EPA 660/2-74-063
July 1974
Environmental Protection Technology Series
Design Parameters for Animal
Waste Treatment Systems
Office of Research and Development
U.S. Environmental Protection Agency
Washington, O.C. 20460
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EPA-660/2-74-063
July 1974
DESIGli PARAMETERS FOR ANIMAL
WASTE TREATMENT SYSTEMS
by
T.B.S. Prakasam
R.C. Loehr
P.Y. Yang
T.W. Scott
T.W. Bateman
Project Number S800767
Roap/Task 21 AYU-01
Program Element 1BB039
Project Officer
Lee Mulkey
Southeast Environmental Research Laboratory
Environmental Protection Agency
Athens, Georgia
Prepared for
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON, D.C. 20460
For sale by the Superintendent o( Documents, U.S. Government Printing Office
Washington, D.C. 20403 - Price $3.00
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ABSTRACT
Laboratory, pilot plant, and full-scale studies evaluated design
parameters for liquid aeration systems treating livestock waste. The
evaluations were conducted using a mass balance approach and equations
developed by previous investigators. The mass balance approach is
the preferred approach since it yielded results comparable to other
approaches and involved fewer assumptions. Equations were developed
to predict the COD and suspended solids concentrations in the effluent
from the aeration systems. A design example is included for both odor
control and stabilization of the waste including minimal aeration as
well as nitrification.
In laboratory and full-scale livestock waste treatment systems uncon-
trolled nitrogen losses occurred. Preliminary investigations identified
the engineering opportunities for the control of nitrogen in aeration
units by either conservation or removal.
Greenhouse corn studies indicated acid soils were more efficient in
retaining poultry manure nitrogen than neutral soils. Neutral soils
developed toxic N02 from poultry manure. There were minor yield
differences from several types of treated poultry manure. Untreated
manure was an inferior source of N. Rates of poultry manure over 30
tons per hectare damaged corn.
Runoff losses of nitrogen and phosphorus were slight. Orchard grass
responded to poultry manure applications but Bromegrass did not.
11
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CONTENTS
PAGE
Abstract
List of Figures
List of Tables
Acknowledgements
Sections
I Conclusions
II Recommendations
III Project Need and Objectives
IV Aerobic Treatment of Animal Wastes
V Nitrogen Removal During Aerobic Waste Treatment
VI Land Application and Crop Response to Treated
Poultry Manure
VII References
VIII Appendices
ii
iv
xi
xiv
1
7
11
14
104
152
207
212
iii
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LIST OF FIGURES
FIGURE TITLE PAGE
1 Conceptual Relationships between Micro- 17
bial Growth Rate and Microbial Substrate
(Soluble BOD)
2 Schematic of the Experimental Apparatus 29
for Laboratory Aeration Studies
3 General Removal Characteristics (Solids 32
and COD) of Unsettled Poultry Manure
Suspension
4 General Removal Characteristics (Solids 33
and COD) of Settled Poultry Manure
Suspension
5 Removal Characteristics of Total COD 35
and Suspended Solids - Semi logarithmic
Plot
6 Semi logarithmic Plot of Soluble COD 36
Removal
7 Removal Characteristics of Total COD and 38
Suspended Solids with Consideration of
the Residues
8 Relationships between Total COD Removal 41
Rate and Total COD Loading
9 Relationship between Filtrate COD Re- 42
moval Rate and Filtrate COD Loading
10 Removal Characteristics of Soluble Poul- 43
try Waste Suspension
11 Graphical Estimation of Different Speci- 44
fie Growth Rates by Using Different Ini-
tial Filtrate COD
12 Graphical Estimation of Monod Kinetic 45
Constants
IV
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LIST OF FIGURES continued
FIGURE TITLE PAGE
13 Graphical Estimation of the Microbial 46
Yield Value
14 Oxygen Uptake Rate Related to Aeration 48
Time
15 Operational Parameters of Laboratory 50
Continuous Flow Units - Unit I
16 COD and Suspended Solids Reduction Re- 51
lated to Total COD Loading Rate
17 Relationship between Oxygen Uptake Rates 52
and Organic Loading Rate - Continuous
Flow Units
18 General Operational Characteristics of 54
COD and Solids in the Oxidation Ditch
19 Effect of Hydraulic Retention Time on the 56
COD and Solids Reduction - Oxidation Ditch
20 Schematic of a Completely Mixed Continuous 57
Flow Reactor Without Recycle
21 Rate of Mixed Liquor COD Removal as Re- 59
lated to COD Loading Rate
22 Suspended Solids Removal Rate as Related 61
to COD Loading Rate
23 Oxygen Uptake Rate as Related to COD 63
Loading Rate
24 Residual Nondegradable Fraction of In- 68
fluent Suspended Solids as Related to
Liquid Detention Time
25 Residuals vs HRT (with Consideration of 69
fi)
26 Graphical Estimation of a and b Values - 72
Laboratory Data
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LIST OF FIGURES continued
FIGURE
27
28
29
30
31
32
33
34
35
36
37
38
39
40
TITLE
Estimation of a and b Values Using
Oxidation Ditch Data
Estimation of a' and b' Values Using
Laboratory and Oxidation Ditch Data
Relationship between Residuals and HRT
Graphical Evaluation of Km Value
Estimation of K-i and K2 Using Laboratory
CMAS Data
Ke related to Soluble COD Loading Rate
COD and Suspended Solids Residuals Re-
lated to Hydraulic Retention Time - fi
was not Considered
COD and Suspended Solids Residuals Compar-
ed to HRT - fi was Considered
Reactors Used in Laboratory Nitrogen Con-
trol Experiments
Change of Characteristics During Batch
Treatment of Poultry Wastes
Operational Modes, Solids and Temperature
Data for the Pilot Plant Oxidation Ditch
TKN, Ammonia Nitrogen, and pH in the Pilot
Plant Oxidation Ditch
In Situ Denitrification of Pilot Plant
Oxidation Ditch Mixed Liquor
In Situ Denitrification of Pilot Plant
PAGE
73
74
77
80
82
84
85
87
108
113
123
124
126
128
Oxidation Ditch Mixed Liquor with Wastes
Added
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LIST OF FIGURES continued
FIGURE TITLE PAGE
41 Percent Nitrogen Losses During the Opera- 129
tional Modes of the Pilot Plant Oxidation
Ditch
42 Nitrogen Changes in the Pilot Plant 132
Oxidation Ditch
43 Mode of Operation of Oxidation Ditch for 134
Maintaining Constant Solids Level
44 Nitrogen Content of ODML in Ditch II at 133
Houghton Poultry Farm
45 Solids Content of ODML at the Houghton 139
Poultry Farm
46 Nitrogen Content of ODML in Ditch I 140
at Houghton Poultry Farm
47 Efficiency of Treatment at Houghton 141
Poultry Farm During Different Months
of 1972
48 Dissolved Oxygen Sampling Points in 142
the Houghton Oxidation Ditches
49 Effect of Liquid Detention Time on 146
Nitrogen Removal
50 Nitrogen Applied over a 2 Year Period as 159
Poultry Manure of Chemical Fertilizer,
Poultry Waste Residue Study, 1971-72.
51 Corn Dry Matter Yields as Influenced by 162
Soil, Manure Source and Rate of Manure
Application L.S.D. @ .01 = 1.7, 2.3 and
2.3 respectively.
52 Ave. Honeoye and Mardin Soil N03-N Concentra- 163
tions for each Manure Source and each Sampling.
53 Ave. Honeoye and Mardin NO^-N Concentrations
for each Source at 3 Sampling Dates.
Vll
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LIST OF FIGURES continued
FIGURE TITLE PAGE
54 Ave. Honeoye and Mardin Soil Nlfy-N Concen- 165
trations for each Manure Source at 3 Sampling
Dates.
55 Effect of Manure Source and Rate of Applica- 166
tion on Corn Yields after 36 Days Growth on
Honeoye and Mardin Silt Loam Soils.
56 Source of Manure Nitrogen and Rate of Manure 168
Application in Relation to Dry Matter Produced
and Nitrogen Content of Corn Plants. Greenhouse
Exp. II.
57 Soil pH and Rate of N Application (kg/ha) in 169
Relation to Dry Matter Produced and Nitrogen
Content of Corn Plants. Greenhouse Exp. II.
58 Soil pH and Source of Manure in Relation to Dry 171
Matter Produced and Nitrogen Content of Corn
Plants. Greenhouse Exp. II.
59 42 Day Dry Matter Corn Yields as Influenced by 172
Soil N02-N from Raw Manure 21 Days After Planting.
60 42 Day Corn Dry Matter Yields as Influenced by 173
Soil NO?-N from Oxidation Ditch Manure 21 Days
After Planting.
61 Influence of Nitrogen Fertilization on 175
Dry Matter Yields and Nitrogen Content
of 42 Day Old Corn Plants. Greenhouse
Exp. II
62 The Relationship of Nitrogen Uptake by 176
Corn to Nitrogen Available from Soil
Mineralization and Additions of Various
Amounts from Various Sources on 2 Soils.
63 The Relationship of Nitrogen Uptake by 177
Corn to Dry Matter Produced on Two Soils
Treated with Various Rates of Nitrogen
from Various Sources.
64 1971 Dry Shelled Corn Yield from Poultry 178
Waste Residue Study - L.S.D. Between Rates
0 .05 = 1891.
vm
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LIST OF FIGURES continued
FIGURE TITLE PAGE
65 1971 Dry Matter Yields of Corn Stover from 179
Poultry Waste Residue Study - L.S.D. Between
Rates @ .05 = 594.
66 Total N in Grain and Stover 1971 from Poultry 182
Waste Residue Study.
67 1972 Dry Shelled Corn Yield from Poultry 183
Waste Residue Study - L.S.D. Between Rates
@ .05 = 459.
68 1972 Dry Matter Yields of Corn Stover from 184
Poultry Waste Residue Study - L.S.D. Between
Rates @ .05 = 318.
69 Total Nitrogen in Grain and Stover from 185
1972 Poultry Waste Residue Study - L.S.D. @
.05 = Grain 7.3, Stover 13.4, Grain and
Stover 9.5.
70 Surface & Subsurface Soil Analysis. Com- 186
posite of Weekly Samples May 25 - Aug. 3, 1972.
71 Cumulative Surface Runoff from 6 Selected 188
Storms as Influenced by Rate and Type of
Poultry Manure. [Corrected 10% for each 1%
Slope Difference (57)].
72 Cumulative Soluble Phosphorous Losses in 189
Runoff from 6 Selected Storms as Influenced
by Rate and Type of Poultry Manure [Corrected
10% for each 1% Slope Difference (57)].
73 Cumulative HQ$-H Losses in Runoff from 6 190
Selected Storms as Influenced by Rate and
Type of Poultry Manure [corrected 10% for
each 1% Slope Difference (57)].
74 Cumulative NH/j-N Losses in Runoff from 6 191
Selected Storms as Influenced by Rate and
Type of Poultry Manure [corrected 10% for
each 1% Slope Difference (57)].
IX
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LIST OF FIGURES continued
FIGURE TITLE PAGE
75 Cumulative Soil Loss from 6 Selected Storms 192
as Influenced by Rate and Type of Poultry
Manure [Corrected for slope Differences by
LS Ratio (52)].
76 Cumulative Organic Matter Loss in Sediment 193
from 6 Selected Storms as Influenced by Rate
and Type of Poultry Manure [Corrected for Slope
Differences by LS Ratio (52)].
77 Cumulative Total Phos. Loss in Sediment from 194
6 Selected Storms as Influenced by Rate and
Type of Poultry Manure [Corrected for Slope
Differences by LS Ratio (52)].
78 Cumulative Total Nitrogen Loss in Sediment 195
from 6 Selected Storms as Influenced by Rate
and Type of Poultry Manure [Corrected for
Slope Differences by LS Ratio (52)].
79 A Comparison of the Effects of 2 Forms, 3 196
Rates and 2 Times of Application of Poultry
Waste and Commercial Fertilizer on the
Yield of Orchard Grass (1st & 2nd Cutting
1973) L.S.D. between Rates ± .05 = 1255.
80 A Comparison of the Effects of 2 Forms, 3 198
Rates and 2 Times of Application of Poultry
Waste and Commercial Fertilizer on the Yield
of Bromegrass (1st & 2nd Harvest (1973) L.S.D.
between Rates @ .05 = 1939.
81 A Comparison of Corn Grain Yield and Plant 199
Population as Influenced by Additions of
Poultry Manure.
82 Inorganic-N Concentrations in Soil as 200
Influenced by Rate of Poultry Manure
Additions. Sampled 7/15/73.
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LIST OF TABLES
TABLE TITLE PAGE
1 Constants Suggested for Use in the 22
Design for the Treatment of Domestic
Wastes
2 Comparison of Total COD Removal Con- 39
stants
3 Pilot Plant Oxidation Ditch Character- 55
istics Data During Equilibrium Periods
4 Application of Design Equations for 62
Total COD and Suspended Solids to Results
from the Pilot Plant Oxidation Ditch
5 Source of Evaluated Constants used to 70
Predict Effluent COD and Suspended Solids
6 Comparison of Constants Based on Data from 75
the Laboratory Unit and the Oxidation
Ditch
7 Comparison of Different Design Approaches 78
for the Aerobic Treatment of Poultry
Wastes
8 Comparison of 02 Uptake Rate by the 88
Modified Mc.Kinney's Approach
9 Influent COD Concentration, HRT, and 91
Volume of Ditch Needed to Yield the
Secondary Effluent Criterion for COD
(60 mg/1)
10 Relationship between HRT, Influent 92
Suspended Solids Concentration, and
Expected Effluent Suspended Solids
Concentration
11 Relationship Between HRT and Influent and 94
Suspended Solids to Achieve an Effluent
Suspended Solids Concentration of 45 mg/1
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LIST OF TABLES continued
TABLE TITLE PAGE
12 Transfer of Oxygen by an Experimental "
Rotor at Various Equilibrium D.O.
Concentrations
13 Rotor Length Needed for Oxygenation of 100
Poultry Waste from 10,000 Birds Based
on the Performance Characteristics of a
Rotor Tested at AWML
14 Design Parameters and Expected Performance 101
of an Oxidation Ditch for 10,000 Birds
at 2" Immersion Depth
15 Nitrogen Balances in Batch Nitrifying H4
Units at Different Initial Solids Con-
centration - Laboratory Study
16 Nitrogen Losses Due to Ammonia Volati- 116
lization and Denitrification - Batch
Study
17 Nitrogen Balance on Batch Reactors at 12°
Constant Aeration Rate
18 Nitrogen Balance on Batch Reactors at 120
Different Aeration Rates
19 Characteristics of the Poultry Excreta 122
Entering the Oxidation Ditch Systems
20 Activity of Nitrosomonas in a Dem'tri- 125
fying Mixed Liquor
21 Nitrogen Loss in Oxidation Ditch System 131
22 Nitrogen Contents of ODML and Supernatant 133
.from Settling Tank
23 Total Nitrogen Loss from Oxidation- Ditches
24 Dissolved Oxygen Levels at Different Points
in Houghton Oxidation Ditches
xi 1
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LIST OF TABLES continued
TABLE TITLE PAGE
25 Amount of Each N Fraction, at Time of 155
Application, Contained in Untreated and
Various Treated Forms of Poultry Manure.
(Greenhouse Exp I)
26 Amount of each N Fraction, at Time of Appli- 157
cation, Contained in Untreated and Treated
Forms of Poultry Manure. (Greenhouse Exp II)
27 Dry Matter Yields and Nitrogen Content of 167
Corn Grown on 2 Soils and 3 pH levels.
(Greenhouse Exp II)
28 The Effect of Soil and Nitrogen Source on 180
Crop Uptake of Nitrogen.
29 Composition of Pullet Manure on Dry Weight 201
Basis. (Sullivan Co. Study)
30 Corn Yield Data as Influenced by 1973 Poultry 202
Manure Additions in Sullivan County Study.
31 Soil Analysis of Topsoil (0-25 cm) Taken Prior 204
to Poultry Manure Additions and Corn Planting.
32 Soil Analysis of Subsoil (25-50 cm) Taken Prior 205
to Poultry Manure Additions and Corn Planting.
xiii
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ACKNOWLEDGEMENTS
This research was supported by the Environmental Protection Agency under
project number S800767 and by the College of Agriculture and Life Sciences,
Cornell University. The guidance of Mr. Lee Mulkey, Environmental Pro-
tection Agency, Athens, Georgia, who served as the project officer is
gratefully acknowledged.
The project is a multidisciplinary effort of the Departments of Agri-
cultural Engineering and Agronomy of the College of Agriculture and
Life Sciences. Drs. R.C. Loehr and P.J. Zwerman are the project
directors.
The principal investigators associated with the project are Drs.
T.B.S. Prakasam, T. Bateman, T. Scott and P.Y. Yang.
The advice of Dr. E.G. Srinath, the help of J.H. Martin, Jr. and
H.T. Grewling; and the support of Dr. M.J. Wright, Chairman, Department
of Agronomy are gratefully acknowledged. Technical assistance was pro-
vided by Y.D. Joo and R. Jones.
The help of R.J. Krizek, J.F. Gerling and E. Callinan in the preparation
of the figures is gratefully appreciated.
The patience and skill of Colleen Raymond, Diane LaLonde, Sally Gray,
and Judy Eastburn in typing this report are most sincerely appreciated.
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SECTION I
CONCLUSIONS
AEROBIC TREATMENT OF ANIMAL WASTES
1. Several approaches were investigated to determine appropriate pre-
dictive equations for the concentration of suspended solids and COD in
the effluent of a liquid aeration system treating poultry wastewater.
The equations developed by a mass balance approach are preferred to
the equations developed from those of Monod, Eckenfelder, and McKinney.
All of these equations were evaluated in this study for use with animal
wastes. The results obtained using the mass balance equations were
comparable to results obtained by the other equations. The mass
balance equations are preferred because fewer basic assumptions had
to be made and fewer empirical constants had to be used.
2. Poultry wastewater has a significant non-biodegradable fraction
which mu'st be included when deriving parameters for the design of liquid
aeration systems.
3. The two mass balance equations developed to predict the total sus-
pended solids and total COD concentration in the overflow from aerated
wastewater are:
a) for suspended solids concentrations
., _ Xi - X
K1 =
X-t
Where K1 = suspended solids removed coefficient
Xi = influent suspended solids concentration (mg/1)
X = effluent suspended solids concentration (mg/1)
t = liquid detention time (days)
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b) for COD concentration
Si - S"
K =
S-t
Where K = COD removal coefficient
Sj_ = influent COD concentration (mg/1)
S = effluent COD concentration (mg/1)
t = liquid detention time (day)
4. The coefficients for suspended solids and COD removal (K1 and K)
were found to increase with an increase in loading factors and obeyed
the following relationships:
a) K1 = 0.011 + 0.15X1
b) K = 0.017 + 0.11X'
Where X1 = the loading factor (gm COD/gm MLVSS)
The value of K' ranged from 0.011- to 0.176 for the range of loading
factors evaluated in the study (0 to 1.1). Similarly K was found to
have a range of 0.017 to 0.138 for the same range of loading factors.
Values for K1 and K were not tested beyond this loading range in this
study. Application of the above relationships should be made with
caution for loading factors above 1.1.
5. The removal rate coefficient at low loading rates essentially repre-
sent the endogenous metabolism coefficient of the waste mixed liquor.
6. Substrate removal in the poultry wastewater exhibited phasic removal
patterns with different kinetic constants for each phase. First order
kinetics were not able to describe the substrate removal patterns with
these wastes.
The phasic removal was attributed to the presence of a readily available
substrate which was used rapidly followed by the slow utilization of a
less readily available particulate and less soluble substrate.
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7. Based on this Investigation and using the mass balance equations,
the following steps can be used to design an oxidation ditch type treat-
ment system for poultry waste and to predict the effluent quality from
such systems.
/ .
a) Determine the number of birds contributing waste to the oxi-
dation ditch, determine the actual surface area occupied by the cages
in, the building, and assume that the ditch will be built directly below
the cages.
b) Size the surface area of the oxidation ditch to fit the space
below the birds so that the waste will drop directly from cages into the
ditch.
c) Assume the liquid depth to be between 18 and 24 inches. This
will permit calculation of the liquid volume and, assuming a constant
liquid and solid input from the birds, will fix the detention time of
the ditch. The waste Input can be obtained from average data on the
waste characteristics for the type of birds in the cages.
d) Assume that a mixed liquor total solids concentration of between
1-2% will be maintained in the oxidation ditch. This will permit maximum
oxygen transfer by the rotor. Based on the volume of the ditch contents
and concentration of volatile suspended solids, the total weight of
volatile suspended solids in the ditch can be obtained.
e) Establish the loading factor by dividing the COD (gm) entering
the ditch (COD, gm/bird x number of birds) by the VSS (gms) in the ditch.
f) From the equations given 1n conclusion 4, obtain K1 and K.
g) Using these values of K1 and K, the effluent quality can be
predicted by using the equation given 1n conclusion 3.
8. The oxygen requirements for the treatment of poultry waste depend
on the objectives of the treatment. A system designed only for odor
control and partial stabilization will have a lower oxygen requirement
than a system designed for odor control and nitrification. For example,
a system designed to treat wastes from 10,000 birds will require about
215 pounds of oxygen/day to achieve odor control and partial stabili-
zation of the wastes. For the type of waste used in the example, an
additional 70 pounds of oxygen per day will be required if nitrification
of the waste is also desired. A higher amount of 02 will be needed for
nitrification, if the waste under consideration has a higher concentration
of TKN than the one considered 1n the above example.
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9. Based on laboratory systems operating under equilibrium conditions,
the oxygen uptake rate of mixed liquors increased as the loading rate
increased. These uptake rates were between 1-3 mg of oxygen/gm TVS/hr
up to a loading rate of 0.13 gm total COD/gm MLVSS/day.
A rotor may be installed to provide aeration of the mixed liquor. The
size of the rotor can be calculated by a) computing the oxygen demand
of the waste per day in pounds; this depends again on whether nitrification
is desired or not, b) computing the oxygen transfer rate for unit
length of rotor, and c) determining the required length of rotor. Our
laboratory experiments and pilot plant data indicated that approximately
0.5 Ibs of oxygen could be transferred per foot of rotor length per hour
at a 2 in. immersion depth, using a Thrive Center rotor.
NITROGEN REMOVAL DURING AEROBIC WASTE TREATMENT
1. Batch scale experiments on the nitrification of poultry wastewater
suspensions confirmed that nitrogen was lost from the nitrifying mixed
liquors by denitrification which occurred under aerobic conditions.
At a constant rate of aeration, nitrogen losses from a nitrifying
reactor were higher as the loading rate increased. This was a result
of increased oxygen demand of the mixed liquor.
2. Observations on a pilot plant scale oxidation ditch and full scale
oxidation ditch indicated that they were effective as odor controlling
devices. Nitrogen losses also occurred in the systems and could be
traced to either ammonia volatilization or denitrification of the nitrate
and nitrate formed during treatment. During the start-up phase of the
operation of the oxidation ditch systems, a loss of as much as 70% of
the input nitrogen could be attributed to ammonia volatilization.
3. In the pilot plant oxidation ditch, as nitrification occurred, the
nitrogen losses due to ammonia volatilization became negligible. When
the system was operated on a flow through mode, about 30%. of the nitro-
gen was lost and could be attributed to the denitrification of the
nitrified mixed liquor. When denitrification was induced deliberately
by stopping the rotor and mixing was provided intermittently by turning
the rotor on, almost all the NOy and NOj-was denitrified. During a
six month operation of the ditch, denitrification was carried out delib-
erately for a short time after the first three months of operation.
The losses of NOg-N due to this denitrification were only 8% during
this short period as compared to the 23% loss due to uncontrolled deni-
trification that took place over a much longer period as the ditch
operated under aerobic conditions. It appears that controlled denitri-
fication losses may be increased by employing a frequent repetitive
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nitrification-denitrification scheme. This will facilitate a higher
removal of oxidized nitrogen.
4. Studies with the full scale oxidation ditch at the Houghton Poultry
Farm revealed that perceptible nitrification could not be achieved due
to low dissolved oxygen concentration in the mixed liquor. The dis-
solved oxygen concentration was less than 1 mg/1 during 64% of the time
and in 70% of the ditch volume. The loss of nitrogen due to ammonia
volatilization amounted to about 40% of the total nitrogen input. When
aeration of the mixed liquor is not adequate, there is the risk of
ammonia odors, particularly when the ventilation in the building is
poor. A practical solution to eliminate the ammonia odor is to design
the system for achieving nitrification as described in the section on
aerobic treatment.
LAND APPLICATION AND CROP RESPONSE TO TREATED POULTRY MANURE
Research activities were equally divided between greenhouse and field
studies.
From the greenhouse studies it was concluded that:
1. Acid soils in the Northeast and North Central U.S.A. have a greater
potential for fixing the nitrogen liberated from poultry manure than do
neutral soils. Soil analysis of greenhouse samples show that nitrogen
from poultry manure, under acid conditions, tends to be held in the soil
as ammonium ions. In the case of neutral soils this ammonium nitrogen
tends to be oxidized to nitrates. The nitrate form is then more easily
leached from the soil.
2._ It was also established that soils at a pH of 7-8 tended to accumulate
NOjj ions which were toxic to the test corn plants. This was especially
true for oxidation ditch treated manure and raw manure.
3. There was no consistently superior corn yield response from one or
the other kind of treated poultry manure application. At lower rates
(about 200 kg/ha) raw manure was generally as good as treated manure. At
higher rates raw manure was a relatively poorer source of nitrogen. Diffused
air treated manure tended to be superior at higher rates of application.
4. Greenhouse production of corn dry matter increased with increased
fertilization by poultry manure of all kinds except where the N0£ ion
caused toxicity to the corn plants.
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5. Under "normal" rates of fertilization with poultry manure corn plants
could extract only 2/3 of the available nitrogen from greenhouse pots. The
higher rates of nitrogen fertilization from manure resulted in a lower
rate of nitrogen extraction by the test corn plants.
From the Field studies it was concluded that:
6. The residual benefits of poultry manure applied in 1971 were clearly
evident in 1972. Using corn as the test crop these 1971 manured plots
yielded 80-90% of similar plots manured both in 1971 and 1972. These
preliminary results suggest alternate years might be used for fertilizing
corn with poultry manure.
7. A normal crop of corn grown in the field will remove approximately
100 kg/ha of nitrogen from the soil. Usually the soil will supply 50
kg/ha of nitrogen. Poultry manure applied at the rate of 100 kg/ha N
will supply approximately 50 kg N/ha. It is apparent that excessive rates
of poultry manure fertilization should result in surplus nitrogen production,
Such a nitrogen surplus either stays in the soil or leaches out into ground
water.
8. A series of runoff plot measurements were made for the following para-
meters: runoff, soluble phosphorus, nitrate, ammonium ions, soil losses,
organic matter losses, total sediment phosphorus, total sediment nitrogen.
Oxidation ditch poultry manure and raw manure were applied at varying
rates. There were no significant differences in losses to the environ-
ment.
9. Two grasses, orchard grass and bromegrass, were established and
utilized for varying rates of poultry manure fertilization. Oxidation
ditch treated manure and raw manure were applied. Bromegrass did not
respond to any kind of poultry manure application. Applied in the
spring oxidation ditch manure was superior to fresh manure when applied
to orchard grass. However, there was no difference in yield of orchard
grass from fall applied manure treatments.
10. In a cooperative field trial rates of poultry manure application
in excess of 30 metric tons per hectare depressed corn yields. Pre-
liminary evidence suggests that this yield depression may be due to a
high content of soluble salts in the poultry manure.
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SECTION II
RECOMMENDATIONS
AEROBIC TREATMENT OF ANIMAL WASTES
1. Since the EPA effluent guidelines do not permit the discharge of
effluents from livestock operation to surface waters, it is not neces-
sary to design treatment systems to meet the secondary effluent
characteristics. The objective in designing treatment systems for
these waste$ should be only to achieve odor control and a degree of
treatment that is compatible with criteria for the ultimate disposal
of the effluents on land.
2. Based on the equations developed in this study, liquid aeration
systems can be designed for the control of odor and stabilization of
livestock wastes. The following approach is suggested for designing
an oxidation ditch type of aeration system and predicting the quality
of effluent resulting from such a system.
a) Determine the number of birds contributing waste to the
treatment system and the actual surface area occupied by the cages
in the building. Assume that the oxidation ditch will be built
directly below the cages.
b) Determine the surface area of the oxidation ditch to fit
the space below the birds so that the waste will drop directly from
cage into the ditch.
c) Assume the liquid depth to be between 18 and 24 inches
(-46 and 61 cm). This will permit calculation of the ditch volume,
and assuming a constant volume of waste input from the birds, will
fix the detention time of the ditch. In actual practice this volume
can be obtained from average data on the waste characteristics for
the type of birds in the cages.
d) Maintain the mixed liquor total solids concentration between
1-2% to permit maximum oxygen transfer by the rotor.
-------
e) Find the loading factor of the ditch as follows: 1) compute
the COD in kg entering the ditch every day, 2) compute the weight of
volatile suspended solids (kg) by multiplying the concentration of
volatile suspended solids in the ditch by the volume of the ditch
contents (mg/1 x liters/1000 = kg of volatile suspended solids). The
loading factor is COD, (kg)/VSS, (kg).
f) To predict the effluent quality use the following approach: 1)
Compute K1 and K, the suspended solids and COD removal coefficients
respectively, using the following equations:
K1 = 0.011 + 0.15 X1
K = 0.017 + 0.11 X1
where
X' is the loading factor.
2) Using the above computed values for K' and K predict the effluent
quality using the following equations:
Xi - x
K =
and
Si - S
where
Xi = influent suspended solids concentration, mg/1
X = effluent suspended solids concentration
8
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Si = influent COD concentration, mg/1
S = effluent COD concentration
t = detention time, days
3. When odor control is the objective, design of the system for
minimal aeration is recommended. In this approach just enough oxygen
is provided to meet the demand for the oxidation of carbonaceous matter.
A residual dissolved oxygen concentration is not needed. However, if
the waste needs to be stabilized to the level of ammonia oxidation,
the aeration equipment size also should consider the oxygen demand due
to nitrification and a residual dissolved oxygen concentration of 2.0
mg/liter of the mixed liquor. For poultry wastes this additional
nitrogenous oxygen demand should be established by analyzing the waste
for nitrogen content and by assuming that at least 80% of it will be
available for nitrification. For designing purposes each kg of nitri-
fiable TKN may be considered to exert about 4.6 kg of oxygen demand.
NITROGEN REMOVAL DURING AEROBIC WASTE TREATMENT
1. Although it is premature to make any recommendations pertaining
to nitrogen control in poultry wastewater, liquid aeration system does
seem to provide opportunities for the control of nitrogen in livestock
wastes. Detailed pilot plant studies are being conducted and appropriate
recommendations will be made from data collected in the final year of
the project.
LAND APPLICATION AND CROP RESPONSE TO TREATED POULTRY MANURE
Recognizing the short duration of the research and weather extremes
experienced with the field trials, recommendations are based on our
limited knowledge to date.
1. Poultry manure that has been aerobically treated for odor control
can be used for crop growth, and is an excellent source of plant
nutrients.
2. Higher rates of poultry manure can be applied to acid soils
(pH<5.0) in contrast to those rates applied to slightly acid to
neutral soils. For maximum yields, it is recommended that application
rates for corn not exceed 224 kg N/ha (200 Ibs N/acre) of aerobically
treated manure on soils with a pH of 5.0 or greater and 448 kg N/ha
(400 Ibs N/acre) on acid soils (pH<5.0). Raw manure containing 50%
moisture and 1% nitrogen (wet weigEt basis) can be applied to soils
at one-half the recommended rate for treated manure.
-------
3. Application rates for perennial forage grasses, from both treated
and untreated sources can be applied at the rate of 112 kg N/ha
(100 Ibs N/acre).
4. Due to residual carryover of nitrogen during the second year,
rates approaching 448 kg N/ha (440 Ibs N/acre), should be applied
only in alternate years to avoid degradation of water quality.
Because of the short duration of the research as well as extreme
weather conditions during this period, 1t 1s inappropriate at this
time to recommend a maximum rate of application for adequate plant
growth while maintaining a high degree of water quality. Additional
data are currently being collected which will hopefully provide for
an accurate estimation of the rate* and water quality interaction
under a variety of climatological sequences.
10
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SECTION III
PROJECT NEED AND OBJECTIVES
Project Need
Agricultural production is becoming more Intensive. Increased efficiency
of agricultural production has generated a variety of pollution control
problems. Large scale confined animal operations developed in the past
decades have resulted in both water and air pollution due to accumulated
wastes. These operations have been a source of fish kills, lowered
recreational values, and nuisances to surrounding areas. With current
animal waste handling methods, odors can be a significant problem,
especially during land spreading. Animal wastes can contribute to
impaired water quality by heavy organic loads, by excessive nutrients,
and by direct discharge to streams. Land disposal of these wastes may
result in subsequent runoff and sub-surface percolation of contaminants.
Liquid waste handling and treatment systems have developed because of
the desire to reduce labor and maintenance costs. These systems also
provide a better environment for the animals and workers within the
controlled production facilities. Experience has indicated that properly
designed and operated aerobic systems can eliminate the odor problems
associated with many of the current systems and can reduce the pollution
potential of the wastes prior to disposal on the land.
Research on aerobic treatment processes for animal wastes has indicated
the extent to which-aerobic treatment can be used with specific animal
wastes and the general management conditions under which the aerobic
processes can function, dnly recently has the necessary design informa-
tion begun to be available for aerobic biological systems to control
odors, provide a specific degree of treatment, or to provide a removal
of excess nitrogen from animal wastes.
The characteristics of animal wastes range from dilute wastes such as
those obtained from duck production operations with characteristics
similar to strong sewage to semi-solid wastes and such as those from
cattle and poultry wastes which may have moisture contents of 75-85%.
11
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To meet effluent criteria for their discharge to surface waters, extremely
high removal efficiencies, 99+%, must be obtained because of the character-
istics of the semi-solid animal wastes. In addition, the EPA Effluent
Guidelines (1) call for no discharge of animal wastes to surface waters.
The high treatment efficiencies and guidelines require close evaluation
of combined treatment-land disposal alternatives.
Land has been the traditional site for the disposal and recycle of
slurry and semi-solid stored, anaerobic animal wastes. With proper crop
and land management, land disposal of animal wastes will remain an
economic and acceptable method. Organic and nutrient constituents
of these wastes can be incorporated into the soil and removed by crops.
Prior treatment to accomplish excessively high BOD, solids, and nutrient
removals may not be necessary with disposal on land. Any treatment or
stabilization that the wastes receive must be compatible with land and
crop management practices including control of excess nutrients that
may cause secondary pollution problems.
Aerobic biological treatment systems for animal wastes result in an end
product with a) decreased pollutional characteristics because of the
treatment, b) different types of available nitrogen, and c) different
physical characteristics due to water added and the microbial breakdown
of the roughage in the untreated wastes. Only very limited information
exists on the rates at which the residue from aerobic animal waste
treatment units can be applied to crop and non-cropped land without
causing secondary pollution problems. Better information is needed on
the best land application methods to dispose of stored untreated animal
wastes. Runoff or percolation associated with such land disposal is
of prime concern. The fate of the soluble organic and nitrogen forms
and the quantities of the treated wastes that can be disposed of under
different cropping patterns also needs to be known.
A common approach to waste management problems is to have researchers
in various disciplines investigate fundamentals and/or processes. Reports
of such research are then made available to the professions. Experience
has indicated that while this approach can provide desirable results, a
multi-disciplinary approach can provide more meaningful results and con-
clusions. This project offers the opportunity to integrate research and
demonstration activities in the disciplines of sanitary engineering and
agronomy. These are key disciplines in agricultural waste management.
The sanitary engineer designs the treatment systems to meet specific
effluent requirements. The agronomist accepts the treated or untreated
wastes and determines the feasible land disposal system. This project
permits coordination of these disciplines to demonstrate appropriate
design parameters for the treatment and disposal of animal wastes.
12
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Project Objective
The specific objectives of this research are to: a) demonstrate the
applicability of sanitary engineering fundamentals to the design of
aerobic biological treatment systems for animal wastes, and to develop
the necessary design parameters for systems to remove excess nitrogen;
b) demonstrate proper management methods for the disposal of animal
wastes, including aerobically treated waste, on the land.
The project consists of two parts:
A - Parameters for Aerobic Liquid Waste Treatment Systems
B - Parameters for Land Application of Animal Wastes
Design parameters for combined animal waste treatment-land disposal and
parameters for the design of individual waste treatment and individual
land disposal methods will be a result of the project. Such a program
of research results in design parameters that provide maximum flexi-
bility for those who will use these waste management alternatives.
The emphasis of the project has been to demonstrate, in the field or in
large scale systems, the feasible approaches to meet the project
objectives. It was necessary, however, to conduct some laboratory and
greenhouse studies to: a) clarify the fundamental relationships of the
potential processes, especially with wastes of different characteristics,
such as land disposal of treated and untreated wastes, and b) to delineate
those relationships that appear most feasible for large scale demonstration.
13
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SECTION IV
AEROBIC TREATMENT OF ANIMAL WASTES
INTRODUCTION
The confined production of animals has the potential of contributing to
air pollution by odors and dusts generated at the production facilities
and to water pollution by the discharge of untreated wastes. Controlled
waste treatment processes can reduce or eliminate the air and water
pollution potential of animal wastes. Aerobic and anaerobic processes
are compatible with these wastes. Aerobic processes are generally pre-
ferred in many areas since they can prevent the generation of obnoxious
odors and can stabilize the wastes prior to disposal. Examples of
possible aerobic processes include oxidation ponds, aerated lagoons,
oxidation ditches, activated sludge modifications, and land disposal.
To date (1973), aerobic treatment processes for animal wastes largely
have been designed on the basis of previous experiences and situations
which produced satisfactory results. Because aerobic treatment pro-
cesses are biological, an understanding of the processes must be based
upon the fundamentals of microbial transformations in the biological
waste treatment units. If this understanding can be achieved, rational
predictions of performance and better design become possible, and the
capabilities of a process can be better utilized. Without an under-
standing of the funadmentals, the processes can be treated only as
"black boxes" in which the performance is subject to parameters seem-
ingly beyond our control. Lack of proper understanding and use of the
fundamentals means that successful design and operation of aerobic
treatment processes can be based only on prior performance which may be
difficult to translate to different wastes and environmental conditions.
The purpose of this study has been to determine and apply the fundamentals
of aerobic waste stabilization processes to the treatment of poultry
manure. Data were obtained from laboratory, pilot plant, and full-scale
aerobic units treating poultry manure. These units were monitored
under the direct control of the Agricultural Waste Management Program
14
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of the College of Agriculture and Life Sciences, Cornell University. In
addition to design parameters developed from the project results, the
relationships developed by Monod (2), Eckenfelder (3-6), and McKinney
(7-9) were evaluated for their use in the aerobic treatment of these
wastes.
The results of the study indicate reasonable approaches for the design
of aerobic treatment units for poultry wastes. The general scope of the
study included:
-general removal characteristics of the organic material in the wastes
-relationship between microbial growth and available substrate removal
-determination of oxygen demand and rate of consumption
-feasibility of a continuous flow, completely mixed aerobic system
-application of design concepts
BACKGROUND
General
Aerobic biological treatment processes have been utilized for a variety
of municipal and industrial wastes. Although the characteristics of
animal wastes and wastewaters are different from those of municipal and
industrial wastes, established design concepts should be valid if they
are modified for the different waste characteristics. The actual appli-
cation of treatment technology to animal wastes is in its early stages.
To facilitate the application of proper design concepts to the aerobic
treatment of animal wastes, established concepts will be reviewed and
applied using data obtained in this study. This section will include a
review of BOD, COD, and solids removal kinetics, available design
approaches, and current processes for the aerobic treatment of animal
wastes.
BOD or COD Removal
BOD and COD removal has been investigated in many studies. Zero and
higher order reactions have been observed with mixed cultures. Sequen-
tial removal patterns have been observed when complex organic wastes
were used as a substrate.
BOD removal is related to sludge growth and to the availability and
utilization of the substrate contained in the waste. The overall
removal rate decreases as the more readily oxidizable components are
removed. The total BOD removal can be estimated by a first or second
order relationship until the residual BOD becomes small. At and below
this residual, the BOD removal will follow a zero order reaction. Dis-
continuous removal kinetics can be used to describe the relationship
15
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between BOD removal rate and concentration of BOD remaining, i.e., first
order relationships can be used before substrate becomes limiting and
zero order after it is limiting.
There are generally two major descriptions of the dependence of growth
rate upon substrate concentration in waste treatment. These are illus-
trated by the work of Monod (2) and by the studies of Garrett and
Sawyer (10). Monod relationships predict that the logarithmic growth
rate is a continuous function of substrate concentration up to the con-
centration of substrate at which growth rate becomes a maximum (Figure 1).
The other (10) indicates that for practical purposes the relation between
growth rate and the remaining soluble BOD is represented by a discon-
tinuous function. Eckenfelder (4), McKinney (7), and others have used
this concept for the design of biological waste treatment systems.
Solids Reduction
Considerable research on solids destruction has been reported, especially
for the aerobic digestion of biological sludge. Equally important
information on solids destruction can be found in studies of the extended
aeration process (11-18). In this process, solids destruction is
accomplished concurrently with removal of exogenous carbon sources in
the incoming waste due to the low food to microorganism (F/M) ratio
maintained in the system.
The rate of solids reduction should be considered as related to both
aeration time and organic loading rate rather than being independent
of these factors. The kinetics of aerobic stabilization has been
described by a first order reaction. Data from both batch and continuous
flow completely mixed reactors were able to be expressed in this manner.
An inert non-biodegradable residue will result from the degradation of
the suspended solids and must be considered in all equations describing
solids degradation.
The solids removal rate is temperature dependent. The sludge stabili-
zation rate may be defined as the decrease of volatile solids or equiva-
lent COD per unit time or as the reduction of the biological activity of
sludge, i.e., the endogenous respiration rate. The percent reduction of
volatile solids is not satisfactory to indicate the stability of sludges
from aerobic digesters under continual loading conditions because the
sludges may have undergone varying degrees of stabilization prior to
entering the aerobic digesters. The specific oxygen uptake rate is one
of the more reliable indicators of the stabilized conditions of the
aerobically digested sludge. Rates in the range of 0.5 to 1.0 mg
Oo/gVSS/hr have been associated with well stabilized sludges.
16
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DISCONTINUOUS
CONTINUOUS
SOLUBLE BOD REMAINING,mg/1
Figure 1. Conceptual relationships between microbial growth
rate and microbial substrate (soluble BOD)«
17
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PROCESS DESIGN
Three major approaches for the design of aerobic biological treatment
processes can be used. These can be illustrated by the use of equations
developed by Monod (2), McKinney (7-9), and Eckenfelder (3-6).
Monod
The equation by Monod (2) to describe the relationship between growth
rate and concentration of growth limiting nutrient is similar to the
Michaelis-Menten equation which described the relationship between sub-
strate and enzyme reactions as follows:
ymS
=
where p = specific growth rate
ym = maximum value of y
Ks = saturation constant or the substrate concentration
where y = l/2um
S = concentration of growth limiting nutrient
The theory and operation of continuous cultures has been reviewed by
a number of researchers (19-22) and will be discussed only briefly.
The design of completely mixed continuous flow biological treatment
processes normally is based on the premise that a steady state equilibrium
can be maintained between the rate at which the substrate is removed or
metabolized and the rate of the growth of bacteria. The logarithmic
growth rate can be expressed as:
where x is the concentration of bacterial cells. The relationship, which
expresses the net change in microbial cell mass is equal to the amount of
microbial cells synthesized from the substrate less the microbial decay:
18
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at Y -"* <3>
where Y is the yield coefficent and b is the endogenous coefficient.
When the steady state conditions are established in a once-through,
completely mixed, continuous flow system, the rate of change in cell
concentration will be zero, i.e.,
= yx - Dx = 0 (4)
y = D = vmf) (5)
D is the dilution rate and equal to the flow rate divided by the volume
of the reactor. S is the concentration of substrate in the reactor and
therefore in the effluent for a completely mixed once-through system.
Therefore, the specific growth rate is related only to the hydraulic
control of the reactor. Rearranging Equation (5) results in:
(6)
The change of the substrate concentration can be written into the mass
balance:
. D-S1 - D-S - u() = 0 (7)
Si is the influent substrate concentration. By rearranging equation 7,
one obtains
x = Y(Si - S) (8)
19
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Equations 6 and 8 can be used to calculate the steady state concentra-
tions of biological solids and substrate for any dilution rate if the
growth parameters, ym, Ks, and Y are available and were evaluated
accurately.
In the evaluation of y, the substrate concentration in Equation 1 has
been expressed as the initial substrate concentration in a batch reactor
(So) or the steady state substrate concentration (S) in a completely
mixed continuous flow reactor (2). Thus, urn and Ks can be evaluated by
either batch or completely mixed continuous flow reactor data. The
evaluation of these two parameters for the aerobic treatment of poultry
waste will be presented in the results section.
Knowledge of the yield coefficient is important in Equations 3 and 8.
The yield coefficient is not necessarily a true constant either for a
pure or a heterogeneous microbial population (23-25). As an example,
the cell yield from heterogeneous microbial populations of sewage origin
which were acclimated to glucose, ranged from 36 to 88% in batch culture,
and 32 to 69% in continuous culture (26). The variability in cell yield
was explained as due to the ecological variation inherent in a hetero-
geneous population. A range rather than a single yield constant may be
more appropriate in the design and operation of biological waste treat-
ment systems. Such is likely to be the case for the treatment of animal
wastes.
Modifications of the Monod equations have been suggested. Chiu et al.
(27) (28) indicated that an endogenous respiration term must be added
to the Monod model, and the growth parameter must be obtained from low
and high dilution rates. The logic was that these values will exhibit
a reasonable range of values rather than a single value. Grady et al.
(29) concluded that the effluent concentration should not be considered
independent of the influent substrate concentration when heterogeneous
cultures are used regardless of the techniques employed to measure the
concentration of growth-11mi ting substrate. They suggested the use of
regression equations to describe the interactions among influent COD,
growth rate, and effluent COD at low growth rate conditions.
McKinney
Conventional waste treatment systems operate in the declining growth
phase and microbial growth is controlled by the rate of addition cf
food. The rate of microbial growth is controlled by the concentration
of unmetabolized food remaining. Recognizing this condition, a number
of equations can be developed (7-9):
20
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where dMs/dt = rate of synthesis of microorganisms
F = concentration of unmetabolized food
K = growth rate constant
In addition,
dMs _ _ dF
-
where Ks = synthesis constant
Therefore
The removal of organic matter is related to the residual organic matter
when the system operates in the declining growth phase.
In a completely mixed continuous flow system, the food removal equation
is defined as:
Km-t
where F = the substrate concentration remaining unmetabolized
Fi = substrate concentration in influent
t = aeration time based on raw waste flow
Km = metabolism factor, temperature dependent
The mixed liquor suspended solids (MLSS) can be separated into four
basic parts: the active mass (Ma); the endogenous mass (Me); the inert
non-biodegradable organic suspended solids (Mi); and the inert, inorganic
suspended solids (Mii). In a completely mixed aeration system (CMAS),
the active mass, Ma, is related to the food metabolized, the length of
aeration time of the sludge, and the rate of endogenous respiration:
21
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Ma =
KsF
1/ts + Ke
(13)
where ts = sludge aeration time
Ke = endogenous respiration factor
The endogenous mass can be related to the active mass in the CMAS system:
Me = 0.2-Ke-Ma-ts
(14)
Obviously Km, Ks, and Ke are key factors in these equations. These
values were summarized by Burkhead (30) (Table 1) and are based on the
treatment of domestic sewage at 20°C.
Table 1. CONSTANTS SUGGESTED FOR USE IN THE DESIGN
FOR THE TREATMENT OF DOMESTIC WASTES
CMAS
constant
Mathematical
definition
Physical
significance
Values
Km
Metabolism
constant
Fi - F
F-t
Food removal rate
15.0
hour
Ks
Synthesis
constant
K-Km
Rate of food
converted into
microbial cells
10.4
hour
Ke
Endogenous
Constant
Mv - 0-2-Ks-T-ts
endogenous solids 0.02
build up rate hour
22
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Mv is the volatile mass in the system, i.e., Ma + Me + Mi. The inert,
non-biodegradable organic suspended solids can be obtained by:
Mi - (Mi1nf)(ts/t) (15)
where Mi = inert, non-biodegradable organic suspended solids in
the reactor
= inert, non-biodegradable organic suspended solids in
influent
ts = sludge retention time
t = raw waste aeration time
The inert, inorganic suspended solids can be determined by:
Mi
i = (Miiinf)(ts/t) + 0.1(Ma + Me) (16)
where Mii = inert, inorganic suspended solids
Mii. - = inert, inorganic suspended solids in influent; ash
fraction of influent suspended solids
The oxygen uptake rate can be described as:
dO 1.5(Fi - F) 1.42(Ma + Me)
at" t -- is
where dO/dt = oxygen uptake rate
The effluent BOD can be expressed as:
BODeff = F+ K.Maeff (18)
23
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where BODeff = BOD5 in
Ma ff = oxygen demanding microbial mass in effluent
K = BOD5 factor, 0.8, a constant since the BOD test is
always at 20°C
CMAS systems are stable, easy to operate, and capable of producing a
high quality effluent consistent with normal variations in organic and
hydraulic loadings. Design of CMAS systems can be accomplished by
Equations 12-18.
Many studies have been conducted with simple substrates such as glucose
or acetate. However, insoluble and particulate contaminants are con-
tained in most wastewaters and must be taken into account when the
constants of these equations are evaluated. This is especially true
with animal wastes and wastewaters.
Eckenfelder
Additional relationships have been developed (3, 5, 6, 31, 32) to describe
aerobic biological systems. In a completely mixed, continuous flow system,
the substrate removal relationship can be defined as:
where So = influent substrate concentration
Se = aeration basin and system effluent substrate concentration
Xv = mixed liquor volatile suspended solids
t = liquid retention time in aeration basin
K = substrate removal rate
The factors which affect the value of K include the temperature, waste
characteristics, volatile material stripped from the waste, and the
turbulence level in the system. Volatile suspended solids or other
appropriate measures of microbial active mass must be considered instead
of total suspended solids when K,is evaluated.
Volatile sludge accumulation can be defined as:
AXvV = a-Sr-Q - b-x-Xv-V (20)
24
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where AXv = volatile suspended solids accumulation
V = volume of aeration basin
a = mass yield rate or yield coefficient, BOD,- basis
Sr = SO - Se = substrate removed
Q = influent flow rate
b = endogenous respiration rate coefficient
x = biodegradable fraction of volatile suspended solids
Xv = mixed liquor volatile suspended solids
and AXv 1 /71\
xXv SRT v '
where SRT is the sludge retention time or sludge age. When the system
is operated as a once-through system,
SRT = t = - (22)
where t = liquid retention time and D = dilution rate.
These equations must be used with an understanding of the way they were
developed and the constraints in their use:
-"b" should be applied only to the degradable portion of the volatile
suspended solids
-"x" can be related to sludge age and F/M ratio
-when the influent waste contains degradable volatile suspended solids,
"x" should be experimentally determined instead of calculated
-the yield coefficient, "a" must be defined as related to BOD, COD, TOC,
or other parameters describing the organic substrate
-the yield coefficient, "a" generally is determined without including
the influent volatile suspended solids in the wastewater. If these
solids were included, the reported values of "a" will be different and
the inclusion of the solids should be noted in the determination of "a"
-when the endogenous respiration coefficient "b" is determined with
volatile suspended solids present in the influent wastewater, the
value of "b" must include both the breakdown and synthesis of the
volatile suspended solids in the wastewater and the degradation of the
biomass
25
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-the value of "b" will be influenced by turbulence, dissolved oxygen level
and temperature.
In a completely mixed, continuous flow system, the basic equation of
oxygen demand is
Rr-V = a'-Sr-Q + b'-x-Xv-V (23)
where Rr = oxygen uptake rate
a1 = synthesis oxygen demand rate, BODg basis
b1 = endogenous respiration oxygen demand rate
The range of values of a1 is between 0.4 and 0.9 for several wastewaters,
Nitrification will result in a larger value of a1.
In a completely mixed system, if only the carbonaceous effluent BOD is
of concern, the effluent BOD can be described as:
BOD5e = Se + fo-Xve (24)
where BOD5e = effluent BOD,, concentration
fo = BODg equivalence of effluent volatile suspended solids
Xve = effluent volatile suspended solids concentration
t
The BOD contributed by the effluent suspended sol Ids can be related to
sludge age and the type of suspended solids present in the effluent.
Comparison
The mathematical models proposed by McKinney and Eckenfelder have been
examined by Goodman and Englande (31). They concluded that for prac-
tical purposes these two models are identical.
A review of available mathematical models to describe biological treat-
ment systems (33) suggested that the Monod model is more suitable for
26
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the design of biological waste treatment process than those proposed by
Eckenfelder and McKinney. The application of these concepts to animal
wastewaters will.,be discussed in this report.
Summary
There are merits in all of the reviewed design approaches. Somewhat
different assumptions underlie the development and use of each approach.
Some of the major differences inherent in the application of the
approaches to animal wastes are: a) the large amount of non-biodegradable
material in the untreated waste, b) the significant amount of biodegra-
dable solids in the waste which will undergo stabilization in a treat-
ment process, and c) the high concentration of oxygen demanding nitrogen
compounds in the wastes. Animal wastes are not the simple soluble sub-
strates around which many theoretical design approaches have been
developed.
The design approaches developed in this study will incorporate the
following:
-The soluble and insoluble part of animal waste will be considered
separately when the design parameters are evaluated.
-Time dependence of the non-degradable influent solids or COD degradation
and the endogenous respiration rate of biomass will be considered.
-The total COD in the effluent, i.e., the soluble COD, the COD equivalent
of biomass, the non-degradable1 and undegraded insoluble COD, and the COD
for nitrite oxidation will be determined.
-Oxygen requirements will include the oxidation of soluble and Insoluble
substrate, micrqbial mass, NH4-N, and N02-N.
Conventional Aerobic Treatment of Animal Wastes
The possible biological treatment processes for agricultural wastes have
been summarized (34). They included oxidation ponds., aerated lagoons,
oxidation ditches, anaerobic lagoons, anaerobic digesters, composting,
and land disposal.
The land will be the ultimate disposal site for treated or untreated
animal wastes. The degree of treatment needed prior to land disposal
will be related to the degree of needed odor control or waste stabili-
zation or nutrient control. Current aerobic treatment processes for
animal wastes are long term aeration systems such as oxidation ditches
or aerated lagoons. Present design parameters for these processes as
animal waste treatment units are based on an organic loading rate to
27
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the reactor volume, or the number of animals per reactor volume, or
reactor detention time. Oxygenation capacity has been estimated as
twice the BOD,- loading to the reactor.
Basic microbial growth rates, substrate removal rates, microbial oxygen
demand rates, or oxidation of ammonia or nitrite have not been considered
explicitly in available design parameters. The present study has been
conducted to incorporate more of these fundamental parameters into the
design of aerobic animal waste treatment systems.
MATERIALS AND METHODS
A._ Batch Studies
Removal Kinetics Study -
The organic wastes used in this phase were obtained from poultry pro-
duction units at Cornell University. The one or two-day old poultry
manure was blended in a Waring blender for two minutes at low speed
with tap water. Approximately 80 grams of manure was added to one liter
of tap water. The blended mixture was filtered through a single layer
of cheesecloth to remove the feathers and the large particulate matter.
This filtered mixture was.diluted with tap water to achieve the concen-
tration needed for a given experiment. Where settled wastewater was
desired, some of the filtered mixtures were settled for 30 minutes
before the supernatant was decanted for use.
Two or 2.5 liters of the diluted mixtures were added to 5 liter batch
study containers, aerated with humidified air, and a high level of
dissolved oxygen maintained. A sketch of the apparatus is shown in
Figure 2. The loss of any water due to evaporation was made up by
adding distilled water.
Before sampling, the container was shaken by hand to assure complete
mixing and homogeneous mixed liquor samples. Because of the large
amount of particulate matter in the mixed liquor, a broken-tip-pipette
was used for sampling.
The COD of the total mixed liquor, the filtrate or soluble COD, the
suspended solids concentration, the pH and the oxygen uptake rates were
measured during tHe aeration period. For the determination of soluble
COD, filtrates were obtained by filtering the samples through a 0.45y
filter paper. All the batch experiments were conducted at room tempera-
ture (23° ± 2°C).
Initial Suspended Solids Concentration Study -
The mixed liquor taken from the poultry manure oxidation ditch of the Agri-
cultural Waste Management Laboratory at Cornell University was diluted with
28
-------
AIR
AIR FLOW METER
SATURATED
WATER
AIR OIFFUSER
BATCH UNITS
\r
REACTOR
MIXED
LIQUOR
AIR DIFFUSER
CONSTANT TEMP 1
(4°C) WATER BATH
AIR-f
^MIXER
r^
BOTTLE
\
AIR DIFFUSER
MIXED LIQUOR
EFFLUENT
COLLECTION
BOTTLE
CONTINUOUS FLOW UNITS
Figure 2. Schematic of the experimental apparatus for
laboratory aeration studies.
29
-------
distilled water to the desired suspended solids concentration. Two liters
of these diluted suspensions were added to a 5 liter container. An
additional 1 liter of filtered, settled poultry manure mixture, prepared
as described earlier, was added to each container. After the addition,
the combined mixture was aerated using humidified air. Samples were
taken for the analysis of COD and suspended solids concentration. Oxygen
uptake rates and pH were measured directly in the containers.
Kinetic Constants
For this phase of the study the settled poultry manure was centrifuged
at 5000 rpm for 10 minutes. The filtrate was passed through a 0.45y
membrane filter, collected and diluted to obtain different concentra-
tions. The filtrate was used as the substrate for these experiments.
The batch apparatus shown in Figure 2 was used.
!>. Continuous Flow Studies
Bench Scale Study -
^^fc^^^" ^~~ ^^^^j^^ _ ^
The bench scale completely mixed continuous flow units employed in the
study are shown in Figure 2. In this study no recycle of solids was
provided. The laboratory units were located in a 20°C constant tempera-
ture walk-in chamber. Settled poultry manure was prepared as described
earlier and used as feed.
During operation of the units, the feed flow rate was varied to study
the effect of detention time on the COD and solids removal efficiency,
and on the oxygen uptake rate. Every day or two, the feed was changed,
the feed line was cleaned, and samples were taken for analysis.
Pilot Plant Study -
The oxidation ditch at the Agricultural Waste Management Laboratory
receives the wastes from about 250 birds. The mixed liquor 1n the
ditch is mixed and aerated by a cage rotor. The concentration of
mixed liquor solids in the ditch was controlled by varying the water
input and output. Thus different periods of equilibrium at varying
mixed liquor solids concentration were obtained. The total and vola-
tile solids, COD, pH, and oxygen uptake rate during these equilibrium
periods were measured and used for the evaluation of the operational
parameters. The temperature varied from 12°C in the winter to 25°C in
the summer.
C.. Analytical Methods
Suspended solids concentrations were determined by the membrane filter
techniques as outlined in Standard Methods (35). The suspended solids
30
-------
contained an unknown fraction of dissolved solids. Total volatile solids
and volatile suspended solids were determined as described in Standard
Methods. The COD of the samples was determined by using the rapid method
(36).the pH of the sample was measured with a Corning pH meter. Dis-
solved oxygen measurements were obtained by a galvanic cell oxygen analy-
zer (Precision Scientific Co.) for the laboratory units and by a YSI
Oxygen Meter (Model 54) at the oxidation ditch.
RESULTS
Batch Studies
Removal Kinetics -
Project personnel hypothesized that degradation of liquid poultry waste
was a sequential removal process in which both the soluble and insoluble
waste components undergo different rates of degradation. The overall
removal mechanism may be described as the rapid microbial metabolism of
the soluble substrate followed by the subsequent aerobic stabilization
of the synthesized biomass and the original, degradable organic solids
present in the waste.
Since the poultry waste contained bacteria which were capable of metabo-
lizing the wastes, no inoculum was needed. The study on the removal
characteristics of COD and suspended solids was conducted by preparing
the different poultry waste suspensions and conducting batch aeration
studies. Three units were initially loaded with unsettled suspensions
of 5, 10, and 50 grams of poultry manure per liter. Three other units
were initially loaded with settled suspensions of 20, 40, and 60 grams
of poultry manure per liter. Figure 3 illustrates results typical of
the unsettled suspensions and Figure 4 indicates typical results of
the settled suspensions.
The removal pattern shown in these Figures can be approximated by first
order kinetics. For the settled poultry manure data, the growth of
microbial solids can be noted within the first two days of aeration.
Such an increase was not observed with the unsettled manure suspensions.
The unsettled suspensions contained a greater amount of solids than what
their corresponding settled suspensions would have contained, and this
higher amount of solids in conjunction with the error involved in the
determination of suspended solids may have masked the actual increase in
microbial solids that occurred.
The ratio of soluble COD removed to total COD removed for these six
batch experiments averaged 0.389. Therefore about 39% of the total
removal of the organics contained in these wastes was due to the
degradable, soluble COD in the waste and about 61% was due to the
degradable particulate material in these wastes.
31
-------
o»
E
O
O
1600
1400
1200
1000
BATCH UNIT
10g/1 UNSETTLED
POULTRY MANURE SUSPENSION
SUSPENDED SOLIDS
O 800
(O
600
MIXED LIQUOR
COD
A A
400
200
FILTRATE COD
I I I I
4 8 12 16 20 24
AERATION TIME, days
Figure 3. General removal characteristics (solids and COD)
of unsettled poultry manure suspension.
32
-------
3200
2800
BATCH UNIT
60 g/l SETTLED
POULTRY MANURE SUSPENSION
SUSPENDED
SOLIDS
MIXED LIQUOR
COD
4 8 12 16
AERATION TIME, days
Figure 4. General removal characteristics (solids and COD)
of settled poultry manure suspension.
33
-------
A residue of mixed liquor COD, soluble COD, and suspended solids occurred,
The biodegradability of this residue 1s unknown, but is assumed to be
minimal.
The COD and solids removals have been approximated as an apparent first
order reaction. With this assumption, the removal constants were
determined with and without considering the non-biodegradable material
in the units. Without considering the non-biodegradable materials, the
following relationships describe the change or removal in total and
filtrate COD and suspended solids.
In f£= -Kt (25)
In = -K't (26)
In = -K"t (27)
where So = mixed liquor COD at time zero
St = mixed liquor COD at time t
F = filtrate COD
X = suspended solids concentration
K = rate constant for removal
K1 = rate constant for degradation
K1' = rate constant for oxidation
Close analysis does not completely support the assumption of a first
order reaction, When the data is plotted on sem1-logr1thm1c paper,
more than one removal rate becomes obvious (Figures 5 and 6). Two or
more removal rates occur 1n the long term aerobic treatment of poultry
manure. The different rates are due to the differences in degradablHty
of the waste components.
If the non-biodegradable material in the units 1s considered, another
set of equations results. The COD and suspended sol Ids never become
zero, but equilibrate to a specific residual level. The difference
between the concentration of the Initial COD or'sol Ids and the residue
represents the biodegradable material. Removal kinetics should be based
on the biodegradable fraction, I.e.,
34
-------
1.0
-------
oo
BATCH UNIT
40g/l SETTLED
POULTRY MANURE SUSPENSION
8 12 16
AERATION TIME, days
20
24
Figure 6. Semi-logarithmic plot of soluble COD removal.
-------
In St - Si = Kn (28)
In = Ki't (29)
(30)
where Si = total COD
Fi = soluble COD
Xi = suspended solids
The values of these residues were determined from graphs such as those in
Figures 3 and 4. When the residues are considered, an apparent simple
logrithmic removal relationship resulted (Figure 7).
The effect of considering the residue in evaluating substrate removal kine-
tics is illustrated in Table 2. The removal rates calculated when the resi-
due was considered were higher than when the residue was not considered.
In addition, the total COD removal rates of the settled suspensions were i
larger than those of the unsettled suspensions. The unsettled sus- ;
pensions contained particulate matter that may have degraded at a
slower rate thus lowering the overall COD removal rate. The settled
suspensions contained a larger amount of soluble COD per unit of sus-
pended solids (Table 2). Soluble and readily available material is more
easily degraded than the particulate matter that is not amenable for
easy degradation. Therefore substrate removal kinetics for the treatment
of poultry manure should consider the residue that will result after
extensive treatment and stabilization. Rate constants developed from
soluble substrate studies are not directly applicable to wastes such as
poultry manure which contains particulate matter that undergoes decompo-
sition slowly. Consideration of both the soluble and particulate fractions
of poultry manure is necessary in the design of aerobic treatment systems
for these wastes.
The initial ratio of COD to suspended solids was useful in explaining
differences in the removal rates of settled and unsettled manure sus-
pensions. However, the parameter used for design of aerobic units should
be expressed as the ratio of oxygen demanding material in the influent
waste to the microorganisms in the reactor. Practically this is expressed
as the F/M ratio or in these experiments, the total #COD/#suspended solids,
or gm total COD/gm suspended solids.
37
-------
u>
00
BATCH UNIT 40 g/l SETTLED
POULTRY MANURE SUSPENSION
0.04
X
I
X
I
o
_J
o
o
IU
o
UJ
Q_
(O
1.0
0.8
0.6
0.4
0.2
I
O.I
O.08
0.06
0.04
I
8 12 0 4
AERATION TIME , days
8
12 14
Figure 7. Removal characteristics of total COD and suspended
solids with consideration of the residues.
-------
Table 2. COMPARISON OF TOTAL COD REMOVAL RATE CONSTANTS
CO
to
Type of
poultry manure
suspension
Settled
Settled
Settled
Unsettled
Unsettled
Unsettled
Initial Total COD
mg/1
2100
4080
3170
1210
1530
11460
Initial Soluble COD
Initial Suspended Solids
0.46
0.39
0.50
0.35
0.28
0.29
K (day"1)
0.327
0.233
0.184
0.156
0.115
0.116
Ki (day"1)
0.560
0.370
0.392
0.274
0.215
0.206
K = removal rate without consideration of residue
Ki = removal rate with consideration of residue
-------
To investigate the effect of the above loading rate on the removal of COD
and influent solids, a series of batch experiments were conducted with
different initial loading rates. Mixed liquor from the pilot plant oxida-
tion ditch was used to assure adequate acclimated organisms and settled
poultry manure was used as the waste. The influence of the loading rates
on the COD and suspended solids removal rates are noted in Figures 8 and 9.
Only the removal rates for the first two phases are noted because rates
of subsequent phases, if any, were considered insignificant. The removal
rate of total COD and suspended solids increased with an increase in the
initial organic loading rate. The removal rate of filtrate COD decreased
with an increase in loading rate.
Constants for the Monod Equations -
The soluble, degradable portion of poultry manure suspensions is the
immediately available substrate for microbial growth. Growth patterns
and kinetic constants can be developed using the soluble fraction of
these wastes. The constants can be helpful in the design of biological
treatment units to obtain desired effluent characteristics.
Poultry manure suspensions were centrifuged and filtered to provide the
substrate for these series of experiments. Mixed liquor from a labora-
tory continuous flow unit treating poultry wastes was used to provide
adequate organisms. Batch experiments were conducted, the microbial
growth pattern was determined, and the Monod growth kinetic constants
(Y, ym, Ks) were obtained. In these experiments the initial filtrate
COD concentrations were 135, 225, 458, and 1565 mg/1. Typical results
are noted in Figure 10.
When the suspended solids were plotted on semilogrithmic paper (Figure
11), the growth rate constants V were determined at the different
initial substrate concentrations. Only data for the initial microbial
growth period was used for the determination of "y".
A plot of the growth rates versus initial substrate concentration indi-
cated a hyperbolic relationship. A "Lineweaver-Burk" plot of these
parameters provided a straight line (Figure 12) that was used to deter-
mine "ym" and "Ks" as shown. The yield constant "Y" was evaluated by the
relationship between the change in suspended solids per unit change in
filtrate COD during the microbial growth period (Figure 13).
Thus for the soluble COD in poultry manure wastewater, as identified by
the centrifuged and filtered fraction, the maximum microbial growth
rate, "ym", was 0.35/hour, the "Ks" value was 895 mg/1, and the yield
constant, "Y" was 0.41 milligram of suspended solids increase per
milligram of COD removed.
40
-------
0.5
I 0.4
UJ
H
(T
0.3
O
O
u
O.I
FIRST PHASE
REMOVAL
SECOND PHASE
REMOVAL
I
I
I
0.4 0.8 1.2 1.6 2.0 2.4
INITIAL TOTAL COD OF FEED, mg/l
INITIAL REACTOR SUSPENDED SOLIDS, mg/l
2.8
Figure 8. Relationship between total COD removal rate and
total COD loading.
41
-------
0.5
. 0.4
UJ
tr
0.3
UJ
(T
O
O
O
i
0.2
O.I
FIRST PHASE
REMOVAL
SECOND PHASE
REMOVAL
1
0 0.2 0.4 0.6 0.8 1.0
INITIAL FILTRATE COD OFFEED,mg/l
INITIAL REACTOR SUSPENDED SOLIDS,mg/l
Figure 9. Relationships between filtrate COD removal rate
and filtrate COD loading
42
-------
2000
BATCH STUDY
CENTRIFUGED AND FILTERED
POULTRY WASTE SUSPENSION
MIXED LIQUOR COD
FILTRATE COD
SUSPENDED
SOLIDS
40 80 120 160 200
AERATION PERIOD, hours
240
Figure 10. Removal characteristics of soluble poultry
waste suspension
43
-------
BATCH STUDY
CENTRIFUGED AND FILTERED
POULTRY WASTE SUSPENSIONS
300
200
N.
O»
CO
g
_j
o
to
o
UJ
o
z
UJ
0.
CO
3
(O
100
80
60
40
INITIAL FILTRATE
COD(mg/l)
458
225
8 12 16
AERATION TIME , hours
20
Figure 11. Graphical estimation of different specific growth
rates by using different initial filtrate COD
-------
O
s
H*.
Ks =895 mg/l
2000 4000
j [SUBSTRATE CONCENTRATION]
Figure 12. Graphical estimation of Monod kinetic constants.
45
-------
0>
uT
o
600
500
400
O
0 300
O
CO
S 200
O
z
u
I 100
CO
YIELD
ASS
200 400 600 800 1000
FILTRATE COD CHANGE , mg/l
1200
Figure 13. Graphical estimation of the microbial yield
value.
46
-------
Oxygen Demand -
The metabolism of the organic waste creates an oxygen demand which
must be met by an aeration device in aerobic treatment. The oxygen
demand is related to the loading rate of a unit. The oxygen uptake
rates, in terms of mg/1/hour and mg/gram suspended solids/hour, were
determined for the batch experiments described earlier. The variation
in these uptake rates as a function of aeration time are shown in
Figure 14. The greatest oxygen demand in terms of mg/1/hour occurred
immediately after the units were fed. The uptake rate in terms of
mg/gSS/hour was the greatest in the most heavily loaded unit. The
maximum demand rate per unit solids occurred several hours after the
units were started.
After the solids became stabilized, i.e., after about 16 hours of
aeration the oxygen demand was in the range of 1.0 to 6.0 mg of oxygen/
gram suspended solids/hour and in the range of 8-14 mg/1/hour. These"
rates are similar to those reported during the aerobic stabilization
of primary and secondary sewage sludges. These residual oxygen demand
rates are related to the.endogenous demand of the microorganisms while
the earlier higher demand rates were due to the synthesis of the micro-
organisms and the rapid uptake of the soluble matter.
Thus aerobic treatment units with short detention times will have high
oxygen demand rates. If the oxygen supply is inadequate to meet the
demand, aerobic conditions will not be obtained. Biological units
treating animal wastes generally have long liquid detention times due
to the low waste volume. Under these conditions, oxygen demand rates
will be low provided the combination of degradable waste is low. The
oxygen demand is also related to the loading rate of the treatment unit.
Continuous Flow Studies
General -
Batch studies are useful'in determining the general patterns of sub-
strate removal for specific wastes. However, practical waste treatment
systems are continuous flow processes. Patterns and removal relation-
ships developed from batch studies should be compared with results of
continuous flow studies to evaluate their applicability. Two types of
continuous flow units were used in this phase of the studylaboratory
units and a pilot plant oxidation ditch.
Laboratory -
The laboratory unit was fed settled poultry manure to avoid clogging
of feed lines and unnecessary variations in the influent waste param-
eters. After 38 days of operation, the pH in the reactor started
47
-------
INITIAL
TOTAL COD
INITIAL
SS
INITIAL
FILT COD
INITIAL
SS
INITIAL
SS
1525
3075
7020
10 15 20 25
AERATION TIME, days
Figure 14. Oxyegen uptake rate related to aeration time.
48
-------
to decrease and the filtrate COD in the reactor increased. Obviously
the process of nitrification occurred in the system. To observe the
effect of increasing flow rate on the performance of the system and to
obtain more operational data, the mixed liquor of the original unit
was split into two units, subsequently called Unit I and II. The flow
rate to these units also was varied during the remainder of the study.
The general characteristics of the units are noted in Figure 15. The
loading rate of the units varied because of the change in flow rate and
had an effect on the removal efficiencies (Figure 16). The removal of
COD and suspended solids increased as the loading rate decreased.
The COD removal efficiency was calculated on the basis of total influent
COD and total mixed liquor COD leaving the unit. The COD removal efficien-
cies would have been greater had the filtrate COD values been used since
most of the COD in the mixed liquor was due to the solids fraction
rather than the soluble fraction. In a long detention time treatment
system, the influent soluble COD has been converted into microbial cell
mass.
Filtrate COD was not used to estimate removal efficiencies since the
filtrate contained nitrite and the COD values of the filtrate would
have included the oxidation of the carbonaceous matter and the nitrite.
Because of the small amount of carbonaceous matter, the inclusion of
nitrite oxidation would introduce erroneous, or at least non-comparable
results since the influent COD did not contain nitrites. Although
the mixed liquor also included the nitrites, the COD of the solids
fraction was large and including the nitrite did not introduce a sig-
nificant error.
The relationships between the organic loading rate to the units and the
oxygen uptake rates are noted in Figure 17. The uptake rate, in terms of
mg/l/hr, increased rapidly as the loading rate increased. At the lower
loading rates, the oxygen uptake rate was essentially that due to solids
degradation. When the uptake rate per unit suspended solids was com-
pared to the loading rate, a straight line relationship occurred. The
higher loading rates increased the solids concentration which resulted
in the linear relationship. The oxygen uptake rates obtained in this
continuous flow study are comparable to those obtained in the batch
study experiments.
Pilot Plant -
The details of tha pilot plant oxidation ditch are outlined in this report
and have been published elsewhere (37). During this portion of the study,
the oxidation di uch was operated at various solids levels to evaluate the
49
-------
10
10
O
en
o
8
CO
9 6
O
CO
UJ
UJ
Q_
(O
^
CO
Q"
o
o
FEED SS
FILTERED
FEED COD
MIXED LIQUOR pH
FILTERED ML COD
8
7
6
0
10
20
30
40
50
DAYS
60
70
80
90
100
Figure 15. Operational parameters of laboratory conti
flow units - unit I.
nuous
-------
80
I-
u
70
60
50
S 40
(E
LJ
e>
<
tr 30
Id
20
10
TOTAL SOLUBLE COD
TOTAL SOLUBLE COD
CORRECTED FOR NITRITE 60D
MIXED LIQUOR COD
'SUSPENDED SOLIDS
I I
0.01 0.02 0.03 0.04
TOTAL COD LOADING RATE
COD.gms / MLSS,gm /hr.
Figure 16. COD and suspended solids reduction as related
to total COD loading rate.
fil
-------
UJ
CL ±
10
z co
UJ CO
8
6
^^ C^ 4
o o»
ll O
^^^ » ^"
O Ld
UJ h- A
Q. < 0
CO CE
RESULTS OF THE
LABORATORY STUDIES
y«3.75+!9lx
> 16
- 12
UJ
-------
magnitude and characteristics of the overflow, the oxygen transfer charac-
teristics, nitrification, and the removal efficiency of the total COD and
total solids. The solids concentration in the ditch was controlled by an
automatic overflow and water addition.
Equilibrium conditions occurred at each solids level. The mixed liquor
characteristics during these periods were used to evaluate operational
parameters and removal efficiencies. Typical patterns during such
periods, are shown in Figure 18. The average and range of characteristics
for all the equilibrium periods are noted in Table 3.
The effect of the hydraulic retention time at the noted flow rates on
performance efficiency is illustrated in Figure 19. The removal of
all parameters increased as the liquid detention time increased.
General Design Equations
General -
In the previous section describing the batch studies, the COD and sus-
pended solids removal could be approximated by a first order reaction
if the solids and COD residue of the studies were considered. The
solids fraction contributed the largest amount of the total COD.
A completely mixed reactor without recycle, such as the continuous
laboratory and pilot plant oxidation systems can be described by the
sketch in Figure 20. At steady state equilibrium conditions, mass
balance equations can be used to evaluate the removal constants, or if
removal constants are known or assumed, to determine effluent
characteristics.
For total COD, the equation becomes:
F-Si-At = F-S"-At + K-S"-V-At (31)
where At = aeration time in days for the period under consideration
K = total COD removal rate, day"
This equation can be rearranged to solve for either the effluent total
COD concentration or the removal constant depending what is desired
and known, i.e.:
53
-------
30,000
25,000
20,000
. 15.OOO
o:
UJ
I-
LJ
2
< 10,000
tr
5,000
TOTAL SOLIDS
TOTAL VOLATILE
SOLIDS
I I I I I I I I
15 20 25 31
* MARCH
10 15 20 25
-APRIL »
1973
Figure 18. General operational characteristics of COD
and solids in the oxidation ditch.
54
-------
Table 3. PILOT PLANT OXIDATION DITCH CHARACTERISTICS DATA DURING EQUILIBRIUM PERIODS
Date
(1972)
Water flow Mixed liquor COD
rate (mg/1)
(liters/day) ave. range
Total solids
(mg/1)
ave. range
Total volatile solids
(mg/1)
ave. range
CJI
Ul
3/14 to 5/2
5/9 to 6/23
6/27 to 7/11
7/18 to 7/25
7/28 to 8/29
208.2
151.4
104.1
66.2
94.6
18,900 13,900 - 25,400 17,900 - 17,700 15,700 -
25,600 30,700 20,000
26,000 23,500 - 33,400 30,500 - 21,800 20,100 -
30,600 36,700 23,300
27,600 23,600 - 38,400 36,900 - 23,900 22,400 -
31,200 39,300 24,200
29,200 28,100 - 41,500 40,400 - 24,300 24,100 -
29,900 43,100 24,800
28,600 26,900 - 42,400 41,200 - 25,300 24,000 -
30,400 43,900 26,500
-------
80
O
o
UJ
(C
o
o
o
o
60
40
20
MIXED LIQUOR COO
TOTAL VOLATILE
SOLIDS
TOTAL SOLIDS
I
1
0 20 40 60 80 100
HYDRAULIC RETENTION TIME, days
Figure 19. Effect of hydraulic retention time on the
COD and solids reduction - oxidation ditch,
56
-------
Si.Xi.F
F,X,S
in
Si = TOTAL COD IN THE INFLUENT, mg/l
Xi = INFLUENT SUSPENDED SOLIDS, mg/l
F = FLOW RATE , I/day
V = REACTOR VOLUME , liters
X = REACTOR AND EFFLUENT SUSPENDED SOLIDS, mg/l
S" = TOTAL COD IN THE REACTOR AND EFFLUENT, mg/l .
Figure 20. Schematic of a completely mixed continuous
flow reactor without recycle.
-------
____
, . K-V 1 + K-t
i + p
where t is the hydraulic retention time of the system and
K = S1 " S (33)
S-t
Results from the previous laboratory project (38) and from the labora-
tory studies in this project phase permit "K" to be evaluated from
Equation 33 and to be related to the organic loading of the units in
terms of gms COD/day/gms mixed liquor volatile suspended solids. The
relationship is shown in Figure 21. An equation of the form
K = 0.017 + 0.11X (34)
appeared to fit the parameters with a correlation coefficient of 0.976.
The value of the intercept (0.017) can be interpreted as an estimate
of the COD autooxidation rate of the mixed liquor solids.
Loading rates up to 1.1 gms COD/day/gms MLVSS were evaluated. The data were
obtained from two studies conducted at an interval of two years apart.
The correlation coefficient of 0.976 indicated that the equation relating
the two parameters adequately explains their interaction. Thus Equation
32 should be able to be used to predict the total COD removal efficiency
or in the effluent of a system treating poultry wastes.
In the same manner a comparable equation can be developed from a mass
balance on solids at equilibrium conditions:
(35)
where K1 is the removal coefficient of suspended solids and
58
-------
o
o
ill
UJ
oc
o
o
o
Or
O
3
O
O
UJ
X
I
I
0.14
0.12
0.10
O.OS
0.06
0.04
0.02
RESULTS FROM LABORATORY
STUDIES AT 20° C
« PREVIOUS STUDY
A THIS STUDY
L
1
0 0.2 0.4 0.6 08 1.0
X-LOADING RATE, MLCOD,gms/doy/MLVSS,gms
Figure 21. Rate of mixed liquor COD removal as related
to COD loading rate.
59
-------
(36)
With appropriate parameters known, either the effluent solids concen-
tration or the removal constant K1 can be determined.
The relationship between K1 and the organic loading rate, X1, was
evaluated (Figure 22). An equation of the form
K1 = 0.011 + OJ5.X1 (37)
appeared to fit with a correlation coefficient of 0.76. In this equation,
X' refers to the loading rate, gms of total COD/day/gm of MLVSS. The value
of the intercept again can be interpreted as an estimate of the auto-
oxidation rate of the mixed liquor solids, this time in terms of solids
rather than COD degradation rate.
These relationships which were developed under laboratory conditions
(Figures 21 and 22) were applied to the pilot plant oxidation ditch data
to determine their validity under practical situations. Table 4 indicates
the results of a comparison and suggests that the above relationships can
be applied to actual situations.
i
The relationship between the oxygen requirements and the organic loading
rate has been compared for the laboratory units (Figure 17) and the oxida-
tion ditch (Figure 23). The differences between the results obtained from
the laboratory and oxidation ditch data are due to the fact that different
substrates were used in each case. Settled poultry wastewater was used
in the laboratory studies and untreated poultry wastes were added directly
to the oxidation ditch. Different oxygen requirements would result from the
demand of the different substrates and the data are not directly comparable.
In addition, the loading rates in the two studies covered different ranges
and different measures of solids had to be used.
As expected, the oxygen requirements increased as the loading rate
increased. The requirements based on the oxidation ditch data were much
closer to the laboratory data on a per unit solids basis (mg Op/gram SS/hr)
than they were on a mg/l/hr basis. In the.practical situation, such as in
the oxidation ditch, the oxygen requirements ranged between 30-40 mg/l/hr
and between l-3mg Op/gram TVS/hr over a loading of up to 0.13 gms of total
COD/gm of MLVSS/day. These ranges provide an estimate of the oxygen
requirements likely to be experienced in field situations.
60
-------
0.16
1
UJ
CO >»
0.12
o
CO
O
LJ
O
z
u
CL
CO
13
CO
.0.08
UJ
0.04
RESULTS FROM LAB STUDIES
PREVIOUS DATA
THIS STUDY
I
I
0.2 0.4 0.6 0.8
X1-LOADING RATE,
total COD.gms /day /MLVSS.gm
Figure 22. Suspended solids removal rate as related
to COD loading rate
61
-------
ro
Table 4. APPLICATION OF DESIGN EQUATIONS FOR TOTAL COD AND SUSPENDED
SOLIDS TO RESULTS FROM THE PILOT PLANT OXIDATION DITCH
MLCOD In the effluent, mq/1
Date of Loading rate
equilibrium gms total COD/day/gm
period (1973) MLVSS est.
3/15 -
5/9 -
7/4 -
7/28 -
4/20
6/16
7/11
8/29
0.129
0.088
0.067
0.061
^6,300
21 ,580
25,040
26,270
meas.
17,560
25,540
25,240
28,800
estimated
measured
(*)
92.0
84.5
99.2
91.2
SS in
est.
12,770
17,200
20,760
22,080
the effluent, mq/1
meas.
11,950
16,290
19,190
20,980
estimated
measured
(%)
106.8
105.5
108.1
105.2
Conditions used for this estimation
a) 250 birds
b) TS = 2-SS
c) VSS = 0.75 SS (based on TVS = 0.75-T-S)
d) equations developed in the laboratory study were used to estimate the parameters
-------
u 1
S* 3
2
c
OXIDATION DITCH
RESULTS
O>
o e
t *
O UJ
UJH
Q. <
wo:
y*0.49-H4.8x
o>
E
uf 30
CCL
£ 20
CL
15
z 10
UJ
o
X
0 0
--" y.30.2.73*
~
1 1 1 1
0 0.04 0.08 0.12 0.16
LOADING RATE , #
total COD,qms/day/MLVSS,gm
* based on the assumptions noted in Table 4.
Figure 23. Oxygen uptake rate as related to COD
loading rate.
63
-------
The above mass balance equations provide an opportunity to determine
removal constants, effluent characteristics, and oxygen demand for the
aerobic treatment of poultry manure. In the following sections, the
results of the laboratory and pilot plant experiments will be used to
compare, other approaches developed by Monod, McKinney, and Eckenfelder
to design aerobic waste treatment systems.
Monod -
The growth of microorganisms during the metabolism of the soluble
fraction of poultry manure suspensions has been found to follow kinetic
relationships developed by Monod. Therefore the soluble part of the
substrate and the microbial solids concentration in effluent of a com-
pletely mixed, continuous flow reactor can be estimated by using Equations
4-8 presented earlier in this report.
- KS'D
-
= Y(Sin - S^) (39)
where S^ = degradable soluble COD in the effluent, mg/1
Ks = saturation constant, mg/1
ym = maximum growth rate, hr"
D = dilution rate, hr" ; (hydraulic detention time)"
X.|.| = biomass concentration in the effluent, mg/1
Y = yield constant
Si-j-j = degradable soluble influent COD
The change in the total COD (S") in the reactor can be expressed as
follows using the system described in Figure 20:
Change of total COD in the reactor = input of total COD - output of total COD
-Change of degradable, soluble COD in the reactor for energy and synthesis
of microbial mass - change of degradable, insoluble COD in the reactor for
energy and synthesis of microbial mass - overall autooxidation of total
COD in the reactor, (i.e., oxidation of microbial mass and degradable
influent organic solids when organic loading is zero)
64
-------
i.e.
jc" _ -M 91
V.Sj| = F-S1 - F-S - -gli V - -jfl V - Kd-S-V (40)
where S,, = degradable soluble COD in the reactor or effluent
Sgi = degradable insoluble COD in the reactor or effluent
Kd = overall auto-oxidation rate of total COD in the reactor
The degradable insoluble COD in the reactor (SL, ) consists of micro-
organisms plus any influent insoluble COD that has not yet been degraded.
The degradation rate of this material is not rapid and probably contributes
Tjttle to the overall growth of the microorganisms. With this assumption,
$2j can be neglected and Equation 40 rewritten under equilibrium
conditions.
F(S. - S) = V- + Kd-S) (41)
Since F/V = D, y= D, X^ = Y(Si1] - S^), $n = p-|y, and Si^ = o.Si
where a is the fraction of the soluble degradable COD in the influent, and
X-|i is the microbial solids that are synthesized. Inclusion of these rela
tionships in Equation 41 results in:
(42)
Using Equation 42, the total COD in the effluent of a completely mixed
continuous flow system can be estimated if the appropriate constants are
known.
The change in total suspended solids in the reactor can be expressed in
a similar manner:
65
-------
(43)
where Xl?VSS = nonde9radable influent VSS
In Equation 43 it was assumed the Xi-|, the degradable influent volatile
suspended solids (VSS), can be oxidized without significantly increasing
the soluble COD in the reactor. It was assumed that when the degradable
influent solids are metabolized, the soluble COD that results will be
used for microbial growth at the same rate as the initial soluble COD.
As noted from the batch experiments discussed earlier, the rate of
removal of soluble COD was greater than that of particulate matter,
thus soluble COD resulting from degradation of the particulate matter
should not accumulate in the reactor.
Assuming that the system is operated under steady state conditions,
Equation 43 can be modified to:
D(XT2VS$ + Xn - X) = Kd.X (44)
Using a as before, B as the volatile fraction of the suspended solids
in the reactor (XVSS/XSS), and "fi" as the undegraded fraction of the
influent volatile suspended solids (xi2VSS^XVSS^' the susPended solids
in the reactor and the effluent can be expressed by:
(45)
"fi" includes both the undegraded fraction of the influent volatile sus-
pended solids and the undegraded fraction of the synthesized microbial
solids, "fi" was operationally defined using the batch laboratory data
as the ratio of the volatile suspended solids in the reactor at any deten-
tion time "t" to the initial SS in the reactor at time zero.
The change of the soluble portion of the total effluent COD can be
expressed as follows, under steady state conditions:
66
-------
where S1 = soluble COD in the effluent
S^ = soluble COD 1n the Influent
Equation 46 differs from Equation 38 1n that Equation 38 estimates the
unmetabollzed soluble degradable COD in the effluent, S,,, and Equation
46 estimates the total soluble COD, S", which includes the biodegradable
and non-biodegradable COD, in the effluent.
Equations 42, 45, and 46 can be used to estimate the total COD, total sus-
pended sol Ids, and total soluble COD in the effluent if urn, Ks, a, 3, Kd, Y,
and f1 are known. The only variable available to those who will design
aerobic treatment systems 1s the dilution rate which 1s equal to one
over the detention time (hydraulic detention time).
The "undegraded" portion of volatile suspended sol Ids "f1" in the Influent
1s hard to define because it was obtained only during a specific aeration
period (Figure 4). It is possible that some of this material could be
degraded 1f the aeration period were longer. The value of "f1" .should be
related to the aeration period in.a logrlthmlc manner. Using data from
this study, Figure 24 was developed. An equation of the form
f1 = 0.967-t'0'157 (47)
fit the data with a correlation coefficient of 0.924.
Using the previously developed kinetic constants for the Monod equations,
and the equation for "Si", Equations 42 and 45 were used to calculate the
effluent total COD and suspended solIds that should result. These cal-
culated results were compared to the data obtained from the continuous
flow laboratory experiments. The comparison was done using the residuals,
I.e., the difference, between the measured values and the predicted
values. These residuals were compared to detention time of the units
to evaluate any particular trends (Figure 25). The source of the con.-
stants used to predict the results were determined as noted in Table 5.
67
-------
X
z c\i_
ll I ^J"
13 x
I *»
U- .~
o o
1.0
0.8
0.6
2 O
I- UJ
u Q 0.4
< z
lu!
o d
0.2
'ff»0.967t
-0157
U1
2 4 6 8 10 15 20 30
LIQUID DETENTION TIME, days
Figure 24. Residual nondegradable fraction of influent
suspended solids as related to liquid detention
time.
68
-------
o»
E
9
CO
UJ
oc
400
200
LABORATORY CONTINUOUS
FLOW UNITS
MIXED LIQUOR COD
A SUSPENDED SOLIDS
HYDRAULIC RETENTION TIME, days
6 8 JO £
14
-200
16
-400
Figure 25. Residuals vs HRT (with consideration of fi).
-------
Table 5. SOURCE OF EVALUATED CONSTANTS USED TO
PREDICT EFFLUENT COD AND SUSPENDED SOLIDS
Constants
ym
Ks
Kd
Y
fi
Source (Figure
12
12
21
13
24
No.)
The basic idea behind the use of residuals as a method of comparison of
expected and observed residuals is that if a proposed relationship is
adequate, the variations, i.e., residuals should be due solely, to experi-
mental errors. A plot of such residuals should reveal the magnitude of
the errors as well as conditions under which other than experimental errors
were the cause of the variation.' If the relationship is adequate, a plot
of residuals should indicate a reasonably narrow horizontal band around
zero.
In Figure 25, Equations 42 and 45 were able to predict the results over
a detention time ranging from about four to sixteen days. The Equations
predicted higher than measured results at a detention time less than
three days.
Eckenfelder -
The basic equations and notation for this approach were described earlier
(page 24). The volatile sludge accumulation in a completely mixed, con-
tinuous flow reactor treating poultry wastes can be defined as:
Change of the MLVSS in the reactor
= Synthesis of Biomass - Autooxidation of MLVSS
= a(So - Se)-Q - bXv-X (48)
70
-------
where AXv = = D-Xv,
0=1, and
So - Se = Sr, therefore
- Se) _ b {49)
The effluent solids is equal to AXv plus fi*Xo.
Using available laboratory and pilot plant oxidation ditch data, Equation
49 was graphically evaluated to determine the values of "a" and "b",
(Figures 26 and 27). The difference of "a" and "b" values (Table 6)
between the laboratory and pilot plant data niay be due to a) different
measurements of solids concentration, i.e., suspended solids were used
for the laboratory data, but total solids had to be used for the pilot
plant data, and b) settled poultry manure suspensions were used for the
laboratory studies while unmodified poultry wastes were used In the oxi-
dation ditch, i.e., wastes were excreted directly into the ditch. In
spite of these differences, the values of "a" and "b" were reasonably
close.
The oxygen requirement can be defined as
Rr --- D>Sr -+b' (50)
- a
XSS or XTVS XSS or XTVS
Using the available data of laboratory and pilot plant, Equation 50
was plotted in Figure 28 and a1 and b1 values (Table 6) were evaluated.
Again, a1 and b1 for the laboratory and pilot plant data are different,
presumably due to the same reasons expressed for the solids data.
71
-------
I
o
o
LJ
<
oc
0.8
0.6
0.4
0.2
5 -0
-0.2
LABORATORY STUDIES
0*4.3
b*-0.08
0.04 0.08 0.12 0.16 0.20
SOLUBLE COD REMOVED,qms
SS,gm day
Figure 26. Graphical estimation of a and b values
laboratory data.
72
-------
0.04
0.03
o
o
»
UJ
fe
tr
0.02
0.01
OXIDATION DITCH
G«4.I3
b « -0.02
3
-0.01
1
0.004
0.008 0.012 0.016 » 0.020
SOLUBLE COD REMOVED,gms
TVS,gm -day
-0.02
Figure 27. Estimation of a and b values using oxidation
ditch data.
73
-------
0.16
I 0.12
to
E
o»
uT
0.08
CL
I-
0.04
o 0.16
6
en" 0.12
H-
g 0.08
Sr 0.04
LABORATORY STUDIES
a'«0.63
b'« 0.096
I
I
1
0.02 0.04 0.06 0.08 0.10
SOLUBLE COD, gms /SS, gm /day
I
OXIDATION DITCH
g'« 1.50
b1* 0.028
I
0 0.02 0.04 0.06 0.08 0.10
SOLUBLE COD,gms/TVS,gm /day
Figure 28. Estimation of a1 and b1 values using
laboratory and oxidation ditch data.
74
-------
Table 6. COMPARISON OF CONSTANTS BASED ON DATA FROM
THE LABORATORY UNITS AND THE OXIDATION DITCH
Correlation Correlation
Data source a b coefficient a1 b' coefficient
Laboratory 4.30 -0.08 0.97 0.63 0.096 0.52
Oxidation ditch 4.13 -0.02 0.99 1.50 0.028 0.99
These two sets of values can be used to predict the oxygen requirements
for the aerobic treatment of the respective types of poultry wastes.
The total COD in the effluent can be predicted when the soluble fraction
and the COD of the solids are known.
Se = Se + Se - Se + fo«AX(or AX) (51)
where Se1 soluble COD in the effluent
Se2 = insoluble COD in the effluent
fo = COD equivalent of effluent suspended solids
or total volatile solids XTV$, I.e., b'/b
The soluble 'COD in the effluent is equal to
Sel ' K- 1 (52>
which is comparable to Equation 19 described earlier.
Where Si^ = soluble influent COD
K = soluble COD removal rate
Xv = MLVSS, MLTVS, or other parameter compatible to the
manner by which K was determined
t = liquid detention time
75
-------
The removal rate constant, K, determined from these studies, can be used
for poultry manure wastewaters.
Equation 51 can be used to estimate the total COD of an effluent. Using
relationships developed in this study, the predicted results are com-
pared to the actual results in Figure 30 for laboratory data and in
Table 7 for the oxidation ditch data. Data obtained by the application
of McKinney's approach are also included here and these will be discussed
later in the report.
The prediction of the suspended solids concentration was better than
that of total COD (Figure 29). This may be because the constants for
the suspended solids originated from a laboratory continuous flow unit
and had a correlation coefficient of 0.95. The prediction of the mixed
liquor COD was based on the sum of the soluble COD and the COD equiva-
lent of the effluent suspended solids. Thus greater randomness of the
MLCOD residuals may be reasonable.
Again, the Equations provide a reasonable fit over a detention time
ranging'from four to sixteen days but not as good a fit at lower deten-
tion times.
McKinney -
The basic equations and notation for this approach were described earlier
(page 20). The design equations developed by McKinney (7-9) have been
for the biodegradable, soluble fraction of wastewater and must be modified
to include any insoluble organic matter in the influent wastewater. Since
most animal wastes and wastewater contain a significant amount of insoluble
or particulate materials which are partially biodegradable, the evaluation
of the constants (Ks, Ke) in these equations must consider the effect of
the presence of particulate materials. The present study has followed the
procedures proposed by Burkhead (30) for the evaluation of CMAS constants
with consideration of the particulate matter in the wastewater.
"Km" was evaluated from the soluble COD data collected from the laboratory
continuous flow unit. These data were corrected for the COD of NOp-N
and the non-degradable soluble COD in the reactor. The influent soluble
COD data were corrected for the non-degradable portion. The result is
shown in Figure 30. "Km" can be calculated from the value of the slope
of the line of best fit.
"Ks" is a function of "Km" or "K"m", where "K" is a composite coefficient
that includes the energy-synthesis relationship that exists for the food
being metabolized and the composition of cellular material produced.
Thus "Ks" can be defined as K^K^Km where ^ is related to the energy-
synthesis constant and K is the reciprocal of the oxygen equivalence
76
-------
800
- 400
0»
Q
CO
-4OO
-800
-1200
HYDRAULIC RETENTION TIME, days
8
10
12
14
LABORATORY UNITS
MIXED LIQUOR COD
* SUSPENDED SOLIDS
16
Figure 29. . Relationship between residuals and HRT.
-------
Table 7. COMPARISON3 OF DIFFERENT DESIGN APPROACHES
FOR THE AEROBIC TREATMENT OF POULTRY WASTES
00
Total effluent
Design
approach
Mass balance -
this study
ave.
Monod
ave.
HRT
(days)
29
43
70
77
29
43
70
77
predicted
(mg/1)
16,300
21 ,580
25,040
26,270
16,300
21,160
24,350
25,400
measured
(mg/1)
17,560
22,540
25,240
28,800
17,560
25,540
25,240
28,800
COD
predicted
measured
0:92
0.85
0.99
0.91
OTW
0.93
0.83
0.97
0.88
0790
Effluent solids concentration
predi cted
(mg/1)
Suspended
12,770
17,200
20,760
22,080
14,950
19,420
22,350
23,300
measured
(mg/1)
Solids
11,950
16,300
19,200
21 ,000
11,950
16,300
19,200
21 ,000
predicted
measured
1.07
1.06
1.08
1.05
1.06
1.25
1.19
1.16
1.11
1.16
continued.
-------
Table 7 (continued). COMPARISON3 OF DIFFERENT DESIGN APPROACHES
FOR THE AEROBIC TREATMENT OF POULTRY WASTES
I
vo
Design
approach
HRT
(days)
Total effluent COD
predicted measured predicted
(mg/1 ) (mg/1 ) measured
Effluent solids concentration
predicted measured predicted
(mg/1 ) (mg/1 ) measured
Suspended Solids
Eckenf elder
ave.
McKinney
ave.
29
43
70
77
29
43
70
77
15,220
21 ,540
29,320
31 ,700
14,600
20,250
26,760
28,800
17,560
25,540
25,240
28,800
17,560
25,540
25,240
28,800
0.87
0.84
1.16
1.10
0.99
0.83
0.79
1.06
1.00
OT92"
10,130
14,190
19,050
20,550
Total Volati
11,450
15,260
19,460
20,750
11,950
16,300
19,200
21 ,000
le Solids
16,500
21 ,300
23,500
24,800
0.85
0.87
0.99
0.98
0.92
0.69
0.72
0.83
0.83
0.77
Design constants for the approaches were developed using laboratory data. The comparison was
made by using these constants to predict the results that should occur in an oxidation ditch
and then comparing the predicted results to those in the pilot plant oxidation ditch.
-------
12
o>
e 10
i
I
UJ
8
§
o
UJ ..
o: 4
UJ
CC
I-
co
CD
3
(0
0.03/hr
I
I
I
1
50 100 150 200 250 300
SUBSTRATE REMAINING.F, mg/l
350
Figure 30. Graphical evaluation of Km value.
80
-------
of the cellular mass synthesized. If the wastewater contained particu-
late material which can be partially degraded, K, and K9 can be defined
as (30): ' L
v - COD of Ma + Me
Kl - COD Amoved
_ Insoluble COD of ML - Insoluble Non-biodegradable COD
~ Total COD - Unmetabolized Soluble Degradable COD
- Total Non-biodegradable COD (53)
Ma + Me
COD ofMa + Me
MT - Mi - Mii
COD of Ma + Me
MT - Mi - Mii
Insoluble COD of ML - Insoluble Non-biodegradable COD
(54)
Based on the above definition, the K, and K« values can be evaluated
from the relationship shown in Figure 31 by using the available labora
tory continuous flow data. Pseudo K, is related to detention time
while K2 is not. '
"Ke" was evaluated by the following equation (55) using data from the
continuous flow laboratory units:
- Mv/ts
Mv - 0.2-Ks-'ts
The values of "Ke" were obtained at different detention times. Previous
studies (8, 30) have adopted a value of (0.02 hr ) to represent "Ke"
81
-------
.9
AVE.- 0.752
.8
CO
.7
.6
10
15
1.0
.8
.6
.2
5 10
HRT, days.t
15
Figure 31. Estimation of Ki and K? using laboratory
CMAS data.
82
-------
at different aeration times. In this study, the "Ke" values were compared
to the organic loading rate (Figure 32) and a reasonable correlation
resulted. "Ke" values lower than those previously reported were observed
at low loading rates.
With some of the necessary constants evaluated, they were applied to
data from the continuous laboratory units and the oxidation ditch to
estimate the effluent COD and solids. The estimates obtained using
the equations were then compared to the measured data. The solids
concentration in the effluent was calculated as proposed by McKinney
while the mixed liquor or total COD in the effluent from a system such
as noted in Figure 20 was estimated as follows:
MLCOD in the effluent = [unmetabolized soluble COD]
+ [non-degradable soluble COD] + [COD equivalent of biomass 1n the effluent]
+ [non-degradable insoluble COD contained in the influent] (56)
where COD of biomass = -a- x (Ma + Me)
1.33 (Ma + Me) (57)
"fi" equaled 0.465 times the total suspended solids in the influent for
the laboratory data. For the pilot plant data, "fi" was equal to:
1.814 x (aeration time, days)"0'52 (58)
and the non-degradable soluble COD in the Influent was 0.25 times the
total soluble Influent COD.
The predicted and measured total COD and solids values were compared
using their residuals (Figure 33). The residuals decreased as the
aeration time increased. This may be due to the fact that the fraction
of non-degradable suspended solids in the Influent was not 0.465 and
may be a function of aeration time. The residuals were more reasonable
at longer detention times, greater than ten days.
83
-------
1.0
0.5
o
o
0.10
0.05
0.01
-Ke»0.97L
1.29
0.01 0.05 O.I 0.5 1.0
LOADING RATE.L, soluble COD, gms / MLVSS,gm/day
Figure 32. Ke related to soluble COD loading rate.
84
-------
oo
en
BOO
6OO
^ 400
e
3 200
CO
UJ
* 0
-200
-400
-MIXED LIQUOR COD
A-SUSPENDED SOLIDS
HYDRAULIC RETENTION TIME, days
I A I
8
14
16
CONTINUOUS
FLOW UNITS
Figure 33. COD and suspended solids residuals related
to hydraulic retention time - fi was not
considered.
-------
Assuming that the non-degradable fraction was a function of detention
time and using the relationship noted in Figure 28 did not increase
the ability of the equations to predict actual values (Figure 34). The
residuals were even greater than before.
The following equation was proposed by McKinney to predict the oxygen
uptake rate:
- F) 1.42(Ma + Me)
dt " t " ts
Equation 59 estimates the oxygen requirement for the soluble substrate
and does not consider the oxidation of the insoluble substrate present
in the influent or the oxidation of NH4-N to N02-N or/and N03-N.
In the aerobic treatment of a waste a£ complex as poultry manure, both
the oxidation of the insoluble components and the oxidation of the
nitrogen should be considered when determining the oxygen requirements
of the aerobic unit.
Accordingly, Equation 59 was modified as follows to incorporate these
factors:
n - Sn -1.42X11+S12(1 -f)
+ Og needed for nitrogenous oxygen demand]
(60)
where Si^ = soluble degradable COD in the influent, mg/1
S"^ = soluble degradable COD in the effluent, mg/1
X,-| = biomass concentration, mg/1
Si2 = insoluble COD in the influent, mg/1
f = undegradable fraction of insoluble COD at an
aeration time, t (days)
0 28
For these experiments, f was equal to 0.87 x t . Equation 60 was
applied to the oxidation ditch data (Table 8).
86
-------
00
400
200
CO
CO
UJ
(T
-200
-400
-600
-8OO
HYDRAULIC DETENTION TIME, days-
8
10 12 14 16
A
MIXED LIQUOR COO
SUSPENDED SOLIDS
Figure 34. COD and suspended solids residuals compared to HRT -
fi was considered.
-------
Table 8. COMPARISON OF 02 UPTAKE RATE BY THE
MODIFIED McKINNEY'S APPROACH
HRT
(days)
29
43
70
77
02 uptake rate
(predicted)
32.7
34.0
30.3
31.3
(mg/l/hr)
(measured)
39.3
37.3
40.5
34.8
Predicted
Measured
0.83
0.91
0.75
0.90
The results indicate that Equation 60 can be used to estimate the oxygen
uptake rate of aerobic systems treating poultry wastes.
Summary
All of the approaches evaluated appeared to be able to predict the
effluent characteristics of an operating aerobic poultry waste treat-
ment system (oxidation ditch) reasonably well. The key to the success
of the approaches lies in being able to evaluate the constants necessary
to each approach. The constants were developed independently using the
results of laboratory studies and were applied to an operating oxidation
ditch. It is interesting to note that the constants developed from the
laboratory data were able to be used to adequately predict the perfor-
mance from a larger scale operating unit, especially since some of the
waste characteristics, operating conditions, and measurements of some
of the parameters were different.
A summary comparison of all of the design approaches that were studied
was presented in Table 7. All of the approaches were able to predict
the actual effluent characteristics, generally within about 10-15%.
This variation is not bad considering the variations that took place
in the laboratory units and the oxidation ditch. The variation is
tolerable enough that any of the approaches can be used for general
predictive purposes and possibly for actual design purposes.
Some of the approaches had wider variations over the detention times
used for comparison than did other approaches. The choice of which
-------
approach should be used will depend upon the ease with which the respec-
tive constants can be obtained and verified and upon the experience of
the design engineer with a particular approach.
The oxygen requirements of the laboratory units and the oxidation ditch
could not be directly compared because different parameters of active
mass were used in each case. Representative oxygen demand requirements
that can be used for design purposes are noted in the report.
DESIGN EXAMPLE
The following section deals with approaches for designing a treatment
system for poultry wastes to accomplish COD and suspended solids removal
and odor control. Poultry wastes and wastewaters are very concentrated
and are disposed of on land adjacent to poultry farms. Therefore, certain
basic constraints exist in developing the design of a feasible treatment
system for these wastes. These constraints are: 1) land will be the
ultimate disposal medium rather than surface water bodies, 2) primary
treatment, i.e., separation of solids prior to biological treatment,
is an unnecessary part of a poultry waste treatment system and will not
be used, and 3) treatment to a level to achieve the EPA set guidelines
for effluent COD and suspended solids is not necessary. It is imprac-
tical to attain the secondary effluent guidelines with these wastes
unless the wastes are diluted either before or after treatment, water
carriage systems are used, and large unit operations are provided.
The two design approaches presented here include one to show the futil-
ity of designing treatment systems to attain the EPA quality for sec-
ondary effluents, and one utilizing the mass balance approach developed
in this study for predicting suspended solids and COD concentration in
the effluent.
An oxidation ditch without solids-recycling is considered as the basic
treatment device in these approaches because of the following considera-
tions: a) it can be used directly under the cages to receive and treat
the wastes without any unit operations ahead of it, b) it can aero-
bically stabilize wastes and provide simultaneous odor control, c) it
can be installed and operated with considerably less degree of sophis-
tication than alternative aerobic treatment systems, and d) it can be
constructed indoors and operated without being affected severely by
seasonal temperature fluctuations.
Approach !_
Objective -
Designing a system to treat poultry waste to attain the EPA guidelines
for domestic wastes for effluent BOD5 and suspended solids, i.e., 30 mg/1
and 45 mg/1 respectively.
89
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Assumptions -
1. Number of birds: 10,000
2. COD/bird/day - 0.0430# (19.5 g)
3. SS/bird/day = 0.024# (10.98 g); Total Solids/bird/day = .068#(21.8 g)
4. Loading rate = 1 Ib COD/1 Ib of MLVSS (1 kg COD/1 kg MLVSS)
5. No primary settling will be needed
6. No secondary settling will be needed
7. 1 mg/1 BOD5 = 2 mg/1 of COD
Using the mass balance approach developed in this study, the influent
COD required to accomplish a COD of 60 mg/1 in the effluent may be com-
puted for various HRT values.
s-t
"1
where K = 0.128 day
Si = influent COD
1= effluent COD
The computed influent COD concentrations, the volume of dilution water
needed to attain this influent COD concentration, and the volume of
ditch to provide the needed HRT are given in Table 9.
The corresponding influent suspended solids concentration at the dilution
water used (Table 9) were computed assuming that the suspended solids
contribution/bird/day was 0.024 Ibs. This influent suspended solids con-
centration was used to predict the effluent suspended solids concentration
by applying the mass equation developed in our study, (k1 = Xi - x/t-x;
k1 = 0.161 days ; Xi = influent suspended solids concentration; x =
effluent suspended solids concentration; and t = detention time, days).
These design computations are given in Table 10.
Since the expected effluent suspended solIds concentration at the various
HRT values Is less than the guidelines set by EPA, the design parameters
90
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Table 9. INFLUENT COD CONCENTRATION, HRT, AND VOLUME OF DITCH NEEDED
TO YIELD THE SECONDARY EFFLUENT CRITERION FOR COD (60 mg/1)
HRT
(days)
5
10
20
30
40
50
60
70
80
90
Influent
COD, mg/1
98
137
214
290
367
445
520
597
674
750
Volume of dilution
water required
to attain the
influent COD
concentration
liters x 106
1.990
1.423
.911
.672
.531
.438
.375
.326
.289
.260
Capacity of the
oxidation ditch,
liters x 106
9.95
14.237
18.229
20.177
21.259
21.916
22.505
22.87
23.151
23.406
Volume of
oxidation ditch/bird,
1 i ters
995
1423
1822
2018
2125
2191
2250
2287
2315
2340
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Table 10. RELATIONSHIP BETWEEN HRT, INFLUENT SUSPENDED
SOLIDS CONCENTRATION, AND EXPECTED EFFLUENT
SUSPENDED SOLIDS CONCENTRATION
HRT
(days)
5
10
20
30
40
50
60
70
80
90
Resultant influent
suspended solids
concentration -
mg/1
55
76
119
162
205
248
290
333
376
419
Expected effluent
suspended solids concentration
mg/1
30.4
29
28
27.8
27.5
27.4
27.2
27.1
27
27
This suspended solids concentration was achieved by diluting the waste
with the quantities of water mentioned in Table 9.
92
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used for achieving the effluent COD criterion (60 mg/1) should auto-
matically yield an effluent suspended solids concentration that conforms
to the EPA guidelines.
Using the equation developed in this report, the influent suspended
solids concentration was computed at various HRT's that are required
to achieve the effluent suspended solids concentration of 45 mg/1 set
by EPA (Table 11). The amount of dilution water necessary to achieve
this suspended solids concentration from the suspended solids excreted
by the 10,000 birds is also given in Table 11.
Even though these considerations (Table 11) show that it is possible
to design a system for achieving the EPA secondary effluent guidelines,
such an approach is not practically feasible because of the following
considerations.
1) EPA guidelines do not permit discharge of wastes from agricultural
operations to surface waters, and thus 1t is not necessary to strive
for these guidelines when land is considered as the ultimate disposal
medium.
2) Parenthetically, even if EPA would allow the discharge of wastes
from agricultural operations, enormous size aeration units and large
quantities of water are needed to achieve the desired effluent criteria.
The cost of water required for dilution of the large size treatment units
required, the operating costs, and the need to dispose of water used
only for dilution, do not justify using this approach. Alternative
approaches are more feasible.
3) Even if the effluent'COD and suspended solids criteria are satis-
fied by this approach, the concentration of nutrients such as N and P
contained in the effluents will be greater than the limits known to
cause eutrophication.
Approach Ij^
In this approach no effort is made to achieve the secondary effluent
criteria for domestic wastes since it is impractical to dilute the waste
first and treat it, or treat it first and dilute it later for discharge
into surface waters, an alternative approach is made to design the
systems to treat the concentrated waste and dispose of the relatively
concentrated effluent on land.
One of the design criteria considered in this approach was to have the
ditch operated at a total solids concentration of less than 2%. Above
this solids concentration, oxygen transfer was shown to be impaired (43).
93
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vo
Table 11. RELATIONSHIP BETWEEN HRT AND INFLUENT AND SUSPENDED SOLIDS TO ACHIEVE
AN EFFLUENT SUSPENDED SOLIDS CONCENTRATION OF 45 mg/1
HRT
(days)
5
10
20
30
40
50
60
70
80
90
Influent SS
concentration
(mg/1 )
81
117
190
262
335
407
480
552
625
697
Dilution water
needed to achieve
the influent
suspended solids
(liters x 106)
1.344
.930
.572
.415
.325
.267
.227
.197
.174
.156
Volume of
ditch needed,
(liters^ 106)
6.72
9.304
11.459
12.465
12.998
13.374
13.608
13.805
13.934
14.057
Volume of
ditch/bird
(liters)
672
930
1145
1246
1300
1337
1360
1380
1393
1405
-------
The size of the ditch needed to give the effective solids concentration
1% at various detention times can be computed using the equations
developed in this study.
Assumptions -
(1) 2 x Suspended Solids = TS in raw waste
(2) 3 x Suspended Solids = TS in stabilized waste
(3) Assume waste is considered stabilized for design purposes beyond
a 10 day HRT
(4) 240# of SS are produced/day
(5) Other assumptions are the same as in Approach I.
Using the equation
K = -*-, K = 0.161 at 1 gm of COD/1 gm of
x-t MLVSS loading
at HRT 10 days, = .161 = 24° " x ; x = 91.95# SS remaining
10-x
- 91.95 x 3 - 275. 85# of TS remaining
To have a 1% slurry means
275.85 Ibs x 453.6 - x = 12512 liters of slurry
i.e., the quantity of manure added daily to the ditch should be diluted
to 12512 liters in order to obtain the same volume of effluent from
the ditch. At an HRT of 10 days, the ditch.capacity would be 12512 liters
x 10 = 125120 liters.
95
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Similarly, in order to achieve a 1% solids concentration in the effluent
at an HRT of 20 days, the volume of effluent to be withdrawn per day would
be 7756 liters. This means that the manure added to the ditch daily
should be made up to 7756 liters to maintain the equilibrium liquid
volume. Thus at 20 days HRT, the ditch volume would be 7756 x 20 =
155,120 liters.
It should be noted that in addition to the water added with the input
manure, additional water may be required to compensate the losses due
to evaporation in order to maintain the equilibrium liquid volume.
The foregoing should only be considered as an example showing the appli-
cation of the equations developed in this study. For predicting the
effluent quality from a treatment system using these equations, the
loading factor should first be ascertained. This will enable the deter-
mination of K1 and K from equations 34 and 37. These values can then
be used in conjunction with the actual detention time of the system to
predict the concentration of COD and SS in the effluent. The values of
K1 and K used in the above example were meant for a loading factor of 1
and may not be typical of actual systems. (See Conclusions Section of
the report also.)
Volume of Water Needed tp_ Maintain the Liquid Depth jji the Oxidation Ditch
In order to maintain a constant liquid depth in the ditch, the volume of
the material (manure + water) entering into the ditch should be equal
to the volume of effluent withdrawn. Thus for a 10 day HRT, the volume
of the manure entering daily into the ditch should be made up to 12512
liters by adding water. Assuming the 480 Ibs (218 kg) of total solids
entering the ditch will have a wet weight of 1920 Ibs (872 kg) and will
occupy a volume of 230.5 gallons (872 liters), 11,640 liters of water
for making up the volume to 12, 512 liters will be needed.
COD Concentration in the Effluent
Assume
a) HRT = 10 days
b) influent COD = 430 Ibs (195.45 kg)/day
c) k = 0.128 (loading rate, 1 gm COD/ 1 gm of MLVSS)
Using the equations developed in this study
96
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0.128 =
MO
s = 188.5 Ibs (85.7 kg)
The effluent COD of 188.5 Ibs will be contained in the 12,512 liters of
effluent that will be withdrawn per day. At this HRT the COD effluent
will be
188.5 x 453.6 xOOO
12,512
Oxygen Requi rements
The computation of oxygen requirements is made with and without con-
sidering the nitrogenous oxygen demand of the poultry waste. The former
consideration is applicable for situations where minimal aeration is
practiced and no nitrification is contemplated while the latter is
applicable to situations where nitrification of the waste is desired.
To accomplish the transfer of oxygen, a rotor made by Thrive Centers
or an equivalent rotor was assumed and oxygen transfer relationships
accomplished by such rotors were utilized. In order to find the rotor
length required to transfer the desired amount of oxygen at various
immersion depths, the following assumptions were made
1) only one-half of COD is biodegradable and consumes oxygen
2) the performance characteristics of rotors are similar to those
determined in our pilot plant studies (43)
3) 80% of the TKN is able to be nitrified
4) 1 mg of NH.-N requires 4.6 mg oxygen for conversion to NO.,.
Case I_: Oxygen Requirements with Np_ Nitrification
Assuming the daily COD input from the birds as 430 Ibs (195-5 kg),
the oxygen demand due to the biodegradable fraction will be 215 Ibs
(97.7 kg)/day.
97
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Two hundred fifteen Ibs of oxygen per day (8.96 Ibs/hr) should be supplied,
This assumes no residual dissolved oxygen in the mixed liquor and repre-
sents the minimum amount of oxygen that must be supplied by a rotor. If
a residual dissolved oxygen concentration is desired, the amount of
oxygen necessary to achieve that concentration, and the possibility of
nitrification needs to be considered.
Case II; Oxygen Requirements with Nitrification
i) 02 required for biodegradable fraction: 215 Ibs/day
ii) 02 required for nitrogenous demand:
TKN (Ib/bird/day) = 0.0018
(Higher TKN contribution per bird
is possible, and it should be determined
prior to the computation of 0? requirements
for nitrification.) *
. TKN of 10,000 birds = 18 Ibs/day
a) Assuming 80% of this is able to be nitrified, 18 x 0.8 or
14.4 Ibs of nitrifiable N/day will result.
b) This will have a nitrogenous oxygen demand of 14.4 x 4.6 or
66 Ibs 02/day, assuming up to the N03" stage
111) Total 02 demand = 215 + 66 - 281 Ib/day or « 12 Ib/hr.
1v) The dissolved oxygen to be maintained in the ditch 1s 2 mg/1;
the ditch volume 1s 125,120 liters at a 10 day HfrT. This dissolved
oxygen concentration Is chosen as the minimum dissolved oxygen concen-
tration to be maintained at all times for sustaining nitrification.
At the above D.O. concentration, the 0« transfer rate, i.e., #0« trans-
ferred/hr can be computed as follows for the experimental pilot plant
at 2 Inch immersion depth having a volume of 6091 liters or containing
a weight of 13,405 Ibs of liquid.
#02 transferred KLa(m1n"1)'(Cs - CL)«lbs of water x 60
nr 106
Assuming a KL, value of 0.166 at 2 Inch Immersion depth, at 20°C and
at 2 mg of equilibrium D.O. (43), this will be . .
98
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Table 12. TRANSFER OF OXYGEN BY AN EXPERIMENTAL ROTOR
AT VARIOUS EQUILIBRIUM D.O. CONCENTRATIONS*
* °2 tsferred/ft/hr'
2 .0.524 (7.89 gm/cm/hr)
3 0.452 (6.7 " )
4 0.379 (5.6 " )
5 0.306 (4.6 " )
6 0.233 (3.5 " )
The Immersion depth was 2 Inches and the liquid volume was 6091
liters.
99
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Table 13. ROTOR LENGTH NEEDED FOR OXYGENATION OF POULTRY WASTE FROM 10,000 BIRDS
BASED ON THE PERFORMANCE CHARACTERISTICS OF A ROTOR TESTED AT AWML
o
o
Immersion Total solids
depth (inches) (% w/v)
Lbs. of Op transferred/hr/ft
at 2.0 mgat 0.0 mg
D.O./l D.O./l
Length of rotor needed (ft)
with
nitrification*A
without
nitrificationt
2" (5.1 cm)
4" (10.2 cm)
6" (15.2 cm)
1 - 2
3
4
5
1 - 2
3
4
5
1 - 2
3
4
5
0.52
0.42
0.34
0.26
1.23
1.0
0.8
0.62
1.64
1.33
1.07
0.82
0.67
0.54
0.44
0.34
1.57
1.27
1.02
0.79
2.23
1.81
1.45
1.12
22.9 (7.0 m)
28.3 (8.6 m)
35.2 (10.7 m)
45.8 (14 m)
9.8 (3.0 m)
12.0 (3.7 m)
15.0 (4.6 m)
19.4 (5.9 m)
7.3 (2.2 m)
9.1 (2.8 m)
11.2 (3.4 m)
14.6 (4.5 m)
13.3 (4.1 m)
16.5 (5.1 m)
20.5 (6.3 m)
26.7 (8.2 m)
5.7 (1.8 m)
7.0 (2.2 m)
8.8 (2.7 m)
11.4 (3.5 m)
4.0 (1.3 m)
5.0 (1.6 m)
6.2 (1.9 m)
8.0 (2.5 m)
These values are computed assuming an equilibrium D.O. of 2 mg/1.
^These values are computed assuming an equilibrium D.O. of 0 mg/1.
AThese computations were based on the assumption that the contribution of TKN per bird was
0.0018 Ibs/day. In computing the rotor length needed for other cases, however, the TKN
contribution per bird should first be determined and then the necessary calculations
should be made as presented under case II.
-------
Table 14. DESIGN PARAMETERS AND EXPECTED PERFORMANCE OF AN
OXIDATION DITCH FOR 10,000 BIRDS, AT 2" IMMERSION DEPTH
HRT (days)
]£ 20
Oxygen required (#/day)
nitrification 281 281
no nitrification 215 215
Estimated rotor length (ft)
nitrification 23 23
no nitrification 14 14
Mixed liquor effluent
Total Solids, mg/1 =10,000 =10,000
Suspended Solids, mg/1 « 5,000 « 5,000
COD, mg/1 6,835 7,060
Volume of effluent or overflow, liters 12,512 7,756
Volume of ditch, liters 125,120 155,120
101
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0.166 x (9.2 - 2) x 13.405 x 60 = ^ ]bs Qf
106 i
Since the experimental rotor length was 1.83 ft, the #CL transferred/ft
of rotor length will be
= 0.523 Ibs/ft/hr
Similarly, at other equilibrium D.O. concentrations, the #0« transferred/
ft/hr were computed and presented in Table 12.
Based on the Op transfer rates (Table 12) and other performance charac-
teristics obtained for the experimental rotor in our pilot studies (43),
the rotor length needed for oxygenation of the poultry waste from the
10,000 birds under consideration is computed for various immersion
depths of the rotor at various solids concentration with and without
considering the nitrification of the waste. The immersion depths of
2 inches, 4 inches, and 6 inches for the rotor were considered in com-
puting the various quantities indicated in Table 13.
Similar computations can be made for other values of HRT and equilibrium
D.O. concentrations in the mixed liquor. Table 14 shows summary design
computations for an oxidation ditch treating waste from a 10,000 bird
operation considering an equilibrium D.O. concentration of 2 mg/1 for
sustaining nitrification, with an HRT of 10 and 20 days.
Sol Ids Accumulation in^ a_ Continuously Filling Reactor With Np_ Intentional
Wastage of Solids
An equation was derived to predict the concentration of total solids at
any time in a continuously filling reactor. At times the oxidation
ditches may be operated as a continuously filled storage and treatment
device. By using the following equation, the total solids and COD con-
centration at any given time in the mixed liquor can be predicted.
Ct = Ci-f [ r - ] + Ci(l-f)t
"
102
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where Ct = Total Solids content after time "t" (days)
. Ci = influent solids contribution, gm/l/day
f = fraction of degradable solids
(1-f) = fraction of non-degradable solids
k = rate constant, reciprocal days
See the derivation and application of this equation in the Appendix A-I
103
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SECTION V
NITROGEN REMOVAL DURING AEROBIC WASTE TREATMENT
INTRODUCTION
The nitrogen content of poultry wastes produced in the United States in
1970 was about 9 x 10 pounds per day. Estimates of the amount of nitro-
gen reaching the surface or ground waters from this source are not
available. With the growing concern for maintenance of our waters,
greater emphasis is being placed on nutrient control with all wastes
and the technical and economic feasibility of nitrogen control of animal
wastes during aerobic stabilization requires investigation.
Several methods have been suggested for nitrogen removal from animal
wastes. These methods can be classified as either physiochemical or
biological. The biological processes of nitrification followed by denitH-
fication has been successfully demonstrated as a possible means of elimi-
nation of nitrogen from municipal wastes. An earlier investigation con-
ducted by the investigators of this project indicated that this process
may be applicable for nitrogen control in animal waste management systems.
The results of the previous EPA study (38) have been extended in this study
to obtain more information on the fundamental factors affecting nitrogen
control in aerobic systems. The fundamental factors included oxygen
input as related to oxygen demand, solids concentration, and nitri-
fying activity. In addition, nitrogen losses under operating con-
ditions were monitored in pilot and full scale aerobic systems treating
poultry wastes. These systems were oxidation ditches treating the
wastes from 250 birds at the Agricultural Waste Management Laboratory
and the wastes from 15,000 birds at the Houghton Poultry Farm.
104
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MATERIALS AND METHODS
Laboratory Studies
General -
A series of laboratory studies were conducted to obtain detailed infor-
mation on the factors affecting nitrogen control in aerobic systems.
Details of the equipment, approaches, and methods used in these studies
are outlined in this section.
Wastes -
The required concentrations of the wastes were made by suspending the
requisite amount of poultry manure in distilled water. The mixture
was blended in a Waring blender and filtered through a single layer
of cheesecloth to remove large particulate matter. The material
retained on the cheesecloth was washed with distilled water to recover
most of the soluble matter. The filtered suspensions were diluted
to the required volume with distilled water.
Mineral Salts Solution -
A mineral salts solution was used in certain experiments to resuspend
centrifuged mixed liquor solids. The salt solution contained the
following: MgSO/,.7H,0, 250 mg/1; FeS0..7H«0, 10 mg/1; CaCl9.2H«0,
10mg/l. * L 4 i *
Oxidation Ditch Liquor -
Mixed liquor from the pilot plant oxidation ditch was used in some
laboratory experiments and is referred to in this report as ODML.
Methods -
Total solids, volatile solids, and BOD were determined as described 1n
Standard Methods (35). COD was determined by a rapid method (36).
Suspended solids were determined by filtering a known volume of the
sample through glass filter paper. The weight of the dry solids
retained on the filter paper was used as an estimate of the suspended
solids. A considerable length of time was generally taken for the
filtration of the relatively concentrated samples. In such situations *
a part of the weight of the suspended solids may have included some
dissolved solids.
The pH of the sample was measured with a Corning pH meter.
105
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Ammonium nitrogen was determined by the distillation method (39). The
sample was buffered with phosphate buffer to pH 7.4 and was distilled
in a micro-Kjeldahl distillation apparatus. The distillate was collected
in boric acid and titrated with KH(I03)2.
Total Kjeldahl nitrogen was determined by a micro-Kjeldahl method (39).
Nitrite nitrogen was determined by a diazotization method using N-l-
napthyl ethylene diamine dihydrochloride (39).
Nitrate nitrogen was determined by the PDSA method as described in
Standard Methods (35) but with some modification (39). Clarification of
the sample with A1(OH)3 was omitted. Clarification was achieved by a
very high sample dilution which was found to be necessary to obtain the
range of NCL-N suitable for determinations. NOp-N in the sample was
eliminated after the chlorides were removed. A neutral aliquot of the
diluted sample was adjusted to pH 2 by the addition of sulfamic acid
crystals. In some of the samples, nitrate was determined by the dis-
tillation procedure (39).
Storage oj' Samples -
All the nitrogen analyses, COD, and BOD were performed on the samples
rapidly and without storage. N02-N and N03-N analyses of samples stored
with H2S04 were found to be unsatisfactory. In the determination of
solids, it sometimes was inconvenient to process all the samples in one
day. On such occasions the samples were refrigerated and determinations
were made as soon as possible.
Measurement of Nitrifying Activity -
Known volumes (5 to 10 ml) of the nitrifying liquor were centrifuged,
washed with 0.8/& sodium chloride solution and suspended in 100 ml of
nitritifying or nitratifying media placed in 250 ml conical flasks. The
suspensions of the media containing the test liquors were agitated
with the aid of magnetic stirrers. At periodic Intervals, samples were
drawn from these flasks and examined for their nitrite content and pH
value.
The total nitrogen content of the nitrifying liquor sample was determined
using aliquots of the same sample. The rate of nitrification was
expressed in terms of milligrams of nitrogen oxidized per hour per
milligram of TKN.
106
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Reactor Uni ts -
These units were utilized to study the nitrogen losses that occur under
controlled environmental conditions. Both pyrex glass aspirator bottles
and plexiglass units constructed by laboratory personnel were used.
Examples of the plexiglass units are shown in Figure 35.
Different quantities of ODML and poultry manure suspensions in tap water
were aerated. The slurries in the reactors were mixed with either magnetic
stirrers or paddle type stirrers, fitted through a mercury seal, and
driven by electric motors. The air flow to the system was monitored with
flow meters. The air bubbling from the system passed through acid traps
to collect any ammonia volatilizing from the system.
Pilot Plant Oxidation Ditch Studies
The oxidation ditch at the Agricultural Waste Management Laboratory has
been operating and evaluated continuously since 1970. The initial eval-
uation was to stress the oxidation ditch system to its maximum to determine
its potential with untreated poultry wastes. This caused the system to
be used as an aerated holding tank. Solids concentration ranged up to
about 8.5 percent due to high evaporation and non-overflow conditions.
Since it is possible that there may be overflow from oxidation ditches
used for poultry operations, during the period of this project it was
decided to operate the pilot plant oxidation ditch at various solids
levels to evaluate the magnitude and characteristics of the overflow.
This permitted nitrogen mass balances to be made. Nitrogen losses in
the ditch were related to the varying operating conditions.
The concentration of total solids in the oxidation ditch was varied by
altering the water input to the ditch. The operational control of the
total solids cpntent necessitated the installation of an automatic
overflow in addition to control of water input to the ditch. The data
collected in this study included: rotor immersion depth, waste output,
water input, rates of oxygen uptake, temperature, COD, total and
volatile solids, and organic, ammonia, nitrite and nitrate nitrogen.
Solids concentrations were changed only after a suitable equilibrium
period was established. During the study, the immersion depth of the
rotor was increased whenever the concentration of dissolved oxygen in
the mixed liquor was close to zero. The reduction in dissolved oxygen con-
centration occurred as a result of the decreased oxygen transfer capabili-
ties of the rotor as the solids concentration increased. Thus an equilib-
rium period, as defined by the concentration of total solids, consisted of
more than one sub-phase if the rotor immersion depth was changed.
107
-------
TO-*~
GAS TRAP
r-FEED & CLEANING
PORT
SAMPLE
PORT
c.
'£)
AIR
STIRRING BAR
PLASTIC AIR
DISPENSER
MAGNETIC
STIRRER
REACTOR I
FEED
TO -
GAS TRAI
SAMPLE
PORT
r-MERCURY SEAL
CLEANING PORT
AIR
BUILT-IN-AERATOR
REACTOR II
Figure 35. Reactors used in laboratory nitrogen control
experiments.
108
-------
In September 1972 the birds were removed from over the oxidation ditch
and the operation of the ditch was restarted after 250 new birds were
placed in the cages on 17 October 1972. About 300 gallons of ODML that
had been saved from the previous operation for purposes of seeding were
added to the ditch. Tap water was added to bring up the total volume in
the system to 1500 gallons. The rotor was operated at an immersion
depth of 1 inch. Several changes were made in the mode of operation
throughout the project.
Houghton Farm Oxidation Ditch Studies
In early January 1972, a full scale oxidation ditch waste treatment system
was installed in a nearby poultry farm. The system was put in by the
owner, Mr. C.L. Houghton, after he had seen the pilot plant oxidation
ditch but without detailed design information from the personnel asso-
ciated with this project. However, since the installation of the
system, the project personnel have worked closely with Mr. Houghton to
monitor the system and to cause it to operate satisfactorily.
Waste disposal at the Houghton Farm prior to conversion to an oxidation
ditch consisted of periodic removal of the stored, liquid manure and
disposal on farm land. After spreading, the manure was immediately
plowed under. The odors generated by the manure disposal and emitted
by the ventilating fans of the production facility caused complaints
from neighbors. Based upon the positive results he had seen demonstrated
with the Cornell pilot plant oxidation ditch,; Mr. Houghton decided to
convert his building and install an oxidation ditch.
The Houghton oxidation ditch consists of two separate ditches side by
side in the building. The ditches: are interconnected to permit liquid
equalization. The building is 45 ft by 325 ft. Each oxidation ditch is
15 ft wide, 276 ft long, consisting of two 6 ft raceways separated by a
3 ft barrier. The waste from about 7500 birds is defecated directly
Into each ditch. Two 5 hp, 27 in. diameter, 6 ft long rotors operate
continuously in each ditch. The rotors operate at 111 rpm.
The bird watering system is of a type that permits excess water to fall
1n,to the ditches necessitating intermittent removal of the mixed liquor
to avoid overflow of the system. The liquid level of the system is
allowed to increase between mixed liquor removals. This increase in
liquid level results in a variable immersion depth and variable oxygen
transfer by the rotor. The rotor immersion depth varies from about 6 in.
to 9 in. The liquor is removed by a conventional liquid manure spreader
to adjacent fields. The liquor is not odorous and no odor complaints
have occurred since the ditches went into operation. The lack of odor
has permitted Mr. Houghton to spread the waste closer to his poultry
house and residence thus reducing disposal time and costs. Approximately
5000-8000 gallons of the liquor are removed from the ditches each week.
109
-------
Project personnel had no opportunity to measure the oxygen transfer
relationships of the rotor before the wastes were added. The rotors are
the same make and diameter as the rotor in the Cornell University pilot
plant oxidation ditch permitting extrapolation of data from the pilot
plant study to this operation.
Analyses of the oxidation ditch mixed liquor such as COD, TKN, NOg-N,
N03-N, total and volatile solids, pH, temperature, oxygen uptake rates,
and liquid depth were obtained once or more per week during the first
six months of evaluation and one to two times a month thereafter.
Calculation of Nitrogen Losses
A loss of nitrogen has been consistently observed in the aerobic labora-
tory units containing nitrified poultry wastewater and in the aerobic
nitrifying oxidation ditches. This loss has been computed as the difference
between the amount of nitrogen that was fed to the system and the nitrogen
that was actually present in the mixed liquors plus any nitrogen that
was removed deliberately from the system such as for disposal or analysis.
These losses were attributed to denitrification and ammonia volatilization.
The gas traps in the laboratory systems permitted an estimate of the
ammonia volatilization losses. No effort was made 'to measure ammonia
losses in the oxidation ditch studies because of the inherent difficul-
ties in such measurements.
If the possibility of nitrogen loss due to ammonia volatilization is
excluded or known, the observed nitrogen losses can be attributed to
denitrification. Nitrogen mass balances in the aerobic systems should
therefore take into consideration the two-sources of nitrogen losses.
The relationship between the nitrogen added, nitrogen content of the
system and the losses can be expressed by the following:
Total Nitrogen added = Total Nitrogen in the system
+ nitrogen lost due to ammonia volatilization
+ nitrogen lost due to denitrification
+ nitrogen removed from the system for disposal or analysis
110
-------
RESULTS
General
In laboratory units containing nitrified poultry wastewater and in
nitrifying oxidation ditches, losses of nitrogen were observed even though
aerobic conditions prevailed in these systems. Losses of nitrogen from
a treatment system can occur by two mechanisms; a) volatilization of
ammonia, and b) denitrification. Volatilization of ammonia takes place
when the pH of a system is in the alkaline range and free ammonia is
present. The loss of nitrogen by denitrification takes place under
anoxic conditions at the expense of nitrate or nitrite being used as an
hydrogen acceptor by the facultative heterotrophs.
When active nitrification is established in a system, the pH generally
is below 7. These pH conditions are not conducive for ammonia volatili-
zation. Although volatilization has been observed in laboratory units
and the oxidation ditch because of alkaline conditions during the start-
up phase, such losses were found to be insignificant once nitrification
is established and the pH dropped below 7. Nevertheless a loss in total
nitrogen of these systems occurred although the dissolved oxygen concen-
tration was in the range of 1-5 mg/1. Excluding the possibility of
nitrogen losses by ammonia volatilization, the loss in total nitrogen is
only possible by denitrification.
As a consequence of this observation on nitrogen losses from nitrifying
mixed liquors maintained under aerobic conditions, investigations were
initiated to study the factors that govern these nitrogen losses. One
factor that is considered important is the loading factor, e.g., #COD/#TS
or #TKN/#TS. Total solids were used as a parameter because we have found
that the determination of suspended solids with concentrated wastes such
as the one used in these studies included always a variable proportion
of dissolved solids. As the loading is increased, a greater oxygen
demand is exerted in the system. In a nitrifying reactor, when a high
oxygen demand is exerted because of a high organic loading, there is a
good probability of N0« and NOo being used as electron acceptors along
With the dissolved oxygen present in the mixed liquor. This is con-
ceivable if it is visualized that the concentration of dissolved oxygen
at the surface or interior of a microbial floe may be close to zero.
This can be possibly due to a high oxygen uptake exerted by the micro-
organisms because of the readily available substrate. In such a
situation a very low oxygen tension or even anaerobiosis can occur
at the surface of the floe and the N0« and NOZ present within its
sphere of influence may be used as electron acceptors and thus denitri-
fied even though a certain concentration of dissolved oxygen is present
in the bulk of the mixed liquor.
Ill
-------
Experimental
To obtain Information on factors affecting nitrogen losses under aerobic
conditions, three batch,reactors were used to study the effect of solids
concentration on such losses of nitrogen in a nitrifying mixed liquor.
With an increase in the biological solids concentration, the oxygen
demand of the mixed liquor will increase and the oxygen transfer capa-
bility of an aerator may decrease. In these experiments the total solids
concentration was used as a measure of the microbial floe as well as the
inert sol Ids contained in the mixed liquor.
Reactor I_ -
Three liters of an actively nitrifying oxidation ditch mixed liquor were
placed in a 4 liter aspirator bottle and air was supplied at 8 SCFH.
The total solids concentration in the reactor was 36,800 mg/1.
Reactors II and III -
The conditions were the same as in Reactor I, except that the reactors
contained different solids concentrations, i.e., 18,500 and 9450 mg/1
respectively.
TKN, N02-N, N03-N, NH4-N, COD, total sol Ids, dissolved oxygen, and
oxygen uptake rates were measured routinely. Typical data are shown in
Figure 36. Nitrogen balances were computed and the results are pre- ,
sented in Table 15.
The results indicated that Reactor I, which contained more solids and
exerted a higher Initial oxygen uptake rate than the other two reactors,
had a total nitrogen loss of 13/L There was no nitrogen loss in Reactors
II and III. The dissolved oxygen concentration 1n the mixed liquor of
Reactor I was Initially 2.6 mg/1 and increased to about 6.5 mg/1 towards1
the end of the experimental run. During the same period the oxygen uptake
rate decreased from a maximum of 48 mg/l/hr to 6.5 mg/l/hr indicating that
the waste was stabilized. The high Initial oxygen uptake rate created
by the mixed liquor of Reactor I was presumably due to the high concen-
tration of readily available substrate. In Reactors II and III the
oxygen uptake rate of the mixed liquor was considerably less than that
of the mixed liquor of Reactor I and no nitrogen losses were observed.
The dissolved1 oxygen levels were higher 1n these reactors. The nitro-
gen loss in Reactor I could have been due to the denitriflcation in
the vicinity of the microbial floes as a result of the creation of
localized anaerobiosis which in turn was a consequence of the high
oxygen demand exerted in the system. In Reactors II and III, such
localized anaerobic conditions might have been as large because of
lower oxygen demand.
112
-------
REACTOR I
35
o
x 25
o
8 20
17
COD
\-
I i i i I i i i I I i i i i I I I I i I i I I I I
45
40
35
30
25 E
*
20 »-
15
O
x
x
o»
2200
2000 -
N03-N
o>
i I i i I I I I I I I
800
700
600
500
400
N.
O>
10
10 15
JULY -
20
25
DAYS-1972
Figure 36. Change of characteristics during batch treatment
of poultry wastes.
113
-------
Table 15. NITROGEN BALANCES IN BATCH NITRIFYING UNITS AT DIFFERENT
INITIAL SOLIDS CONCENTRATION - LABORATORY STUDY
Reactor
I
II
III
Period of
operation -
(days)
25
14
14
Initial
total solids
concervtrati on
(mg/1)
36,800
18,500
9,250
Dissolved
oxygen
(mg/D
Init. Fin.
2.6 6.5
6.0 6.5
6.5 6.3
02 uptake
rate
(mg/l/hr)
Init. Fin.
48 6.5
24 9.5
12 4
Total
ni trogen
(mg/1)
Init. Fin.
2487 2156
1258 1261
622 615
Nitrogen
Loss (%)
13.3
0
0
-------
To confirm the results obtained with Reactor I, two more reactors were
used. These reactors contained total solids concentrations of 3.96 and
4.95% respectively. In these two reactors, 18 and 195K of the total
nitrogen was lost in 10 and 6 days, respectively. During this time
period the dissolved oxygen concentrations were greater than 2 mg/1.
From these experiments it was seen that while the aeration rate was
constant, nitrogen losses from a nitrifying reactor can be increased
by increasing the solids concentration and thereby the oxygen demand.
Another series of experiments were used to further investigate these
relationships. Instead of using a nitrified mixed liquor as in the
above studies, two batch reactors were set up using raw poultry waste-
water to increase both solids concentration and oxygen demand.
Reactor la
Two liters of an actively nitrifying mixed liquor were placed in a 4
liter unit. One liter of a poultry manure suspension containing
100 g of wet manure/liter was added to this reactor.
Reactor Ib
Two liters of the same nitrifying seed used for Reactor la were added
to another unit. One hundred ml of the same poultry manure suspension
was added daily for 22 days. When the liquid level in the unit
reached 3 liters, the unit was operated on a fill and draw basis with
100 ml of the poultry manure suspension being added each day after
100 ml of the mixed liquor was withdrawn. This procedure was followed
to distribute the oxygen demanding material over a period of time rather
than in one dose as was done in Reactor la.
Reactor Ic
In a third reactor, three liters of the nitrifying mixed liquor that
was used as the seed for the above reactors were kept and used as a
control. No waste was added to this unit.
Humidified air was bubbled through all the reactors at a rate of 8 SCFH.
TKN, N02-N, N03-N, NH4-N, total solids, dissolved oxygen and the
oxygen uptake rate of the mixed liquors were measured routinely.
Ammonia losses from these reactors were measured by trapping the
volatilized ammonia in a standard acid solution. Nitrogen balances
were obtained and the percent nitrogen losses due to ammonia volatili-
zation and denitrification were computed. The results from this study
are presented in Table 16.
115
-------
Table 16. NITROGEN LOSSES DUE TO AMMONIA VOLATILIZATION
AND DENITRIFICATION - BATCH STUDY
Period of operation
(days)
Total solids, mg/1
Initial
Final
D.O., mg/1
Initial
Final
0,, uptake rate, mg/l/hr
^Initial
Final
Total nitrogen, mg/1
Added
Accounted
% N losses
Ammonia volatilization
Denitrifi cation
la
15
21 ,400
14,000
0.3
6.5
80
4
1,465
765
31
17
REACTOR
Ib
22
9,560
23,680
3.5
3.5
36
265
2,200
1,820
5
12.5
Ic
15
7,580
7,600
5.0
7.0
22
2
420
405
4
0
116
-------
The nitrogen losses were the highest in Reactor la. Of the 48% of the
total nitrogen lost, 31% was accounted for by losses due to ammonia
volatilization. The remaining 17% was lost due to denitrification.
Thus if treatment systems are started with a heavy load of TKN, sig-
nificant losses of nitrogen can be expected due to ammonia volatiliza-
tion. The nitrate that was added in the nitrifying seed was lost from
the mixed liquor of Reactor la during the first day of its operation.
This indicates that the high oxygen demand of the mixed liquor and the
low initial dissolved oxygen concentration (0.3 mg/1), might have
created anaerobic conditions at the floccular level resulting 1n
denitrlfication. Such losses of NO* were not noticed either in
Reactor Ib or Ic during the first day of operation. In these reactors
the oxygen uptake rates were significantly lower, and the dissolved
oxygen concentrations were significantly higher than the Reactor la
during their entire operation.
Denitrification losses can be expected to be lower in systems treating
nitrogenous wastes when they are loaded uniformly. For example, when
Reactor Ib was fed with poultry wastewater to reach a theoretical total
nitrogen concentration of 1425 mg/1 on the eighth day, 1395 mg/1 of
TN were accounted for. Only 10 mg N/l was lost due to ammonia vola-
tilization. The 20 mg N/l that was not accounted for could be due to
denitrification or experimental error.
In Reactor Ib, until the eighth day the dissolved oxygen in the mixed
liquor was approximately three mg/1 but during the period of 8-13 days,
nitrogen losses occurred in the system. The dissolved oxygen concentra-
tion in the mixed liquor during this period was about 1.0 mg/1. This
may have been due to faulty aeration. A total nitrogen loss of about
15% was observed during this period, although nitrification continued
to occur simultaneously as noticed by an increase in the N03-N con-
centration. After this period no significant loss of nitrogen was
noticed and the dissolved oxygen in the mixed liquor was above 3.0 mg/1.
The loss of nitrogen in Reactor la was significantly higher than in
Reactor Ib, although the initial total nitrogen in Reactor la was in
the same range of the total nitrogen found on the eighth day in Reactor
Ib. The difference in nitrogen losses between these two reactors lies
in the manner in which these reactors were operated with respect to
loading rates as well as the concentration of dissolved oxygen that was
able to be maintained.
The nitrogen loss in Reactor Ic was very small and was due to the high
concentration of dissolved oxygen prevailing throughout its operation and
the relatively low oxygen uptake rate of the mixed liquor.
117
-------
By starting a system with a single high loading initially (la) rather
than distributing the same by daily installments (Ib), it was possible
to obtain a considerable solids reduction. In Reactor la the initial
total solids concentration of 21,440 mg/1 decreased to 11,250 mg/1
amounting to about 50% reduction in 22 days. The solids concentration
in Reactor Ib, however, increased from 9560 mg/1 to 23,680 mg/1 during
the same period. An increase in the solids concentration was expected
because the manure suspension was added daily to this reactor without
removing any mixed liquor up to the fourteenth day. The solids level on
the fourteenth day in the reactor was 20,000 mg/1 which is only slightly
lower than the concentration of solids on the twenty-second day.
Although a good total solids balance could not be made in this investi-
gation, it can be said that if any solids reduction had occurred in
Reactor Ib, on a percentage basis it was much less than the 50% of
solids reduction observed in Reactor la. The high solids reduction in
Reactor la presumably was due to volatilization of ammonia, denitrifi-
cation, oxidation of organic matter, lysis of cells and further oxi-
dation of the cell constituents under prolonged aeration. The absence
of significant loss of solids in Reactor Ib possibly was due to minimal
losses of nitrogen and less lysis and subsequent oxidation of biological
solids.
From the above studies it appears that by maintaining a certain minimum
dissolved oxygen concentration in the mixed liquor and by manipulating
the loading rate, it may be possible to increase the total nitrogen
losses by denitrification while maintaining an actively nitrifying system.
The nitrogen loss in aerobic systems is related to the relationship
between oxygen demand and oxygen input. Altering the solids concentra-
tion will affect the oxygen input by affecting the oxygen transfer
capability of the aeration system. Altering the aeration rate while
maintaining a constant loading to the reactor is another way to vary
the oxygen input. To investigate the effect of aeration rate and hence
oxygen input or aerobic nitrogen losses, three additional batch studies
were conducted.
One liter of a well nitrified mixed liquor was added to 250 ml of a
poultry manure suspension. Aeration was held at 10 SCFH. One hundred-
fifty ml of the poultry manure suspension was added daily until the
volume of mixed liquor in the reactor reached 2.5 liters. Thereafter a
daily fill and draw procedure was maintained in which 250 ml of the
manure suspension was added after 250 ml of the mixed liquor was with-
drawn. The reactors were tightly sealed and stirred magnetically. The
air outlet of the reactors was connected to a train consisting of a
foam trap, two traps containing 0.2 N sulfuric acid, and a final trap
containing boric acid. The traps were to collect any volatilized
ammonia.
118
-------
Some ammonia was volatilized in the beginning of the experiments. How-
ever, once nitrification occurred, no ammonia was volatilized. Nitrogen
balances were made in the three reactors after equilibrium was established
to obtain baseline data (Table 17). Variations in losses of ±10% are
not significant due to the sampling and analytical errors inherent in
the balances. Thus the fact that an apparent nitrogen gain occurred
may have been due to analytical errors. The apparent gain also indi-
cated that no nitrogen losses occurred under the baseline conditions.
After baseline equilibrium conditions were established, the air flow
rates in two of the reactors were altered to 6 and 2 SCFH. All other
operational factors remained the same. Problems did occur in the
operation of the Bill reactor. Occasionally the magnetic stirrer stopped,
ammonia losses increased and nitrification slowed. A close watch was
kept on the unit to minimize such problems. Sufficient equilibrium
data was obtained under the altered aeration conditions to compare the
nitrogen losses in the reactors (Table 18).
The results (Table 18) indicate that as the aeration rate per unit volume,
and hence the oxygen input, decreased the nitrogen losses due to denitri-
fication increased. Even with the operational problems in Reactor Bill,
adequate nitrification took place to obtain the noted denitrification
losses.
The operation of the reactors at the low aeration rates was difficult.
Slight decreases in the air flow or mixing rates resulted in cessation
of nitrification. The pH of the mixed liquor increased and the con-
version of organic nitrogen to ammonia nitrogen increased. Some
ammonia volatilized under these conditions. When these conditions were
corrected, production of nitrites and nitrates again occurred confirming
the ability of the nitrifying organisms to continue to exist under
inhibitory conditions and to respond when the inhibitory conditions were
alleviated.
Further work is continuing to more precisely determine the relation-
ships between oxygen input, oxygen demand, and nitrogen losses. These
studies are being done under controlled laboratory conditions.
Oxidation Ditch Studies
General -
Samples of the wastes excreted by the birds at the pilot plant and the
Houghton Poultry Farm were obtained periodically over the project period.
The samples were analyzed for a number of parameters that were used in
calculating mass balances. The samples were collected by randomly
putting a collection pan under one cage of birds for 24 hours. The
119
-------
Table 17. NITROGEN BALANCE ON BATCH REACTORS AT CONSTANT AERATION RATE
Aeration rate Nitrogen loss3
Reactor (SCFH) (%)
BI
BII
Bill
10
10
10
+15
+12
+ 4
aThe losses were computed over a ten day equilibrium period. The + sign
Indicates no losses occurred and an apparent Increase was noted.
Table 18. NITROGEN BALANCE ON BATCH REACTORS
AT DIFFERENT AERATION RATES
Aeration rate Nitrogen loss3
Reactor (SCFH) (%)
BI 10 -13
BII 6 -17
Bill 2 -52
aThe minus sign indicates that nitrogen was unaccounted for. The losses
were assumed to be due to denitrlfication because all other loss
possibilities were accounted for.
120
-------
samples were diluted with tap water, blended, and analyzed. The average
results of these analyses are presented in Table 19.
The excreta of the birds at the pilot plant were collected and analyzed
over two separate periods. The periods reflect the two different groups
of birds that were in the cages. With few exceptions, the characteristics
of the excreta during the two periods are comparable. The birds at the
Houghton Farm were fed different rations. This and the sampling problems
noted in Table 19 account for the differences in characteristics between
the birds at the two locations.
Pilot Plant -
i) General operation - The operation of the pilot plant oxidation ditch
was varied throughout the project period to investigate a number of
operational parameters and to investigate nitrogen losses under con-
trolled conditions. The operational procedures and some analyses of the
mixed liquor during the project periods are shown in Figures 37 and 38.
The concentration of dissolved oxygen in the mixed liquor fluctuated
depending upon the solids concentration and rotor immersion depth.
Dissolved oxygen levels were always above zero and at times were up to
6 mg/1. The ODML contained organisms associated with satisfactory
aerobic treatment, i.e., flagellated, free swimming and-stalked protozoa,
rotifers, and bacteria.
The pilot plant oxidation ditch was primarily a nitrate production unit.
Even with nitrification to the nitrate form, the pH remained near neutral.
The performance of the system appeared affected by seasonal temperature
variations. Even though the birds and the ditch were housed in a heated,
enclosed building, the ditch was constructed in the ground and is
affected by the ground temperature. Mixed liquor temperatures decrease
in the fall and increase in the spring. The lowest temperature in the
ditch was about 12°C in January and increased gradually to over 20°C in
June.
ii) Nitrogen loss - In September 1972, the chickens were taken out from
the pilot plant facility and there was an opportunity to study the deni-
trification of the oxidation ditch mixed liquor in situ. The objective
of this investigation was two-fold: a) to studyThe time required for
removing the N03 by denitrification and the subsequent opportunity for
renitrifying the denitrified mixed liquor, and b) to study the activity
of nitrifying organisms under denitrifying conditions.
On September 7, 1972, the rotor in the oxidation ditch was stopped and
denitrification of the mixed liquor started without the input of poultry
wastes. On September 21, 1972 the rotor was started and run for 30
121
-------
Table 19. CHARACTERISTICS OF THE POULTRY EXCRETA ENTERING THE OXIDATION DITCH SYSTEMS
ro
ro
Pilot Plant
6 June 1972
to
24 August 1972
15 November 1972
to
17 May 1973
Houghton Farm
3 May 1972
to
3 April 1973
Grams per bird per day
Total weight of excreta
Dry weight of solids excreted
Volatile solids excreted
Percent on a dry weight basis
Total solids content in excreta
Total volatile sol ids/ total solids
Milligrams per gram of total solids
COD
BOD5
TKN
NHj-N
112
30
22
27
71
729
200
88
6
123
31
22
25
72
658
140
79
4
21 Oa
38
29
18
76
797
214
83
6
Feeding and watering devices at the farm are of a different design and had an influence on the
samples collected. Spilled water and some feed were in the samples collected at the Houghton
Farm.
-------
= NORMAL , NIT= NITRIFICATION , ON = DENITRIFICATION
ro
u>
NITROGEN
CONTROL APPOAC
ROTOR IMMERSION
DEPTH, inches
TEMPERATURE
°C
DITCH DEPTH,
inches
HES
2
20
15
16
14
N NIT ON .N. NIT 1 |, NIT 1, N 1
4 ' III III
n i
JI^ """
__^ ~ " ""
n i
14,000
IO.OOO
TOTAL SOLIDS
CONCENTRATION,
mg/l
6000
3OOO
OCT« NOV. I DEC.
U - 1972 - >
JAN.
APR. ' MAY
1973
Figure 37. Operational modes, solids and temperature
data for the pilot plant oxidation ditch.
-------
Figure 38. TKN, ammonia nitrogen and pH in the pilot
plant oxidation ditch.
-------
minutes to mix the ditch contents to ensure a good contact between the
microorganisms and the substrate. The denitrification in the ditch was
stopped on October 4, 1972. Five hundred gallons of the mixed liquor
was pumped into a separate tank and aeration resumed to renitrify the
denitrified mixed liquor. The TKN and N03-N concentration was measured
routinely. The results are presented in Figure 39. Most of the N03-N was
lost in the first 15 days. About 90% of the initial N03~N was lost over
the entire 27 day denitrification period. The unexpected decrease in TKN
of the mixed liquor may be due to sampling error, because during the
denitrification phase, settling and compaction of the MLSS occurred.
Renitrification of the mixed liquor was possible even after it was
subjected to 27 days of denitrification confirming the observations made
in. previous studies.
During the denitrification of this study, the nitrifying activity, i.e.,
activity of nitrosomonas organisms 1n the mixed liquor, decreased
(Table 20). Although the activity of the nitrite forming organisms
decreased rapidly, active organisms persisted even after two months.
Denitrification conditions prevailed for 27 days of this period. The
mixed liquor could be renitrified successfully after it was denitrified
and when the nitrifying activity was only about one tenth that which
existed at the beginning of the denitrification period.
Table 20. ACTIVITY OF NITROSOMONAS IN A DENITRIFYING MIXED LIQUOR
Nitrosomonas activity
Day
0
4
6
13
29
54
62
mg NU2-IV i/nr/iiiy IMI/I
53.3 x 10"4
48.1 x 10"4
26.0 X 10"4
9.0 x 10"4
4.6 x 10"4
3.9 x 10"4
4.7 x 10"4
125
-------
1000 -
BATCH STUDY
NO WASTES ADDED
2000
- 1500
10
15 20
SEPTEMBER -
25
30
5
OCT.
Figure 39. In situ denitrification of pilot plant
oxidation ditch mixed liquor.
126
-------
The results of this study confirm that the denitrification of the
nitrified poultry waste proceeds slowly in the absence of an exogenous
oxygen demand and that renitrification of the denitrified mixed liquor
is possible even after it is subjected to a prolonged denitrification
of as long as a month.
After this initial in situ denitrification study, the ditch was placed
into operation as a flow through unit as described earlier. Two addi-
tional in situ denitrification studies were made in the ditch, one in
January~T973 and the other in April 1973. In these latter studies, the
birds continued to add wastes to the ditch thus adding an additional
oxygen demand for denitrification. In both studies, the rotor was turned
on briefly each day to mix the ditch contents. In the January study no
overflow was permitted and in the April study overflow did'occur. Results
obtained in these denitrification studies are presented in Figure 40.
The detailed analytical results relating to nitrogen in the pilot plant
oxidation ditch treatment system are given in Appendix A-II. The nitrogen
Input to the oxidation ditch was computed by multiplying the number of
birds in the cages above the ditch by the average nitrogen content
excreted daily by a bird.
When the oxidation ditch was filling, effluent was not wasted. Hence the
output of nitrogen was zero. For other phases of operation, the difference
between the nitrogen input and output of the ditch was used in deter-
mining the net output. The total nitrogen in the ditch determined by
the actual analysis was known. The difference in the nitrogen content
in the ditch between two consecutive periods was given as the change in
the nitrogen content of the ditch. The difference between the actual
amount of nitrogen retained in the ditch in a given period and the change
in nitrogen content as measured by actual analysis of the mixed liquor
was noted as the loss. The average loss or gain in nitrogen content of
the system per day during each of the periods was obtained. From the
data presented in Appendix A-II, the percentage losses of nitrogen were
computed and are given in Figure 41. The loss of nitrogen (about 73*
observed during the initial filling period is high and may be due to:
a) ammonia volatilization which was greater when the system was restarted;
b) some incidental denitrification of N0« and NO, contained in the seed,
c) errors in obtaining a representative sample of the mixed liquor, and
d) errors in estimating the TN input to the ditch. Compaction of the
solids in the mixed liquor took place whenever the rotor was stopped,
and it was very difficult to obtain a uniform sample. TKN estimates
of the mixed liquor samples generally tended toward low figures.
In the first flow through period (November 1, 1972 to January 9, 1973),
the loss in nitrogen was about 31$. This was primarily due to denitri-
fication even though "aerobic" conditions prevailed in the system.
127
-------
280
^,240
"200
z
i
10
o 160
z
1 120
z
£* 80
z
40
- /-TOTAL -1
\ ^^^***^^^
\ ^^^^
\
\~^
\
NO -N+ V
wn^ M--^
\
k
\ FLOW -THROUGH]
i i i I V--I J i I i
7
60
^m
X
5 ^
?
4 ^
o
3 ^
8
2 -J
<
h=
1 ?
200
ISO
100
50
APRIL 1973
10
TOTAL
SOLIDS
NO FLOW-THROUGH
I I I I I I I I I I I I I VILLI I
II
10
9
10
o
8 x
7f
62
58
15 20 25
JANUARY 1973
Figure 40. In situ denitrification of pilot plant
oxidation ditch mixed liquor with wastes
added.
128
-------
lOO-fr-
ro
CO
0
z
UJ
o
o
H 50-
z
h-
o
cr
Ul
Q.
INITIAL LOADING
NO FLOW -THROUGH
20 3C
nrr .
FLOW -THROUGH
) 10 20 3
* WOW J
K-OC
UlO
OZ
1
0 10 20 30 10 20 3
* nrr J« JAM .
^FILLING PERIOD
NO FLOW-THROUGH
zo
00
1
Is
z11-
UJO
oz
»
FLOW-THROUGH
10 10 20 2
JL FFR J
8 10 20 3(
* MAR »
) 10
4 APR
1972
1973
TIME
Figure 41. Percent nitrogen losses during the operational modes
of the pilot plant oxidation ditch.
-------
Ammonia volatilization was negligible. The pH of the ODML was well
below 7.0 and there was active nitrification. Therefore, the losses
of nitrogen observed in the system could be attributed to denitrification
even though there was active nitrification in the system.
In the denitrification phase from January 9 to 25, 1973, the nitrogen
loss was about 66%. During this denitrification period, mixing was
provided by operating the rotor for about one-half hour every day. It
is doubtful whether any significant part of the nitrogen input into
the ditch during this period was nitrified. The losses of nitrogen
input as indicated in this period only represent the loss of the
nitrites and nitrates which were in the mixed liquor at the start of
the denitrification period.
The nitrogen losses in the second filling period were not as high as
during the first period since the ditch contents were well equilibrated
and nitrification was induced rapidly due to the presence of adequate
numbers of nitrifying organisms in the seed material. The nitrogen loss
during this period was 32%.
The second flow through period also showed a nitrogen loss (about 29%)
comparable to the first flow through period (about 31%). These losses
were primarily due to denitrification as the pH value of the ODML was
low and unfavorable for ammonia volatilization.
The nitrogen losses during the second denitrification period was 52%,
less than that encountered during the first denitrification period. This
may be due to the lower amount of oxidized nitrogen present in the ditch
during this period as compared to that of the first denitrification
period. Some oxidized nitrogen was lost via the effluent as the ditch
was operated on a continuous flow basis during this period. The rotor
was turned on for about eight hours per day during this period to provide
mixing. With such an operation, the denitrifi cation rates were higher
as compared to the rates obtained during the previous denitrification
period when mixing of the contents of the ditch was provided by operating
the rotor for one-half hour dally.
Because of the difference in time periods for the denitrification periods
and the regular flow through periods of the ditch, losses due to denitri-
fication during continuous operation of the ditch were much higher than
the losses achieved during deliberate denitrification. The total loss
of nitrogen due to the deliberate denitrification 1n the two denitrifi-
cation stages was about 8% as compared to 23% loss attributable to
denitrification under "aerobic" conditions, I.e., continuous operation
of the rotor in the ditch. The amount of nitrogen lost during the two
filling periods was 7.3% of the total nitrogen Input to the oxidation
ditch during the overall period, This loss was perhaps due to ammonia
130
-------
volatilization occurring 1n the system when the pH value of ODML was
high. High pH values and high NH4 concentrations were observed during
the filling periods.
The N02-N and NOg-N and the total sol Ids contents of the ODML at different
times during the two den1tr1f1cation periods were noted in Figure 40. The
rates of denltrlflcatlon were 0.08 and 0.24 mg of oxidized nitrogen per
hour per gram of total solids, respectively, during the January and
April den1tr1f1cation periods. Adequate mixing appears to be essential
for achieving better den1trif1cation rates. The mixing did not inhibit
den1tr1f1 cation.
An overall summary of the nitrogen balance in the oxidation ditch is
shown 1n Figure 42. A summary of the nitrogen losses over the period
of the oxidation ditch operation, October 1972 through April 1973, is
Indicated 1n Table 21.
Table 21. NITROGEN LOSS IN OXIDATION DITCH SYSTEM*
Total N loss during flow-through stages
Total N loss during den1tr1f1cation
Total N 1n effluent
Total N loss during the two filling periods
Total
Expressed 1n terms of the Initial estimated nitrogen Input to the system
During the first "flow-through" stages of the oxidation ditch, nitrifica-
tion occurred. At the same time significant amounts of nitrogen were
lost. This was presumably due to localized denltriflcation 1n the
anoxlc zones of the floe since ammonia volatilization was negligible.
The probability for nitrogen loss through this mechanism may be high
1n a nitrifying system 1f the localized anoxlc conditions for denltrl-
flcatlon are Increased while maintaining active nitrification. This
may be achieved by Increasing the solids concentration. Addition of
131
-------
CO
ro
10
9
o 8
§ 7
o"
x 6
uj 4
e>
2 3
K
z 2
I
TOTAL NITROGEN ACCOUNTED
FOR IN THE DITCH
TOTAL NITROGEN
INPUT
TOTAL NITROGEN REMAINING
AFTER DENITRIFICATION LOSSES
III
I I I I
20 30 10 20 30 10 20 30 10 20 30 10 2028 10 20 30 10
OCT?H NOV. + DEC. *{*JAN. 4* FEB. »|< MAR 4-- APR.
1972
TIME, days
1973
Figure 42. Nitrogen changes in the pilot plant oxidation ditch.
-------
raw manure will increase both the suspended solids content and the oxygen
demand of the system and increase the probability for anoxic conditions
in the microbial floe. Under these circumstances, the probability for
denitrification of N02 and N03 will increase.
An attempt was made to compare the oxygen uptake rates of the ODML
(expressed as mg 0«/hr per gm solids) during each flow through period and
the corresponding percent nitrogen losses. The available data was meager
and the results were inconclusive. More controlled studies could deter-
mine the actual relationship between oxygen demand and nitrogen losses in
an aerobic system.
111) Recent Operation - In a continuing phase of these studies at the
pilot plant, attempts are being made to control the solids content of
the oxidation ditch mixed liquor without adding fresh water. The mixed
liquor is being pumped intermittently into a settling tank and the super-
natant liquid is returned to the ditch (Figure 43). The mixed liquor is
pumped into the settling tank at intervals of eight hours. The actual
duration of pump operation is 4.5 minutes at each interval.
In addition to monitoring the total solids content, chemical analysis of
the mixed liquor from the ditch and the supernatant liquor from the
settling tank is being made on a regular basis. The results of the
nitrogen data collected over the period of June 28, 1973 to July 10, 1973
are given in Table 22 which indicate that denitrification has been
occurring in the settling tank. These studies will be continued to
develop procedures for nitrogen control in an oxidation ditch-liquid
recycle system.
Table 22. NITROGEN CONTENTS OF ODML AND
SUPERNATANT FROM SETTLING TANK
6/29
NHj-N, mg/1
NO'-N "
NO--N "
TKN
ODML
0
0.8
250
431
ST*
13
2
175
74
7/3
ODML
6
3
245
395
ST
18
0.9
175
92
7/6
ODML
8
0.8
235
487
ST
18
13
75
80
7/10
ODML
0
1
230
511
ST
22
41
3
146
Supernatant from settling tank
133
-------
WASTE
WASTE
WATER
WATER
I
OXIDATION
DITCH
OXIDATION
DITCH
MIXED LIQUOR
OVER FLOW
(DISPOSAL)
RETURN -
SUPERNATANT
LIQUOR
PUMP
SETTLED SOLIDS
(DISPOSAL)
Figure 43. Mode of operation of oxidation ditch for
for maintaining constant solids level.
134
-------
Houghton Poultry Farm -
i) General Operation - There have been two phases of operation since
the oxidation ditches were installed at the Houghton Poultry Farm in
January 1972. Phase I existed for the first 78 days of data collection.
The liquid depth was maintained at six to eight inches and the rotor
immersion depth varied from four to six inches. Thus the utilized ditch
q
capacity was 0.88 to 1.2 ft per bird. During this phase of operation,
nuisance odors were controlled, but there was a persistant ammonia odor
in the building and a foam problem in the ditches.
At the end of phase I, steps were taken for the purpose of controlling
the foam and reducing the ammonia odor. These steps included; a)
removal of 50 percent of the mixed liquor of the ditches, b) diluting
the remainder with water from a nearby pond to a liquid level of approxi-
mately thirteen inches, c) raising the rotors so the immersion depth
would be approximately six inches, and d) an addition of 500-1000 gallons
of seed from the pilot oxidation ditch at Cornell University.
The results of this action were anticipated to be; a) reduction of the
ammonia nitrogen concentration, BOD, and COD of the system by approxi-
mately three to four times, b) reduction in the ammonia concentration
would reduce any inhibition to nitrification. With the lower COD and
more efficient biomass, the oxygen demand would be reduced to a point
at which a residual dissolved oxygen level might be maintained in the
ditches, and c) with residual dissolved oxygen and the seed from the
pilot plant oxidation ditch, nitrification could begin.
After these steps were taken, the ditches were put back into operation.
Phase II consisted of the remaining 268 days of the study. The per-
formance of the ditches has been evaluated for a one year period,
January 1972 through December 1972. The nitrogen transformation and
losses are summarized in the following sections.
Foaming was a problem throughout the twelve month study and was con-
trolled by the addition of approximately two quarts of used motor oil
to the ditches per day. The ammonia odor varied in strength but was
usually present in the building.
Due to the large amount of leakage from the dew-drop watering system at
the Houghton operation, a portion of the mixed liquor in the ditches had
to be removed three to five times a week to maintain a relatively con-
stant liquid level. Better water control would have reduced the frequency
of mixed liquor removal and would have increased the mixed liquor solids
concentration. Mass balances were prepared on the oxidation ditches to
determine the percent reduction of total solids, total volatile solids,
ash, total Kjeldahl nitrogen, ammonia nitrogen, organic nitrogen, N02-N,
135
-------
N03-N, and COD. The mass balances considered the amount of these param-
eters entering the oxidation ditches, changes in their concentration in
the mixed liquor, and the amount of the parameter in the mixed liquor that
was withdrawn from the ditches for disposal. The loss of ammonia nitrogen
due to ammonia stripping was not included in the mass balance of ammonia
nitrogen since it could not be properly assessed. The samples of mixed
liquor removed for analysis were not included in the mass balances since
they represented a fraction of a percent of the mixed liquor withdrawn
for disposal.
i '
Monthly mass balances were calculated for February through December 1972.
Due to a change in operation in early April, the calculations for April
represented only the last 23 days of that month. The percent reduction
of any of the above parameters represents the amount of that parameter
that could not be accounted for in the mass balance. The mass balance
for any of the above parameters can be represented by the following:
Input - (± A Storage) - Output = A Parameter
where Input - raw waste entering the oxidation ditches
Storage - accumulated bottom deposits and the change in
concentration in the mixed liquor
Output - amount in mixed liquor be withdrawn from oxidation
ditches
A Parameter - the change in the parameter
The change in parameters due to storage is primarily due to a change in
mixed liquor concentration and the accumulation and compaction of materials
on the bottom of the ditches. The mixed liquor concentration of the
above parameters was determined by sampling and analysis. The change in
storage was calculated over the monthly periods. The bottom accumula-
tions were not sampled and analyzed throughout the study, but were measured
and analyzed for total solids, total volatile solids and ash after 14
months (432 days) of the start-up of the ditches. By measuring the depth
of the bottom deposits, the volume of the bottom deposits were calculated
and from the analysis of the deposits, the daily accumulation of total
solids, total volatile and ash were estimated. Since ammonia nitrogen
is soluble, it was assumed that it would have the same concentration in
the liquid of the bottom deposits as in the mixed liquor. The output
represented only that amount of a parameter that was in the mixed liquor
being removed from the oxidation ditches for final disposal on land.
ii) Mixed liquor characteristics - The mixed liquor of both ditches
was sampled and analyzed periodically throughout the study period.
136
-------
Because the two ditches received the same loadings, were roughly the same
size, and were interconnected, the characteristics of both ditches were
comparable. The solids and nitrogen data for ditch II are presented in
Figures 44 and 45 and the nitrogen data for ditch I is presented in
Figure 46. The variations noted in the Figures are due to the variations
in ditch operation such as removal of about 50% of the mixed liquor on
day 78, variations in the amounts of mixed liquor removed each week,
variability of water added by the leaky waterers, and variations in
microbial activity.
The nitrogen concentrations exhibited greater variations than did the
solids concentrations. Oxidized nitrogen forms were rarely found. Nitrites
were found only during one period of the study. No nitrates were found
during the study.
iii) Process efficiency - From the results of raw waste, mixed liquor,
and bottom deposit analysis, monthly mass balances were obtained on both
oxidation ditches for total solids, total volatile solids, total Kjeldahl
nitrogen, organic nitrogen and COD. The percent reduction of solids
and nitrogen are shown in Figure 47.
Total Kjeldahl nitrogen losses from the oxidation ditches could have
occurred by nitrification and ammonia volatilization. Table 23 indicates
the total Kjeldahl nitrogen loading to the system, and the amount lost
in terms of kilograms and as a percentage of the input.
Dissolved oxygen levels in the oxidation ditches ranged from a low of
zero mg/1 to a high of 8 mg/1. In each ditch, dissolved oxygen measure-
ments were taken at six points (Figure 48) over a period, of 13 months.
During this period, the D.O. measurements were made on an average of
twice a week. Table 24 shows the dissolved oxygen level at various
points in the ditch as a percent of the measurements made. The dis-
solved oxygen level in the ditches was less than 1 mg/1 for approxi-
mately 65-70 percent of the time and for approximately 70 percent of
the ditch length.
The oxygen uptake rates of the mixed liquor in each ditch were estimated.
The range of uptake rates was from 38 to 620 mg/l-hr. If one eliminates
the extremes, the range of uptake rates was from approximately 100 to
400 mg/l-hr. These rates were determined in the laboratory and not in
the oxidation ditches. Higher than expected oxygen uptake rates occurred
in the ditches. At no time after start-up of the operation was dissolved
oxygen consistently observed throughout the entire length of these ditches.
Shortly after the start-up, ammonia began to be released from the ditches
in the vicinity of the rotors. The high ammonia concentration in the
mixed liquor resulted from the incapacity of the rotor to add enough
oxygen to sustain nitrification.
137
-------
OXIDATION DITCH H
HOUGHTON POUTRY FARM
5000
-4000
300°
L/N
38
UJ z
Jg
II
2000 -
1000 -
,TOTAL KJELDAHL
NITROGEN
NITRITE
10
5
0
120 160 200 240
DAYS OF OPERATION
280 320 360
Figure 44. Nitrogen content of ODML in ditch II at Houghton poultry farm.
-------
CO
50,000
E 40.OOO
30,000
20,000
UJ
o
z
o
o
CO
§ 10,000
o
CO
OXIDATION DITCH H
HOU6HTON POULTRY FARM
TOTAL SOLIDS
VOLATILE SOLIDS
FIXED SOLIDS
I I
I
40 80 120 160 2OO 240
DAYS OF OPERATION
280
320
360
Figure 45. Solids content of ODML at the Houghton poultry farm.
-------
600O
5000
;o 4000
3000
<^
OO
-JO
Ul^, 2000
*OC
ot 1000
i-z
OXIDATION DITCH I
HOUGHTON POULTRY FARM
TOTAL KJELDAHL
NITROGEN
NITRITE
NITROGEN
AMMONIA
NITROGEN
o>
10 E.
5 I
.CM
40 80 120 160 200 240
DAYS OF OPERATION
280
320
360
Figure 46. Nitrogen content of ODML in ditch I at Houghton poultry farm.
-------
70
O 60
O 50
O
U 40
UJ
20
|0
0
o
o
UJ
-------
IS*
ro
92' r . 190'
/ cV
ROTOR /\
A
",... .M. ETI r\\H
*. rLUW
E WALKWAY
^ PLOW^X
\
1 P
1
D
ROTOR /
OXIDATION DITCH
Figure 48. Dissolved oxygen sampling points in the Houghton
oxidation ditches.
-------
Table 23. TOTAL NITROGEN LOSS FROM OXIDATION DITCHES
Month
February
March
April
May
June
July
August
September
October
November
December
TKN loading
(kg)
1249
1370
1012
1203
1388
1422
1410
1357
1344
1395
1430
TKN loss*
(kg)
635
547
375
601
736
655
466
407
780
405
457
% loss
' 49
40
37
50
53
46
33
30
58
29
32
The TKN reduction represents the amount of total Kjeldahl nitrogen that
could not be accounted for in the mass balance of the system.
143
-------
Table 24. DISSOLVED OXYGEN LEVELS AT DIFFERENT POINTS
IN HOUGHTON OXIDATION DITCHES
Sampling
point
Ditch I
A
B
C
D
E
F
Ditch II
A
B
C
D
E
F
Range of the
>3
Frequency of
ranges noted
21
13
9
0
7
7
23
15
0
0
4
0
dissolved
2-3
occurance
29
25
0
6
7
5
26
33
10
0
11
8
oxygen concentrations (mg/1)
1-2
of dissolved
45
47
12
6
17
4
49
50
7
10
21
13
0<1
oxygen
5
15
23
27
45
33
2
2
24
10
46
33
0
concentration
0
0
56
61
24
51
0
0
59
80
15
46
144
-------
The pH of the mixed liquor varied only slightly. Microbial activity was
high consisting primarily of bacteria and free swimming ciliates. No
stalked ciliates or rotifers were found, indicating that a high degree
of stabilization of the waste was not accomplished.
There were a number of factors that may have affected the treatment
efficiency of the oxidation ditches at the Houghton Farm. These include
dissolved oxygen, temperature, and the detention time of the mixed
liquor. Due to the lack of control over the system, any effect tempera-
ture or dissolved oxygen had on the treatment efficiency were not de-
tected or able to be determined.
The level of dissolved oxygen in the Houghton oxidation ditches was less
than 2 mg/1 50 percent of the time, and 70 percent of the ditch had a
dissolved oxygen concentration of less than 1 mg/1 approximately 64
percent of the time. Therefore, the treatment efficiency of this system
may have been adversely affected by inadequate dissolved oxygen.
An increase or decrease in temperature of a biological system will
respectively increase or decrease the efficiency of the bacteria if other
factors are held constant. The wide scattering of data shown in Figures
44-46 implies that other factors may have had a greater effect on
treatment efficiency than the effects of temperature.
The factor that affected treatment efficiency the most was the mixed
liquor detention time. This varied due to inability to control the input
of water from the leaky waterers. The detention time has a direct effect
on the efficiency of a treatment system. In each case, the trend was that
with a decrease in detention time, the percent reduction or treatment
efficiency was reduced (Figure 49). The lower efficiency in the removal
of solids, nitrogen, and COD that was caused by a reduction in detention
time was due to a number of factors. With a shorter detention time, the
microbial population would have to be increased. This increase in size
of the microbial population could only take place if there was the oppor-
tunity for solids separation and recycle. These oxidation ditches did
not have this capacity. An increase in microbial efficiency could have
occurred if the type of substrate could have been changed or the tempera-
ture increased. Neither of these factors could be controlled in these
oxidation ditches.
iv) Loss of Nitrogen - A reduction in mixed liquor detention time affects
the reduction of total nitrogen in the same manner as the other parameters,
Total nitrogen was removed from the system by two processes, nitrification-
denitrification (biologically) and ammonia volatilization (physically).
For an efficient nitrification-denitrification process to be established
while decreasing the detention time, the system would have to provide
enough oxygen to develop a large nitrifying microbial population. As
145
-------
z
o
1
r
O
O
UJ
QC
£
UJ
O
QC
UJ
Q.
90
80
70
60
50
40
30
20
10
n
«^_
^mm ^M^B)
~ X ^ KJELDAHL
4* NITROGEN
^^^
5 90
i
0 80
g
UJ 70
a:
^ 60
UJ
0 50
C£
Ul
Q. 40
m^
^* ***^*
^^^ g-*-*"^
- -**, ORGANIC
NITROGEN
-
i i i i i i i i
i i i i i i i i
04 8 12 16 20 24 28 32
. -"
i i
i i
36 4(
LIQUID DETENTION TIME,days
Figure 49. Effect of liquid detention time on
nitrogen removal.
146
-------
discussed above, the Houghton system was oxygen limiting and therefore,
as detention times were decreased, nitrification opportunities decreased.
The nitrifying population undoubtedly remained low due to the low
dissolved oxygen concentrations.
The average loss of total Kjeldahl nitrogen in the Houghton oxidation
ditches system was 42 percent. This percentage represents the amount
of total nitrogen completely lost from the system. The total Kjeldahl
nitrogen loss was approximately equivalent to total nitrogen loss since
the amounts of nitrites and nitrates in the mixed liquor were negligible.
In a system where nitrification is taking place without denitrification,
the percent of total Kjeldahl nitrogen change would be greater than that
of total nitrogen.
In the Houghton system, since there was an ammonia odor in the building
and traces of nitrites were found in the mixed liquor, the process of
ammonia volatilization and perhaps some nitrification followed by denitri-
fication were responsible for the observed loss of total nitrogen. In
both of these processes, the removal of total nitrogen depends on the
hydrolysis of organic nitrogen to ammonia-nitrogen. The organic nitrogen
hydrolysis to ammonia nitrogen remained fairly constant and averaged
approximately 65 percent. This indicates that the highest average per-
cent loss of total nitrogen by the two processes mentioned above could
be at best 65 percent. The loss of total nitrogen from the waste
handling system reached a high of 58 percent in October 1972.
Theoretical calculations were made to determine the role of ammonia vola-
tilization in the removal of total nitrogen using procedures developed
in the previous report (38). When some nitrification did occur in
October 1972, the ammonia loss due to volatilization was approximately
8.5 percent based on the equations developed earlier. However, about
83 percent of the ammonia nitrogen in October was nitrified. Since
there were only small amount of nitrites in the ditches, it can be
surmised that the process of denitrification also was taking place.
Obviously the proper conditions for an efficient nitrification-denltri-
fication process were established in the Houghton oxidation ditches
1n October and possibly in the other months of operation.
Two factors that may have contributed to a more efficient nltrification-
denitrification process have been discussed previously: temperature and
detention time. In general, treatment efficiency decreased with a
decrease ,in detention time. In October the detention time was the second
shortest during the eleven month sampling period. The effect of tempera-
ture on this sytem could not be determined from the data, but in general,
1n a biological system, the efficiency will be greater at higher tempera-
ture. The average temperature for October was the third lowest during
the study period. These facts suggest that neither temperature or
147
-------
detention time were the controlling factors that produced an efficient
nitr1fication-denitrification process in October.
A third factor is the availability of oxygen for nitrification to occur.
In an oxygen limiting system, the efficiency of nitrification would
control the overall efficiency of nitrification-denitrification. During
October the dissolved oxygen concentrations in the mixed liquor was
greater than zero mg/1 throughout the ditches for three out of the four
sampling dates. With the higher dissolved oxygen levels, the oxygen
input was greater than the demand and nitrification could be obtained.
At the same time, reduced conditions within portions of the ditches did
occur and resulted in denitrification. For at least one sampling date
each month, dissolved oxygen levels throughout the oxidation ditches for
the months of February, May, June, and July were also greater than zero.
The ammonia-nitrogen loss during these months was greater than that for
March, November, or December for which there was no evidence of dissolved
oxygen concentration being greater than zero throughout the ditches.
The availability of oxygen for nitrification in October can be inferred
from two additional factors. First, the concentration of all parameters
in the mixed liquor were at their lowest except for April, and temperatures
were fairly low, both of which would increase oxygen transfer. Second,
the percent reduction of COD was the lowest in the eleven months. This
would mean that the oxygen demand'for oxidizing organic matter was at its
lowest. Both of these conditions would increase the amount of oxygen
available for nitrification. The increased amount of oxygen available
to the system was the primary reason for the increase in nitrification
during October.
GENERAL DISCUSSION
The bench scale and pilot plant studies reported herein on the bio-
logical treatment of poultry wastewater have confirmed the previously
observed nitrogen losses under aerobic conditions (>1 mg of DO/1) and
provided information on the circumstances under which these occurred.
Similar nitrogen losses are known to occur in sewage treatment plants,
lakes, and other aquatic ecosystems presumably under aerobic conditions
(40, 41, 42). The losses of nitrogen could be due to ammonia vola-
tilization and denitrification of the oxidized forms of nitrogen into
gaseous end products. A knowledge of the conditions that control
these losses would be useful for designing and operating a treatment
system, such as the oxidation ditch for nitrogen control in addition
to preventing malodors.
Nitrogen Losses Due t£ Ammonia Volatilization
The degree of ammonia volatilization from a system depends on the
a) concentration of NH. -N, b) pH; losses being greater in the alkaline
148
-------
range particularly above pH 9, and c) degree of aeration. Everything
being equal, losses of ammonia increase with an increase in temperature.
During the start-up of oxidation ditches for treating poultry waste-
waters, the conditions for ammonia volatilization are at their optimum.
During the start-up phase relatively large concentrations of NH. -N are
available due to deamination of the organic nitrogen contained in the
poultry wastewater. The pH of mixed liquor suspensions at this time
(during start-up) is generally in the range of 8.0-9.0, which facilitates
the formation of free ammonia. This ammonia can be removed by the
aeration provided by the rotor in the oxidation ditch.
In the oxidation ditch at the Houghton Farm, odor control was achieved,
but the aeration was not adequate throughout the ditch to sustain
nitrification. The result was the occurrence of a large concentration
of NH4+-N (>2000 mg/1) in the mixed liquor and a pH within the range of
8.0-8.5. Although it was not possible to evaluate the losses of nitrogen
due to ammonia volatilization by a mass balance approach, 1t could be
predicted by the equations developed 1n another study (38). These
losses were approximately 8.5% of the total nitrogen input Into the
ditch. In the pilot plant oxidation ditch, these losses were 7.5%
and occurred during the start-up phase of the ditch when nitrification
was not yet established.
Observations revealed that relatively larger amounts of ammonia were
lost near the rotor of the Houghton Farm as evidenced by the conspicuous
ammonia odor near it in contrast to the absence of such an odor elsewhere
in the poultry house. A similar observation was made in another oxida-
tion ditch located in Manorcrest Farms, Camlllus, N.Y. This is plau-
sible since greater agitation of the mixed liquor occurred near the
rotor and hence more ammonia stripping at the rotor than at any other
location in the ditch.
In view of the operational results of the oxidation ditch, it appears
that if perceptable nitrification has to be sustained, adequate aeration
of the mixed liquor should be provided to maintain a dissolved oxygen
concentration of *2 mg/1. This will not only help decrease free ammonia
that generally occurs in the start-up phase, which may be toxic to the
nitrifying organisms, but also maintain the needed supply of oxygen
for their growth.
Nitrogen Losses Due tp_ Denltrification Under Aerobic Conditions
In the pilot plant oxidation ditch, nitrification was established after
the initial start-up phase. As a result of this nitrification, the pH
of the mixed liquor dropped below neutrality. Under these conditions,
losses of nitrogen due to ammonia volatilization were negligible since
149
-------
all the ammonia was in the ionic form. Nevertheless, a materials
balance on nitrogen indicated that about 25% of the nitrogen entering
the ditch was lost from the systems. These losses could be attributed
to the dissimilatory utilization of nitrite and nitrate for the res-
piratory activity of the microorganisms in the mixed liquor under
seemingly aerobic conditions. This observation suggests that if nitro-
gen removal from manures is contemplated as one of the goals, it can
perhaps be optimized in the ditch by increasing the probability of the
oxidized nitrogen species to be utilized as the electron acceptors
without significantly disrupting the process of nitrification. Two
ways of increasing this probability and thereby increasing the losses
of nitrogen are a) reducing the dissolved oxygen concentration in the
ditch, and b) increasing the hydrogen donating ability of the mixed
liquor. Since the latter can not be changed easily, because the input
of manure per day is relatively constant, the parameter that can be
changed is the dissolved oxygen concentration in the mixed liquor,
which can be achieved by turning off the rotor periodically.
This hypothesis has been verified in bench scale units at various
loading rates and oxygen inputs to the mixed liquor. The results of
these studies have shown that correspondingly higher losses of oxidized
nitrogen occurred as the loading rates were increased and oxygen inputs
decreased until dissolved oxygen became a limiting factor in the
reactors (Table 18). When dissolved oxygen became limiting, nitrifica-
tion ceased and accumulation of NH^-N resulted with an increase in the
pH of the mixed liquor to about 8.5, thus providing conditions conducive
for ammonia volatilization. Although nitrification ceased under these
conditions, it could be reestablished by aerating the mixed liquor to
maintain a dissolved oxygen concentration of >1 mg/1, confirming earlier
observations (38).
With the increase in the loading rate, nitrogen losses increased under
aerobic conditions because of an increase in the oxygen uptake rate of
the mixed liquor. The increased suspended solids concentration may also
have impeded the transfer of oxygen to the microbial floes, thus pro-
viding a greater probability for the N02" and N03~ to be utilized as
the electron acceptors. Thus while maintaining nitrification in a mixed
liquor, an increase in the loss of nitrogen by denitrification can be
expected when the oxygen uptake rate of a mixed liquor is increased by
increasing the loading rate. Conversely, if it is desired to minimize
nitrogen losses, and thereby conserve nitrogen, the treatment system
can be designed such that the aeration devices are sized to provide
sufficient aeration in order to minimize the probability of the utili-
zation of N0?" and N03" as electron acceptors at the expense of the
dissolved oxygen.
150
-------
Another factor that seems to influence the losses of nitrogen in a
treatment system, such as the oxidation ditch, is mixing. When the rotor
was stopped in a nitrifying oxidation ditch, the concentration of nitrates
decreased from 780 mg/1 to 260 mg/1 in about a week and remained constant
at this level for an additional week at which time the rotor was turned
on for about 30 minutes to provide mixing. In about five hours the N03~-N
decreased from a concentration of 250 mg/1 to 110 mg/1. The rates of
denitr'ification under quiescent and mixing conditions were 3.1 mg/l/hr
and 28 mg/l/hr. Prior to the mixing of oxidation ditch mixed liquor, a
blanket of sludge was noted at the bottom of the ditch, with a clear
supernatant. Since the oxidized nitrogen species are soluble and no
intimate mixing was occurring between the settled solids and the super-
natant, the N02" and NO.," remained in the supernatant and no odorous
conditions existed in the poultry house. When mixing was provided for
30 minutes, the NOg" and N0j~ in the supernatant came in contact with
the anaerobic sludge at the bottom and rapid denitrification took place
as evidenced by the higher denitrification rates. Such high denitri-
fi cation may not be observed in actual practice using in-situ denitri-
fication with continuous mixing since the conditions used in this study
were different and a sludge that settled for more than a week was brought
Into contact with the supernatant. Although an odor of hydrogen sulfide
was noticed initially, it quickly subsided during the mixing period.
The very low denitrification rates under quiescent conditions and the
odorless conditions that existed during the in-situ denitrification of
the mixed liquor may perhaps enable the storage of nitrified waste for
relatively longer periods of time. The storage period may even be pro-
longed in winter time, since the denitrification rates will be even
lower than in the spring and summer. This enables the poultry farmer
to store nitrified manure suspensions in a separate storage tank during
winter under relatively odorless conditions for extended periods without
hindering the performance of the oxidation ditch.
151
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SECTION VI
LAND APPLICATION AND CROP RESPONSE TO TREATED
POULTRY MANURE
INTRODUCTION
There has been Increasing concern on the part of commercial poultry-
men and the general public regarding odors and pollution of streams
and lakes resulting from the land disposal of poultry manure. This
problem has been accentuated 1n recent years with the increasing
number of birds in a given poultry operation. Since the land is the
utlimate disposal medium for most of this product, available land
area should be increased in proportion to the number of birds per given
poultry operation. Rural development has resulted in low tolerance
on the part of the public regarding offensive odors and water
pollution from agriculture. It is essential to improve the handling
and disposal of poultry manure. Several methods of aerobically
treating poultry wastes to control odors have been investigated at
the Cornell Agricultural Waste Management Laboratory.
It has been established that the aerobic treatment of animal wastes
can alter the kinds and amounts of various inorganic nitrogen fractions
in the material. It has not been determined how well these aerobi-"
cally treated materials will serve as plant nutrients after applica-
tion to the soil nor is their potential as water pollutants known.
Greenhouse and field studies were designed to study the behavior of
aerobically treated poultry manure. Manures from the different
treatment processes were compared with untreated manure. Initially,
the quantities of various aerobically treated wastes were limited.
This necessitated greenhouse experiments to evaluate the behavior
of the various wastes as sources of plant nutrients. These green-
house experiments also provided the opportunity to compare the effect
of different soil pH values on the plant availability of the various
N compounds in the manure. The pollution potential of these manures
was determined by measuring runoff throughout the growing season.
Runoff from field plots was collected and analyzed for nitrogen and
phosphorus compounds.
152
-------
In addition to direct economic benefits, properly utilized poultry
manure applied to the land will help avoid undue nutrient enrichment
of water courses. This same proper utilization Of poultry manure will
also help avoid the urgent need to seek new sources of plant nutrients.
Such new sources of nutrients might be most demanding in terms of
energy consumption.
Research is needed to study the response of field crops to manure
addition It is necessary to determine optimum rates and optimum
periods of application. Poultrymen realize that the nutrient content
of chicken manure can be very high relative to cattle manure-and
yield response studies with poultry manure are especially important
to producers. For those poultrymen with inadequate acreage for dis-
posal, maximum rates without crop damage is most important. The
majority of poultrymen need to determine the optimum amount to
apply to significantly increase crop yields. This is especially
true for corn.
The objectives of the studies reported here were:
1. Determine the effect of soil pH on corn response in the green-
house when extremely different rates of aerobically treated poultry
manures are applied to the soil.
2. To evaluate the effect of soil pH on inorganic nitrogen trans-
formations in the soil following the application of aerobically
treated manures.
3. Determine the rate, form and time of manure application permissible
without causing pollution of runoff waters as determined by collections
from surface runoff plots.
4. Determine maximum rate of application of poultry manure to which
corn will produce a yield response in a single application or in
cumulative applications over a period of years.
5. Determine to the extent possible through soil and plant tissue
testing the fate of nitrogen and other nutrients introduced to the
soil through land application of poultry wastes at various rates,
forms and times of application.
6. Evaluate potential or Orchard and Brome grass meadows for util-
ization of poultry manure as a fertilizer.
7. Determine optimum treatment systems for poultry wastes applied to
field crops.
153
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REVIEW OF LITERATURE
The value of poultry manure for crop production has long been recog-
nized. (53) It is a matter of record that such manures improve soil
physical condition and soil productivity. (54,55,56)
In terms of poultry manure utilization the major questions are rate
of application and also possible water pollution from such manure
application.
Recently Loehr and his associates have demonstrated that phosphorus,
ammonia, and nitrogen can be removed from poultry manure by advanced
waste treatment. (38) It then becomes a practical question of water
pollution control and management to learn how much this advanced
waste treatment will decrease runoff water contents for nitrogen and
phosphorus under a system of land disposal.
Nitrogen compounds found in poultry manure will undoubtedly go
through the same transformations as have recently been shown to be
important in fertilizer applications. (57-58) Between soil pHs
of 7-8 these transformations may involve the build up of nitrous acid
compounds which are known to be toxic to corn plants. In this study
such compounds have been observed in greenhouse studies pn corn when
poultry manure has been applied to the soil.
Organic wastes and sludges are known to have a stimulating influence
on crop growth. (59-60) Ascorbic acid, carotene, tryptophane,
tyrosine, and similar compounds are, supposedly, the sources of these
sludge growth promoting substances. It would seem reasonable to
suppose that poultry manures would generate similar growth promoting
substances.
METHODS AND MATERIALS
Three greenhouse studies were conducted to determine the effect of
different rates of aeroblcally treated poultry manure on corn growth
and nitrogen transformations in the soil. Soil pH affects were
also studied. Several soils important in Northeast crop production
were used.
Three field studies were established for the purpose of determining
nitrogen balances in corn plants, perennial forages, and the soil.
The effects of poultry manure sources and application rates on
surface runoff and corn yields were also studied.
154
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Greenhouse Experiment I
Nitrogen Transformations in the Son From Aerobically Treated Poultry
Manure --
This greenhouse study was conducted to determine the effect of different
rates of aerobically treated poultry waste on corn response and nitrogen
transformations in the soil. Two soils developed from glacial till,
Honeoye silt loam pH 7.1 and Mardin silt loam 4.2, were used. These
soils were selected because of their importance to Northeastern agri-
culture. Poultry manure sources that were used were the following:
oxidation ditch manure which was material that had been aerated by
passing the contents of a 324 cubic foot ditch through a mechanical
surface aerator; stored oxidation ditch manure which was oxidation
ditch manure that had been stored after treatment in a holding tank
under reducing conditions for 9 months; diffused air manure previously
aerated by bubbling air through the slurry of a ditch similar in size
to the oxidation ditch; and raw manure taken from a poultry house
where manure had accumulated below the poultry cages for 3 months and
to which litter had not been added. The different aeration treatments
brought about a change in the kinds and amounts of nitrogen compounds
present in the various manures. The amount of the four major nitrogen
sources in the various manure are presented in Table 25.
Table 25. AMOUNT OF EACH N FRACTION AT TIME OF APPLICATION CON-
TAINED IN UNTREATED AND TREATED FORMS OF POULTRY MANURE
(GREENHOUSE EXPERIMENT I).
Initial
composition
Organic N
NHt -N
NO" -N
N03-N
Stored Oxidation
ditch manure
83
17
0
0
Oxidation
ditch manure
49
14
35
2
Diffused
A1r manure
35
65
0
0
Raw
manure
32
68
0
0
Manure was applied to each soil at rates that would provide 0, 168,
247, 694,-and 1389 kg N/ha soil from the raw manure. All other manures
were applied at rates of 0, 280, 560, 1120 and 2240 kg N/ha. Each
greenhouse pot contained about 3000 grams of soil. Each treatment
was replicated four times. Each pot was sampled at three different
155
-------
times during the experiment and analyzed for the different inorganic
nitrogen sources listed in Table 25 and also for total soil nitrogen.
The differences in percent of nitrogen fraction noted in Table 25 can
be explained by the fact that approximately 2/3 of the N in raw manure
exists as NH4-N. Diffused air treated manure was very similar since
the treatment did little oxidation. By way of contrast the oxidation
ditch manure was effectively oxidized -- at least to the N02-N stage.
Proportional amounts of stable organic nitrogen were increased. When
oxidation ditch manure was stored, denitrification apparently elimin-
ated the N02-N.
Greenhouse Experiment II
Corn Response on Two Soils From Different Rates of Treated Poultry
Manure as Influenced by pH --
Observations made in the first greenhouse experiment suggested that
the availability of nitrogen from manure to corn and/or leaching could
be significantly affected by the soil pH. The soils used in the first
experiment were used again with the Mardin soil of pH 4.2 being limed
to achieve additional pH levels of 5, 7 and 7.2.
Three manures were used: manure treated with diffused air; oxida-
tion ditch manure and raw manure. These materials were applied to
both soils at the rates of 0, 280, 560 and 1120 kg N/ha soil. The
N content of the various manures at time of application is presented
in Table 26.
It can be noted that the percentage values for the several nitrogen
compounds in the various manure sources are somewhat different from
those reported in Table 25. The nitrogen compounds present depend
on the state of the biological environment and organisms present at
the time of sampling. The oxidation ditch material for Greenhouse
Experiment II was obtained from a 15,000 bird commercial operation.
Oxidation ditch manure used in Greenhouse Experiment I came from the
Animal Waste Laboratory on the Cornell campus. Thus, differences in
the kinds and amounts of nitrogeneous compounds can and do occur with
different operations of a given treatment system. No residual of
dissolved oxygen in the oxidation ditch slurry and a higher total
solids content can result in the presence only of organic and ammon-
ium N.
T56
-------
Table 26. AMOUNT OF EACH N FRACTION AT TIME OF APPLICATION CON-
TAINED IN UNTREATED AND TREATED FORMS OF POULTRY MANURE.
(GREENHOUSE EXPERIMENT II).
Initial Composition
Organic N
NH'-N
NO--N
Oxidation
Ditch
46
54
0
0
Diffused
Air
52
0
46
22
Raw
Manure
18
82
0
0
Again, each treatment was replicated four times and corn was grown for
42 days. Each pot was sampled three times during the growing period.
The samples were analyzed for inorganic soil nitrogen and total soil
nitrogen.
Greenhouse Exp III
Corn Response and Nitrogen Uptake From Soils Receiving Various Rates
of Oxidation Ditch and Raw Manure "~
The purpose of this study was to determine corn response, nitrogen
uptake and the behavior of nitrogen compounds in raw and oxidation
ditch manure when applied to soils in the greenhouse. The soils used
were taken from areas adjacent to field studies where poultry manure
was being applied for crop response and runoff studies. These loca-
tions were the Aurora Research Farm (Honeoye soil pH 7.1) and Ithaca
Poultry Farm (Collamer soil pH 7.2). This greenhouse study provided
the opportunity of comparing greenhouse and field results with corn
using the same soils and manure sources.
Rates of nitrogen applied from the two manure sources were 0, 112,
and 224 kg N/ha. However it should be noted that the fresh manure
application was based on previous analyses which were 1% total nitro-
gen. Subsequent analysis of this material established the total
nitrogen as 1.36%. The applied rates were in fact 152 and 304 instead
of 112 and 224 kg N/ha.
In addition a chemical fertilizer treatment of 448 kg/ha of 20-10-10
fertilizer was included as one of the treatments. Corn was then
planted in soil which was in eleven quart plastic pails serving as
greenhouse containers. Each pail contained about 10 kg of soil.
157
-------
The plants were harvested 80 days after planting. Silking had
occurred. Fresh weight and dry weight were determined. Labor-
atory analysis for TKN, was carried out on the plant materials
produced in the greenhouse.
Poultry Waste Residue Field Study
Corn Yield Response to Poultry Manure in the Year of Application
and Subsequent Residual Effects --
A field study was initiated in 1971 and was concluded in the fall of
1973. It was established at the Aurora Research Farm on a high
lime soil pH 7.0, a Honeoye silt loam. The object of this test was
to study and determine the balance of nitrogen in the corn plant and
in the soil in order that fertilization and manuring practices can
be regulated to result in the least water pollution with economic
corn production. In addition, it provided the opportunity to com-
pare manure with commercial fertilizer as a source of N.
Untreated poultry manure was applied at rates of 0, 56, 112, 224,
448 and 896 kg N/ha. A seventh treatment consisted of commercial fer-
tilizer at the rate of 22.4 kg/ha each of nitrogen, phosphate and
potash. Corn was grown and harvested.
In 1972, the original plots of this field study were split and the
same treatments repeated on one-half the original plots. Corn was
again grown on both halves of these field plots. This permitted a
measurement of residual effects of manure applied in 1971 as well as
the effects of a wide range in rates over two years. In the spring
of 1973 the sub-plots which had received 112 and 448 kg N/ha from
manure the two previous years were the only ones to receive additional
manure. The chemical fertilizer treatment was also continued at an
increased rate of 90-45-45 kg/ha of N, P, and K, respectively. See
Fig. 50.
Surface Runoff Loss Field Studies
Effects of Land Applied Poultry Waste on Runoff Losses
A field study was established in 1972 that would permit the col-
lection of surface water runoff from plots that had received appli-
cations of poultry manure. The experiment was designed to permit
the application of different rates of manure, 0, 112, and 224 kg N/ha,
from different sources, oxidation ditch and fresh poultry manure (no
litter), was applied to land for corn in both spring and fall
applications.
158
-------
NITROGEN, kg /_ho_
MANURE
CHEM
PERT
56
12
224 448 896
22
0
0
0
0
56
56
,
0
i ..
56
112
112
0
112
224
224
1
0
224
i
448
448
0
i
448
896
896
0
896
22
22
0
22
1971
1972
Figure 50. Nitrogen applied over a 2 year period as poultry manure
or chemical fertilizer, poultry waste residue study,
1971-72.
159
-------
Plots were established on a Collamer silt loam soil near the Poultry
Farm at Ithaca. Several different degrees of slope ranging from
4-10% were utilized. The experimental area had been in a grass sod
for many years prior to 1972. The chemical herbicides, atrazine
and paraquat, were applied to the soil surface 5 days prior to plow-
ing. Plowing was done within 2 days following application of the
manure. Corn was planted May 22.
Individual plots measured 3.0 m by 9.1 m and were surrounded by lawn
edging. At the base of the plot slope, collection troughs were
installed that were connected to a flow divider which diverts one-
twentieth of the entire amount of flow into a storage tank. Runoff
water was then measured and analyzed for soluble orthophosphate,
ammonium, nitrite, nitrate, total Kjeldahl nitrogen and total sol-
uble phosphorus. Sediment samples were secured and analyzed for
total phosphorus, total nitrogen and organic matter. Soil samples
were taken at weekly intervals during the period May 25 - Aug 3
from both the surface, 0-30 cm, and subsurface 30-60 cm depth.
Analysis included ammonium, nitrite, nitrate nitrogen and total
kjeldahl nitrogen.
Poultry Waste on Grasses Field Study
Yield Response of Grasses to Poultry Manure --
An additional yield study was made to determine the response of brome-
grass and orchardgrass to varying rates and different sources of
poultry manure. Applications of poultry manure were made at rates of
0, 56, 112 and 224 kg/ha N for each of fresh manure and oxidation ditch
manure. These treatments were applied both in the fall and in the spring,
Commercial fertilizer, 56 kg N/ha was used as an additional treatment.
Poultry Waste at Extreme Rates
A further study was made in Sullivan County, which has a very dense
poultry population, at the request of the county agent and in cooper-
ation with the agent. The purpose of this study was to measure the
effects of extremely high rates of poultry manure on yield and on the
soil environment.
A field that had been in continuous corn for 5 years was selected.
This small field was subdivided into fourteen plots. Each measured
11 x 44 meters (36 x 180 feet). One half of each plot (or 90 feet,
27.5 meters) on the uphill side had received 22 metric tons/ha (10
ton/acre) of cow manure the previous year. The remaining half of the
plot had no cow manure. The design consisted of two randomized
blocks. Within each block, each whole plot received one of seven
rates of poultry manure at random. These rates were 0, 24, 68, 100,
160
-------
200, 270 and 370 metric tons/ha (0, 15, 30, 45, 90, 120 and 165
ton/acre). The manure was from a pullet rearing house and the
actual weight of manure applied to each plot was determined by
weighing random loads of manure. Each load was made uniform and a
composite manure sample was secured for analysis.
Upon application, the soil was plowed, fitted and planted to corn
at an intended rate of 25,000 plants/acre. A starter fertilizer of
15-15-15 was used. Atrazine plus Lasso was applied for weed control.
The plots are located on Lackawanna silt loam. Soil samples were
taken before the addition of poultry manure but after the application
of cow manure. Topsoil (0-25 cm, 0-10 in) and subsoil (25-50 cm,
10-20 in) samples were again taken in mid- July 1973 to study the
difference in available nitrogen in each treatment.
RESULTS AND DISCUSSION
Greenhouse Experiment I
Some results of this study are presented in Figure 51 which summarizes
all measurements for a given variable.
It is apparent that the corn grown on acid Mardin silt loam (4.2)
out yielded the corn grown on neutral Honeoye silt loam by more than
100%. When one considers the source of nitrogen, raw poultry manure
is inferior. In terms of rate of application 1120 kg/ha of nitrogen
resulted in a yield decrease of corn produced in 36 days.
Fig. 52 and 53 show that NOs-N and N02-N were the most available
forms of nitrogen in the Honeoye soil (pH 7.2). However the most
abundant form on the Mardin soil (pH 4.2) was NH^-N. See Fig. 54.
Although there was little or no N02-N and NOj-N in the various manure
sources when applied to the soil, the initial analysis after appli-
cation showed various amounts present, especially in the Honeoye soil.
The manure sources were mixed with the soil and the mixture allowed
5 days to dry. Sampling for analysis was done after drying. This
amount of drying time apparently permitted the formation of N02-N
and N03~N. Fig. 55 illustrates yield response curves for* the various
treatments. Maximum dry matter yields obtained on Honeoye and Mardin
silt loam soil were 23 and 54 gms respectively, whereas check yields
were 8 and 9 gms suggesting a strong soil-manure source interaction. No
visual symptoms of nutrient deficiency were observed in plants from
either soil. On the Honeoye soil, maximum rates of oxidation ditch
(OD) and untreated or raw manure (R) greatly depressed corn yields.
161
-------
HONEOYE
MARDIN
STORED OXIDATION DITCH
OXIDATION DITCH
DIFFUSED AIR
RAW
280 kg /ha
560 kg /ha
1120 kg/ ha
2240 kg/ ha
i
J
SOURCE
RATE
0 10 20 30
DRY MATTER YIELD, gm/pot
Figure 51. Corn dry matter yields as influenced by soil,
manure source and rate of manure application.
L.S.D. @ .01 = 1.7, 2.3 and 2.3 respectively.
162
-------
HONEOYE MANURE APPLICATION, kg/ha MARDIN
300-
300-
100-
100
A.Q = 695
«I74 O«I390 d>
D*346
RAW
280 0*2240
D.560
DIFFUSED
AIR
A«0 «I
B.28O 0 1 2240
D.56O
OXIDATION
DITCH
1120
280 OB 2240
0 1960
STORED
OXIDATION
DITCH
CHECK
18 36
DAYS AFTER APPLICATION
18
a
_L
36
Figure 52. Average Honeoye and Mardln soil NO,-N concentrations
for'each manure source and each sampling.
163
-------
MANURE APPLICATION, kg/ho
RAW ALL' OTHER SOURCES
£ = 0 =695 A = 0 =1120
= 174 O=I390 B = 280 O=2240
D=348 D=560
RAW
dUU
I00(
>^
Jn ^^^^* ^^^n A. I
100
A
DIFFUS
ED AIR
1
) fT* 1 U ^ A
I. 300
o.
200
I00
-------
HONEOYE
300-
E
a
a
300
O
en
5 300
tf>
O
100
sr^-i
T i i_
MANURE APPLICATION kg /ha
A»0 695
= 174 Os|39Q
D = 348
RAW
s280 Oa2240
Q* 560
DIFFUSED
AIR
AsQ = 1120
28O O«2240
0=560
OXIDATION
DITCH
MARGIN
= 1120
s28O O«2240
Os 560
STORED
OXIDATION
DITCH
CHECK
18 36 0 18
DAYS AFTER APPLICATION
36
Figure 54.
Honeoye and Mardin soil NH.-N concentrations for
Hveraye nuneuye onu noruin SUM nn.-tN L
each manure source at 3 sampling dates.
165
-------
40
30
20
10
*
50
40
30
20
10
°(
= MARDIN o.HONEOYE
STORED OXIDATION DITCH
r /
/
*
f j
ft
RAW
s/* ~*
*^° ^^*o
III 1
) 280 560 1120 2240 174 348 695 1390
OXIDATION DITCH
- /
^°x.
DIFFUSED AlR^^^-«
/
/
-xxn_
iii -91 i i i i
>280560 1120 2240280560 1120 2240
MANURE APPLICATION, kg/ho
Figure 55. Effect of manure source and rate of application
on corn yields after 36 days growth on Honeoye
and Hardin silt loam soils.
166
-------
Yield differences within the four treatment rates of stored oxidation
ditch (SOD) and diffused air treated manures (DA) were not significant.
On Mardin soil increasing rates of application gave yields as great
or greater than those at the immediately lower rate.
Greenhouse Experiment II
Table 27 summarizes yield results and nitrogen contents from three
levels of pH with the Mardin soil series and one level with the
Honeoye series. It is apparent that six week dry matter production
yields of corn grown on all soil situations are similar except for
the Mardin series limed to pH 7.2. These yields are significantly
lower. The nitrogen content of the plants is, however, significantly
higher. (3.54%)
Table 27. DRY MATTER YIELDS AND NITROGEN CONTENT OF CORN GROWN
ON 2 SOILS AND 3 pH LEVELS. (GREENHOUSE EXPERIMENT II).
Soil Series
and pH
Mardin
pH 4.2
Mardin
pH 5.7
Mardin
pH 7.2
Honeoye
pH 7.1
Yield In Grams
per pot
20.3
20.5
11.1
19.6
L.S.D
1.1
Nitrogen Content
% N.
1.92
1.88
3.54
1.95
L.S.D.
.11
Fig. 56 demonstrates that for all soils, as rates of application of
nitrogen Increase, corn dry matter yield per pot Increased. Nitro-
gen contents of the corn plants also increased as the rate of nitro-
gen application increased. All of these differences were statisti-
cally significant.
F1g. 57 shows the interaction of soil treated at various pH values
with varying rates of manure applications for all of the sources of
manure. The most easily understood situation is the Hardin series
167
-------
CT»
00
£30
^
o>
cT
uj 20
cc
10
0
YIELD L.S.D. AT .05 = 2.8
Q PL ANT N L.S.D. AT .05 -.28
_OD DA
CHECK
OA
00
MANURE TREATMENT
OD=OXIDATION DITCH
DA=DIFFUSED AIR
R = RAW (UNTREATED)
DA
OD
DA
4.0
OD
1_
125 250
RATE OF MANURE APPLICATION, ppm
500
3.0
2.0
1.0
Figure 56. Source of manure nitrogen and rate of manure application in relation
to dry matter produced and nitrogen content of corn plants. Greenhouse
Exp. II.
-------
o
Q.
>v
E
o»
| YIELD L.S.D. AT .05 = 3.2
D PLANT N L.S.D. AT .05O2
MARDIN
MARDIN
MARGIN
HONEOYE
4.0
RATE' CK 125 250 500
pH: 4.2
CK 125 25O 5OO
5.7
CK 125 25O500
7.2
CK 125 250 500
7.1
Figure 57. Soil pH and rate of N application (kg.ha) in relation to dry matter
produced and nitrogen content of corn plants. Greenhouse Exp. II.
-------
of soils with a pH of 4.2. Under this circumstance increments of
added nitrogen from all of the various materials resulted in signifi-
cantly higher yields of dry matter produced. There are corresponding
increases in % of N with increased dry matter production. Growth
response of the corn plants on Mardin silt loam at pH 5.7 and Honeoye
silt loam at pH 7.1 are very similar. Differences between the
growth produced by the check treatment and the 125 parts per million
treatment of nitrogen are in the order of 15 grams per pot. Sub-
sequent increments of nitrogen added to these two soils result in
a much lower dry matter increment. These incremental yield
increases in the case of the Honeoye silt loam are not significant
statistically. In the case of the Mardin silt loam at pH 5.7 only
the difference in dry matter produced by 125 parts per million
as compared to 500 parts per million is significant.
The most unusual feature of this presentation is the exceedingly
low yields of corn produced on the Mardin silt loam at pH 7.2.
These low yields are associated with very high corn plant nitrogen
contents. Recently it has been shown (57-58) that nitrates can
become a problem in corn production. This is especially true when
soil pH ranges between 7-8. The nature and extent of this toxfcity
has been discussed in literature cited above.
Fig. 58 shows the relation between the various treated poultry
waste material and the soil used for greenhouse corn production.
With the Mardin silt loam soil at pH 4.2 diffused air treated manure
gave the highest dry matter yield. However, 1t did not significantly
exceed the yield from the raw manure treated soil. It should be
noted that the plant nitrogen content of the diffuse air manure was
exceedingly low 1n all soil situations except under the circumstance
of Mardin s1It loam 7.2. The Honeoye silt pH 7.1 soil treated with
diffused air poultry waste was Intermediate In nitrogen content.
However, 1t was one of the higher yielding treatments for the
production of dry matter by corn plants.
Oxidation ditch treated manure and raw manure for the Mardin silt
loam at pH 7.2 gave the lowest dry matter production. It 1s Inter-
esting that these two treatments also showed appreciable quantities
of nitrite at the end of 21 days of corn growth. This was not true
for any other treatments.
Fig. 59 and Fig. 60 show the N02-N 1n the soil treated with raw
manure and oxidation ditch manure respectively. It should be noted
that yield tends to Increase as N02-N Increases. This can be
associated with the fact that as N02-N Increases so does N03-N.
The N03 values are not shown here. Since Mh-N tends to stimulate
growth and dry matter production, the toxic influence of quantities
170
-------
o
o.
I YIELD L.S.D. AT .05=2.8
QPLANT N L.S.D. AT .05=.28
MARDIN
oo
DA
n
5.7
PH
MANURE TREATMENT
OD = OXIDATION DITCH
DArDIFFUSED AIR
R = RAW (UNTREATED)
MARDIN
00
r
DA
7,2
HONEOYE
DA
R
00
3.0
2.0
7.1
1.0
Figure 58. Soil pH and source of manure in relation to dry matter produced
and nitrogen content of corn plants. Greenhouse Exp. II.
-------
ro
RAW MANURE
Y = 7.4 + . 122 (X)
r = .60
40 60
SOIL N02-N, ppm
80
Figure 59. 42 day dry matter corn yields as influenced by soil N02-N from
raw manure 21 days after planting.
-------
-4
co
20
o
Q.
v»
E
01
**
o
_j
15
a: in
llJ IV-*
h-
<
2
O
OXIDATION DJTCH MANURE
.I34(X)
= .82
20
.L..
4O
60 80
SOIL N02-N, ppm
100
Figure 60. 42 day corn dry matter yields as influenced by soil NQ-2-N from
oxidation ditch manure 21 days after planting.
-------
Fig. 61 indicates that corn dry matter yields increased with nitrogen
levels up to 1,120 kg N/ha.
Greenhouse Exp III
Fig. 62 illustrates that soil #2, a Col lamer silt loam provided a
higher rate of nitrogen uptake per given unit of supposedly available
nitrogen than did soil #1 which was a Honeoye Lima. This resulted
in a higher dry matter production also as can be seen in Fig. 63.
The uptake on both soils was in a straight line relationship in an
upward direction, with the available soil N. There was a very
high correlation between crop uptake and dry matter produced. It
is interesting to note (in Fig. 62) the consistent relationship be-
tween treatments on both soils. Treatments 1 and 7 represent the
same treatment on 2 different soils and are in the same relative
position to the other treatments. This is true of all other treat-
ments.
Table 28 shows that the Collamer silt loam (soil #2) had an initial
soil N content that was approximately double that of the Honeoye silt
loam (soil #1). An estimation of available N from the various sources
was made as follows: 1/2 of 1% of the initial soil N + 50% of manure
N or 100% of commercial fertilizer N. These estimates of N vail ability
in greenhouse studies are consistent with estimates by other inves-
tigators including Bouldin and Lathwell (45). Ninety kg/ha of
commercial fertilizer nitrogen compared most favorably to 112 kg/ha
of nitrogen applied as poultry manure in crop uptake and in dry matter
of corn produced. This was regardless of soil. If as assumed 100% of
the commercial fertilizer N was available and only 50% of the manure
nitrogen was available this means that 56 kg/ha of manure nitrogen
produced as much dry matter as 90 kg/ha of commercial fertilizer nitro-
gen. The implications would be that either a- large percentage of the
commercial nitrogen is being lost to the environment by denitrification
or else it is not available in as desirable a form as from the manure
N. The corn was watered in such a way as to prevent any loss from
leaching.
POULTRY WASTE RESIDUE STUDY
It can be seen in Fig. 64 that shelled corn yields in 1971 increased
from 5830 to 6773 kg/ha with increasing N rates from manure of 0 to
224 kg/ha. Applications of N from manure above 224 kg/ha resulted
in yield reductions. The highest dry matter stover yields in 1971
from manure as an N source was obtained at the 224 kg/ha rate, Fig 65
The range in stover yields was 2176 to 2979 kg/ha with the highest yield
174
-------
YIELD L.S.D. AT .05 = 1.1
-2.8
PLANT N L.S.D. AT .05=. 11
2.6
2.4
2.2
100 20O 300 400 500
NITROGEN FERTILIZATION, ppm
2.0
Figure 61 Influence of nitrogen fertilization on dry matter yields and
nitrogen content of 42 day old corn plants. Greenhouse Exp. II.
-------
CROP UPTAKE VS AVAILABLE SOIL N
o>
60
40
g 20
o
cr
u_
o
UJ
120
g 80
o
40-
AURORA SOIL
_L
POULTRY FARM SOIL
Y=60.3 + .25(X)
_L
1
30 60 90 120 150
AVAILABLE SOIL NITROGEN, kg/ho
Figure 62. The relationship of nitrogen uptake by corn to nitrogen
available from soil mineralization and additions of
various amounts from various sources on 2 soils.
176
-------
125
o>
;IOO
ui
o
o
-------
00
6720
o
o>
of 5600
UJ
h-
S4480
oc
o
«3360
IT
O
f POULTRY MANURE
-
-
^fe.
-
^^M
CHEM
PERT
^H
I
56 112 224 448
APPLICATION IM, kg/ho
896
22
Figure 64. 1971 dry shelled corn yield from poultry waste residue study
L.S.D. between rates 0 .05 = 1891
-------
3360
POULTRY MANURE
CHEM
PERT
OC
UJ
2240
oc
o
(T
UJ
I
1120
56 112 224 448
APPLICATION N, kg/ha
896
22
Figure 65. 1971 dry matter yields of corn stover from poultry waste
residue study - L.S.D. between rates 0 .05 - 594.
-------
Table 28. THE EFFECT OF SOIL AND NITROGEN SOURCE ON CROP UPTAKE OF NITROGEN.
o
(S)
CM
O
OO
Treat
No.
1
2
3
4
5
6
7
8
9
10
11
12
Source
Check
Oxld. Ditch
Oxid. Ditch
Fresh
Fresh
Chem. Fert.
Check
Oxid. Ditch
Oxid. Ditch
Fresh
Fresh
Chem. Fert.
Initial
Soil N
kg/ha
2361
2032
1941
2479
2283
2364
4665
4624
4570
4810
4460
4500
Ferti 1 i zer
Nitrogen
Added
kg/ha
0
112
224
152
305
90
0
112
224
152
305
90
Assumed
Nitrogen*
Available
kg/ha
12
66
122
88
164
102
23
79
135
100
175
113
Crop N
Uptake
kg/ha
31.2
38.4
58.6
55.3
56.5
34.7
72.8
76.6
111.6
79.3
97.5
69.2
End
Soil N
kg/ha
2330
2106
2106
2576
2531
2419
4592
4659
4682
4883
4861
4659
*.005 of initial soil N + 50% of manure N or 100% of commercial N.
-------
obtained with commercial fertilizer N. All manure treatments as well
as the commercial fertilizer N treatment produced somewhat higher
yields than did the check or no N plot. Nitrogen uptake by grain and
stover is shown in Fig. 66. Grain uptake of N was greatest at 224
kg N/ha from manure
In 1972 each increase 1n poultry manure rate was reflected in an
Increase of both grain & stover. This was true of plots treated
during 1971 only, as well as plots treated both 1971 and 1972.
However, yields on the plots treated both years were consistently
though not significantly higher than those receiving only one years
treatment. See Fig. 67 and 68.
The yield range in 1972 was from 3204 - 3944 kg/ha shelled grain
on plots receiving only one year of application and from 3322-5288
kg/ha on plots receiving 2 years of the treatment. It should be
noted that the highest yields in 1972 were less than the lowest yield
in 1971. The yield from the 22 kg N/ha in chemical fertilizer was
about equal to 50-100 Ibs of N from chicken manure. Nitrogen
uptake in the grain and stover was not greatly affected by treatment
in 1971. In 1972, however, increased rates of N from poultry manure
generally resulted in increased N uptake by both grain and stover.
See Fig. 69.
Responses were obtained up to the maximum rate of N application in
1972, but not in 1971. It would appear that this was because of the
very wet spring and early summer of 1972 which leached much of the
nitrogen from the soil and depressed mineralization. Thus the high
rates in 1972 were not in excess as they appeared to be under 1971
growing conditions. It is interesting to note that the highest
N uptake in 1971 compares favorably with the highest values in 1972.
See Fig. 69.
Field Runoff Studies
Data for ammonium and nitrate nitrogen taken from soil samples
collected at intervals in the field indicated that there was a greater
accumulation of nitrates in the subsoil (30-60 cm) where fresh manure
had been applied at the highest rate when compared with oxidation
ditch manure. See Fig. 70. There was very little change in subsoil
nitrate content under oxidation ditch treatments when compared with
the check or zero manure application. Nitrate content of surface soils
also increased with time and rate to a greater extent under the fresh
manure treatments compared with oxidation ditch treatments.
Movement of ammonium nitrogen from the surface soil to the subsoil
was greatest at the 224 kg/ha application rate of oxidation ditch
181
-------
00
112
I88
o>
zf66
_i
K44
POULTRY MANURE
GRAIN
STOVER
CHEM
PERT
56 112 224 448 896
APPLICATION N, kg/ha
Figure 66. Total N in grain and stover 1971 from poultry waste residue study.
-------
00
CO
0 5040
-C
O»
^ 4480
UJ
i
b
5 3920
o:
o
z 3360
£T
0 28OO
POULTRY MANURE
~ D 971
QI97I + I972
w^^
XXXXXXXI
i
j
/
Tn
/>
^r
/
/;
^
^
/
/
/
V
X
/-
1
/
/t
/
f
/
/
/
/
/
/
CHEM
PERT
r ^
^"~
> XXXXXXXXXM
56
112 224 448
APPLICATION N,kg/ha
896
Figure 67. 1972 dry shelled corn yield from poultry waste residue study -
L.S.D. between rates § .05 = 459.
-------
00
o
o»
<£ 4480
Lu
1-
I-
i 3360
o:
a
c 224O
LU
O
w 1120
E2 1971 + 1972
POULTRY MANURE
i
^^
i
^^
i
^i
'y
71
XXXXXXXXXXN
^^"
>
\
\
CHEM
PERT
i
*
i
56 112 224 448
APPLICATION N, kg/ha
896
22
Figure 68. 1972 dry matter yields of corn stover from poultry waste residue
study - L.S.D. between rates @ .05 = 318.
-------
CO
<
POULTRY MANURE
1971+1972
l97l
112 224 448
APPLICATION N, kg/ha
Figure 69. Total nitrogen in grain and stover from 1972 waste residue
study - L.S.D. 3 .05 = grain.7.3, stover 13.4, grain and
stover 9.5.
-------
44.8
o 33.6-
**
LJ
< 22.4
LL
or
^ 11.2
0
E
o
33.6
i
O
ro
NH4-N
OXIDATION
DITCH
MANURE
-OXIDATION
DITCH
MANURE
FRESH
MANURE
FRESH
MANURE
OXIDATION
DITCH
MANURE
o
Qll2
Q224
OXIDATION
DITCH
MANURE
APPLICATION N, kg/ha
FRESH
MANURE
FRESH
MANURE
I
Fiaure 70 Surface and subsurface soil analysis. Composite
of weekly samples May 25 - Aug. 3, 1972.
186
-------
manure. Both the 112 and 224 kg/ha rates of fresh manure showed
an increase in subsoil NH4-N. At the 224 kg N/ha rate, there was
a greater accumulation of subsoil nitrates from the fresh manure
source than from oxidation ditch manure. See Fig. 70.
Due to problems associated with new installations and with flooding
which accompanied hurricane Agnes, it was decided that data enter-
pretation would best be based on 6 selected storms for which reason-
ably uniform samples were collected on all plots. These storms
comprise 2 prior to Agnes (June 4 and 16) for a total of 2.46 inches of
rainfall and 4 storms after Agnes (July 16, 25, August 4 and 7)
which total 2.03 inches for an overall total of 4.49 inches which is
nearly 1/4 of the growing season rainfall.
Results from the selected storms are presented graphically in Figs.
71-78. Again, losses in surface runoff water were greatest from the
check and low manure application rates. See Fig. 71. In Fig. 72, it
can be seen that the lowest soluble phosphorus and N03-N losses
occurred at the high rates of application of both manure sources.
Losses of NH4-N were greatest at the low application rate of fresh
manure. See Fig. 74.
The greatest.losses, particularly the sediment and its related
nutrients, were associated with fresh manure at the lowest rate of
application. These differences were not statistically significant
at the 5% level. It is possible that oxidation ditch manure and
the high rate of fresh manure provided greater bonding of soil
particles thus reducing movement of soil particulate matter.
Field Study of Grass Response to Applications of Poultry Manure
Orchard Grass
Fertilizer and manure applications were made in the Fall (Nov. 3)
and Spring (May 3). A dry matter yield response was obtained with
all rates (56, 112 and 224 kg/ha) of both sources, oxidation ditch
and fresh manure, applied either in the fall or spring. Each of the
first two harvests produced a dry matter yield increase with the
exception of spring applied commercial fertilizer which resulted in a
yield loss. The first cutting responded most to the fall applications
and the 2nd cutting responded most to the spring application. The
greatest response to fresh manure was obtained when applied 1n the
fall, however, 224 kg/ha was superior to 112 kg/ha when applied 1n
the spring. This could be due to a time factor allowing nitrogen to
be mineralized in the soil. See Fig. 79.
187
-------
Z5
. 2.0
E
o
1.5
0.5
FRESH
MANURE
CHECK
OXIDATION
DITCH
MANURE
0 112224 112224
NITROGEN APPLIED AS POULTRY MANURE, kg/ha
Figure 71. Cumulative surface runoff from 6 selected
storms as influenced by rate and type of
poultry manure. [Corrected 10% for each
1% slope difference (57)].
188
-------
V.
o>
JC
of
LJ
CO
3
(O
Q.
8
.02
LJ
_J
00
3"
CO
_l
<
OXIDATION
DITCH
MANURE
CHECK
FRESH
MANURE
0 112224 112224
NITROGEN APPLIED AS POULTRY MANURE Kg/ha
Figure 72. Cumulative soluble phosphorous losses in
runoff from 6 selected storms as influenced
by rate and type of poultry manure [corrected
10% for each 1% slope difference (57]].
189
-------
3.0-
2.0-
CO
o
1.0
OXIDATION
DITCH
MANURE
CHECK
MANURE
0 112224 112224
NITROGEN APPLIED AS POULTRY MANURE, kg/ha
Figure 73. Cumulative NOg-N losses in runoff from
6 selected storms as influenced by
rate and type of poultry manure [corrected
10% for each 1% slope difference (57)].
190
-------
.12
.10
o .08
to -06
O
Z
V .04
z
.02
n
FRESH
MANURE
OX
M
O
EC
:K
ID/
Dll
AN
*TION
rcH
URE
1
0 112224 112224
NITROGEN APPLIED AS POULTRY MANURE, kg/ha
Figure 74. Cumulative NH.-N losses in runoff from 6 selected
storms as influenced by rate and type of poultry
manure [corrected 10% for each 1% slope difference (57)],
191
-------
0 3000
o»
c/f
en 2000
O
O
w 1000
n
.
FRESH
MANURE
^uim/ OXIDATION
CHECK niTPU
. ui i i^n
MANURE
0
NITROGEN APPLIED AS POULTRY MANURE, kg/ho
Figure 75. Cumulative Soil loss from 6 selected storms as
influenced by rate and type of poultry manure
[corrected for slope differences by LS ratio (52)],
192
-------
o80
o>
JC
CO
§60
MATTER
^
0
ORGANIC
ro
D 0
FRESH
N
O
-------
o
JC
01
^2.00
of
D
DC
O
I
Q.
o'-50
X
Q.
z
LJ
1 1.00
0
| .50
r>
FRESH
MANURE
-
0
-------
5.0
o
cc
4.0
UJ
1 3.0
O
<5 2.0
CHECK
OXIDATION
DITCH
MANURE
FRESH
MANURE
0 112 224 112 224
NITROGEN APPLIED AS POULTRY MANURE, kg/ha
Figure 78. Cumulative total nitrogen loss 1n sediment from 6 selected
storms as Influenced by rate and type of poultry manure
[corrected for slope differences by LS ratio (52)].
195
-------
90OO
80OO
0
^,7000
cT
deooo
5000
4000
FALL
ox
DATION
DITCH
IV
1ANURE
I
-
S
/
/
/
/
/
/
/
/
/
/
FRESH F
MANIIRF
i
;\
^
\//////////s
'/.
'i
't
\
y
^
X
\
V
X
?A
CHEM
FERT
rr~\
'*
SPRING
224
1.
OXIDATION
DITCH
MANURE
i
y
/
/
/
/,
'/
i
FRESH
MANURE
i i
"\
\
\J
\
X
\
\
\^
\
\
X
/
/
/,
\
^
^
CHEM
FERT
7
Y/
/
/,
ty
Figure 79. A comparison of the effects of 2 forms, 3 rates, and 2 times
of application of poultry waste and commercial fertilizer on the
yield of orchard grass (1st & 2nd cutting 1973) L.S.D. between
rates @ .05 = 1225.
-------
Brome Grass --
There were no significant yield responses to either source at any
rate at any time of application when compared with the zero treatment.
There was a slight response, however, to the two highest rates of
oxidation ditch material when applied in the fall and the highest rate
when applied in the spring. The upper rate of fresh manure produced
a slight response when applied in the fall, but none when applied in
the spring. There was little or no response to chemical fertilizer at
either time of application, Fig. 80.
These materials had to be surface applied without benefit of soil
incorporation. The oxidation ditch material, being more liquid,
penetrated into the root zone more easily than the fresh manure which
was more viscous. Spring application of the fresh manure resulted in
a substantial amount of the young foliage being covered for a time
with manure. There were no visual symptoms of foliage "burning". The
time of application, however, was sufficiently late that soil water
movement downward would tend to limit the movement of nutrients into
the deeper root zone. It should also be noted that this experiment
had only two replications so that the information here presented only
serves as a guide for further study.
Sullivan Co. Study
The composition of the manure used in this experiment is presented in
Table 29 along with the actual amounts of N, P and K added per ton of
fresh manure. The response of corn to varying rates of this manure is
given in Table 30. Each observation as illustrated in the upper
portion of the table is comprised of two replicates. The mean for each
factor is given in the lower segment of the table. It*is evident from
the data in Table 30 that the addition of cow manure the previous year
had only a small and insignificant influence on increasing corn yields
when making a comparison over all rates of poultry manure.
The yield of both grain and silage did not show a significant response
to poultry manure as compared to the check plot for rates not exceeding
200 tons/ha. Apparently the addition of a starter fertilizer of 7-7-7
kg of N - P205 - K?0 in itself and the availability of these elements
from the soil by the mechanism of mineralization was sufficient to
produce respectable yields. A significant negative response is evident
for rates exceeding 200 tons/ha (90 tons/acre).
The effects of rate of manure application on plant population and yield
are illustrated in Fig. 81. Inorganic N levels in the topsoil and sub-
soil are illustrated in Fig. 82.
197
-------
C»
FALL
7000k
6000!-
5000
40OOh
OXIDATION
DITCH FRESH
MANURE MANURE
/'
y.
V
SPRING
RATE-kgN/ho
CHECK
056
S3 CHEM
N FERT
!
OXIDATION
DITCH
MANURE
FRESH
MANURE
CHEM
PERT
Figure 80. A comparison of the effect of 2 forms, 3 rates and 2
times of application of poultry waste and commercial
fertilizer on the yield of bromegrass (1st and 2nd
harvest 1973) L.S.D. between rates @ .05 = 1939.
-------
10
O>
PLANT POPULATION,
L.S.D. AT .05=9.1
I ELD,
L.S.D. AT .05=1254
34
-20
- 10
68 100 134 168 200 235 270 302 336 370
POULTRY MANURE, metric tons/ha
Figure 81. A comparison of corn grain yield and plant population as influenced
by additions of poultry manure.
-------
500
400
TOPSOIL (0-25 (
L.S.D. AT .05 = 285
- 300
PO
o
o
CD
OC
a
200
100
34 68
0 SUBSOIL (25-50 cm)
L.S.D. AT .05 = 56
L
100 134 168 200 235 270 302 336
POULTRY MANURE, metric tons/ha
370
Figure 82. Inorganic -N concentrations in soil as influenced by rate
of poultry manure additions. Sampled 7/IS/73.
-------
ro
o
Table 29. COMPOSITION OF PULLET MANURE ON A DRY WEIGHT BASIS
HgO Total N
t
kg/dry metric
ton
Ibs/dry ton
52 4
47
95
.77
.7
.4
NH4-N
1
12
25
.27
.7
.4
P
0.85
8.5
16.9
K CaC03
1.92
19.2
38.4
6
62
124
Equiv.
.2
.0
.0
Soluble Salts
NaCl Equiv.
3.
32.
65.
25
5
0
pH
6.7
-------
Table 30. CORN YIELD DATA AS INFLUENCED BY 1973 POULTRY MANURE
ADDITIONS.
Rate, Cow Manure (72)
kg/ha Addition, 22 t/ha
0
34
68
100
200
270
370
Cow
Manure
Rate,
kg/ha
L.S.D@5$
For Rate
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
0
34
68
100
200
270
370
Grain,
kg/ha @15%
5770
4892
6021
5017
6335
5393
5833
5896
5457
5896
3889
4515
2634
2885
MEANS
5134
4928
5331
5519
5864
5865
5677
4242
2760
1254
Silage ,
t/ha @75%
38.1
33.8
38.3
33.2
43.5
36.1
36.1
36.3
32.0
37.6
25.5
26.7
17.2
18.8
33.0
31.8
36.0
35.8
39.8
36.1
34.7
26.1
18.0
7.2
Population
Plants/ha x 10'
55.1
52.6
51.9
53.4
56.1
55.6
54.3
58.5
52.1
57.1
42.0
47.4
24.9
38.5
48.0
51.9
53.9
52.7
55.9
56.4
54.6
44.7
31.7
9.1
Non-significant difference @ 5% level
202
-------
The fertility status of the soil before poultry manure was applied is
presented in Tables 31 and 32. It is evident that the prior soil
fertility status for each treatment area was essentially identical,
since there were no significant differences in the amounts of organic
matter, N, P, and K present. Any fluctuation in yield between treat-
ments should unquestionably be a function of the rate of the poultry
manure applied.
The yield of corn appears to be closely related to the stand count.
See Fig. 81. Both yield and stand count decrease with additions
exceeding 200 tons/ha (90 ton/acre). It would seem logical that the
yield would increase with increasing increments of poultry manure
because of the addition of increasing rates of the primary plant
nutrients, especially nitrogen. See Fig. 82. In view of this,
it is interesting to note that there is a negative relationship
between available nitrogen (inorganic N), yield and plant population.
Apparently, either a toxic level of a certain form of nitrogen is
coming into play at the higher rates and/or salt concentration is
having an adverse effect.
SUMMARY
A series of greenhouse studies were made using three representative
soils. In one of these soils the pH was adjusted to range from 4.1
to 7.2. A series of studies on poultry manure rate applications were
made on the various soils and at the various pH levels. The attempt
was to determine the best possible rate of applying treated and
untreated poultry manure. Acid soil conditions resulted in the
nitrogen in the poultry manure being held much more firmly against
the forces of leaching and nitrification as compared to neutral pH
values for the soil.
Greenhouse corn growth and dry matter increased in accordance with
rates of nitrogen fertilizer applied in the poultry manure. For
certain treatments of oxidation ditch treated manure and raw manure
at pH 7.2, N02 ions accumulated in the soil and became toxic to the
corn plants. In general there was limited variation in dry matter
corn yields produced by the various treated manures. At higher rates
of application raw manure was a poorer source of nitrogen than were
treated manures.
Field studies were conducted on the residual benefits of poultry
manure applied to corn as a fertilizer. These tests were made by
applying poultry manure to corn plots at varying rates during the
year 1971.
203
-------
Table 31. SOIL ANALYSIS OF TOPSOIL (0-25 cm) TAKEN PRIOR TO POULTRY
MANURE ADDITIONS AND CORN PLANTING.
Rate,
t/ha
0
34
68
100
200
270
370
Cow
Manure
Rate,3
t/ha
Cow Manure (72)
Addition, 22 kg/ha
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
0
34
68
100
200
270
370
O.M.,
%
4.5
4.3
4.5
4.5
4.4
4.5
4.9
4.4
4.4
4.9
5.0
4.5
4.4
4.2
MEANS
4.6
4.5
4.4
4.5
4.5
4.7
4.7
4.8
4.3
P,
ppm
11
7
10
9
15
13
15
9
9
12
17
12
12
9
13
10
9
10
14
12
11
15
11
K,
ppm
153
138
142
141
143
142
159
149
149
171
199
165
151
149
157
151
146
142
143
154
160
182
150
Total -N,
ppm
1963
1937
1913
2045
1900
2035
2050
1850
2000
2250
2250
2065
1900
1850
1997
2005
1950
1979
1968
1950
2125
2158
1875
Soluble Salt
NaCl Equiv. %
.009"
.011
.012
.026
.009
.015
.013
.007
.011
.015
.020
.016
.011
.013
.012
.015
.010
.019
.012
.010
.013
.018
.012
Non-significant @ 5% level.
204
-------
Table 32. SOIL ANALYSIS OF SUBSOIL (25-50 cm) TAKEN PRIOR TO POULTRY
ADDITION AND CORN PLANTING.
t/ha
0
34
68
TOO
200
270
370
Cow
Manure
Rate,3
kg/ha
Cow Manure (72)
Addition, 22 kg/ ha
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
Yes
No
0
34
68
100
200
270
370
O.M.,
%
2.0
1.2
1.4
1.3
2.2
1.7
0.9
0.9
1.5
1.6
1.6
1.7
1.5
2.1
MEANS
1.6
1.5
1.6
1.4
2.0
0.9
1.6
1.7
1.8
P,
ppm
2.5
1.0
2.0
1.5
4.0
2.0
1.0
1.5
1.5
2.5
2.0
3.5
2.0
2.0
2:1
2.0
1.8
1.8
3.0
1.3
2.0
2.8
2.0
K,
ppm
76
61
58
55
83
63
51
63
63
79
91
73
69
70
70
66
69
57
73
57
71
82
70
Total -N,
ppm
987
950
763
687
1025
875
575
675
700
815
775
875
800
1025
804
843
969
725
950
625
758
825
913
Soluble Salt
NaCl Equiv. !
.0035
.0030
.0020
.0010
.0055
.0010
.0010
.0010
.0030
.0055
.0010
.0030
.0010
.0030
.0024
.0025
.0033
.0015
.0033
.0010
.0043
.0020
.0020
Non-significant @ 5% level.
205
-------
Yield response varied with the season. Maximum yields were obtained
with 100 Ibs of nitrogen in 1971 and up to 800 Ibs nitrogen in 1972.
In 1972 these plots were divided so one portion could be manured and
one portion could be left unmanured. A comparison of corn yields
showed that the residual influence of the previous years manuring
was great enough so that 80-90% of the corn yield was sustained
without additional manure application. Additional information on
fertilizing corn with poultry manure was obtained from a field trial
in cooperation with a county agent. It was apparent from this field
trial that applications of poultry manure in excess of 30 tons per
hectare on corn greatly depressed corn yields. This yield depression
was associated with increased salt content of the soil.
Additional soil fertility trials were made with Orchard grass and
Bromegrass. Varying rates of oxidation ditch treated manure and raw
poultry manure were applied both spring and fall on these two grasses.
There was a statistically significant yield increase with Orchard grass
for applied poultry manure. This increase was greater for fall applied
manure. In the case of Bromegrass there was no yield increase for
poultry manure applied spring or fall.
A series of runoff measuring plots were installed. Corn was grown on
these plots. There were no significant differences in runoff values
for water soluble phosphorus, nitrate, or ammonium ions. Also, there
were no differences in the solid phase of these substances lost from
the plots.
206
-------
SECTION VII
REFERENCES
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3. Eckenfelder, W.W., Jr. Theory of Biological Treatment of Trade
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5. Eckenfelder, W.W., Jr. Industrial Waste Pollution Control.
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207
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10. Garrett, M.T., Jr. and C.N. Sawyer- Kinetics of Removal of Soluble
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1958.
12. Kountz, R.R. and C. Forney, Jr. Metabolic Energy Balances in a
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Extended-Aeration Wastewater Treatment Units. Jour. Water Poll.
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16. Gaudy, A.F., Jr., et, al_. Studies on the Operational Stability of
the Extended Aeration Process. Jour. Water Poll. Control Fed.
42:165-179, 1970.
17. Gaudy, A.F., Jr., et a]_. Studies on the Total Oxidation of Activated
Sludge With and Without Hydrolytic Pre-Treatment. Jour. Water Poll.
Control Fed. 43:43-54. 1971.
18. Yang, P.Y. and Gaudy, A.F. Control of Biological Solids Concen-
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Industrial Waste Conf., Purdue University, Lafayette. May 1-3, 1973).
19. Herbert, D., et al_. The Continuous Culture of Bacteria; A Theore-
tical and Experimental Study. Jour. Gen. Microbiology. 14:601-622,
1956.
20. Herbert, D. A Theoretical Analysis of Continuous Culture Systems.
Soc. Chem. Ind. Monograph No. 12. 1956. p. 20-53.
21. Novick, A. Srowth of Bacteria. Ann. Review of Microbiology.
9:97. 1955.
22. James, T.W. Continuous Culture of Microorganisms. Ann. Rev.
Microbiology. 15:27-46. 1961.
208
-------
23. Rao, B.S. and A.F. Gaudy, Or. Effect of Sludge Concentration on
Various Aspects of Biological Activity in Activated Sludge.
Jour. Water Poll. Control Fed. 38:794-812. 1966.
24. Hetling, L.J., e_t a]_. Kinetics of the Steady-State Bacterial
Culture, II. Variation in Synthesis. Proceedings of the 19th
Purdue Industrial Waste Conference, Purdue Univ., Lafayette.
p. 687-715. 1964.
25. Moustafa, H.H. and E.S. Collins. Molar Growth Yields of Certain
Lactic Acid Bacteria as Influenced by Autolysis. Jour. Bacteriol
96:117-125. 1968.
26. Gaudy, A.F. Jr. and M. Ramanathan. Variability in Cell Yield for
Heterogeneous Microbial Populations of Sewage Origin Grown on
Glucose. Biotech, and Bioengineering. 13:113-123. 1971.
27. Chiu, S.Y., et. al_. Kinetic Behavior of Mixed Populations of
Activated Sludge. Biotech, and Bioengineering. 14:179-199. 1972.
28. Chiu, S.Y., et al_. Kinetic Model Identification in Mixed
Populations Using Continuous Culture Data. Biotech, and Bio-
engineering. 14:207-231. 1972.
29. Grady, C.P.L., e_fc a]. Effect of Growth Rate and Influent Substrate
Concentration on Effluent Quality from Chemostats Containing
Bacteria in Pure and Mixed Culture. Biotech, and Bioengineering.
14:391-410. 1972.
30. Burkhead,. C.E. Evaluation of CMAS Design Constants. (Presented
at International Conference sponsored by the International
Association on Water Pollution Research (IAWPR) at Atlanta, Ga.
October 5-6, 1972).
31. Goodman, B.L. and A.J. Englande. A Consolidated Approach to Activated
Sludge Design. (Presented at an International Conference Sponsored
by an International Association on Water Pollution Research (IAWPR)
at Atlanta, Georgia, October 5-6, 1972).
32. Eckenfelder, W.W., Jr., et. al_. A Rational Design Procedure for
Aerated Lagoons Treating Municipal and Industrial Wastewaters.
(Presented at the 6th International Water Pollution Research
Conference. Proceedings published by Pergamon Press, Ltd.,
June 18-23, 1972).
33. Toward a Unified Concept of Biological Wastewater Treatment Design.
An International Conference sponsored by the International Associa-
tion on Water Pollution Research at Atlanta, Georgia. October
5-6, 1972.
209
-------
34. Loehr, R.C. Liquid Waste Treatment, I. Fundamentals, II.
Oxidation Ponds and Aerated Lagoons;. III.- The (bddatton Ditch.
Cornell University Conference oh Agricultural Waste Management.
Ithaca, New York. 1971. P. 54-78.
35. American Public Health Association. Standard Methods for the
Examination of Water and Wastewater. 12th ed. 1965.
36. Jeris, J.S. A Rapid COD Test. Water and Wastes Engineering.
4:89-91. 1967.
37. Loehr, R.C., D.F. Anderson, A.C. Anthonisen. An Oxidation Ditch
for the Handling and Treatment of Poultry Wastes. Proceedings:
International Symposium on Livestock Wastes, ASAE. 1971. p. 209-212.
38. Loehr, R.C., et al. Development and Demonstration of Nutrient
Removal from flmrnal Wastes, EPA - R2-73-095. January 1973.
39. Prakasam, T.B.S., ejt al_. Evaluation of Methods for the Analysis
of Physical, Chemical and Biochemical Properties of Poultry
Wastewaters. (Paper presented at Pre-ASAE Meeting, held at
Chicago, Dec. 1972).
40. Gayon, V. and G. Dupetit. Recherches sur la Reduction des
Nitrates par les Infiniments Petits. Soc. Sci. Phys. Nat.
Bordeaux. Ser. 13, 2:201-207. L886.
41. Wuhrmann, K. Nitrogen Removal in Sewage Treatment Processes.
Verh. Int. Verein. Limnol. 15:580-596. 1964.
42. Jones, P.M. and N.K. Patni. The Fate of Nitrogen and Phosphorus
in an Oxidation Ditch Treating Swine Wastes. A Study of a Full-
Scale Swine Waste Disposal System. Water Res. 6:1425-1432. 1972.
43. Baker, D.R. Oxygen Transfer Relationships in a Poultry Waste
Mixed Liquor. M.S. Thesis. Cornell University, Ithaca, N.Y. 1973.
44. Anderson, D.F. Unpublished Data. 1972.
45. Bouldi'n, D.R. and D.J. Lathwell. Behavior of Soil Organic Nitrogen.
Cornell University Agr. Exp. Sta. Bull. 1023. Dec. 1968.
46. Bremmer, J.M. Analysis of Total Nitrogen and Inorganic Forms
of Nitrogen. In: Methods of Soil Analysis. Am. Soc. Agron.
Madison, Wisconsin, 1965. p. 1149-1232.
47. Buckman, H.O. and N.C. Brady. The Nature and Properties of
Soils. MacMillan, 7th ed. 1969.
210
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48. Cline, M.G. Soils and Soil Associations of New York, Cornell
Ext. Bull. 930, 1963.
49. Greweling, T. and M. Peech. Chemical Soil Tests. Cornell Ur\iv.
Agric. Exp. Sta. Bull. 960, 1965.
50. Loehr, R.C. and S.D. Klausner and T.W. Scott. Disposal of
Agricultural Wastes on Land. In: 4th Environmental Eng. Conf.,
University of Montana. Feb., 1973.
51. Webber, L.R., T.H. Lane and J.H. Nodwell. Guidelines to Land
Requirements for Disposal of Liquid Manure. In: 8th Industrial
Water and Waste Water Conf., Lubbock, Texas. June 1968.
52. Wischmeier, W.H. and D,C. Smith. Predicting Rainfall-Erosion
Losses from Cropland East of the Rocky Mountains. U.S.D.A.,
A.R.S., Agr. Handbook No. 282. 1965.
53. Dyal, R.S. Agricultural Value of Poultry Manure. National
Symposium on Poultry Industry Waste Management, Lincoln:
University of Nebraska. 1963.
54. Schumaker, G.A., C.W. Robinson, W.D. Kemper, H.M. Golus and
M. Amemiya. Improved Soil Productivity in Western Colorado
With Fertilizers and Alfalfa. Fort Collins: Colorado
Agricultural Experiment Station Tech. Bulletin 91, 1967.
55. Benne, E.J., C.Hoglund, E.D. Longueker, and R.L. Cook. Animal
Manures, What are They Worth Today. East Lansing: Michigan
Circular Bulletin 231, p. 6. 1961.
56. Salter, Robert M. and C.J. Schollenberger. Farm Manure. Columbus:
Ohio Agricultural Exp. Station Bull. 605, 1939.
57. Wetselaar, R., J.B. Passioura, and B.R. Singh. Consequences of
Banding Nitrogen Fertilizers in Soil. I. Effects of Nitrification
Plant and Soil. 26:159-175, 1972.
58. Passioura, J.B., and R. Wetselaar. MS1685. Consequences of
Banding Nitrogen Fertilizers 1n Soil. II. Effects on the Growth
of Wheat Roots. Plant and Soil. 36:461-473. 1972.
59. Anderson, M.S. "Sewage Sludge for Soil Improvement" U.S.D.A.
Circular No. 972. pp. 1-27. (1955).
60. Rudolfs, W. and B. Heinemann. "Growth Promoting Substances in
Sewage and Sludge. III. Vitamin C., Carotene, Amino Adds,
Fatty Acids and Naphthyl Compounds" Sewage Wks. J. 11, 527-594, 1939.
211
-------
SECTION VIII
APPENDICES
TABLE TITLE PAGE
Al Solids Accumulation in a Continuously Filling 213
Reactor with no Intentional Wastage of Solids
A2 Nitrogen Balance Data and Profile of Oxidation 216
Ditch Operation
212
-------
Table Al. SOLIDS ACCUMULATION IN A CONTINUOUSLY FILLING REACTOR
WITH NO INTENTIONAL HASTAGE OF SOLIDS
The solids entering the ditch are comprised of degradable and non-
degradable fractions.
If 'f is the fraction of degradable solids then the quantity of non-
degradable solids is C.. (1-f); where C. is the total concentration of
solids.
Total solids concentration
i .e.
'i
concentration of degradable solids
+ concentration of non-degradable solids
[C..f)] + [C.(l-f)]
i i
degradable non-degradable
As manure is added daily to the oxidation ditch, the non-degradable
solids accumulate and the degradable solids fractions that are added
daily are in varying stages of degradation. The concentration of total
solids after the time 't1 can be calculated if the rate of decomposition
of degradable solids is known. It is assumed that this follows first-
order reaction kinetics such that
St = SQ . exp (-kt)
where St and S are the concentration of degradable solids at time:
and zero, 'k1 is the rate constant.
Therefore, the total solids content after 't' days of addition is:
C^
't'
(quantity of inert solids) + (quantity of the
degradable solids
in the system)
(C. =
ci
f {e"kt+ e"k
1} + inert solids
Degradable solids of 1st addition re-
maining after 't' days plus degradable
solids of 2nd addition'remaining after
't1 days plus degradable solids
added on the day 1
+ inert solic
= C
i
e"kt (l+ek +e2k + - etk) + inert solids
213
-------
This is a geometric series of the sum
= a
p-kt _k
- C.f .{ - ~T-* } + inert solids
1 l-eK
= C.f .{ - r - }+ inert solids
1 l-e"K
i e-k (t+1)
C. (l-f) . t
l-e~ 1
If the rate constant is expressed to the base 10; then
1 !Q-k
Ct = C.f . [1J5 - ] + C (l-f) t
1 1 1-10"K 1
f
Using the value of k = 0.161 ay~ as obtained in this report, and
assuming C^ = 0.855 g/liter and assuming that 75% of this is degradable
C.(0.75)(0. 99958)
Ct after 20 days = - + 0.25 C. .20
1 0.3098 1
= 6.3298 g/liter
Ct after 30 days = 8.463 g/liter
Ct after 40 days = 10.595 g/liter
Thus, in the operation of an oxidation ditch it will take 40 days to
reach a 1.1% solids concentration.
Use of_ the above Equation for the Verification of the Total Solids
Balance i_n the Pilot Plant Oxidation Ditch;
Total solids contributed from 227 birds
C. = 0.6525 g/l/day
Total period of operation (t) = 276 days
Final concentration of total solids = 8.5% (85 g/1)
Assuming k = 0.161 per day, what would be the
value of f? (i.e., fraction that is degradable)
214
-------
Using the equation:
-k
Ct = C. . f { __ } + c. (1-f) t
I 1 10
, ln-.161 (276 + 1)
85 = (0.6525) . f . {^^ }
1-10 °'161
+ 0.6525 . (1-f) . 276
f = 0.534 or 53.4%
The observed loss in total solids was 53%(44). The predicted value
is in good agreement with the observed value, suggesting that the
models developed in this section can be used satisfactorily for the
production of solids accumulation in a continuously filling reactor
with no intentional waste of effluent.
215
-------
Table A2. NITROGEN BALANCE DATA AND PROFILE OF OXIDATION DITCH OPERATION
ro
Nitrogen
Input
(gm)
3127
1876
2502
625
1251
2502
1876
2502
1876
4378
2502
1876
2502
1876
2502
4378
1876
4378
2502
1876
2502
Nitrogen
Output
(gm)
0
0
0
0
1584
2567
1287
1520
828
2041
1358
985
1255
1281
1824
3819
1544
3550
1887
1512
2010
Estimated
N- Input
(1-2)
3127
1876
2502
625
-333
-65
589
982
1048
2337
1144
891
1247
595
678
559
332
828
615
364
492
Total N
in Ditch
(gm)
2975
3634
4749
4690
4570
2362
2215
2186
2277
2532
3163
3003
3258
3759
3673
3290
3168
3134
3242
3168
3465
Observed
Change of
N in Ditch
497
659
1115
-59
-120
-2208
-147
-29
91
255
631
-160
255
501
-86
-383
-122
-34
108
-74
297
Loss of
N, gm
(3-5)
2630
1217
1387
684
-213
2143
736
1011
957
2082
513
1051
992
94
764
942
454
862
507
438
195
Time
Period
(days)
5
3
4
1
2
4
3
4
3
7
4
3
4
3
4
7
3
7
4
3
4
N- Loss
per day
(gm)
526
406
347
684
-107
536
245
253
319
297
128
350
248
31
191
134
151
123
127
146
49
Period
Initial Filling
Period
Oct. 19 - Nov. 1, 1972
Flow- through
Period
Nov. 1, 1972 -
Jan. 9, 1973
-------
Table A2. NITROGEN BALANCE DATA AMD PROFILE OF OXIDATION DITCH OPERATION (continued)
Nitrogen
Input
(gin)
1876
1876
2502
1876
2501
Nitrogen
Output
(gm)
0
0
0
0
0
Estimated
N- Input
(1-2)
1876
1876
2502
1876
2501
Total N
in Ditch
(gm)
3588
3624
4247
5049
7313
Observed
Change of
N in Ditch
123
36
623
802
2264
Loss of
N, gm
(3-5)
1753
1841
1879
1074
237
Time
Period
(days)
3
3
4
3
4
N- Loss
per day
(gm)
584
614
470
358
59
Period
Denitrifi cation
oeriod
without flow- through
operation
1876
ro
1876
8545
1232
644
215
5003
4324
1197
5003
2394
1796
2394
1796
2394
1796
2394
1796
2394
1796
2394
5010
4167
1046
4448
1868
1439
2109
1585
1736
1239
1743
1351
1725
1214
1534
-7
157
151
555
527
357
285
211
658
557
651
445
669
582
860
5771
6421
6166
5041
4648
5178
5691
4991
4786
4518
4647
4457
4150
3827
3923
-2774
651
-256
-1125
-394
530
513
-700
-204
-268
129
-190
-307
-324
97
2767
-494
407
1680
921
-173
-228
911
862
825
522
635
976
906
763
8
7
2
8
4
3
4
3
4
3
4
3
4
3
4
346
71
204
210
230
-58
-57
304
216
275
131
212
244
302
191
Second filling period
w/o flow-through
Jan. 25 - Jan. 30, 1973
Second flow-through
period
Jan. 30 - April 3, 1973
-------
Table A2. NITROGEN BALANCE DATA AND PROFILE OF OXIDATION DITCH OPERATION (concluded)
Nitrogen Nitrogen Estimated Total N Observed Loss of Time N- Loss
Input Output N- Input in Ditch Change of N, gm Period per day
(gm) (gm) (1-2) (gm) N in Ditch (3-5) (days) (gm)
Period
599
599
599
599
1197
598
397
386
364
337
657
314
202
213
235
262
540
284
3804
3520
3225
3500
3312
3476
-119
-284
-295
275
-189
165
321
497
530
-13
738
119
1
1
1
1
2
1
321
497
530
-13
369
119
Second
period
Apri 1
denitrification
3 - April 9, 1973
ro
oo
-------
SELECTED WATER
RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
/. Rep..'tIf9.
w
4. Title
Design Parameters fox Animal Waste Treatment Systems
: S,
T.B.S. Prakasam, R.C. Loehr, P.Y. Yang,
T.W. Scott and T.W. Bateman
9. Organization Agricultural Waste Management Program
College of Agriculture and Life Sciences, Cornell Univ.
Ithaca, New York 14850
Orgaai>«tJon
10. Project Wo.
I!. Contract/Grant No.
S800767
13. sponsoring Orgitnizaiwn Environmental Pr6tection Agency
75. Supplementary Notes
3. Typei 'Repot an
------- |