WATER POLLUTION CONTROL RESEARCH SERIES • 12040 ELW 12/70
Aerated Lagoon Treatment
of Sulfite Pulping Effluents
U. S. ENVIRONMENTAL PROTECTION AGENCY
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¥ATER POLLUTION CONTROL RESEARCH SERIES
The Water Pollution Control Research Reports describes
the results and progress in the control and abatement
of pollution of our Nation's waters. They provide a
central source of information on the research, develop-
ment and demonstration activities of the Environmental
Protection Agency, through inhouse research and grants
and contracts with Federal, State and local agencies,
research institutions, and industrial organizations.
Inquiries pertaining to Water Pollution Control Research
Reports should be directed to the Head, Publications
Branch, Research Information Division, Research and
Monitoring, Environmental Protection Agency, Washington,
D. C. 20^60.
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AERATED LAGOON TREATMENT OF
SULFITE PULPING EFFLUENTS
By
Crown Zellerbach Corporation
Lebanon Division
Lebanon, Oregon
for the
Environmental Protection Agency
Program Number 12040 ELW
Project Number WPRD 69-01-68
December, 1970
For sale by the Superintendent of Documents, U.S. Government Printing Office
Washington, D.C., 20402 - Price $1.25
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EPA REVIEW NOTICE
This report has "been reviewed "by the Environmental
Protection Agency and approved, for publication.
Approval does not signify that the contents neces-
sarily reflect the views and policies of the
Environmental Protection Agency, nor does mention
of trade names or commercial products constitute
endorsement or recommendation for use.
11
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ABSTRACT
Secondary treatment of sulfite pulp and paper mill effluents in aerat-
ed stabilization basins was tested on a full-scale basis over a 17 month
period of continuous operation. The secondary treatment plant consisted
of two aeration basins. One basin was equipped with two 75-h. p. surface
aerators and the other basin of equal volume was equipped with six 25-
h. p. aeration units. Piping was designed to permit series and parallel
operation of the two basins and provisions were made to recycle treated
waste. The waste treated was a mixture of weak wash water from the
pulp mill, evaporator condensate from the spent liquor recovery system
and paper machine white water.
Experimentation conducted over the 17 month period showed that
series operation was more efficient than parallel operation and that the
75-h. p. surface aerators were much more efficient mixing and aeration
devices than equivalent capacity of 25-h. p. units. An 80% BOD reduc-
tion in the combined secondary system could be achieved at a BOD load
of 3. 53 Ibs. /I, 000 cu. ft. of aeration capacity or 2. 2 Ibs. /h. p. -hr.
This was equivalent to a daily BOD load of 16, 000 Ibs. Biological treat-
ment of the mill waste to a BOD reduction of 80 to 85% produced a waste
which did not readily support slime growth when added to simulated
experimental streams. Although slime growth was closely related to the
amount of BOD added to the simulated streams, two to three times as
111
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much slime was produced from untreated waste than for equivalent BOD
additions of treated waste.
Total operating cost including interest on investment and depreciation
was $169, 500 per year or $4. 79/ton of production. Total operating cost
per pound of BOD destroyed was 3. 48 cents.
This report was submitted in fulfillment of Grant Number WPRD
69-01-68, Program Number 12040 ELW under the sponsorship of the
Federal Water Quality Administration.
KEY WORDS : Aeration basin, BOD removal, Pulping wastes, Sulfite
wastes, Slime growth, Sphaerotilus natans, Surface
aerators, Treatment costs.
IV
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CONTENTS
Page
TITLE PAGE i
FWQA REVIEW NOTICE ii
ABSTRACT iii
SUMMARY AND CONCLUSIONS 1
INTRODUCTION °
GRANT PROGRAM PLAN 11
PROCESS DESCRIPTION AND WASTE TREATMENT
FACILITIES 12
METHODS AND PROCEDURES 20
Sampling 20
Analytical Methods 21
OPERATIONAL RESULTS AND DISCUSSION 26
Nutrient and Chemical Requirements 26
Series Versus Parallel Operation 31
Effect of BOD Load on BOD Reduction 37
Effect of Retention on BOD Reduction 45
Temperature Effects 4#
Recirculation of Treated Waste 54
Surface Aerator Comparison 59
Solids Production in Secondary System 71
Nutrient Content of Waste Discharged 73
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CONTENTS CONTD.
Page
Composite Waste Characteristics 74
Waste Load Discharged to South Santiam River 76
Slime Growth from Treated and Untreated Waste 76
Capital Cost of Secondary Treatment System 80
Operating Costs Si
A CKNOW LEDGEMENTS 85
REFERENCES 92
APPENDIX 96
VI
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FIGURES
No. Page
1 An Aerial Photograph of Lebanon Division of 14
Crown Zellerbach Corporation Showing Aeration
Basins in Background
2 Detailed Flow Diagram of Lebanon Waste Treatment 15
Plant
3 Aerial Photograph of Secondary Treatment Plant IB
4 Simplified Flow Diagram of Lebanon Waste 19
Treatment Facilities
5 Effect of pH on BOD Reduction - Laboratory 2?
Experiments
6 Effect of Phosphorous on BOD Reduction - 29
Labo ratory Expe rim en z ~
7 Dissolved Oxygen Profiles for Aeration Ponds in 38
Series Operation - Pond II to Pond I, February
16, 1970
8 Dissolved Oxygen Profiles for Aeration Ponds 39
When Operated in Parallel on February 23, 1970
9 Effect of BOD Load on BOD Reduction for Ponds I 39
and II
10 Relationship Between BOD Loading and BOD 42
Reduction for Combined Secondary System
11 Effect of BOD Load on BOD Reduction for 44
Combined Secondary System
12 Influent and Effluent BOD Concentrations, 46
Secondary System
13 Effect of Retention on BOD Reduction Under 49
Variable BOD Load, Pond II
VII
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FIGURES CONTD.
No.
Page
14 Effect of Ambient Temperature on Heat Losses 53
and Temperature Drop in Secondary System
15 Schematic Flow Diagram of Secondary System 56
During Recirculation Experiment, September 19
to October 22, 1969
16 Aerator Costs versus Horsepower 61
17 Performance Comparison, Large versus Small 63
Surface Aerators
18 Relationship Between Size of Surface Aerators and 64
Allowable BOD Load
19 Sample Points Used in Conducting Concentration 65
Profiles
20 Relationship Between COD and BOD, Composite 75
Effluent
21 Slime Growth from Untreated and Treated Waste in 79
Simulated Streams
Vlll
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TABLES
No. Page
1 Aeration Pond Dimensional Details 16
2 The Effect of pH on BOD Reduction in Combined 30
Treatment System
3 The Effect of Phosphorous on BOD Reduction 32
(Combined Treatment System)
4 Characteristics of Influent and Effluent During 34
Parallel and Series Operation
5 Comparison of Performance - Series versus 35
Parallel Operation
6 Summary of Performance Under Series and Parallel 36
Operation
7 BOD Performance of the Two Aeration Basins 41
8 Performance of Combined Treatment System 43
9 The Effect of Retention on BOD Reduction 47
10 Average Monthly Ambient Temperatures and 50
Evaporation Rates at Corvallis-Albany Stations
11 Secondary Treatment System Temperature Data 51
and Calculated Heat Losses
12 Recirculation of Treated Waste - Character- 57
isties of Influent, Effluent and Composite Samples
13 Recirculation of Treated Waste - Summary of BOD 58
Data
14 Effect of Recycle on Operating Performance of 59
Pond II
15 Comparison of Performance of 75-h. p. Surface 70
Aerators in Pond II
IX
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TABLES CQNTD.
No. Page
16 The Effect of Bacterial Suspended Solids on the 73
Growth of Vorticella in Simulated Streams (by
Rader)
17 Slime Growth Potential of Treated and Untreated 78
Waste Added to Simulated Streams
18 Capital Cost of Secondary Treatment System 81
19 Monthly Direct Operating Costs Exclusive of 33
Interest and Depreciation
20 Summary of Direct and Indirect Operating Costs 84
21 Direct Operating Costs Exclusive of Interest and 85
Depreciation
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SUMMARY AND CONCLUSIONS
Secondary treatment of sulfite pulp and paper mill effluent in
aerated stabilization basins was tested on a full-scale basis over a
17 month period of continuous operation. The secondary treatment
plant consisted of two aeration basins each having a surface area of
5. 42 acres or a liquid volume of 17 million gals. At a total waste flow
of 4 mgd from the mill, the combined secondary system provided a
detention of about eight days. The ponds were constructed to permit
series or parallel operation and provisions were made to recycle
treated waste. One basin was equipped with two 75-v: v . arfaee aer-
ators and the other basin of equal volume wa;;- equip ; v six 25-h.p,
aeration units. One of the 75-h.p. aerators was a direct drive, high
speed unit whereas the other was a low speed gear driven unit. The
25-h. p. surface aerators were direct drive, high speed units.
The treatment works were designed and constructed to achieve
economy, efficiency and effectiveness in the prevention or abatement
of pollution. Furthermore, the design of the process piping, equipment
arrangement and structures in the facility provided for a maximum flex-
ibility of operation and convenience in operation and maintenance. The
waste treated was a mixture of weak wash water from the pulp mill,
evaporator condensate from the spent liquor recovery system and paper
machine white water.
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The results from 17 months of experimentation warrant the follow-
ing conclusions:
1. Series operation was considerably more efficient in BOD
destruction than parallel operation. At a BOD load of 22, 000
Ibs. /day or 4.85 Ibs. /I, 000 cu. ft. of aeration capacity, para-
llel operation resulted in the destruction of 14, 300 Ibs. of BOD/
day (3. 15 Ibs. /I, 000 cu. ft.) compared to 16,200 Ibs. /day
(3. 57 Ibs. /I, 000 cu. ft.) for series operation.
2. To achieve an 80% BOD reduction in the secondary system, the
pond with the six 25-h. p. surface aerators was loaded at 1. 9
Ibs. of BCD/h. p. -hr. or 6, 600 Ibs. /day (2. 91 Ibs. /I, 000 cu.
ft.) and the pond with the two 75-h. p. surface aerators received
a load of 2.8 Ibs. /h.p. -hr. or 9,740 Ibs. /day (4.29 Ibs. /I, 000
cu. ft.). The BOD load to the combined system should not
exceed 16, 000 Ibs. /day (3. 53 Ibs. /I, 000 cu. ft.) or 2.2 Ibs. /
h.p. -hr. to maintain the desired 80% BOD reduction in the
secondary system. An 80% reduction at a load of 20, 000 Ibs. /
day or 4. 41 Ibs. /I, 000 cu. ft. could be achieved by increasing
the total aeration capacity from 300 h.p. to 375 h.p.
3. The 75-h. p. surface aerators were much more efficient mixing
and aeration devices than equivalent capacity of 25-h. p. units.
Nine 25-h. p. surface aerators would be required to achieve the
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same BOD reduction as the two 75-h. p. units. Good mixing
characteristics for the 75-h. p. surface aerators were obtained
at a spacing of about 2. 1 ft. /h. p. The installed cost of the 75-
h.p. Welles surface aerator was $285/h.p. compared to $375/
h. p. for the 25-h. p. Welles units. On the basis of equivalent
BOD reductions, the installed aeration capacity of 75-h. p.
Welles units would have a total cost of $85, 500 compared to
$140, 500 for the 25-h.p. Welles units.
4. No conclusive data were collected which demonstrated any dif-
ference in mixing characteristics and aeration capacity between
the direct drive, high speed, Welles aerator and the low speed,
gear driven Mixco unit.
5. D. O., temperature and BOD profiles conducted in the two ponds
showed the pond with the two 75-h. p. surface aerators was com-
pletely mixed, i. e. , BOD concentration and temperature grad-
ients were not noted from waste inlet to outlet. There was a
definite BOD concentration gradient from inlet to outlet of the
pond with the six 25-h. p. surface aerators. The velocity
profiles also confirmed that the large surface aerators -were
much more effective mixing devices than the small units.
6. Operational labor requirements for the secondary system were
very low because of the ease of operation. Wide variation in
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the incoming waste strength had only minimal effects upon treat-
ment efficiency.
7. Although slime growth was closely related to the amount of BOD
added to the simulated experimental streams, two to three times
as much slime was produced from untreated waste than for
equivalent BOD additions of treated waste. Biological treat-
ment of the combined mill waste to a BOD reduction of 80%
resulted in slime growth reductions in excess of 80% as mea-
sured in the simulated streams.
8. Optimum pH ranged from 6. 5 to 7. 5. Ammonia usage for neu-
tralization varied from 198 Ibs. /day to 2, 500 Ibs. /day and phos-
phorous addition rates of less than 40 Ibs. /day were sufficient
to maintain optimum efficiency. Sodium hydroxide and ammo-
nium hydroxide were interchangeable as neutralization chemi-
cals but sodium hydroxide was considerably costlier.
9. Retention periods in excess of 7 days did not show a significant
improvement in operating efficiency.
10. Aeration temperatures within the range of 16° C. to 26° C.
(61° to 79° F.) did not have a significant effect upon BOD
reduction.
11. The average heat loss from the secondary system during the
summer period was 534, 000 BTU/day when the incoming waste
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temperature averaged 33° C. (91° F.). During the winter sea-
son, the heat losses averaged 793, 000, 000 BTU/day. During
the winter, a drop in pond temperature of 11.7° C. (21° F.) can-
be expected and during the summer the temperature drop will
average 8. 3° C. (15° F. ).
12. Recirculation of treated waste resulted in a drop of efficiency
which was attributed to an overall reduction in waste retention.
13. The effluent discharged from the treatment plant contained about
62 ppm of suspended solids and had an average turbidity of 214
JTU. The turbidity consisted of dispersed bacteria which were
not removed by sedimentation. Suspended biological solids
buildup was calculated at 0. 16 Ibs. /lb. of BOD destroyed.
14. The final treated effluent contained about 155 ppm of total
Kjeldahl-nitrogen and 0. 6 ppm of soluble phosphorous. Elimi-
nation of ammonia for neutralization reduced the Kjeldahl-nitro-
gen concentration in the treated effluent to about 98 ppm.
15. The capital cost of the Lebanon secondary treatment plant was
$665, 000. Total annual operating costs including interest on
investment and depreciation was $169, 500 or $4. 79/ton of
production. Total operating cost per pound of BOD destroyed
was 3. 48 cents or $ 111. 20 per million gallons of waste treated.
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INTRODUCTION
The Crown Zellerbach pulp and paper mill at Lebanon, Oregon has
been in operation since 1890. Straw was first used as a raw material
and major changes were made in the basic pulping equipment in 1906 when
the mill was converted to the use of hemlock logs. Changes and modifi-
cations have bean made since and the plant now has a rated capacity of
100 tons/day of,unbleached sulfite pulp which is converted on two paper
machines.
Late in 1949 the mill was converted to ammonia base pulping and a
pilot plant recovery unit was installed to study the possibility of evapor-
ating and burning the digester strength cooking liquor. The recovery
phase of the operation is described in detail by Palmrose and Hull (1).
Based upon the successful pilot plant work, a full scale by-product
recovery unit was placed on stream in 1952. A detailed description of
the by-product operation has been presented by Amberg (2).
The Lebanon mill is located on the South Santiam River which supports
a sizeable anadromous fish run. Upstream impoundments now provide
for a minimum drought flow of about 500 to 600 cfs. The discharge of
untreated waste to the South Santiam River created two problems, both
of which could have adverse effects upon the fishery resource. Heavy
bacterial slime infestations generally extended to about six miles below
the introduction of the untreated waste and a significant depression in
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the dissolved oxygen concentration of the stream occurred during the
summer drought period.
The effects of waste effluents upon the aquatic environment and
particularly on the microbiological population of streams have been
studied by many investigators. Cawley (3) has called attention to the
biological imbalance in a stream receiving the effluents from a pulp mill
producing dissolving grade pulp by the kraft process. Lincoln and
Foster (4) have reported in detail the problem of slime infestations below
the outfalls of sulphite pulp mills on the lower Columbia River. The
factors affecting slime growth and an evaluation of several control methods
were discussed by Amberg and Cormack (5).
Amberg and Cormack (5) found that one of the most effective pro-
cesses for controlling slime growths from ammonia base spent sulfite
liquor was an aerobic bacterial treatment employing a mixed culture of
bacteria capable of reducing 80% to 95% of the applied BOD load. These
experiments were in agreement with experimentation reported by
Wuhrmann (6). Because of the small size of the Lebanon mill and the
marginal economics of the operation, a treatment system to be success-
ful must meet the following basic requirements: (1) ease of operation,
(2) high BOD reduction, (3) low capital investment, and (4) low operating
and maintenance costs. These requirements could be expected to apply
equally to many small sulfite mills throughout the country which face
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similar problems. The ultimate treatment plant design selected for
the Lebanon mill met all of these requirements and since sufficient land
was available on the mill property, the construction of the aerated
stabilization basins presented no serious problems. A comparison of
capital and operating costs for several types of treatment has been pre-
sented by Amberg (7) which shows the economic benefits of aerated
stabilization basin treatment over the activated sludge process.
Aerated stabilization basins are quite widely used throughout the
pulp and paper industry in the United States and Canada. Early labora-
tory studies (8) showed that paper machine white water could readily be
treated by aeration in the presence of dispersed bacterial growths and
that relatively high BOD reductions could be achieved in 5 to 6 days.
Gellman (9) has discussed the application of this method for the treatment
of pulp and paper mill effluents.
Although laboratory and field investigations have demonstrated the
potential of secondary treatment by the aerated stabilization basin pro-
cess, a number of factors which could have a decided effect upon oper-
ational performance and economics have not been thoroughly studied
and evaluated by means of a full scale field study. Some of these factors
such as series versus parallel operation, waste recycle, aerator con-
figuration, aerator size, nutrient levels, etc. have not been studied in
detail because of lack of adequate funds to conduct a study of this nature.
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With the anticipated demands on the nation's water resources, it is
essential that treatment works be designed and constructed to achieve
economy, efficiency and effectiveness in the prevention and abatement
of pollution. The aerated basin design for the Lebanon mill was selec-
ted to be economically attractive to small pulp and paper mills or other
industrial operations which operate at rather small margins of profit.
An application was made to the Federal Water Quality Administra-
tion for funding of a research and demonstration facility which would
meet all of the foregoing requirements. The results of this work and
conclusions evolved from these results are the subject of this final
report for the project.
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GRANT PROGRAM PLAN
The experimental program described in this report may be divided
into two phases. The first and major phase of the project was a large
scale evaluation of aeration lagoon treatment of unbleached sulfite pulp
and paper mill effluents and the second phase involved a study of the
effects of varying levels of organic enrichment when added to simulated
streams. The specific program objectives were as follows:
1. Evaluation of the factors affecting aeration lagoon efficiency to
pinpoint those factors influencing treatment efficiency and to
optimize treatment.
2. Optimization of treatment plant operation to achieve maximum
improvement in stream conditions at the lowest possible cost.
3. Develop operating cost data for aeration basin treatment which
will be useful to the industry.
4. Determine the degree of treatment necessary to eliminate slime
growths in the receiving stream.
5. Compare the effectiveness of different size surface aerators as
mixing and aeration devices in aerated stabilization basins.
o
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PROCESS DESCRIPTION AND WASTE
TREATMENT FACILITIES
The pulp mill at Lebanon, Oregon shown in Figure 1 is an ammonia-
base sulfite mill using batch digesters and blow pit pulp washing.
Liquor from the washing operation is separated by temperature sensing
into three fractions, "Strong" liquor, "Weak" liquor and "Dilute" spent
liquor.
From collecting tanks the strong liquor is processed by evaporation
and spray drying to produce commercial lignin sulfonate products.
When product sales are not adequate, the strong liquor is disposed of by
burning in a steam generating furnace. Weak liquor is recycled to the
pulp mill where it is used for cooking liquor dilution and blow pit
padding. The weak spent liquor from the collecting system enters the
•waste treatment process just prior to the effluent collecting sump S-2
shown in Figure 2.
Excess white water from the paper machines, general non-chemical
mill effluent and fresh water are combined in evaporator sump S-l.
Water from here is used in the evaporator system for direct condensa-
tion of the vapors produced by strong liquor concentration. These com-
bined effluents overflow the hotwell and into collecting sump S-2.
Total mill effluent is pumped over side-hill screens and into a
primary treatment pond. Fiber recovered on the screens is returned to
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the paper mill. Suspended solids settle to the bottom of the primary
pond and areperiodically removed for disposal by land fill. Clarified
effluent flows into waste sump WS-1 for pumping to secondary treatment
at an average rate of four million gallons per day.
Chemicals such as ammonia, caustic soda and phosphoric acid are
added for pH regulation and biological nutrition. The effluent is next
distributed to one or both of two stabilization lagoons. Pond No. I
contains six 25-h. p. surface aerators. These are direct drive Welles
units with two-bladed 13-3/4-inch diameter propellers turning at 1, 200
rpm. Two 75-h. p. aerators are installed in Pond No. II. One is a
gear driven Mixco unit with a four-bladed turbine impeller, 116 inches
in diameter operating at 37 rpm. The other is a direct drive Welles
aerator with a three blade propeller, 23-3/4 inches in diameter running
at 900 rpm.
Up to 8-1/2 days retention of the effluent is provided by either
parallel or series operation of the ponds. These are diked basins con-
structed by cut-and-fill excavation, lined with a four-inch layer of sand
and sealed with 14-mil black polyvinyl chloride film. Dimensional
details are presented in Table 1.
Each pond overflows into separate sumps (WS-4 and 5) from where
the effluent can be recycled or discharged into a slough leading to the
South Santiam River.
13
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Figure 1. An Aerial Photograph of Lebanon Division of Crown
Zellerbach Corporation Showing Aeration Basins in Background
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SECONDARY TREATMENT PLANT
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An experimental streams station is included containing six flumes
for simulating the effects of mill discharge into the river. Pumps and
flow metering are provided for two concentration levels of non-treated
and three levels of treated effluent in fresh stream water.
TABLE 1
Width @ Bottom, ft.
Width @ Top. ft.
Length @ Bottorr
Length @ Top, ft.
Overall Depth, ft.
AERATION POND DIMENSIONAL DETAILS
Pond No. I
•riz. /Vert. 3/1
n. ft. 218
ft. 296
>m, ft. 785
ft. 863
ft. 13
dd Depth, ft. 9-9
Surface, sq. ft. 236,000
lillion gal. 17.0
.iner sq. ft. 260,000
Pond No. II
3/1
279
357
625
703
13
9.9
236,000
17.0
260,000
A variety of construction materials are used throughout the treat-
ment plant. Piping to the primary pond and to WS-1 is fabricated from
304 stainless steel. Fiberglass reinforced polyester pipe is used to
distribute and recycle effluent to the secondary lagoons. Both cast iron
16
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and concrete pipe are used to handle treated effluent. The Welles
aerators have 304 stainless steel propellers with 17-4PH stainless steel
shafts and are supported by fiberglass reinforced plastic floats housing
polyurethane foam. The Mixco aerator has a 304 stainless steel shaft
and impeller. The floats on this unit consist of polystyrene foam
shrouded by galvanized steel. The latter is showing substantial signs of
corrosion after almost two years of operation. Stainless steel cable is
used to moor the aerators to anchor posts on the shoreline.
An aerial photograph of the aeration basins is shown in Figure 3
and a simplified flow diagram of the system is presented in Figure 4.
The secondary system was designed to permit either parallel or series
operation. Recycle of treated waste from the outlet of either pond to
the inlet is also possible.
17
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Figure 3. Aerial Photograph of Secondary Treatment Plant at Lebanon Division.
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PAPER MACHINE
EFFLUENT
DILUTE SPENT
LIQUOR
EVAPORATOR
OUTFALL
1
I
O
WELLES ( V75HP
SECONDARY POND
N0.2.
MINK)
O
HP
I W-
-M-B
I
O O
SECONDARY POND
NO. I.
O O
WELLES 26 HP
AERATORS
O O
•oa—i
FtQURE 4-FLOW DIAGRAM OF THE LEBANON MILL TREATMENT PLANT.
19
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METHODS AND PROCEDURES
Sampling
Daily 24-hour composite samples were taken from the influent to
the aeration basins, the effluents from Pond I and Pond II and the com-
bined effluent. The daily 24-hour composites were split and shipped by
mill personnel to the Pacific Northwest Water Laboratory of the FWQA
at Corvallis, Oregon and to the Central Research Division of Crown
Zellerbach Corporation at Camas, Washington. The Pacific Northwest
Water Laboratory conducted the following tests: BOD, total suspended
solids, volatile suspended solids, chemical oxygen demand and total
organic carbon. Since there was an unavoidable delay between collec-
tion of samples and analyses, the following procedure was used by the
FWQA laboratory for sample preservation:
1. BOD - refrigeration at 4° C. for up to 24 hours.
2. Total suspended and volatile suspended solids - refrigeration
at 4° C. up to 24 hours.
3. Chemical oxygen demand (COD) and total organic carbon (TOC) -
acidification with 2 ml/liter of concentrated sulfuric acid plus
refrigeration at 4° C.
Weekly composite samples were taken by the FWQA laboratory for
the following analyses: Kjeldahl-nitrogen, ammonia, nitrate, nitrite,
total phosphorous and ortho-phosphate. These samples were preserved
20
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by the addition of 40 mg of HgCl2/liter and refrigeration at 4° C.
Samples were shipped from the Lebanon mill to the Central Research
Division laboratory at Camas, a distance of 120 miles, by truck. A
shipment period of two days was involved which necessitated preserva-
tion of the samples. The daily 24 hour composite samples shipped were
preserved by adjusting the pH to 2. 0 with concentrated sulfur ic acid.
Prior to conducting the BOD test and turbidity measurement, pH was
readjusted to 7. 0 by the addition of sodium hydroxide.
The following data were recorded at the site by the personnel from
the mill technical department: pH, flow, ammonia and phosphoric
acid addition rates, power consumption and pond temperatures.
Extensive sample preservation studies were conducted which showed
that acidification of samples with concentrated sulfuric acid did not
affect the determinations and protected the samples for more than a
week. However, whenever possible, samples were analyzed as soon as
received in the laboratory.
Analytical Methods
Biochemical oxygen demand was conducted as outlined in Standard
Methods for the Examination of Waste Water and Sewage (10) with the
exception of the seed preparation stage. Seed was prepared by centri-
fuging 400 ml of biologically treated effluent at 10, 000 rpm. The ino-
culum or seed was •washed with cold water and re suspended in 150 ml
21
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of dilution water. Microscopic examinations were made on the effluent
before centrifuging to ensure that active motile bacteria were present.
The bacterial suspension was again examined microscopically to determine
whether the bacteria were concentrated and not adversely affected by the
separation step.
The chemical oxygen demand was determined in accordance with
Standard Methods (10). Total organic carbon was measured using a
Carbon Analyzer. A micro sample was injected into a catalytic combus-
tion tube which was enclosed by an electric furnace thermostatically con-
trolled at 950° C. The water is vaporized and the carbonaceous material
is oxidized to carbon dioxide which is measured by an infrared analyzer.
Total solids (TS) were determined by pipetting a 100 ml sample into
a tared crucible and drying at 110° C. for 24 hours. Total suspended
solids (TSS) were determined by vacuum filtering 500 ml of waste
through a tared 12. 5 cm No. 40 Whatman filter paper. The residue was
dried to constant weight at 105° C. The dried residue was fired at 600°
C. for two hours for the volatile suspended solids determination. This
procedure has been outlined in detail in another publication (11).
The Azide modification of the Winkler method as outlined in Standard
Methods (10) was used to determine dissolved oxygen. A D. O. probe
designed and manufactured by Precision Scientific Company was used to
conduct the D. O. profiles in the ponds.
22
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A Beckman Model N pH meter was used and turbidities were measured
with a standard Jackson candle in accordance with the procedure outlined
in Standard Methods (10).
Kjeldahl-nitrogen was run in accordance with Standard Methods. A
Technicon AutoAnalyzer was used to determine ammonia-nitrogen,
nitrate-nitrogen and nitrite-nitrogen. The ammonia determination was
based upon the formation of an indophenol blue color by reaction of
ammonia with alkaline phenol hypochlorite. Sodium nitroprusside was
used to intensify the blue color. The cadmium reduction of nitrates to
nitrites in the presence of a cadmium-copper catalyst was used to deter-
mine nitrate and nitrite. The nitrites originally present plus the reduced
nitrates were then reacted with sulfanilamide to form the diazo compound
which was then coupled in an acid solution at pH 2. 0 to 2. 5 with N-l
napthylethylenediamine hydrochloride to form an azo dye. The azo dye
intensity which is proportional to the nitrate concentration is then measured.
Separate rather than combined nitrate and nitrite values were readily
obtainable by carrying out the procedure with and without the cadmium-
copper reduction step.
The ammonium molybdate and potassium antimonyl tartrate method
(12, 13) was used to determine total and ortho-phosphate. These compounds
reacted in an acid medium with dilute solutions of phosphorous to form an
antimony-phosphate-molybdate complex. The complex was reduced to an
23
-------
intensely blue-colored complex by ascorbic acid. The color developed
was proportional to the phosphorous concentration.
Because of the tremendous volume of data collected over the 17
month period, the daily analyses were averaged for each run. The
rough data will be filed at the Central Research Division of Crown
Zellerbach for reference. The average values have been prepared in
table form and are presented in the Appendix of this report.
24
-------
OPERATIONAL RESULTS AND DISCUSSION
Nutrient and Chemical Requirements
To approximate nutrient and neutralization requirements, laboratory
shaker flask studies were conducted. Inoculum for this study was
obtained by centrifuging treated effluent from several shake flasks. The
cells were then added to 12 flasks, each containing 100 ml aliquots of
raw spent sulfite liquor. The pH of the raw waste was adjusted to a
range from 4. 0 to 9. 5 in 0. 5 pH unit increments. Each day 20 ml were
removed and replaced with 20 ml of untreated waste. BOD determinations
were conducted after 15 days of continuous operation. The data are
shown in Figure 5. The initial BOD of the untreated waste was 608 ppm.
Optimum pH appears to be in a range of 6. 0 to 7. 5. The BOD reduction
within this range -was close to 90%. Microscopic examination of the
samples showed that the predominant microorganisms at the low pH
levels were yeast. At the higher pH values there were considerable
numbers of long rods. Yeast, however, were present over the entire
pH range studied. On the basis of the laboratory studies it appeared that
the aeration basins could be operated at quite low neutralization chemical
requirements.
Phosphorous requirements were also determined in the laboratory
using the laboratory shaker flasks. In these experiments the raw waste
pH was adjusted to pH 8. 0 with ammonium hydroxide and/or sodium
-------
FIGURE 5r-EFFECT OF pH ON BOD REDUCTION
AFTER FIVE DAY RETENTION.
100
90
80
o
3
70
60
1
1
1
(NITAL BOO -608 PPM.
1
o
567
pH IN REACTION VESSEL.
8
-------
hydroxide. The BOD to phosphorous ratios studied were 160:1, 80:1,
and 40:1. The results of the laboratory trial are shown in Figure 6.
The effects of increasing phosphorous additions were not too dramatic
and very little difference was noted between the "control" which received
no supplemental phosphorous and the maximum phosphorous level.
To evaluate the effect of pH upon treatment efficiency, three large
scale trials were chosen which varied in pH from ,5. 7 to 7. 0. Pond
temperatures during the three trials averaged 24° C. A summary of
the average operating results is presented in Table 2.
The neutralization chemical requirements for the three runs were:
pH 5.7 - 198 Ibs. of ammonia-nitrogen/day
pH 6. 4 - 2, 623 Ibs. of sodium hydroxide/day
pH 7. 0 - 2, 512 Ibs. of ammonia-nitrogen/day
In referring to Table 2 it can be seen there was an increase in
BOD removal as the pH approached neutrality. The difference in
efficiency, however, was small. No difference in operating efficiency
could be attributed to the substitution of sodium hydroxide for ammonia
as a neutralization chemical. Because of the difference in molecular
weight between the tv/o chemicals, cost of neutralization to the same
pH would be substantially higher for sodium hydroxide than for
ammonium hydroxide. All of the runs conducted during the experimental
17 month period except the July 1970 run utilized ammonia for reaction
control.
28
-------
FIGURE 6-EFFECT OF PHOSPHOROUS ON BOD
REDUCTION AFTER 5 DAY RETENTION.
!>
•
4 8 12 16
PHOSPHOROUS ADDED, PPM AS R
-------
TABLE 2
THE EFFECT OFpH ON BOD REDUCTION IN COMBINED TREATMENT
Run No. *
1
2
3
pH in
Pond
5.7
6.4
7.0
Waste
Volume
mgd
4.16
4.17
4.42
Waste
Retention,
Days
8.2
8.2
7.7
Pond
Temp. ,
°C.
24
26
23
BOD,
In
17,445
17,908
17,489
BOD
Lbs. /Day Red.
Out Red. %
4,821 12,624 72.4
4,590 13,318 74.4
3,903 13,586 77.6
SYSTEM
BOD,
Added
2.42
2.49
2.43
Lbs. /hp. hr.
Reduced
1.75
1.85
1.89
*Run 1 - May 6-June 9, 1970
Run 2 - June 27-July 13, 1970
Run 3 - Sept. 1-Sept. 19, 1969
-------
Several large scale field trials at varying phosphorous addition rates
were conducted during the summer of 1969 and the average results are
presented in Table 3. The four tests were conducted under quite simi-
lar conditions of BOD loading and temperature. To ensure equilibrium
between each run, about 14 days were allowed prior to the collection
of samples.
The pounds of BOD removed per day were fairly uniform under all
phosphorous addition rates. It appears that the ponds can be operated
without supplemental phosphorous or at very low phosphorous addition
rates of less than 40 Ibs. /day. The total and soluble phosphorous con-
centrations in the treated effluent were 1. 74 and 0. 53 ppm, respective-
ly, when operating at the low phosphorous addition rates.
The laboratory and field trials have shown that neutralization and
phosphorous requirements are quite low. For example, during the May
6 to June 9, 1970 run, ammonia neutralization requirements were 198
Ibs. /day and satisfactory operation was maintained without phosphorous
supplements.
Series Versus Parallel Operation
Because of the ease of operation and the lower power costs, most of
the trials during the 17 month experimental period were conducted by
operating the ponds in parallel. However, from January 16 to February
18, 1970 the aeration ponds were operated in series. The untreated
31
-------
TABLE 3
THE EFFECT OF PHOSPHOROUS ON BOD REDUCTION (COMBINED TREATMENT SYSTEM)
Phos-
phorous Soluble Phos- %
Added phorous. ppm Temp.. BOD, Lbs. /Day BOD BOD, Lbs./hp. hr.
in No. *
1
2
3
4
Lbs. /Day
100
106
0
0
Influent
__-.-
2.30
0.19
0.46
Effluent
—
1.40
0.21
0.50
8C.
24
25
26
23
In
16
14
14
17
,180
,620
,833
,489
Out
3,385
2,484
1,964
3,903
Red.
12,795
12,140
12,869
13,586
Red.
79.1
84.1
86.8
77.6
Added
2.25
2.03
2.06
2.43
Reduced
1.78
1.69
1.79
1.89
*Run 1 - June IZ-June 26, 1969
Run 2 - July 7-July 21, 1969
Run 3 - Aug. 1-Sept. 1, 1969
Run 4 - Sept. 1-Sept. 19, 1969
-------
waste entered Pond II which contained the two 75-h. p. aerators and was
then pumped by means of the 75-h. p. recirculation pump back to the
inlet of Pond I which contained the six 25-h. p. aerators. To compare
series and parallel operation, the results from a parallel run conducted
from November 20, 1969 to January 16, 1970 were used.
The neutralization, nutrient and power usage for the two runs were
as follows:
Series Parallel
Ammonia addition rate, Ibs. /day 1,810 1,703
Phosphorous addition rate, Ibs. /day 29 33
Power usage, kw-hr. /day 11,030 8,351
There was a considerable increase in daily power usage when
operating the ponds in series because of the use of the recycle pump.
If the ponds had originally been designed for series operation, the flow
would have been by gravity thereby eliminating the need for the pump.
The characteristics of the influent and effluent from the two runs are
shown in Table 4.
Under parallel operation both ponds assumed an equilibrium temper-
ature of 16° C. Although the final waste temperatures were about the
same for parallel and series operation, it was possible to maintain Pond
II at a substantially higher temperature during series operation. The
suspended solids concentration of the final effluent during the series
operation was considerably higher than during parallel operation. This
33
-------
TABLE 4
Operation Waste
Series Influent
Series Pond II
Series Pond I
Parallel Influent
Parallel Pond 11
Parallel Pond I
Parallel Composite
CHARACTERISTICS OF INFLUENT AND EFFLUENT
DURING PARALLEL- AND SERIES
OPERATION, RATED HORSEPOWER - 150/BASIN
Vol.
Waste Susp. Susp. Tot.
Vol. , Temp. , BOD COD Sol. Sol. Sol.
mgd pH °C. PPm PPm ppm ppm ppm
4.49 7.1 29 593 1864 117 92 1580
6.9 19 258 1547 90 72 1679
6.8 15 161 1431 114 96 1639
4.31 7.3 28 604 2211 88 76 2661
2.18 7.2 16 188 1813 77 66 1919
2.13 7.0 16 235 1845 72 66 1939
4.31 6.9 16 207 — — — 1873
JTU
112
276
229
116
299
248
274
-------
may result from the somewhat higher velocity attained under series
operation since the waste volume to each pond is doubled.
A comparison of the operating efficiencies for the two runs is pre-
sented in Table 5.
TABLE 5
COMPARISON OF PERFORMANCE - SERIES VERSUS PARALLEL
OPERATION RATED HORSEPOWER - 150 PER BASIN
Waste BOD BOD
Flow, BOD, Lbs. /Day Red. Lbs. /hp. hr.
Operation Waste mgd In Out Red. % Added Red.
Series Pond II 4.49 22,000 9,667 12,533 56.5 6.17 3.48
Pond I 4.49 9,667 6,033 3,634 37.6 2.69 1.01
Composite 4.49 22,000 6,033 16,167 72.8 3.06 2.25
Parallel Pond II 2.18 10,988 3,420 7,809 71.1 3.05 2.17
Pond I 2.13 10,741 4,129 6,562 61.1 2.98 1.82
Composite 4.31 21,729 7,447 14,282 65.7 3.01 1.98
Under series operation the major portion of the BOD reduction was
accomplished in the first pond (Pond II) which received the untreated
waste. The readily available organic material was rapidly destroyed in
the first of the series operated ponds and the more resistant organic
material was left for the second pond. A total of 16, 167 Ibs. of BOD/day
was destroyed or 72. 8% of the appli ed load. The BOD reduction under
35
-------
parallel operation averaged 14, 282 Ibs. /day or 65%. There was a
definite improvement in efficiency when the two ponds were operated in
series.
A summation of the average performance under series and parallel
operation is presented in Table 6. It can be seen that series operation
TABLE 6
SUMMARY OF PERFORMANCE UNDER SERIES AND
PA RA LLEL OPERA TION
Parallel Series
Volumetric Load, mgd *'31 *'*9
BOD Load, Ibs./day 21,729 22,200
BOD Discharged, Ibs. /day 7,447 6,033
BOD Reduction, Ibs. /day 14,282 16,167
BOD Reduction, % 65-7 72'8
Suspended Solids Discharged, Ibs. /day 4,568 4,272
Suspended Volatile Solids Discharged, Ibs. /day 4,280 3,597
Ammonia-nitrogen Discharged, Ibs. /day 5,684 5,433
Soluble Phosphorous Discharged, Ibs. /day 30 16
resulted in an additional 1,414 Ibs. /day BOD reduction. About 78% of
the total BOD reduction occurred in the first of the series operated ponds
and 22% occurred in the second pond. It appears that the major portion
of the BOD is easily destroyed in about 3. 8 days, the retention in Pond
36
-------
II during the series operation.
The D. O. profiles shown in Figure 7 clearly show that BOD reduc-
tion could probably have been improved by increasing the aeration
capacity of Pond II during the series operation since the D. O. in most
of the pond was zero during the run. The D. O. content in Pond I was
uniformly high during the run.
It is of interest to compare the D. O. profiles under series and paral-
lel operation. Profiles conducted on February 23, 1970, when operating
in parallel, are shown in Figure 8. It will be noted that when the ponds
are equally loaded under parallel operation, the large aeration units
were able to supply substantially greater amounts of D. O. than the small
25-h. p. units.
Effect of BOD Load on BOD Reduction
The average operating data for the individual ponds and the combined
treatment system are presented in Tables I, II and III of the Appendix.
Since aeration capacity appears to be the limiting factor affecting BOD
removal, plots of the BOD reduction/h. p. -hr. versus BOD loading have
been prepared and are shown in Figure 9 for the two ponds. BOD reduc-
tion appears to be a straight line function of BOD load over a rather wide
range of loadings. The BOD reductions in the two ponds over a loading
range from 1. 5 Ibs. to 5. 5 Ibs. /h.p. -hr. are presented in Table 7.
37
-------
FIGURE 7-DISSOLVED OXYGEN PROFILES FOR PONDS IN SERIES OPERATION,
FLOW FROM POND TL TO POND, I, ON FEBRUARY 16, 1970.
A.)
WELLES 75 HP
200 300 400 500 BOO
DISTANCE,IN FEET, FROM INFLUENT TO WEIR.
-------
4.0.
z 2.0
X
o
ui 0
FIGURE 8.-DISSOLVED OXYGEN PROFILES FOR PONDS IN PARALLEL OPERATION
ON FEBRUARY 23, 1970.
I
T
t
T
POND I
300 400 500 600
DISTANCE, IN FEET, FROM INFLUENT TO WEIR.
70O
800
-------
ce
I
s
Q
O
CD
I
POND I
POND n
I
1345
BOO LOAD M LBS/HP-HR .
FIGURE 9. -EFFECT OF BOO LOAD ON BOD REDUCTION.
-------
TABLE 7
BOD REDUCTIONS IN THE TWO AERATION
BOD Load,
Lbs. /h. p. -hr.
1.5
2.0
2.5
3.0
3.5
4.0
BOD Reduction
Lbs. /h. p. -hr.
Pond I
1.25
1.58
1.88
2.20
2.50
2.80
Pond II
1.40
1.75
2.05
2.37
2.67
3.00
BASINS
BOD Reduction, %
Pond I
83.4
79.0
75.3
73.3
71.4
70.0
Pond II
93.3
87.7
82.0
79.0
76.3
75.0
To achieve an 80% BOD reduction, Pond I would have to be loaded
at 1. 9 Ibs. of BOD/h. p. -hr. or 6, 840 Ibs. /day and Pond II could receive
a load of about 2. 8 Ibs. /h. p. -hr. or 10, 000 Ibs. /day. It becomes
apparent that Pond II which is equipped -with the two 75-h. p. surface
aerators is much more efficient than Pond I with the six 25-h.p. units.
An additional three 25-h.p. surface aerators would be needed in Pond I
to bring it up to the efficiency of Pond II. On the basis of the work con-
ducted, the two 75-h. p. units were equivalent to nine of the small 25-h.p.
aerators.
The performance of the combined aeration systems is presented in
Figure 10 and summarized in Table 8.
41
-------
FIGURE 10-RELATIONSHIP BETWEEN BOD LOADING AND REDUCTION
FOR COMBINED SECONDARY SYSTEM (300 HP AERATION CAHVCITY).
3.2
28
i
2.4
9 2.0.
1.6
r
IB
2 X)
22 £4 2J6
BOD LOAD IN LBS/HP-HR.
26
r
3.2
-------
TABLE 8
PERFORMANCE OF COMBINED TREATMENT SYSTEM
BOD Load
Lbs. /h. p. -hr.
2.00
2.30
2.60
2.90
3.10
BOD Load
Lbs. /Day
14,400
16,550
18,700
20,900
22,400
BOD
Reduction
Lbs. /h. p. -hr. Lbs. /Day %
1.68
1.80
1.92
2.05
2.13
12,100
12,970
13,820
14,770
15,320
84.0
78.3
73.9
70.7
68.7
If the overall requirement for primary and secondary treatment is
considered to be 85% and if 5% is allotted to primary treatment, an 80%
reduction must be reached in the combined secondary system. To per-
mit selection of the allowable BOD load, Figure 11 has been prepared
which presents the percent BOD reduction as a function of BOD loading.
To achieve an 80% BOD reduction in the secondary system the BOD load
must be limited to about 15,800 Ibs. /day or 2. 2 Ibs. /h. p. -hr. At a
daily load of 20, 000 Ibs. /day the BOD reduction can be expected to be
72%. An 80% BOD reduction at a load of 20, 000 Ibs. /day could be
achieved by the addition of another 75-h. p. surface aerator which would
bring the total aeration capacity for the two ponds to 375 h. p.
During the 17 month experimental period, the incoming BOD load to
the aeration ponds varied quite widely from day to day. It was noted,
43
-------
90
80
7O
o
£T
12
8 9Q
Q
UJ
oe
o
o
B
8Q
7Q
60
1.4
14 16 18 20
BOD LOAD IN LBS/DAYX 1000.
22
\
1.8
2.2 2.6 3.0
BOD LOAD IN LBS/HP-HR.
3.4
24
3.8
FIGURE 11-EFFECT OF BOD LOADING ON BOD REDUCTION FOR
COMBINED SECONDARY SYSTEM (300 HP AERATION CAPACITY).
-------
however, that these fluctuations had very little effect upon the final
effluent which had a fairly uniform BOD concentration. Very high
shock loadings were readily absorbed without drastically affecting the
final BOD. This can readily be seen by referring to Figure 12 which
shows the daily BOD concentrations into and out of the secondary
system. The effects of shock loadings are minimized because of the
mixing characteristics of the system and the long retention available
for equilization.
Effect of Retention on BOD Reduction
Although various retention periods were studied, it was impossible
to provide a constant BOD load at the various retentions, i. e. , there
were generally two variables. Under these conditions, the low reten-
tions showed better BOD reductions than would have been achieved if
the BOD load had remained the same for all runs. Three runs from
Pond II and one from Pond I were selected and a summation is pre-
sented in Table 9.
In referring to Table 9, it appears that considerable nitrification
may be occurring during the 16. 7 day retention and at the low BOD load
used during this run. This would account for the relatively low BOD
reduction. Unfortunately, nitrate and nitrite determinations were not
available for the run. Weekly checks for nitrite and nitrate during runs
conducted from April 14 through July 10, 1970 at fairly heavy BOD loads
-------
FIGURE 12.-DAILY OPERATING DATA CONCERNING BOD OF INFLUENT AND
EFFLUENTS FROM PONDS I ANDIL.
800
I 1 I I I I I I I I I II |
600
I
a.
Z400
200
EFFLUENTS
20 25
SEPTEMBER 1969.
5 10
OCTOBER 1969.
-------
TABLE 9
THE EFFECT OF RETENTION ON BOD REDUCTION
BOD BOD, Lbs.
Retention BOD, Lbs. /Day Red. h. p. -hr.
Run No. *
1**
2
3
4
Days
16.7
7.2
5.3
3.8
In
5,329
11,364
16,779
22,200
Out
1,200
2,610
6,621
9,667
Red.
4,129
8,754
10,158
12,533
%
77.5
77.0
60.5
56.5
In
1.48
3.16
4.66
6.17
Red.
1.15
2.43
2.82
3.48
*Run 1 - Mar. 23-Apr. 7, 1970
Run 2 - Apr. 7-May 6, 1970
Run 3 - Mar. 23-Apr. 7, 1970
Run 4 - Jan. 16-Feb. 16, 1970
**Run from Pond 1
showed only traces. The average nitrite and nitrate concentrations from
14 weekly samples taken of the influent, effluent from both ponds, and
composite were as follows:
NQ2-N, ppm NO3-N. ppm
Influent 0.18 0.54
Effluent Pond I °-17 °*52
Effluent Pond H 0.19 0.49
Composite Effluent 0.19 0.51
47
-------
No significant differences in nitrite or nitrate were detected between
the influent and effluent. It is of interest to note that the D. O. concen-
tration in the ponds during these runs was close to zero except close to
the aerators which would explain the absence of nitrifying bacteria.
The results from the three trials conducted on Pond II are presented
in Figure 13. Based upon the results obtained, it is doubtful whether
significant improvements in efficiency can be gained by exceeding the
design retention of 7 to 8 days. Additional aeration capacity would be
expected to have more pronounced effects upon efficiency than increases
in waste retention. For example, Pond I was generally devoid of D. O.
which resulted in facultative operation instead of the desired aerobic
operation.
Temperature Effects
During the experimental period, the feed temperature to the sec-
ondary treatment system varied from 28° to 35° C. (82° to 95° F.)
whereas the composite outlet temperature varied from 16° to 26° C.
(61° to 79° F. ). There was a substantial temperature drop at all times
of the year. The summer temperature drop was caused by heavy evapor-
ation rates whereas the winter drop was attributable to low ambient
temperatures and dilution by cold rain water. Typical ambient monthly
average temperatures and evaporation rates for the Lebanon area are
presented in Table 10. The average evaporation rate from May 1
-------
w
I
UJ
cr
o
i
80
70
60
50
40
30
20
10
0
1
/
/
/ 1
1
Q
/
f
7
f
\
X
1
1
/**
1
,-J"~
1
4 6
RETENTION IN DAYS
e
10
FIGURE I3.-EFFECT OF RETENTION ON BOD REDUCTION
UNDER VARIABLE BOD UOAD IN POND TL.
49
-------
through September 30, 1969 was about 6.8 inches per month, whereas
the average ambient temperature was 62. 5°.
TABLE 10
AVERAGE MONTHLY AMBIENT TEMPERATURES
AND EVAPORATION RATES AT CORVALLIS -
ALBANY STATIONS
Month
Jan., 1969
Feb.
March
April
May
June
July
Aug.
Sept.
Oct.
Average
Monthly
Temp. ,
°F.
35.4
40.0
46.6
49.1
58.2
64.4
64.6
63.6
61.6
51.2
Evaporation
Rate
Inches/Mon.
~
—
—
3.25
6.06
6.31
7.62
8.51
5.34
2.16
Month
Nov.
Dec.
Jan., 1970
Feb.
March
April
May
June
July
Average
Monthly
Temp. ,
°F.
46.2
41.9
41.1
45.3
46.3
46.8
55.0
63.8
66.3
Evaporation
Rate
Inches/Mon.
—
—
—
0.92
2.02
3.48
5.44
7.01
9.45
The average temperature data for each run were used to calculate
the heat losses. The results of these calculations are shown in Table
11. The average heat loss from May through September of 1969 was
534, 000, 000 BTU/day when the incoming waste temperature averaged
50
-------
33° C. (91.4° F.)« During the winter period from November through
April, heat losses averaged 793, 000, 000 BTU/day. Heat losses were
found to be greater for series operation than for parallel operation.
TABLE 11
SECONDARY TREATMENT SYSTEM TEMPERATURE DATA AND
CALCULATED HEAT LOSSES
Run No. *
1
2
3
4
5
6
7
8
9
10
**11
Av.
Vol.
mgd
4.22
4.08
4.42
3.75
4.31
4.54
4.53
4.16
4.17
4.21
4.49
Temp. ,
In
33.4
33.7
31.5
32.5
28.0
29.2
30.1
32.0
35.0
34.4
29.0
0 C.
Out
24.9
25.6
23.5
21.0
16.0
17. 3
18.5
24.0
26.0
25.3
15.0
Temp.
•c.
3.5
8.1
8.0
11.5
12.0
11.9
11.6
8.0
9.0
9.1
14.0
Diff.
°F.
15.3
14.6
14.4
20.6
21.6
21.4
20.9
14.4
16.2
16.4
25.2
Heat Loss/
Day
BTU X 106
539
495
531
645
777
811
790
500
563
575
945
*Run 1 - July 7-July 21, 1969 Run 7 - April 12-May 6, 1970
Run 2 - Aug. 1-Sept. 1, 1969 Run 8 - May 6-June 9, 1970
Run 3 - Sept. 1-Sept. 19, 1969 Run 9 - June 17-July 13, 1970
Run 4 - Sept. 19-Oct. 22, 1969 Run 10 - July 25-Sept. 5, 1970
Run 5 - Nov. 20-Jan. 16, 1970 Run 11 - Jan. 16-Feb. 18, 1970
Run 6 - Mar. 1-Mar. 12, 1970
** Series Operation, Pond II to Pond I.
51
-------
The relationship between monthly ambient air temperatures and
average heat losses is shown in Figure 14. At an average ambient
summer temperature of 65° F. , heat losses will average 500, 000, 000
BTU/day and at an average winter temperature of 40° F. heat losses
can be expected to average 815,000,000 BTU/day. These calculations
are based on an average inlet waste temperature of 32° C. (89. 5° F.).
The actual waste temperature drop that can be expected at various
ambient temperatures is also shown in Figure 14. During the winter
season a drop of pond temperatures as great as 11. 7° C. (21° F.) can
be expected and summer operation can be expected to result in a drop
of 8. 3° C. (15° F.).
Since temperature in the ponds could not be controlled, temperature
was in equilibrium with the ambient temperature. Pond temperatures
varied from 16° C. (61° F.) during the winter to 27° C. (80° F. ) in
the summer. Since biological activity increases with increasing
temperature, it would be expected that BOD reductions would be sub-
stantially greater in the summer than the winter. However, a careful
analysis of the data indicated that temperature had no significant effect
upon the secondary system. This can be shown by referring to Figures
9 and 10 which include all of the BOD data regardless of temperature.
The data used to develop these figures covered an 11° C. spread in
temperature, yet no significant effect upon treatment efficiency could
-------
1000
^ 800
fe
5
q eoo
400
35
25
en
30
/WERAGE INLET TEMPERATURE IS 90°F.
40 50 60 70
AMBIENT TEMPERATURE IN °F.
80
FIGURE 14-EFFECT OF AMBIENT TEMPRATURE ON
HEAT LOSSES FROM SECONDARY TREATMENT AND
ON TEMPERATURE REDUCTION IN THE PONDS.
-------
be attributed to temperature effects. If temperature was critical, a
much greater spread in the individual points would be expected and
BOD reduction would not plot as a linear function of BOD load.
In evaluating the data, it appears that other factors have a more
pronounced effect upon BOD removal than temperature for this particu-
lar system. For example, if aeration capacity or nutrient concentra-
tions were limiting factors, increases in temperature would not
necessarily result in an increase in efficiency. Since nutrients have
been found to be adequate, aeration rate may be the limiting factor,
thereby masking the temperature effect. If aeration capacity were suf-
ficient to maintain a 2 ppm D. O. residual in the ponds, a more pro-
nounced temperature effect would undoubtedly have been experienced.
During most of the runs, the D. O. in Pond I, which contained the 25-
h. p. aerators, was close to zero. It has already been shown that addi-
tional aeration capacity in Pond I would improve efficiency. Furthermore,
laboratory shaker flask studies have shown that BOD reductions of 90%
can readily be attained in five days of aeration with dispersed bacterial
growths. However, in the laboratory studies, the rate of oxygen transfer
was not a limiting factor.
Recirculation of Treated Waste
Recirculation of treated waste was studied to determine whether
dilution of the untreated waste with treated waste containing acclimatized
-------
bacteria would have a beneficial effect upon the performance of the
treatment system. The initial plan of operation called for a series of
experiments in which the recirculation rate would be varied over a
range from 1. 4 mgd to 5. 8 mgd.
To evaluate the effectiveness of recirculating treated waste, the
two ponds were operated in parallel with recycle of 2 mgd of treated
waste in Pond II from September 19 through October 22, 1969. A sche-
matic diagram of the flow pattern is shown in Figure 15. During the
trial, 2, 694 Ibs. /day of ammonia and 33 Ibs. /day of phosphorous were
added to the raw waste. Power consumption during the trial averaged
9, 900 kw-hr. /day.
The characteristics of the influent and effluent from the two aeration
basins and the composite for the test period are shown in Table 12.
In general, recirculation resulted in a deterioration of effluent
characteristics. The suspended solids concentration was increased by
recirculation and there was a substantial increase in BOD. The average
BOD data for the run are summarized in Table 13.
Recycle of 2 mgd of treated effluent in Pond II resulted in a decrease
in BOD removal. Pond II has always shown better BOD reductions than
Pond I. For example, at an equivalent BOD load to Pond II, the BOD
reduction without recirculation should have been about 6, 950 Ibs. /day
instead of 6, 274 Ibs. /day. The difference was even more pronounced
55
-------
.EFFLUENT TO RIVER 3.8 MOD
SULFITE^
MILL
WELLES 75 HP
O
poNon
MKC075 HP
2MGD
3.8 MOD
IJ9MGD
O O
POND I
O O
25 HP WELLES
O O
IJ9MGD
FIGURE I5.-SCHEMATIC FLOW DIAGRAM OF SECONDARY SYSTEM DURING
RECIRCULATION EXPERIMENT.
56
-------
TABLE 12
vn
RECIRCULAT1ON OF TREATED WASTE - CHARACTERISTICS OF INFLUENT,
EFFLUENT AND COMPOSITE SAMPLES
Waste
Rated Volume
HP mgd
Influent
Pond I 150 1.88
Pond II 150 1.88
Composite 300 3.75
Susp.
Susp. Vol. Tot.
Recycle Temp. BOD COD Sol. Sol. Sol.
mgd pH °C. ppro PP171 PPm PPm PPm JTU
6.9 32.5 529 1,930 163 — 1,930 168
0 7.2 20.2 114 1,435 57 49 1,623 205
2.00 7.2 21.5 128 1,467 72 44 1,616 220
7.0 21.0 124 1,364 47 37 1,544 213
-------
TABLE 13
RECIRCULATION OF TREATED WASTE - SUMMARY OF BOD DATA
Waste Re- BOD BOD
Flow cycle BOD, Lbs. /Day Red. Lbs. /hp-hr.
mgd mgd In Out Red. % Added Removed
Pond I 1.88 — 8,295 1,788 6,507 78.5 2.30 1.81
Pond II 1.88 2.00 8,277 2,003 6,274 75.8 1.54 1.16
Composite 3.75 - 16,572 3,885 12,687 76.6 1.84 1.41
when the power requirements of the 75-h. p. recirculation pump were
taken into consideration. Normal operation without recirculation should
result in a BOD reduction in Pond II of about 1. 93 Ibs. /hp-hr. whereas
the reduction was reduced to 1. 16 Ibs. /hp -4ir. when recirculating 2 mgd
of treated waste to Pond II.
The negative results of recirculation can probably be attributed to
reduction in the waste-retention. Since Pond II is uniformly mixed,
recycle would not be expected to improve treatment efficiency. However,
it would be expected that recirculation would be more effective in aera-
tion basins with a well defined BOD gradient from inlet to outlet. Table
14 presents a comparison of recycle with a previous run -without recycle.
Because of the negative effects of recirculation, no additional tests were
conducted.
-------
TABLE 14
EFFECT OF RECYCLE ON OPERATING PERFORMANCE OF POND II
Sept. 1 to Sept. 19, 1969 Sept. 19toOct. 22, 1969
No Recycle 2 mgd of Recycle
BOD Added,
Ibs./day 9,224 8,277
BOD Out,
Ibs. /day 2,078 2,003
BOD Red. ,
Ibs. /day 7,146 6,274
BOD Red. ,
Ibs. /hp-hr. 1.98 1.16
BOD Red. , % 77.5 75.8
Surface Aerator Comparison
A great deal of flexibility was designed into the secondary treatment
system to permit comparisons of large surface aerators versus smaller
units and to compare the high speed units with the low speed units employ-
ing gear reducers.
To evaluate the difference between different size aerators, Pond I
was equipped with six 25-h. p. Welles surface aerators and Pond II with
two 75-h. p. units. Selection of optimum size is of utmost importance since
it has a sizable impact upon capital cost. A detailed cost analysis of the
different size units is shown in Table IV of the Appendix. A plot of
59
-------
aerator cost as a function of rated horsepower is shown in Figure 16.
Because of the limited data used, data taken from this figure are only
rough approximations. However, it can readily be seen that the installed
cost of the large 75-h. p. units is substantially lower than for equivalent
capacity of the smaller 25-h. p. units. For example, the installed cost
of the 25-h. p. units was $378/rated horsepower whereas the installed
cost for a 75-h.-p. unit ranged from $285 to $305/rated horsepower.
A reduction of 24% in installed cost can be accomplished by selection of
the larger units. It becomes imperative, then, to determine whether
equivalent horsepower of small and large units are equally effective in
the transfer of oxygen and mixing of the basin contents.
In referring to Figure 16 it can also be seen that the installed cost
of the low speed Mixco units was somewhat higher than for equivalent
horsepower of the direct drive high speed Welles units. A comparison of
performance based upon efficiency of oxygen transfer, mixing and relia-
bility of operation would also be helpful in making a selection between
these two different pieces of equipment.
Comparison of operational data for the 17 month experimental period
presented an exceptional opportunity for a critical performance evaluation.
The average data for each run, shown in Tables I and II of the Appendix,
clearly show that Pond II containing the two large 75-h. p. surface aera-
tors consistently performed better than Pond I with the six 25-h. p.
60
-------
500
a.
400
300
1
Z
200
100
20 40 60 80
RATED HORSEPOWER
FIGURE I6.-AERATOR COSTS VS RATED HORSEPOWER.
61
-------
units. The difference between the two sizes has already been demon-
strated and can be seen by referring to Figure 17. If 80% BOD reduc-
tion in the secondary system is used as a design basis, the two large
aerators were capable of treating 9, 740 Ibs. of BOD/day compared to
6, 660 Ibs. /day for the equivalent horsepower in 25-h. p. aerators (6
units). The relationship between size of aeration equipment and the
allowable BOD load for an 80% BOD reduction is shown in Figure 18.
If the line is drawn as a straight line and extrapolated beyond 75-h. p.
to 100-h. p. units, an allowable BOD load of 3. 14 Ibs. /h. p. -hr. could
possibly be achieved. However, if the relationship follows the curve
shown by the dotted line, the allowable BOD load would be expected
to be somewhat less, i. e. , about 2. 8 Ibs. /h. p. -hr.
The improved efficiency of the larger units may also be related to
the configuration within the ponds or distance between the units. For
example, the distance between aerators in Pond II was about 315 ft.
which provided a radius of 157 ft. for each unit or 2. 1 ft. /h. p. It be-
comes evident in referring to Figure 19 that the space between the small
aerators in Pond I is too great. In the longitudinal dimension the spacing
is more than 260 ft. leaving considerable dead area between the aerators
for sedimentation of settleable solids. It is questionable whether the
small units could do an effective job in either lagoon without additional
aerators. It becomes apparent that selection of the proper size unit and
62
-------
FIGURE 17.- PERFORMANCE COMPARISONS OF LARGE VS SMALL SURFACE AERATORS.
35
30
ui
K
20
L5
1.0
1.5
POND n-
V075HPA
I— SIX 25 HP AERATORS
2.0 2.5 3.0
BOD LOAD IN LBS/HP-HR.
3.5
4.0
4.5
-------
tr 3.4
3.0
or 2.6
§
oo
2.2
g 1-8
CD
O
1.4
10
30 50 70 90
RATED HORSEPOWER OF AERATOR.
FIGURE 18.-RELATIONSHIP BETWEEN SIZE OF
AERATION UNIT AND ALLOWABLE BOD LOAD.
110
-------
i
' i
659 FT
t
619 g
579 §
539
519
j
i
479
459
419
379
k '
N E
*• 347 N
ON O
S 317 '
\
277
237
217
n
157 T
117
77
E
37 g
t 1
|l 176.75 F
r
r
WEIR
26
25 POND II
24
23
22
IB i!9 ,20 ,21
T 1 ' »T 1
17
16
15
. 14
. 13 CENTER
- 12
. 11
. 10
- 9
i is ifi i? i«
1 1 r i r
- 4
- 3
_ 2
. 1
*
TJ- 1-ȣ -1C VP
- 342
5 FT NO. I NO. II '
H
.A
oo
s
1
WALL SLOPE, HORIZ./VERT. 3/1 3/1
WIDTH @ BOTTOM, FT. 218 279
WIDTH (? TOP, FT. 296 357
LENGTH @ BOTTOM, FT. 785 625
LENGTH @ TOP, FT. 863 703 ,
OVERALL DEPTH, FT. 13 13
OPER. LIQ. DEPTH, FT._ 9.9 9.9
71"
70.
69-
68.
WEIR 845 FT
805
POND I 765
725
674- 705
62, 61 1 6.6 ,65 64, 63 _ 685
1 P m r i ' i T •
60-L 665
594- 645
1
58-
57.
55-
54-
53-
605
565
CENTER 56
531
491
451
52J_ 431
47. 4615.1 ,50 49, 4B- ill
''t r • r i i r •
45± 391
44_|_ 371
43-
42_
40,
39-
38-
37-
36i 36.
ii«
30-
29-
28.
27-
331
291
_CENTER 41 27Q
230
190
170
L34 .33 32 3d. i^n
W 1 1 11 —
130
110
70
30
1
E
S
H
^.
^
^
-------
spacing is of the utmost importance in attaining optimum efficiency.
To gain additional insight into the overall performance of the dif-
ferent aerator sizes and configuration, extensive temperature, D. O.
and suspended solids profiles were conducted on July 16, 1969. The
location of the sampling stations are shown in Figure 19. The tempera-
ture gradients from inlet to outlet are shown in Figure 1A of the Appendix.
Although the temperature gradients would have been somewhat steeper
during winter, there appears to be a gradient in Pond I as the waste
passes through. There was a slight increase in temperature in Pond II
from inlet to outlet. The lateral temperature profiles shown in Figure
2A of the Appendix indicate uniform temperature readings across the
short pond dimensions.
The D. O. profiles presented in Figure 3A of the Appendix show a
substantial difference in D. O. between Pond I and Pond II. For all
practical purposes the D. O. in Pond I was zero except in the immediate
vicinity of the surface aerators whereas the large aerators and parti-
cularly the slow speed geared unit (A 2) appeared to have a much greater
zone of influence. This was also evident in the lateral profiles as shown
in Figure 4A (Appendix).
The average suspended solids profiles for the two ponds are shown in
Figure 5A (Appendix). There appeared to be an increase in the suspended
solids of Pond I from inlet to outlet whereas there was a slight decrease in
66
-------
the suspended solids concentration in Pond II.
To gain insight into the mixing characteristics of the different size
aerators, velocity profiles were conducted on the two ponds. The velocity
profiles from inlet to outlet are shown in Figure 6A of the Appendix. The
velocity in Pond II which contained the two 75-h. p. aerators was much
greater than in Pond I. Velocity noted in Pond I was limited to the upper
12 inches of depth and dropped rapidly below that depth. The zone of
influence of the 25-h. p. units was very restricted. The lateral profiles
shown in Figure 7A (Appendix) confirm this observation, i. e,, the overall
mixing capability of the large units is superior to an equivalent horsepower
of smaller units.
Another set of D. O. and BOD profiles was run on the ponds on
September 17 and 18, 1969. The ponds again were operated in parallel
and samples were taken at the same stations shown in Figure 19. The
BOD profiles through the two ponds are shown in Figure 8A. A definite
BOD concentration gradient was noted in Pond I from inlet to outlet.
The BOD dropped rapidly at the inlet from about 500 ppm to 190 ppm and
then gradually decreased in passing through Pond I. The BOD concen-
tration throughout the length of Pond II was uniform indicating complete
mixing of the basin contents. The longitudinal aerator spacing in Pond
II was 155 ft. /aerator or 2. 1 ft. /h.p. If the two aerators in each section
of Pond I are considered as a single entity, the spacing in this pond then
67
-------
becomes 2. 6 ft. /h. p. From the data collected it appears that a spacing
of about 2 ft. /h. p. will ensure complete mixing of the basin contents.
A completely mixed basin is to be preferred since it has the capacity to
absorb fluctuations in waste strength. Complete mixing also minimizes
the potential for odor production.
The D. O. profiles taken on September 17, 1969 are shown in Figure
9A (Appendix). It appears that the Welles aerator in Pond II is actually
maintaining a. higher D. O. level than the Mixco unit. This may, how-
ever, be due to aerator location. For example, the Mixco unit receives
the brunt of the BOD load since it is located near the raw waste inlet.
The D. O. in Pond I was somewhat higher than in the previous run shown
in Figure 3A.
D. O. , BOD and temperature profiles were again conducted on Novem-
ber 3 and 17, 1969. The 75-h.p. Welles surface aerator in Pond II was
out of order which permitted an evaluation of the 75-h.p. Mixco unit.
There was a slight BOD concentration gradient through Pond II whereas
the gradient was considerably steeper in Pond I as shown in the BOD
profiles in Figures 1 OA and 11A of the Appendix. The one 75-h.p.
aerator was more effective in mixing than the six 25-h. p. units in Pond
I. The single 75-h.p. aerator appeared to have an effective D. O. zone
of 240 ft. as shown in the November 17 D. O. and temperature profiles in
Figures 12A and 13A of the Appendix -whereas the remainder of the pond
68
-------
had very little D. O.
From March 1 through March 12, 1970, the 75-h. p. Mixco surface
aerator was shut off and the 75-h. p. Welles unit was moved to the inlet
end of Pond II. The two ponds were operated in parallel during this
short trial to permit an evaluation of the mixing and reaeration potential
of the 75-h, p. Welles unit. The BOD and temperature profiles for the
two ponds are shown in Figures 14A and 1 5A (Appendix). The BOD con-
centrations throughout Pond II were quite uniform indicating complete
mixing with but one 75-h. p. surface aerator whereas there was a
definite BOD concentration gradient from inlet to outlet of Pond I. On
the basis of the data collected, there appears to be little difference in
mixing characteristics and aeration capacity between the high speed,
direct drive aerator and the low speed unit.
A comparison of the two large 75-h. p. surface aerators in Pond II
was made showing the effectiveness of each individual aerator as well
as the two aerators together. The results are presented in Table 15.
The March 1 to March 12, 1970 and May 13 to June 3, 1969 runs
were conducted at similar BOD and volumetric waste loads. A compari-
son of these two runs appears to indicate that the Mixco aerator is a
more efficient aeration device than the Welles. However, the results of
the October 22 to November 19, 1969 run did not show a significant dif-
ference in the pounds of BOD removed. The data collected including the
69
-------
TABLE 15
COMPARISON OF PERFORMANCE OF 75-H.
Run No. *
1
2
3
4
Aerators
Operating
Welles
Mlxco
Mlxco
Both
Waste
Retention Volume,
Days rngd
7.2
10.2
7.5
7.8
2.37
1.67
2.27
2.18
i
pH '
6.5
7.2
7.5
7.2
P. SURFACE AERATORS IN POND II
Temp. , BOD,
"C. In
18.7 9,426
19.0 7,786
23.0 9,520
16.0 10,988
Lbs. /Day
Out
3,794
2,312
2,710
3,420
Red.
5,692
5,474
6,810
7,809
BOD BOD
Red. Lbs. /hp-hr.
% Added
59.7 5.24
70.4 4.33
71.6 5.28
71.1 3.05
Removed
3.13
3.04
3.78
2.17
*Run 1 - March 1 to March 12, 1970
Run 2 - Oct. 22 to Nov. 19, 1969
Run 3 - May 13 to June 3, 1969
Run 4 - Nov. 20 to Jan. 16, 1970
-------
BOD, D. O. and temperature profiles although extensive do not conclu-
sively demonstrate significant differences between the two different
types of aerators. Additional profiles taken during the 17 month experi-
mental period are included in the Appendix (Figures 16A, 17A, 18A, 19A,
20A, 21A and 22A).
In summation, it can be concluded that the large horsepower units
were more efficient aeration and mixing devices than equivalent horse-
power of smaller units, i. e. , one 75-h. p. surface aerator will be more
effective than three 25-h. p. units. The data are inconclusive in regards
to comparing the two large surface aerators (direct drive versus geared
unit).
Solids Production in Secondary System
A certain amount of suspended solids were always present in the
waste pumped to the aeration basins and the concentration of suspended
solids varied quite widely depending upon the condition of the primary
settling lagoon. The average influent and effluent characteristics of
the waste are presented in Tables V and VI of the Appendix.
The average suspended volatile solids concentration of the influent
to the aeration ponds was 62 ppm, whereas the average suspended vola-
tile solids of the treated effluent was 62 ppm. Because of the carry-
over from the primary system, it was difficult to determine the bac-
terial solids buildup per unit of BOD destroyed. Turbidity measurements
71
-------
were actually more indicative of cell buildup than suspended solids.
The average JTU's going to the aeration ponds was 112 whereas the
treated effluent had an average JTU reading of 214. Most of the tur-
bidity in the final effluent could not be removed by settling but required
ultra-filtration or high speed centrifugation. If it is assumed that most
of the suspended solids leaving the aeration basins were biological in
nature, then 0. 16 Ibs. of bacterial cells were discharged per pound of
BOD destroyed. This is considerably lower than what would be expected
from activated sludge which usually averages 0. 4 to 0. 5 Ibs. /lb. of
BOD destroyed when treating similar wastes (14).
Removal of the biological cells would reduce the final BOD some-
what, but it is questionable whether this would have any beneficial
effect upon the receiving stream. For example, Rader (15) found that
simulated streams receiving the treated wastes supported a heavy
population of the protozoan, Vorticella . The growth rate of this organism
increased in proportion to the suspended bacterial load in the treated
•waste added to the simulated streams whereas the untreated waste and
control supported low concentrations of Vorticella. The number of
attached individuals on one side of a microscopic slide (1612 mm2)
after a seven day period is shown in Table 16. It becomes apparent
that the bacterial cells discharged readily serve as food for higher forms
of life in the food chain which could have an overall beneficial effect upon
72
-------
productivity of aquatic life in the receiving stream providing D. O. is
not adversely affected by discharge of the biological suspended solids.
TABLE 16
THE EFFECT OF BACTERIA L SUSPENDED SOLIDS ON THE
GROWTH OF VORTICELLA IN SIMULATED STREAMS (15)
Waste Added
to Stream
Control
Untreated
Treated
Treated
Treated
Nutrient Content
Total Susp.
TOC in Sol. in Stream,
Stream, ppm ppm
__
31 2.5
38 12.7
19 6.4
9.5 3.2
of Waste Discharged
Number of
Vorticella
5
7
51
28
18
Since the pulping base used at Lebanon was ammonia, considerable
ammonia-nitrogen would be expected in the final effluent. The nutrient
characteristics of the influent and treated effluent are presented in
Table VII of the Appendix. The average nutrient concentration into and
out of the secondary system -were as follows:
Total Soluble
Kjeldahl-N Ammonia-N Phosphorous Phosphorous
ppm ppm ppm ppm
Influent
Effluent
156
155
145
139
1.54
1.73
0.96
0.57
73
-------
No significant difference in Kjeldahl-nitrogen could be detected
between the influent and effluent over the 17 month experimental period
whereas a decrease of 6 ppm in ammonia-nitrogen was noted after
treatment. Based upon the 62 ppm of suspended volatile solids leaving
the secondary ponds, the nitrogen content of the suspended solids would
then be about 9. 7% which is quite typical of bacterial cells.
A slight increase in total phosphorous was noted after treatment.
Whether this difference is statistically significant is questionable.
Soluble phosphorous decreased by 41% indicating a significant utiliza-
tion for cell synthesis or precipitation in the aeration basins. Reduction
in the ammonia usage for neutralization would bring down the ammonia-
nitrogen concentration in the final effluent to about 98 ppm and elimination
of phosphorous additions would reduce the concentration of this element
to less than 0. 5 ppm.
Composite Effluent Characteristics
A tabulation of the physical and chemical characteristics of the
final effluent discharged for each of the individual trials is presented in
Table VI of the Appendix. The lowest average BOD concentration per
trial was 58 ppm.
An attempt was made to correlate COD and BOD using the average
concentrations from each run. A plot of COD versus BOD is presented
in Figure 20. Although a line of best fit can be drawn through the points,
74
-------
220
180
I
Q.
1
140
100
60l_
800
1000
1200
1400
1600
1800
CHEMICAL OXYGEN DEMAND IN PPM.
FIGURE 20-RELATIONSHIP BETWEEN COD
AND BOD COMPOSITE EFFLUENT FROM THE
SECONDARY TREATMENT SYSTEMS.
:
-------
using the COD to predict BOD values does not appear to have applica-
tion for accurate prediction of treatment plant efficiency.
Waste Load Discharged to South Santiam River
The average waste load discharged to the South Santiam River dur-
ing each run is presented in Table VIII of the Appendix. The average
waste volume was 4. 2 mgd. The average BOD discharge from June 12,
1969 through October 22, 1969 was 3, 120 Ibs. /day which is probably
the lowest level attainable with the existing treatment system. Ammonia-
nitrogen discharges can probably be reduced to 4, 000 Ibs. /day by
operating at a somewhat lower pH and soluble phosphorous discharge
can be maintained below 20 Ibs. /day without sacrificing operational
efficiency.
Slime Growth from Treated and Untreated Waste
The major compounds in spent sulfite liquor -which serve as a
readily available source of carbon for Sphaerotilus natans are the six
carbon sugars such as glucose and mannose, the five carbon sugar
xylose, and acetic acid. Scheuring and Hohnl (16) demonstrated by
extensive laboratory experimentation that these compounds support
luxuriant growths of Sphaerotilus.
A series of experiments was conducted using the experimental
streams described in a previous section of this report to determine the
amount of slime growth that would be produced by adding various amounts
76
-------
of treated and untreated waste to South Santiam River water. The
amount of slime obtained after 2, 4 and 6 days of continuous operation
is shown in Table IX of the Appendix and the average results are pre-
sented in Table 17. In general, slime growth was closely related to
the amount of BOD added to the simulated streams. However, the
experiments conducted indicated that the treated waste always produced
considerably less slime per unit BOD added than the untreated waste.
For example, if streams 2 and 6 are compared, it can be seen that
although the BOD additions to these two streams were almost identical,
the amount of slime produced was considerably greater in the stream
receiving the untreated waste. After treatment most of the readily
available BOD is destroyed leaving a substantial amount of BOD which
evidently cannot be used by Sphaerotilus or is used at a very slow rate.
This has also been confirmed by Amberg and Cormack (5, 17) who
found that aerobic bacterial treatment of ammonia base spent sulfite
liquor resulted in much lower slime growth than raw waste at equivalent
BOD concentrations. These experiments are also in agreement with
Wuhrman (6) who found that equal concentrations of BOD achieved in a
river by dilution of settled or biologically treated sewage did not pro-
duce comparable associations of microorganisms. Wuhrman concluded
that biological treatment of domestic sewage produced qualitative as
well as quantitative alteration of sewage compounds, which could not be
77
-------
detected by the usual comprehensive criteria such as BOD, organic
nitrogen, organic carbon, etc.
TABLE 17
SLIME GROWTH POTENTIAL OF TREATED AND UNTREATED
WASTE ADDED TO SIMULATED STREAMS
Stream
Number
1
4
3
2
6
5
Waste
Added
None
Treated
Treated
Treated
Untreated
Untreated
BOD in
Stream,
ppm
1.0
2.9
5.8
11.7
13.0
26.1
Slime Growth
Total
Solids
107
106
122
163
295
428
Relative
Growth
1.0
1.0
1.1
1.5
2.8
4.0
in mgm/ft. 2/day
Volatile
Solids
17
23
27
42
117
170
Relative
Growth
1.0
1.4
1.6
1.9
6.9
10.0
In general, the studies conducted at Lebanon showed conclusively
that treatment of the mill waste to a BOD reduction of 80 to 85% pro-
duced a waste which did not readily support slime growth. The effect
of treatment can readily be seen by referring to Figure 21. Two to
three times as much slime was produced from untreated waste than
for equivalent BOD additions of treated waste.
It becomes apparent that biological treatment of the Lebanon waste
serves two very important functions: the first, destruction of oxygen
-------
o
3
2
FIGURE 2I.-SIMULATED STREAM STUDIES AND THE EFFECT OF BOD
UPON SLIME GROWTH FROM SEPTEMBER 26 TO OCTOBER 13,1970.
12
co
1
WASTE
WAffTF
10 15 20
BOD ADDED, IN PPM.
25
30
-------
depleting organic material which could affect the D. O. of the South
Santiam River during the critical low flow period and the second,
reduction or elimination of the waste's ability to support troublesome
filamentous slime growths.
Capital Costs of Secondary Treatment System
A detailed breakdown of capital costs is shown in Table X of the
Appendix and a summary of the major capital items is presented in
Table 18. Total capital cost for the secondary system was $665, 000.
Of the total capital cost, 29. 3% was attributable to labor and 70. 7% to
materials. Capital costs based upon waste volume, BOD and pulp
tonnage capacity were as follows:
Dollar s /Daily A D Ton of Pulp 6,650
Dollars/mg of waste treated/day 166,000
Dollars/lb. of Daily BOD Removed* 55.50
*Based on 12, 000 Ibs. of BOD removed/day.
Because of the small size of the mill, unit capital costs based upon
tonnage are quite high. Furthermore, since the waste being treated
had a BOD of about 500 ppm, capital costs based upon volume were also
high. If the calculations are adjusted to a waste BOD of 200 ppm, the
volume would then become 10. 5 mgd and the unit capital cost would be
$63, 400/mgd of treated waste. Because of the experimental program,
80
-------
the capital costs were somewhat higher than would normally be expected.
For example, the simulated streams, recirculation system, series,
etc. added close to $100, 000 to the cost of the installation.
TABLE 18
CAPITAL COST OF SECONDARY TREATMENT SYSTEM
Cost in Dollars
Item
Aeration Ponds
Aerators
Pumps and Sumps
Nutrient Tanks
Piping
In strum entation
Control Building
Electrical
Miscellaneous
Engineering
TOTALS
Operating Costs
Labor
62,796
2,010
6,579
316
28,377
8,354
5,476
15,952
18,660
46,455
194,975
Materials
67,178
65,225
73,123
6,187
113,542
19,426
12,817
55,375
57,152
• -»
470,025
Labor +
Materials
129,974
67,235
79,702
6,503
141,919
27,780
18,293
71,327
75,812
46,455
665,000
The items which make up the operating costs in the calculations
presented are: electric power, operating labor, repair labor, repair
81
-------
materials, water, chemicals, administrative overhead, fringe bene-
fits, interest on capital and depreciation. Electric power rates
averaged about 5 mils/kw-hr. during the 17 month period. The chemi-
cal costs included a small amount of phosphoric acid nutrient and
ammonia for neutralization. Interest on the $665, 000 capital investment
was calculated at 9% and straight line depreciation was taken over 15
years.
A breakdown of the direct operating costs exclusive of interest,
depreciation and research and development costs is presented in Table
19. The total direct operating costs averaged $5,430 per month. A
summary of the operating costs including interest on the capital and
depreciation is presented in Table 20. Monthly total operating costs
averaged $ 14, 120. The largest items were the fixed costs, interest
on the capital investment and depreciation which accounted for 61. 5%
of the total operating costs. Electric power and chemicals were the
largest cost items of the direct operating costs and they accounted
for 22. 53% of the total operating costs. The ease of operation of the
secondary treatment system is reflected in the low operating labor
cost of 1. 35% of the total or $191 /month.
82
-------
TABLE 19
MONTHLY DIRECT OPERATING COSTS EXCLUSIVE OF INTEREST
DEPRECIATION (DOLLARS)
AND
Ol
Electric
Month Power
April,
1969
May
June
July
u *•*•* y
Aug *
o
Sept.
Oct.
Nov.
Dec.
Jan. ,
1970
Feb.
Mar.
April
May
June
July
Aue.
^o*
Total
Average
% of
Total
1,155
1,092
1,193
1,315
1,198
1,167
1,180
967
1,149
1,583
1,304
1,039
1,107
1,145
1,220
1,310
1,098
20,222
1,190
21.9
Operating Repair
Labor
37
-
19
-
215
292
242
189
266
210
231
231
289
231
231
281
277
3,241
191
3.5
Labor
751
332
1,025
646
824
392
468
774
732
1,044
883
297
229
306
649
648
773
10,773
633
11.7
Repair
Material
557
511
1,984
2,829
718
755
173
172
531
730
492
701
116
220
363
274
769
11,890
699
12.9
A dm.
Water
-
319
353
341
278
284
269
325
256
239
232
246
232
251
264
276
263
4,428
261
4.8
Chemicals (
3,143
3,570
2,214
2,374
2,191
2,417
2,810
1,531
1,916
1,866
1,218
1,487
1,358
563
2,014
1,824
1,395
33,891
1,992
36.7
Dverhead
388
388
388
388
388
388
388
388
388
388
388
388
388
388
388
379
-
6,1»9
365
6.7
Fringe
Benefits Total
85
40
141
84
135
79
102
124
88
156
1.8
6,076
6,253
7,317
7,977
5,947
5,774
5,632
4,470
5,326
6,216
4,887
4,429
3,782
3,169
5,236
5,103
4.701
92,295
5,430
100.0
-------
TABLE 20
SUMMARY OF DIRECT AND INDIRECT OPERATING COSTS -
AVERAGE OF 17 MONTH PERIOD
APRIL 1969 THROUGH AUGUST 1970
Item
Electric Power @ $. 005 kw/hr.
Operating Labor
Repair Labor
Repair Material
Water
Chemicals
Administrative Overhead
Fringe Benefits
Interest on Capital @ 9%
Depreciation, S. L. - 15 years
TOTAL
Dollars /Month
1,190
191
633
699
261
1,992
365
99
4,990
3.700
14,120
% of Total
8.43
1.35
4.48
4.95
1.85
14.10
2.58
0.70
35.00
26.20
99.94
Direct operating costs (exclusive of interest and depreciation)
have been calculated per unit of production, BOD, waste volume bases
as shown in Table 21. The following table summarizes the direct
operating costs and the total operating costs including interest and
depreciation:
-------
TABLE 21
DIRECT OPERATING COSTS EXCLUSIVE OF INTEREST
AND DEPRECIATION APRIL 1969 THROUGH
AUGUST 1970
Month
April,
1969
May
June
July
Aug.
Sept.
Oct.
Nov.
Dec.
Jan. ,
1970
Feb.
Mar.
April
May
June
July
Aug.
Dollars/
Month
6,076
6,253
7,317
7,977
5,947
5,774
5,632
4,470
5,326
6,216
4,887
4,429
3,782
3,169
5,236
5,103
4.701
Dollars
Per Ton
A . D. Pulp
2.02
2.35
2.62
2.65
1.93
2.00
1.85
1.50
1.87
2.07
1.73
1.41
1.27
1.00
1.75
1.79
1.46
Dollars
Per
mg
49.90
44.90
63.10
61.00
47.00
43.60
48.40
41.40
39.90
46.60
38.90
32.70
27.80
25.40
41.80
39.60
36.10
Dollars
Per Lb.
BOD Added
.0092
.0100
.0151
.0176
.0129
.0110
.0110
.0089
.0079
.0092
.0080
.0072
.0058
.0061
.0098
.0092
.0098
Dollars
Per Lb.
BOD Removed
.0136
.0143
.0191
.0212
.0149
.0142
.0143
.0127
.0121
.0141
.0108
.0113
.0084
.0084
.0131
.0123
.0133
5,430
1.84
42.80
.0099
.0134
-------
Dollars/Month
Dollars/Year
Dollars/AD Ton
of Production
Dollar s/mg
Dollar s/lb.
BOD Added
Dollar s/lb.
BOD Removed
Direct Costs
Without Interest
and Depreciation
5,430
65,200
Total Costs
Including
Interest and
Depreciation
14,120
169,500
1.84
42.80
4.79
111.20
.0099
.0134
.0257
.0348
The average unit cost over the 17 month period was $4. 79/ton of
production or about 1 1. 1 cents/1, 000 gallons treated. On a BOD
basis, the operating costs averaged 2. 57 cents/lb. of BOD added and
3.48 cents/lb. of BOD destroyed. Although some minor economies
could be realized in the operation of the facilities such as reduction
in chemicals, it is doubtful whether the total operating costs would
be significantly affected. It becomes evident that secondary treatment
is quite costly and certainly adds a substantial amount to production
costs.
86
-------
A CKNQWLEDGEMENTS
This project -was conducted at the Lebanon Division of Crown
Zellerbach Corporation. Those involved at the mill in ensuring
the success of the development program were:
Mr. R. G. Kott, Manager
Mr. A. M. Neelley, Manager
Mr. E. C. Mays, Manager
Mr. K. F. Byington, Technical Director
Mr. A. C. Moncini, Plant Engineer
Mr. H. P. Burrelle, Office Manager
The treatment plant facilities -were designed by Mr. J. J. Ehli
of the Crown Zellerbach Central Engineering Division, Seattle,
Washington and Mr. Kenneth R. Blaney served as Acting Deputy
Project Director during the engineering and construction phases of
the project.
The technical aspects of the program such as testing and evalu-
ation of data were undertaken at the Crown Zellerbach Central
Research Division by the following personnel:
Dr. H. R. Amberg, Manager, Environmental Research
Dept. (Project Director)
Dr. T. R. Aspitarte, Supervisor, Microbiological
Research
Mr. S. H. Watkins, Research Microbiologist
87
-------
Mr. J. G. Coma, Supervisor, Process Engineering
Mr. O. Hamblen, Technician
Mr. R. Bafus, Technician
The support of the project by the Federal Water Quality
Administration and the help provided by Messrs. A. Cywin and G.
R. Webster is gratefully acknowledged and appreciated. We were
particularly pleased with the help and guidance provided by Mr.
R. H. Scott, the Project Officer and Dr. H. K. Willard of the
Pacific Northwest Water Laboratory. A substantial portion of the
analytical work was conducted by the staff of the Pacific Northwest
Water Laboratory and we wish to acknowledge the following who were
active in the analytical program: Mrs. F. Cole, Mrs. M.
Carpenter, Mr. J. O'Donnell, Mr. C. Greenup and Mr. F.
Roberts.
Advice and help was received from the staff of the National
Council for Air and Stream Improvement and we would like to express
our thanks to Messrs. R. O. Blosser, A. L. Caron and E. L. Owens.
The suggestions and advice provided by Dr. E. J. Ordal,
Professor Microbiology at the University of Washington were very
helpful in the planning and execution of the experimental program.
The cooperation received from the Oregon State Department of
Environmental Quality is gratefully acknowledged. Messrs. W. C.
89
-------
Westgarth, A. Hose and G. Carter of the Department served as
advisors to the project.
90
-------
REFERENCES
1. Palmrose, G. V. and J. H. Hull, "Pilot Plant Recovery of Heat
and Sulphur from Spent Ammonia-Base Sulphite Pulping Liquor. "
TAPPI24:241 (1951).
2. Amberg, H. R. , "By-Product Recovery Methods of Handling
Spent Sulphite Liquor. " Jour, of Water Poll. Control Fed.
_2:278 (1965).
3. Cawley, W. A. , "An Effect of Biological Imbalance in Streams. "
Sew. andlndust. Wastes ^(9):! 124-1182 (1958).
4. Lincoln, J. H. and R. F. Foster, "Investigation of Pollution in
the Lower Columbia River." Wash. State Pollution Control
Comm. and Oregon State Sanitary Authority (1943).
5. Amberg, H. R. and J. F. Cormack, "Factors Affecting Slime
Growth in the Lower Columbia River and Evaluation of Some
Possible Control Measures. " Pulp and Paper Magazine of
Canada, Tech. Sect. (Feb. I960).
6. Wuhrmann, K. , "High Rate Activated Sludge Treatment and Its
Relation to Stream Sanitation. II. Biological River Tests on
Plant Effluent. " Sew. andlndust. Wastes, 26:212(1954).
7. Amberg, H. R. , "The Status of Water Pollution Control in the
Pulp and Paper Industry. " Paper presented at National
Pollution Control Conference and Exposition, San Francisco,
91
-------
April 2, 1970.
8. Rudolfs, W. and H. R. Amberg, "White Water Treatment. "
Sewage and Indust. Wastes Journal ^5:191 (1953).
9. Gellman, I. , "Aerated Stabilization Basin Treatment of Mill
Effluents." TAPPI 48 :(June 1965).
10. Ana. Pub. Health A s soc. , Am. Water Works A ssoc. , Water
Poll. Control Fed. , "Standard Methods for the Examination of
Water and Waste Water, " 12th Ed. , Am. Pub. Health A ssoc. ,
Inc., 1740 Broadway, N. Y. (1965).
11. Oregon State Sanitary Authority, "Tentative Procedures for
Analysis of Pulp and Paper Mill Effluents. " April 1968.
12. Murphy, J. and J. Rile, "A Modified Single Solution Method
for the Determination of Phosphate in Natural Waters."
Analytical Chim. A eta, 21_, 31 (1962).
13. Galew, M. , E. Julian, and R. Kroner, "Method for Quantitative
Determination of Total Phosphorous in Water." Jour. AWWA
j>8_:10, 1363 (1966).
14. Amberg, H. R. and J. F. Cormack, "Aerobic Fermentation
Studies of Spent Sulphite Liquor," Sew. and Indust. Wastes 29
(5):570-576 (1957).
15. Rader, L. , "Vorticella Growth in Experimental Streams,"
liipublished data (April 23, 1970).
93
-------
16. Scheuring, L. and Hohnl, G. , "Sphaerotilus natans, Seine
Okologie und Physiologie, " Schriften Des Vereins der Zellstoff
und Papier - Chemiker und Ingenieure Vol. 26 (1956).
17. Cormack, J. F. and Amberg, H. R. , "The Effect of Biological
Treatment of Sulphite Waste Liquor on the Growth of
Sphaerotilus natans. " Proc. 14th Indust. Waste Conf. , Purdue
Univ., Lafayette, Ind. (May 1959) .
-------
APPENDIX
95
-------
APPENDIX
Tables Page No.
I. Average Performance Data for Pond I 95
II. Average Performance Data, for Pond II 96
III. Average Performance Data for Combined 97
Secondary System
IV. Calculation of Aerator Delivered and Installed 98
Costs
V. Average Analyses of Untreated Feed to 101
Secondary Systems
VI. Average Analyses of Treated Effluent from 102
Combined Treatment System
VII. Average Nitrogen and Phosphorous Content of 103
Untreated and Treated Waste
VIII. Average Load Discharged to South Santiam River 104
IX. Slime Growth in Simulated Streams 105
X. Capital Cost Details 106
Figures
1A Longitudinal Temperature Profiles for Ponds, 109
July 16, 1969
2A Lateral Temperature Profiles for Pond, July 110
16, 1969
3A Longitudinal DO Profiles for Pond, July 16, 1969 111
4A Lateral DO Profiles for Pond, July 16, 1969 H2
5A Longitudinal Suspended Solids Profiles for Pond, 113
July 16, 1969
97
-------
APPENDIX CONTD.
Page No.
6A Longitudinal Velocity Profiles for Pond, 114
July 16, 1969.
7A Lateral Velocity Profiles for Ponds, July 16, 115
1969.
8A BOD Profiles for Ponds, Sept. 17, 18, 1969. 116
9A DO Profiles for Ponds, Sept. 17, 1969. 117
10A BOD Profiles for Ponds, Nov. 3, 1969. 118
11A BOD Profiles for Ponds on Nov. 17, 1969. 119
12A DO and Temperature Profiles in Pond II on 120
Nov. 3, 1969.
13A DO and Temperature Profile for Pond on Nov. 121
17, 1969.
14A BOD Profiles for Ponds on March 5, 1970. 122
ISA Temperature Profiles for Pond on March 5, 123
1970.
16A BOD Profiles for Ponds on February 16, 1970. 124
17A Temperature Profiles for Ponds on February 125
16, 1970.
18A Velocity Profiles for Ponds on February 16, 126
1970.
19A DO Profiles for Ponds on February 16, 1970. 127
20A DO Profiles for Ponds on February 23, 1970. 128
21A Temperature Profiles for Ponds on February 23, 129
1970.
-------
APPENDIX CONTD.
Page No.
22A BOD Profiles for Ponds on February 23, 1970. 130
99
-------
TABLE I
May 3-May 10
May 13-June 3
June 12-June 26
July 7-July 21
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
Nov. 20-Jan. 16, 1970
Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 7
April 17-May 6
May 6-June 9
June 27-July 13
July 25-Sept. 5
Date of Run
April 17-April 29, 1969 8.3
7.6
7.5
8.4
8.2
8.3
8.1
9.0
8.8
8.0
3.8
7.8
16.7
7.8
8.2
8.2
8.8
Temp.
19
22
23
24
25
25
23
20
19
16
15
17
17
18
23
26
25
)R POND I (SIX 25 HP. SURFACE AEKAT<
Vol.
mgd
2.05
2.23
2.27
2.03
2.08
2.05
2.09
1.88
1.94
2.13
4.49
2.17
1.02
2.18
2.08
2,08
1.93
HP.
150
150
100
150
150
150
150
150
150
150
150
150
150
150
150
150
150
BOD,
In
12,200
10,680
9,400
8,480
7,194
7,449
8,265
8,295
9,026
10,741
9,667
8,626
5,329
10,514
8,710
8,956
7,081
Lbs. /Day %
Out
3,020
3,450
2,730
2,100
1,383
1,139
1,897
1,788
2,729
4,129
6,033
3,309
1,200
3,904
2,909
2,661
1,920
Red.
9,180
7,230
6,670
6,380
5,811
6,310
6,368
6,507
6,297
6,562
3,634
5,317
4,129
6,610
5,801
6,295
5,161
BOD
75.3
67.8
71.0
75.3
80.8
84.7
77.1
78.5
69.8
61.1
37.6
61.6
77.5
62.9
66.6
70.3
72.9
BOD
Lbs. /Hp.Hr.
Added Red.
3.39
2.97
3.92
2.36
.00
.07
.30
.30
2,
2.
2.
2,
2.51
98
76
40
48
92
2.42
2.49
1.97
2.
2.
2,
1,
1,
1,
55
01
78
78
61
75
1.77
1.81
1.74
82
01
48
15
84
61
75
1.43
-------
TA BLE U
Nov. 20-Jan. 16,
Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 17
April 7-May 6
May 6-June 9
June 17-July 13
July 25-Sept. 5
1970
Date of Run
April 17-April 29, 1969 8.3
May 3-May 10
May 12-June 3
May Av.
June 12-June 27
July 7-July 21
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
7.6
7.5
7.6
9.2
8.0
8.4
7.3
9.1
10.0
7.8
3.8
7.2
5.3
7.2
8.2
8.2
7.5
Temp.
19
22
23
22
25
26
26
24
22
19
16
19
19
21
19
25
27
26
'OR POND II
Vol.
mgd
2.05
2.23
2.27
2.25
1.84
2.14
2.03
2.33
1.88
1.67
2.18
4.49
2.37
3.21
2.35
2.08
2.08
2.28
Hp.
75
150
75
99
150
150
150
150
150
75
150
150
75
150
150
150
150
150
(TWO 7 5 HP. SURFACE A EB
BOD,
In
11,150
10,680
9,520
—
7,690
7,430
7,384
9,224
8,277
7,786
10,988
22,200
9,426
16,779
11.364
8,735
8,952
8,345
Lbs. /Day
Out
4,150
3,070
2,710
--
1,335
1,115
826
2,078
2,003
2,312
3,420
9,667
3,794
6,621
2,610
1,962
1,929
2,090
Red.
7,000
7,610
6,810
--
6,355
6,315
6,558
7,146
6,274
5,474
7,809
12,533
5,632
10,158
8,754
6,773
7,023
6,255
BOD
Red.
62.8
71.3
71.6
--
82.7
85.0
88.8
77.5
75.8
70.4
71.1
56.5
59.7
60.5
77.0
77.5
78.5
75.0
BOD
Lbs. /Hp.Hr.
Added Red.
6.78
2.96
5.28
3.93
2.14
2.06
2.05
2.56
2.30
4.32
3,05
6.17
5.
4.
3,
24
66
16
2.43
2.49
2.32
4.58
2.11
,78
,75
.77
.75
.82
.98
.74
3.
2.
1.
1.
1.
1,
1.
3.04
2.17
3.48
3.13
2.82
2.43
88
95
1.74
-------
TA BLE III
AVERAGE PERFORMANCE DATA FOR COMBINED SECONDARY SYSTEM
(AERATION CAPACITY 300 HP.)
Date of Run
April 17-April 29, 1969
May 3 -May 10
May 12- June 3
June 12-June 26
July 7 -July 21
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
Nov. 20-Jan. 16, 1970
Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 7
April 7 -May 6
May 6 -June 9
June 27 -July 13
July 25-Sept. 5
Vol.
mgd
4.10
4.46
4.54
3.87
4.22
4.08
4.42
3.75
3.61
4.31
4.49
4.54
4.23
4.53
4.16
4.17
4.21
Temp.
°C.
19
22
23
24
25
26
23
21
19
16
17
17
19
18
24
26
25
Hp.
225
300
175
300
300
300
300
300
225
300
300
225
300
300
300
300
300
BOD,
In
23,350
21,360
18,920
16,180
14,620
14,833
17,489
16,572
16,812
21,729
22,000
18,052
21,754
21,878
17,445
17,908
15,426
Lbs. /Day %
Out
5,910
6,520
5,440
3,385
2,484
1,964
3,903
3,885
5,041
7,447
6,033
6,926
7,558
6,764
4,821
4,590
4,010
Red.
17,440
14,840
13,480
12,795
12,140
12,869
13,586
12,687
11,771
14,282
16,167
11,136
14,196
15,114
12,624
13,318
11,416
Red.
74.8
69.7
71.3
79.1
84.1
86.8
77.6
76.6
70.0
65.7
72.8
61.7
65.3
69.1
72.4
74.4
74.0
BOD
Lbs. /Hp. Hr.
Added
4.33
2.96
4.51
2.25
2,03
2.06
2.43
2.30
3.11
3.01
3.08
3.34
3.02
3.01
2.42
2.49
2.14
Red.
3.23
2.06
3.21
1.78
1.69
1.79
1.89
1.76
2.18
1.98
2.25
2.06
1.97
2.10
1.75
1.85
1.59
-------
TABLE IV
CALCULATION OF AERATOR DELIVERED COST
AND INSTALLED COST
POND I - Six 25 hp. Welles Aerators
A. Delivered Cost Basis:
Motors $ 3,776
Aerators 27.481
Delivered Cost $31,257
Delivered Cost/hp. - $31,257/150 = $208
B. Installed Cost Basis:
Aerators & Motors $31,257
Mooring Cables 2,729
Installation Mtls. 102
Installation Labor 1,097
Electrical Gear & 21.480
Hookup
Installed Cost $56,665
Installed Cost/hp. = $56,665/150 = $378
POND II - One 75 hp. Mixco and One 75hp. Welles
A. Mixco Aerator (75 hp.)
1. Delivered Cost Basis:
Motor $ 838
Aerator -1L891
103
-------
TABLE IV (CONTINUED)
CALCULATION OF AERATOR DELIVERED COST
AND INSTALLED COST
Delivered Cost
Delivered Cost/hp.
2. Installed Cost Basis:
Aerator and Motor
Mooring Cables
Installation Matls.
Installation Labor
Electrical Gear &
Hookup
Installed Cost
Installed Cost/hp.
B. Welles Aerator (75 hp.)
1. Delivered Cost Basis:
Motor
Aerator
Delivered Cost
Delivered Cost/hp.
2. Installed Cost Basis:
Aerator and Motor
Mooring Cables
$14,729
$14,729/75 - $196
$14,729
557
800
377
6.445
$22,908
$22,908/75 - $305
$ 2,298
11.075
$13,373
$13,373/75
$13,373
557
$178
104
-------
TABLE IV (CONTINUED)
CALCULATION OF AERATOR DELIVERED COST
AND INSTALLED COST
Installations Matls. 800
Installation Labor 377
Electrical Gear & 6.445
Hookup
Installed Cost $21,552
Installed Cost/hp. = $21,552/75 - $287
105
-------
TABLE V
Date of Run
June 12-June 26-1969
July 7-July 21
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
Nov. 20-Jan. 16,
Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 7
April 17-May 6
May 6-June 9
June 27-July 18
July 25-Sept. 5
1970
Vol.
mgd
3.87
4.22
4.08
4.42
3.75
3.60
4.31
4.49
4.54
4.23
4.53
4.16
4.17
4.21
7.5
6.2
7.5
7.3
6.9
6.9
7.3
7.1
6.6
6.7
6.5
5.7
6.1
6.6
ID WASTE FEED TO SECONDARY TREATMENT SYSTEM
Temp.
°C.
29.4
33.4
33.7
31.5
32.5
30.0
28.0
29.0
29.2
30.4
30.1
32.0
35.0
34.4
BOD,
PPm
501
415
438
475
529
559
604
593
477
626
579
503
515
439
Susp.
Sol.,
ppm
102
36
51
78
163
87
88
117
98
164
110
29
20
32
Susp.
Vol.
Sol. ,
ppm
94
30
43
40
-
32
76
92
87
145
101
24
17
27
Total
Sol.,
ppm
1,802
1,452
1,585
1,845
1,930
2,006
2,661
1,580
1,944
1,878
1,416
1,405
1,596
1,211
JTU
N»
-
-
119
168
146
116
112
95
114
87
81
91
108
COD
PP*"
228
215
145
1,433
1,930
2,168
2,211
1,864
1,690
1,809
2,580
1,793
1,614
1,412
-------
TABLE VI
Date of Run
May 13-June 3, 1969
June 12-June 26
July 7-July 21
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
Nov. 20-Jan. 16,
Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 7
April 17-May 6
May 6-June 9
June 27-July 13
July 25-Sept. 5
1970
. OF TREATED EFFLUENT I
Vol.
mgd
4.54
3.87
4.22
4.08
4.42
3.75
3.60
4.31
4.49
4.54
4.23
4.53
4.16
4.17
4.21
PH
7.1
7.2
7.0
7.1
7.0
7.0
6.9
6.9
6.8
6.6
6.9
6.5
5.7
6.4
6.7
Temp.
22.0
24.3
24.9
25.6
23.5
2i;o
19.0
16.0
15.0
17.3
19.5
18.5
24.0
26.0
25.3
BOD,
ppm
140
105
70
58
106
124
169
207
161
183
214
179
139
135
114
Susp.
Sol. ,
92
48
54
77
73
47
60
114
51
79
69
111
72
71
Susp.
Vol.
Sol. ,
48
73
60
70
37
25
96
49
68
75
107
42
55
Total
Sol. ,
ppm JTU
1,660
1,433
1,329
1,305
1,544
1,902
1,873
1,639
1,650
1,587
1,815
1,463
1,443
1,175
216
301
220
177
181
213
208
274
229
217
170
175
202
244
183
COD
PPm
1,176
1,364
1,431
1,698
1,569
1,450
1,415
1,448
1,093
-------
TA BLE VII
Date of Run
July 7-July 21, 1969
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
g Nov. 20-Jan. 16,
» Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 17
April 17-May 6
May 6-June 9
June 27-July 13
July 25-Sept. 5
Average
1970
SID PHOSPHOROUS CONTENT OF UNTREATED AND TREATED WASTE
Phos-
phorous,
Influent Waste, ppm
Kjeldahl-N
136
173
141
183
204
193
166
165
158
147
116
107
136
156
Ammonia-N
128
159
138
180
189
181
153
155
146
134
111
96
113
145
ppm
Total
2.60
0.45
0.75
1.57
2.00
2.40
1.57
0.98
1.46
1.58
1.53
1.62
1.51
1.54
Sol.
2.30
0.19
0.46
0.87
0.99
1.20
0.71
0.59
0.88
0.94
1.16
1.16
1.06
0.96
Treated
Kjeldahl-N
159
160
150
173
200
178
163
158
161
147
122
118
127
155
Effluent, ppm
NH3-N
142
153
136
165
177
158
147
136
143
131
113
98
109
139
Tot.
P
2.60
0.92
1.11
1.55
1.96
2.32
1.85
1.05
1.91
1.93
1.72
1.88
1.73
1.73
Sol.
P
1.40
0.21
0.50
0.41
0.82
0.82
0.36
0.29
0.34
0.43
0.45
0.64
0.76
0.57
-------
TABLE VIII
AVERAGE LOAD DISCHARGED TO SOUTH SANTIAM RIVER JUNE 1969 THROUGH JULY 1970
Vol.
Susp. Susp. Sol.
Vol. BOD Sol., Sol. , Ammonia-N Phosphorous
mgd Lbs. /Day^ Lbs. /Day Lbs. /Day Lbs. /Day Lbs. /Day
H
0
vO
J—/(_LV%-' \S * J.XV***
June IZ-June 21, 1969
July 7 -July 21
Aug. 1-Sept. 1
Sept. 1-Sept. 19
Sept. 19-Oct. 22
Oct. 22-Nov. 19
Nov. 20- Jan. 16, 1970
Jan. 16-Feb. 18
Mar. 1-Mar. 12
Mar. 23-April 7
April 7 -May 6
May 6 -June 9
June 17 -July 13
July 25-Sept. 5
o
3.87
4.22
4.08
4.42
3.75
3,60
4.31
4.49
4.54
4.23
4.53
4.17
4.17
4.21
3,385
2,484
1,964
3,903
3,885
5,041
7,447
6,033
6,926
7,557
6,764
4,821
4,580
3,783
1,550
1,900
2,620
3,320
1,472
3,638
4,568
4,272
1,932
2,789
2,608
3,850
2,504
2,494
_
2,040
2,560
1,159
3,175
4,280
3,597
1,856
2,400
2,835
3,711
1,460
1,933
.
5,000
5,210
5,010
5,168
5,323
5,684
5,433
5,152
5,047
4,952
3,919
3,408
3,829
-
49.3
7.1
18.5
12.8
24.7
29.5
16.1
11.0
« A f\
12.0
16.3
15.6
22.3
26.0
-------
TABLE IX
SLIME GROWTH IN SIMULATED STREAMS - SEPT. 26 - OCT. 13, 1970
Growth in Grama/Sq. Ft./Day
Channel
Age of Slime on Boards
2 Days
1
2
3
4
5
6
9/29
.166
.260
.175
.150
.670
.586
10/6
.155
.271
.146
.125
.382
.295
10/13
.119
.128
.126
.104
.359
.312
Av.
.147
.220
.149
.126
.470
.398
9/22
.113
.101
,077
.112
.604
.261
4 Days
10/1
.100
.290
.134
.141
.472
.306
9/22
.117
.087
.096
.107
.384
.226
Av.
.110
.159
.102
.120
.487
.251
9/24
.068
.057
.041
.029
.252
.146
6 Dave
10/3
.061
.128
.148
.076
.285
.310
10/10
.059
.145
.122
.115
.442
.255
Av.
.063
.110
.104
.073
.321
.237
Grand
Av.
.107
.163
.122
.106
.428
.295
Channel
1
2
3
4
5
6
2 Days
9/29 10/6 10/13
Grams of Volatile Solids/Sg. Ft./Day
Age of Slime on Boards
4 Days
6 Day s
9/22 10/1 9/22 Av. 9/24 10/3 10/10 Ay.
.0267 .0298 .0190 ,0195 .0235 .0178
.0874 .0794 .0390 .0439 .0292 .0966
.0481 .0333 .0268 .0254 .0181 .0379
.0347 ,0270 .0207 .0205 .0222 .0373
.4730 .1681 .1572 .1427 .2126 .2544
.3891 .1230 .1185 .1143 .0796 .1658
.0138 .0185 .0109
.0204 .0455 .0140
.0192 .0244 .0112
.0138 ,0233 .0059
.1590 .2118 .0761
.0667 .0956 .0721
.0126 .0131 .0124
.0544 .0537 .0381
.0492 .0373 .0320
.0230 .0559 .0241
.1907 .2099 .1571
.2021 .1604 .1403
Grand
Av.
.0168
.0425
.0273
.0226
.1705
.1167
-------
TA BLE X
CAPITAL COST DETAILS
$
$ $ Labor f
Item Labor Materials Materials
1. Aeration Ponds
Land Clearing 10,949 - 10,949
Earth Moving 32,950 - 32,950
Pump Rental - i.564 1»564
Sand Liner (520,000 sq. ft.) 7,436 11,999 19,435
Plastic Liner (520,000 sq. ft.) 4,304 34,990 39,294
Overflow Weirs 7.157 18,625 25,782
62,796 67,178 129,974
2. Aerators, Pond No. 1
6 - 25 h. p. Aerators & Motors - 31,257 31,257
2 729 2 729
Mooring Cables " <•»' ' »
1 097 102 1.199
Installation 1tuyy — —»
1,097 34,088 35,185
3. Aerators, Pond No. 2
1 -75h.p. Mixco Aerator & Motor - 16,110 16,110
1 - 75 h. p. Welles '« " " ' 13>671 13>6H
1,114 1,114
Mooring Cables
, . 913 242 1.155
Installation —
913 31,137 32,050
111
-------
TABLE X (CONTINUED)
CAPITAL, COST DETAILS
Item
$
$ $ Labor +
Labor Materials Materials
4. Pumps & Sumps
Pumps & Motors
Installation
5. Nutrient Tanks
6. Piping
7. In strum entation
8. Control Building &
Tank Slab
9. Electrical System
10. Experimental Streams
11. Miscellaneous
Boats
Samplers
Roads
Footbridge
Fencing
Ejector
35,260
6,579 37.863
6,579 73,123
35,260
44,442
79,702
316 6,187 6,503
28,377 113,542 141,919
8,354 19,426 27,780
5,476 12,817 18,293
15,952 55,375 71,327
12,873 28,155 41,028
360 360
240 1,462 1,702
490 5,384 5,874
1,146 3,281 4,427
2,843 5,000 7,843
1,068 897 1,965
112
-------
TABLE X (CONTINUED)
CAPITAL COST DETAILS
$
$ $ Labor +
Item Labor Materials Materials
Spare Parts - 12,613 12,613
5,787 28,997 34,784
. . 46,455
Totals 194,975 470,025 665,000
113
-------
FIGURE IA.-TEMPERATURE PROFILES FOR PONDS ON JULY 16, 1969,
i
27.4
27.0
26.6
26.2
25.8
o 25.4
27.4
QC
Ul
27.0. ^
uu
26.6
26.2
2S.8
25.4
25.0
MIXCO
INFLUENT TEMPERATURE 35eC.
800
DISTANCE, IN FEET, FROM INFLUENT TO WEIR.
-------
28_U
2'
2a_
2a-
27..
Ul
a:
cc
UJ
Q.
UJ
2a_
27. _
26-
2Z_
2a-
27-_
26
1
POND n
1
WELLES 75 HP
MIXCO 75 HP
A
POND I
I FT.
5 FT.
9C"T _.
r I.
8
^0~ 60
120
20 40 60 8"0
THE DISTANCE FROM SHORE TO THE AERATORS.
FIGURE 2A.-TEMPERATURE PROFILES ON JULY 16, 1969,
iJo~
115
-------
FIGURE 3A-DISSOLVED OXYGEN PROFILES FOR PONDS ON JULY 16, 1969.
T
100
200 300 400 500 600
DISTANCEJN FEET, FROM INFLUENT TO WEIR.
700
800
-------
Q
-?
SSOLVED OXYGEN II
0
0.8.
0.4
Q
0.8
0.4
:
0.8
0.4
0
0.8
0.4
D
0.8
0.4
1 1 1
poNon
WELLES 75 HP
.„ A|
'v MIXOO 7fi HP
^ ^s *
\
POND: , FT
5CT
t T
: T
- '
*i8 ^."''"\
^••^ ^
^ x
'• ' , -; : : 1 = — 1»*
L i 1 1 i ' ' ^
1 _
2 _
r
—
— _
—
1 .4 /\
20 40 60 80 ivu i^w i-»u
THE DISTANCE, IN FEET, FROM SHORE TO THE AERATORS.
FIGURE 4A.-DISSOLVED OXYGEN PROFILES ON JULY 16, 1969.
117
-------
FIGURE SArAVERAGE TOTAL SUSPENDED SOLIDS PROFILE FOR PONDS ON JULY 16,1970.
OJ
CO
o
o
CO
O
UJ
o
z
bl
o.
CO
I
OL
0.
150. _
I00._
50. _
0
ISO
100. _
50
NMXCO 75 HP
WELLES 75'HP
POND n
INFLUENT SUSPENDED SOUPS 16 PPM
POND I
00 2 30
300 400
DISTANCE, IN FEET-INFLUENT TO WEIR.
-------
FIGURE 6ArVELOCITY PROFILES IN THE PONDS ON JULY 16, 1969.
20 J_
1.5.
1.0
0.5
g
UJ
(ft
UJ
0.
UJ
UJ
o '•*
UJ
>
1.0
0.!
B
POND I
100
200
300
400
500
600
700
800
DISTANCE, IN FEET-INFLUENT TO WEIR.
-------
20 40 60 60 100
DISTANCE FROM SHORE TO AERATORS.
FIGURE 7A.-VELOCITY PROFILES IN THE PONDS.
120
-------
'
FIGURE 8A.-BOD PROFILES FOR PONDS ON SEPTEMBER 17, 1969.
90
100
200
300
400
500
600
700
800
DISTANCE, IN FEET, FROM INFLUENT TO WEIR.
-------
FIGURE 9A.-DISSOLVED OXYGEN PROFILES FOR PONDS ON SEPTEMBER 17, I96S
Q.
Q-
?
X
o
s
o
V)
V)
I I
MIXCO 78 HP
Al2
WELLES|75 HP
POND n
I FT DEPTH
DEPTH AT I FT
INTERVALS
700
800
DISTANCE, IN FEET FROM INFLUENT TO WEIR.
-------
FIGURE IOA.-BOD PROFILES FOR PONDS ON NOVEMBER 3, 1969.
Q
a
i •
o
CD
POND H A
I OUT OF SERVICE.
MIXCO 75 HP
Y»-.OI62 X -I- 185.5
INFLUENT BOD 558 PPM
Y--0708X + 207.I
DISTANCE FROM INFLUENT TO WEIR.
-------
FIGURE IIA.-BOD PROFILES ON NOVEMBER 17, 1969.
T
220-_
20CL-
OUT OF SERVICE
POND IT
Q.
Q-
INFLUENT BOD 487 PPM.
Y-.063X 4236.6
100 200
300 400 500 600
DISTANCE FROM INFLUENT TO WEIR.
700 800
-------
FIGURE I2A.-TEMPERATURE AND D.Q PROFILES FOR POND EL ON NOVEMBER 3, 1969.
Q.
£L
C>
Q
2.5|_
2.0
l.5._
1.0.-
0.5.-
INFLUENT
TEMP 32?C
MIXCO
75 HP
TEMR
D.O.
PONDU
OUT OF SERVICE
2I°C_|
20°C_
cc
iu—I
100 200 300 400 500
DISTANCE IN FEET FROM INFLUENT TO WEIR.
600
-------
FIGURE I3A.-DISSOLVED OXYGEN AND TEMPERATURE
PROFILES FOR PONDS ON NOVEMBER 17, 1970.
T
I
T
I
a.
a.
ui
O
i
a
UJ
OUT OF SERVICE
*!'
D.O.
I8«C.
I
I
aa
INFLUENT TEMPERATURE 31 *C
CO
Q
100
200 300 400 500 600
DISTANCE, IN FEET FROM INFLUENT TO WEIR.
700
-------
FIGURE I4A.-BOD PROFILES FOR AERATION PONDS IN PARALLEL OPERATION ON MARCH 5,1970.
1
1
300. J>
E 150.-
Q.
O.
z K)0
1 1
INFLUENT BOD, 469 PPM.
WELLES 175 HP
1
OUT OF 1 SERVICE
5 FT LEVEL
POND H
ge
UJ
INFLUENT BOD, 469 PPM.
5 FT LEVEL
POND I
100
4-
Al6
4-
gc
ui
ICO
200 300 400 500 600
DISTANCE FROM INFLUENT TO WEIR.
700
800
-------
H
M
0}
FIGURE I5A.-TEMPERATURE PROFILES FOR PONDS IN PARALLEL OPERATION ON MARCH 5,197Q
22.0-
o
21.!
UJ
K.
21.0
22.5-
21.0-
20.5
WELLES|75 HP
iti
T
T
OUT OF I SERVICE
r
POND n
INFLUENT TEMPERATURE 29°C.
INFLUENT TEMPERATURE 29°C.
•1'
POND I
9 FT.
100
4-
ifc
200 300 400 500 600
DISTANCE, IN FEET, FROM INFLUENT TO WEIR.
T
700
-------
FIGURE I6A.-BOD PROFILES FOR PONDS IN SERIES OPERATION,
POND n TO POND I, ON FEBRUARY 16, 1970.
a.
0.
400
300
200
100
o
400
300
200
100
n
€£00
-------
FIGURE I7A -TEMPERATURE PROFILES FOR PONDS IN SERIES OPERATION ON FEBRUARY 16, 1970.
H
O
22. _
^
21
o
o
Ul
ae.
^
L_
5
K
UJ
20
i iai-
ui
15-
14
,1
WELLES 75 HP
MIXCO
1
75 HP
TEMPERATURE OF INFLUENT 28°C.
POND H
AVERAGE OF 3 DEPTHS 1 1, 5, AND 9 FT.).
TEMPERATURE OF INFLUENT 20°C.
8
A, 7
*
POND I
A, ,6
AVERAGE OF 3 DEPTHS (1, 5, AND 9 FT.).
c
(00
"560 600~
200 300 400 500 6(
DISTANCE, IN FEET, FROM INFLUENT TO WEIR.
700
-------
FIGURE I8A.-VELOCITY PROFILES FOR PONDS IN SERIES OPERATION,
POND n TO POND I, ON FEBRUARY 16, 1970.
3.78/ I FT/\ \2-37
100
200 300 400 5(
DISTANCE, IN FEET, FROM INFLUENT TO WEIR.
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JO
FIGURE I9A.— D.O. PROFILES FOR PONDS IN SERIES OPERATION,
POND n TO POND I,ON FEBRUARY 16, 1970.
200 300 400 500 600
DISTANCE, IN FEET. FROM INFLUENT TO WEIR.
700
800
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FIGURE 20A-D.Q PROFILES FOR PONDS IN PARALLEL OPERATION ON FEBRUARY 23,197Q
100
200 300 400 500 600
DISTANCE.IN FEET, FROM INFLUENT TO WEIR.
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FIGURE 2IA-TEMPERATURE PROFILES FOR PONDS IN R&RALLEL ON FEBRUARY 23, 1970.
21
20
19.-
_> 18 _
UJ
oc
i
i 2I
UJ
POND H
i
INFLUENT TEMPERATURE 30°C.
oc
hJ
\ INFLUENT TEMPERATURE 30°C.
-\ A|8 Ai7
*
.1.
20-
JJN.
19.- /9 FT
18-
PONOI
4-
K
UJ
£.
100 200 300 400 500 600
DISTANCE,IN FEET, FROM INFLUENT TO WEIR.
700 800
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VJ1
FIGURE 22A.-BOD PROFILES FOR PONDS IN PARALLEL OPERATION ON FEBRUARY 23,1970.
Q.
Q.
MIXCo|?5 HP
A 2
I
PONDU
f 140 - / INFLUENT BOD, 550 PPM.
120
200 _
ISO-
160 -
I40J- TlNFLUENT BOD, 550 PPM. POND I
120
100
200 300 400 500 600
DISTANCE FROM INFLUENT TO WEIR.
T
K.
&
700
I
800
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v4rce.s\s/on Number
Subject Field & Group
SELECTED WATER RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
Title
Crow:i Zeuerbach Corporation
Lebanon Division
Lebanon, Oregon
Aerated Lagoon Treatment of Sulfite Pulping Effluents
10
Authors)
Amberg, H. R.
Aspitarte, T. R.
Coma, J. G.
Byington, K.
Ehli, J.
16
21
Project Designation
WPRD 69-0-68 12040 ELW
Note
11
Citation
23
Descriptors (Starred First)
^Aeration basin, *Pulping wastes, Capital costs, -^Operating costs,
•^Surface aerators, *Sl±me growth, *Sphaerotilus natans, Sulfite waste,
Water pollution control, Waste water treatment.
25
Identifiers (Starred First)
^Aeration basin, ^Pulping wastes, ^Slime growth, -^Surface aerators,
-^Treatment costs.
97 I Abstract Secondary treatment of sulfite pulp and paper mill effluents in aerated.stabili-
•^ i7a-t--i/~,n Kna-ina woe: -f-ao+or? r«n a -fiill —flpfll p hasTR nvRT* a 17 month neriod of continuous
Abstract secondary treatment 01 suj-iioe pm-p aiiu paper mi i i ej.-i.-i-LUSH us _LU aci a. ucu. ouauj_i
zation basins was tested on a full-scale basis over a 17 month period of continuous
operation. The secondary treatment plant consisted of two aeration basins. One basin was
equipped with two 75-h.p. surface aerators and the other basin of equal volume was equipped
with six 25-h.p. aeration units. Piping was designed to permit series and parallel oper-
ation of the two basins and provisions were made to recycle treated waste. The waste treated
was a mixture of weak wash water from the pulp mill, evaporator condensate from the spent
liquor recovery system and paper machine white water.
Experimentation showed that series operation was more efficient than parallel
operation and that the 75-h.p. surface aerators were much more efficient mixing and aeration
devices than equivalent capacity of 25-h.p. units. An 80$ BOD reduction could be achieved
at a BOD load of 3.53 lbs./l,000 cu. ft. of aeration capacity of 2.2 Ibs./h.p. -hr. This
was equivalent to a daily BOD load of 16,000 Ibs. Biological treatment to a BOD reduction
of 80 to 85$ produced a waste which did not readily support slime growth when added to
simulated experimental streams.
Total operating cost including interest on investment and depreciation was
$169,500 per year or $4.79/ton of production. Total operating cost per pound of BOD
destroyed was 3.48 cents.
Abstractor
H. R. Amberg
Crown Zellerbach Corp., Camas. Wash. 93607
WR.102 (REV. JULY 19691
WRSIC
WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U S DEPARTMENT OF THE INTERIOR
WASHINGTON, D. C 20240
* GPO: 1969-359-339
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