PB-22J 621
A RECIRCULATING WASTE SYSTEM FOR SWINE
UNITS
J. R. Miner
Iowa State University
Prepared for:
Office of Research and Development
1973
D'^TRIBUTED BY:
Nations! Technics! Infomutisn Service
U. S. BFPARTMT OF CGKRCE
5285 Port Royal Road, Springfield Va. 22151
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BPA-670/2-73-025
j
1 .. - July 1973
PB 221 621
A RECIRCULATING WASTE SYSTEM
FOR SWINE UNITS
By
J. R. Miner [
Department of Agricultural Engineering J
Iowa State University |
Ames, Iowa 50010 {
Grant No. EP-00283
Program Element No. 1D2063 {
Project Officer
Harry Stierli
Solid Waste Research Laboratory
National Environmental Research Center
Cincinnati, Ohio 45268
Bvproducrd by
NATIONAL TECHNICAL
INFORMATION SERVICE
U 5 Pppatlfnent of Commerce
Spiinadeld VA3215I
Prepared for
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON, D.C. 20460
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o c,saa .n......c __ .. .
16. /tbstact.
The purpose of this project was to develop and characterize a swine
manure management system. The goal of the system was to collect,
transport, treat, reuse and dispose of the manure in such a way that
it would be compatible with current confinement swine production sys- -
tems, yet minimize both labor and pollution potential. Such a system
was devised and evaluated. Its basis was to hydraulically flush manure
from shallow dunging gutters with the treated wastewater. The treat-
n ent devices evaluated included an anaerobic lagoon and an oxidation
ditch. Excess water from the system was applied under controlled ob-
servation to adjacent cropland using conventional sprinkler irrigation
equipment. The overall validity of this concept was proven.
17b . Identifiers/Op en-Ended Terms *
*Swjne wast s, Reuse, Oxidation ditch, Chemical oxygen demand, Solids
reduction, Irrigation disposal, Solid waste management, MaDure haul-
ing, Ditch pump, Flush tanks, Soil prep& :ation
BIBLIOGRAPIIJC DATA I. Report No. 2.
SHEET EFA670/2-73-025
3. recipients Accession No.
-J
4. 1 icic. and Subtitle
A RECIRCULATING WASTE SYSTEM
FOR SWINE UNITS
.
S. kepori Date - -
l973-issuing date
6.
7. Author(s)
J. R. Miner
8. Jeriorming Orjηanisation Kerr.
No.
9. Pctlnimrng Organization Name und Address -
Dep:rtment of Agricultural Engineering
Iowa State University
Ames, Iowa 50010
10. Pro,ect/rask/Worlc Unit No.
.
11. Conuact/Grant No.
EP-00283
12. Sponsor in Organi.t.ition Name and Address
U.S. Environmental Protection Agency
National Environmental Research Center
Office of Research and Development
Cincinnati, Ohio 45268
13. T pc of Report & Period
Covered
Fi 1
14.
15. Supplementary Notes
17. K. y ords and Document Analysis. lla.I)eccripcors
Swine, Ditch, Lagoons, Biochemical oxygen demand, Waste treatment,
Waste water, Soil water percolation, Effluents, Drain tiles, knmonia
17c. COSAT! Ficld/GOLp 13B
18. Availabilay Statement 119. Security Class (This 21. No, of Pages
I Report)
UNCLASSIP1I1D I 2 5-1 .2ηiJ
20. Security Class CThus 122. Puce
Pane I
Release to Public UNCLASSIFIED I
FORM NTISS IRCV. 3-721 2 1. -
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REVIEW NOTICE
The Solid Waste Research Laboratory of the National
Environmental Research Center - Cincinnati, U.S. Environmental
Protection Agency, has reviewed this report and approved its
publication. Approval does not signify that the contents
necessarily reflect the views and policies of this laboratory
or of the U.S. Environmental Protection Agency, nor does
mention c trade names or commercial products constitute
endorsement or recommendation for use.
The text of this report is reproduced by the National
Environmental Research Center - Cincinnati, in the form re-
ceived from the Grantee; new preliminary pages have been
supplied.
Li-I c ,
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FOREWORD
Man and his environment must be protected from the
adverse effects of pesticides, radiation, noice and other
forms of pollution, and the unwise management of solid
waste. Efforts to protect the environment require a
focus that recognizes the interplay between the components
of our physical environment--air, water, and land.
The National Environmental Research Centers pro-
vide this multidisciplinary focus through programs
engaged in
o studies on the effects of environment_i
contaminants on man and the biosphere, and
0 a search for ways to prevent contamin-
ation and to recycle valuable resources.
In an attempt to sclve the problem of solid
waste treatment, this study examines a waste system
for swine units. This report, published by the
National Environmental Research Center - Cincinnati,
devised and evaluated a swine manure management sys-
tern that would be compatible with current swine pro-
duction systems.
A. W. BreidenbaCh, Ph.D.
Director
National Environmental
Research Center - Cincinnati
iii
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ABSTRACT
The purpose of this project was to develop and characterize a swine manure
management system. The goal of the system was to collect, transport, treat,
reuse and dispose of the manure in such a way that it would be compatible with
current confinement swine production systems, yet minimize both labor and
pollution potential. Suth a system was devised arid evaluated, its basis was
to hydraulically flush manure from ha) low dunging gutters with the treated
wastewater. The treatment devices evaluated included an anaerobic lagoon
and an oxidation ditch. Excess water from the system was applied under
controlled obscrvation to adjacent cropland using conventional sprinkler
irrigation equipment.
The overall validity of this concept was prov n. The system eliminated the
need for manual manure handling within the building, improved pen and animal
cleanliness, reduced odors, and eliminated manure h iuling or stream discharge
all without adversely affecting the perforrnanr.e of animals within the building.
Operating problems were largely related to equipment failures, caused mostly
by the necessity to use adapted equipment designed for some other intended
operation or fabricated peclalty itcm5 not otherwise available.
The report includes complete operating data on the waste management system
and a record of the various equipment problems and their alleviation. The
anaerobic lagoon effluent was found safe for recirculation and represented
least cost alternative. Using the lagion and oxidatio, ditch in series
produced on improved effluent quality but at a somewhat increased cost.
Using the oxidation ditch only resulted in solids handling problems and
further Increased costs.
This report was submitted in fulfillment of Grant No. RO 1 EP 00283 from the
Bureau of Solid Waste Management, Public Health Service, Department of Health,
Educat ion and Welfare.
Key words: Swine wastes, reuse, oxidation ditch, lagoon, B.0.D. removal,
C.0.D., solids reduction, waste treatment, irrigation disposal.
FRECE J G. PAGE&M i(
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TABLE OF CONTENTS
Page
CONCLUS IONS
Manure Handling xx
Phase I. Anae-obic Lagoon In the System xxi
Phase 2. Manure Diverted to the Ditch xxii
Aero Ic Sludge Digestion xxiii
Pigs Water Supply xxiv
Liquid Handling xxiv
Irrigation Disposal. 1968 xxv
Irrigation Disposal. 1969/70 xxvi
Desorptlon of Ammonia from the Anaerobic Lagoon xxvii
OBSERVATIONS xxviii
INTRODUCT lOW 1
Renovation and Reuse of Wastewater
Oxidation Ditches 9
Renovation by Soil Percolation
Summary 20
OBJECTIVES 22
SYSTEM AND ITS OPERATION 2
Hydraulic Circuit 2 i
Unit i 2 i
Anaerobic Lagoon 26
Ox.dation Ditch 26
Flush Tanks 26
Lagoon to Ditch Pump. Pump 5 27
Rotor Drive Unit 30
Settling Tank and Sludge Return 31
Effluent Return Pump. Pump 1 33
Manure Lift Stations 3
Metering 38
Irrigation Field 39
vii PRECEDING PACE LM
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The Plots and Tile Drains
Intermediate Sampling Points 43
Soil Preparation and Cover Crops 43
Irrigation Equipment 45
Irrigation Schedule 1 5
Sample Collection 48
RESULTS
Phase 1. AnaerobIc Lagoon in the System. 1969 51
Phase 2. Manure Diverted to the Ditch 70
Aerobic Sludge Digestion 85
Pigs Water Supply. 93
Irrigation Disposal. 98
irrigation Dl5posal. 110
Desorption of Amitonia 121
ACKNOWLEDGMENTS 139
REFERENCES 1141
PUBLICATiONS 148
APPENDICI ES
A. Chemical Analyses 151
B. Raw Results Phase 155
C. Raw Results Phase 182
D. Raw Results Aerobic Sludge Digestion 207
E. Raw kesults Pigs Water Supply 213
Phase 2 Treatment System
1968
1969/70
from the Anaerobic Lagoon
Differing from Standard Methods
2
v ii i
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LIST OF FIGURES
Page
Figure I. Transformation of nitrogen in soil 17
Figure 2. Hydraulic circuit, unit K 25
Figure 3. Float actuated flush tank discharge mechanism 28
Figure 4. Mg(NH 4 )P0 4 deposits on a pump after being
submerged in the lagoon for six months 29
Figure 5. Settling tank for oxidation ditch effluent 32
Figure 6. Manure lift stations 35
Fig.ire 7. Electrical schematic of the level control
used to activate manure pumps 37
Figure 8. General layout of irrigation area 41
Figure 9. Plan of one-half of plot and tile drainage
system 42
Figure 10. Lysimeter pan 44
Figure I I. Experimental plot layout 46
Figure 12. The chemica 1 oxygen demand of the supernatant
From the anaerobic laggon during Phase 1 55
Figure 13. The total phosphate concentration and the
temperature of the supernatant from the
anaerobic lagoon during Phase 1 56
Figure 14. The chemical oxygen &inand and the five day
biochemical oxygen demand conce,trations of the
settled effluent from an oxidatio, ditch fbd
anaerobic lagoon supernatant during Phase 1 61
Figure 15. The forms of nitrogen and the temperature
found in the settled effluent from an oxidation
ditch fed anaerobic lagoon supernatant during
Phase 1 62
Figure 16. The volatile suspended solids and the fixed
dissolved solids concentrations found in an
oxidation ditch fed anaerobic lagoon supez-
natant during Phase 1 63
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1
r_t- c
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Page
Figure 17. The chloride ion concentration found in the
settled effluent from an oxidation ditch fed
anaerobic lagoon supernatant and the rainfafl
record for a location near the lagoon during
Phase 1 64
Figure 18. The chemical oxygen demand and the five day -
biochemical oxygen demand of settled effluent
from an oxidation ditch fed raw manure. The
results for August and September 1970 are for
the supernatant; the results for January and
February 1971 are for centrifuge supernatant.
Phase 2 77
Figure 19. The forms of r,itroqen and the temperature
found in the settled effluent from an oxidation
ditch fed raw manure; the results are for Phase 2 78
Figure 20. The volatile suspended solids and the fixed dis-
iolved solids concentrations found n an oxida-
tion ditch fed raw manure; the results are for
Phase 2 79
Figure 21. The chloride ion and sulphate ion concentrations
lound in the settled effluent from an oxidation
ditch fed raw manure and the rainfall record in
a location near to the ditch; the results are
for Phase 2 80
Figure 22. Chloride ion concentration and time for the
settled effluent from an oxidation ditch fed
raw manure; the results are for Phase 2 83
Figure 23. Reduction in volatile suspended scuds during
aerobic sludge digestion. After Phase 2 87
Figur . 2 4. Logarithmic plot of the reduction in volatile
suspended solids during aerobic sludge diges-
tion. After Phase 2 88
Figure 25. Sequence of pens along the gutter. Pigs
water supply. 94
C
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Page
Figure 27. COD concentration in soil solution under
appl ication of anaerobic livcstock lagoon
effluent during sumer 1968 103
Figure 28. Nitrogen concentratiors in applied effluent
and tile outflow 104
Figure 29. Total nitrogen concentration in soil solution
i. nder application of anaerobic livestock 1ag on
effluent during summer 1968 105
Figure 30. Total phosphorus concentration in soil solution
under appication of anaerobic livestock lagoon
effluent during summer 1968 109
Figure 31. Tile drainage water quality with 2.0 inches of
anaerobic lagoon effluent applied in 3, 2/3
inch applications 112
Figure 32. Tile drainage water quality with one application
of 2.0 inches anaerobic lagoon effluent 113
Figure 33. Concentration of total-N at various depths in
the soil solution of Treatment 1970-14 on which
anaerobic lagoon effluent was applied - 117
Figure 34. Concentration of total-P at various depths in
tte soil solution of Treatment 197c4 on which
anaerobic lagoon effluent was applied 119
Figure 35. Concentration of total-P n tile drainage water
caused by Precipitation after various amounts
of Total-P had been applied in anaerobic lagoon
effluent 120
Figure 36. Anaerobic manure lagoon nitrogen concentration,
pH, and mean air temperature durine. 1969-1970
at Ames, iowa - 122
Figure 7. Percentage of NH 4 + NH 3 -N in solution that Is
N11 3 -N at equilibrium at various expected condi-
tions in an anaerobic manure lagoon 126
Figure 38 The calculated vapor pressure, P , of ammonia-N
in an anaerobic manure lagoon and the rr2acured
vapor pressure, Pg of ammonia-N in air directly
around the lagoon during 1970 128
Figure 39. Air sampling location around the anaerobic manure
lagoon at Swine Nutrition Research Farm 130
xi
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Page
Figure 40. Ammonia transfer coefficient versus gas
ve1 city for amri nia abcorption into water
fom Hal sam 131
Figure 41. Desorption of ammoniaN from anaerobic manure
lagoon liquid in laboratory by drawing air over
the liquid surface and catching desor. d ammonia-N
In boric acid 137
xii
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LIST OF TABLES
Page
Table I. Lysimeter pan sizes I 4
Table 2. Overall summary of field experlment used to
study soil filtration treatment of anaerobic
manure lagoon liquid 196870 49
Table 3. Fecal production per pig. Phase 1 53
Table 4. Loading and treatment efficiency. Phase 1 54
Table 5. Food to nicroorganism ratio in the oxidation
ditch. Phase 1 65
Table 6. Phosphate and pH in the lagoon and returned
effluent. Phase 1 69
Table 7. Fecal production per pig. Phase 2 71
Table 8. Loading and treatment efficiency. Phase 2 74
Table ,. Food to microorganism ratio in the oxidation
ditch. Phase 2 75
Table 10. 10 and I c at a mean temperature of 56.3°F 89
Table 11. Ratios of VSS:COD:N in the susper ded solids.
Aerobic digestion 90
Table 12. Suspended solids and SVI. Aerobic digestion 91
Table 13. COD in centrate and suspended solids. Aerobic
digestion 92
Table lie. Weight gain, feed and feed conversion. Pigs
water supnly 96
Table 15. Detection of TC 1 E virus in system 97
Tabie 16. Average water i 1 ua lity cnncentrations from
June 18-September 20, 1968. Samples collected
12 hours after start of irrigation 100
T:eble 17. rorm and concentration of nitrogen In sampled
soil solution at various depths for treatment
14 - 3.0 inches at 95 available moisture
suniner 1968 102
Table 18. Estimation of nitrogen and chloride reduction
by soil filtration considering effects of excess
tile drainage 1968-70 108
xlii
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Page
Table 19. Nitrogen balance on anaerobic manure lagoon
at Swine Nutrition Research Farm, Iowa State
University, Ames, Iowa from I Nov. 1969 to 31
Oct. 1970 423
Table 20. Prediction of the overall mass-transfer coef-
ficient of ammonia-N, K, from mass-transfer -
considerations and conditions prevailing at
the surface of an anaerobic manure lagoon dur-
ing 1970 1311
Table 91. Nitrogen forms, manure slurry $55
Table 82. Nitrogen forms, lagoon 156
Table 83. Nitrogen forms, returned effluent 157
Table ak. Phosphate (as r°k 3 158
Table 85. pH, temperature and colif-orms, manu e slurry 159
Table 86. pH, chloride, temperature and colitonns, lagoon 160
Table 87. pH, chloride, temperature and coliforms, returned
effluent 161
Table 88. Total solids, manure slurry 162
Table 89. Dissolved solids, manure slurry 163
Table 910. Suspended solids, manure slurry 16k
Table 911. Total solids, lagoon 165
Table 912. Dissolved solids, lagoon 166
Table 813. Suspended solids, iagocn 167
Tab le 814. Total solids, returned effluent 168
Table 815. Dissolved solids, returned effluent 169
Table 916. Suspended solids, returned effluent 170
Table 817. Total salids, ditch i l l
Table al8. Dissolved solids, ditch 172
Table 819 Suspended solids, ditch ;73
Table 820. linear regression for volatile suspended solids
ditch
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Page
Table 821. Total solids, sludge 175
Table 822. Dissolved solids, sludge 176
Table 323. Suspended solids, sludge 177
Table B2 1 4. Oxygen demand, manure slurry 178
Table B25. Oxygen demand, lagoon 179
Table 626. Oxygen demand, returned effluent 180
Table B27. Air temperature, pig population, flow rate and
power 181
Table Cl. Nitrogen forms, manure slurry 182
Table C2. Nitrogen forms, returned effluent 183
Table C3. Nitrogen forms and pH, ditch 1814
Table C 1 i. Nitrogen forms, overflow 1814
Table C5. Phosphate (as PO 3 ), manure slurry 185
Table C6. Phosphate (as PD 1 4 3 ), returned effluent 186
Table C7. pH, chloride, sulphate, temperature and co1iforms
manure slurry 187
Table C8. pH, chloride, sulphate, temperature and coliforms,
returned effluen*. 188
Table C9. Total solids, manure slurry 189
Table dO. Dissolved solids, manure slurry 190
Tabe dl. Suspended solids, manure slurry 191
Table Cl2. Total solids, returned effluent 192
Table C13. Uissolved solids, returned effluent 193
Table C 114. Suspended solids, returned effluent 194
Table C15. Total solids, ditch 195
Table C 16. Dissolved solids, ditch 196
Table Cl7. Suspended solids, ditch 197
Table C18. Total solids, sludge 198
xv
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Page
Table C19. Dissolved solids, sludge 199
Table C20. Suspended solids, sludge 200
Table C21. Total solids, overflow 201
Table C22. Suspended solids, overflow 201
Table C23. Oxygen demand/manure slurry 202
Table C2 1 4. Oxygen demand/returned effluent 203
Table C25. Oxygen demand, ditch 20 i
Table C26. Oxygen demand, overflow 2O
Table C27. Air temperature and relative humidity 205
Table C28. Pig population, flow rate and power 206
Table Dl. Nitrogen forms, chloride and temperature 20;
Table D2. Total solids 208
Table 03. Dissolved solids 208
Table Di. Suspended solids 209
Table 05. Oxygen demand, rotor power and temperature 209
Table 06. Linear regress Ion for K rate volatile suspended
solids 210
Table 07. Linear regression for K rate COD suspended
solids 211
TaHe D8. Linear regression for K rate KJeldahl N in
suspended solids 212
Table !i. Pig weight gain p .n 16 gutter water (G) 213
Table E2. Pig weight gain pen 17 normal waterer (N) 213
Table E3. Pig weight gain pen 18 gutter water (C) 2l 1
Table E4 Pig weight gain pen 19 normal waterers (N) 2 l i
Table E5. Pig weight gain pen 20 gutter water (C) 215
Table E6. Pig weight gain pen 21 normal waterer (N) 215
Table E7. Feed weight record 216
xvi
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Page
Table E8. Pen weight gain totals 218
Table E9. Weight gain ANOV (completely randomized desIgn) 218
Table ElO. Weight gain ANOV (randomized complete block
design) 218
Table Eli. Feed consumed totajs 219
Table E 12. Feed consumed ANOV (completely randomized
design) 219
Table E 13. Feed consumed ANOV (randomized complete
block design) 219
Table Ell+. Feed conversion 220
Table El5. Feed conversion ANOV (randomized complete
block design) 220
xvii
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SUMMARY AND CONCLUSIONS
Accompi Ishments
The work described In this report was performed with the objective
of determining the practicality of a reccled eff aent system fo.- manure
transport in swine finishing buildings. The system was developed around
Unit K, an existing 700-lead confinement swine_finishing building erected
in 1960. Manure transport, treatment methods used recyclc.d effluent
quality, fluid handling equipment as well as treatment and disposal of
the excess from the system are evaluated.
This project resulted in the development of a swinefinishing facility
in which 700 animals are confined on a continuous basis, in which manual
labor for manure removal has been elmost totally eliminated, and from which
there is mo waste discharge to surface streams. The building is less odorous
than conventional swine production units because of the frequent manure
removal. The only net waste product is excess liquid which is applied to
croplarid during the summer using conventional irrigation equipnent.
Based upon the success c i this project a demonstration project supported
by tIe Environmental Protection Agency was instituted. The derr.,nstration
project includes eight buildings fitted wth flushing gutters ad incor-
porating three independent waste treatment systems all of which produce an
effuent to be used in the flushing system. This facility Is to be placed
in operation during the summer of 1971. In addition to this dettonstratiop
project,, the concepts developed in this research have been incorporated by
numerous midwestern swine producers.
P ECE 1N6
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Manure Handling
In the early days of Unit K, the use of a small continuous stream of
fresh water through the dunging gutters lndcated that hydraulic manure
transport was a promising manure removal system. More recent experience
suggests that, with flushing tanks, 1. gpd per pig discharged in regular
2 hr interval flushings will transport the manure adequately in this 120 ft
long building Containing 350 animals to Lach gutter. Pen cleanliness was
improved even more by reducing the interval between flushes but this also
Increased the volume of manure slurry requiring treatrnen . The per pig
value of transport liquid given is only approximate as no tests were per-
formed to find an optimum relatir n between total flow quantities and
individual pig quantties. Moreover,all the wrk described was performed
using a fixed channel slope of I ft In 120 ft. Gutter width and depth are
other variables not examined in detail. Visual examination of slurry flow
pattern Just downstream of the tank, and at the far er d of the gutter, does
suggest that liquid velocity in the bulk of the channel is more a function
of the channel gecnetry than the rate of discharge at the head. It also
appears that the minimum total quantity of liquid required to satlsfy the
hydraulic capacity of the gutter Is independent of the number of pens along
the gutter. It was found that an unoccupied 42 in. gutter width was too
great because manure particles may settle out and the slurry then takes a
meandering course between banks of settled manure. In the test facility this
meandering could be overcome by reducing the channel width to 15 in.
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Phase 1. Anaerobic Lagoon and Oxidation Ditch In The System. 1969
Operation was started in February 1969 and continued until May.
The flow process was to hy JrauIicaIly transport wastes from a 700 head swine
finishing building (Unit K) to initial treatment in an anaerobic lagoon, then
to an oxidation ditch and a final settling tank whereupon the clarified
effluent from the settling tank was returned for manure transport in Unit K.
Derived fecal paramc ers, reduced to a unit pig basis 1 compared favorably
with values reported in the literature.
The anaerobic lagoon functicned as a useful part of the system. it
reduced VS, BOD and COD by more than 85 , though N was only reduced by 6O .
The lagoon also served to reduce coliforrns i .y 99L No evidence of a
trend in the concentration of dissolved inorganic solids could be determined
In the i mo recyclinq period. Vigoroas bIological activity, as evidenced by
rising boils of gas and bottom material, occurred whenever the agoon
temperature was above 55°F. Some possible machanisms of nitrogen reduction
are discussed, including precipitation as Mg and Ca amonlum phosphates and
dilution effects. In the Spring, biologi al resurgence brouqht an unexpected
increase in phosphate levels, attributec to two sources in the bottom
sediments; one supply of P was organic matter but the other, most probably,
was inorganic P in t e iGrm of hg and Ca phosphates.
Deposition of Mg(Ni1 )P0 on equipment submerged in the lagoon is cited as
contributory evidence.
The clarified effluent from the oxidation ditch, though slightly
yellow and turbid, was odor-free and contained a BOD 5 of less than 120
xxi
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mg/I. Food to microorganism ratios, examined throughout the test, were
all lower than 0.05 lb 80D 5 /lb MLSS. Until the upsurge of lagoon activity
caused a reduction in influent strength to the ditch, the rate of
production of volatile suspended solids, as derived by linear regression,
was J6.2 lb/day. A cell yield parameter could not be obtained because of
other uncertainties. The generation of VSS was examined in relation to
phosphate uptake and the results indicate that the sludge was storing 77.
P (dry weight basis). The excess aeration capacity of the rotor caused
extensive nitrification after the ditch temperature climbed above 39°F.
Power requi ementa, per unit of BOD.. removed, were higher than values
J
normally reported in the literature becau5e f the excess aeration
capacity. The power requirement per pig was 0.09 kwh/day.
Phase 2. Manure Diverted to The Ditch. 1970/71
This research began in August 1970 and ended in March 1971, with a
major breakdown during October and November. The raw manure slurry from
Unit K flowed directly to the oxidation ditcI , the settled effluent from
the ditch then retur9ed to Unit K for transporting manure. The anaerobic
lagoon served only as a receptor for the overflow from the ditch.
Reductions In VS, COD and N obtained in the ditch were all in excess
of 75%. Nitrogen reduction now averaged 80% and the contribution of
nitrification and denitrification Is discussed. Food to microorganism
ratios were calculated as about 0.05 lb BOD 5 /lb MLSS during most of the
operation. Lack of aeration capacity, hair and husks were all considered
as factors contributing to the poor settPng observed after the MISS
xxii
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exceeded 12,000 mg/i. The small total volume of the ditch allowed detection
of the expected trend of dissolved inorganic salt concentration. Experi-
mental results correlated well with a theoretlca l exponential equation.
Actisai rates of accretion of Ci were compared with the literature, and
Inhibition from salt toxicity was rejected as a concern for this or a
comparable system. Power requirements were much higher than in Phase I,
though the power consumption per unit of BOD 5 (0.705 kwh/lb 8005) was now
more comparable with municipal experience. The power requirements for the
individual pig increased to 0.2 1 i kwh/day.
Aerobic Sludge Digestion. 1.971
After ending Phase 2 the liquor remaining in the ditch was allowed
to digest aerobically, without further feeding, for 10 wk. After the
third week, settling improved markedly. For convenience in examining the
results, an exponential decay model was selected, with tie exponents being
determined for volatile matter, D and Kjeldahl nitrogen in the
suspended solids. A sudden rise in all parameters, occurring after 30
days, reduced the agreen nt between tile model and the results. This
rise was most probably due to some sediment being resuspended. Comparison
of the values of the exponer. s, and also the ratios VSS:COD:N, showed
that the N content of the sludge decreased most rapidly. Aerobic sludge
digestion was judged beneficial with regard to VS reduction and Unproved
settling.
cxiii
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Liquid Flandliri
The poor settling, hair and husk laden ditch liquor obtained in
Phase 2 presented problems. Whereas the low solids content ditch liquor
In Phase 1 had settled readily and the supernatant liquor was easily
pumped, returning pumping of settled sludge back to the oxidation ditch
finally required the use of a large bore diaphragm pump. Based on these
experiences, aerobic treatment of raw manure at MISS above 10,000 mg/i
cannot be recommended if the liquor is to be settled and reused. A
larger ditch volume and controlled sludge discharge could overcome the
encountered problems but they would likely introduce equally serious
management problems for most producers. Pumping anaerobic lagoon super-
natant did produce some problems because of the deposition of Mg(NH )P0 .
It Is w 1iIely that this can be overcome completely, but difficulties
can be minimized by using plumbing with few fittings, by selecting
suitable pumps, ana by occasional flushing of the system with an
appropriate solvent. Experience has shown that flexible impellor
pumps work well. Flushing tanks using mechanical valves were useful
for research purposes, but a better desThn uses a syphon having no
moving parts. The design of low cost, lightweight syphon tanks h s been
described by Person and Miner (57).
Pigs Uater Supply Phase 2 Treati nt System. 197]
An experiu nt was conducted tb determine the effect on the pigs of
being forced to drink out of the flushing gutter, no other drinking water
xxiv
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being available. Statistical analyses of weight gain, feed consumed and
feed conversion were performed. Both weight gain and feed conversion were
shown to deteriorate (5% level). TGE virus was monitored as it passed
through the treatment system. No diminution of viral intensity, in ditch
or lagoon, was noted until the water temperature exceeded 60°F.
Irrigation Disposal &68
Irrigation was begun in June 1968 and continued until the following
November. The irrigation equipment worked well without noticeable
corrosion wr plugging from suspended materials. Odor during sprinkling
was not a problem or was insect breeding encouraged since no permanent
ponding occure.d. Infiltration rates remained approximately constant
throughout the season. Four treatments were applied, 1.5 and 3 in.
irrigation quantities at 70% and 90% available moisture levels. Appfl-
cation rate was 0.30 lph and, although less than recommended for clear
water, this was found the maximum feasible rate using lagoon liquor.
Samples were collected from tile drains installed at 48 in. and at inter-
mediate depths from buried pan lysimeters. Differences between treatments
were smdll. An average of 97% of the applied COD was removed by the time
the effluent reached the tIle, 50% removed I the top 3 in. of soil.
Nitrogen was removed as the effluent moved through the soil and it was
concluded that biological denitrification was the predominant phenomena
causing t.R t 80% reduction observed. Phosphorus removal was judged
excellent since percolation removed 99% with 83% being removed in the top
3 In. of soil.
x xv
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Irrigation Disposal 1969-70
Irrigation was practiced from hay to October during both seasons.
The plots continued to accept water readily but problems with cracking of
the soil in the tile field trenches caused some short circuiting from
the surface to the tile.
Por us cup sai.iplers and soil moisture tensiometers were Installed
and these allowed more information to be obtained over a greater range
of soil moisture content. Treatments in 1969 were 2 in. of clear water,
water spiked with a known amount of nitrogenous fertilIzer and l. igoon
water. These three treatments were applied at 750 mb tension and a fourth
treatment of lagoon water was also applied at 350 mb. In 1970, only
four applications of lagoon water were used; In one amount of 2 in. and
3 daIly amounts of 213 in. The two moisture tensions were 750 rub and 350 mb.
Fertilized water behaved as lagoon water wlL.i regari to nitrogen removal.
The 1970 season showed that small consecutive applications were better than
one major application if transient tile effluent strengths were of major
Importance, though removals on a mass basis were nearly the same for both
regimes. Mass removal of COD ranged from 79 to 9 %. Better remval was
obtained with the 3 daily 2/3 in. applications. COD removal deteriorated
as t e irrigation season progressed. Porous cup sampling IndIcated 89%
removal of COD at 6 in. Nitrogen removal allowing for various water losses,
amounted to a mass removal of 49 to 63%. This was lnferiqr to the 1968
result of 86% but the soil cracking Introduced short circuiting of NH 3 -N.
xxvi
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Useful decreases In N were obtained between the sprinkler nozzle and the
ground due to ammonia desorption. Denitrificetion was examined in the
laboratory and lagoor water organic carbon was Judged a poor substrate,
solutions of nitrate in lagoon water denitrified most rapidly if dosed
with glucose. Phosphorus removal remained high (90 - 97Z) but some
Indication of a linear relation between accumulated applied P and tile
drainage became apparent. In three years the chnride ion removal had
declined to zero indicating dynamic equilibrium with the soil solution.
Desorption of Ammonia From the Anaerobic Lagoon
Loss of nitrogen from the anaer-bic lagoon o. r an annual cycle was
well established, but could not be entirely explained by sediientation
and precipitation. Aninonia can migrate across i.he liquid-vapor boundary
of water, the d 1 rectjon and rate of migration dependent upon such factors
as partial pressure differentials, pH, temperature and relative motion
between liquid and vapor. Examination of the literature revealed that the
ecperimerital results obtained in the field could be made to yield kinetic
rate coefficients for desorption that compare quite favorably with published
absorption results, It was concluded tLt between May and October ammonia
desorption could account for 80 to l1i5 of the N influent to the lagoon.
xxv i i
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OBSERVAT IONS
Manure is composed of the same basic building blocks as food:
protein, carbohydrates, vitamins and minerals. Future waste handling
systems will be designed to recover these in a useful form.
A typical Midwestern swine manure slurry, examined physically,
breaks down into three basic fractions; a supernatant containing
soluble and colloid flatter, a fine settleable particulate fraction and
a course settleable particulate fraction. There is mounting Justi-
fication that systems which segragate these fractions will be superior
to those that handle them together. The fractions should separate
readily because they have physically different properties; but little
work has been done to examine the chemical properties of each fraction in
detail, a necessary step before firm recommendations for their treatment
can be made.
A reasonable insight Into the probable processes can be developed,
however. The coarse, fast settling fraction cjnsists of undigested corn
particles, lgnaceous husk material and hair. Such material should be
re-fed on an experimental basis to find out if a better tot 1 fraction of
the corn may be used, or if excess addition of bulk material, such as husk
and hair, simply lowers animal perforn*amce. This coarse material could
probably be drained so that it would not putrefy in storage and Iandspread
at a convenient time. A1ternatively a large Uvestock producer might
examine the use of this fraction as fuel to power an engine and generator.
uvili
-------
The fine particulate fraction is largely unquantified. However, it
appears to be metabolic by-products that wil surely be v ry putrescible.
Of the many possibilities that present themselves, two seem worth examining.
Since the material is finely divided, quite simple chemical treatment
might render it suitable for re-feeding. Another alternative might be
incineration and use of the ash as fertilizer. The ash would, at least,
concentrate P and K to a bulk comparable with conmercial fertilizers.
Nitrogen loss to the atmosphere does need to be controlled to avoid produc-
tion of NH 3 and NOx as air pollutants.
The liquid portion remaining after Fractionation putrefies readily
and will need Immediate treatment. This liquid free of large particulate
matter, will therefore treat easily using any of the established biological
processes. The remaining COD after fractiona..ing will be much lower than
that of the manure slurry, hence treatment in an aerator may be economically
attractive. Two alternative aerobic processes which need very ltttle
power, compared to direct aeration, are the Rotating Biological Contractor
and the high rate trickling filter using plastic media. in any case,
facilities will need to be provided for excess sludge treatment and for
excess liquid disposal.
Additional work is also indicated to refine the flushing gutter design
to improve manure transport. The 2 in. wide gutter used in this facility
proved satisfactory when pigs had access to the area but was not self-
cieani g when pens were empty. Reduction of the gutter width is helpful in
this respect but such reduction is limited by animal acceptance and training
habits.
xxix
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* - - - -
INTRODUCTION
Renovation and Reuse of Wastewater
Man is now past the point from which he could look at water as a
disposable and unlimited commodity. Before- the industrial-revolution,
cities were quite small and could satisfy their water needs from rivers
without worrying about, or even comprehending, pathogens or pollution.
But by themid-l9th Century, the rural migration to the cities had caused
an explosion in city populations and untreated water was no longer
potable without considerable risk of infection. Fortunately, the impetus
given to science by the industrial revolution had revealed the knowledge
necessary to institute treatment facilities for both drinking water and for
wastewater. So, by the beginning of this century the spectre of massive
epidemics of cholera, typhoid dnd other water-borne diseases had been laid
to rest. -
However, man is now entering an-era of water shortage; because his
phenomenal success at organizing an industrial society has led him to
expect extensive material possessions as the norm. Mans eating habits
have also change. As he becomes more affluent, he eats more animal than
veyetable protein and his consumption of animal protein is increasing (79).
This increasing appetite of man, the consumer, means that the number of
units of industrial output required to keep an individual fed, watered,
clothed and amused Increases daily. Essentially all these industrial
processes use water as a raw material. However, this is not the whole story.
Mans water use is rising annually, an so is the number of men.
----- - ---- -- - - - -- 9 P.!ACE LA
-------
Although there are certain industrial processes, such as condenser
cooling, that leave water unchanged chemically, most other industrial and
agricultural processes cause an increase in the burden of dissolved and
suspended matter carried by the water. The water and sewage treatment
systems developed in the last part of the 19th Century were quite
adequate for removal of organic matter, but they left the concentration
of inorganic materials largely unchanged. The end result of this treatment
deficiency was to render the water more saline after each use. At first
this was not significant, since rainfall was sufficient to dilute the
salts before the next user took in the water.
Today there are only two low co9t sources of new water; surface
storage in lakes and rivers, and groundwater storage in aquifers.
Berger (9) reports that the United States has only a limited supply of
water available from these sources and that the countrys requirements
will, exceed this by 1980. Berger (9) also notes that conventional
secondary treatment, even if applied to all wastewaters, will not
suffice; because the natural purification cycle does not adequately cope
with such materials as refractory industrial organic compounds, viruses,
and certain pathog na such as Salmonella. To some degree these materials
pass through onventLonal treatment systems, making the task of treating
the water for drinking increasingly more difficult.
Water resources are not evenly distributed throughout the United
States; hence some states have encountered supply problems well before the
1980 deadline predicted by Rerger (9). Two such states, Texas and
California, have begun practicing water reclamatthn. Fleming and Jobes
(20) state that by 2020, Texas is expected to require 28 million acre-ft
2
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of water for all purposes, double that used in 1960. Texas haz. an
estimated safe yield of 21.3 million acre-ft of water from all sources;
thus the state already has extensive experience with water reuse. The
economy of Texas leans heavily upon oil and its derivatives, and these
industries are heavy water users. However, Rickles (63) has shown that
large integrated petrochemical complexes, such as that at Odessa, can make
good use of reclaimed water. Foster and Jopling (22) have summarized
CalifornLas attitude toward water reuse. At this time the st4te does not
envisage direct reuse of effluent for potable supplies, but it is actively
promoting reuse for irrigation and industrial cooling. California divides
reclaimed water into three categories; primary effluent, oxidized waste-
water and filtered wastewater. Some control over quality standards was
obviously necessary, but the state did not wish to inhibit potential
reusers by imposition of rigorous chemical standards. Instead, coliform
counts were used since these might be performed with a minimum of skill
and technical equipment, following development of some simplified
techniques. As an example, the state code will allow spray irrigation if
the water meets a most probable number of coliforms less than 2.2/ 100 ml.
Garthe and Gilbert (2 t) reviewoi one of the countrys lomigest running
water reclamation projects. The Grand Canyon in Arizona I,as tourist
accommodation on the South rim, but the major water hearing strata are on
the North rim. Because potable water is at a premium on the South rim,
water from an activated sludge plans has been reclaimed by filtration
throu&h anthracite followed by ch1or ination. This water has been reused
for water closets, irrigation of gardens around the hotel and for the
3
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boilers. keclajgiatton has bcc i)rflCtiL d sinct 19 T h wIthout III t fCt ctg.
Not all authorities agree on the wisdom of using wastewaler for
agricultural irrigation. For example Hirsch (27) discusses the effects
of metallic cations, The effect of sodium on soil is well documented and
irrigation waters are characterized by their sodium absorption ratio,
Na
SAR/Ca+Mj (1)
.I 2
Todays effluents may also contain boron, copper, chroiniwn and other
potentially toxic cation , Hirsch (27) presents a table showing that
0.9 - 1.4 mg/i of boron was found in the Rose Canyon reclaimed irrigation
water. A boron concentration of 1 mg/i is generally accepted as safe for
irrigation water.
Thus far, only simple 5ystems such as primary settling, secondary
biological treatment and chlorination have been discussed. Although
these are often adequate for i:rigation, industrial r potable reuse may
require more advanced treaLment. This tertiary tr. atment is required for
removal of inorganic material, trace refractory organic material and
virus .s. Thus industrial reuse may entail chemical coagulation, lime
treatment, ion exchange, active.ted carbon, etc. Koenig and Ford Q9)
have examined che various processes availdule and have presented some
cost information. Evaporation will remove the major part of all
contaminants, but it can cost $1.45 per 1000 gal at a flow rate of 10,000
.3
gpd for a single effect evaporator. At the other end of the scale
natural purification in an oxidation pond may be adequate, and this will
only cost $0.Oll per 1000 gal at 10,000 gpd. Koenig and Ford (39) point
3
-------
out succinctly that the economics nf reuse will depend upon the
following parameters:
Cobt. of raw water
Quality of raw water
Cost of treatment for disposal
Cost benefit of product recovery from the waste stream
As an example they mention a case in which 150 lb/day of Cr was being
discharged to a sewer. Not only did this amount to a $100/day loss to
the plating firm but also Cr+ 6 is biologically toxic and unwelcome at
municipal sewage treatment plants. Equipment was installed to recover
the chromium and this recovery paid for the equipment.
Industrial areas which have arid climates have all encountered water
resource defici acjes (20, 22) but only one country appears to hava
progressed as far as water reuc for municipal drinking supplies. Stander
and VanVuuren (72) have described the researc , , necessary to develop a
1.2 mgd demonstration plant at Windhoek, the capital of South West Africa.
The processes employed are of some interest since they indicate the degree
of complexity required to produce potable water. Water is taken from an
oxidation pond ied with secondary effluent. This water is dosed ith lime
and passed through a flotation process, removing algae and some fraction
of the nhosphorus and nitroge-t. The high pH of the effluent from the
liming process is capitalized UPOU by following the flotation with
anunonia stripping. Calcium and a large fraction of the suspended solids
are then removed by chemical coagulation following carbonation. Sand
filtration and foam fractionation, for detergent removal, are followed by
activated carbon filtration and fin9l chlorination. Stander and VanVuuren
(72) present data showing that removal of phosphorus, organic matter,
5
-------
detergents, pathogens and viruses is essentially complete; but they do
point out that nitrate nitrogen is little affected by the processes.
Wtndhoek now has one-third of its water rupply provided by this plant
and public acceptance has been very good.
Lake Tahoe in California offered a rather different engineering
challenge. Culp ( 8) discusses the treatment necessary to provide an
effluent of cufficient quality that car, be returned to the lake witho t
danger of eutrophication. The system chosen is very similar to that
outlined by Stander and VariVuuren (72) except that the effluent is taken
from the final clarifiers of an activated slud plant, thus obviating
flotation to remove algae. All solid wastes from the processes are
thermally processed to recover the lime and activated carbon.
To this point the literaturc reviewed shows that water may be reused
for all purposes if sufficient treatment is provided. Even in the United
States a large portion of future needs will have to be met from reclaimed
water. Agriculture is a large watet user and has practiced water
reclamation unknowingly for some years. Irrigation and groundwater
recharg just amount to using t ie soil as a treatment prr.:ess. Although
irrigation has accounted for the major fraction of agricultural water
use, the changing pattern of livestock production is beginning to demand
attention. Livestock in confinement present a neu water demand because
hydraulic transport promises low labor and equipment requirements. One
of the pioneers in this field was Ilercules whose labors are describ .. d by
Apollodorus (5).
6
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The fifth labour he laid on him was to carry out the dung of
the cattle of Augeas in a single day. Now Au8eaB was king
of Elis; some say that he was a son of the Sun, others that
he was a son of PoseLdon, and others that he was a son of
Phorbas; and he had many herds of cattle. Hercules
accosted him, and without revealing the command of
Eurystheus, said that he would carry out the dung in one
day, if Augeas would give him the tithe of the cattle.
Augeas was incredulous, but promised. Having taken Augeas
son to witness, hercules made a breach in the foundation
of the cattle-yard, and then, diverting the courses of
the Aipheus and the Peneus, which flowed near each other,
he turned them into the yard, having first made an outlet
for the water through another opening.
Water quality standards In Greece must have been rather lax at that time.
Johnson (32) has reported a more practical system which was used
for poultry. The birds were kept in cages ov c a rectangular section
channel. The channel was connected to a three compartment settling
tank. Effluent could be pumped from the last compartment to the head of
th channel. This effluent was contained behind a moveable scraper
placed in the channel. The hydraulic forces propelled the scraper along
the channel shunting the ccwnulated manure out. Johnson (32) operated
the system for four months, during which perio. dissolved solids built
up appreciably. The set .led solids in the tanks were field spread at
convenient intervals. Witz et al . (86) used a similar system to
Johnsons (32); however, they objected to the smell of the returned
effluent. They were able to control odor by coagulation with alum, or by
aeration in the settling tank. No details were given of the aeration
device or its capacity. Pratt etal. (59) have described a pilot plant
system for two beef animals. The animals were kept on a slotted floor,
and facilities were provided for flushing t.he manure accumulation out from
under the floor. me slurry first entered a 600 gal settling tank and
7
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then flowed into a 100D ga.l treatment basin, effluent from the second tank
was used for underficor flushing. Three methods of treatment were applied
to the 100.) gal tank; simple settling, aeration and aeration combined with
chemical coagulation. It was .found.that none of these could provide a
coapletely odor free effluent, although coagulation with aeration did
pro idc a useful reduction in DOD 5 . Clayton and Feng (15) used a pilot
plant to treat the inure from one dairy cow. About 33 gal. of settled
effluent was added to the 7 gal of fresh manure from the cow, and this
mixture was fed to a 2000 gal primary sedimentation tank. The effluent
from this tank flowed into a 1000 gal aeration tank and was finally
settled n a 200 gal sedimentation tank. Both sedimentation tanks were
maintained at 70°F but the aerator was held at 95°F. No sludge return
was made to the aerator. The system operated for 78 wk, producing an
odorless effluent with a 907. reduction in BOD 5 . The only major problem
mentioned via a heavy scum buildup in the primary sedimentation unit. The
scum, which was removed after 53 wk of operation, was described as being
dense an3 recognizable as the fibre from bedding and silage. The material
was easily handled with a fork and manure spreader, the odor wab described
as not being too disagreeable. Although the recycled effluent was stable
and udorless, it was dark ;drown in color; and Clayton . .nd Feng (15) doubt
that the reuse of such an effluent in a dairy unit would be acceptable -
from the public health standpoint. The aeration capacity was generous
since nitrification was established early, continuing at a high level,
300-600 mgI 1, throughout the test. Foaming was not a problem in the
aeraor.
8
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Smith and Jenkins (f,q) were concerned that increasing salt Levels
might prove inhibitory to treatment. Bench scale aeration units were
established using poultry manure, but after one year the increase in salt
concentrations was small. !iencc Smith and Jenkins (69) had analyses
performed on the raw manure to determine the inorganic ions present, and
their relative magnitude. Solutions of these ions were then prepared in
strengths of Ox, lx,.5x, lOx and bOx. The lOx concentration approached that
of normal sea water. When the aerobic digesters were established using
these solutions, it was found that treatment efficiency was not
significantly different among concentrations, a Sept for the bOx
concentration. Thus it was concluded that salt buildup should have no
effects on biological treatment up to 20,000 mg/i, but that a
concentration of 250,000 mg/i does impair treatment.
Oxidation Ditches
The aerobic process of biological treatment will generally produce a
lower strength of effluent than the anaerobic process. The two aerobic
processes most commonly found in municipal pollution control pl.rnts are
the trickling filter and the activated sludge process. The trickling
filter haa not seen extensive use for high strength wastes in the United
States but it has received some attention in Britain (Eden et al . (19) ) ,
following the development of plastic media.
McLellan and Busch (51) have examined the fundamentals of activated
sludge treatment. They have shown th t as influent strength rises the
mixed liquor suspended aolida must also rise in order to produce low
.9
-------
effluent strengths. This concept is vezy significant when applied to
agricultural and industrial wastes, because the l fl.SS may now be as high
as 30,000 mg/i, compared with 2000 mg/I for municipal wastes. These high
soflds levels are difficult to handle in conventional sparser aeration
plants, hence recent years have seen a revival of interest in mechanical,
sometimes called surface, aeration. Such aerators have mere control over
the partition of mixing vs. oxygen transfer.
One of the few innovations in sewage treatment was introduced by
Passveer (56) in 1957. He used a shallow trench in the form of a closed
loop. The rator is a brush or paddle wheel with its axis parallel
to the water surface, and normal to the cente line of the trench. As
first conceived, the oxidation ditch was merely a canal with earthen
slopes. This simplicity, and low construction cost per unit volume, has
tended to persuade designers that the oxidation ditch is ideal for
extended aeration activated sludge. At first it was thought that
continuous return of solids from the final clarifier would drive the
system into endogeneous respiration so that:
New cell growth from Souls destruction by
substrate utilization endogenous respiration
However, more recent work, typically that by Washington and Symuns (80),
shows that some biologically refractile material is continually being
produced and this will accumulate in the system. Even if volatile
solids destruction is not complete, the oxidation ditch, used as an
extended nerction system, does offer the potential of large volatile
solids reduction, a stable, well minerali-ed sludge and simplicity in
operation
10
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The majority of oxidation ditches constructed up to the present have
been for isolated rural communities or as quickly constructed additional
facilities (or an existing overloaded plant (Passveer (56), Rurchinal and
.Ienkins(14) ). Since strong industrial wastes are often best treated by
extended aeration, the literature is beginning to contain reports on
ditches which have been used for more exotic wastes. Adeina (1) has
described the largest oxidation ditch the world for the treatment of
coking and chemLcal plant wa8tes in Holland. This monster has a capacity
of 30,000 in 3 (1.06 x 10 6 ft 3 ) and is fitted with 10 rotors, each driven by
a 80 hp motor. Some initial difficulties were experienced because the
waste was below design strength. Excess aeration capacity soon promoted
nitrification and, since the waste was insufficientJy buffred, the pH
dropped to 4.4, severely inhibiting further biological activity. This
phenomena did not occur when the plant was more heavily loaded.
Scheltinga (67) has pioneered the use of oxidation ditches for the
treatment of agricultural wastes in Holland. Total return of manure to
pasture would lead to overfertilization with P and K which might adversely
af..ect the animals grazed on it. This, and the growth of confinement
liveBtock housing, has forced the country to handle its farm wastes by
nontraditional methods. Discussing the application of oxidation ditches
to cvlf and poultry waste, Scheltinga (67) concludes that BOD 5 loading per
mass of solids carried is the only rational basis for design. He suggests
0.05 lb BUD 5 day/lb MLSS in the systems. Whereas 6000 mg/i would be a
realistic MLSS concentration, 12,000 - 15,000 mg/i may be carried under
some circumstances, though excess sludge production will not drop in
proportion. Pontin and Baxter (58) have described a two ditch system for
11
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pigs. The first in an underfloor ditch and the effluent [ roan this flows
into second ditch for polishing. In prLactice th firnL ditch served
mainly to keep the manure mixed and to control odor. Th MLSS in the
second ditch rose to 20,000 mg/i after 12 wk because of the poor treatment
effected in the first ditch. Effluent from the second ditch was passed
through a final settling tank but the supernatant still contained a mean
of 620 mg/I SS and a BOD 5 of 590 mg/i.
Jones et al . (3-14) have recently pubiished the results of several
years study on underfloor oxidation ditches. Initial studies using
laboralory aeration vessels showed that a ditcP volume of 8 ft 3 per
finishing pig provided good treatment and no serious foaming. Although the
fl.SS of this unit was 21,000 uag/l, after 13 weeks the mean BOD 5 of the
supernatant was only 45 mg/i. Although Jones et al . (314) are optimistic
about oxidation ditches in swine confinement buildings, they do note that
the clarified effluent will need further treatment before discharge. They
suggest oxidation ponds. A recent study based on design parameters from
Jones et aL . (314) work Itas been reported by Windt et al . (85). Their
uncnrfloor ditch treated the wdste from 330 pigs. The ditch was located on
a commercial farm and marketing practices affected the loading rate.
Approximately half thc pigs were marketed at a time, hence there was a peak
loading on the ditch at 60 day intervals. Evidence is presented that the
fl..SS showed a cyclic variation in accord. yith the variable loading. Ditch
level was maintained constant by an overflow weLt, thus solids vete
continually discharged. This overflow was metered so that hydraulic
detention times could be established. Windt et al . (85) were surprised by t e
12
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large overflows measured, much in excesa of reports by other workers such
as Jones Ct al . (314). The disparity was attributed to the pigs playing
with their waterers. The ditch had a working volume of 3300 ft 3 and a
designed hydraulic detention time of 50 days, based on the expected
overflow of 60 ft 3 /day. However, hydraulic detention times occasionally
dropped to 10 days, and Windt et al . (85) comment that some of the
apparent reduction in oxygen demand may be due to dilution. Complete
odor control was achieved since the ditch always h.ad ample dissolved
oxygen present. Power requirements were reported to be 60 kwh/day. No
indication was giv n of the ultimate destination of the ditch liquor but
since this contained a 0D of 16,000 mgIl (just before marketing) i ,. would
seem further treatment would be essential.
Most of the literature is occupied with reports on underfloor
oxidation ditches. Though Pontin and Baxter (58) and Smith and Hazen J1 )
have e.perted on external ditches, there is little published information
on the effect of low temperatures upon treatment efficiency for livestock
wastes. Grube and Murphy (25) have described the operation of a ditch for
municipal wastes in Alaska. The rotor was covered but the dit h was open.
The minimum ditch temperature observed was 35.5°F (1.9°C) but SOD 5 removal
during the winter period exceeded 90Z. They practiced complete sludge
return, but they observed that auto-induced sludge discharge took place
intermittently. The hydraulic detention time was 2.3 days and the average
MLSS was 2000 mg/i. These results are very different from those reported
for agricultural wastes, though rather typical for municipal wastes.
3
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Renovation by Soil Percolation
Although the treatment systems described by Stander and VanVuuren (72)
and by CuIp (18) are capable of providing potable water, such systems are
not presently applicable to agriculture. Fortunately, using the soil
Itself for wastewater treatment can result in an effluent approaching
drinking water quality, as has been demonstrated by mans successful
use of wells for generations. Until recenty,groundwater recharge after
soil percolation has been unplanned, or ,ubsid a.ry to other water use
such as Irrigation or the disposal of septic tank overflow.
McCauhey and Krone (50) have coinpi led a very comprehensive review
of the literature associated with t e soil mantle as a wastewater
treatment system and their work will be referred to extensively in this
report. McGau iey and Krone (50) developed their review from preliminary
work with septic tank disi,osal fields because they found that engineering
guidelines were sparse, ir only applicable regionally.
The soil may be described qualitatively as comprising four distinct
components, inorganic solids, organic solids, aqueous solutions and
gases. Soil can exist in two states, aerobic and anaerobic. A fertile
soil which sustains a thriviig crop Is aerobic si,ce plant roots require
oxygen. A completely waterlogged soil containing organic matter and
suitable microfiora will genet alIy turn anaercSic. McGauhey and Krone (50)
examined the action of the soil on wastewater percolating through It and
they cite the iit rature as showing that soil maintained in an aerobic
condition will be able to remove mo e organic matter from the liquid applied
-------
than anaerobic soils, moreover aerobic soils will retain their ability to
transcnit water longer than anaerobic soils. Two reasons for anaerobic
clogging are cited: either that facultative bacteria seem to use the
wastewater to generate slime capsules of polysaccharides which block
the soil pores, or sulphur compounds are reduced to insoluble metallic
sulphides which cement the soil Particles together blocking further water
transmission.
The n vement of water through soil is governed by the rate at which
water may enter the surface, called infiltration, and the rate at which
water is conducted through the soil, called permeability. Unlike some
elgineering parameters neither infiltration r,te nor permeability are
immutable properties of the soil type. Continuous inundation of the soil
surface will ultimately decrease the infiltration rate because of anaerobic
bacterLal growth clogging the soil pores. Allison (3) conducted tests
using sterile soil and sterile irrigation water and proved conclusively
that after steady state Conditions (with regard to air entrapped in the
soil) were reached, soil permeability remained constant. Although Allison
(3) taks about permeability he also mentions that the maximum resistance
to fLw in nonsterile soil occurs in the top 12 in., hence it is the
infiltration rate which is affected by th microbial growth. -
The decrease in infiltration rate of inundated soil has led to two
approaches for groundwater recharge. Bouwer (10) has reported on the
Flushing Meadows project in Arizona using six parallel recharge basins with
grass, gravil or soil surfaces. Decreasing infiltration rates were overcome
-------
by using a cycle of 3 days wet and 1; days dry; in this manner, infiltration --
rates around 21; ipd per ft of water depth could be maintained. The other
approach, that of spray irrigation, has beer. used by Flower (21) for
disposing of a high strength drinking waste. Sprinklers were set up on
30 ft towers above a 30 ac wooded hillside, the Irrigating schedule was
8 hr on and 1 +8 hr off. Some runoff was observed b t this was small.
The object of any system of soil percolation is to ensure that the
percolate is inoffensive when It reaches the groundwater. In the past this
has merely required that the carbonaceous matter and the suspended solids
needed removal. However, recent concern over the eutrophication of lakes
has led to investigations into the rate of N £ P during passage through
the sell.
Carbonaceous material is removed very readily If the soil is allowed
to become aerobic intermIttently. Flower (21) reports that springs fed from
percolate that had passed through 9 ft of sand under forest floor litter
showed a SOD 5 10 mg/i, when the applied effluent was 4O0 mg/l. Bouwer (10)
found, using secondary effluent from a municipal treatment plant, that a
BOD 5 = 0.2 r. j/i could be obtained after soil percolation. But the soil may
not ilways be able to renovate the organic load adequately if it Is held
In an anaerobic condition; Stewart et al . (73) found that the groundwater
under actively used corrals In Nebraska showed an average soluble carbon
contents of 73 mg/l compared with 14 mg/i found under irrigated fields,
moreover, these ...orral samples were noted as having ar. offensive odor
suggesting anaerobic conditions.
16
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0ig. nte AMMUNII1CA1 l(I . VflI AT1I Il l I $
N;Ir,%en - I Il u ll 4 1 1 , 11,0
Compound. ii Ing urganlsni ,m,.,.o.n ion... i.e
ASSIMILATION
or
- - IMMOBII hAl ltI P. it roe..,. ..t.,
II P. 1 ), N,I ,.J.... II , . I, ..i
1 ) 1114 1, ill, II, I .. .. I. ii
C I.. i, I. I
In, r In ii , . Iii 1.11111 1 I. .. I
Figure 1. TransformatIon of nitrogen in soil
The application of nitrogen to soil can lead to a variety of effects.
Frederick and Broadbent (23) show that microorganisms cause a variety
of reactions as shown In Figure I. The agronomist has been most interested
In retaining N in the soil for plant use but the engineer s more interested
in removing N before it can accumulate in groundwater. Reference to Figure 1
shows that if a readily available carbon source is present some nltr gen
is converted into cell matter in the microorganisms using the carbon as
a substrate. However, as the carbon source is depleted, if aeration and
temperature conditions are favorable, then the nitrogen wi:l be converted
to nitrate via autotrophlc bacteria. Nitrate Is not readily absorbed by
soil particles or organic matter, hence the nitrate will readily move down
into the soil with leaching water. Brem9er and Shaw (ii , 12) examined
the reaction of nitr ne in conslderable detail and determined that if
conditions became anaerobic, and an available carbon source was prescflt,
most nitrate would be converted to gaseous N 2 0 and N 2 . Some very small
17
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conversion to NH 3 was determined, but this was considered trivial.
Temperature, pH, and degree of saturation were all (actors affecting rate
of denitrification. Over a 20 day period little denitrification occured
If the temperature dropped below 111°F (5°C). The percentage of dcnltrifl-
cation obtained was the same for all soils in the pH range 5 8. If the
soil water content exceeded 200% of field capacity then denitrification
was rapid. Aeration of soils below 70% of field capacity Inhibited
denitrificatlon completely.
Parlzek et al . (55) have described extensive renovation studies using
sprinkler iri ation. Using 1 or 2 ln./wk application rates on woodlands,
they found that 68 to 82% of the nitrate nitrogen in a secondary sewage
effluent was removed by the first 12 in. of soil. Four in./wk was also
tried but it gave inferior removals of 11. These tests were conducted
from June to December In Pennsylvania.
Meek et al . (Le4) have reported a field laboratory study using lysimeters
fitted with drain tiles. The lysimeters were 120 in. in depth and l5 In.
dia and the tiles were fitted at 76 in. 96 In. and 120 in. depths. The
tiles could be held below the water table b means of a syphonic discharge
tube. The lower pa-t of the columns ere maintained in an underground
laboratory L e1d at 77°F (25°c) but the top 3 In. of the column was exposed
to the atn sohere. All columns were plantea with Safflower ( Arthamus
tinctorius 1.) and the water table In all columns was held at 70 In. depth.
The Irrigation water was spiked with HH 11 NO 3 during the first and fifth
irrigation to gi ,e 100 lb/ac. Curves are presented that show the nitrate
18
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concentration to peak at 28 in. but to drop severely at the tile ot tlets.
Denitrification increased as the depth of the tile chosen for sampling.
Soluble carbon was shown to be present at all depths but the level decreased
with increasing total irrigation amount. Thirty seven in. of water were
applied to each cQLumn in the perIod October to January at approximately
two week intervals; only 140% of the water applied was recovered in the
drainage. Although DO-was shown to be present at all depths, It was
usually less than 1 mgll. The soil redox potential declined from 1400 my at
the water table to 0 my at 120 in. depth. Meek et al . (1414) conclude
by suggesting their results show that periodic drying increases soluble
carbon iii the soil solution and this should promote denitrification.
Another element of interest to engineers is phosphorus since this has
been implicated in the eutrophication of lakes. An early 10-yr study by
Morgan and Jacobson (146), using lysimeters plaited with tobacco, showed no
phosphorus leaching. Coleman (16) examined the P adsorptIon of kaolinite
and montmorillonite ciays and showed that, although pure clays with Fe and
Mn removed would adsorb PD 4 3 , twice as much would be retained In the
presence of Fe & Mn; however, such retention was hen a function o pH.
Mor . PO 3 was retained at pH 3 than pH 9.5. Cooke (17) has examined P
6 K mobility in soils and finds that P0 1 4 3 ions are very immobile, to the
extent that often more than 50% of applied P fertilIzer will remain in the
soil after harvest. He also conciudcs that In most cases soluble phosphate
fertilizer are better than less soluble forms. Retention of P by clays is
sometimes sufficient to cause large removals in the soils percolate
19
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(Parizek et al . (55) ) however Johnston et al . (33) have noted some
anomalies since they found appreciable quantities (i - 17%) of applied
P in Irrigation wattr, or fertilizer, could appear ii. the tile dualnage
effluent. The soils were Californian Panoche and Oxalis silty clays
which are permeable basin rim soils.
Summary
Wide spread water reclamation and reuse Is not only desirable, it
is imperative. By changing from straight through to recycled flow, one
establishment, or a complex using coordinated reuse, will use less fresh
water and also discharge less wastewater.
Hydraulic handling and transport of livestock wastes has much to
offer in terms of efficiency and labor savings. It does, however, employ
large volumes of liquid. Thus agricultural producers can learn much from
the manufacturing industries, although equally elaborate systems should
not In iediately be necessary. For example, the renovated effluent which is
to be used for hydraulic manure transport need not be wholly free of
organic matter. But some requirements which do emerge from the literature
are: the liquid must not smell b .d; it should be easy to handle using
standard equipment; and biological, or other, treatment should be low In
cost. The most frequently-recommended treatment system that satisfies all
three requirements seems to be the extended aeration process, In the con-
figuration of the oxidation ditch. The literature reveals, however, that
design data for treatment of livestock wastes by this method are currently
inconsistent, and often seem arbitrary. Odor control has been of more
20
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concern than has final disposal of the treated waste. Consequently
information concerning sludge production rates and the problems of handling
this material is sparse. Nutrient imbalance is of concern to agronomists,
but little information Is available on the levels of nutrients which may
be established in a recycling system.
Any excess water from the treatment system Immediately associated
with recycling may require further treatment before release to groundwater
or a watercourse. Spray Irrigation should be possble during the warmer
period of the year when the soil is thawed. The literature reviewed has
shown that C N & P are all decreased during soil percolation and the
effluent is very similar in quality to existing groundwater. Spray Irrigation
would seem irore promising than ponding or ridge and furrow appllca.Ion since
accurate grading of the terrain is of less Importance and control of
application rate more easily achieved.
21
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OBJECTIVES
Of the various methods for keeping low odor levels in a confinement
livestock buildings, two stand out. Either the manure can be aerobically
treated within the buiding to eflminate septic odors, or the manure can
be continuafly removed from the building before it can putrefy. The main
objection to the first alternative Is that restarting the aerator, following
a prolonged stoppage, may release sufficient toxic gases, such as
(Taiganides and White (55) ), to kill the animals in the house. Hence,
Iowa State University has elected to investigate external treatment systems.
Early disappointments with a mechanical manure remova system led to the
adoption of hydraulic transport. The work described in this report is one
segment of an ongoing project in which the basic parts of the system already
established were:
A 700 head environmentally controlled swine finishing building
A functioning anaerobic lagoon
An existing, but unconnected oxidation ditch
A preliminary study by Smith (70) had shown the feasibility of
treating t)e aup rnatant from the anaerobic lagoon and reusing this
treated effluant for hydraulic manure transport. The objective of the
present study was to develop a better, and more reliable, system for
recycling the treated effluent. The parameters selected for monitoring
were mainly chemical and were related to water quality. Odor is generally
associated with anaerobic or septic conditions, thus oxygen demand was
expected to indicate the potential that the treated effluent still
possessed for putrefaction. Both COD and BOD 5 were to be measured because
their ratio gives some indication of the stability of the organic matter
22
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In the liquid. Solids content of the liquids would give useful Information
on volatile solids reduction, sludge production, solids retention time and
th rate of buildup of dissolved inorganic matter. Measurements of nitrogen
forms and phosphate were made to find the fertilizer potential of the
effluent. The chloride ion is generally accepted as a useful inert tracer
in flow studies; hence this was chosen for detecting changes In concentration
of inorganic salts as recycling progressed. Total coliform counts were made
to indicate the sanitary quality of the returned effluent. Other measure-
ments of interest were temperature, water flow and power use.
The excess water contributed by waterer bplll, feces and urine was
stored in an anaerobic lagoon. This lagoon water was still a potent
source of pollution and cou d not be released to a water course without
further treatment. Rath (61) had tried this anaerobic lagoon effluent
in laboratory lysimeters the local prevailing soil type (Webster
silty clay loam) and found reductions in COD could be obtained in as
little as 2 in. of soil, if the lagoon liquor was applied for an interval
exceeding 8 hr in 24 hr. However, Rath (61) only ran each lysimeter for
4 days so his results are incor..;lusive with regard to quality renovation.
Thus, the Irrigation portion of this research was designed to determine
the degree of removal of C, N and P as the liquid moved down through the
soil. It was also necessary to relate applied quantities with soil moisture
conditions. Flnally,soIl samples were to be taken at intervals to monitor
the effect that treatment has on soil carbon and nitrogen. The study was
to be conducted over several lrrigat on seasons to determine if use of the
soil in this manner has any long..term detrmental effect.
23
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SYSTEM AND ITS OPERATION
Hydraulic Circuit
The research was planned in two phases. in Phase I. the manure slurry
was flushed from the confinement house, hereafter referred to as Unit K, to
an anaerobic lagoon (Figure 2). The ditch was 8upplied from the lagoon and
settled effluent from the ditch was then returned to flush tanks in Unit K.
Minor trouble with plugging occurred in the 8 inch sewers connecting Unit K
and the lagoon, these had too many abrupt changes in direction and
insufficient 8lOpe.
ecauae anaerobic lagoons are reputed to be evil smelling, Phase 2
diverted the manure slurry directly to the oxidation ditch. Gravity flow
was not feasible so Pumps 6 and 7 were installed. A lagoon was srill
essential to receive the overflow from the oxidation ditch.
Unit K
Unit K has an average capacity of 700 fL.ishing pigs. It is a totally
enclosed steel frame uilding, 50 ft .ide by 120 ft long. The floor slopes
at 1 ft in 120 ft in the longer dimension. The pens are nominally 5 ft
wide and are spaced each side of a central alleyway. The pen floors slope
at 1 ft in 2 ft from the center alley to a gutter 42 in. wide by lJ in.
deep. The two gutters are adjacent to the longer walls of the house. The
pigs are floor fed and have fre eccesa to the section of the gutter in
their pen. The liquid used for flushing is held in a tank, supported 8 ft
above the floor, at the upper end of each gutter. Each tank can discharge
2k
-------
GRAVEL FILTER
MANURE LIFT SUMP
$ETTLEO EFFLUENT
ro rLush TANKS
Si.ubGt RETURN
DITCH OVERFLOW
FILTER BACKWASH
LAGOON TO DITCH
NAP4URE LIFT STATIONS
Ftgure 2. Hydraulic crcuit Unit K
-------
up to 120 gal in 20 sec, this discharge is initiated by a time switch.
Anaerobic Lagoon
The lagoon has two cells; the fir t cell is about 8.8 ft deep nd
has a volune of 40,700 ft 3 , the second cell being a shallow extension of
the deep cell with a depth of about 3.05 ft and a volume of 46,300 ft 3 .
Only approximate depths can be given since the lagoon serves as storage
and thus varies in depth. This lagoon and its operating parameters have
been described by Wilirich (84).
0 idati n Ditch
The oxidation ditch is a simple oval with a single Passveer rotor.
A plywood cover was installed over the whole ditch in 1969 bec. use
intermitte t use of the ditch in wiflter had led to icing difficulties.
The cross section is t apezoida1 and is lined with concrete alabs. The
working volume of the ditch, as measured at the end of Ph ise 2 using a
chloride d]lution method, is 47,000 gal. Since this report is a
continuation of previous reae ch, the reader is referred to Smith (70)
for more detail. The aeration characteristics of the ditch before lining
are described in Knight (37).
Flush Tanks
Prelimir ary work had shown that a simple flap valve connected directly
to a small solenoid would not function reliably. The initial rush of water
dawn the discharge pipe just slammed the valve straight back on its s. at;
then this opening and closing cycle would continue rythmical ly until the
26
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tank was .e. cy. A mechanism was developed (Figure 3) in which a large
expanded polystyrene foam float provided the lifting force for the valve
and the solenoid only operated a latch mechanism. This device has worked
well once suitable construction materials were chosen. The float rod is
b:ass and siLdcs tn a nylon bush. Most of the latch pivots are small
sealed ball be.ar].ngs. The two tanks are identical and are adjusted to
contain the same quantity of liquid.
Lagoon to Ditch Pump. Pump 5
Previous experience (Smith (70) ) with a helical rotor pump mounted at
ground level was not satisfactory. This system was replaced by a wet hell
consisting of two 4 ft vertical sections of 5 ft dia concrete pipe. The
vet well is connected to the lagoon by a length of 4 .n. fibre pipe)
valved to facilitate maintenance. A domestic sump pump 1 with a Ό in.
mesh wire fabric screen, was used to pump lagoon aupernatsot from the wet
well into the ditcn. This pump was controlled by a float switch moun .ed
in the settling tank.
TI.is pump functioned until May 1969 and then burned out. When
irtspecLed the rotor and pump body were found covered in a dense layer cf
gray crystals (Figure 4 . These were later analyzed as Mg(N}1 4 )P0 4 . Rawn
et l . (62) had reported this material would plug pipes in anaerobic
digeaters. They mention that removal of c0 2 , causing an increase in pH,
would cause deposition. T e material has since l..een found wherever
anaerobic lagoon liquor is passed through a pump or small constriction.
Mg(NH 4 )P0 4 does dissolve in acid but it does not dissolve appreciably in
hot water. -
27
-------
r
y cz
I
L
l
- ____ S .4
--I . __ 4
I
Figure 3. Float actuated flush tank discharge mechanism. Top center.
Total assembly with the dust covers removed. Bottom left.. A
Float and flap valve latched In upper position by solenolt.
Bottom right. Valve mechanism in bier, seai p*tt?. . ., .
p
lr
-------
1
I . ,
.. . :
; ..tt % ;
Zt. -
. 4
1 P
.,-.___ 1 . - -
;a .__.jc. : -
r
F
I
(.
I
h
. . - -
4 _ \ ,
1 - -- . 4 _A -
L -
:e. P):4 A
Ά; xi :.
- b
L . - - - - - .
___________________________________________________
F Igure 4. Mg(NH 4 )P0 4 deposits on a puiip after being submerged in the lagoon for six months.
p . . ,
b D
-------
Rotor Drive Unit
The original rotor drive unit used in prior studic& (Knight (37) and
Smith (70) ) was a variable speed drive coupled to the rotor by a single
strand 1 in. pitch chain. Phase I. continued to use this unit since the
depth of im ar&ion was not great (7.5 in.) and the speed was only 75 rpm.
Roweveir, after Phase 1 was finisned, it was found that the output drive
shaft bearing of the variable speed drive unit was badly worn. Since
greater oxygen transter was required in Phase 2, the final speed of the
rotor was to be increa,jed to 120 rpm. Because this was the second failure
of the bearing, it was decided to replace the variable speed unit by a
simpler, more robust, unit. Tnis had a jack shaft ruaning in roller
bearings, belt drwen from a 900 rpm motor. Some changes were also made in
the chain case in an atte ,t tc control lubricant loss.
As operation was about to begin in August 1970, it was discovered that
the rotor bearings were a1s badly worn. These were replaced at short
notice with bearings fitted with incorrect grease seals. This deficiency
w s overcome durthg the test period by liberal daily greasing. Chain
lubricant was lost from the final drive case, partially as a caisequence of
the iacorc ct seals, hence wear on the chain drive has been rather severe.
The au hor has observed the .ator m&iufacturers design changes over the
years, and it seems that drive train longevity is a problem in cage-type
rotors. Robinson or nt . (65) have reported a completely new design of
rotor consisting of perforated discs, which they say show none of the
drive train problems of the Passveer design. Moreover, they claim Less
30
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horsepower is required for the same oxygen transfer rate, particularly at
high immersion depths and high speeds.
Settling Tank and Sludge Return
The settling tank shown in Figure S has a plan area of 5 ft x S ft, is
8 ft from the top to the apex of the hopper bottom, and is divided into two
parts by a baffle. In the Phase l plumbing prior to May 1969, the liquid
flowed through compartment B and into compartment A. Compartment A was
to function as a clear well for the suction of the effluent return pump
(Pump 1). The sludge was pumped back into the ditch by Pump 2. Two major
problems were encountered with this configuration: first, compartment A
began to fill with the fine material not settled out in B, ultimately
choking Pump 1; secondly, the rather tortuous st.ction to the sludge return
pump plugged causing this pump to run dry.
These problems were largely overcome in Phase 2. The effluent
return pump suction was brought up into compartment B and A was blanked off
by extendinpr the dividing wall. The sludge return pump was remounted over
compartr ent B with a more direct suction line. A further feature which had
to be incorporated was an overflow weir. This was fabricated from an
invarted 2 in. condulet box. The overflow drained into compartment A and
was then pumped into the lagoon by a domestic submersible swap pump
(Pump 3).
In spite of theae modifications the system did not function according
to plan. Thb m* ch higher solids level), established in the ditch with the
e
raw manure influent, producud a liquor that was more in the nature of a
fluidized carpet than a liquid. The hair, husk and dense biological floc
3 1
-------
EFFLUEN
SUCTION
(PHASE
AFTER
(Pi AsE2
Figure 5. Settling tank for oxidation ditch effluent
JULY 1969
SETTLED
SUCTION
SLUDG
RETURN
TO MAY 1969
1)
SLUDGE RETURN OVERFLOW
PUMP
32
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conspired to plug both the 1Ό in. suction to the sludge pump and the 1% in.
overflow line. Moreover, when the suspended solids level in the ditch rose
above 12,000 mg/i, n i appreciable solid/liquid separation took place) and
the hairy liquor plugkvd the suction strainer to the effluent return pump.
An open topped box, partially filled with a 3 zu. layer of 3 18 in.
gravel, was attached to the suction of the effluent return pump. Initially
this filter could be manually backwashed with fresh water, but later it was
connected to an extra pump (Pump 4) which could automatically backwash it
with settled effluent. By late January solid/liquid separation was so poor
that all screening was abandoned and a different pump was substituted for
effluent return.
After running dry for the second time, the small helical rotor pump
used for sludge return was abandoned. The initial replacement was a
domestic suap pump but it, too, pligged with hair, and polyethylene film
thought to be from rat bait bags used in Unit K. Finally a diaphragm
pump, fitted with 3 in. suction line, was installed and no further problems
were encountered.
Effluent Return Pump. Pump 1
Phase 1 used a conventionAl clear water centrifugal p z controlled by
a pressure switch responding to closure of the float valves zn the flush
tanks. This pump worked with little attention, except for periodic air
replenishment in the surge chamber.
For Phase 2 a new surge chamber was installed. This had a diaphragm
separating the liquid and air compartments and proved more satisfactory.
The centrifugal pump was regulated to deliver against 32 psi head. At this
33
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pressure, the pump was rated at 40 gpm. This producec an average upf low
rate in the settling tank of 460 gpd/ft 2 . However the tank was small 1 and
the positioning of baffle such that local upflow rates may have been much
in excess of 460 gpd/ft 2 . The poor liquid/solid separation was attributed
to excessive upilow rates. The Water Pollution Control Federation (81)
does not recommend a rate in excess of 800 gpd/ft 2 for small final settling
tanks. This view was further reinforced when it was found that the sludge
interface was at least 24 in. below the water surface after two hours of
quiescent settling. The centrifugal pump was replaced by a low speed
flexible impellor pump which was rated at 3.5 g m. Although the results
were at first encouraging, the sludge blanket would eventually rise and
plug the gravel filter. One favorable feature of the flexible impelior
pump is that it vii ]. pump some solids, so, for the last two months of the
test, no screening was practiced and the material was simply returned to
Unit K with the consiszency of thin soup.
To avoid prob]eme with the thicker fluid, the plumbing of the flush
tanks was altered so that they were bottom fed through their drain plugs.
The float valves thus were bypabsed and filling was contr iled by-a time
clock. The liquid levels in the two tanks could equalize through a
connecting pipe, maintaining approxiraately equal discharge from each tank.
Manure Lift Stations
As mentioned earlier, Phase 2 re quired that the manure be pumped from
Unit K to the ditch. The design of p amping facilities was affected by the
existence of two 8 ft dia and 8 ft deep manure storage pits, hence it was
decided to build two separate, but identical, pumping stations. A wet and
34
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FIgure 6. Manure lift stations
35
4
-1
1
-------
.. . . - - - - - -
- - _ _ _
dry well construction was chosen as shown in Figure 6. Helical rotor pumps
were selected because they handle solids quite well and are capable of
developing the high discharge heads needed should plugging occur in the
discharge line. Submerged auctions were used and discharge was to a 2 in.
d ia polyethylene force main: Valving was provided so that both stations
cot±Ddischarge either to the lagoon or to t-te oxidation ditch. This is
shown more clearly in Figure 2. Raw manure slurry contains a substantial
fraction of readily settled material, hence the i et well was constructed
with a sloping floor and the pump auction was located at the lowest point.
Upon flushing, manure entered through a duct high on the side of the we
veil and this gush of material proved very effective in scouring any residue
from the prior pumping.
Since flushing is intermittent, this was capitalized upon in the design
of the level control as shown in Figure 7. The switch has neutral bouyancy;
it hangs vertically down in air but tolls to a horizontal po;ition when
immersed. The two way mercury switch has two functions. When the liquid
level rises the float rolls over and the pump turns on. Then as the level
fal!s, the other contact starts a delay timer which is set so that the pump
stops after draining the wet well completely. The delay timer resets to
zero automatically on completion of the cycle. This rather elaborate
system was designed to ensure that the minimum quantity of solids are left
on the bottom of the wet well between flushes.
A simple 2 x I in. wire mesh screen was placed in the duct to catch
hard debris such as pieces of concrete, bolts and nails befote they could
injure t e pump. This screen plugged within two days with a dense mat of
36
-------
----- -- :i: :: - -- ...-
ROLL 90T0
HIGH
POSITION
Figure 7. Electr ca1 schematic
manure pumps.
I
----4
of the level control used to activate
37
-1
I
-I
I
.1
.1
I
1
1
II
I
.j
1
r- ..T
I . ....
SWITCH
DELAY
PUMP
MOTOR
MP
/OFf
L _
SOLENOID
STARTER
FLOAT
2
3
SWITCH
LINE
-
-------
--,---_.-- . ----------_ ____
hair. A ledge 2 in. high was placed In the duct and worked quite well as
a trap for heavy debris.
Metering
During Phase 1 the quantity of liquid being pumped into the tanks was
measured by two do atic water meters. No simple and low coat meter could
o devised to measure the effluent slurry flow, although it was known that
this was in excess of the tank discharge by the amount contributed by feces
and waterer spill. A three phase wattmeter measured the power consumed by
the rotor but the other motors were not metered.
At the start of Phase 2 the returned effluent pump, Pump 1, delivered
through water meters, but these rapidly plugged with hair, forcing the flow
to the flush tanks to be measured by a bucket and stopwatch. The delivery
of Pump 3 was correlated with running time. Neither of these measures are
likely to be very accurate. Motor metering was improved by switching
arrangements which allowed the choice of metering the rotor alone or the
rotor and Pumps 1, 2 and 3. Pumps 6 and 7 were not metered.
38
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-- -,----.----- - -_.i_. _
irrigation Field
An area 220 ft wide and 550 ft long, located directly south of the
lagoon, was used or the Irrigation field. This area has been in continuous
corn production since 1961; prevIous to that time it had been in rotation
pastures for swine. The field of which this area was a part had been
fertilized in the fall of 1967 with 120 lb/ac of N In anticipation of corn
production again the spring of 1968. The stalks were chopped and plowed
undi r in November 1968.
The soil of this area is Wisconsin glacial drift. In original form
it is characterized by a generally leve to flat or even depressed topography
with few natural drainage channels but frequent lakes, ponds and sloughs.
Artificial drainage has changed the characteristics greatly. The soils in
the irrigation area are of the Clarion/Webster complex. The subsolls are
heavy in texture, high in clay and relatively imperneabie. The lime
content is usually high. A shallow water table is also characteristic of
the area.
The Iowa Sprinkler Irrigation Guide (29) shows that ClarionWebster
soils may be expected to have an infiltration rate, when a cover ciop Ts
present, of 0.5 1 iph. Figure 8 shows the general layout of the irrigation
area. The topography is well suited to sprinkler irrigation with a maximum
slope of 3 in the northeast corner to nearly level in the southwest corner.
A small dike was built on the north, east and south sides as shown to
eliminate foreign drainage. No attempt was made to control surface drainage
across the plots within the irrigation field itself.
39
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...
The Plots and Tile Drolr s
The layout of the system used consisted of twelve plots 40 rt by 60 ft
in a rectangular patt -n (Figure 9). Each plot was provided with a 5 in.
clay drain tile at its cent r, laid appri..ximat-ely 4 ft deep. Th- b ffer
area between the plots was 40 ft which gave a tile spacing of 80 ft. The
two drainage dimensions were taker. from the Iowa Drainage Guide (29) for
the soils In question. The drains were deei. e necessary to ensure
drainage of the profile and to follow renovation of the effluent as It per-
colated through the soil. rhe tile lines drained to a sump where outflow
measurements and sampling for quality could be done. The buffer area
provided enough separation between pots so that percolating woter on one
plot would have no influence on tile flow rates C: those adjacent unirrigated
plots. The section of drainage line from each plot to iti associated sump
was not sealed.
Each of the three sumpb received drainage from four adjacent pots.
These sumps were 48 in. dia corrugated metal culverts with five connections.
Four connections led to each one of the plots and the fifth led to the main
drainage line. This main line drained nt an cdJacent surface drainage
ditch. The sumps had poured concre botto,ns.
The tile drain system was lnst..,led in M , 1968. The water table was
penetrated in all plots, usually at 3 ft below ti.e ground surface. The area
had been tile drained previously an old lines about 2 ft deep were uncovered,
these were sealed with a plug of clay . Because the new lines were now
below the water table, considerable drainage was observed once the construction
work was completed.
40 1;
I
-------
LAGOON
FINISHING
BUILDING
I
48
SWINE PASTURE
CONTINUOUS
CORN
47
CONT I NUOUS
CORN
45/
2 miles to
Iowa State campus
44
Scale: 1100
Pigure8. General layout of irrigation area
+1
-------
I io to
Lagoon
Sump Outlet Une
oa .
Sealed with Plastic
$0
10
1 LJ LL
4ftdeep I /
/
/
4
2T
a a
60
Scale: I 30
0
12
I
a
4
/
/
/
Sump
/
/
/
f
3
FLgure9. Plan of onehalf of plot and tile drainage system.
-------
Intermediate Sampling Points
During the first season of irrigat ion, lysimeter pans 1 as shown in
Figure I3, were placed at 3, 6, 12 and 30 In. depth at the center of each
plot. The pans were enbeddec in undisturbed soil in the walls of the tile
trench, the pans were partially filled with a layer of river sand before
being placed In position. The pans drained into sample bottles cor,tained
in a 2 ft x 2 ft plan by 1. ft deep lined and covered pit. These lysimeters
were similar to those used by Parizek at al . (55) in their study on the spray
irrigation of secondary municipal effluent.
These pans were not entirely satisfactory since they required the
soil moist,.lre content to exceed field capacity before sufficient sample
collected. In 1969 the plots were fitted with porous cup sampling points
at 6, 12, anI 21. in. As a check on the water passing below the tiles, two
well points at 6 and 8 ft were also installed. Figure H shows the position
of all sampling points in a plot.
Soil Preparation and Cover Crops
When drain installation was finished in 1969, the entire field was
springtooth cultivated three times and then seeded to tall fescue with a
Br ill (on seeder. however, because of the late seeding date of 10th May, the
fescue had difficulty competing with lrdigenous giant foxtail. The foxtail
was not a problem since the only Interest was to establish a good cover crop.
-------
Table 1. Lysimeter pan sizes
Depth from S4rface-j Pan Size-in
3 6by6
6 6by6
12 9by9
30 12by12
20-gauge gal van i zed
sheet metal
1/2 in. copper tubing
to collection bottle
Figure 0. Lysiineter pan
1&I.
-------
Irrigation Equipment
An engine driven centrifugal pump was used for Irrigation, this
developed 20 145 psI at the required Irrigation rates. An intake screen
with 1/8 in. mesh was used on the pump suction to prevent large pieces of
grass and other debris from entering the distribution system. The
aluminium irrigation pipe was 3 in. dia for both main and laterals, all
joints were fitted with quick couplers. A pressure gauge 20 ft downstream
of the pump discharge was used to set Irrigation rate.
Initally the system included six Rain Bird 25 TNT part circle
sprinklers with 9/614 in. dia nozzles. These were located one at each
corner of the plot, and are on each of the later-is halfway between the
o.L 4 - 0.70 iph, delivery at the ground depended upon line pressure and
climatic conditions. Application efficiency would include about a 20
loss due to sideways spraying caused by the sprinkler turning arms plus
loss due to evaporation. Later tests were run using only four sprinklers
and only one line per plot. The location of these and the resulting water
distribution is shown in Figure 11.
Irrigation Schedule
This section will discuss soil noist. re Criterion used for irrigation
scheduling, the terminology use as by Bayer (8). In l9 6 8,soil moisture
condition was determined gravimetrically. Shaw et al . (68) have examined
Iowa soils with regard to their wilting point and their field capacity.
WIlti.ig point was defined as that moisture content at which the soil
misture tension was 15 atm and field\capaclty was determined for well
drained field soils in situ . Usir.g this data,90% available moisture
145
-------
1I I I I
SOUTHWEST WIND
8 15 MPH
TEM PERATURE //
728I F
(0
rt
Oi
0
0i
C
0
C
rt
0
WELLS 6 8 FT DEEP
8/84INCH R%RT
CIRCLE SPAINKLER - ,
=
TILE DRAIN 4 FT DEEP
O. 0
4OBY6OFT PLOT
PIPE
1
EFFECTIVE APPLICATION
RATE, IPH
SUMP
0
5 10
SCALE IN FEE T
20
-------
(hereafte-r abbreviated as AM) corresponded to a soil moisture content of
29.0% (by weight) and 70% AM corresponded to 2 .5%. Since gravimetric
analysis required 2 hr for completion,soil tenslometers were Installed In
1969. The criteria used with these Instruments were; higher moisture content
for irrigation corresponded to 350 rib (note 1000 mb 0.987 atm) and lower
to 750 mb. All the above moisture contents refer to the top 12 In. of soil.
in 1968 the four treatments used were; t levels of effluent amount,
1.5 and 3.0 in. per application, and two levels of sofl moisture, 90% &
70% All. Seventy percent represented a high criterion for conventional
Irrigation, while 95% might be more typical of a disposal field criterion.
The lower application rate of 1.5 in. was a realistic minimum for
Irrigation set, while the upper application was near the maximum increment
this soil profile could hold between 95% AM and saturation.
If the rate of application is compatible with the infiltration and
percolation rates for a soil, application of lagoon effluent virtually assures
that anaerobic conditions will be established in the profile for a time.
This condition s caused by the Increased biological activity engendered by
the organic 1.mding in the nearly saturated soil. The literature reviewed
earlir (50) indicated that an aerobic rest period is almost mandatory
so that infiltration rare may be recovered. Only Irrigating after the soil
achieves an available moisture level of 95* AM indicated that the soil has
become aerated to at least the 12 in. depth.
For the next season it was decided to apply nitrogen in a known form
and also to irrigate with clear water In addition to lagoon water. The
47
I
-------
-.- -.
4
four treatments were now-equal in amount (2.0 In. per application) but
different in quality.
By 1970 it had become apparent that single applications of 2 in. caused
high transient concentrations of COD & N to reach the tile lines. Hence,
the four treatments were nowthe same total amount but one treatment was
3 daily applications of 2/3 in., while the second treatment was one
Continuous application of 2 in. Two moisture tensions were used for each
method of application. The three seasons applications are summarized in
Table 2.
Sanple Collection
In 1968 samples from the tile under each plot, the lysimeter collection
bottles and the surface catch pan were collected 12 hr after the beginning
of each irrigation. Collection of samples caused by natural precipitation
were collected 12 to 24 hr after the storm. The outflow rate from each
plot was measured daily by the bucket and stopwatch technique. In addition,
each sump was equipped with a V-notch weir and stage recorder that could
record the continuous outflow from any one plot.
In 1969 and 1970 tile draina;e water was sampled during each application
of 2.0 in. and during the first and third application of the 3 x 2/3 in.
daily applications. After the total 2.0 in. Irrigation was complete,
4 more samples were taken at 2 hr intervals. The flow rate was recorded
by bucket and stopwatch t each sampling so that a weighted composite
sample for analysis could be made for teach plot. Increased tile flow
caused by precipitation was also samp1 d. This sampling procedure biased
-------
JI
1
Ta le 2. Overall su r ary of field experiments used to study soil filtration treatment of anaerobic manure
lagoon liquid I968-O.
L
0
Njr bcr
Treatment
App1icatIc ns
Amount
in.
Ilic
drainage
concentration,
mg/I
COO
Total-N
P
C 1
1968-)
1968-2
1968-3
1968-4
Prec.
1.5 In. 7O A.M.a
3.0 In. at 7O A.M.a
1.5 in. at 95 A.M.a
3.0 in. at 95 A.M.a
9
7
10
11
-
139
20.9
15.2
30.5
12.5
513 b
30
30
32
33 ,b
65
52
54
72
72 b
0.2
0.7
0.li
0.7
110 b
75
80
76
79
.
1969-)
1969-2
1969-3
1969-4
Prec.
.
2.0 In. at 750 mb
2.0 In. at 750 mbc
2.0 in. at 750 JC
2.0 in. at 350 mbC
8
13
9
24
15.7
29.3
I8.Z
48.?
31.1
939 b
18
22 d
145
22
43e
120
306 b
60
9 d
76
58
296
98
.
73 b
0.2
0 3 d
2.1
0.2
1 j 1 e
2.8
127 b
75
2 ;d
95
75
2 1°
91
1970-1
1970-2
1970-3
1970-4
Prec.
2.0 in. weekly in 3,
2/3-In. daily applications
2.0 In. at 750 mbC
2.0 in. bi-wcckly In 3,
2/3 in. daily applications
2.0 in. at 350 mbC
13
7
7
15
27.3
15.3
14.8
3)4
32.0
1332 b
106
147
93
280
389 b
128
117
111
149
74 b
3.5
3.4
1.0
7.0
159 b
101
119
100
132
available moisture in soil at 6 -ln. deep, gravimetrically
lagoon liquid caught on plot surface
mU1ibars soil suction at 6-in, deep
tapwater after stored In reservoir and pumped to plots
etapwate ,. + N(NH 4 NO 3 + Urea) after storage in reservoir and
pumping to plots.
.4
U
-------
the results somewhat because it was assumed that a l flow caused by
Irrigation was of uniform quality; however, later work showed that quality
Improves shortly after Irrigation ceases. The low flow between events was
not sampled. The porous cups and well poInts (2 in the plot and 3 paIrs
In adjacent unirrigat d areas) were sampled as time p rmitted, usually
every 2 to 3 wk.
50
-------
RESULTS
Phase 1. Anaerobic Lagoon in the System. 1969
Manure transport:
During this phase each flush tank dIscharged 85 gal once each hour.
Cleanliness of the pens varied according to position and tii e. Just after
the fluah the top two pens (15 t of the flushing gutter) were essentially
clear of all manure. A hydraulic jump occurted after this distance and
cleaning was less spectacular. The action of the pigs feet in the gutter
was very beneficial since this kept the manure moe mobile. Watching the
slurry at the lower end of the house showed that it had adequate velcity
to transport 1 in. dia x 2 .n. manure pellets by rolling. At no time was
old septic manure observed in the pens containing pigs, but such conditions
would be observed if a pen were empty. The width of the gutter, 42 in.,
was too great for the available flow, hence some meandering would tate
place in empty pens, thus forming banks of decomposing manure. Since the
majority of the pens were occupied all the time these manure banks were not
important. An area in which settl d manure solids caused diffIcuties was
the 10 ft sect on of gutter between the last pen and the sewer, fly breeding
was observed here during he summer, but this was not difficult to control
by periodic hosing down.
Buildup of manure solids near a wafl has also been observed by Jones
et al . (35) and they suggest that a shllow 6 in. wide trough be formed
in the gutter at the wafl side. This c hange in channel cross section
increases veloci.ty and shear, thus Improving manure transport. The report
51
-------
by Jones et al . (35) also lends strength to the theory that flow
rates in a long flushing gutter are determined more by the hydraulic
characteristics of the channel than by the rate of release of water at the
head.
Fecal parameters:
Samples were collected for analysis daily. The collection was made
in the early afternoon immediately following a flush. The manure slurry
sample was taken by dipping three 300 ml samples from an open portion of
the sewer leading to the lagoon. The three subsamples were spaced equally
dering the time the wave of manure passed by the sampling point and were
composited. The samples from the lagoon and the settling tank were taken
from taps on the pump discharge lines. All samples were transferred to
the laboratory for analysis within 10 mi i i.
The difference between the raw manure and returned effluent strengths.
correlated with the quantity at water discharged from the flush tanks and
the pig population, was used to obtain fecsl parameters for the individual
pig. These are presented in Table 3 and it is seen that they agree well
with values in the literature as summarized by Nuehlung (47). The volume
of water tontribisted by waterer spill, ur 4 ne and feces was unknown during
this phase.
52
-------
Table 3. Fecal prothiction per pig. Phase 1
All in units of lb/lOOlb pig day
Month Feb. Mar. Apr. May Avg.
COD 0.5 0.89 0.87 0.61 0.72
B0D 5 Oioji al) 0.17 0.36 (1.38 0.24 0.29
Total N 0.04 0.045 0.03 0.032 0.037
Volatile solids 0.44 0.5 0.36 0.34 0.41
Lagoon as a treatment system: -
The lagoon is an unmixed anaerobic digester with an unusually long
hydraulic detention time of about 200 days. Some mixing is observed during
the warrer months of the year wRen boils of sludge lifted by CO 2 and CR 4
come to the surface periodically. During the winter it is postulated
that the methane forming phase of bacteria are dormant because of the
very lou temperatures and though the math function of the lagoon will be
settling there should also be some waste liquefaction by facultative
bacteria. OR.ourke (53) has found that at 59°F (15°C) methane formation
was inhibited, even at BolLds retention times of 60 days.
Reference to Table 4 and Figure 12 shows that the COD in the lagoon
supernata t was approximately ceristant from February to Apri I when the
temperature stayed around 34°F (Figure 13). Vigorous biological activity
and gas product onwerewel l underway by May as the temperature increased,
and it is evident that the accumulation of winter COD is readily digested.
Only one temperature measuring location was used, so this work is
insufficient to contradict 0 Rourkes (53) fIndings. However the present
- 53
j
-------
Table 4. Loading and treatment efficiency Phase I
Values based on measured parameters
Month February March April May Avg.
Number of pigs 640 661 618 666 646
7. COD removal 89.5 91 95.5 92.0
7. SOD 5 removal 78 88 88 96.5 87.6
7. total nitrogen removal 57.5 64 60.5 65 61.8
7. volatile sQlids removal , 89.5 91 91 86.5_ 89.5
VS loading, lbfft 3 day x l0 3.54 4.01 2.72 2.92 3.3
Hydraulic detention time 1 days 202 178 213 264 214
Oxidation ditch
7. COD removal 70 76 64 -- 70
7. SOD 5 removal 84.5 81.5 83.5 - - 83.2
7. total nitrogen removal 26.5 6 27 6 16.4
7. volatile solids removal 25 50 10.5 30 28.9
F/N ratio 0.058 0.039 0.028 0.006 0.033
Hydraulic detention time, days 13 11.5 16 17 13.9
Overall
7, (X)1) removal 95 97.5 97 87 94.1
7. SOD 5 removal 96.5 98 98 87 94.9
7. total nitrogen removal 66.5 66 69 67 67.1
7. volatile solids removal 92 95.5 95 90.5 93.3
-------
LAGOON SUPERNATANT
CHEMICAL OXYGEN DEK AND
(0 17 24
FE
to I
(4 21 28 6
MAR APR
I I
2 19
MAY
Figure 12.
The cnemcal oxygen demand of the
naerobc lagoon during Phase 1
supcrnatant from the
COD
MG/L
ooo
2000
(000
0
2b ( 1969)
55
-------
20
Figure 13.
The total phosphate concentration and the temperature of
the supernatant from the anaerobic lagoon during Phase 1
P0; 3
P40/ L
600
0O
LAGOON SUPERNATANT
TOTAL ORGANIC PHOSPHATE
a
T
F
I E PE RAT (JR E
90
30
I
FE B
NA.R APR MAY
56
-------
- - - ---- - --- - - -- S t
information does give some indication that methane formation (as Indicated
by gas production) does take place at 55°F. The lagoon is a good waste
treatment system for livestock producers because it will accomplish large
reductlor.s In COD BOO 5 and volatile solids; but it is very obvious 1
noting the values of the COD shown In Figure 12, that anaerobic lagoon
effluent is not suitable for direct discharge Into public waters.
Table i shows that there was an apparent removal of 60% in nitrogen
on passage through the lagoon. Several mechanisms may be responsible;
dilution, volatilization from the surface, cell formation and precipitation
dre but few. Dilution cannot be neglected since it was found in Phase 2
that for each pig, about 1.26 gpd of extra liquid is added due to waterer
leakage, washdown, urine feces, etc. Addi-ionally there will be unknown
quantities of water added by runoff, snownelt and ice melting. Volatiliza-
tion is examined later in this report, but it is unlikely that loss by this
mechanism is significant until the Ice is melted. Cell formation in
anaerobic systems is slow compared with aerobic systems, so,..4. ring the
winter, the fraction converted to cell mass should be very small.
Precipitation of nitrogen an inorganic form Is a distinct possibility when
magnesium, calcium and phosphate are also present. Recently Salutsky et al .
(66, reexamined the formation of Mg(NH, )P0, in a municipal anaerobic
digester, because this product has poter ,tIa l value as a ferti zer and is
also capable of reduci. g N and P in sewage lant effluents. The Handbook
of Chemistry and Physics (82) shows that Ca(N.1 4 )P0 4 and I1g(NH 4 )PO are
poorly soluble in cold water and neutral pH. No measurements of Ca or Mg
were made but some estimates can be mjde. The feed used in Unit K is
57
-------
compounded acccrding to Iowa State University recommendations found in
Hodson et al . (28). lne feed contains 0.66% of Ca on a dry weight basis)
and a pig weighing 125 lb (mean weight of the pigs in the house) will
consume 6.4 lb of feed each day. The Agricultural Research Council U.K.
has surveyed the literature on swine nutrition up to 1967 and they conclude
that Ca stored ii. the finishing pig body amounts to 7.5 x 1O lb/lb of
daily gain. Hence,at a daily gain of 1.75 lb/day (Hodson et al . (28) )
the retention rate of Ca will be about 1.3 x l0 2 lb/day. The amount
of Ca fed is 4.26 x io2 lb/day;hence,an average 125 lb pig will excrete
about 2.95 x 102 lb/day of Ca. Using valies of 646 pigs in the house
(Table Li) and 4000 gpd for the flush quantity, then the expected Ca
concentrat on in the manure slurry is 570 mg/I. Observations indicate
that P is not limiting; hence, if all the Ca fed remained in the lagoon
In the form of insoluble Ca(NH 4 )P0 4 , then this compound could account
for 200 mg/I of the influent N.
Figure 13 shows an increase in phosphate concentration after the
spring thaw. At first this was attributed to organic material being lifted
from the bottom ind mixed in the main mass of liquid. However the analysis
of the crystalline deposits found on the pump led to some other possibili-
+2 +2 + -3
ties. As mentioned previously, it is known that Ca , Mg , NH 4 and P0 4
will form a variety of insoluble, or poorly soluble compounds. Under
laboratory conditions, Ca 3 (P0 4 ) 2 or Ca(NH 4 )P0 4 (hydration status not known
for either compound) are both very easily resuspended by mild agitation.
The Murphy and Riley (48) method for phosphate determination uses an
acidic solution of amnonium molybdate and ascorbic acid. Since Mg(NH 4 )P0 4
58
-------
is soluble in weak acid, it Is assumed that this phospnate test wifl
measure the phosphate in Mg(NH 4 )PO, 4 , and most probably other calcium
and magnesuim phosphates as well. Hence It is postulated that scme
part of the phosphorus increase observed during the spring biological
activity is due to particulate Inorganic phosphates being brought into
suspension.
The total coliform reduction in the lagoon varied with time. During
the period (up to the end of March) when the lagoon was quiescent, the
percentage remaining in the lagoon effluent was 0.257.. As the biological
activity increased the count varied widely and in May the least count was
a percentage remaining of 0.0537., and the ,reat st 0.6Z. This variation
could be correlated with the suspended solids carried in the lagoon
effluent.
The dissolved ino ganic solids and chloride concentrations in the
lagoon fluctuate according to rainfall. A discussion of these measurements
in the later section on the results of Phase 2 explains more clearly why no
upward trend in dissolved inorganic solids concentration was noted.
Oxidation ditch as a treatment system:
The literature ( l, 67) indicates t iat treatment efficiency will
primari .y be a function of influent strength and MLSS content. The volume
of the treatment tank will be a secondary variable related to the solids
level that can be carried in accordance with the solid/liquid separation
devices available. Another econdary variable is the aeration capaci-ty.
Because the system is operating in the extended aeration regime, aeration
capacity may approach the COD pluB nitrification requirements of the
59
-------
in fluent.
It should be noted that the ditch was not initially void of biological
material because of its intermittent use after the preliminary study (70).
Together Figures 1 s and 15 show that there was little change in the BOD 5
of the settled effluent as the level of volatile suspended solids in the
ditch increased. This seeming contradiction to McLellan and Busch (51)
may not oe so, since their theory relates to soluble BOD 5 and the
supernatant BOD 5 measured was known to contain some fine suspended matter.
MiddlebrGoka et al . (i 4 5) have also examined the composition of the soluble
and suspended fractions from extended aeration and they conclude the major
part of the BOD 5 is present in the solids.
Table 5 shows how the food to microorganism ratio varied through the
test. Fooci is based on BOD 5 concentration and microorganisms arcs based on
MLSS so that values of this parameter may be compared with those of
Scheltinga (67). The wide variation in influent load to-the ditch was
caused by mechanical difficulties with the flush tanks. Tie F/M ratios
are generally less than the 0.05 lb BOD 5 /lb )4LSS value recommended by
Scheictaga (67). This indicates that the ditch was larger than necessary
sin ..e no difficulties were encountered in settling, even at the highest
MLSS encountered. The sludge volume inc x was generally less than 50 and
the greatest value was only 66.
t4cCarty and Brodersen ( 1 e9) have examined the extended aeration
process and they conclude that a mathematical model may be written for a
steady state condition. This model starts with the equation
dM dL-bM
a (2)
60
-------
a
cooa
MGIL
1200
1000
800
600
400
200
0
3 10 17 24 3 tO I7 ir5
FEB MAR
12 19 26
MAY (1969)
Figure II.. The chemical oxygen demand and the five day biochemical
oxygen demand concentrations of the sectled effluent from
an oxidation ditch fed anaerobic lagoon supernatant during
Phase 1
6
-J
BOO 5
SETTLED EFFLUENT
CHEMICAL OXYGEN DEMAND th
BIOCHEMICAL OXYGEN DEMAND
/
14 21 2816
APR
-------
- - - - -
N
MG/L
600
500
400
00
200
100
FE B
MA
Figure 15.
The forms of nitrogen and the temperature found ir the
settled effluent from an oxidation ditch fed anaerobic
lagoon supernatant during Phase I
SETTLED
NITROGEN
TEMPERATURE
EFFLUENT
FORMS &
T
F°
90
70
I
/60 ,
I
r_JN TRO
__.
50
R APR MAY( 1969)
.4
62
.. -. - - - (_r
-------
SOLIDS
MG/L
3000
2000
P 000
- -- - -
10
17 24 3 10 I7 24 3 1 7 (4 21 28S 12 19
F
EB
MAR APR MAY
Figure 16.
The volatfle suspended solids and the fixed dissolved
solids c.. ncentrations foui,d In an oxidation ditch fed
anaerobic lagoon supernatant during Phase I
DPTCH CONTENTS
VOLATILE SUSPEP4DED SOLIDS
a
FIXED DISSOLVED SOLIDS
0
3
.1
63
-------
CC
IlG/L
300
SETTLE D E
CHLORIDE
FFL UENT
a
RAINFALL
RAIN
INCHES
3
2
0
FEB
APR MAY
MAR
Figure 17. Th chloride Ion concentration found in the settled
effluent from an oxidation ditch fed anaerobic lagor,
supernatant and the raLnfafl record for a location near
the lagoon during Phase I
6 1 e
-------
Table 5. Food to microorgariis n ratio in the oxidation ditch. Phase 1.
Date
BOD 5
MLSS
F/M
1bBOD 5 I
Day/No/Yr
1 1 b/Day
lb
1b SS
3/2/69 19.5 498 0.0392
10/2/69 32.9 560 0.0588
17/2/69 49.4 1050 0.0470
24/2/69 -- -
3/3/69 33.5 954 0.0351
10/3/69 69.1 8S1. 0.0812
17/3/ 69 25.7 1010 0.0254
24/3/69 27.6 1l7 0.0236
31/3/69 30 1240 0.0242
7/4-/&9 -- - - --
14/4/69 42.6 1680 0.02 .4
21/4/69 40.6 1310 0.0310
28/4/69 31.7 1400 0.0226
5/5/69 -- -
12/5/69 6.98 1500 0.00 65
1915/69 13.8 1430 0.00 65
26/5/69 8.53 902 0.00945
65
-------
Where
Rate of generation of volatile suspended solids
a Cell yield coefficient
Rate of soluble substrate removal
dt
b Endogeneous decay coefficient
Ma Mass of organisms undergoing endogenous respitation
The results of this research were examined carefully to determine if
a and b could be evaluated; but it was concluded that since the system
never achieied steady state, no use could be made of the model. The model
is considered good for the process in hand because it allows the prediction
of the effluent &,D 5 , incorporating all the solids discharged. It is
interesting to note that McCarty and Brodersen (49) conclude, on
theoretical grounds, that the effluent BOD 5 is a function of the suspended
solids and that this was vericied by Middlebrooks et al . (45) using
chemical analysis.
The jump in COD and BOD 5 observed in late April was due to an
unintended discharge of sludge from c..mpartinent A (Figure 4). Before
this occurence tne effluent from the settling tank was slightly turbid,
odorless and pale yellow in color. Similar descriptions were made by
Clayton and Feng ( 5)and Scheltinga (67).
The axii zm aeration capacity of the rotor under standard conditions
(68°F, 0 mg/i DO and p 29.92 in Hg) at 7.5 in. immersion and 75 rpm
was 102 lb 02 per day. Reference to Table 5 shows ttat this was more than
adoquate to cope with the influent load. Such excess aeration capacity
66
-------
should have ensured nitrificat on but Figure 11 shows that this did not
occur for 8 wk. The minimum solids retention time for nitrifying bacteria,
given by Balakrishnan and Eckenfelder (7), is 3 days at 68°F (20°C); thus
it is assumed that the delay was a temperature effect. Ludzack and -
Ettinger ( 3) have indicated that nitrificatiori 18 insignificant below
41°F (5°C). Excess aeration capacity is evident from Figure 5 because the
ammonia N recorded before nitrification is almost entirely replaced by
oxidized N. The irregularity during the week beginning 21st April was due
to a period when the rotor stopped. -
Reduction in volatile solids was not as great as had been expected.
This is attributed to fine suspended solids being carried over in the
effluent.
Phosphorus reduction during passage through the ditch varied. During
the period from 3rd February to 34th April, when the solids level in the
ditch was rising, there was an appreciable phosphate removal. however the
last part of the test period was marked by solids decline and the trend of
phosphate :eduction disappeared. Nesbitt (52) has reviewed phosphate
re-ioval by activated sludge, and he reports that the VSS from a treatment
plant can contain between 2.67. to 77. P by weight (dry solids), depending
upon operating conditions. The upper figure was for a well aerated sludge
with an F/M ratio of 0.5 lb BOD/lb } SS. A linear regression applied to
the VSS results from 3rd February to 14th April (Figire 16) yields a rate of
growth of 11.6 lb/day. An estimate of the VSS removed in the returned
effluent yields 4.56 lb/day. Therefore, enou h P must be supplied to
produc.2 a total of 16.2 lb/day of VSS. Using a mean flow rate through the
67
-------
ditch during this period of 3170 gpd shows that a VSS phosphorus content of
2.61 would require 41 mg/i 2O 1 3 to be removed from the flow, but the uppe
value of 7.07. would require ill mg/i. Table 6 shoirs tnat the mean
difference between infltient add, effluent during the same time period was
118 mg/I. Even allowing for the variability in measurements, it does appear
that the sludge was storing a rather high quaztity of phosphorus, escecially
considering the F /N ratio was only 0.04 lb BOD 5 /lb 14LS5 during thi.s period,
compared with the value of 0.5 lb 80D 5 /lb ass quoted by Nesbitt (52).
For reasons discussed earlier, the chloride concentration shown in
Figure 17 does not show the expected urward trend. The rapid decline in
late March is attributed to the melting of the lagoon ice cover.
The record of nR in Table 6 may be correlated with the establishment
of nit :ification by the and of March. The early p H was around 8 when the
ammonia level was high, but this dropped to 6.5 !fter nitrification was
well established. This drop in pH is mentioned by Adema (1) and al.o by
Mccarty arid Brodersen (I 9)
Power requirements: -
The average power consumed by the rotor on a wire to water basis was
57.9 kwh/day. The whole test period yields an average value oZ SOD 5
destroyed in the ditcn of 24.8 lb/day which gives a power demand, per unit
of ROD 5 destroyed, of 2.3 kwh /tb 8OD . Nitrification was extensive?
suggesting that the aeration capacity pf the rotor was in excess, so the
value of 2.3 kwh/lb B0D 5 may be unrepreaentatively high. On an individuat
pig oasis, the power requirement is 0.09 kwh per pig.
68
-------
Table 6. Phosphate and pH in the Lagoon and returned effluent. Phase 1
Date
Acid hydrolysed phosphate pH
Lagoon Ret. Eff. Diff. Lagoon Ret. E ff.
Day!2 ko/Yr
mg/i
mg/i
mg/I
3/2/69 192 73 119
10/2/69 205 84 121 7.4 8.3
17/2/69 230 93 137
24/2/69 -- -- - - --
3/3/69 228 93 135 7.4 8.1
101 3/69 278 120 158
17/3/69 286 116 170 7.5 8.2
24/3/69 160 110 50 7.5 8.2
31/3/69 214 96 118 7.4 8.0
7/4/69 200 80 120 7.4 7.9
14/45f9 280 128 152 7.6 7.8
21/4/69 350 154 7.5 7.7
28/4/69 324 784 7.3 6.3
515/69 530 660 7.3 5.6
12/5/69 - - -- --
.9/5/69 428 616 7.3 6.2
26/5/69 440 468 7.3 6.8
69
-------
Phase 2. Manure Diverted to the Ditch
Manure transpo t:
This phase started using a 1 hr flush period, but difficulty with
rising sludge in the settling tank was experienced. The flush interval
was increased to 2 hr in the hope of improving settling. The flush
quantity was increased by raising the float valves in the tanks to
compensate for the longer interval. In practice, flush quantities were
variable, but the average flush was judged to be 100 gal for each tank.
Liquid flow into the tanks was not measured accurately during this part of
the test because the water meters were not reliable. The pen cleanliness
did suffer from the reduced water use, but the effect was margina.
Fecal parameters:
The values presctted in Table 7 are lower than those shown in Table
3 (Phase 1). They are also lower than those reviewed by Muehling Qe7).
The discrepancies are ascribed to faulty sampling technique. During Phase
1 the samples were collected after lunch when the pigs were fully active,
whereas sampling in Phase 2 took place in the early morning, before the
morning feed. The difference between the results clearly indicate the need
of composite 24 hr sampling.
The non-nitrifying 80D 5 teat (outlined in Appendix A) is of some
significance, if BOD 5 is to be used as a design parameter. Young (88) has
indicated that 4.33 g of 02 will be required for each 1 g of N converted
to HNO 3 (this value adjusts stoichiometric values for cell growth and 02
contribution by the autotrophic nitrifiers). Therefore the BOD 5 measured
70
-------
Table 7. Fecal production per pig. Phase 2
All in units of lb/bUlb pig clay
Month Aug. Sept. Oct. Jan. Fcb. Mar. Avg.
0.25 0.51 0.27 0.39 0.29 0.26 0.33
BOD 5 (Normal) 0.12 0.23 0.16 0.14 0.l 0.22 0.18
BOD 5 (Non-nitrifying) - -- 0.11 0.12 0.12 0.14 - 0.12
Total N 0.024 0.025 0.04 0.026 0.033 0.025 C ,.029
Volatile solids 0.26 0.19 0.17 0.24 0.23 0.24 0.23
3
Total P0 4 0.041 0.028 0.018 0.019 0.0086 0.0047 0.02
-------
on raw manure, using a seed containing active nutrifiers, may be expected
to give values appreciably greater than tL true carbonaceous B0D 5 values.
Fron the nature of the recycling system, in Phase 2 the raw manure was
continuously seeded in this fashion. During the period 11th January to 1st
March, when the mean difference between the normal anc nitrificatior.
inhibited BOD 5 was 3870 mg/i, the mean value of NH 3 - N was 455 mg/i
yielding a theoretical nitrogeneous oxygen demand (NOD) of 1970 mg/i.
Although this theoretical value was only half the NOD measured, the
discrepancy may well be due to the easily hydrolyzed organic N in the
manure not measured in the NH 3 - N test.
Overflow quantity:
A bettsr water balance was obtained during the second phase because
the treatment volumes were better defined. The supply to the tanks was
measured and an overflow welt maintained the ditch level constant.
Discharge over this weir represented excess water entering the system.
The cover over the ditch was not watertight so an unknown quantity of
water was contributed by rainfall and snowmelt. Rainfall between lAth
January and 15th February was minimal, hence the overflow originating
during this period may be considered as originating entirely from Unit K.
The mean value of overflow during thiS period was 773 gal, :r 1.26 gpd per
pig. Taiganidea (75) reported g average winter value of 0.71 gpd per pig
in the same building. The difference may be due to increased waterer
leakage and less floor evaporation.
72
-- -- .-
-------
Oxidation ditch as a treatment system:
As in Phase 1 the oxidation ditch was started witn some initial
biological solids. The break in data collection between October and
December was caused by equipment malfunction. The helical rotor sludge
pump proved inadequate and some time elapsed before it was replaced by a
diaphragm pump. Concurrent with this delay was an electrical fault in the
rotor control gear. The fault was finally traced to corrosion in a switch.
Although these difficulties were corrected by late December, reliable
results during early January were prevented by a severe blizzard at the
tu of the year.
As explained earlier, the fecal parameters obtained during Phase 2 are
not considered representative, therefore the iz.fluent load to the system is
based on earlier results obtained by Taiganides and Hazen (J6). These
measurements were also made on Unit K, but hr composite sampling was
employed. The decrease in COD, VS and N are shown in Table 8. Removal
has been defined as:
Removal Influent - (Effluent + t.orage)
wnere the storage term was calculated from:
Storage Daily rate of parameter concentration increase x Ditch volume
Since the settling tank was ineffective during the last part of the
research, the solids concentration in the ditch was not very different from
the concentration in the overflow. Therefore the solids retention time was
approximately equal to the hydraulic detention time and, using 77 gpd as
the discharge from the system, a detention time of 61 days was obtained.
This long detention time accounts for the large decreases in COD, VS and
73
-------
Table 8. Loading and treatment efficiency. Phase 2. Influent data based on Taiganides and
Hazen (76) data for the 100 lb pig
COD 0.84 lb/day VS 0.70 lb/day N 0.06 lb/day
11 Jan.
L v Jan.
25 Jan.
1 Feb.
8 Feb.
15 Feb. 2
2 Feb.
Avg.
Number of pigs
582
616
632
621
596
613
626
612
Overflow rate, gpd
685
573
722
1160
725
2140
650
950
Hydraulic detenU.on time,
days
69
82
65
41
65
22
72
59
Chemical oxygen demand
611
647
664
652
626
644
657
643
Influent, lb/day
Effluent, lb/day
56
57.4
112
144
65.3
314
6 .5
Storage, lb/day
151
182
73
&.16.8
38.8
-42
78
Removal, lb/day
404
408
479
525
522
372
672
483
Percent removal
66.1
63
72.1
80.5
83.4
57.8
102.2
75.0
Volatile solids
509
539
553
543
522
536
548
538
Influent, lb/day
Effluent, lb/day
46.5
18.3
123
118
64.1
228
57.8
Storage, lb/day
22.4
69.8
63.9
78.5
27.5
22.7
-78.8
Removal, lb/day
440
451
366
04
430
285
569
435
Percent removal
86.4
83.7
66.2
92.8
82.4
53.2
103.8
81.2
Nitrop .en
,
Influent, lb/day
Effluent, lb/day
43.7
5.43
46.2
3.72
47.4
6.27
46.6
14.2
44.7
5.02
46
30.7
47
2.92
45.9
Storage, lb/day
Removal, lb/day
Percent rea ova1
10.7
49
112
6.16
36.3
78.6
6.43
34.7
73.2
-1.96
34.4
73.7
1.69
38
85
-7.02
22.3
48.5
3.37
40.7
86.6
36.5
79.7
-------
Table 9. Food to microorganism ratio in the oxidation ditch. Phase 2.
Based on 0.38 lb BOD 5 I100 lb pig, Taiganides and Hazen (76)
Date
Day/Mo/Yr
BOD
lb/Day
)ILSS
lb
F/N
1bB OD 5 /
1bi .ft.SS
24/8/70
273
2275
0.12
31/8170
273
3037
0.09
7/8/70
236
2966
0.078
14/8/70
236
21/8170
236
2385
0.099
28/8/70
236
2581
0.092
5/10/70
219
2993
0.073
12/10/70
222
3558
0.062
28/12/70
273
4520
0.060
4/1/71
2 3
--
11/1/71
276
4810
0.057
18/1/71
293
4845
0.060
25/1/71
300
6156
0.049
l2/71
295
6277
0.047
8/2/71
283
5186
0.055
15/2/71
291
6771
0.043
22/2/71
297
5932
0.050
1/3/71
314
5908
0.053
75
-------
N noted in Tab e 8.
Zecaut of the large increase in loading on the ditch, the F/M ratio
is considerably different from Phase 1, as a comparison of Tables 5 and 9
shows. The F/M ratio becomes stable around 0.05 lb BOD 5 /lb SS when the
cuspenoed solids level off at about 14,000 mg/i (Figure 20). This value
is at the upper end of the recommended range of solids concentrations
given by Scheltinga (67).
Conventional waste treatment incorporates liquid/solid separation
hence treatment efficiency is usually related to the oxygen demanding
substances remaining in soluble or colloidal form in the effluent. When
such a standard is applied to the re turned effluent, both the BOD 5 and
COD of the liquid portion of the effluent are quite low (Figure 18),
andicating a high level of treatment by the system. However, in Phase 2,
settling proved difficult even though the results obtained in Phase 1,
where sludge densities of 20,000 mg/I were found, indicated that settling
should be possible at 1 SS of 14,000 mg/i. Part of the settling problem
is as..ribed to the hair and husk now present in the influent.
Denitrification also contributed to settling difficultieg.
The solids generated in the ditch will need further treatment, since
they are not stable and the mixed liquor putrefies readily on standii.g for
more than 8 hr. The high level of suiphates (Figure 21), which are thought
to be an unidentified component of the feed, ar,.. a source of odor, since
these arc :educed by a period of anaerobioais. This aulphw transformatiurn
might prove to be a major disadvantage of recycling since the sulphate
levels at the end of the test had exceeded 500 mg/i.
76
-------
- -, --
6 BOO 8
SETTLED EFFLUENT(SUPERNATANT)
CHEMICAL OXYGEN DEMAND
BIOCHEMiCAL OXYGEN DEMAND
I7 z43i T 7
AUG SEP
Figure 18.
(C EN TR A TE)
.COD
J/ OD5
12 19 262 9 16 2 d 14 21 284 II lB 25I 9 l&22I 6
OCT NOV 0EC0970) JAN FEB (1971)
Thu chemical oxygen demand an the five day biochemical
oxygen demand of settled effluent from an oxidation ditch
fed raw man .sre. The results for August nd September 197fl
are for the supernatant; the results for January and
February 1971 are for centrifuge supernatant Phase 2
COD
c 4 O/L
1500
1000
500
0
77
-------
C . - . - - - -
N
N G/L
300
200
100
0
Figure 19.
The forms of nitrogen and the temperature found in the
se t)ed effluent from an oxidation dtch fed raw manure;
the results are for Phase 2
78
SETTLED EFFLUENT
NI TROGN
FOR US
a
TEMPERATURE
T
F
90
NITRO
80
I\
I
I
I
I
/
I
70
/
/
\,
4
)
:1
AUG SEP OCT NOV DECU970 dAN FEB( 197 1)
4
3
-------
- =_i - - -
vSs
£IG/L DITCH CONTENTS
I5 OO VOLATILE SUSPENDED SOLIDS
a
FIXED DISSOLVED SOLIDS
10000
-, vSs
7 FDS
5000
0
I 243I 7 42l 28 5 12 19 26 2 9 16 233d7 1421 2814 II 18
AUG SEP OCT NOV DEC(1970) JAN
Figure 2 . The volatile suspended solids and the fixed dissolved
solids concentrations found In an Oxidation ditch Ld
raw manure; the results are for Phase 2
79
FDS
MG/ L -
. 00
.9
- I 000
0
I I I T
8 15221 8
FE 8(1971)
I
I
2000
1
j
I
-i
- - .-. - -
___ _. _ __ . _-._ .,_., _-_.-._, __ _& . -
-------
CC,S 042
.tGIL
600
500
400
300
200
1 00
0
FIgure 21.
IJT1
NOV DEC(1970) JAN
RIUN
F E B(l 7I)
The chloride ion and sulphate Ion concentratIons found In
the settled effluent from an oxidation djtc fed raw manure
and the r infal1 record in . location near to the ditch; the
results are for Phase 2
80
SETTLED EFFLUENT
CHLORIDE SULPHATE
8i
RAI N FALL
INCHE
3
S Y 2 \
4
S
I
F
I
I
c 1
A
N
AUG SEP OCT
H
T
-------
Nitrogen removal in the dicch during Phase 2 as around 807.
(Table 8) compared with 167. in Phase 1. This difference seems best
explained by inspection of the aeratiOn capacity available. The otor
was running at 12 in. immersion and 120 rηm, and Knights (37) data shows
that the aeration capacity was 504 lb 02 per day under standard conditions
(68°F. 0 mg/I DO and p 5 29 . 9 Z in Hg). The COD edu. tLon amounted to a
mean value of 684 lb/day; hence this would iii Itcate that aeration capacity
was very marginal, particularly since Loehr ejj.j i . ( 2) have shown that
the oxygen transfer coefficient drops appreciably as the concentration of
solids increases. Thus it is hypothesized that there is adequate
diasolved oxygen in the zone just downstream of the rotor for nitrific ition
to ta.e place; but farther along the ditch oxygen is depleted by
carbonaceous oxygen demand, thus denitrification takes place. Balakrishnan
and Eckeiiielder (6, 7) have studied both nitrification and denitrification
and their findings are:
a) Nitrification.
Solido reteL.tion tine is to exceed 3 days at 68 F.
P/H ratio shot)d be less than 0.8 lb BOD 5 /lb MLSS.
Nitrification increases as the ratio C/N increases.
h) De itr1 ficat ion.
.SS level should be high.
Readily available carbon source is necessary.
Anaerobic conditions must prevail.
High levels of nitrate nitrogen enhance denitrification.
All these conditioi a can be met as the liquor passes round the dich.
A qualitative indication of denitrification was the permanent formation
of a acun layer around three quarters of the ditch length. Denitrification
also took place in the settling ta ik since the levels of nitrate nitrogen
measured in the returned effluent were consistently lower than those
recorded in the dttch. Figure 19 shows that reduction of ammonia N did
81
-------
not correspond to increase in oxidized N, as in Phase 1.
The peak in both NH 3 - N and oxidized N observcd in January, is most
probably from hydrolysis of organic N accuaslated in the ditch during the
prolonged rotor stoppage in December. Phosphate results were very inconsis-
tent. The difference between P0 4 3 contents of the influence and overflow
effluent cannot be calculated because PO4 levels were not measured for the
overflow. However at termination of recycling the total P0 4 level was in
excess of 1700 mg/l. Such a high level should have some potential as
fertilizer.
Total coliforms were reduced by 93.5% during passage through the ditch
(11th January to 1st March). This reductinn exceeds that found in Phase 1,
85.9 %, by a considerable margin. The improvement is a little surprising,
because the concentration of suspended solids ifl the returned effluent during
Phase 2 far surpassed that found in Phase 1. These total coliform counts
are ot rather dubious sanitary significance and in future both total and
fecal counts should be wade.
The rate of buildup of inorganic dissolved salts (Figure zo) has been
suggested as being hazardous to biological treatment (Smith and Jenkins (69) ).
In fact 1 this is unlikely to be the case for recyclig biological tnatment
systems where there is appreciable fresh water input from waterer spill
and washdown. Thc concentration increase rate of an inert material may be
analyzed mathematically if some reasonable assumptions are made. these
are: that the flow-thrcudh rate of excess water La specified, that the
rate of addition of the inert 4ubatance is specified and that the treatment
system is completely mixed. Using the diagram and symbols showy on Figure
22 an eouation relating concentration with time may be derived.
.2
-------
Cx
LB/GAL.
SETTLED EFFLUENT
9
CHLORIDE CONCENTRATION VS.TIME
a 1 I V
PLOTTED AS x
a
c
LEGEND
V VOLUME OF COMPLETE
-V
MIXED TANK
6 Q :FLOW RATE THROUGH
THE TANK
x RATE OF ADDITION
OF INERT SOLUTE
C CONCEMTRATION OF
6
SOLUTE IN TANK
EQUAT ION
4
C
LQj Q
3
CC 0 ATtO
2
0
I I I- I I I I
0 0-5 I
e t
Figure 22. Chloride ion concentration and time for the settled effluent
from an oxidation ditch fed raw manure; the resL.lts are for
Phase 2
83
-------
1x+cQ1 - t x
C _j, QJe + (3)
If t 0 at C C 0 and Q and V are both specified, the equation may
be plotted in the linear form of C vs. e . This has been done for
chloride ion concentration in Figure 22, using the time span from 11th
January to 15th February. This period was chosen because there was no
significant rainfall (Figure 2)) and the pig population was fairly constant.
The values used in coding the data were Q 773 gpd, V 47,000 gal and
C 2.25 x lb/gal (267 mg/i). The results show good linearity and
yield a rate of Cl addition of 6.25 lb/day. This value may be compared
with 11.5 lb/day of CI in the pig feed and 7.5 lb/day from fecal measure-
ments. If an arbitrary figure of 10 lb/day is chosen, then the ultimate
concentration as t is , or 1550 mg/i. Using Equation 3 it may also
be shown that it would take 140 days tn reach 907. of this value. This is
a low rate of increase, and Kincannon and Gaudy (36) could find no
inhibition of continuous heterogeneous cultures even when the C l. concentra-
tion was changed from 0 to 30,000 mg/i in 24 hrs. It is felt that this
analysis shows clearly why the expected trends in Cl increase were not
observed in Phase 1. The otai volume of the system (V) was about io6
gal, and this overshadowed the numerator of the exponent (Qt) in the
period available. Moreover rainfall and snowmelt over the large area of
the lagoon invalidate the assumption that Q wa constant. Thus, in most
biological treatment systems employing recycling, a combination of waterer
spill and washwater, with realistic treatment volumes will preclude salt
toxicity. An exception might be for poultry; but even in this c ae, the
84
-------
results of Smith and Jenkins (69) suggest that salt concentrBtionS can be
very high before inhibition occurs.
Power requirements:
The average power consumed by the rotor during this phase was 146
kwh/day. Further calculation shows the power requirement per unit of BOD 5
destroyed to be 0,705 kwh/lb BOD 5 . This value LB nearly one third that
derived ir Phase 1 but in Phase 2 aeration capacity was marginal. The
Water Pollution Control Federation (81) reports an average value of
0.446 kwh/lb BOD 5 for municipal plants employing surface aeration. A
direct comparison between municipal practice ard this study is not wise
because of the much greater MLSS level here present. The individual pig
power consumption amounted to 0.24 kwh/day per pig. Power consumption for
the pumps was 20.4 kwh/day.
Aerobic Sludge Digestion
Objectives:
At the end of Phase 2, the ditch contained a-fairly concentrated mass
cf unsettlable sludge. Javorski etal . (31) have report d that extended
aeration of activated sludge without further feeding can improve settling
characteristics. The concept of aerobic sludge digestion has been applied
to small municipal plants with some success (Ritter (6 e) ), since it can
achieve reasonable reductions in -volatile solids and also produce a stable,
easily-dried sludge.
The feed to the ditch wa closed and contents were allowed to digest
aerobically. Analyses were limited to o1Lds, COD in mixed liquor and
85
-------
centrate, Kjeldahl nitrogen in mixed liquor and centrate, chloride and
temperature. These analyses were cho8en 80 that some measure of the
volatile solids reduction could be obtained, and also 8ome measure of the
change in sludge composition with age in respect to VSS:COD:N ratios. The
chloride concentration was measured-so that an estimate could be made of
rainfall dilution during the experimental period. Settleability was
measured using the sludge ,olume index. One set of data points was
obtained each week for 10 wk, the test was ended prematurely by incipient
failure in a rotor countershaft bearing.
Analysic of results:
Spring 1971 was rather exceptional in Iowa, negligible rainfall
occurring during the experimental period. The temperature varied from 470
to 67°F, with a mean temperature of 56.3°F. The results from Phase 2 had
shown that the contribution of the ce trate to the total volatile solids,
COD or N was fairly small; hence attention was focused ou the reduction
of volatile matter, COD and N, in the suspended solids.
A graph of VSS vs. time is shown in Ligure 23. The graphs of COD
and N in the SS, ieing very similir, are not shown. All resuLts show a
jump between the 28th and 35th day. It is suspected that this jump may be
due o resuspension of materials from the floor of the ditch.
800 is often approximated by a first order curve
dL kL
(4)
and It seemed reason&.1e to examine the data from this aspect. The choice
of first order curves by sanitary engineers is widespread. Even if it
86
-------
vSS
AEROBIC SLUDGE DIGESTION
VOLAT L GU PEND D $0L108
0
0
0
0
loP R
I 7(I 1I)
Figure 23. Reduction in volatile suspended soHds during aerobic
sludge digestion. After Phase 2
87
-------
Lo 0 CVSS)
Figure 2 i.
Logarithmic plot of the reduction in volatile suspended
solids during .erobic sludge digestion. After Phase 2
88
AEROBIC SL JDGE DIGESTION
LO (VOLATILE 8USPEL oED SOLIDS)
4
0
0
0
0
0
0
U AY
70
.1
-------
has no easily derived theoretical Justification, it does have very real
practical value; since it allows experimental data to be codified for
design purposes. The model chosen is -
where
L Parameter remaining after time t
L Initial value of L at t 0
K Rate constant
t Time in days
This equation may be rewritten as
log 10 L -Kt + log 10 L 0 (6)
and this should yield a straight line if a graph of log 10 L vs. t is
plotted. The value of and K have been obtained using linear regression
(Ostlo (94) ). The graph of iog 0 (VSS) vs. t is shown in Figure 24. The
values obtained ignored the jump in parameters appearing after the 28th
day.
Table 10. and K at a mein temperature of 56.3°F
Parameter
L 0
mg/I
K
1
day
Volatile
suspended
solids
13,350
0.00556
0D in SS
20,700
0.00583
Kjeldahl
N in SS
1,390
0.00774
89
-------
Tables 10 and ii suggest that there is a alight change in sludge
composition as the test progreosed. The ratio of VSS:COD remained
approximately constant as borne out by the similarity of the two K rates.
However, the N content appears to decrease faster and shows an accordingly
higher K rate.
Table 11. Ratios of VSS:COD:N in the suspended solids. Aerobic digestion
Date
Day/Mo/Yr VSS :COD:N
8/3/71 1 1.57 0.0996
15/3/71 1 1.44 0.106
22/3/71 1 1.67 0.104
29/3/71 1 1.4 0.0943
5/4/71 1 1.59 0.0917
12/4/71 1 1.44 0.0784
19/4171 1 1.89 0.0821
26/4/71 1 1.34 0.0741
3/5/71 1 1.61 0.085
10/5/71 1 1.33 0.0802
17/5/1 1 1.52 0.0724
A finding of this study is that aerobic sludge digestion does help
settleabih.ty considerably. After 21 days, the. SVI was 72 and the MLSS
was still at 13, 800 mg/I (Table 12). It is surmised that the rather
mac ir. aeration capacity during Phase 2 may have caused the bacteria to
90
-------
store substrate as increased polysarcharides in the slime layer and this
layer prevented proper flocculation. The slime layer was digested by
endogenous respiration once the influent was shut off. The rise in SVI
noted in the last week of the test is not understood. The fraction of
the sludge whicn was vo1ati1 did not change appreciably through the test,
a similar finding to that of Randall and Koch (60).
Table 12. Suspended solids and SVI. Aerobic digestion
Date
Day/Mo/Yr
Total
mg/i
Volatile
mgf l
Fixed
mg/i
Percent
volatile
SVI
ml/g
8/3/71
17,410
14,360
3 .050
82.5
N ?
15/3171
15,360
12,530
2,830
8l.o
NS
22/3/71
13,760
11,080
2,680
80.5
72
29/3/71
11,820
9,410
2,410
79.6
MS
5/4/71
9,050
7,630
1,420
84.3
109
12/4/71
11,880
9,640
2,240
81.1
78
19/4/71
10,120
8,340
1,780
82.4
65
26/4/71
9,640
7,680
1,960
;9.7
51
3/5/71
7,320
5,690
1,630
77.7
74
10/5/71
7,330
5,720
1,610
78.0
72
17/5/71
7,740
5,970
1,770
77.1
114
= No settling.
9)
-------
Table 13 shows that toe decrea8e in su3pended solids COD was not
accompanied by an increase in centrate COD. This seems to suggest this
fraction of the COD was leaving as c0 2 instead of being converted to
biologically re.fractile liquor.
Table 13. COD in centrate and suspended solids. Aerobic digestion
Date
Day/Mo/yr
Centrate
COD
rn /l
SS
COD
mg/i
8/3/71
1,240
22,600
15/3/71
1,060
18,040
22/3/71
915
18,490
29/3/71
856
13,140
5/4/71
760
12,140
12/6/71
703
13,910
19/4/71
657
15,740
26/4/71
581
10,320
3/5/71
547
9,150
10/5/71
440
7,630
17/5/7:
406
9,090
In spite of the iong detention time, the ditch liquor was not stable
at the end of the test. A bottle of mixed liquor, held at room temperature
(750?) bhow d slucge riaing and gave o a strong odor upon standing for
24 hr. This was unexpected, as Jaworski ct al . (31) had indicated that a
92
-------
60 day sludge was quite stable ana did not putrefy on standing.
Application:
The data are not directly applicable since any process for animal
wastes Imist be Continuous. However, the beneficial reductions in VSS,
COD and N, combined with improved settleability, suggest that extended
aeration of the effluent from a first stage aeration process might
occasionally be useful. The process could use a floating aerator and
could be used for conditioning and storing excess sludge before Final
disposal by irrigation. The feasibility would hinge upon a livestock
producers Location 8irlce the process is expensive both in terms of the
initial capital outlay and power costs for operation. In general an
anaerobic lagoon for storage nd some treatment of excess water would
seem more practical.
Pigs Water Supply. Phase 2 Treatment System
Establishment of feeding trial:
All p .gs in Unit K have access to the manure and flushing w. ter in
the gutter at the end of the pens. An experiment was conducted to
determine how pigs would be affected if they were fed normally, but were
forced to use the flushing gutter as their only drinking source. A group
of six pens were established at the lower end of the flushing gutter and
these were equipped with self-feeders. Ten pigs of similar age were
placed in each pen on 9th December 1970 but the trial could not begin
until 5th January 1971 because recycling of effluent had been interrupted
by mechanical difficulties. The layout of the pens and how they were
93
-------
supplied with water is shown in Figure 25.*
GUTTER! - ___ T
____ ____ PLOW
16 17 18 19 20 21
C N C N G N
___________ II ___________ ii _____________________
N AL8O HAVE AGC E8 TO dOfl AL WATERE $
G U8T D I tC RO GUTY R
Figure 25. Sequence of pens along the gutter. Pigs water suppy
When the trial started the mean weight of the 60 pigs was 57.1 lb.
The trial was continued for 36 days. It was to have co. .tinued for a
longer period; but an outbreak of Transmis8able Gasto-enteratjs (TGE)
occurred at the station and it was reconm ended that the trLal cease,
since TGE, as it spread to Unit K, could confuse the results.
Statistical analysis of the results:
Three parameters were measured in the study: weight gain per pen
over the 36 day period, feed consumed per pen over the 36 day period and
feed conversion efficiency. Two statistical designs using analysis of
*There is no Figure 26.
91
-------
variance seemed possible, completely randomized design (CR) or randomized
complete block design (RCB). Randomized complete block design seemed more
reasonable because of the possible effects of pen position along the
gutter length.
The weight gained parameters were analyzed using RCB and the F
statistic was not found significant at 5 . Since the degrees of freedom
are very low for a RCB of two treatments and three blocks, a test of the
relative efficiency of an RCB analysis vs. a CR analysis was performed.
This relative efficiency (RE) is given by Ostle (54) as
(7)
(bt l)E
where
b Number of blocks
t Number of treatments
B Mean square, among blocks
E Experimental error mean square
In the case of the weight gained, RE 0.71 which indicates blocking doe&
not justify the loss of degrees of freedom entaJed. Reworking the A OV
as CR, an F 14 12.4 was obtjinecj, and this was significant .. t 5 but
not at 1.
The feed consumed w s treated in the same fashi n yielding a non-
aignific nt F (at 5 t) in either RCB or CR designs, although RE was
only 0.65. However the feed conversion ANOv as RCB produced an
F 12 21.2 wnich was significant at 5 , but not at 1%. In this case
R E 1.14 indicating that blocking was beneficial.
95
-------
Table 14. Weight gain, feed and feed conversion. Pigs water 5upply
Parameter
Treatment
Result
Standard
errora
Mean pig weight
Gb
78.9
Over test period lb
NC
85.4
--
Daily weight gain per pig
C
1.22
0.028
lb/day
N
1.57
0.028
Daily feed consumed per pig
G
3.69
0.297
lb/day
N
4.27
0.297
Feed conversion efficiency
C
3.04
0.049
lb/lb
N
2.73
0.049
aF ron randomized complete block ANOV.
b
Must drink from gutter.
CAl have access to normsi waterera.
Tabe 14 presents the mean parameters and their standard errors.
Outbreak of ICE, which ended tie drinkng water trial, eemed a useful
opportunity to check the passage of a known pathogen through the system.
Through the excellent cooperation of th 0 National Animal Disease
Laboratory, it proved possible to monitor the TGE virus. Table 15
IndI ates the results obtained.
96
-------
Table 15. Detection of TGE virus in system
Date
Day/Mo/Yr
Sample
Dilution 5
Temperature
16/2/71
Manure
1O
53
1612/71
Ditch
io
52.5
26/2/71
Manure
10
53
26/2/71
Ditch
lO
50.5
2413/71
Manure
1O 4
--
24(3/71
Ditchb
47
28/4/71
Manure
IO
2814/71
Ditchb
Not
present
60
2814/71
Lagoon
Not
present
dilution at which TCE detectable.
bDjtcj sealed off, lagoon being recycled.
Lambert 1 of the NADL ha indicated that animels may remain carriers
of the virus even after complete recovery; this) therefore, would seem
to explain the continued detection throug - into April. TCE is a very
resistant virus and remains viruent when kept cool and away from
sunlight. Thus it would appear that the treatment system does little to
control the virus until the temperature rises. At the time of the last
1 C. Lacsbcrt , Virological Investigation, National Animal Disease
Laboratory, Ames, Iowa. Private communication.
97
-------
sampling, the ditch was at 60°F. It would also appear that exposing some
portion of the ditch through a window might be considered. However,
Lanberts opinion is that rats and birds will spread the disease very
quickly once it has entered a swine production unit, thus ellialnation in
the treatment system alone might be pointless.
Irrigation Disposal 1968
Tile drainage flow quantities:
Irrigation was begun In June 1968 and continued until the following
November. The results discussed In this section were obtained from
18th June to 18th September. The irrigation eηuipment functioned well
during the study. There was no no .iceable corrosion or the pipe, fittings
or pump. A light salt deposit (later analyzed as Mg(NH )PO 14 ) appeared
on the sprinklers and the pipes, but it did not hamper operation. No
nuisance problems from odor or insect breeding were encountered. Even
when the lagoon odor was quite strong, this odor dissipated during
sprinkling. Little ponding was caused because of the low application rates
used. The cover crop was mowed periodically to encourage new growth, but
was noc removed. This residue, along with the organic material i the
applied effluent, created a thin organic mat on the soil surface and this
may h?ve been beneficial in lissipating the energy of th water from the
sprinklers. Because of drought conditions during part of the test period
the supplemental Irrgation caused much higher growth rates on the plots
than on adjacent untreated areas.
98
-------
There was no noticeable change In Infiltration rate so the initia
appflcation rate selected was satisfactory for the entire operation.
In prel iminary trials, a higher rate had been tried and found to lead
to excessive runoff and ponding. Though less than the recommended
Permissible rate for this soil and cover condition (30), the appfled
rate was near the maximu n possible since minor ponding was observed at
the end of an irrigation. Hcncc,ths experience indicates that applica-
tion rates relating to clear water irrigation should e reduced to 30 -
50% when the irrigation water contains appreciable organic matter. Main-
tenance of infiltration rate through the test period was attributed to
the periodic loading and recovery practiced.
99
-------
Table 16.
A- .icrage water quality concentrations from June 18-September 2O
1968. Samples coll.ected 12 hours after start of irrigation
Depth
COD
Total-N
C1
P
in.
mg/i.
mg/i.
mg/i.
mg/i. pH
Surface
1
512
333
110
72
2
510
334
7.8
3
499
335
4
532
340
3
1
246
164
120
2
225
152
103
8
7.3
- 3
246
140
110
14
7.3
4
199
158
115
12
7.6
7.5
6
1
269
124
118
14
2
209
154
105
7.3
3
173
182
117
7.5
4
175
196
115
9
7.3
7.4
12
1
142
137
112
2
156
103
108
4
7.2
3
202
129
115
7.3
4
126
137
117
7
7.7
7.3
30
1
-.
2
94
91
95
2
3
104
145
85
3
7.0
4
126
151
94
4
7.5
7.3
41,-Tile
1
17
65
75
2
30
52
80
7.3
3
20
54
76
7.2
4
32
72
7.2
1.
1.5-in,
Co
707.
avaiLable
moisture
at
6-12
in.
2.
3.0-in.
@
7O
available
moisture
at
6-12
in.
deep.
eep.
3.
1.5-in.
Co
957,
availabLe
moisture
at
6-12
in.
4.
3.0-in.
957.
available
moisture
at
6-12
in.
deep
100
-------
Effluent renovation:
Effluent renovation for all parameters is indicated in Table 16.
Removal of COD was judged excellent, with an average of 97% for all
treatments. Treatment 3, comprising frequent small applications, seemed
the most efficient for decreasing COD. The relation between depth and
remaining COD is sF own in Figure 27. Approximately one-half of the COD
was removed in the upper 3 in. of soil where biological activity Is
greatest, and physical filtration removed any particulate matter. The
COD continued to decrease as the solution percolated through the soil
profile.
Removal of N ranged from 79% to 83%, with an average of 80%. Again
there was little difference between treatments although Treatment 3 appears
slightly superior. The percentage removal of nitrogen was fairly constant
throughout the entire perioc. The relation between appUed N concentration
and tile drainage N is shown in Figure 28, possIble explanations for the
decline in applied N discussed in a later section. The applied N from
the anaerobic lagoon was about 90% NH 3 -N but that draining from the tile
at I 8 in. depth was essentially all In the form of oxidized N. The change
in total N concentration with depth is shown in Figure 29. Ta Ic 17
Presents the changes in form which occured during percolation. It is
postulated that nitr fication and denitrification took place as the
liquor moved down through the soil. The organic nitrogen applied was
filtered out near the soil surface as particulate matter. The oxidized
nitrogen in the applied liquor would percolate freely down into the soil
with the liquid but NH 3 N was adsorbed on clay particles near the surface
101
-------
TABLE 17. Fcrm and concentration of nitrogen In sampled soil solution
at various. depths for treatment 1i - 3.0 inches at 95 avail-
able moisture - s.immer 1968.
Sampled
Depth Total-N NH 3 -W NO 3 +NO -N Organic-N
inches mg/i mg/i mg/I mg/I
0-surface 3t40 285 38 17
6 198 21 174 3
30 135 12 123
48 -ti ie 60 1 59 - -
as NH ions. if this process of adsorption was the only factor affecting
the NH 3 -N, then the total N in the soil solution below about 6 In. would
have been less than 70 mg/I. A150, soil anal:ses should have indicated
a considerable acummulatlon of N in the surface inches, but none was found.
The slightly acidic soil (pH 6.5) made volatilization loss of NH 3 unlikely.
Some N was probably assimilated by the cover crop, but the most likely
fate of tne NH 3 -tl was nitrificatiori by nitrosomonaS to N0; followed by
oxidation to NO 3 by nitrobacter Such oxidation would occur when aerobic
conditions were restored during the rest period following an irrigation.
Lees and Quaste l (41) have observed that nitrification in soil does not
occur unless the NH ion is f 1 rst absorbed on soil par icies.
Initially the N concentration in the soil percolate samples was
less then 70 mg/I, bt.t af er one month of operation, the concentration
in the 6 in. deep sampleb was about 250 mg/i. This lag In higher 14
concentrations in the soil solution was attributed to the time needed to
increase the population of nitrify ng bacteria sufficiently to oxidize
the N supplied. Frederick and Broadbent (23) have indicated that
102
-------
E
0
C .)
c
- 0
0
4 J
3
0
(I)
0
C/)
Figure 27. COD
application of
during summ,er
-
Sampled
depth,
concentration in soil
anaerobic livestock
solution under
lagoon effluent
1
968
48
ol, 1 5
o2, 3 ,0
A3, 1 5
4, 3 0
Ifle at
in at
in 0 at
in, at
70%
70%
95%
95%
0
20&
A
6
4
12
_
30
inches
-------
T i TiiiT TTTEIiI
400
300
200
E
a
C
a)
0
L
- 4- I
100
Tile Outflow
I I I
20 40 60
Time, days
Figure 28. Nitrogen concentra
applied effluent and tile ou
80
tions
tf low
C
6
Applied Effluent
C
C
C
-J
100
in
1 014
-------
1
E
. 4 - ,
0
0
.IT
4 - ,
0
C,)
400
300-
200
100-
0
r31, 1 5
02, 3 0
3, 1 5
N
4, 3 0
B ---
in 0
in 0
in.
in.
at
at
at
at
70%
70;
95%
95%
1
I
H
I
1
)
I
;
1
.,
I
I
1
I
I
I
I
1
.
0
o,
,
036
I
I
12
I
30
-
1:
Sampled depth, inches
Figure
tion under
29.Total
nitrogen
application
of
concentration
anaerobic
effluent
during
summer
1968
48
in soil solu-
livestock
a goon
U
-------
nitrificatlon becomes very rapid when the population exceeds JO 5 per g
of soil and they indicate that lag periods may be expected until such a
population Is developed.
Much of the N In soil solution samples collected after an applica-
tion of lagoon effluent originated in earlier applications. This was
evidenced by the time lag for nitrificatlon and by the fc t that N
coftcentrations in 6 In. samples caused by precipitation were as high,
or higher, than those collected after application of lagoon effluent.
Samples from the application of effluent after precipitation contained
considerably less nitrogen because the percolating rainwater had leached
out .art or the NO stored in the upper inches of the soil.
The nitrogen reduction in the soil solution between the 6 in. depth
and the tile outlet was about 140 mg/I. The N in this area of tF e soil
profile was almost all in the oxidized form. Uptake by the cover crop
at This depth was unlikely, and soil analyses did not indicate an increase
in N content of the soil. Therefore this loss must be attributed to
deni trifjcat ion of NO 3 and NO 2 to N 2 0 and N 2 which could escape to the
atmosphere (Brcnrner and Shaw (Il) ). Inc nitrifying bacteria in the --
surface soil pr .duc J a good supply f oxidized N during the aerobic rest
period after irrigation. This oxidized N was leached d ,nwards by the
applied effli.ent until It encountered anaerobic conditions in the nedriy
saturated subsoil. Sufficient available carbon, as indicated by COD
in Fi guce 27, was present for denitrifjcatlon to proceed, until either
the s thstrate or the oxidized l was deoleted. A descending aerobic
106
-
-------
-
front di.iring a rest period would also Inhibit denitrification. Host
of the water in the effluent applied from one Irrigation remained in che
soil profile until more water was added on the surface. Under these
conditions, the percolation depth was estimated as being 3 ft, this Implied
that: the period for which the oxidized N and the available C were together
in the denitrifying region was at least 5 days. Bremner and Shaw (12)
have shown that, if the substrate is readily available, 5 days are quite
adequate for extensive denitrification. However, they do show that a
poorly available substrate may require up to 20 days for extensive denitri-
fication, thus explaining, in part perhaps,why appreciable COD and oxidized
N were always present in the drainage.
The only other likely factor in N reduction in the soil profile
would L e dilution by foreign crainage from adjacent areas. This was a
possibiHty since the drainage area for each tile was 9000 ft 2 and the
plot area was only 2400 ft 2 . Table 18 presents an estimate of flow
quantities and their relation to the nitrogen balance showing that 86%
of the N appi .ed could not be accounted for and was presumed lost by
denitrification. The cover crop yield was not determined, but a nitrogen
content of 2.5 was measured ir. three random samples.
All treatments proved .ery effective In removal of phosphates, each
removing 99z or more of the application. The reduction in P concentratIon
was 83 in the top 3 Tn. of soil, Figure 30. The decrea5e is attributed
to soil absorption. Removal continued as the solution percolated through
the profile but the rate decreased with increasing depth.
107
-------
Table 18. Estimation of nitrogen and chloride reduction by soil filtration
considering effects of excess tile drainage 1968-70.
Water, nitrogen, and chloride quantities 1968 19 .9 1970
Lagoon liquid, inches 30.5 48.o 31.5
Runoff, inches 3.0 2.5 0.5
Preciptarion, inches 12.5 31.0 32.0
RunoFf, inches 2.0 5.5 3.0
Total water into plots, inches 38.0 71.0 60.0
Estimated evapotranspiration, inches 18.5 33.0 27.0
Expected drainage, inches 19.5 38.0 33.0
heasured drainage, inches 17.5 56.0 46.0
Excess drainage, inches -2.0 +18.0 +13.0
Nitrogen in total drainage, lb/acre 285 1235 1540
Chloride in total drainage, lb/acre 310 1145 1360
Nitrogen in excess drainage, ib/acrea .... - 185 135
Chloride in excess drainage, Ib/acrea .... -- 220 160
Nitrogen in expected drainage, lb/acre ... - 285 1050 1405
Chloride in expected drainage, lb/acre ... 310 925 1200
Nitrogen into plots, lb/acre 2070 3140 2740
Chloride into plots, lb/acre 680 1300 1110
Nitrogen reductiork, 86 63 49
Chloride reduc tion. 54 29 8
aConcentrations irk excess drainage assumed to be the same as in 6 and 8-ft
wells in areas where no liquid w i applied, 46 mg/I nltrooen and 54 mg/I
chloride.
108
-------
E
I
60
(6
4 J
0
4
0
4-,
0
C l)
20
0
C)
Figure 30. Total
solution under
lagoon effluent
phosphorus
application
during summer
concentration
o anaerobic
1968
8
ol,
02,
4
1.5
3.0
1.5
3 0
0
0
in.
n.
in.
in.
at
at
at
at
70%
70%
95%
95%
Sampled depth, inches
a
in soil
livestock
-------
As can be seen from Table 18, the chloride concentration decreased
514% in the first year. Such a large removal was not entirely expected
since Cl is biologically inert, however, the next two seasons results
indicate that the fIrst years results represent equilibration with the
existing soil soluton.
irrigation Disposal 1969/70
Plot condition:
The soil in plots has continued to accept the lagoon liquid as
well as or better than during the first year. Equipment traffic on the
plots has been kept to a minimum. Some liquid movement on the plot
surface occurs because of distribution irregularities, but liquid usually
did not move outside the plot boundaries. The Irrigation intensity was
lower near the edges, and the liquid usuali Infiltrated. If ponding
occured in the low areas, infiltration was reduced or lost until those
areas dried.
One major problem in the plots was that the backfilIing i 1 the
tile trenches settled and cracks developed between the trench walls and
the fill material as the soil dried between applications. This allowed
shortcircuiting of any liquid irrig ted over these cracks. sInce
similar cracks also developed outside the plots, it was conclud?d that the
phenomenon was not related specifically to lagoon water. Yamazaki et al .
(87) have reported cracks in top soil and surface soil would benefit
drainage, but hey were not using the soil as a treatment system. No
major tillage had been done sInc th. tile Installation, and no repairs
110
-------
were attempted until all data collection was complete. Short circuiting
caused a marked Increase in COD. NH 3 -N and total P in the tile drainage.
The effective application rate In the immediate area of the tile trenches
was about 0.5 iph, which is higher than the recommended rate for application
of irrigation water on this type of soil, thus some runoff was expected.
Table i8 shows the treatment schedule for 1970/71 . The difference
in flow pattern from the tUe drains of a typical plot may be seen in
Figures 1 and 32; the results of 3 x 2/3 sn., application are seen 1r
Figure 31 and they show that the tile drainage concentrations of COD,
NH 3 -N and total P reach Increasingly higher peaks after each application.
Figure 32 shows the effect of a single 2 in. application and it is quite
apparent that the maximum transient concentration is much higher. Short
cil;uiting resulted as soon as the soil near the tile lines became
saturated and drainage ;tarted. The quality of this drainage w s poor
and remained so until the surface was no longer oversaturated. On a
concentration basis at peak flow, only about 60% of the COD, 80% of the
NH 3 -N and 75% of the total P were removed from the liquid applied. On
a mass basis, renovation seems much better because only about 20% of the
liquid volume applied drained during the first 10 hr after application
be-an. The regular but often system did not improve overall COD removal, -
but It did reduce the peak concentration in the drainage. Total P and
NH 3 -N removals were better. Seemingly, these nutrients are removed more
rapidly than Is COD when the liquid is in prolonged contact with the soil.
-------
±TL L -
-j
2
d160
0
0
-j
0
I ii
C)
z
Fig. 31. Tile drainage water qual
lagoon effluent; appi Iec
. - .
112
-j
0
4.-
a-
ji
0
0
Ity wIts 2.0 inches of anaerobic
in 3, 2/3inch applications.
BEGINNING APPLICATIQN,DAYS
APPLICATION RATE 0.12 IPH
COO, 775 MO/L
- AMMONIAN, 180 UG/L
. . - . . . . ... . ...TOTAL...P47N0/L
OR A INAGE
0
0 2 4 6 8
TIME AFTER
-------
60
a
a-
4 O ..j
0
I
20Z
z
0
APPLICATION, HR
of 2.0 Ii&ches
Tile drainage water quality with one application
anaerobic lagoon effluent.
I
I
I
1)3
I
300
200
APPLICATION RATE 0.40 IPH
COD, 72 MG/L
AMUONIA..#I22 uo/L
-TOTAL p, 41
DRAINAGE
- .3
I .,
*
0
C-)
x
-I
0
Li
0
z
a:
0
0
12
TIME AFTER BEGINNING
Fi :. 32.
24 36
-------
Effluent renovation:
In the 1970 field experiments, the mass removal of COD ranged from
79 - 93%. Better removal was obtained wIth 3 daily applications of 2/3 In.
than with a single 2 in. application. As more liquid was applied during
the season, removal of COD declined. Samples from the porous CUPS) which
were filtered by both the ceramic material and the soil, indicated re-
ductions in COD of 89% at 6 in., 95% removal at 12 in. and 97% removal
at 24 in. As in 1968, removal was most marked in the top few inches of
sol where. biological activity is greatest. Initial results from labora-
tory soR columns containing: sand, sand and soil in various proportions
and sand, soil and straw showed that 4 ft of coarse sand could remove
90% of the applied COD. Finer textured soils did not remove substantial 11
more COD when the application rate exceed 2 in/wk. Extrapolation of
these results to a real soil situation suggests that achieving an effluent
strength of 30 - 60 mg/i COD should be feasible.
Almost all the N reaching the tile drainage was in the form of
oxidized N. Exceptions caused by short circuiting, which ?assed appre-
ciable N}4 3 -N, have been mentioned earlier. The concentration of oxidized
N did not change markc dly over the season; the same was true for Cl
concentration, which was measured to follow water movement and as an
indicator of salt buildup in the treatment system.
The concentration of total N in the tile drainage water, Table 18,
from the various treatments does not show the whole picture of the N
removal by the soil system. Part of the decrease is attributed to
dlllution by foreign drainage from the buffer areas around the plots.
114
-------
The excess water in the tile drainage was assumed to have the same
concentration of total N and C I (46 and 54 mg/i, respectively) as the
6 & 8 ft wells in the buffer areas. As may be seen from the Cl removal
value for 1970 in Table 18, on a mass basis a point has been reached
where the biologically inert soluble salts, such as Cl, are no longer
being removed. A conditio . of dynamic equilibrium has been achieved.
At the same time, the total N continues to be decreased by nearly 50 .
Figure 33 shows the N concentration in the 1970 soil system for
Treatment 4 (2 in., one time at 350 mb). As in 1968, the N concentration
of the lagoon declined as the irrigation system progressed. Also, it
should be noted that the surface catch on the plot surface always
contal ed a lower concentration of total N because volati I ization was
enhanced by the sprinkling process. This finding is somewhat at variance
with that of Koch (38) who could not detect N loss from sprinkler water
using (NH )HP0 4 or NH 4 NO 3 + (NH 2 ) 2 C0 solutions in the pH range 5.5 to
8.5k however, he did find considerable losses using a solution of anhy-
drous NH 3 in water. urther loss of N taking place in the soil system
may hav t been caused by continued desorption of NH 3 N on the soil surface
before infiltration. The amount of total N in the surface catch was
used as a basis for calculating N removal oy the soil system. Finally, an
unk,.own amount of N was assimilated by the crop. -
The quantity of water that moved through the soil profile near the
porous cups is not known. When the peak in the concentration of total
N at the 6 in. depth occured, li .:le net downward movement of water was
occuring becaise evapotranspirat ion nearly equalled water addition. After
115
1
-------
-.
late July, the rest of the season was abnormally wet, and the N moved
downward with the excess water. The total N In the soil solution
decreased with depth, partly because of dilution. The quantity of water
that moved through the soil near the cups could not have been more than
the quantity of expected tile drainage from the plots in this treatment
(Table 18). Thus, the reduction in concentration was mainly a result of
cenitrificatjon.
Laboratory studies have shown that It makes little difference in
denitrification rates whether the soil is saturated with lagoon liquid,
or with water from precipitation, when the initial N0N content is
1*00 mg/I. About 10% of the N0-N added would .. e removed in 7 days. If
no soil was added to the lagoon liquid plus N0 3 -N solution, almost no
reduction took place, but if glucose were added at 1*00 mg/i as an energy
source then denjtrification began in 2 days. It emerged that 2000 mg
of glucose was required to reduce completely 400 mg of NO; in 7 days.
The amount of total P removed is a function of both the application
rate and the time in the soil. When the liquid flows through cracks,
total P removal is low. Each particular soil has a definite capability
for P removal, depending on its type, clay content and c..rganic matter
content. In the field experiment, removal ranged from 90 to 97 ; cracks
were responsible for the poor rates of removal that resulted during the
second and tiird seasons. In the laboratory sand columns 3 ft would ceuse
.1
a loss of 95%-of the total P for two months (equivalent to 900 lb/ac).
But as the saturation front progressed, the concentration In tha leachate
116
-------
12INCH CUP
24INCH CUP
6INCH CUP
O LAGOON
SURFACE CATCH
$FT WELLS
LE DRAINAGE
FIgure 33.
Concentration of total-N at various depths in the soil solution of
Treatment l97O-L on which anaerobic lagoon effluent was applied.
- - - . - . - . - . - - - - - -. -. - - - . -
60
IRRIGATION SEASON
0 -
-J
1
,
z
F-
0
F-
200
100
-o
MAY
I
UL
AUG
1970
OCT
-------
- . - - . - ----- -
increased until it was half that being applied at 1600 lb/ac equivalent.
Greate-r P reduction In the field would be expected because natural soils
have a much greater capacity for P adsorption than does sand.
The total P in the tile drainage can be expected to increase slowly
as more liquid is applied. The regions of greater permeability will
eventually become satirated, although the bulk of the field may be well
below saturation. Figure 34 shows the concentration of total P in the
soil solution at various depths in treatment 1970 - 4. Over three seasons,
1700 lb/ac of P had been applied. The concentration at the 6 and 12 in.
depths had more than doubled since the first season. The system would
still be capable of removing nearly all the total P from the applied
effluent if it were not for the cracks. Figure 35 shows the concentration
of total P in the tile drainage water caused by significant precipitation
after various amounts of lagoon liquid had be-n applied. The drainage
from precipitation did not produce a peak of total P as did the applica-
tions; thus, this drainaqe should be representative of the level of total
P that could be expected in the tile drainage water if cracks were absent.
There seems a definite correlation between the amount of total P applied
anc the concentration in the drainage water and, for the moment, a
linear relation seems most valid. Linear regression analysis (Ostle (54) )
gives
Expected total P, mg/I = (k) total P applied 1 lb/ac
This relation Is tentative and may be lacking other variables such as
yearly application rates and annual precipitation.
118
-------
$20 RRIGATIQN SEASON
I00
80 0
Oo
60 0 00
0
40 0
0
1970
Figure 31.. Concentrat on of total-P at various depths in the soil
of Treatment 1970-1. on which anaerobic lagoon effluent
SURFACE
12 INCH CUP
6INCH CUP
2 4INCH CUP
TILE DRAINAGE
solution
was applied.
(9
0
0
2 o
.0
I
cL
- r
H
0
I-
I0
MAY JUN JUL AUG SEP OCT
. ... .
-------
Y
1000
1500
TOTALP APPLIED, LB/ACRE
Figure 35.
Concentration of total-P in tile drainage water caused by Precip-
itation after various amounts of totalP had been applied In
araerobc lagoon effluent.
APPLIED
TOTALP 73 MG/L
2
p. .)
0
-J
CD
w
(9
z
a
Ui
F-
a-
jJ
0
F-
I C
x
0
Y 0.OQIIX+ 0.10
0 500
I .
x
2000
-------
:9
Desorption of Ammonia From the Anaerobic Lagoon
Annual variation of nitrogen concentration:
The rate of N influent to the lagoon is approximately constant
since the pig population Is 500 + 100 throughout the year. However,ear1j r
sections in this report have alluded to N losses from the lagoon other
than those accou ,ted for by 1 iquio abstraction. In the cold weather when
bilogcal activity is low and an Ice cover is present,N removal can only
be via precipitation or sedimentation, but during hot weather, loss of
ammonia by volatilization Is a distinct Possibility. This section will
discuss some of the theories of NH 3 adsorption and desorption and how
these have been correlated with the behavior of the lagoon. Figure 36
shows a typical yearsvariation in lagoon N concentration.
Nitrogen balance to estimate nitrogen lost L-y ammonia desorption:
No quantitative method was available to measure the amount of nitrogen
lost by desorption. Thus, a nitrogen balance of known quantities of
nitrogen added, removed, and accumulated In the iaooon had to be used, and
the unaccuuntable loss was assumed to be by ammonia desorption.
Table 19 shows this balance for the year. In late August, research
with the oxidation ditch began, and for the rest of the year, the lagoon
received only the overflow from the ditch. The only discharge from the
lagoon was either to a temporary holding pond or by irrigation on nearby
grassland, so the amount of nitrogen discharged in the excess liquid was
closely measured. Seepage losses are very small from this lagoon.
The accumulation of nitrogen within the lagoon is only an estimate.
A small fraction of the manure solids are relatively inert and contain
some nitrogen. This particular 7yearold lagoon has shown little solids
121
-------
700
600 Total-N
E 500-
I . . -- \ --.--...--
c
D 400 , NH +N -N \\
o
χ300 /
200- ;
8.0 _________
7.0
., 30 - -
4 N FEB MA A
1969 1970
Figure 36. Anaerobic manure lagoon nitrogen concentration, pli, and mean ar temperature during 19691970 at Ames, Iowa.
-------
Table 19. NItrogen balance on anaerobic manure lagoon at SwinQ tiutritlon Resear
Farm 1 Iowa State UnIversity, Ames, Iowa from 1 Nov. 1969 to 31 )ct. 1
IN
Feed: 1 Nov. 1969 to 20 Aug. 1970
650 hogs at 130 lb av weight
85,000 lb total weight at 0.048 lb N/day 100lb hog
40 lb/day x 293 days
21 Aug. to 31 Oct. 1970
Discharge from oxidation ditch
2,500 gal at 500 mg/I N
tO lb/day x 72 days _______
I Feb. 1970
Discharge to temporary holding pond
200,000 gal at 600 mg/i N
2 Apr. to I Nov. 1970
Re .earch irrigation
540,000 gal at 1485 mg/I N
15 May lS7O
FIc id irrigation disposal
200,000 gal at 500 rrg/i N
1 Oct. to 31 Oct. 1970
Fiei irrigation disposal
500,000 gal at 220 mg/i ________
ACCUI4IJLAT I ON
I Nov. 1969 to 31 Oct.. 1970
MgNH 4 PO, 4 6K 2 0 precipitation
0.27 lb/day N + 100 lb
I Nov. 1969 to 31 Oct. 1970
Net voIurr change
-200,000 gal at 220 mg/I N - 300 lb
Organic sludge accumulation o lb
Total ACCUMULATION, - 200 lb
UNACCOUNTABLE IN - OUT - ACCUMULATION
12,400 - 4,700 - (-200)
UNACCOUNTABLE 7,900 lb N
Note: lb x 0.454 kg; gal x 3.8 1.
OUT
11 ,700 lb
- 700 lb
Total IN, l2 ,IiOO lb
I .000 lb
2,000 lb
800 lb
900 lb
4,700 lb
Total OUT.,
123
-------
increase over the past 4 years, and no significant accumulation in solids
was Hkely. A crystalline precipitate of magnesium ammonium phosphate
(M9NH 4 PO 4 6H 2 0) has been found In this lagoon. The amount of nitrogen in
this form depends on the amount of magnesium added. In this lagoon, the
loss of nitrogen is believed to be less than 1 percent of the amount
added. Other precipitat ion may be occurring along with other processes
that result in r.itroyen accumulation, but the amount removed is probably
small.
The 7,900 lb (3,600 kg) of unaccountable nitrogen lost is attributed
to ammonia desorption and amounts to 64 percent of the added itrogen.
Ammonia des. rption equilibrium conditions:
In aqueous solution, ammoniu, dissociates according to ec t,ation 8,
HO
NH 4 2 NH 3 + H 4 (8)
Water enters the reaction, also. At equilibrium,
[ oHil K (9
E H31E2 b
and
K (10)
[ H2o] w
which yield
[ NH 3 N]= L*J (ii)
124
-------
Equation Ii is more easily solved by expressing Kb, K , and H as
pKb, pK, and pH, respectively. Eqe3tion ii then becomes
lO(pKb+ pH - I1 +_NJ 02)
The exact concentration of ammonia-N in solution cannot be measured
directly; however, Equation 12 makes prediction routine if the ammonium +
ammonta-N concentration, liquil temperature, and pH are known. Equation
12 is solved simultaneously with Equation 13 and the percent ammonia-N
[ N11 3 _NJ + [ NH _N] [ NH, 4 + + NH 3 - (13)
In solution at the specified conditions is obtained.
During the year, the temperature of a lagoon surface in Iowa ranges
from 0 to 35°C; over this range, pkb and pK change considerable (actual
values are readily available in chemistry handbooks). Values of pH
from 6.5 tc 8.5 might also be expected. Figure 37 shows the percentage
ammonia-N in solution over these ranges of temperature and pH. The per-
centage NK 3 N approximately doubles with either a 10°C rise in temperature
or 0.3 rise in pH.
Desorptiori of ammonia-N:
Volatile components, such as ammonia in aqueous solution, exhibit a
vapor pressure because the compcinen seek to establish equal pressure be-
tween the two phases (gas-liquid system). With a lagoon open to the at-
mosphere, eqiillbrium usually is never reached. The pressure difference
between the ammonia-N in the liquid and the air represents the potential
or driving force for desorptlon. This potential is analagous to a temper-
ature difference that causes heat flow.
To evaluate the prd:ssure difference, the partial pressure of ammonia-N
In solution must be acc.urateiy known. A derivation by Kowalke etal. (4o)
125
I
-------
1)
C.)
C-.
cDO
0 - .
0
0.
0
pH
Figure 37. Percentage of NI1 + NH -N in solution that Is NH 3 -N at
equilibrium at various xpected conditions in an
anaerobic manure lagoon.
126
--
0
6.5 7.0 7.5 8.0 8.5
- -
-------
at standard conditions and 25°C, yields a working relationship,
in !_. . .4L 4 2 5 + 10.82 (l It)
where
a partal pressure of ammonia-N In liquid, in atm
m = molality of ammonia-N In liquid, in moles/i
T a temperature,
This derivation assumes that Henrys law holds over the range In which the
equation is used and that the heat of solution of amfl onia is independent
of temperature, art assumption justified over only a small temperature range.
(ammonia-N pressure in the liquid) is readily calculated from
Equation iItby substituting
( NH 3 -N )(NH 4 + NH 3 -N, mqII )
(15)
Ioot(l4ooo
and solvinq for P 1 . Figure3 8 shows L during the season as calculated from
Equation it..
The partial pressure, P. in the air above the lagoon can be found
by measuring the ammonia-N in air samples around the lagoon. The air around
the lagoon in this study wiis sampled frequently during 1970. A measured
volume of air is. bubbled through distillel water. The absorbed ammonia-N is
measured by Nesslerlzation. P 9 is then calculated as
(NH -N)(29)(SVA)
3 (16)
9 (AVJ (14) (454000)
where
P a partial pressure of ammonia-N in air, in atm
NH 3 -N a weijht of absorbed ammonia-H, in mg
SVA specific volume of air at times of test, in cu ft/lb
AV a volume of air sampled, in cu ft
127
-------
10-
9-
8-
7.
(0
0
x
E
5.
S
04.
3-
2-
1-
°MAR APR MAY 1 JUN JUL AUG SEPOCT NOV
1970
Figure 38. The calculated vapor pressure, P 1 , of ar inonia-N in an anaerobic manure lagoon and
the measured vapor pressurη, P , o ammonia-N In air directly around the lagoon
d -D
urlng 1970 (Note: I x JO atm 0.55 pg/I Ni, 3 N).
P
00
0
00
0 %
0
00
0
0
-------
29 weight of air per mole, In g/mole
14 u weight of ammonia-N gas per mole, In c/mole
454,000 mg per pound, In mg/lb
The lower curve on Fi ure3 8 is the line of best fit through the points
plotted on the graph. These points are the average Pg of the air sampled
directly around the lagoon. The sampling locations are 11 - 15 on Figure 39.
There is considerable scatter in the data; the different climatic conditions
may well be responsible. No consistent pattern was established. Pg was
usually higher when the wind velocity was very low. At sampling points 9
and 10, the P 9 1 s usually were less than half the average Pg verb near the
lagoon.
Masstransfe Considerations:
The familiar mass-transfer relation Is assumed to apply for the
desorption process,
d(NK 3 N )
dt AK(P 1 - P 9 ) (17)
where
I*1 3 -N = weight of ammonia-N transferred, in lb
= time, in days
A = area of liquid-gas interface, in sq ft
K over-all transfer coefficient, in lb/day-sq ft-atm
partial pressure of anvnonia-N in liquid, in atm
P 9 partial pressure of ammonia-N in air, in atm.
All the parameters in EquatIon l6excePt K, the over-all transfer coefficient,
can be evaluated from collected data and previous equations.
The mass transfer In this case Is analogous to heat transfer from
liquid to gases. There arc two films that offer resistance to transfer of
amonla-N just as there are two films that offer resistance to heat flow.
129
-------
200
20011
SHALL.0W CELL I 106
DEEP CELL
- - 275k 7O-
1r sampling locetion
Figure 39. Air sampflng location around the anaerobic manure lagoon
at Swine Nutrition Research Farm
130
- .
-------
In absorption, the overall transfer coefficient Es the sum of transfer
coefficients of the separate films. In series, the resistances are
additive and equal to the reciprocal of the overall transfer coefficie 1 t:
1 1 1
(18)
where
K transfer for air film
K 1 transfer for liquid film.
A classical experiment to measure the absorption of amonla into
water was done by Halsamctai. (26). Water flowed down the walls of
a column, and an ammonia-air mixture was blown up through the tower.
The experiment was done at different gas velocities and temperatures.
Figure 40 rep:eSents these data.
Figure 40. Ammonia transfer coefficient versus gas velocty for ammonia
absorption into watAr from Haisam et al.
200- ____________________
150
100
50 -
0_ - -
0.0
E
4 -a
4-.
7
I
a.
0
Is
0.
1 I
0.? 0.4 0.6 0.8 1.0
CA VELOCITY, fps
.4
30 °C
20
10 °C
1.2
131
-------
-- - --;- --
For ammonia, the gas film fully controlled the value of K K (In
this paper) for low velocities. Further work by the same authors on the
effect of gas velocity and temperature was done With these data. The
equation for K was found to be
K = 2.6 x 10 V 1 day-sq ft-atm (19)
where
V gas velocity, in ft/sec
T temperature, in °K.
Other work by Whitman and Davis (83) found K 67 at 20°C for an
ammonia-air mixture passing over a freewater surface with the water stir-
red at a constant rate. Absorption was Controlled by resistance of the
gas film. Kowalke etal. (140) found K 1.6 for an ammonia-air mixture
being absorbed from quiet air at 25°C.
Equation 19 will hold for desorption if the same conditions that
control absorption are met. These cOnditions are that the liquid film
has the same P 1 as the bulk liquid and that all the pressure drop P 9 )
occurs across.the air film, if only the diffusion of ammoniaN through
the bulk liquid is considered, it would be difficult to maintain the
liquid film at or near equi1 rium. But diffusion is not the only process,
the liquid film probably is replenished mainly by ionization of amnmonium
to ammonia according to Equation 8. The diffusion of ammonium need only
be about 1/60 to 1/100 as great as diffusion of ammonia to the liquid
film. The pH may be slightly lowered at the film because of ionization.
The acceptance of K for absorption being nearly the same for desorption
from a lagoon seems plausible.
132
-------
- -.-- ., .-- .--
- .-ar.- ?V
Evaluation of K:
To determine if K can be predicted from Equation 19 by using surface
conditions of mean air temperature and average wind velocity, the data
from 16 March to 3 Oct. 1970 were divided into half-month increments,
and K was evaluated for each increment. For the same increments, K was
also calculated by using mass-transfer data for the lagoon in EquatIon 17.
For the mass-transfer evaluation, one estlmat had to be made of the
amount of nitrogen in undigested and settleable solids that were stored
during cold conditions and released during the warm s ason. The amount
Stored and released was about 600 lb. These esimates are in column B
of Table 20. The amount of change in nitrogen in solution in column A
takes Into account the change in concentration and the change in Volume
over each increment because of rainfall, irrigation withdrawal, evaporation,
and additic ., from waste flow. The feed rate, column C, was constant up
to late August when the oxidation ditch treatment system was put Into oper-
ation. From then on, the lagoon received only the overflow from the ditch.
The nitrogen lost in column D is the unaccounted for difference between
inputs and withdrawal. This los is considered to be the amount that was
desorbed over the increment. To complete the list of needed variables in
Equation 17, (P 1 - P) was picked from Figure 38 for each Increment.
The surface area of the lagoon averaged about 29,000 sq ft.
K from masstransfer considerations in co lumr E are the final results
of the mass-transfer calculations. During periods of low temperature,
(P 1 - P) is very small or negaUve, s K has no meaning. At low tempera-
tures either other processes are Involved, or some of the underlying
equations break down.
133
-------
a
b
Ό
first two digits represent the month and the last digit conifies
assumes the partial pressure of aru,onia-N above the lagoon is C.
first or second half of the month.
- Tal le 20. Pred c c o the over-all masstransfer coefficient of a ior.ia-U, K, frrim masstransfer cons iderations and
Dre%ailinη at the surface of an anaerobic manure lagoon during 1970.
A
I I
1
1
- -= ___, - - - -
- ._ . .-
.
._.
.
B
C
0
t
F
C
H
N added or
N stored in
N lost
K from mass
Time
lost fror
or released
by apparent
transfer
Ave. mean
Ave. wind
K from surface
increrienta
1970
solutor,
!bloav
from settled
soiids,lb/day
N in manure
fed, lb/day
desorpt k m,,
lb/day
cons derat ions
lb/day-sq ft-atm
air temp,
0 C
velocity
fps
conditIons,
lb/day-sq ft-atm
032
+
+6
40
32
neg
I8 o
1
9.5
620
0111
+2
+5
40
33
neg
l065
7
9.5
588
042
+
110
39
2635
752k
13
8.9
5117
051
- -15
-4
40
29
933
17
8.8
530
057
+8
-10
40
42
7211
20
7.8
473
061
+5
-10
40
115
1131
21
7.5
1 157
062
0
-7
.0
47
290
21
7.2
442
071
-10
-4
110
54
252
23
4,8
320
072
-15
-3
43
58
271
24
5.1
333
081
-17
-1
hO
58
327
22
3.5
249
082
-14
0
20
34
279
21
3.8
267
091
-6
0
10
16
187
18
6.6
419
092
-8
0
8
16
394
16
4.5
3111
101
-L i
0
8
12
690
295 b
13
7.9
498
102
-Li
+2
8
10
3450
492 b
9
5.4
3711
-------
No data were taken on the lagoon for temperature and wind velocity
that could be used in Equation 19 for K from prevailing surface conditions.
So, data from the recording station Ames 8wsw (78) were used. The lagoon Is
6 miles east of the station. The mean air temperature for each increment
was assumed to be the temperature at the liquid-air interface In column .
The wind velocity at the station is measured approximately 4 ft above the
ground surface so that should be representative of the velocity at the
lagoon surface in column C.
K from prevailing surface conditions in column H are the flral results
of the calculations from Equation 19. This use of Equation 19 may be open
to question because the velocities used to determine it were from 0.2 to
1.4 fps, while it has been extrapolated In this case to velocities as high
as 9.5 fps. But from period 52 through 92, the two Ks compare quite well.
The average K from mass-transfer considerations 15 355 and average K for
prevailing surface conditions is 364. Much of the desorption occurs during
this period. So, the amount of desorption from this lagoon can be estimated
if the ammonium + ammonia-N, pH and surface area of the lagoon are known
along wth the climatological data for the area.
Laboratory study:
Ano her phase of this work involved desorption under controlled con-
ditions in the laboratory. Several 500-mi 5amples of lagoon liquid taken
In late November were placed in Iliter flasks. Air wa drawn Into the
f 1.sk through a glass tube located from 0.5 to 2.0 in. above the surface
of the liquid. The air leaving the flask was bubbled through weak boric
acid to catch the ammonia-N. The nitrogen corIc ntration in the lagoon
liquid and boric acid solution were measured periodically by Nesslerization
135
-------
of a small sample. The recoveries in the boric acid were from 95 to 105
percent of the measured amounts desorbed from the lagoon liquid. The desorp
tion from four of these runs are shown in Figure 41, along with temperature,
pH, and the resultant P 1 for Run No. 4.
The desorption process was nearly linear over time. This was caused
by a rise in pH over time that cannot be explained. Such a rise likely would
not occur in the lagoon. For Run No. 4, the P averaged 11.5 x atm
and L averaged 12.2 x 106 atm over the run. This resulted in K from mass
transfer considerations of 122. K from prevail ing surface was not measurable.
These data support the previous findings that nitrogen does escape from the
lagoon liquid by ammonia desorption.
Implications of ammonia desorptlon:
The loss of about twothirds of the nitrogen to the air by desorption is
important in several respects:
First, the anaerobic lagnon is a major source of nitrogen For the
nearby environment. Enough escaped during 1 year from this lagoon to ade-
quately fertilize 60 acres of corn with nitrogen. The desorption is similar
to overfertilizat.ion of nearby 1a.es with nitrogen from catle feedlots. i
concentration of ammonia In the air is of little conseq .Jence unless a lake
is nearby.
Second, there is now a major co s tituentof the gases from this lagoon
that can easily be measured. Possible, ammonia concentrations in air can --
be correlated to odor levels in a quant ltative evaluation.
Third, and probably the most Important result of this reduction of
nitrogen in the lagoon liquid, iS the reduction of land needed for 1-rtlg.a
tion disposal of the excess lagoon liquid. A reasonable criterion for how
136
-------
+
χ
(0
0
E
0
C-)
0
E
0)
I
1
8
8
7
Time,hr
Figure 41. Desorption of amrrv;nia-N from anaerobic manure lagoon liquid I
laboratory by drawing air over the liquid surface and catching
desorbed ai vnonia-N In boric acid.
137
20
I
,1
a
I;
-------
much liquid to apply per year appears to be an anount contairing up to
600 lb of nitrogen per acre. The ammonia desorptlon rate not only dictates
h w much land will be needed, but also gives tie best time of the yea- for
disposal. If disposal can be delayed untl Aug. to Oct., only about two-thirds
as much land would be needed as compared with uniform disposal from May to
Oct. DurIng application of the lagoon liquid with sprinkler irrigation
equipment, more nitrogen is lost by desorption, from 15 to 30 percent of the
nitrogen pumped from the lagoon lost by the time the liquid reached the soil
surface.
138
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- -4 ,---..----
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AC KHOWLEDGMENTS
This project was conducted as part of the overall animal waste
management program at Iowa State University. Without the support given
related projects the success achieved in this work would not have been
possible. Particularly helpful has been support provided by the Iowa
Agriculture and Home Economics Experiment Station, Iowa State Engineering
Research Institute, Iowa State Water Resources Research Institute and
the Environmental Protection Agency.
The development of the waste management system, system operation,
data collection and report preparation were a part of the graduate
training program of Richard J. Smith. His sustained devotion to the pro-
ject and diligent work are gratefully ackno i!edged. T e associated
effluent disposal project, reported here in part, was the work of James
K. Koellik r. Other students who measurably contributed are Richard
Larson, Dennis Jones, Howard Person, and Richard Keith. The project was
directed by Agricultural Engineering Department faculty members : Drs.
J. Ronald Miner and Thamon E. Hazen. Other Agricultural Engineering
staff members with major nput were Arthur R. Mann and Dr. Duane W .
Mangold.
The cooperation and helpful assistance of Dr. Vaughn C. Spear,
Professor of Anmal Science, and the per nnel at the Swine Nut.ltion
Station In maintainIng the animals, assisting with animal performance
trials, arid the many other duties associated with operating a production
size research unit are gratefully acknowledged. Particular thanks are
due to Rex Meyer and Don Baker. The bacteriological and virology work
139
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reported we e possj ie due to the close cooperation of Dr. William P.
Switzer, Professor, Veterinary Medicine Research Institute. The data
reporting the detection and isolation of ICE virus were obtained through
the efforts of Dr. C. Lambert, Vlrological Investigator, National
Animal Disease Laboratory, Ames, Iowa.
The support of the project by dureau of Solid Waste Management,
U.S. Public Health Service, and the help provided by Louis W. Lefke,
Chief, Research and Training Grants Section, and by Alvin C. Keene,
Staff Engineer, is acknowledged with sincere thanks.
140
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147
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-r - -. . -. _ -- ..- - -r - fl t-,r r
LIST OF PUBLICATIONS
This project:
I. Smith, R. J., T. E. Hazen and J R. Miner, Piggery cleaning using
renovated wastes. Proceedings of Symposuum: Farm Wastes,
University of Newcastle upon Tyne, pp. 101-109. January 7-8, 1970
2. Smith, R. J., Manure management In a 700 head swine finishing
building: two approaches using renovated waste water, Presented
at International Symposium on Livestock Wastes, Columbus, Ohio
(1971) (ASAE publication) (In oress).
3. Smith, R. J., and 1. E. Hazen, The amelioration of odour and
social behavior in, together with the pollution reduction from
a hog-house with recycled wastes. Presented at the 1967 Sumer
Meeting, American Society of Agricultural Engineers, Saskatoon,
Saskatchewan, Canada. June (1967).
4. Miner, J. R., E. R. Baumann, 1. L. Willrich and T. E. Hazen,
Pollution and confinement production of animals, Journal Water
Pollution Control Federation, 42, No. 3, pp. 391-398. (1970).
5. Smith, P. J., Manure transport in a Piggery using the aerobically
stabili7ed dilute manure, Unpub)ithed M.S. thesis. Ames, Iowa,
Library, Iowa State Universtly, 99 pp. (1967).
6. S nith, P. J., A prototype system to renovate and recycle swine
wastes hydraulically, Ph.D. thesis, Department of Agricultural
Engineering, Iowa State University, Ames, Iowa, 176 pp. (1971).
7. Koelliker, J. K. and J. R. Miner, Desorption of ammonia from
anaerobic lagoons. Presented at Mid-Central Meeting of the
American Society of Agricultural Engineers, St. Joseph, Missouri
(April 1971) (In press).
8. WilIrici -,, T. L. .nd J. K. Koelliktr. Fluid disposal systems for
animal wastes. Proceedings of the Vth International Zootecnny
Symposium, Milan, Italy. (1970).
9. Koelliker, J. K. and J. R. Miner. Reduction of nitrogen concen-
trations in swine lagoon effluent by biological denitrificatio,-,.
Purdue University Engineering Extension Series. (1970) (In press).
148
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Related Projects:
1. Miner, J. R. and T. E. Hazen. An alternative to oxidation ditches
under slotted floors, Proceedings Tenth National Pork Industry
Conference (1967). -
2. Merkel, J. R., T. E. Hazen and J. R. Miner. Identification of
gases In a confinement swine building atmosphere, Transactions
ASAE 12:3, 10. (1969).
3. Miner, J. R., 1967 Literature review, agricultural (livestock)
wastes, Journal Water Pollution Control Federation, 40:6,
1150-58. (1968).
4. Miner, J. R. and T. E. Hazen. Ammonia and amines: components of
the swine building atmosphere. Transactions ASAE 12:6, 772
774, (l96 ).
5. Miner, J. R. Annual review of literature: agricultural (livestock)
wastes. Journal Water Pollution Control Federation, 41:6, 1169.
(1969).
6. Frus, J. D., T. E. Hazen ane J. R. Miner. Chemical Oxygen demand
as a numerical measure of odor level. Presented December 1969,
American Society of Agricultural Engineers, Paper No. 69-929.
7. Miner, 3. R. The universities role in feedlot pollution control.
Proceedings of Animal Waste Management Conference, Federal Water
Pollution Control Administration, Kansas City, Missouri. (1969).
8. Hazen, T. E. and J. R. Miner. Waste-Environment complex in
confinement production of swine. Seventh International Congress
of Agricultural Engineering, Baden Baden, Germany. (1969).
9. Willrich, 1. 1. and J. R. Miner. Anaerobic lagooning of swine
wastes, Seventh International Congress of Agricultural Engineering,
Baden Baden, Germany. (1969).
10. MIner, J. R. Raising livestock in the urban fringe. Agricultural
Engineering, 51:12, 702, (19/0).
I I. Koelliker, J. K. and J. R. Miner, Use of soil to treat anaerobic
lagoon effluent: renovation as a function of depth and application
rate. Transactions ASAE 13:4, 496. (1970).
12. Miner, J. R. Annual review of literature: agricultural (livestock)
wastes. Journal Water Pollution Control Federation, 43:6, 1171. (1970).
13. Min r, 3. Ronald. Editor, Farm animal waste management. (North Central
Regional Research Publication 206) Iowa Agr. Exp. Sta. Spec. Rep.
67. (1971). - -
149
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14. Willrich, T. L. and J. R. Miner. Experiences of five !ivestock
and poultry producers facing nuisance or damage litigation.
Proceedings international Symposium on Livestock Wastes. (1971).
(In press).
15. Harting, L. D., E. C. Hammond and J. R. Miner. Identification of
carbonyl compounds in a swine building atmosphere. Proceedings
International Symposium on Livestock Wastes. (1971). (in press).
16. Miner, J. R., J. D. Dodd ar.d J. II. Wooten. Water hyacinths to
further treat anaerobic lagoon effluent. Proceedings International
Symposium on Livestock Wastes. (1971). (In press).
17. Koelliker, J. K., J. R. Miner, C. E. Beer and T. E. Hazer,. Treat-
ment of livestock lagoon effluent by soil filtration. Proceedngs
International Sympocium on Livestock Wastes, (197;). (In press).
18. Miner, J. R. A nua) review of literature: agricultural (livestock)
wastes. Journal Water Pollution Control Fe . . ration, 44:6, pp.
991-998. (1971).
19. Koelliker, J. K., Soil percolation as a renovation means for live-
stock waste lagoon effluent. Unpublished M.S. thesis, Iowa State
University, Ames. (1969).
20. Vanderhr ,lm, D. H., and C. E. Beer. Use of soil to treat anaerobic
lagoon effluent: design and operation of a field disposal system.
Iran. Ames Society Agricultural Engineers, 13:5, 562-564. (1970).
21. Vanderholm, 0. H., Field treatment and disposal of livestock :
lagoon effluent by soil percolation. Unpublished u.S. thesis,
Department of Agricultural Engineering, Iowa State University, Ames
(1969).
150
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APPENDIX A. CHEMiCAl. ANALYSES DIFFERING FROM
STANDARD METHODS
Eiochemical Oxy&en Demand
The non-nitr fying BOD test us ng N-Serve 3 (2 - chloro - 6 -
(trichioromethyl) pyridLne) has een outluied by Yout g (83). In this
reference II) mg/ ]. of N-Serve is recommended in the diLution vater however
since the chemical is only soluble to 40 mg/i at 6?? a saturated
solution was substituted. Di.lutjons of this saturated solution were
tr .ed but the saturated solution did not appear to inhibit the carbonaceous
demand. It is admitted that these tests were not very comprehensive , hut
Young (88) indicates that N-Serve concentrat .on is not cr tical because of
its low slubil ty.
Solids
Solids deteran.nation by Stand. .rd Methods (1k) were not satisfactory
because the excesa of fine material, in st samples plugged any filter
before a reasonable volume could be passed through. The technique
developed was to measure total Holidb conventionally and alan to measure
sol da on the filtered (8 , membrane) supernatant from a swinging arm
centrifuge. The difference b-tween the two was regarded as suspended
solids.. The method was subject to some errors. The centrifuge tubes had
no caps and hence some evaporation way have taken place during centrifuga-
tion, also, the centrate was never wholly clear. An angle head centrifuge
3 Registered trademark of the Dow Chemical Company.
151
a -_ -
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of greater g racirg would e an improvement.
Kjeldahl Nitrogen
Thi3 parameter was determined by the Standard Methods (Li) technique
until part way throu Phase 2. The eccepeed method works well but seems
prone to froth very vigorously when adding concentrated NaOU prior to
distillation a.;d occasionally the frothing would be sufficient to
contaminate the boric acid trap. Alternatives to the mercuric ion used as
a catal ,st are selenium and copper. Copper selenite was available in the
laboratory and about 0.2 g/l0 ml conc. H ..S0 4 was tried in place of mercuric
sulphate. Raising the pH after digestion proved a much more docile process
and no quantitative differences in r.itrogen recovery were obvious. Since
concluding the laboratory work, the use of Se and Cu as catalysts has been
better documented. Streuli and Avercil (7 1 i) discuss the use of Hg, Se and
Cu and the; conclude that Hg is the most effective catalyst since it
catalyzed the c igestion of heterocyclic compounds but Sc and Cu used in
the correct proportion are more convenient for many substances. Future
laboratory work s needed to det rin ne the efficiency of Se or Cu vs. Hg
with respect to the liquors en ountered in animal waste treatment.
Nitrate Nitrogen
Nitrate nitrogen was reduced to nitrite by cadmium and measured
spectrophotometrically. The method used encapsulated commercial reagents. 4
A standard nitrate solution was used periodically to check the accuracy.
6 Hach Chcu ical Company.
152
V
a... . a. a .._ .L.J a
-------
No reference to this admium reduction method has been found in the
familiar literature.
Chlorides
Chlorides were measured using the mercuric nitrdtc/diphenyjcIrbazofle
method, when this test was first tried in preliminary work very indistinct
endpoints were obtained. Knowing that mineral supplements are fed in the
form of sulfates it was thought that some might be reduced to sulfite, and
Standard Methods (4) lists thj as an interference. To overcome such
interference the samples were digested on a reflux rack for 30 mm. The
reagents add-d to 50 ml of sample were 50 rag Ba(N0 3 ) 2 and 0.2 ml fuming
11N0 3 . Although this technique improved precision markedly, it has since
been found redundant when the sample is first centrifuged to r ove
organic particles. -
Phosphate
The method used was a commercially available modification of the
ascorbic acid method of Murphy and Riley ( 8). The types of phosphate
measured were ortho, soluble but able to be hydrolyzed by acid, and total
phobphate. The P0 3 is measured &pectrophotometrica] ly and may range from
0 - 3 rag/i. Because the phosphate levels uncountered w re often greater
than 500 mg/i rather extreme dilutjo had to be made. The reagent for the
acid hydrolyzed phosphate is a measured amount of a powdered acid and the
sample is boiled in a water bath for 30 rain. Total organic P0 4 3 is
determined by using a measured amount of acid and pet-sulfate and ref luxing
153
-------
the sample for 30 mm. After cooling the sample pH is adjusted. The final
step in both procedures is the determination of the hydrolyzed P0 4 3 . Even
when taking great care with the initial sample dUutions, considerable
difficulty was encountered with the total phosphate. The determtnation
would quite often be less tnan the orthophosphate value on the same
sample. Standard Methods (14) did not give any clue. Although tannin,
lignin and silicates are said to interfere, these were not thought to be
present in appreciable quantitieb after the 1:500 or 1:1000 sample dilution.
Finally better total organic results were obtained by taking:
2 gin K 2 S 2 0 8
5 ing conc. H 2 S0 4
5 ml raw sample
18 ml H 2 0
This mixture was refluxed for 30 mm on a boiling rack. After cooling
the mixture would be diluted to 1:500 or 1:1000. Tnis further dilution
was extreme enough to obv3.ate the need for neutralization. Finally the
phosphate was meai ured using the spectrophotometric method.
154
-------
APPENDiX B RAW RESULTS PHASE 1
Table Bl. Nitrogen forms 1 mar*ure slurry
155
Date
Day/Mo/Yr
Kjcldahl
mg/i
Ammor ia
mg/I
Organic
mg/I
Nitrate
mg/i
3/2/69
11480
630
850
0
10/2169
1590
505
1,085
0
17/2/69
1,300
420
880
0
24/2/69
--
--
--
--
313/69
1,790
840
950
0
1013169
1,430
730
700
0
l7/ i/69
1,410
476
934
0
24/3/69
1,710
545
1,165
0
31/3/69
1,090
350
740
89
7/4/69
855
392
463
78
14/4/69
1,020
280
740
50
2114/69
1,340
s99
941
28
28/4/69
644
133
511
164
5/5/69
830
164
66
178
12/5/69
--
--
--
-
19/5/69
.,I90
252
938
220
26/5/69
1,380
448
1,132
228
-
-------
Tabe B2. Nitrogen forms, lagoon
Date
Day/Mo/Yr
Kjeldah l
mg/i
Ammonia
mg/i
Organic
mg/i
Nitx ate
trig/i
3/2/69
6QC)
500
100
0
1012F69
615
268
347
0
17/2/69
626
435
191.
0
24/2/69
--
--
-
3/3/69
610
560
50
0
iO/3 69
625
z45
180
0
17/3/69
580
451
129
0
24/3/69
395
305
90
0
31/3/69
465
354
111
0
7/4/69
373
312
61
0
14/4(69
435
333
102
0
21/4/69
430
320
110
4
28/4/69
420
312
108
10
5/5/69
570
.
240
330
14
12/5/69
-
--
19/5/69
493
450
43
20
26/5/69
485
462
23
20
156
-------
Table 83. Nitrogen forms, returned effluent
157
Date
Day/Mo/yt
Kje ldah].
mg/i
Ammonia
mg/i
Organic
mg/i
Nitrate
cngl l
3/2/69
470
425
--
0
10/2/69
493
336
157
0
17/2/69
519
400
119
0
24/2/69
--
-
--
3/3/69
455
468
-
0
10/3/69
667
525
142
0
17/3/69
501
451
50
0
24/3/69
428
366
62
0
31/3/69
368
280
150
130
7/4/69
232
235
--
164
14/4/69
201
160
41
206
21/4/69
210
195
15
24
28/4/69
90
43
47
198
5/5/69
85
32
53
190
12/5/69
--
-
-
19/5/69
119
56
63
412
26/5/69
-------
Table 84. Phosphate (as P0 3 )
Date
Day/Mo/Yr
Lagoon
Poly Total
mg/I rag/i
Returned
poly
mg/i
Effluent
total
mg/i
3/2/69
192
L87
73
100
10/2/69
205
245
84
96
17/2/69
230
310
93
143
24/2/69
--
-
--
--
3/3/69
228
340
93
159
10/3/69
278
410
120
170
17/3/69
286
308
116
180
24/3/69
160
220
110
154
31/3/69
2]4
278
96
318
7/4/69
200
330
80
150
14/4/69
280
274
128
226
21/1/69
350
384
154
192
28/4/69
324
444
748
380
5/5/69
530
507
6C .
523
12/5/69
--
-
--
--
19/5/69
428
360
616
820
6/5/69
440
564
468
564
158
-------
Table B5. pH, temperature and coliforms, manure slurry
aMembrane filter technique.
159
Date
Day/Mo/Yr
pH
Temp
°F
Coliforins 8
N°/l00 ml
3/2/69
41
10/2169
8.1
35.5
-
17/2/69
--
42.5
3.3 x 1O 7
24/2/69
--
--
--
3/3/69
8.0
42.5
2.1 x IO
10/3/69
--
43.5
0.33 x 1O 7
17/3/69
7.9
48
2.4 x l0
24/3/69
7.7
48.5
2.6 x 1O 7
31/3/69
7.8
43
0.78 x 1O 7
7/4/69
7.5
60
7.0 x
14/4/69
7,3
56
4.7 x 1O 7
21/4/69
7.3
61
2.3 x 1O 7
2814/69
7.0
55
2.1 x 10
5/5/69
6.9
71
-
1215/69
-
72
5.3 x 1O 7
1915/69
6.9
64
1.9 x 10
26/5/69
7.2
70
1.9xx 101
-------
Table R6. PH, chloride, ten erature and coliforms, lagoon
Date
Day/Mo/Yr
pH
C1
mg/-i
Temp
0 F
Coliformsa
N°/lOO ml
3/2/69
-
-
36
--
10/2/69
7.4
-
32
-
17/2/69
--
35.5
120 x 1O 5
24/2/69
--
-
--
--
3/3/69
7.4
--
35
7 x 10
10/3/69
-
--
35.5
6.5 x 1O 5
17/3/69
7.5
37
8.7 x I C 5
24/3/69
7.5
144
37.5
8.2 x
31/3/69
7.4
163
35
7.1 x l0
7/4/69
7.4
155
54.5
4.2 x lO
14/4/69
7.6
168
55
3.9 x 1O
21/4/69
7.5
174
58
2.6 x 10
28/4/69
7.3
168
57
1.8 x 1O
5/5/69
7.3
144
65.5
--
12,5/69
--
--
69
6.7 x 10
19/5/69
7.3
186
61
1.6 x 1O
26/5/69
7.3
184
10
aMembrane filter technique.
160
.1
-. - - . .-- - - . - __.. ._.J .-- - i,-. -. - - - _,
-------
Table B7. pH, chloride, temperature and coliforms, returz ed effluent
D;ji
Day/Mo/Yr
pH
-
Cl
mg/i
Temp
.
Co] .fo
N°/l00
a
rms
3/2/69
--
--
34.5
--
ml
10/2/69
8.3
224
32
17/2/69
--
234
36
- -
0.85 x
1O 5
24/2/69
--
--
-
3/3/69
8.1
226
37.5
--
10
10/3/69
--
240
x
10
17/3/69
8.2
245
37
x
0.3
10
24/3/69
8.2
236
39.5
x
0.41
1O 5
31/3/69
8.0
188
35.5
x
1O
7/4/69
7 :9
177
45.5
10
14/4/69
7.8
173
52
x
10
21/4/69
7.7
172
56
10
28/4/69
6.3
162
56
x
0.85 x
1O 5
5/5/69
5.6
164
62
--
12/5/69
--
--
61
19/5/69
6.2
179
61
-
1O
26/5/69
0.055 x
LiMembrane filter technique.
161
I ._&J_. * _ . .. . ___A __ . _
-------
Table 38. Total solids, manure slurry
162
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/ ].
Fixed
mg/I
3/2/69
13,290
9,970
3,320
10/2/69
17,760
13,830
3,930
17/2/69
13,450
-
-
24/2/69
--
--
--
3/3/69
16,390
12,410
3,980
10/3/69
16,630
12,790
3,640
17/3/69
11,940
9,050
2,890
24/3/69
14,520
11,170
3,350
31/3/69
15,6 .)
12,080
3,570
7/4/69
-
--
-
14/4/69
9,20
7,440
2,280
21/4/69
10,510
8,020
2,490
28/4/69
16,130
12,570
3,560
5/5/69
-
-
-
12/5/69
18,620
14,810
3,810
19/5/69
11,210
8,300
2,910
26/5/69
17,870
14,210
.,r. - _ .-.-- -
__ 1
-------
-- -r . - i-- c r r - -
Table B9. Dissolved Bolids, manure slurry
Date
Day/Mo/Yr
Total
mgft
Volatile
mg/i
Fixed
mg/i
3/2/69
-
-
--
10/2/69
4,950
- 2,700
2,250
17/2/69
2,680
1,290
1,390
24/2/69
-
--
--
3/3/69
4,740
2,390
2,350
10/3/69
4,450
2,290
2,160
17/3/69
3,620
-
1,840
1,780
24/3/69
4,160
2,190
1,970
3 f3/69
4.860
2,620
2,240
7/4/69
--
--
--
14/4/69
2,970
1,460
1,510
21/4/69
3,270
1,680
1,590
28/4/69
4,360
2,290
2,070
5/5/ 9
-
--
--
12/5/69
4,550
2,220
2,330
19/5/69
4,020
2,020
2,000
26/5/69
3,920
1,940
1,980
163
-------
_.r._ - . .- - - _, - , - ..T-_-__, -.. - ?
Table B10. Suspended solids, manure slurry
Datc
Day/Mo/Yr
Total
mg/I
Volatile
mg/i
Fixed
mg/I
3/2/69
-
--
--
10/2/69
12,810
11,130
1,680
17/2/69
10,770
-
24/2/69
--
--
--
3/3/69
11,650
10,020
1,630
10/3/69
12,180
10,500
1,680
17/3/69
8,320
7,210
.,l10
24/3/69
10,360
8,980
1,380
31/3/69
10,790
9,460
1,330
7/4169
--
--
--
14/4/69
6,750
5,980
770
21/4(69
7,240
6,340
900
28/4/69
11,770
10,280
1,490
5/5/69
--
--
--
12/5/69
14,070
12,590
1,48
19/5/69
7,190
6.280
910
26/5169
13,950
12,270
0
164
-------
Table B11. Total solids, lagoon
Date
DaylMo/Yr
Total
mg/i
Volatile
mg/i
Fixed
mg/i
3/2/69
2,250
1,080
-
1)170
10/2/69
2,340
1,320
1,320
17/2/69
2,510
--
24/2/69
-
-
--
313/69
2,540
1,170
1,370
10/3/69
2,600
1,170
1,430
17/3/69
2,160
1,150
1,010
24/3/69
1,770
760
1,010
31/3/69
1,930
830
1,100
7/4169
--
-
14/4/69
1,950
870
1,080
21/4/69
1,850
780
1,070
28/4/69
1,960
960
1,000
5/5/69
-
-
--
12/5 /69
1,840
710
1,130
19/5169
),760
580
1,180
26/5/69
2,540
1,090
1,450
165
* .
_a- a.- sa&V. *4 a s..LZs*O.. 4* > - -
-------
Table B12. Dissolved solids, lagoon
Date
Day/Mo/Yr
Total
mg/I
Volatile
i g/l
Fixed
mg/i
3/2/69
1,820
10/2/69
2,040
--
17/2169
2,290
900
1,390
24/2/69
--
--
3/3/69
2,460
970
1,490
10/3/69
2,410
890
1,520
17/3/69
1,760
750
1,010
24/3/6
1,500
580
920
31/3/69
1,960
750
1,210
7/4169
14/4/69
1,600
580
1,020
21/4/69
1,500
510
990
28/4/69
1,440
490
950
5/5/69
-
-
12/5/69
1,440
470
970
19/5/69
1,590
460
1,130
26/../69
1,040
190
166
. _ -.-
I.
-------
Table B13. Suspended solids, lagoon
D tc
Total
Volatila
Fixed
Day/Mo/Yr
mg/i
mg/I
mg/i
3/2/69 430
10/2/69 300
17/2/69 220
24/2/69
3fl/69 80
10/3/69 190
17/3/69 400 .00 0
24/3/69 270 180 90
31/3/69
7/4/69
14 14 169 a 350 293 60
350 270 80
28/4/6 ? 520 470 50
5/5/69
12/5/6? 400 240 160
19/5/6? 170 120
26/5/698 1,500 900 400
8 Measured using glasafibre filter.
167
. --- -.- - --- --- --. - - 1.
-------
Table 814. Total solids, returned effluent
Date
Day/Mo/yr
Total
mg/I
Volatile
mg/i
Fixed
mg/i
312/69
1,600
610
990
1012/69
2,3]0
1,220
1,090
17/2/69
1,890
-
24/2/69
-
--
-
3/3/69
1,660
520
1,140
10/3/69
1,620
430
1,190
17/3/69
1,780
630
1,150
2413/69
1,580
540
1,040
31/3/69
1,520
500
1,020
7/4/69
--
-
-
14/4/69
1,510
470
1,040
21/4/69
1,3(,0
370
990
28/4/69
2,140
580
1,560
5/5/69
--
--
- -
12/5/69
2,290
730
1,560
19/5/69
2,120
730
1,390
26/5/69
168
a---- ---- - -
--- - - .. .- - - - ..- - -. _ _ * ;: .: -
-------
Table B15. Djsgo1v d bolids returned effluent
Datc
Day/Mo/yr
Total
mg/i
Volatile
mg/i
Fixed
mg/i
3/2/69
1,390
--
10/2/69
1,380
-
-
17/2169
1,660
520
1,140
24/2/69
--
-
--
3/3/69
1,640
480
1,160
10/3/69
--
--
-
17/3/69
1,630
550
1,080
24/3/69
1,300
400
900
31/3/69
1,4 o
450
1,030
7/4/69
-
--
14/4/69
1,400
420
980
21/4/69
1,255
305
950
28/4/69
1,795
310
1,485
5/5/69
-
-
--
l2/ /69
1,900
420
1,480
19/5/69
L82 0
480
1,340
26/5/69
1,640
169
-------
S
Table 816. Suspended solids, returned effluent
Date
Day/Mo/Yr
Total
mg/I
Volat:ile
mg/i
Fixed
mg/i
3/2169
210
--
10/2/69
930
--
--
1712/69
230
-
-
24/2/69
-
3/3/69
20
--
--
10/3/69
-
17/3/69
150
80
70
24/3/69
280
160
140
3 1/3/69
40
--
--
7/4/69
--
--
--
14/4/6 ?
110
50
60
2)/4/6?
2814169 a
105
34r
65
270
40
75
5/5/69
--
-
-
12/5/6?
390
310
80
19/5/6?
300
250
50
26/5/6 ?
2,040
1,610
430
aMd uaing gias fibr fi 1t r.
170
-------
Table Bl7. Total solids, ditch
Date Total Volatile Fixed
Day/Mo/Yr mg/i mg/i mg/i
3/2/69 2,480 1,230 1,250
10/2/69 2,960 1,710 1,250
17/2/69 3,390 - -
24/2/69 -- --
3/3/69 4,130 2,300 1,830
10/3/69 3,990 2,220 1,770
1713/69 4,700 2,930 1,770
24/3/69 4,460 2,780 1,680
31/3/69 - 4,770 3,080 1,690
7/4169 --
14/4/69 5900 3,800 2,100
21/4/69 4,770 2,910 1,860
28/4/69 5,680 3,580 2,100
5/5/69 -- -
1215)69 5,960 3,850 2,310
19/5/69 5,570 3,620 1,950
26/5/69 4,150 2,450 1,700
171
-------
- - - . - -r-- -- - .
Table 318. Dissolved solids, ditch
Date
Day/Mo fYr
Total
mg/i
Volatile
mg/i
Fixed
3/2/69
1,350
220
mg/i
1,13C
10/2/69
1,430
220
17/2/69
1,710
480
1,210
1,230
24/2/69
-
3/3/69
1,720
510
-
10/3/69
1,820
530
17/3/69
1,880
610
24/3/69
1,470
360
1,270
1,110
31/3/69
1,600
450
7/4/69
-
14/4/69
1,620
480
-
21/4/69
1,430
350
28/4/69
2,110
530
1,080
S/5/69
-
-
1,580
12/5/69
2,140
540
--
19/5/69
l 920
470
1,600
26/5/69
172
-------
T Ii e 619. Suspendcd 5o1&da, d1t ..lL
Date
Day/Mo/?r
Total
rngfl
Volatile
mg/I
FLxed
mg/i
Percent
volatile
%
Sludge
volume
index
ut l/g
3/2/69
1,130
1,010
120
89.4
31
10/2/69
1,530
1,490
40
97.4
29
17/2169
1,680
--
-
30
24/2/69
--
--
--
--
--
3/3/69
2,410
1,790
620
74.3
37
10/3/69
2,170
1,690
480
77.9
41
17/3/6Q
2,820
2,320
500
82.3
43
24/3/69
2,990
2,420
570
80.9
40
31/3/69
3,170
2,630
540
83
49
7/4/69
--
--
--
--
14/4/69
4,280
3,320
960
77.6
44
21/4/69
3,340
2,560
780
76.6
57
2814/69
3,570
3,050
520
85.4
5/5/69
-
-
12/5/69
3,820
3,310
510
86.6
63
19/5/69
3,650
3,150
500
86.3
59
26/5/69
2,300
1,870
430
8).)
52
173
-------
-. . Jr rwr,, -.-;r-- ---J-.
;__ - 1
Table B20. Linear regression for volatile suspended solids, ditch
Date
Day/Mo/Yr
X
Day
Y
vss
a g/1
3/2/69
0
1,010
10/2/69
7
1,490
17/2/69
J4
24/2/69
21
--
3/3/69
28
1,790
10/3/69
35
1,690
17/3/69
42
2,320
24/3/69
49
2,420
31/3/69
56
2,630
7/4/69
63
--
1414/69
70
3,320
287
16,670
( X) 2 /8
10,296
14,259
Growth rate
XY
715,400
(Ex)(ZY)/8
29.6 mg/i day
or 11.6 lb/day
598,036
! .
(EX)( :Y)J8
(EX) /8
1 74
-------
Table B21. Total solids, sludge
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/i
Fixed
mg/i
3/2/69
7,800
5,400
2,400
10/2/69
27,600
20,440
7,160
17/2/69
30,120
-
24/2/69
-
-
3/3/69
17,990
13,070
4,920
10/3/69
18,350
13,790
4,560
l7/3/6
19,880
14,400
5,480
24/3/69
20,410
15,230
5,180
31/3/69
14,270
10,570
3,700
7/4/69
14/4/69
17,880
12,820
5,060
21/4/69
14,930
10,430
4,500
28/4/60
18,930
13,950
4,980
5/5/69
-
-
12/5/69
18,370
14,420
3,950
191)169
18,690
14,600
4,090
26/5/69
175
-------
\
Tabl B22. Dissolved solids 1 sludge
Date
Day/Mo/Yr
.
Total
mg/i
Volatile
mg/i
Fixed
mg/i
3/2/69
1,850
400
1,450
10/2/69
11500
550
950
17/2/69
.,68O
520
1,160
24/2/69
-
-
-
3/3/69
1,750
530
1,220
10/3/69
1,810
460
1,350
17/3/69
1,810
560
1,250
24/3/69
1,430
380
1,050
31/3/69
1,540
420
1,120
7/4/69
--
14/4/69
1,490
420
1,070
21/4/69
1,310
290
1,020
28/4/69
2,210
580
1,630
5/5/69
-
12/5/69
2,100
520
1,580
19/5/69
i 910
480
1,430
26/5/69
--
-
-------
Table B23.
Date
Day/Mo/Yr
Suspended solids, sludge
Total
m 1
Volatile
Fixed
Percent
volatile
- m g/I
mg/i
3/2/69
5,950
5,000
950
84
10/2/69
26,100
19,890
6,210
76.2
17/2/69
28,440
-
-
24/2/69
-
--
3/3/69
16,240
12,540
3,700
77.2
10/3/69
16,540
13,330
3,210
80.6
17/3169
18,070
13,840
4,230
76.6
24/3/69
18,980
14,850
4,130
78.2
31/3/69
12,730
10,150
2,580
79.7
7/4/69
-
-
- -
1414/69
16,390
12,400
3,990
75.7
2114/69
13,620
10,140
3,480
74.4
28/4/69
16,720
13,370
3,350
80
5/ /69
12/5/69
16,270
13,900
2,370
85.4
19/5/69
16,780
14,120
2,660
84.1
26/5/69
--
--
177
-------
Table B24. Oxygen demand, manure Blurry
Date
Day/Mo/Yr
COD
mg/i
SOD 5
mg/I
3/2/69 7,080 2,830
10/2/69 13,500 4,770
17/2/69 17,600 4,810
24/2/69
3/3/69 - 6,750
10/3/69 22,700 8,280
17/3/69 17,800 8,800
24/3/69 17.100 7,850
31/3/69 22,600 8,700
7/4/69 27,200
14/4/69 22,300 10,200
21/4/69 23,800 10,000
28/4/69 14,900 8,500
5/5/69 --
12/5169 25,000 ,8O0
19/5/69 23,700 8,700
26 /5/69 20,600 9,100
178
-------
Table B25. Oxygen demand, lagoon
Date
Day( oIYr
COD
mg/i
ao l ) 5
mg/i
3/2/69
831
728
10/2/69
-
890
17/2/69
1,120
24/2/69
- -
--
313/69
2,420
1,080
10/3169
2,500
1.240
1713169
1,670
765
24/3169
1,560
960
31/3/69
714/69
2,270
1,820
885
600
14/4/69
1,940
1,260
21/4/69
2,140
1,230
28/4169
5/5/69
1,800
-
1,030
--
12/5/69
1,290
375
19/ 5169
960
345
26/5/69
1,050
276
179
-------
Table 1 26. Oxygen demand, returned eCfluent
Dati
Day/Mo/Yr
COD
m /1
8005
mg/ i
3/2169
425
175
10/2/69
570
95
17/2/e 9
790
139
24/2/69
-
-
3/3169
557
67
10/3/69
440
116
17/3/69
452
71
24/3/69
-
475
31/3/6V
544
159
7/4169
408
80
14/4/69
480
11.9
21/4169
425
90
28/4/69
1,420
465
5/5/69
-
-
1215/69
990
170
19/5/69
2,050
26/5/69
2,810
1,340
180
-------
Table B27. Air temperature, pig population, flow rate and paver
Dat
0ut ide
Inhide
Pig
Tank
Rotor
Day/Mo/Yr
Unit
° ?
K
Unit
O
K
population
discharge
gpw
power
kwh/wk
3/2/69 35.5 45 640 22,500
10/2/69 20 48.5 640 31,000
17/2/69 35 60 640 37,000
24/2/69 -- 640 20,500 434
3/3/69 26 54.5 661 26,000 434
10/3/69 37 57 u61 46,697 482
17/ /69 43 63 661 28,209 417
24/3/69 38.5 65 661. 28,588 412
31/3/69 46 65 661 28,457 417
7/4/69 65 73 618 23,281 333
14/4/69 54 67 618 28,393 461
21/4/69 68 73.5 618 27,682 370
28/4/69 62 74 618 25,806 388
5/5/69 80 79 666 10,160
12/5/69 84 84 666 15,576 -
19/5/69 62 71 666 33,362 368
26/5/69 83 83 666 25,892 346
181
-------
APPENDIX C. RAW RESULTS PHASE 2
Table CL. Nitrogen forms, manure slurry
Da .e
Kjeldahl
Ammonia
Organic
Nitrate
Day/Mo/Yr
mg/i
mg/i
mg/i
mg/i
24/8/70 670 314 356 0
31/8/70 754 510 244 0
7/9/70 650 260 390 0
14/9/70 -
21/9/70 443 130 313 95
28/9/70 1,220 385 835 40
5110/70 1,280 427 853 3
12/10/70 1,340 361 979 38
28/12/70 1,240 313 827 0
4112/71 --
1 111/71 1,220 340 780 140
18/1/71 1,690 3d2 1,308 255
25 1L/7 1 2,015 502 1,513 210
1/2/71 2,570 506 2,C64 60
8/2/71 2,6 0 580 2,070 0
15/2/71 1,870 362 1,508 40
22/2/71 2,380 490 1,890 0
1/3/71 2,360 481 1,879 0
182
-------
Table C2. Nitrogen forms, returned effluent
Date
Kjeldah l
Aa onia
Organic
Nitrate
Day/Mo/Yr
mg/I
mg/i
mg/i
mg/I
24/ /70 615 187 428 0
31/8/70 233 174 59 0
7,9/70 450 249 201 0
14/9/70
21/9/70 22.5 5.5 17 90
2 /9/70 53 6 47 60
5/10/70 56 1.5 54.5 10
12/10/70 32 1.5 30.5 60
28/12/70 380 46 336 10
4/12/70
11/1/71 431 76 355 215
18/1/71 974 185 789 335
25/1/71 1,060 218 842 280
1/2/71 600 154 446 150
sizi;i 1,210 118 1,092 0
15/2/71 1,140 Trace 1,140 100
22/2/71 1,030 0 1,030 12
1/3/71 1,170 13 1,l57 0
183
-------
Tabli C3. Nitrogen forms and pH, ditch
Date
Day/Mo/Yr
Kje ldah l Ammonia
mg/i mg/i
Organic
mg i ]
Nitrate pH
mg/i
11/1/71
1,240 76
1,164
225
_
18/1/71
1,050 185
865
315
7.0
25/1/71
1,460 276
1,184
260
7.3
1/2/71
1,280 173
1,107
170
7.5
8/2/71
1,390 123
1,267
0
7.7
15/2/71
1,340 Trace
1,340
130
7.2
22/2/71
1,140 .5
1,138
40
7.6
1/3/71
1,460 14
1,446
0
7.6
Table C4.
Nitrogen forms, over flow
Date
Day/Mo/Yr
Kje idah l
mg/i
Anxnonia
mg/i
OrgE.nic
mg/i
11/1/71
7+
76
658
18/1/71
442
171
271
25/1/71
760
-
233
527
1/2/71
1,320
190
1,130
8/2/71
830
106
726
15/2/71
1,620 -
8
1,612
22/2/71
526
4
522
1/3/71
48
184
-------
Table CS. Phosphate (a*, P0 ), manure slurry
Datc
Day/Mo/Yr
Ortho
mg/i
Poly
mg/I
Total
mg/i
24/8/70 550 450
31/8/70 1,100 715
7/9/70 1,150 1,220
14/9/70 - - - -
21/9170 670 1,300 770
28/9/70 1,000 1,000
5/10/70 1,000 1,490 1,300
12/10/70 1,390 1,430 1,920
28/12/70 850 1,020 1,420
4/12/71 -
11/1/71 1,000 1,200 1,250
18/1/71 1,540 1,490 1,980
25/1/71 1,590 1,000 1,520
1/2/71 900 900 850
8/2/71 1,870 1,870 2,050
15/2/71 1,810 1,750 1,870
22/2/71 1,490 1,540 1,920
1/3/71 1,590 1,650 1,980
185
-------
Ta),Ie C6. Phosphate (as PO ), returned effluent
D4t
Ortho
Poly
Total
Doy/Mo/Yr
mg/I
mg/I
mg/i
24/8/70 450 700
31/ /70 215 215
7/9/70 1,380 1,510
14/9/70 - - --
21/9/70 345 500 3b5
Th19170 500 500
5/ 10 17C 430 1,340 420
12/10/70 625 430 430
28/12/70 500 820 820
4/12/11
11/1/71 660 930 580
18/1//1 9 0 1,000 1,390
25/1/71 1,000 1,750 1,000
1/2/71 960 960 490
8/2/. l 1,250 3,390 1,540
L5/ f7l 1,300 1,540 1,540
22/2/71 1,100 1,340 1,700
1/3/71 1,340 1,540 1,750
186
-------
Table C7. pH 1 chJoride, sulphate 1 temperature
slurry
and coliforms 1 manure
Date
Day/No/Yr
pH
i
C l
mg/i
SO 2
mg l
Temp
0 F
Co1iform
N°/100 ml
24/8/70
7.7
-
76
1.1 x 1O 7
31/8/70
7.6
235
275
78
0.87 x
7/9/70
-
205
-
73
--
14/9/70
21/9/70
--
7.1
--
240
--
240
--
69.5
-
11 x 1O 7
28/9/70
7.2
470
365
62
19 x 1O 7
5/10/70
7.2
527
345
63
12 x 1O
12/10/70
7.0
474
--
64
--
28/12/70
7.0
465
--
45
-
4/12/71
-
11/1/71
6.9
267
430
9
6.:, x 1O
18/1/71
6.9
720
440
47.5
6.0 x
25/1/71
7.3
680
580
50.5
-
1/2/71
8/2/71
7.2
7.6
860
7 s0
940
650
50
53
62 x 1O 7
3.4 x 1O
15/2/71
7.5
630
560
--
5.5 10
22/3/71
1/3/71
7 4
7.4
760
830\
590
560
53.5
55
6.5 x 10
2.6 x 10
aMembranc £ilicr technique.
187
-------
Table CS. . 2 H, chloride, sulphate, temperature and coliforms, returned
effluent
Date
D .y/aMo/Yr
-
pH CI
mg/I
SO
mΰ l
Temp
°F
a
Coliforms
N°/100 ml
24/8/70 7.8 I1 198 79.5 2:0 x 106
7.7 152 180 82 0.31 x io6
719170 199 79
14/9170 - - - -
21/9/70 6.8 168 240 74 9.5 x
28/9/70 7.0 216 325 71.5 2.4 x io6
5/10/70 7.2 270 335 70.5 1.2 x io6
12/10/70 6.9 315 69
28/12/70 7.0 265 420 45.5
4/12(7 1. -- - - --
11/1/71 6.4 267 355 45 1.1 x io6
18/1/71 6.8 335 380 41 12 x 106
25/1/71 7.2 400 440 47
1/2/71 7.6 443 570 46.5 .7 x 10
8/2/71 7.6 520 550 48.5 2.1 x 106
1512/71 7.2 570 470 52.5 3.0 x io6
22/ i/ lI 7.5 540 610 50.5 3.0 x io6
1/3171 7.5 540 500 50.5 2.1 x io6
aKenJ rane filter technique.
388
-------
Table C9. Totdl. Nolids, manure . 1urry
Date
Total
Vo1a i1e
Fixed
DayIMo/Yr
m g/i
mg/i
mg/i
2418/70 11,600 8,460 3,140
31/8/70 12,720 9,070 3,650
7 9/70 7,760 5,920 1,840
1419/70
2)/9/70 5,360 3,250 2,110
28/9/70 11,610 7,030 4,580
5/10/70 l1,9 0 8,500 3,430
12/10/70 7,820 4,590 3,230
28/12/70 16,810 13,290 3,520
4/12/71 - -
11/ 1/71 14,500 10,980 3,520
18/1/71 17,650 13,010 4,640
25/1/71 23,440 17,8/0 5,570
1/2/71 20,490 15,260 5,230
8/2/71 25,960 19,990 5,970
15/2/71 .i9,240 31,500 7,740
22/i/71 26,100 19,920 6,180
1/3/71 29,560 23,120 6,440
189
-------
Table ClO. Dissolvcd solids, manure slurry
Date
Total
Volatile
Fixed
Day/Mo/Yr
mg/i
mg/i
mg/i
24/τ/70
2,490
1,300
1,190
31/8/70
6,350
3,790
2,560
7/9/70
2,300
1,160
1,140
14/9/70
21/9/70
2,910
1,240
1,670
28/9/70
5,350
2,750
2,600
5/10/70
4,870
2,490
2,380
12/10/70
4,620
1,9 0
2,700
28/12/70
4,560
2,890
1,670
4/12/71
11/1/71
7.610
5,120
2,490
18/1/71
6,990
4,000
2,990
25/1/71
7,010
3,870
3,140
1/2/71
4,860
2,030
2,830
8/2/71
3,640
840
2,800
15/2/71
6,100
2,740
3,360
22/2/71
5,860
2,680
3,180
1/3/71
7,320
3,620
3,700
I
-------
Table Cli. Suspended solLds, manure slurry
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/i
Fixed
mg/i
24/8/70
9,100
7,160
1,950
31/8/70
6,370
5,280
1,090
7/9/70
5,460
4760
700
14/9/70
-
-
21/9/70
2,450
2,010
440
28/9/70
6,260
4,280
1,980
5/10/70
7.060
6,010
1,050
12/10/70
3,200
2,670
530
28/12/70
12,250
10,400
1,850
4/12/71
-
11/1/71
6,890
5,860
1,030
18/1/71
10,660
9,010
1,650
25/1/71
16,430
14,000
2,430
1/2/71
15,630
13,230
2,4 0
8/2/71
22,320
19,150
3,170
15/2/71
33,140
28,760
4,380
22/2/71
20,240
17,240
3,000
1/3/71
22,240
19,500
2,740
19]
-------
Table C12. Total solids, returned effluent
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/I
Fixed
mg/i
24/8/70
7,100
4,500
2,600
31/8/70
1,850
840
1,010
7/9/70
1,660
740
920
14/9/70
--
21/9/70
2,740
1,230
1,510
28/9/70
2,390
770
1,620
5/10/70
2,420
710
1,710
12/10/70
2,630
610
2,020
28/12/70
15,910
12,410
3,500
4/12/71
-
-
11/1/71
4,210
2,070
2,140
18/1/71
6,970
4,320
2,650
25/1/71
15,430
11,210
4,220
1/2/71
lo,710
11,90 ;
4,810
8/2/73.
15,670
10,920
4,750
15/2/71
17,770
12,440
5,330
22/2/71
17,490
12,270
5,220
1/3/71
16,370
11,140
5,230
192
-------
Table C13. Dissolved solids, returned effluent
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/i
Fixed
mg/i
24/8/70
900
230
670
31/8/70
1,240
320
920
7/9/70
1,190
320
870
l4 9/7O
- -
- -
--
2119/70
1,650
370
1,280
28/9/70
1,910
460
1,450
5110/70
2,330
640
1,690
12110/70
2,450
480
1,970
28/12/70
2,050
540
1,510
4/12/71
--
11/1/71
3,910
1,640
2,270
18/1/71
4,240
2,180
2,060
25/1/71
3,900
1,510
2,390
1/2/71
3,670
1,030
2,640
8/L/71
5,900
1,500
4,400
15/2/71
3,960
940
3,0_0
22/2/71
3,260
650
2,610
113171
3,430
800
2,630
193
-------
Table C14. Suspended solids, returned effluent
Date Total Volatile Fixed
Day/Mo/Yr m g I I mg/i mg/i
2418/70 6,200 4,270 1,930
70 610 520 90
7/9/70 470 420 50
34/9170
21/9/70 1,090 860 230
28/9/70 480 310 170
5/10, 70 90 70 20
12/10/70 180 130 50
28/12/70 13,860 13,870 1,990
4/12/71
11/1/71 300 430
18/1/71 2,730 2,140 590
25/1/71 11,530 9,700 1,830
:/2/71 13,040 10,870 2,170
8/2/71 9,770 9,420 350
15/2/71 13,810 11,500 2,310
22/1/71 14,230 11,620 2,610
1/3/71 12,940 10,340 2,600
194
-------
Table C15. Total Holid , ditch
195
Date
Day/Mo/Yr
Total
mg/i
Volatile
mall
Fixed
mg/i
24/8/70
6,6Z0
4,190
2,430
31/8/70
9,040
6,010
3,030
7/9/70
8,750
6,010
2,740
14/9/70
-
-
--
21/9/70
7,800
4,190
3,610
28/9/70
8,680
5,650
3,030
5/10/70
9,930
6,55(.
3,380
12/10/70
11,500
7,530
3,970
28/12/70
13,730
10,660
3,070
4/12/71
-
11/1171
16,250
12,560
3,690
18/1/71
16,570
12,410
4,160
25/1/71
19,860
15,050
4,810
1/2/71
19,750
14,690
5,060
8/2/71
17,250
12,250
5,000
15/2/71
21,410
15,670
5,740
22/2/71
18420
13,040
5,380
1/3/71
18,340
12,850
5,490
3
-------
fable C16. Di&801v0d solids, ditch
Date
Totil
Volatile
Day/Mo/Yr
mg/i
mg/i
Fixed
mg/i
24/8/70
31/8/70
7/9/70
14/9/70
2 1/9/70
28/9/70
5/10/70
12/10/70
28/12/70
4/12/71
11/1/71
18/1/71
25/1/71
1/2/71
8/2,71
15/2/71
22/2/7 1
1/3/71
820
1,300
1 , 190
1,720
2,100
2,300
2,430
2,210
3,990
4,220
4,170
3,750
4,030
4,150
3,300
3,280
196
140
370
310
420
530
600
470
710
1,710
2,140
1,670
1,100
1,000
1,010
640
920
680
930
880
1,300
1,570
1,700
1,960
1,500
2,280
2,080
2,500
2,650
3,030
3,140
2,660
2,360
-------
Table C17. Suspended solids, ditch
Date
Day/Mo/Yr
Total
rig/I
Volatile
mg/i
Fixed
mg/l
Percent
volatile
I.
Sludge
volume
index
mug
24/8/70
5,800
4,050
1,750
69.8
58
31/8/70
7,740
5,640
2,100
72.9
67
7/9/70
7,560
5,700
1,860
75.4
72
14/9/70
21/9170
6,080
3,770
2,310
62.0
91
28/9/70
6,580
5,120
1,460
77.8
74
5/10/70
7,630
5,950
1,680
78.0
79
12/10/70
9,070
,060
2,010
77.8
108
28/12/70
11,520
9,950
1,570
86.4
65
4/12/71
11/1/71
12,260
10,850
1,410
88.5
74
18/1/71
12,350
10,270
2,080
83.2
80
25/1/71
15.690
13,380
2,310
85.3
62
1/2/71
16,000
13,590
2,ll O
84.9
62
8/2/71
13,220
11,250
1,970
85.1
15/2/71
17,260
14,660
2,600
84.9
-
22/2/71
15,120
12,400
2,720
82.0
-
1/3/71
15,060
11,930
3,130
79.2
-
197
-------
Table C18. Total solids, sludge
198
Date
Day/Mo/yr
Tot l
mg/i
Volatile
Tag/i
Fixed
mg/i
24/8/70
20,230
12,830
7,400
31/8/70
21,770
15,250
6,520
7/9/70
17,490
12,670
4,820
14/9/70
--
-
21/9/70
11,610
8,360
3,250
28/9/70
7,900
5,030
2,870
5/10/70
12,260
7,290
4,970
12/10/70
14,430
9,960
4,470
28/12/70
29,440
24,850
4,590
4/12/71
-
11/1/71
16,520
12,710
3,810
18/1/71
15,520
11,500
4,020
25/1/7
-
-
1/2/71
19,820
14,610
5,210
8/2/71
17,270
12,270
5,000
15/2/71
18,750
13,360
5,390
22/2/71
18,480
13,020
5,460
1/3/71
16,800
11,500
5,300
-J
-------
-
_______________ , rr ._
Table C19. Dissolved solids, sludge
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/i
Fixed
mg/I.
24/8/70
950
230
720
31/8170
1,470
460
1,010
7/9/70
1,240
310
-
930
14/9/70
-
--
21/9/70
1,620
400
1,220
28/9/70
2,080
510
1,570
5/10/70
2,250
540
1,710
12/10/70
2,460
450
2,010
28/12/70
2,130
580
1,550
4/12/71
11/1/71
3,920
1,560
2,360
18/1/71
5,310
3,180
2,130
25/1/71
-
1/2/71
3,710
1,160
2,550
8/2/71
3,900
940
2,960
15/2/71
4,130
1,000
3,130
22/2/71
3,390
660
2,730
1/3/71
3,570
700
2,870
199
-------
- -- ---. - .-. - ..
Table C20. Suspended solida, sludge
Date
Total
Volatile
Fixed
Percent
Day/No/Yr
mg/i
mg/i
mg/i
volatile
V.
24/8/70 19,280 12,600 6,680 65.4
31/8/70 20,300 14,790 5,510 72.9
7/9/70 16,250 12,360 3,890 76.1
14/9/70
21/9/70 9,990 7,960 2,030
28/9/70 5,820 4,520 1,300 77.7
5110/70 10,010 6,750 3,260 67.4
12/10/70 11,970 9,510 2,460 79.4
28/12/70 27,310 24,270 3,040 88.9
4/12/71 - - --
11/1/71 12,600 11,150 1,450 88.5
18/1/71 10,210 8,320 1,890 81.5
2 f1/71 -- -
1/2/71 16,110 13,450 2,660 83.5
8/2/71 13,370 11,330 2,040 84.7
15/2/71 14,620 12,360 2,260 84.5
22/2/71 15,090 12,360 2,730 81.9
1/3/71 13,230 10,800 2,430 81.6
200
-------
Table C21. Total solids, overflow
Dale
Day/Mo/Yr
Total
mg/i
Volz.ti le
mg/i
Fixed
mg/i
11/1/71
11,170
8440
3,030
18/1/71
6,290
3,820
2,470
25/1/71
26,100
20,480
5,620
1/2/71
16,410
12,190
4,220
8/2/71
15,270
10,600
4,670
15/2/71
18,110
12,750
5,360
22/2/71
15,560
10,660
4,900
1/3/71
19,750
14,160
5,590
Table C22.
Suspended
solids, overflow
Date
Day/Mo/Yr
Total
mg/i
Volatile
mg/i
Fixed
ing/l
11/1/71
7,260
6,500
760
18/1/71
2,050
1,640
410
25/1/71
22,200
18,970
3,230
1/2/71
12,740
11,160
1,580
8/2/71
9,370
9,100
270
15/2/71
14,150
11,810
2,340
22/2/71
12,300
10,010
2,290
1/3/71
16,320
13,360
2,960
202.
-------
14
Table C23. Oxygen demand/manure slurry
a
Ke, isteeeo trademark of thL
D.,w Chem i.ca1 Company.
202
Date
Day/Mo/yr
COD
mg/i
BOD
5
mg/i
+
BOD
5 a
N-Serve
mg/i
24/8/70
6,550
2,950
--
31/8/70
6,850
2,900
--
7/9/70
9,800
3,850
--
14/9/70
--
--
--
2119/70
10,350
4,130
--
28/9/70
17,600
8,300
--
5/10/70
10,000
5,550
3,700
12/10/70
-
-
28/12/70
16,000
6,900
--
4/12/71
-
-
--
11/1/71
16,100
7,530
6,000
18/1/71
20,800
8,100
5,250
25/1/li
30,800
8,050
6,180
1/2/71
32,900
16,800
8,710
8/2/71
26 .300
10,800
7,450
15/2/fl
27,700
11,300
8,030
22/2/7].
ii, 100
13 .800
Lo,ioo
1/3/71
27,70o
16,200
9,680
I
-------
α fr c..rr, . -: :- -- --- -ew - .--. - --
E7 -
Table C24. Oxygen demand/returned effluent
1.
I,
Date
Day/Mo/Yr
COD
mg/I
ROD 5
-
mg/i
ROD 5 a
+ N-Serve
mg/i
COD
mg/i
Centrate
ROD 5
mg/i
24/8/70
530
141
-
-
--
31/8/70
1,630
495
-
-
-
7/9/70
840
134
-
--
--
14/9/70
-
-
21/9/70
490
40
- -
--
--
28/9/70
860
126
-
--
-
5/10/70
750
69
60
--
--
12/10/70
28/12/70
810
58
--
4/12/71
- -
11/1/71
8,200
2,550
1,140
-
18/1/71
4,220
2,470
-
-
25/1/71
14,200
3,920
2,570
1,030
72
1/2/71
18,700
4,430
2,910
1,010
74
8/2/71
15,900
/,050
2,850
880
54
15/2/71
18,400
5,950
3,970
740
45
22/2/71
17,600
6,450
4,100
1,110
240
1/3/73.
14,700
5,430
2,910
726
45
a gistered trademark of
the Dow Chemical Company.
203
-------
TabL. C25. Oxygen demand, ditch
Date
Day/Mo/Yr
COD BOD
mg/i mg/i
COD
mg/i
Centrate
ROD 5
mg/i
11/1/71
15,100 4,400
18/1/71
18,600 5,600
2,800
-
25/1/71
21,600 5,550
965
66
1/2/71
20,400 5,800
945
42
8/2/71
21,000 7,050
900
60
15/2/71
21,500 6,900
720
33
22/2/71
19,500 7,300
920
138
1/3/71
j.8,700 6,550
772
57
Table C26.
Oxygen
demand, overflow
Date
Day/Mo/Yr
COD
mg/i
ROD
mg/i
11/]/71
9,800
2,100
18/1/71
-
1,540
25/1/71
18,600
3,730
1/2/71
14,900
4,180
8/2/71
15/2/71
10,800
17, 6O0
2,770
5,300
22/2/71
11,700
4,140
1/3/71
9,450
3,420
r.
204
-------
Table C27. Air temperature and relative humidity
Date
Outside Unit K
Temp
Inside Unit K
Day/Mo/yr
op
7
Temp
°F
R u
7.
24/8/70 67.5 79.5 75 87
3 1/8/70 67 75 68 84
7/9/7ij 7] 69 74 76
14/9/70 -- - -
21/9/70 68 67 68.5 69
28/9/70 57 52 59.5 66
5/10/70 62 65 64 73.5
12/10/70 59.5 64.5 65.5 64.5
28/12/70 29 42.5 54.5 93.5
4/12/71 18 49 59 97
1 1/1//l 17 45 59.5 94
18/1/71 17.5 29 60 92
25/1//I 18 46.5 62.5 91
1/2/71 14 49 62 93
8(2/71 15.5 50.5 63 92
152/7 1 38 5 72 66 92
22/2/71 31.5 64.5 64 87
1/3/71 30.5 57 60 94
205
-------
Table C28. Pig population, flow rate and power
Date
Day1W /Yr
Pig
population
Tank
discharge
gpw
Ditch
overflow
gpw
Rotor
power
kwh/wk
Total
power
kwhfwk
24/8/70
31/8/70
575
575
31,620
27,534
--
-
1,040
915
--
-
7/9/70
496
22,863
--
1,124
14/9/70
496
22,273
-
--
1,126
21/9/70
496
32,980
--
1,162
28/9/70
496
10587 a
1,028
-
5/i0/70
446
12137 b
--
1,192
12/10/70
468
16,120
1,122
28/12/70
575
-
-
-
-
4/12/71
595
5,653
950
11/1/71
582
20,680
--
1,046
18/1/71
616
19,900
4,011
-
1,225
25/1/71
632
19,380
5,091
1,018
1/2/71
621
16,820
8,125
867
8/2/71
596
13,580
5,077
1,065
15/2/71
613
15,120
14,983
-
1,124
22/2/71
626
15,840
4, 51
678
1/3171
662
14,100
4,177
-
1,204
a 3 hr flush interval.
b 2 hr flush interval from here on.
206
-------
APPENDIX 1). RAW RESULTS AEROBIC SLUDGE DIGESTION
Table Dl. Nitrogen forms, chloride and temperature
Date
Day/Mo/Yr
Kjeldahl
mi::ed
mg/i
Kjeidahi
centrate
m g/i
Nitrate
mg/i
Chloride
mgi ].
Temp
°F
8/3/71
i,4l 0
41
65
710
50.5
15/3/71
1,370
41
-
714
50
22/3/71
1,195
45
-
715
47
29/3/71
927
40
33
700
49.5
5/4/71
734
34
-
694
52
12/4/71
790
34
--
717
57
19/4/71
613
28
-
729
64.5
26/4/71
593
24
270
729
60
3/5/71
504
21
240
724
59.5
10/5/71
476
17
60
725
62
17/5/71
454
22
45
724
67
207
-------
Table D2. Total solids
Date
Day/Mo/Y:
Total
rag/i
Volatile
rag/i
Fixed
mg/i
8/3/71
21,780
15,350
6,430
15/3/n
19,790
13,530
6,260
22/3/71
18,180
11,970
6,210
29/3/71
16,010
10,400
5,610
5/4/71
13,700
8,500
5,200
12/4/71
15,920
10,290
5,630
1914/71
14,270
9,100
5,170
26/4/71
13,610
8,3O
5,240
3/5/71
11,300
6,340
4,960
10/5/71
11,240
6,360
4,860
17/5/71
11,790
6,740
5,050
Table D3.
Dissolved
solids
Date
Total
Day/Mo/Yr
mg/i
Volatile
mg/i
Fixed
mg/i
8/3/71
4,370
990
3,380
15/3/71
4,430
1,000
3,430
22/3/71
4,420
890
3,530
29/3/71
4,190
990
3,200
5/4/71
4,650
:
870
3,780
12/4/71
i.04 0
650
3,390
19/4/71
4,150
760
26/4/71
3,970
690
3,390
3,280
3/5/71
3,980
650
3,330
10/5/71
3,910
640
3,270
17/5/71
4,050
770
3,280
208
- £_ - .
-------
Table D4. Suspended soiLds
Date
nay/Mo/Yr
Total Volatile
t ag/i mg/I
Fixed
mg/i
Percent
volatile
Sludge
volume
index
mi/ c t
8/3/7].
17,410 14,360
3,050
82.5
NSa
15/3/71
15,360 12,530
2,830
81.6
NS
22/3/71
13,760 11,080
2,680
80.5
72
29/3/71
11,820 9,410
2,410
79.6
NS
5/4/71
9,050 7,630
1,420
84.3
109
12/4/71
11,880 9,640
2,240
81.1
78
19/4/71
10,120 8,340
1,780
82.4
65
26/4/71
9,640 7,680
1,960
79.7
5].
3/5/71
7,320 5,690
1,630
77.7
74
10/5/71
7,330 5,72 )
1,610
78.0
72
17/5/71
7,740 5,970
1,770
77.1
114
no settling.
Table D5.
Oxygen demand, rotor power
and temperature
Date
Mixed
Centrate
Rotor
Temp
Day/Mo/Yr
mg/i
COD
mg/i
power
kwh
,
F
8/3/71 23,800 1,240 1,257 34
15/317 1 19,100 1,060 1 2S1 36
22/3/71 19,400 915 1,253 32
29/3/71 14,000 856 1,216 45
5/4/71 12,900 760 1,171 59.5
12/4/71 14,610 703 1,137 54
19/4/71 16,400 657 1,118 61
26/4/71 10,900 581 1,129 55
3/5/71. 9,700 547 3120 66
10/5/71 8,070 440 1,099 63
17/5/71 9,500 406 - 67
209
- -
-------
- I ____
- . - . - ---- . . - ?__
Table D6. Linear regression fur K rate
Date
Day/Mo/yr
X
Day
VSS
mg/I
Y
VSS
813/71
0
14,360
Log 10
15/3 17 ].
7
12,530
4.157
22/3/71
14
11,080
4.098
29/3/7j
21
9,410
4.045
5/4/71
28
7,630
3.974
12/4/71
35
9,640
3.883
19/4 /71
42
8,340
3.984
26/4171
49
7,680
3.921
3/5/71
56
5,690
3.885
10/5/71
63
5,720
3.755
17/5/7 ].
70
5,970
3.757
3.776
ZX = 385
18,865
K -
LY
£XY
43,235
1,483,272
=
(EX) 2 /1 1
( X)(Zy)/lI
0.00556 Day 1
13,475
1,513,225
-
LX
(ZX)( y)/li
ax) /11
Log 10 V5S 0
Y 0
Y+K
4.125 or
w
210
-------
---..--- .. -
____ _________- -- - - - -
Table D7. Linear regreasion for K rate COD in suspended solids
Datc
Day/Mo/Yr
X
Day
COD
mg/i
Y
Log 10 C OD
8/3/71
0
22,600
4.354
15/3/71
7
18,040
4.256
22/3/71
14
18,490
4.267
29/3/71
21
13,140
4.119
5/4/71
28
12,140
4.084
12/4/71
35
13,910
4.143
19/4/71
42
15,740
4.197
26/4/71
49
10,320
4.014
3/5/71
56
9,150
3.961
30/5/71
63
7,630
3.883
17/5/71
70
9,090
3.959
= 3s5 45,237 QX) 2 /i l 13,475
ZX 2 = 18,865 1,551,921 (EX)(EY)/11 1,583,295
XY (EX Y)/1l
0.00583
- - (EX) 2 /l1
Log 10 c0D 0 Y 0 .1- xi
4.316 or COD 0 20,700 mg/i
211
-
-------
I
_____ --
Table D8. Linear regression for K rate Kjeldahl N in suspended solids
Date X Kjeld hi Y
N
Day/Mo/Yr Day nigh Log 10 N
8/3/71 0 1,430 3.152
15/3/71 7 1,330 3.124
22/3/71 14 1,150 3.061
29/3/71 21 887 2.948
5/4/71 28 700 2.845
12/4/71 35 56 2.879
19/4171 42 685 2.836
26/4/71 49 569 2.755
3/5/71 56 483 2.684
10/5/71 63 459 2.662
17/5/71 70 432 2.635
385 31,581 (ZX) 2 /ii 13,475
18,865 ZXY 1 ,06i,622 ( x)(EY)/11 -- 1,105,335
- - 0.00774 t?ay 1
LX (ZX) / 11
Log 10 N 0 I + XX
3.142 or NG 1,390 mg/J.
22.2
-------
APPENDIX E. RAW RESULTS PIGS t WATER SUPPLY
Table El. Pig weight gain pea 16 gutter water (C)
Pig
5/1/71
Body weigiLt
19/1/71
in lb
2/2/71
10/2/71
Weight
gain
lb
2956
46
62
78
84
38
4022 B
46
66
87
102
56
2951 S
57
62
70
75
18
4046 8
53
74
94
116
63
4049 8
60
83.
95
105
45
4044 B
61
86
93
103
42
2195 B
68
76
93
10].
33
4070 S
52
71
78
86
34
2972 S
54
70
80
90
36
2934 S
67
84
89
103
36
Table 1 2.
Pig
weight gaiu
pen 17 normal
waterer
(N)
Pig
5/1/71
Body weight
19/1/71
in lb
2/2/71
10/2/71
Weight
gain
lb
2954 z
69
102
110
127
58
2994
56
82
98
122
66
4000 S
61
90
115
128
67
4043 S
59
90
110
121
62
4009 3
62
96
120
138
76
4060 S
53
82
103
112
59
4063 8
52.
80
103
117
66
2193 B
73
108
126
142
69
4821 S
56
82
100
112
56
4820 S
48
62
71
85
37
213
I.
-------
r
- c - -- ?-
Table E3. Pig ieLght gain pen 1 gutter water (C)
Pig
5/1/71
Body weight
19/1./71
in lb
2/2/71
10/2/71
Weight
gain
lb
4233 B
53
75
98
108
55
4137B
40
54
71
80
40
4234 B
63
90
117
127
64
4300s
44
60
79
89
45
4065 B
52
68
85
94
42
4162 B
62
88
113
124
62
4040 B
64
78
101
112
48
4016 B
72
74
87
96
24
2192 B
82
98
124
135
53
2952 s
55
74
95
104
49
Table E4.
Pig
weight gain
pen 19 normal
waterers
(N)
Pig
5/1. 171
Body weight
1911/71
in lb
2/2/71
10/2/71
Weight
gain
lb
4133 5
48
66
97
100
52
4153 S
55
72
83
92
37
4157 S
61
84
107
117
56
4064 S
53
72
90
96
43
4126 B
52
74
100
112
60
4291 S
58
80
104
117
59
4123 S
55
78
103
118
63
4210 B
50
74
106
110
60
4134 B
50
73
92
108
58
4260 S
50
70
99
112
62
214
-------
- - r -
Table ES. Pig weight gain pen 20 gutter water (G)
r
ti
I-
Pig
5/1/71
Body weight
19/1/71
in lb
-
Weight
gain
4090 S
63
80
2/2/71
105
10/2/71
122
lb
4315 B
55
74
81
91
4160 S
58
74
91
100
36
4100 S
54
70
91
102
42
4101 S
57
69
82
96
48
4232 S
58
74
93
102
39
41 16B
44
52
67
76
44
4220 S
63
82
107
114
32
4132 S
51
67
81
93
51
4168 B
55
66
81
92
42
37
Table E6.
Pig
weight gain
pen 21 normal
waterer
(N)
P t 8
5/1/71
Body weight
19/1/71
J.n lb
Weight
gain
2606 B
67
4
2/2/71
121
10/2/71
132
lb
2943 S
48
70
83
94
65
2973 B
62
84
107
118
46
2947 B
60
83
108
124
56
2955 B
61
88
100
105
64
2970 S
55
78
94
104
44
2957B
57
78
93
93
49
2928 B
71
100
102
124
36
2634 B
69
96
123
137
53
2971S
46
70
82
91
68
4
215
-------
3
0 %
Table El. Feed weight record
Pen
511/11
8/1/71
11/1/71
Weight
12/1/71
of feed in lb
14/1/71 15/1/71
18/1/71
21/1/71
16(C)
200
50
51
50
5
100
75
100
17(N)
202
50
51
100
100
100
200
100
1 9(G)
19(N)
200
200
50
30
51
51
50
50
75
100
100
100
75
75
100
100
20(G)
200
50
51
50
100
100
75
100
21
200
50
-- 51
50
100
100
100
200
-------
Table V. (Contini ed)
-
Pen Weight of feed in lb
22/1/71 27/1/71 !9/1/71 1/2/71 5/21,1 8/2/71 Rennant Total
16( 0) 100 100 0 150 200 100 110 1,241
17(N) 100 100 100 200 200 200 71 1,732
18(G) 100 100 lOO 150 200 100 62 1,389
19(N) 100 103 100 200 200 100 64 1,462
20(G) 100 100 100 150 200 50 68 1,358
21(N) 100 100 0 150 200 100 76 1,425
-------
Table E8. Pen weight gain totals
Treatment
Block
3005
Table E9.
G N
401 616 1017
482 550 1032
_ 430 I 520 956
1313 1692
a 159,515 Myy 150,500.4
Weight gain ANDy (completely randomized design)
Tyy 2394 Eyy 771.3
Syy 5849.3
Source cf Degrees of Sum of Mea F
variation freedom sguare square statistic
Mean 1 150,500.4 150,500.4
Treatmen s 1 2,396 2,394 12.42
Experimental error 4 771.3 192.8 (F 14 =7.7 1
SampI ir g errer 54 5,849.3 108.3 at 5 . )
Total 60 159,5]5
Table ElO. Weight gain ANDy (randomized complete block design)
Sft 3165.3 Syy 5849.3 Byy 162.1
Tyy 2394 Eyy 609.2
Source of Degrees of Sum of Mean F-
variation freedom sguare Statistic
Mean 1 150,500.4 150,500,4
Blocks 2 162.1 81.1
Treatments 1 2,394 2,394 7.8 6
Experimental error 2 609...2 304.6 (F 1 2 8.5
Sampling error 54 5 9 .3 108.3 at 57 )
Total 60 159,515.0
1:
1
218
-------
TabTe Eli.. Feed conaijm d totals
Treatment
C N
1,261 1,732 2,973
Block 1,389 1,462 2,851
1,358 1,425 2,783
3,988 4,616
ZY 8607 £Y 2 12,481,459 Myy 12,346,741.5
Table E12. Feed consumed ANOV (completely randomized design)
Tyy 57,125.2 Eyy 77,592.3
Source of Degrees of Sum of Mean
variation freedom
F
squares square
Mean
Statistic
1 12,346,741.6 12,346,741.6
Treatments
1 57,125.2 57,125.2
Experiigental error 4 77,592.3 19,398.1
2.94
7.71
Total 6 12,481,459.1
at 57.)
Table E13. Feed consumed ANOV (randomized complete block
Byy 9268 Tyy 57,125.2 Eyy
design)
68,324.3
Source of
Degrees of Sum of Mean
variati freedom
F
squares square
Mean
statistic
1 12,346,741.5 12,346,741.5
Blocks 2
9,268 4,634
Treatments i
57,125.2 57,125.2
Exprimental error 2 68,324.3 34,162.2
1.67
(F 1 f 8 5
Total 6 12,481,459.1
at 57.)
219
I - ... 4
-------
Table 14. Feed conversion
Treatment
G N
3.09 2.81 5.90
Block 2.88 2.66 5.54
3.t 1 6 2.71 5.87
9.13 8.18
17.31 50.1439 Myy 49.9394
Table E15. Feed conversion ANOV (randomized complete block design)
Byy 0.0399 Tyy 0.1504 Eyy 0.0142
Source of
variation
Degrees of
freedom
Sum of
squares
1 ean.
square
F
statistic
Mean
1
49.9394
49.93.9
Blocks
2
0.0399
0.0199
Treatments
1
0.1504
0.1504
21.2
Experimental
Total
error
2
0.0142
50.l4 9
0.0071
(F
1,2
at
18.5
57.)
220 1
j
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