 / POLISHING PONDS
BASIN \ \y
*-JT?
TRANSFFR
PUMPS (3)
RECIRCULATED SLUDGE
TREATED WASTE
r
-------
99.99
99.9 99.S
99 98
95 90
1 0.5 O.Z 0.1 0.05
0.01
70 CO 50 40 30 20
0.01
0.05 0.1 0.2 0.5 1
10 20 30 40 50 60 70 80 90
Percent of Time Equal to or Less Than
98
99.8 99.9
99.99
-------
PAGE NOT
AVAILABLE
DIGITALLY
-------
1 0.5 0.2 0.1 0.05
0.01
80 70 60 50 40 30 20
0.01
0.05 0.1 0.2 0.5
20 30 40 SO 60 70 80
Percent of Time Equal to or Less Than
90 95
98 99
99.8 99.9
99.99
-------
WJ9 99.9
32
28
24
J» n 98 90 80 70 60 M 40 80 20 10
2 1 0.5 0.1 0.1 0.05
- f
:
20
X
3
16
12
I
/
::p
_
r
:
i
0.05 0.1 U U 1 2
5 U 20 30 40 50 60 70 60
Percent of Time Equal to or Less Than
90 95 98 99 99.8 99J 99.99
-------
99.99
99.9 99.8
99 98 95 90 80 70 60 50 40 80 20
10
5 2 1 O.J 0.2 0.1 0.08 0.01
45
«a
35
.30
25
|_ L
:
-H
:EE
8
±EE
13
10
3*rl
T
'
;
:
±
S-
ui oo9 ai oj oj i 2
10 20 JO 40 M 80 70 80
Percent of Time Equal to or Less Than
90 95 98 99
89.8 99.9
-------
100
140
120
100
co 00
.0
It
10
Jf
1
j
01
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it
tt
tt
i |
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99.9
0.05
i 1
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99.
Percent of Time Equal to or Less Than
-------
1 O.S 0.2 0.1 0.05 0.01
260
240
200
n, n
i ?o
80 70 60 50 40 30 20
0.01 0.05 0.1 0.2 O.S 1 2
10 20 30 40 50 60 70
Percent of Tine Equal to or Less Than
-------
FIGURE 10
F-10
-------
FIGURE 11
DAILY OPERATION RECORD
WEEKDAY
MONTH
FLOW DATA - H6D (ftCURES IN TEN THOUSANDS OF GALLONS (POND t) AND THOUSANDS OF GALLONS (RS), AS
RECORDED ON TOTALIZERS. READINGS TAKEN AT N., EACH DAY.)
EFFLUEHT POND 1
PRESENT DAY
PREVIOUS DAY
DIFFERENCE
RECIRCULATED SLUDGE
« INFLUENT FLOW
PLANT INFLUENT
EFFLUENT POND 1
RECIRCULATED SLUDGE -_
FLOI
PHOSPHORIC ACID
TIME
SETTING (GALS/24 HRS)
NUTRIENT FEED
AMMONIA
TIME
SETTING (GALS/24 HRS)
RAINFALL
INCHES
WASTE SLUDGE
ROUTINE SAMPLING AND TESTING RESULTS
SAMPLING POINT
t. PLANT INFLUENT
2. POND 1 EFFLUENT
3. POND 2 EFFLUENT
4. POND 3 EFFLUENT
S. POND 4 EFFLUENT
6. RECIRCULATED IASTE
7. PLANT INFLUENT
8. POND 1
B. ADAMS
REMARKS:
TYPE OF SAMPLE
DAILY COMPOSITE
DAILY GRAB
DAILY COMPOSITE
BAILY GRAB
DAILY COMPOSITE
DAILY GRAB
GRAB
BRAB
BAILY COMPOSITE
TEMP.
°C.
-
-
-
-
-
-
-
-
_
_
-
-
-
pH
-
-
-
00
•t/l
-
COD
•»/l
-
-
-
-
-
-
-
-
BOD
•B/l
-
-
-
-
-
-
-
_
—
-
-
SETT.
SOL.
• I/!
-
-
-
_
—
SUSPENDED SOLIDS
TOTAL
•B/l
-
* VOL.
-
-
-
-
-
-
-
_
-
-
-
—
OPERATOR
F-1
-------
APPENDICES
-------
APPENDIX 1
GRAB SAMPLE ANALYSES TAKEN DURING
JANUARY AND FEBRUARY
INDICATED THE FOLLOWING IN-PLANT FLOWS
AND WASTEWATER STRENGTHS: (1>
Source Flow, mgd COD,
The Coca— Cola Company
Hi-C Plant 2.0 2,750
By-products, including
feed mill and molasses
evaporator 2.0 640
Concentrate Plant
Process 3.0 810
Evaporator 7.0 50
Adams Packing Company
Concentrate Plant (total) 8.4 660
Juice Plant 1.5 830
Sectioning Plant 1.5 280
By-products, including
feed mill and molasses
evaporator 1.7 430
These are grab samples taken during periods of overload at the wastewater
treatment plant and the values are not considered to be typical under all operating
conditions.
Estimated flows.
A-l
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APPENDIX 2
AUBURNDALE - THE COCA-COLA COMPANY FOODS DIVISION
Kinetic Study at 20° C
Lo = 92 mg/1 Air 5 1pm
S.S. = 160 mg/1
Samples filtered through glass wool
Calculated O= 1.06
No Nutrients -
Hours
2
4
6
8
13
24
.0833
.1666
.2500
.3333
.5420
1.0000
Let x = Lo/L
Let y = t
83
71
44
50
30
27
Lo/L
Experimental
1.11
1.29
2.09
1.84
3.07
3.40
Lo/L
Least Squares
1.33
1.55
1.76
1.97
2.51
3.68
Slope
dy
dx
2.35 = 2.56
.9167
xy
m =
b =
m =
1.
2.
3.
4.
5.
6.
2
n 2 xy - 2 x
1.11
1.29
2.09
1.84
3.07
3.40
12.80
2y
1.11
1.29
2.09
1.84
3.07
3.40
0.0833
0.1666
0.2500
0.3333
0.5420
1.0000
0.0069
0.0277
0.0625
0.1111
0.2938
1.0000
0.0927
0.2149
0.5225
0.6133
1.6639
3.4000
n2y2-(Z y)2
x -
xy
nS y2-(2 y)2
6(6.5073) -(12.80)(2.375)
6(1.502) -(2.37S)2
2.373
n
= m
1.502
6.5073
= 2.564
b = (1.502X12.80)-(2.375X6.5073) =
6(1.502)-(2.375)2
n =
number of points
XQ = (2.564)(0) + 1.119 = 1.119
xj = (2.564)00833)+ 1.119 = 1.333
x2 = (2.564)01666) + 1.119 = 1.546
x3 = (2.564)02500) + 1.119 = 1.760
x4 = (2.564)(.3333) + 1.119= 1.967
x5 = (2.564)05420) + 1.119 = 2.508
x. = (2.564)(1.000) +1.119 = 3.683
A-2
-------
APPENDIX 3
AUBURNDALE - THE COCA-COLA COMPANY FOODS DIVISION
Kinetic Study at 20° C
Lo 92 mg/1 Air 5 1pm
S.S. = 160 mg/1
Samples filtered through glass wool
Calculated 0 = 1.06
Nutrients - 5 mg/1 NH3 - N + 1 mg/1 - PO4 - P ^2Q°C = 2.77
t L Lo/L Experimental Lo/L Least Squares
.0833 79 1.16 1.76
.1666 62 1.48 1.99
.2500 31 2.97 2.22
.3333 35 2.63 2.45
.5420 25 3.68 3.03
1.0000 24 3.84 4.30
dy 2.54
~ = 2'77
y xy
1. 1.16 .0835 .0069 .0969
2. 1.48 .1666 .0277 .2466
3. 2.97 .2500 .0625 .7425
4. 2.64 .3333 .1111 .8766
5. 3.68 .5420 .2938 1.9946
6. 3.84 1.0000 1.0000 3.8400
15.76 2.375 1.502 7.797
6(7.797) -(15.760X2.375) _
m = - /» - ~
6(1. 502) -(2.375)2
(1.502X15.760) - (2.375X7.797) _
b ~ 6(1. 502) -(2.375)2
x0 = (2.774)(0) +1.529 = 1.529
Xl = (2.774)(.0833) + 1.529 = 1.761
x2 = (2.774)(. 1666) + 1.529 = 1.991
x3 = (2.774)(.2500) +1.529 = 2.223
x4 = (2.774)03333) +1.5 29 = 2.454
x5 = (2.774)05420) + 1-529 = 3.033
x6 = (2.774)(1.000) +1.529 = 4.303
A-3
-------
APPENDIX 4
- THE COCA-COLA COMPANY FOODS DIVISION
k20°C = 2'86
Lo = 121
Temp = 25° C
S.S. = 220 mg/1
Lo/L Lo/L
Experimental Least Squares
.0833 121 1.00 0.729
.2708 95 1.27 1.413
.3542 81 1.49 1.717
1.0000 29 4.17 4.073
dy 3.344
Slope =
y2
xy
1. 1.00 .0833 .0069 .0833
2. 1.27 .2708 .0733 .3439
3. 1.49 .3542 .1244 .5278
4. 4.17 1.0000 1.0000 4.1700
S= 7.93 1.708 1.206 5.125
4(5.125)-(7.93X1.708) _
m ~ 4(1.206)-(1.70S)2
_ (1.206X7.93)-(1.708X5.125) = 0.425
4(1.206)-(1.708)2
x0 = 3.648 (0) + 0.425 = 0.425
xj = 3.648(.0833) + 0.425 = 0.729
x2 = 3.648C2708) + 0.425 = 1.413
x3 = 3.648C3542) + 0.425 = 1.717
x4 = 3.648(1.000) + 0.425 = 4.073
ir -V n 0T-20
kt k20°C G
k20°C =
» 3.65
1.276
k20oc =
A-4
-------
APPENDIX 5
THEORETICAL CONSIDERATIONS
AERATED LAGOON DESIGN
THE COCA-COLA COMPANY FOODS DIVISION
AUBURNDALE, FLORIDA
(Reference No. 3)
Influent BOD , XT> . „. ^ ,
= kt (Detention Tune) +1
Effluent BOD *
Where k* = BOD removal rate coefficient
Combined Wastewater Characteristics
Flow, mgd 30
BOD, mg/1 130
BOD, Ibs/day 32,500
BOD removal rate coefficient (^2Q°(^ * '^
Temperature coefficient, O 1.05
Wastewater temperature, °F 91.5
Minimum monthly ambient temperature, °F 59.0
1. Pond No. 1 Temperature 25.4° C
x
= (1.46X1-05)5-4
*25.4 = L9°
2. Detention Time (Winter Conditions)
Initial BOD _
Final BOD ~ 25A
130
— = 1.90D + 1
D = 5.2 days.
A-5
-------
3. Volume - (Average Pond Depth 12.0 Feet)
V = MGD x D
= (30X5.2)
= 156 MMG = 20.9 mcf = 1.74 mft2 = 40A
= (30X91.5) +(12)(1.74)(59) = o
rw 30+(12X1.74) h
Compared to 77.7°F from actual plant operation.
4. Oxygen Requirements
Ibs02/day = (1.3)(30X130X8.34)(.90)
= l,584pph
5. Oxygen Due to Surface Aeration
Ibs O2/hr/sq ft = 0.7(7.8 - 2.0) x 62.4 x 10"6
= 253 x 10"6
Surface area 1.74 x 106 sq ft
Ibs02/hr = (253)(1.74)
= 440
6. Oxygen Required from Mechanical Aerators
Nm = NfNs
N_ = O2 from mechanical aerators
Nt = Total oxygen required
NL = O^ from surface aeration
9 £
1,144 = 1,584-440
A-6
-------
7. H. P. Required - (Assume 12 large units will be sufficient)
= 95 Ibs 02/hr
95 Ibs (Whr/hp
2.51bS02/hr =38hp-Say40hp
.'. 12 - 40 hp units required (minimum)
A-7
-------
LIST OF REFERENCES
1. Fiske and Gay — Engineering Report on Florida Citrus Processing Industry
Wastewater Survey for Florida Citrus Commission, Lakeland, Florida,
(October 15,1965).
2. McNary, R.R., Dougherty, M.H., Wolford, R.W., "Determination of the Chemical
Oxygen Demand of Citrus Wastewaters." Sewage and Industrial Wastes, 29,
8, 894 (August, 1957).
3. Eckenfelder, W.W., Industrial Water Pollution Control, McGraw-Hill, New York
(1966, page 206).
4. Eckenfelder, W.W., "Designing Biological Oxidation Systems for Industrial Wastes."
Wastes Eng. May, June, July, 1961.
5. Penfound, W.T. and Earle, T.T., "The Biology of the Water Hyacinth." Ecological
Monographs, 18,447 (1948).
6. Clock, Raymond Maurice, "Nitrogen and Phosphorous Removal from a Secondary
Sewage Treatment Effluent," Doctoral Dissertation, University of Florida,
1968.
7. Furman, T. de S. and Gilcreas, F.W., "The Application of Oxidation Ponds to
Treatment of Residential Wastes," Phelps Laboratory, Department of Civil
Engineering, University of Florida, unpublished, 1965.
8. Mueller, J.A., Boyle, W.C., and Lightfoot, E.N., "Oxygen Diffusion Through a Pure
Culture Floe of Zooglea Ramigera." Proc. 21st Industrial Waste Conf.,
Purdue University, Extension Service 121, 964 (1967).
9. Eckenfelder, W.W., "A Theory of Activated Sludge Design for Sewage." Presented at
"The Activated Sludge Process in Sewage Treatment — A Seminar,"
University of Michigan, Ann Arbor, February 17,1966.
-------
Additional References — Not Cited in Text
Moore, W.A., Kroner, R.C., and Ruchhoft, C.C., "Dichromate Reflux Method for
Determination of Oxygen Consumed." Anal. Chem. 21, 8, 953 (August,
1949).
McNary, R.R., Wolford, R.W., and Patton, V.D., Food Technology, 5, 319 (1951).
Moore, W.A., Ludzach, F.J., and Ruchhoft, C.C., "Determination of Oxygen
Consumed Values of Organic Wastes." Anal. Chem. 23, 9, 1927 (September,
1951).
O'Neal, B.F., "Progress Report No. 1, Citrus Waste Research Program." Florida
State Board of Health (August 5,1952).
Ibid., Final Report (August 10,1953).
McNary, R.R., Wolford, R.W., and Dougherty, M.H. Proceedings 8th Industrial
Wastes Conference, Purdue University (1953).
Wakefield, J.W., O'Neal, B.F., and Kelson, F.S., Proceedings 9th Industrial Wastes
Conference, Purdue University (1954).
McKinney, R.E., Poliakoff, L., and Weichlein, R.G. "Citrus Waste Treatment
Studies." Water and Sewage Works, 101, 123 (1954).
Dougherty, MM., Wolford, R.W., and McNary, R.R., "Citrus Waste Water Treatment
of Activated Sludge." Sewage and Industrial Wastes, 27, 7, 821 (July, 1955).
Lackey, James B., Call aw ay, Wilson T., and Morgan, George B., "Biological
Purification of Citrus Wastes." Presented at the 28th Annual Meeting,
Federation of Sewage and Industrial Wastes Assns; Atlantic City, N.J.,
October 10-13,1955.
McNary, R.R., Wolford, R.W., and Dougherty, M.H., "Pilot Plant Treatment of
Citrus Wastewater by Activated Sludge." Sewage and Industrial Wastes, 28,
7, 894 (July, 1956).
Dougherty, M.H., and McNary, R.R., "Elevated Temperature Effect on Citrus Waste
Activated Sludge." Sewage and Industrial Wastes, 20,1263 (October, 1958).
Ludwig, R.G., and Stone, R.V., "Disposal Effects of Citrus by-products Wastes."
Water and Sewage Works 109, 11, 410 (November, 1962).
Dougherty, M.H., "Activated Sludge Treatment of Cirrus Waste." Jour. Water
Pollution Control Federation 36, 72 (January, 1964).
-------
BIBLIOGRAPHIC: Black, Crow and Eidsness, Inc. Citrus Processing
Wastewater Treatment FWQA Publication No. WPRD-38-01-67.
1970.
ABSTRACT: Plant scale studies were performed to determine
operational and treatment parameters for citrus processing
wastewaters. Part I discusses treatment of concentrated citrus
processing wastewaters combined with domestic sewage using a
modified activated sludge process; namely, extended aeration. Part
II discusses treatment of weak processing wastewaters using a
system which functioned as an aerated lagoon. Extended aeration
yielded 94 to 95 percent BOD removal; however, difficulties
concerning positive control of the treatment process were
encountered. Variations in mixed liquor suspended solids
concentrations, sludge volume indices, sludge reciiculation rates,
and hydraulic loading were considered principal causes adversely
affecting the treatment process. Excess sludge buildup amounted to
approximately 0.5 pounds per pound of influent BOD and sludge
wastage accounted for the greater portion of overall nutrient
removal from the system. The aerated lagoon process afforded 91
percent BOD removals when daily average hydraulic and organic
loadings were controlled at 6.4 mgd and 6,770 pounds, respectively
(detention time 7.9 days). Kinetic studies yielded a BOD removal
ACCESSION NO.
KEYWORDS:
Citrus wastewater
treatment
Extended aeration
Aerated lagoons
Organic nutrients
removal
Hyacinth plants
Cattle feed
Removal rates
coefficient
Ecological study
COD/BOD ratio
BOD:N:P ratio
BIBLIOGRAPHIC: Black, Crow and Eidsness, Inc. Citrus Processing
Wastewater Treatment FWQA Publication No. WPRD-38-01-67.
1970.
ABSTRACT: Plant scale studies were performed to determine
operational and treatment parameters for citrus processing
wastewaters. Part I discusses treatment of concentrated citrus
processing wastewaters combined with domestic sewage using a
modified activated sludge process; namely, extended aeration. Part
II discusses treatment of weak processing wastewaters using a
system which functioned as an aerated lagoon. Extended aeration
yielded 94 to 95 percent BOD removal; however, difficulties
concerning positive control of the treatment process were
encountered. Variations hi mixed liquor suspended solids
concentrations, sludge volume indices, sludge recirculation rates,
and hydraulic loading were considered principal causes adversely
affecting the treatment process. Excess sludge buildup amounted to
approximately 0.5 pounds per pound of influent BOD and sludge
wastage accounted for the greater portion of overall nutrient
removal from the system. The aerated lagoon process afforded 91
percent BOD removals when daily average hydraulic and organic
loadings were controlled at 6.4 mgd and 6,770 pounds, respectively
(detention time 7.9 days). Kinetic studies yielded a BOD removal
ACCESSION NO.
KEY WORDS:
Citrus wastewater
treatment
Extended aeration
Aerated lagoons
Organic nutrients
removal
Hyacinth plants
Cattle feed
Removal rates
coefficient
Ecological study
COD/BOD ratio
BOD: N:P ratio
BIBLIOGRAPHIC: Black, Crow and Eidsness, Inc. Citrus Processing
Wastewater Treatment FWQA Publication No. WPRD-38-01-67.
1970.
ABSTRACT: Plant scale studies were performed to determine
operational and treatment parameters for citrus processing
wastewaters. Part I discusses treatment of concentrated citrus
processing wastewaters combined with domestic sewage using a
modified activated sludge process; namely, extended aeration. Part
II discusses treatment of weak processing wastewaters using a
system which functioned as an aerated lagoon. Extended aeration
yielded 94 to 95 percent BOD removal; however, difficulties
concerning positive control of the treatment process were
encountered. Variations in mixed liquor suspended solids
concentrations, sludge volume indices, sludge recirculation rates,
and hydraulic loading were considered principal causes adversely
affecting the treatment process. Excess sludge buildup amounted to
approximately 0.5 pounds per pound of influent BOD and sludge
wastage accounted for the greater portion of overall nutrient
removal from the system. The aerated lagoon process afforded 91
percent BOD removals when daily average hydraulic and organic
loadings were controlled at 6.4 mgd and 6,770 pounds, respectively
(detention time 7.9 days). Kinetic studies yielded a BOD removal
ACCESSION NO.
KEYWORDS:
Citrus wastewater
treatment
Extended aeration
Aerated lagoons
Organic nutrients
removal
Hyacinth plants
Cattle feed
Removal rates
coefficient
Ecological study
COD/BOD ratio
BOD:N:P ratio
-------
rate coefficient foe chnis processing wastewaten of 1.46 and an
avenge temperature coefficient of 1.05. Ecological studies
indicated that BOD:N:P ratios of the older of 150:5:1 were
adequate for supporting the population of organisms required for
effective bio-oxidation. Organic nutrient removal studies using
hyacinths indicated a mhrfmnm of 5 day,* detention would be
required to afford substantial nutrient reduction. Significant
organic loading redactions (BOD.COD) wen also attained by the
hyacinth plant system during the 5-day detention period. It was
found mat dried hyacinth plants were similar in food value to
alfalfa hay and could be used as a supplement in cattle feed. This
report was submitted in fulfillment of Demonstration Giant No.
WPRD-3M1-67 between the Federal Water Quality Administration
and the Coca-Cola Company. Foods Division.
rate coefficient for dtros processing wastewaten of 1.46 and an
avenge temperature coefficient of 1.05. Ecological studies
indicated mat BOD:N:P ratios of the order of 150:5:1 were
adequate for supporting the population of organisms required for
effective bio-oxidation. Organic nutrient removal studies using
hyacinths indicated a minimum of 5 days* detention would be
required to afford substantial nutrient reduction. Significant
organic loading reductions (BOD.COD) were abo attained by UK
hyacinth plant system during the 5-day detention period. It was
found mat dried hyacinth plants were similar in food value to
alfalfa hay and could be used as a supplement in cattle feed. This
report was submitted in ruHUhnent of Demonstration Grant No.
WPRD-38-01-67 between the Federal Water Quality Administration
and the Coca-Cola Company, Foods Division.
rate coefficient for citrus processing wastewaten of 1.46 and an
average tempetanue coefficient of 1.05. Ecological studies
indicated mat BOD:N:P ratios of the order of 150:5:1 were
adequate for supporting the population of organisms required for
effective bio-oxidation. Organic nutrient removal studies using
hyacinths indicated a minimum of 5 days' detention would be
requked to afford substantial nutrient reduction. Significant
organic loading reductions (BOD.COD) were abo attained by the
hyacinth plant system duiing the 5^1ay detention period. It was
found mat dried hyacinth plants were shnflar in food value to
alfalfa hay and could be used as a supplement in cattle feed. This
report was submitted in fulfillment of Demonstration Grant No.
WFRD-38-01-67 between the Federal Water Qnalty Administration
and the Coca-Cola Company, Foods Division.
-------
1
5
Accession Number
Organization
Coca-Cola
2
Subject Field & Group
05D
SELECTED WATER RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
Company, Foods Division
Orlando, Florida
Title
Treatment of Citrus Processing Wastes
10
Authorfs)
Goodson, James B. and
Smith, Jack J.; Black, Crow
and Eidsness
16
Project Designation
O1 Note
-fUDate:
Project Number: 12060 Series
July, 1970 Contract Number: FWQA Grant
WPRD 38-01-67
22
Citation
23
Descriptors (Starred First)
*Citrus wastewater treatment
^Extended aeration
*Aerated lagoons
Organic nutrients removal
Hyacinth plants
Cattle feed
Removal rates coefficient
Ecological study
COD/BOD ratio
BOD:N:P ratio
95 Identifiers (Starred First)
27
Abstract
Plant scale studies were performed to determine operational and treatment parameters
for citrus processing wastewaters. Part 1 discusses treatment of concentrated
citrus processing wastewaters combined with domestic sewage using a modified activated
sludge process; namely, extended aeration. Part 11 discusses treatment of weak
processing wastewaters using a system which functioned as an aerated lagoon. Extended
aeration yielded 94 to 95 percent BOD removal; however, difficulties concerning positive
control of the treatment process were encountered. Variations in mixed liquor sus-
pended solids concentrations, sludge volume indices, sludge recirculation rates, and
hydraulic loading were considered principal causes adversely affecting the treatment
process. Excess sludge buildup amounted to approximately 0.5 pounds per pound of
influent BOD and sludge wastage accounted for the greater portion of overall nutrient
removal from the system. The aerated lagoon process afforded 91 percent BOD removals
when daily average hydraulic and organic loadings were controlled at 6.4 mgd and
6,770 pounds, respectively (detention time 7.9 days). Kinetic studies yielded a
BOD removal.
Abstractor
D. W. Hill
Institution
Southeast Water Laboratory, FWQA.
WR:102 (REV. JULY I9S9)
WRSIC
SEND TO:
WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U.S. DEPARTMENT OF THE INTERIOR
WASHINGTON. D. C. 20240
ft GPO : 1971 O - 421-931
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