SERA
United States
Environmental Protection
Agency
Municipal Environmental Research EPA 600 1 79-132
Laboratory November 1979
Cincinnati OH 45268
and Development
Septage
M
Addition
Waste water
Treatment Plsnts
Volume
Addition
Liquid Stre
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RESEARCH REPORTING SERIES
Research reports of the Office of Research and Development, U.S. Environmental
Protection Agency, have been grouped into nine series. These nine broad cate-
gories were established to facilitate further development and application of en-
vironmental technology. Elimination of traditional grouping was consciously
planned to foster technology transfer and a maximum interface in related fields.
The nine series are:
1. Environmental Health Effects Research
2. Environmental Protection Technology
3. Ecological Research
4. Environmental Monitoring
5. Socioeconomic Environmental Studies
6. Scientific and Technical Assessment Reports (STAR)
7. Interagency Energy-Environment Research and Development
8. "Special" Reports
9. Miscellaneous Reports
This report has been assigned to the ENVIRONMENTAL PROTECTION TECH-
NOLOGY series. This series describes research performed to develop and dem-
onstrate instrumentation, equipment, and methodology to repair or prevent en-
vironmental degradation from point and non-point sources of pollution. This work
provides the new or improved technology required for the control and treatment
of pollution-sources to meet environmental quality standards.
This document is available to the public through the National Technical Informa-
tion Service, Springfield, Virginia 22161.
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EPA-600/2-79-132
November 1979
MONITORING SEPTAGE ADDITION TO
WASTEWATER TREATMENT PLANTS
Volume I: Addition to
the Liquid Stream
by
Burton A. Segall
Charles R. Ott
William B. Moeller
University of Lowell
Lowell, Massachusetts 01854
Grant No. R805406010
Project Officers
Steven W. Hathaway
Robert P. G. Bowker
Wastewater Research Division
Municipal Environmental Research Laboratory
Cincinnati, Ohio 45268
MUNICIPAL ENVIRONMENTAL RESEARCH LABORATORY
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
CINCINNATI, OHIO 45268
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DISCLAIMER
This report has been reviewed by the Municipal Environmental
Research Laboratory, U. S. Environmental Protection Agency, and
approved for publication. Approval does not signify that the
contents necessarily reflect the views and policies of the U.S.
Environmental Protection Agency, nor does mention of trade names
or commercial products constitute endorsement or recommendation
for use.
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FOREWORD
The U. S. Environmental Protection Agency was created be-
cause of increasing public and government concern about the
dangers of pollution to the health and welfare of the American
people. Noxious air, foul water, and spoiled land are tragic
testimony to the deterioration of our natural environment. The
complexity of that environment and the interplay between its
components require a concentrated and integrated attack on the
problem.
Research and development is that necessary first step in
problem solution and it involves defining the problem, measuring
its impact, and searching for solutions. The Municipal Environ-
mental Research Laboratory develops new and improved technology
and systems for the prevention, treatment, and management of
wastewater and solid and hazardous waste pollutant discharges
from municipal and community sources, for the preservation and
treatment of public drinking water supplies and to minimize
the adverse economic, social, health, and aesthetic effects of
pollution. This publication is one of the products of that
research; a most vital communications link between the research-
er and the user community.
This report assesses the effects of septage addition to
municipal wastewater treatment plants. It provides treatment
costs and guidelines for designing receiving facilities and
treatment works for combined septage and sewage treatment.
Francis T. Mayo
Director
Municipal Environmental Research
Laboratory
111
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ABSTRACT
The report provides information needed to facilitate
septage disposal at municipal wastewater treatment plants.
Research assessed the effects of septage addition to primary
and secondary biological waste treatment processes. Septage
was added to an extended aeration process at Medfield, Massa-
chusetts, to a two-stage conventional activated sludge process
at Marlborough, Massachusetts, and to a University of Lowell
pilot plant, operated both as an extended aeration and a conven-
tional activated sludge facility.
A three phase monitoring program was conducted at each
plant. All processes were monitored during a no-septage-feed
baseline period, which was followed by constant feed and slug
loading periods.
Research results included acceptable process loading for
existing plants, design criteria for new facilities, the cost of
treating septage and regulations for controlling disposal.
Experience gained in feeding and treating large quantities of
septage is reported.
Septage is readily treated biologically with domestic sew-
age. The organic and solids content of septage averages about
50 times that of domestic sewage. Solids removal in primary
clarification is excellent and in combination with primary or
secondary sludge, septage dewaters well.
This report was submitted by the University of Lowell in
fulfillment of Research Grant No. R805406010, under the sponsor-
ship of the U. S. Environmental Protection Agency and under Grant
No. 76-19 under the sponsorship of the Massachusetts Division of
Water Pollution Control. This report covers the period August
25, 1977, to November 24, 1978.
IV
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CONTENTS
Disclaimer ii
Foreword iii
Abstract iv
Figures x
Tables xiv
Abbreviations and Symbols xxiii
Acknowledgments xxvi
1. Introduction 1
Septage - An Overview of the Problem 1
The Scope of This Research 4
Septage Characteristics and Quantities 5
2. Conclusions 8
Septage Treatability 8
Treatment with Sewage at Municipal Plants . . 8
Recommended Septage Loading 9
Design Parameters for New Facilities ...... 9
Dissolved Oxygen 9
Nitrogen 10
Sludge Production 10
Handling and Receiving 10
Costs ......... 11
Cost of Septage Treatment 11
3. Experimental Facilities 12
Medfield Wastewater Treatment Plant 12
Marlborough Easterly Wastewater Treatment Plant . 14
University of Lowell Pilot Plant ........ 17
4. Monitoring Program 20
Summary of Procedures . , 20
v
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CONTENTS (continued)
Monitoring Program at Medfield 20
Monitoring Program at Marlborough 26
Research at the University Pilot Plant 28
Extended Aeration Mode of Operation 28
Conventional Mode of Operation 30
5. Results at Medfield 31
Phase 1 - Baseline for Comparison 31
Process Characteristics 31
Influent Wastewater Characteristics 32
Effluent Quality Prior to Septage Addition . 34
Mixed Liquor and Secondary Sludge 37
Sludge Dewatering 38
Phase 2 - Continuous Feeding 41
Process Characteristics 41
Influent Sewage and Septage 41
Effluent Quality 45
Nitrogen 47
Nitrification and Denitrification -
An Explanation 50
Phosphorus 50
Dissolved Oxygen 52
Thickener Supernatant and Vacuum
Filtrate Quality 55
Sludge Production 56
Settlometer Tests 57
Sludge Dewatering 61
Phase 3 - Shock Loading 61
Influent and Septage 62
Effluent Quality 62
Nitrogen 66
Dissolved Oxygen 68
Settling 68
6. Results at Marlborough 73
Phase 1 - Baseline for Comparison 73
vi
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CONTENTS (continued)
Operating Parameters 73
Influent Characteristics 73
Primary Clarification 73
Secondary Treatment 76
Nitrification Stage 77
Solids Production 77
Phase 2 - Continuous Feeding . 79
Process Characteristics 79
Influent Characteristics 79
Primary Effluent 81
Secondary Treatment 87
Nitrification Stage 90
Biological Solids Production 91
Phase 3 - Shock Loading 91
Sewage and Septage Characteristics 93
Primary Effluent 93
Primary Clarification 97
Secondary Treatment 102
Nitrification Stage (Stage 2) 109
7. Results at Lowell - Extended Aeration 117
Phases 1 and 2 117
Sewage and Septage Characteristics 117
Food/Microorganism Ratio 117
Dissolved Oxygen Requirements 120
Treatment Efficiency 120
Extended Aeration - Phase 3 122
Mixed Liquor 122
Oxygen Concentrations 123
Effluent Quality 123
8. Results at Lowell - Conventional
Mode of Operation 125
Phase 1 - Baseline for Comparison 125
Operating Parameters 125
vInfluent Characteristics 125
vii
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CONTENTS (continued)
Effluent Characteristics .......... 126
Mixed Liquor Characteristics ........ 127
Phase 2 - Continuous Loading ......... 127
Operating Parameters ............ 127
Influent Characteristics .......... 127
Effluent Characteristics .......... 131
Mixed Liquor Characteristics ........ 133
Phase 3 - Shock Loading ............ 136
Influent - Sewage Plus Septage ....... 136
Effluent Characteristics .......... 136
Mixed Liquor Characteristics ........ 137
9. Microbiology .................. 139
Microbiological Studies ............ 139
Medfield - Microscopic Studies ........ 139
Results .................. 140
Medfield - Phase 1 ............. 140
Medfield - Phase 2 ............. 141
Medfield - Phase 3 ............. 145
Marlborough Microscopic Analyses ....... 147
Floe Characteristics ............ 147
Microorganisms ............... 152
Phase 1 - Results ............. 152
Phase 2 - Results ............. 155
Phase 3 - Results ............. 155
10. Economics of Septage Treatment ......... 156
Cost of Treating Septage at Municipal Plants . 156
Operating and Maintenance Costs for
Treating Septage at Medfield ......... 156
Method 1 - Budget Item Cost Distribution . . 156
Method 2 - Limited Budget Cost Distribution. 159
Method 3 - Incremented Effort Cost
Evaluation
Marlborough - Economic Impact of
Septage Addition
vii
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CONTENTS (continued)
Capital Costs 164
11. Synthesis of Results 167
Design Parameters 167
Septage Strength , 167
Dissolved Oxygen Requirements 167
Sludge Production 169
Aeration Process Loading 170
Primary Clarification 171
Secondary Clarification 172
Guidelines for Septage Addition 172
Septage Handling and Receiving 172
Continuous and Slug Loading 173
Operation Control Strategies 174
Appendices
A. Treatment Plant Process Dimensions 175
B. Medfield - Phase 1 179
C. Medfield - Phase 2A 186
D. Medfield - Phase 2B 193
E. Medfield - Phase 3A 201
F. Medfield - Phase 3B 212
G. Marlborough - Phase 1 223
H. Marlborough - Phase 2 233
I. Marlborough - Phase 3 245
J. Marlborough - Sludge Quantities 269
K. University of Lowell Pilot Plant - Conventional
Operation - Phase 1 274
L. University of Lowell Pilot Plant - Conventional
Operation - Phase 2 277
M. University of Lowell Pilot Plant - Conventional
Operation - Phase 3 281
N. University of Lowell Pilot Plant - Conventional
Operation - Extended Aeration Mode of Operation . 289
ix
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FIGURES
Number Page
I Process schematic for the Medfield plant .... 13
2 Process schematic for the Marlborough Easterly
treatment plant 15
3 Process schematic for the University of Lowell
plant 18
4 Septage feed systems - Medfield 25
5 Influent total solids - Medfield - Phase 3 ... 25
6 Septage feed system - Marlborough 27
7 University of Lowell pilot plant feed systems . . 29
8 Effluent nitrogen and Basin 2 dissolved oxygen -
Medfield - Phase 1 35
9 Effluent nitrogen and Basin 2 dissolved oxygen -
Medfield - Phase 2A 48
10 Effluent nitrogen and Basin 2 dissolved oxygen -
Medfield - Phase 2B 49
11 Settlometer Readings - Medfield - Phases 1 and 2. 59
12 Mixed liquor 30-minute settlometer readings -
Medfield - Phase 1 60
13 Mixed liquor 30-minute settlometer readings -
Medfield - Phase 2A 60
14 Septage feed vs. capillary suction time -
Medfield 62
15 Effluent BOD and COD - Medfield - Phase 3A ... 64
16 Effluent BOD and COD - Medfield - Phase 3B ... 64
17 Effluent total solids and suspended solids -
Medfield - Phase 3A 65
18 Effluent total solids and suspended solids -
Medfield - Phase 3B . . 66
19 Effluent nitrogen and Basin 2 dissolved oxygen -
Medfield - Phase 3A 67
20 Effluent nitrogen and Basin 2 dissolved oxygen -
Medfield - Phase 3B 67
x
-------
FIGURES (continued)
Number Page
21 Basin 3 dissolved oxygen uptake - Medfield -
Phase 3A 69
22 Basin 1 and 3 dissolved oxygen uptake -
Medfield - Phase 3B 69
23 Thirty-minute settlometer reading Basin 4 -
Medfield - Phase 3A 70
24 Thirty-minute settlometer reading Basins 1 and 4-
Medfield - Phase 3B 70
25 Average settlometer readings Basin 4 - Medfield 71
26 Settlometer supernatant turbidity - Medfield -
Phase 3B 72
27 Primary effluent COD and BOD,. - Marlborough -
Phase 3A .......... 7 94
28 Primary effluent COD and BOD- - Marlborough -
Phase 3B 95
29 Primary effluent total and suspended solids -
Marlborough - Phase 3A 96
30 Primary effluent total and suspended solids -
Marlborough - Phase 3B 97
31 Primary clarifier total solids profiles -
Marlborough - Phase 3 98
32 Primary clarifier total solids distribution -
Marlborough - Phase 3 99
33 Clarifier effluent responses to a pulse input . . 100
34 Primary clarifier, effluent total solids/influent
total solids - Marlborough - Phase 3 101
35 Secondary effluent COD and BOD- - Marlborough -
Phase 3A 7 102
36 Secondary effluent COD and BOD- - Marlborough -
Phase 3B 7 103
37 Secondary effluent total and suspended solids -
Marlborough - Phase 3A 103
38 Secondary effluent total and suspended solids -
Marlborough - Phase 3B 104
39 Secondary effluent nitrogen - Marlborough -
Phase 3A 105
40 Secondary effluent nitrogen - Marlborough -
Phase 3B . 105
xi
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FIGURES (continued)
Number Page
41 Mixed liquor dissolved oxygen, first stage -
Marlborough - Phase 3A 106
42 Mixed liquor dissolved oxygen, first stage -
Marlborough - Phase 3B 106
43 Mixed liquor dissolved oxygen uptake, first
stage - Marlborough - Phase 3A 107
44 Mixed liquor dissolved oxygen uptake, first
stage - Marlborough - Phase 3B 108
45 Thirty-minute settlometer, first stage -
Marlborough - Phase 3A 1°8
46 Thirty-minute settlometer, first stage -
Marlborough - Phase 3B 109
47 Final effluent COD and BOD^ - Marlborough -
Phase 3A 110
48 Final effluent COD - Marlborough - Phase 3B . . 110
49 Final effluent total and suspended solids -
Marlborough - Phase 3A Ill
50 Final effluent total and suspended solids -
Marlborough - Phase 3B Ill
51 Dissolved oxygen, first and last compartment,
second stage - Marlborough - Phase 3A 112
52 Dissolved oxygen, first and last compartment
second stage - Marlborough - Phase 3B 113
53 Dissolved oxygen uptake, first compartment,
second stage - Marlborough - Phase 3A 114
54 Dissolved oxygen uptake, first compartment,
second stage - Marlborough - Phase 3B 115
55 Thirty-minute settlometer, last compartment,
second stage - Marlborough - Phase 3A 116
56 Thirty-minute settlometer, last compartment,
second stage - Marlborough - Phase ,3B 116
57 Septage COD and feed rate - Lowell - Extended
aeration Phases 1 and 2 118
58 Mixed liquor suspended solids, settleability,
and sludge wastage - Lowell - Extended aeration
Phases 1 and 2 119
59 Effluent COD - Lowell - Extended aeration
Phases 1 and 2 121
xxi
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FIGURES (continued)
Number Page
60
61
62
63
64
65
66
67
68
69
70
71
72
COD removal efficiency -
aeration Phases 1 and 2
Microbiological indices,
Medfield - Phase 1. . . .
Microbiological indices,
Medfield - Phase 1. . .
Microbiological indices,
Phase 1
Microbiological indices,
Medfield - Phase 2A . .
Microbiological indices,
Medfield - Phase 2A . . ,
Microbiological indices,
Phase 2A
Microbiological indices,
Phase 2B ,
Microbiological indices,
Medfield - Phase 3A . . ,
Microbiological indices,
Phase 3A ,
Microbiological indices,
Medfield - Phase 3A . . ,
Microbiological indices,
Phase 3B ,
Microbiological indices,
Medfield - Phase 3B . . ,
Lowell - Extended
mixed liquor -
return sludge -
effluent - Medfield -
mixed liquor -
return sludge -
effluent - Medfield -
effluent - Medfield -
mixed liquor -
effluent - Medfield -
mixed liquor -
mixed liquor - Medfield -
secondary effluent -
122
141
142
142
143
143
144
145
146
148
149
150
151
Xlll
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TABLES
Number
1 Lists of Plants Treating Septage in
Massachusetts
2 Septage Characteristics ............ 6
3 Medfield Treatment Plant Process Dimensions . . 14
4 Marlborough Treatment Plant Process
Dimensions .................. 16
5 University of Lowell Pilot Plant Process
Dimensions .................. 19
6 Schedule of Samples and Analyses ....... 21
7 Analytical Procedures ............. 23
8 Test Periods and Septage Loading at Medfield . 24
9 Test Periods and Septage Loading at
Marlborough .................. 26
10 Test Periods and Septage Loadings at University
of Lowell Pilot Plant ............. 30
11 Process Characteristics - Medfield Phase 1 . . 32
12 Influent, Effluent, Thickener Supernatant
and Vacuum Filtrate Characteristics -
Medfield - Phase 1 .............. 33
13 Mixed Liquor and Secondary Sludge Character-
istics - Medfield - Phase 1 .......... 38
14 Thickener Sludge and Vacuum Filter Cake -
Medfield - Phase 1 .............. 39
15 Volatile Suspended Solids Balance - Medfield -
Phase 1 .................... 40
16 Process Characteristics and Loading - Medfield-
Phases 1 & 2 ................. 42
17 Sewage and Septage - Medfield - Phase 2A ... 43
18 Sewage and Septage - Medfield - Phase 2B . . . 44
19 Effluent Quality - Medfield - Phases 1 & 2 . . 46
20 Analysis of Variance Results - Medfield .... 47
21 Phosphorus Removal - Medfield - Phases 1 & 2 . 51
xiv
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TABLES (continued)
Number Page
22 Mixed Liquor Characteristics - Medfield -
Phases 1 & 2 52
23 Dissolved Oxygen Utilization - Medfield -
Phases 1 & 2 54
24 Thickener Supernatant Characteristics -
Medfield - Phases 1 & 2 56
25 Vacuum Filtrate Characteristics - Medfield -
Phases 1 & 2 57
26 Thickener Sludge and Vacuum Filter Cake -
Medfield - Phases 1 & 2 58
27 Volatile Suspended Solids Balance - Medfield -
Phase 2 58
28 Solids Ratios - Medfield - Phase 2A 59
29 Sewage and Septage Characteristics - Medfield -
Phase 3 63
30 Process Characteristics - Marlborough -
Phase 1 74
31 Influent, Primary Effluent, Secondary
Effluent and Final Effluent - Marlborough -
Phase 1 75
32 Mixed Liquor - Marlborough - Phase 1 76
33 Volatile Suspended Solids Balance - Marl-
borough - Phase 1 78
34 Return Sludge and Combined Sludge - Marl-
borough - Phase 1 80
35 Vacuum Filter Filtrate and Cake - Marlborough-
Phase 1 81
36 Process Characteristics - Marlborough -
Phase 2 82
37 Sewage, Septage and Combined Influent -
Marlborough - Phase 2A • 83
38 Sewage, Septage and Combined Influent -
Marlborough - Phase 2B 84
39 Primary Effluent, Secondary Effluent and
Final Effluent - Marlborough - Phase 2A . . . 85
40 Primary Effluent, Secondary Effluent and
Final Effluent - Marlborough - Phase 2B . . . 86
41 Ratios of Characteristics - Marlborough -
Phases 2A & 2B 87
xv
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TABLES (continued)
Number Page
42 Efficiency of Primary Clarifiers -
Marlborough - Phases 2A & 2B 88
43 Mixed Liquor - Marlborough - Phase 2A . . . . 89
44 Mixed Liquor - Marlborough - Phase 2B . . . . 90
45 Return Sludge and Combined Sludge -
Marlborough - Phase 2A 92
46 Return Sludge and Combined Sludge -
Marlborough - Phase 2B 92
47 Vacuum Filter Filtrate and Cake -
Marlborough - Phases 2A & 2B . 93
48 Sewage and Septage Characteristics -
Marlborough - Phase 3 94
49 Oxygen Utilization at Septage/Sewage Ratio of
3.1% - Lowell - Extended Aeration - Phase 2 . 120
50 Process Characteristics - Lowell - Conven-
tional Mode - Phase 1 125
51 Influent and Effluent - Lowell - Conventional
Mode - Phase 1 126
52 Mixed Liquor - Lowell - Conventional Mode -
Phase 1 128
53 Process Characteristics - Lowell - Conventional
Mode - Phase 2 129
54 Sewage, Septage, and Combined Influent -
Lowell - Conventional Mode - Phase 2A .... 129
55 Sewage, Septage and Combined Influent - Lowell-
Conventional Mode - Phase 2B 131
56 Effluent - Lowell - Conventional Mode -
Phase 2 . 132
57 Mixed Liquor - Lowell - Conventional Mode -
Phase 2 134
58 Mixed Liquor Microbiological Indices and Floe
Characteristics - Marlborough - First Stage . 153
59 Mixed Liquor Microbiological Indices and Floe
Characteristics - Marlborough - Second Stage-
First Compartment 153
60 Mixed Liquor Microbiological Indices and Floe
Characteristics - Marlborough - Second Stage-
Last Compartment 154
xvi
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TABLES (continued)
Number Page
61 Medfield Treatment Plant Averages and
Yearly Totals 157
62 Percent Distribution - Medfield - Method 1 . . 157
63 Cost Distribution - Medfield - Method 1 .... 158
64 Budget Item Cost Distribution - Method 1 ... 160
65 Plant Cost Component Distribution 161
66 Solids Handling and Disposal Unit Costs and
Estimated Increases as a Function of Solids
Loading Increase - Marlborough 163
67 Present and Projected Costs of Solids Handling
and Disposal - Marlborough 165
68 Typical Design Parameters ..... 170
APPENDIX A
A-l Medfield Treatment Plant Process Dimensions . . 175
A-2 Marlborough Treatment Plant Process
Dimensions 176
A-3 University of Lowell Pilot Plant Process
Dimensions ...... 178
APPENDIX B
B-l Medfield - Phase 1 (no septage) - Influent . . 179
B-2 Medfield - Phase 1 (no septage) - Secondary
Effluent 180
B-3 Medfield - Phase 1 (no septage) - Mixed
Liquor 181
B-4 Medfield - Phase 1 - Secondary Return Sludge . 182
B-5 Medfield - Phase 1 (no septage) - Thickener and
Vacuum Filter 183
B-6 -Medf-ield-—• -Pha-s-e 1 (no septage) - Micro-
biological indices 184
xvn
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TABLES (continued)
Number Page
APPENDIX C
C-l Medfield - Phase IIA (continuous loading)
Septage 186
C-2 Medfield - Phase IIA (continuous loading)
Influent 187
C-3 Medfield - Phase IIA (continuous loading)
Secondary Effluent 188
C-4 Medfield - Phase IIA - Mixed Liquor 189
C-5 Medfield - Phase IIA (continuous loading)
Secondary Return Sludge 190
C-6 Medfield - Phase IIA (continuous loading)
Thickener and Vacuum Filter 191
C-7 Medfield - Phase IIA (continuous loading)
Microbiological Indices 192
APPENDIX D
D-l Medfield - Phase IIB (continuous loading)
Septage 193
D-2 Medfield - Phase IIB (continuous loading)
Influent 194
D-3 Medfield - Phase IIB - Secondary Effluent . . . 194
D-4 Medfield - Phase IIB - Mixed Liquor 195
D-5 Medfield - Phase IIB - Dissolved Oxygen .... 196
D-6 Medfield - Phase IIB - Secondary Sludge .... 196
D-7 Medfield - Phase IIB - Thickener and Vacuum
Filter 197
D-8 Medfield - Phase IIB - Microbiological Indices. 198
D-9 Medfield - Heavy Metals - Influent, Effluent
and Septage 199
D-10 Medfield - Heavy Metals - Thickener and
Vacuum Filter 200
APPENDIX E
E-l Medfield - Phase IIIA (shock loading) -
Septage 201
XVlll
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TABLES (continued)
Number Page
E-2 Medfield - Phase IIIA (shock loading) -
Influent 201
E-3 Medfield - Phase IIIA (shock loading) -
Secondary Effluent 202
E-4 Medfield - Phase IIIA (shock loading) -
Dissolved Oxygen 206
E-5 Medfield - Phase IIIA (shock loading) -
Mixed Liquor Basin 1 and 4 207
E-6 Medfield - Phase IIIA (shock loading) -
Mixed Liquor Basin 1 208
E-7 Medfield - Phase IIIA - Secondary Sludge . . . 209
E-8 Medfield - Phase IIIA (shock loading) -
Thickener and Vacuum Filter 209
E-9 Medfield - Phase IIIA (shock loading) -
Microbiological Indices 210
APPENDIX F
F-l Medfield - Phase IIIB (shock loading) -
Septage 212
F-2 Medfield - Phase IIIB (shock loading) -
Influent 212
F-3 Medfield - Phase IIIB (shock loading) -
Secondary Effluent 213
F-4 Medfield - Phase IIIB (shock loading) -
Dissolved Oxygen 216
F-5 Medfield - Phase IIIB (shock loading) -
Mixed Liquor 218
F-6 Medfield - Phase IIB - Secondary Sludge . . . 222
F-7 Medfield - Phase IIB (shock loading) -
Microbiological Indices 222
APPENDIX G
G-l Marlborough - Phase I - Influent 223
G-2 Marlborough - Phase I - Primary Effluent . . . 224
G-3 Marlborough - Phase I - Secondary Effluent . . 225
G-4 Marlborough - Phase I - Final Effluent .... 226
xix
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TABLES (continued)
Number page
G-5 Marlborough - Phase I - Mixed Liquor 227
G-6 Marlborough - Phase I - Mixed Liquor - Second
Stage - First Compartment 228
G-7 Marlborough - Phase I - Mixed Liquor - Second
Stage - Last Compartment 229
G-8 Marlborough - Phase I - Returned and Combined
Sludges 230
G-9 Marlborough - Phase I - Vacuum Filter .... 232
APPENDIX H
H-l Marlborough - Phase II - Septage 233
H-2 Marlborough - Phase II - Influent 233
H-3 Marlborough - Phase II - Primary Effluent . . 234
H-4 Marlborough - Phase II - Secondary Effluent . 235
H-5 Marlborough - Phase II - Final Effluent . . . 236
H-6 Marlborough - Phase II - Mixed Liquor -
First Stage 237
H-7 Marlborough - Phase II - Mixed Liquor -
Second Stage - First Compartment 238
H-8 Marlborough - Phase II - Mixed Liquor -
Second Stage - Last Compartment 239
H-9 Marlborough - Phase II - Returned and Combined
Sludges 240
H-10 Marlborough - Phase II - Vacuum Filter .... 242
H-ll Marlborough - Phases I and II - Heavy Metals . 243
APPENDIX I
1-1 Marlborough - Phase III - Septage 245
1-2 Marlborough - Phase III - Influent 246
1-3 Marlborough - Phase III - Primary Effluent . . 247
1-4 Marlborough - Phase III - Secondary Effluent . 251
1-5 Marlborough - Phase III - Final Effluent . . . 255
1-6 Marlborough - Phase III - Mixed Liquor -
First Stage 258
1-7 Marlborough - Phase III - Mixed Liquor -
Second Stage - First Compartment 261
xx
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TABLES (continued)
Number Page
1-8 Marlborough - Phase III - Mixed Liquor -
Second Stage - Last Compartment 265
APPENDIX J
J-l Marlborough - Phases I, II and III -
Sludges Wasted 269
J-2 Marlborough - Phases I, II and III - Sludge
Quantities Wasted 271
J-3 Marlborough - Phases I, II and III - Sludges
Wasted 272
J-4 Variation of Solids Concentration with Depth
in the Primary Clarifier During Shock Loading -
Phase III - Total Solids 273
APPENDIX K
K-l University of Lowell Pilot Plant - Conven-
tional Mode of Operation - Phase 1 - Influent . 274
K-2 University of Lowell Pilot Plant - Conven-
tional Mode of Operation - Phase 1 -
Secondary Effluent ..... 275
K-3 University of Lowell Pilot Plant - Conven-
tional Mode of Operation - Phase I - Mixed
Liquor 276
APPENDIX L
L-l University of Lowell Pilot Plant - Conven-
tional Mode of Operation - Phase II - Septage . 277
L-2 University of Lowell Pilot Plant - Conven-
tional Mode of Operation - Phase II - Influent. 278
L-3 University of Lowell Pilot Plant - Conven-
tional Mode of Operation - Phase II - Effluent. 279
L-4 University of Lowell Pilot Plant -
Conventional Mode of Operation - Phase II -
Mixed Liquor 280
xxi
-------
TABLES (continued)
Number Page
APPENDIX M
M-l University of Lowell Pilot Plant -
Conventional Mode of Operation - Phase III -
Septage 281
M-2 University of Lowell Pilot Plant -
Conventional Mode of Operation - Phase III -
Influent 282
M-3 University of Lowell Pilot Plant -
Conventional Mode of Operation - Phase III -
Effluent 283
M-4 University of Lowell Pilot Plant -
Conventional Mode of Operation - Phase III -
Mixed Liquor 285
M-5 University of Lowell Pilot Plant -
Conventional Mode of Operation - Phase III -
Dissolved Oxygen 287
APPENDIX N
N-l -University of Lowell Pilot Plant -
Operation in Extended Aeration Mode -
Phase III - Septage 289
N-2 University of Lowell Pilot Plant - Operation
in Extended Aeration Mode - Phase III -
Influent 290
N-3 University of Lowell Pilot Plant - Operation
in Extended Aeration Mode - Phase III -
Effluent 291
N-4 University of Lowell Pilot Plant - Operation
in Extended Aeration Mode - Phase III -
Dissolved Oxygen » 292
N-5 University of Lowell Pilot Plant - Operation
in Extended Aeration Mode - Phase III -
Mixed Liquor 293
xxii
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LIST OF ABBREVIATIONS AND SYMBOLS
ABBREVIATIONS
AS —activated sludge
AWT —advanced waste treatment
BODj —five day biochemical oxygen demand
BODL --ultimate biochemical oxygen demand
C --composite sample
cm —centimeter
COD —chemical oxygen demand
CST —capillary suction time
cu ft —cubic feet
cu m --cubic meter
D —daily
D.O. —dissolved oxygen
EA --extended aeration
F/M --food to microorganism ratio
g —gram
G —grab sample
gal --gallon
hp-h —horsepower-hour
hr —hour
kg —kilogram
km —kilometer
kw-h —kilowatt hour
1 —liter
LAS —linear alkyl sulfonate
Ibs —pounds
mgd —million gallons per day
mg/1 —milligrams per liter
mi —mile
njl —milliliter
MLSS —mixed liquor suspended solids
MLVSS —mixed liquor volatile suspended solids
ORP —oxidation reduction potential
PRI —primary plant
rpm --revolutions per minute
s --standard deviation
sec --second
SEC —secondary plant
SF --sand filter
sq ft —square feet
sq m —square meter
XXlll
-------
ABBREVIATIONS AND SYMBOLS (CONT'D)
ABBREVIATIONS
SRT
SS
susp
SW
TF
TKN
TSS
Vol
VOL
VSS
x
yr
—solids retention time
—suspended solids
--suspended
--semi weekly
—trickling filter
—total kjeldahl nitrogen
-—total suspended solids
—volatile
—volume
—volatile suspended solids
—mean of readings
—year
SYMBOLS
Al
A1203
ABOD
C
°C
CaCOo
Cd
Cr
Cs
Cu
H
HC03
H2C°3
H20
K
Kd
Kn
°2
n
ni
N
NH3-N
NH4
Ni
NO 3
N03-N
Pb
-aluminum ion
-aluminum oxide
-difference in BOD5 input between Phases 1 and 2
-carbon, dissolved oxygen concentration, or cost
-degrees centigrade
-calcium carbonate
-cadmium
-chromium
-saturation dissolved oxygen concentration
-copper
-empirical formula for cell tissue
-diversity index
-bicarbonate ion
-carbonic acid
-water
-oxygen transfer coefficient
-endogenous decay coefficient
-half saturation constant for oxygen
-total number of organisms
-number of organisms in the i
•nitrogen
-ammonia> nitrogen
-ammoniom ion
-nickel
•nitrate ion
-nitrate nitrogen
-oxygen
•phosphorus
-lead
.th
species
XXIV
-------
ABBREVIATIONS AND SYMBOLS (CONT'D)
SYMBOLS
Q —flow rate
Qr —recycle flow rate
U --food to microorganism ratio
v —cost per cu m (1000 gal) liquid
w —cost per kg (Ib) BOD
x —cost per kg (Ib) COD
y --cost per kg (Ib) suspended solids
Y —actual cell yield coefficient
Y0ks —observed cell yield coefficient
z —cost per kg (Ib) phosphorus
Zn --zinc
0C --mean cell residence time
y —micron
PN —nitrosomonas growth rate
0 —peak nitrosomonas growth rate
xxv
-------
ACKNOWLEDGMENTS
The authors gratefully acknowledge the contributions made
by their research associate Mark Laquidara and graduate research
assistants, Robert Gingras, George Hoag and Michael Ackerman.
The accomplishment of this research would not have been possible
without their interest and considerable efforts.
Operators at both the Medfield and Marlborough, Massachu-
setts wastewater treatment facilities participated in this study,
aiding in sampling, septage feeding and controlling processes
for desired testing. The cooperation of Mr. Kenneth Feeney,
Chief Operator, Town of Medfield and Mr. John Hartley, Super-
intendent of Treatment of Marlborough, is particularly appre-
ciated. Appreciation is expressed to Dr. John Mallet, Assistant
Professor of Biological Sciences, University of Lowell and Mr.
Brian Kelleher, Massachusetts Department of Environmental
Quality Engineering, for assistance in microbiological examina-
tions.
The towns of Medfield and Marlborough permitted the use of
municipal facilities for this study and provided support.
xxvi
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SECTION 1
INTRODUCTION
SEPTAGE - AN OVERVIEW OF THE PROBLEM
At the inception of this project a cross-section of waste
water treatment plant operators in the Commonwealth of Massa-
chusetts were asked if they had experience treating septic tank
wastes or septage. Many indicated that they had difficulties
treating this waste; many accepted only small quantities of
septage and some were reluctant to treat it at all. These
operators were justifiably concerned about process upset or about
violating regulatory requirements for effluent quality. They
expressed a need for information upon which to base a reasonable
estimate of the incremental cost of treating septage.
At relatively small treatment plants a 4 to 12 cu m (1,000
to 3,000 gal) truckload of concentrated waste, discharged in a
period of minutes, can represent a significant load on the plant,
depressing oxygen levels. Plants designed for comparatively
consistent sewage solids and organic concentrations and the nor-
mal diurnal fluctuations in sewage flow can have difficulty if
subjected to slug loadings of septage in which organic and
solids concentrations can be two orders of magnitude greater
than the concentration found in sewage. In the past, operators
and local community governments have exercised minimal control
over haulers' schedules and the origin of collected wastes.
Regulating an occasional load of restaurant septage with high
grease content or a potentially toxic industrial load is diffi-
cult at pl-ants which do not exercise tight controls on incoming
trucks.
In contrast to the experience at small plants, large treat-
ment plants experience little difficulty in handling septage.
Primary clarifiers and large volume aeration tanks at these
plants attenuate the impact of slug loading. In addition, sep-
tage volume has been a minor fraction of their sewage flow. Few
plants in Massachusetts now receive more than 0.5% of their
design sewage flow capacity, and most plants treat considerably
less.
-------
Plants that now treat septage in Massachusetts are shown on
Table 1.
TABLE 1. LISTS OF PLANTS TREATING SEPTAGE IN MASSACHUSETTS
Plant
location
Amherst
Barnstable
Boston-Deer Is.
Boston-Nut Is.
Brockton
Chicopee
Fall River
Fitchburg West
Franklin
Gardner
Greenfield
Haverhill
Ipswich
Lawrence
Leominster
Manchester
Type of
process
AWT
PRI
PRI
PRI
AS
PRI
PRI
AWT
TF
TF
TF
AS
EA
AS
AS
EA
Marlborough East AS
Marshfield
Medfield EA
Middleboro
Milford
Mills EA
Newburyport
Northampton
Pittsfield
SEC
& SF
TF
TF
& SF
PRI
PRI
TF
** Design
flow
cu m/sec (mgd)
0.15
0.06
15.03
4.91
0.53
0.53
1.10
0-54
0.07
0-17
0.14
0.79
0.08
2.28
0.22
0.03
0.24
0.07
0.04
0.18
0.01
0.11
0.13
0.48
(3.5)
(1.4)
(343)
(112)
(12)
(12)
(25)
(12.4)
(1.5)
(3.8)
(3.2)
(18)
(1.8)
(52)
(5)
(0.6)
(5.5)
(1.5)
(0.8)
(4)
(0.3)
(2.6)
(3)
(11)
Average
daily flow
cu m/sec ( mgd)
0.31
0.07
0.44
0.31
0.66
0.44
0.08
0.09
0.14
0.53
0-04
1.31
0.26
0.01
0.11
0.01
0.05
0.11
0.01
0.11
0.15
0.39
(7)
(1.5)
(10)
(7)
(15)
(10)
(1.8)
(2)
(3.2)
(12)
(0.8)
(30)
(6)
(0.3)
(2.5)
(0.3)
(1.1)
(2.5)
(0.3)
(2.5)
(3.5)
(9)
Percent
septage/
sewage
0.22
1.79
unknown*
unknown*
0.15
0.14
0.22
0.10
0-27
0.01
0.13
0.03
0.50
0.04
0.01
0.30
0.16
0.40
0.73
0.04
0.07
unknown*
0.17
0.07
(continued)
2
-------
TABLE 1. (continued)
Plant
location
Plymouth
Rockland
Rockport
Scituate
Shrewsbury
Southbridge
Springfield
Sunderland
Taunton
Webster
Westborough
Westf ield
Worcester
*
Type of
process
EA
AS
EA
EA
TF
EA
PRI
EA
AWT
EA
EA
AS
AS
,# Design Average
flow daily flow
cu m/sec (mgd) cu m/sec (mgd)
0.08
0.04
0.07
0.04
0.08
0.10
1.31
0.02
0.44
0-28
0.05
0.18
2.45
(1.8)
(1.0)
(1.6)
(1.0)
(1.8)
(2.3)
(30)
(0.5)
(10)
(6.3)
(1.1)
(4)
(56)
0.13
0.04
0.04
0.01
0.05
0.09
0.96
0.01
0.26
0-15
0.04
0.18
1.53
(3)
(0.9)
(1.0)
(0.3)
(1.2)
(2)
(22)
(0.2)
(6)
(3.5)
(1.0)
(4)
(35)
Percent
septage/
sewage
0.67
0.50
0.80
1.00
0.33
0.10
0.09
0.67
0.40
0.23
0.15
0.35
unknown*
* Septage discharged directly into sewer system
** Type of treatment category
PRI - Primary wastewater treatment
AS - Conventional activated sludge
EA - Extended aeration
SEC - Secondary biological treatment
TF - Trickling filter
AWT - Advanced wastewater treatment
SF - Sand filter
-------
The list was compiled from telephone surveys conducted in the
spring of 1977 and in July 1978 and from engineering consul-
tant studies.1&2 An effort was made to include all plants now
treating septage. The list shows the present low percentage in-
put to plants, and indicates that only a small number of the
more than 144 plants in Massachusetts treat septage.
There is an obvious need to facilitate septage treatment
where homes served by septic tank disposal systems are within an
economical hauling distance of wastewater treatment plants :
16 km (10 mi) is considered to be a reasonable distance, 32 km
(20 mi) excessive. Acceptance can be encouraged by providing
treatment plants with facilities to receive and process domestic
septage, as well as commercial and industrial septage. It can
also be encouraged by establishing process loading guidelines,
determining alternative ways of treating septage, by devising
methods of monitoring septage characteristics, and controlling
the rate and strength of septage input to plants.
Above all, communities need a basis for establishing hand-
ling and treatment charges. The widespread septage pollution of
land and water that now occurs can be greatly reduced if sewered
communities with treatment plants will accept septage from ad-
jacent non-sewered communities. Bases are needed to establish
equitable charges. Regulations are needed to facilitate plant
use, where applicable, and to discourage contamination of our en-
vironment.
THE SCOPE OF THIS RESEARCH
This research provides information needed to facilitate the
treatment of septage at municipal treatment plants. It assesses
the effects of septage addition to full and pilot scale plants,
including the impact of various loading methods and loading
levels on unit process performance and effluent quality. Oper-
ating procedures, difficulties and costs are examined. Guide-
lines are recommended for septage loading rates, plant opera-
tion control strategies, designing septage receiving and hand-
ling facilities?1 and regulatory procedures for septage disposal.
Whitman and Howard, Inc., "A Study of Waste and Septic Tank
Sludge* Disposal in Massachusetts", a report for Massachusetts
DEQE, December, 1976.
2
U.S. EPA, "Municipal Wastewater Treatment Facilities in New
England", Region 1, July 1977.
-------
SEPTAGE CHARACTERISTICS AND QUANTITIES
In 1977, EPA reported over seventeen million on-site waste-
water disposal systems in use, nearly 25 percent of all house-
holds in the United States. These systems predominate in sub-
urban and rural areas of New England, the Pacific Northwest, and
in some southeastern states. Estimates of the total quantity of
septage pumped yearly, based upon average tank pumping frequency,
or treatment plant and pumper surveys, reveal the magnitude of
this regional problem. It is obvious that immense quantities
of septage are generated yearly and that a high percentage of
this potentially hazardous waste is discharged directly to the
environment.
Septage consists of the mat of grease and scum on the sur-
face of septic tanks, the accumulated sludge at the bottom of
tanks and the sewage present at the time of pumping. Organic
solids and nutrient concentration are a function of the relative
proportion of sludge and supernatant. The fraction of each
component is determined by the interval between pumping and the
quantity and characteristics of the waste discharged. Septage
solids and organic concentrations can vary over three orders of
magnitude. Commercial and industrial septage, that is typically
hauled with domestic septage, increases this variability, and
may contribute particular contaminants in concentration suffi-
cient to inhibit or upset biological processes. Quality charac-
teristic variability has often been stressed in literature
dealing with septage; but for practical purposes, variability at
municipal plants is significant only when viewed in terms of
the holding capacity at inlet works and the size of plant pro-
cesses, both of which tend to attenuate the effects of a single
concentrated load.
During the course of this study, approximately 2,160 cu m
(570,000 gals) of septage were added to the treatment plants.
Septage was analyzed throughout the study. Samples were collect-
ed from individual trucks and from storage tanks containing up
to 254 cu-m (67,000 gals) of the waste. Table 2 shows an esti-
mate of average concentration based upon the results of all
analyses. These estimates are compared in Table 2 with values
published by EPA. Other estimates are readily available. &
I. A. Cooper and J. W. Rezek, "Septage Treatment and Disposal" ,
prepared for U.S. EPA, 1977.
A. J. Condren, "Pilot Scale Evaluations of Septage Treatment
Alternatives", U. S. EPA, EPA-600/2-78-164, September 1978.
-------
TABLE 2. SEPTAGE CHARACTERISTICS (mg/1)
1 .-,..., . . I . .-" ^— _— — — —
Total Solids
Total Volatile Solids
Total Suspended Solids
Volatile Susp. Solids
BOD5
COD
Total Organic Carbon
Total Kjeldahl-N
Ammonia-N
Total Phosphorus
Alkalinity, CaCO-
Grease
pH
LAS
Metals
Aluminum
Arsenic
Cadmium
Chromium
Copper
Iron
Mercury
Manganese
Nickel
Lead
Selenium
Zinc
Average values
this study
11,600
8,170
9,500
7,650
5,890
19,500
410
100
190
610
3,850
6.5
0.1
0.6
87
0.4
2
9.7
EPA average
concentration
38,800
25,260
13,000
8,720
5,000
42,850
9,930
677
157
253
9,090
6.9
157
48
0.16
0.71
1.07
6.4
205
0.28
5.02
0.9
8.4
0.076
49
-------
In many respects, septage is a waste similar in character-
istics to sewage, but more highly concentrated. Due to these
similar characteristics, the effects of septage upon a plant are
predictable. For example, design parameters, such as air re-
quirements and solids production, can be estimated. However,
when considering the design of inlet works, screens, pumps and
conduits throughout a plant, septage is distinctly dissimilar to
sewage. The waste is anaerobic and odoriferous. It contains
hair, plastic material and grit that clog and wear pumps and
conduits. Unclogging pumps, air draft tubes and screens pro-
duces operational problems and is time-consuming. Personal con-
tact with septage, for maintenance purposes, is highly objection-
able—a fact the design engineer must be aware of.
-------
SECTION 2
CONCLUSIONS
SEPTAGE TREATABILITY
Treatment with Sewage at Municipal Plants
Septage is readily treated biologically when combined with
domestic sewage. Microbial cultures found in conventional
activated sludge and extended aeration processes are well adapted
for rapid assimilation of septage organics. Microbiological
examination of mixed liquor, dissolved oxygen uptake measure-
ments and effluent monitoring have shown conclusively that sep-
tage is effectively oxidized when processes are loaded within
design capacities.
Septage is about 50 times as concentrated as domestic
sewage. A constant 2% addition of septage approximately doubles
the organic input to an aeration basin at an extended aeration
facility or doubles the solids loading on a primary clarifier at
a conventional activated sludge facility. Secondary aeration
basins at conventional plants receive about one fifth of the in-
fluent septage organic loading since the major fraction of or-
ganics in septage is usually associated with suspended solids,
which are effectively removed in primary clarification.
Nutrient:carbon ratios are lower for septage than for sewage,
but septage provides adequate nutrients for biological oxidation.
The obvious variability of domestic septage chemical char-
acteristics is not overly critical at municipal treatment facili-
ties where storage and dilution tend to attenuate the impact of
a single concentrated truckload.
Without the addition of chemicals septage dewaters slowly
and cannot be processed on a vacuum filter. This study has
shown that a secondary sludge, derived from a combination of
sewage and septage, vacuum.-filtered well with the addition of
polymer. A secondary sludge derived from sewage and septage
combined with primary sludge, containing septage also dewatered
well on a vacuum filter with the addition of lime.
-------
Recommended Septage Loading
The quantity of septage that a wastewater treatment facility-
can handle is normally limited only by available aeration and/or
solids handling capacity. Aeration capacity is most critical at
extended aeration plants where the entire quantity of septage
undergoes oxidation. Solids dewatering and disposal facilities
are often taxed at existing plants but where capacity exists it
can be well utilized for septage disposal.
An existing extended aeration facility that is loaded with
sewage to 25% of its design capacity can reasonably be expected
to take a 3% (by volume) addition of septage; a plant loaded to
50% can handle about 2%. At 75% capacity the recommended sep-
tage loading is 1%. These estimates are for constant septage
addition or frequent periodic additions, i.e., every hour or
half hour. Loading up to and exceeding 5% of the sewage flow
is possible if an extended aeration plant has adequate aeration
capacity or is provided with excess capacity specifically for
septage.
When septage is fed to aeration basins in slug loads as it
is received, the loading limit should be about half of the
values suggested for constant loading. Obviously, experience
at existing facilities is the best measure of available capacity.
for septage loading.
While there are definite advantages to feeding septage to
extended aeration plants at constant rates, this method of
addition-may not be necessary at conventional activated sludge
plants because primary clarifiers function well with either con-
stant or shock loading. The method of feeding septage to plants
does not affect dewatering processes.
DESIGN PARAMETERS FOR NEW FACILITIES
Dissolved Oxygen
The design of aeration facilities for extended aeration and
activated sludge plants can be based upon combined sewage and
septage COD or BOD input to the secondary process. Average
sewage and septage characteristics should be used for design.
Oxygen transfer efficiency and oxygen utilization estimates
should be selected from within the range Of conventional values
for the specific process used.
Oxygen utilization for septage fed at constant rates in
this study averaged 0.7kg 02/kg BOD5 and 0.3 kg 02/kg COD.
Oxygen transfer was about the same with or without septage addi-
tion—about 1.3 kg 02/kw h (2.2 Ib/hp-h). Generally, increasing
-------
organic loading by adding septage depresses dissolved oxygen
levels in an aeration process, which in turn increases the
efficiency of oxygen transfer.
Nitrogen
Nitrification and denitrification monitored during the
course of this research were caused by both organic loading and
mixed liquor dissolved oxygen concentration. Without the addi-
tion of septage the Medfield treatment plant normally converts
ammonia to nitrate in the first aeration basin. Denitrification
occurs in the remaining aeration basins which usually carry
little dissolved oxygen. Increased organic loading derived from
septage inhibited nitrification in the first basin. Absence of
dissolved oxygen in the remaining basins resulted in high-
ammonia concentrations in secondary effluent. When dissolved
oxygen levels were increased in the second basin nitrification
was again complete and denitrification followed in the remaining
two basins.
Sludge Production
Thickener and vacuum filter design for extended aeration
and conventional activated sludge plants can be based upon total
anticipated solids in the combined influent sewage and septage.
A reasonable estimate is to assume the septage solids contri-
bution at 50 times that of an equivalent volume of raw sewage.
In the course of this study, dewatering was monitored for
secondary sludge derived from septage and sewage at Medfield,
and a combination of primary sludge containing septage and
secondary sludge derived from septage and sewage at Marlborough.
In each case septage solids were equal to or exceeded the sewage
contribution. Septage did not affect dewatering either by
changing the cake or filtrate characteristics or by requiring
process changes. Chemical conditioners were fed on the basis
of dewatering process influent solids quantity, irrespective of
whether the solids were derived from sewage or septage.
Handling and Receiving
Septage can contain hair, grit, and stringy and plastic
materials. It is highly odoriferous and a health hazard. Odors
permeate clothing and body tissue. This combination of physical
characteristics make septage a particularly difficult material
to feed at controlled rates, to screen or to pass through small
size conduits and pumps.
Controlled septage feeding requires storage facilities and
hydraulic transmission systems. While constant feeding or feed-
ing at selected times has distinct advantages, particularly
10
-------
at extended aeration facilities, there are inherent practical
problems. These can be eliminated only through careful design
that considers the nature of septage.
There are practical advantages to having receiving stations
at municipal plants designed specifically for septage addition.
Holding-tanks permit flexibility in process feeding and pro-
cesses selection. Septage odors can be controlled, grit can be
removed and separate treatment provided when desired.
A possible receiving system would consist of an enclosed
aerated grit chamber with sludge removal and odor control equip-
ment. Provision should be made for bleeding sewage through the'
chamber for continuous septage displacement. Conduit size
should be equal to or in excess of 15 cm (6 inches) for septage
transfer.
COSTS
Cost of Septage Treatment
Septage treatment costs can be divided into three cate-
gories: capital equipment, operation and maintenance, and dis-
posal site acquisition. Capital and operation costs are mini-
mized by expeditiously moving septage to dewatering processes.
Capital costs are site specific but generally involve the cost
of solids handling equipment, designed on a solids basis, and
aeration facilities, based upon organic loading. Receiving
station costs would be comparable with conventional aerated grit
chamber costs plus the cost of an enclosed receiving area and
pumps if needed.
Operation and maintenance costs for septage addition are
largely dependent upon whether or not a plant has primary
clarification and the economics of scale. For example, the
operation and maintenance cost of treating septage at Medfield
was between $2 and $3/cu m ($8 and $12/1000 gal). This 5,700
cu m/day (1.5 mgd) plant had a sewage input averaging 1,040 cu
m/day (0.28 mgd) and was operated as an extended aeration facil-
ity.
Processes in use at Marlborough were loaded to full capa-
city at 12,100 cu m/day (3.3 mgd) and septage cost about $0.54/
cu m ($2/1000 gal). Septage loading was 2% in both cases. The
cost difference was due to the high power cost of oxidizing
septage organics at Medfield and the economic advantages in-
herent at the larger plant.
11
-------
SECTION 3
EXPERIMENTAL FACILITIES
MEDFIELD WASTEWATER TREATMENT PLANT
Septage addition was monitored at three wastewater treat-
ment plants: Medfield, Marlborough, and a University-operated
pilot plant. The Medfield treatment plant is a new conventional
activated sludge facility incorporating primary and secondary
treatment, tertiary sand filtration, solids thickening, and
vacuum filtration. Medfield is characteristic of new treatment
plants that receive only a fraction of their design sewage flow,
and accept septage. As a result of low sewage flow, this plant
is operated in an extended aeration mode. As sewers replace
septic tanks in the community, sewage flow will increase and
septage input will decline, unless septage is accepted from ad-
jacent communities. During the sewer construction period, the
plant is accepting the contents of abandoned systems in addition
to routine pumpage. The Medfield plant does not, at present,
accept septage from adjacent communities, although there is
expressed interest in doing so. Establishing an equitable price
for deliveries has been a deterrent.
Figure 1 is a schematic diagram of the Medfield facility.
Process units in use during this monitoring study are indicated
with bold lines. In-coming sewage was screened in the intake
structure and pumped to one compartment of the dual-compartment-
ed aerated grit chamber. The other compartment was used during
this study to store and feed septage. Sewage and septage com-
bined in a channel that separates the two chambers, and the mix-
ture flowed through conduits to aeration basin 1. The primary
settling tanks are bypassed in the extended aeration mode of
operation. One of the primary tanks was used for septage
storage.
Four of the six aeration tank sections were in use during
monitoring. Basin 1 received sewage and septage from the grit
chambers and sludge returned from the secondary clarifier.
Wastewater flowed from basin 1 to basin 2, and sequentially
through 3 and 4 to a single secondary clarifier.
12
-------
Pti
H
OS,
%*
u
CHLORINE CONTACT
t
I
o
o
i D
I
K
SAND FILTER
1
S t
r
SEWAGE
SCREENS
SAMPLING LOCATIONS
SECONDARY
CLARIFIER
SLUDGE
HOLDING
*" "^"
M I
4
1 ' THICKENERS
I
L _^- J
AERATION
1
1*
4*
3.
2
|
B
AERATED
GRIT
PRIMARY
SETTLING
Figure 1. Process schematic for the Medfield plant,
13
-------
Sludge collected at the bottom of the secondary clarifier
was lifted through four draft tubes and held in the equalizing
chamber located adjacent to the return sludge pumping station.
The sludge was either returned to aeration basin 1 or pumped to
one of two flotation thickeners. Thickened sludge was vacuum
filtered and land-filled on property adjacent to the plant.
Process dimensions are summarized in Table 3, and listed in de-
tail in Appendix A-l.
TABLE 3. MEDFIELD TREATMENT PLANT PROCESS DIMENSIONS
Design flow rate: 0.066 cu m/sec (1.5 mgd)
Average flow during test period: 0.012 cu m/sec (0.28 mgd)
Aerated Grit Chamber
Volume: 56.8 cu m (2,005 cu ft) (15,000 gals)
Detention time during test period: 1.29 hrs
Detention time at design flow: 0.48 hrs
Aeration Tanks
Number of compartments in use: 4
Compartment volume: 302 cu m (10,800 cu ft) (80,800 gals)
Detention time during test period: 7.08 hrs/compartment
Detention time at design flow: 1.29 hrs/compartment
Final Clarifier
Surface area: 117 sq m(l,257 sq ft)
Volume: 316 cu m (11,310 cu ft) (84,600 gals)
Detention time during test period: 7.25 hrs
Detention time at design flow: 2.71 hrs
Overflow rate during test period: 8.87 cu m/sq m-day (219 gpd/
sq ft)
Overflow rate at design flow: 24.4 cu m/sq m-day (602 gpd/sq ft)
MARLBOROUGH EASTERLY WASTEWATER TREATMENT PLANT
The Marlborough Easterly plant is a 20,800 cu m/day (5.5
mgd), two-stage activated sludge process, incorporating nitri-
fication and phosphorous removal. Figure 2 is a schematic dia-
gram of the treatment plant, with the processes in operation
during monitoring indicated with bold lines.
Raw sewage passes through one compartment of a dual-com-
partmented aerated grit chamber and flows to a distribution
box, where it combines with waste-activated sludge and septage.
The combined flow is discharged to a single primary clarifier.
14
-------
SECONDARY
CLARIFIERS
•m—*•
AERATION
AERATED f
GRIT U
CHAMBERS \
SEPTAGE
STORAGE
18
H
tf
PRIMARY
CLARIFIERS
I
1 FIRST STAGE
I
I
I
BASINS X""X
?rvH
RETURN |
"
L
WASTE SLUDGE
T
W I O
EH I O
W 4 D
SECOND STAGE
FINAL
CLARIFIERS
VACUUM FILTERS
SAMPLING LOCATIONS
Figure 2. Process schematic for the Marlborough Easterly
treatment plant.
15
-------
The plant consists of two parallel process trains with facility
for crossover at every process. During monitoring, half of the
available treatment units were in use for a flow slightly great-
er than one-half of the plant design capacity. This enabled
process loading essentially at design capacities. Process
loading characteristics and capacities are shown in Table 4.
Dimensions are shown in detail in Appendix A-2.
TABLE 4. MARLBOROUGH TREATMENT PLANT PROCESS DIMENSIONS
Design flow rate: 0.24 cu m/sec (5.5 mgd)
Average flow during test period: 0.14 cu m/sec (3.3 mgd)
Aerated Grit Chamber
Volume: 62.1 cu m(2,194 cu ft) (16,400 gals)
Detention time during test period: 0.12 hrs
Detention time at design flow: 0.14 hrs
Storage Tanks
Volume: 254 cu m (8,957Cu ft) (67,000 gals)
Primary Settling Tanks
Surface area: 356 sq m (3,848 sq ft)
Volume: 1,318 cu m (46,180 cu ft) (345,440 gals)
Detention time during test period: 2.51 hrs
Detention time at design flow: 3.01 hrs
Overflow rate during test period: 35.1 cu m/sq m-day
(857 gpd/sq ft)
Overflow rate at design flow: 29.1 cu m/sq m-day
(715 gpd/sq ft)
Aeration Tanks - First Stage
-------
TABLE 4. (continued)
Aeration Tanks - Second Stage
Number of units in use: 1
Unit volume: 2,178 cu m (76,800 cu ft) (574,465 gals)
Detention time during test period: 4.20 hrs
Detention time at design flow: 5.00 hrs
Nitrification Settling Tanks
Surface area: 468 sq m (5,027 sq ft)
Volume: 2,157 cum (76,200 cu ft) (570,000 gals)
Detention time during test period: 4.15 hrs
Detention time at design flow: 5.04 hrs
Overflow rate during test period: 13.4 cu m/sq m-day
(328 gpd/sq ft)
Overflow rate at design flow: 11.1 cu m/sq m-day (247 gpd/sq ft)
Plant laboratory data showed that the first stage at Marl-
borough normally reduces carbonaceous biochemical oxygen demand,
BOD5, from an average of 100 mg/1 to about 11 mg/1. The second
stage further reduces BODc to 2.6 mg/1 and converts about 15
mg/1 of ammonia nitrogen to nitrate nitrogen.
Primary and secondary sludges were wasted daily during the
course of the study. Sludge from the nitrification stage was
not wasted during the monitoring period. When secondary and
nitrification stage sludges are wasted they are returned to a
primary clarifier, combined with primary sludge and sent to a
vacuum filter. Ferric chloride and lime are used as sludge
conditioners.
UNIVERSITY OF LOWELL PILOT PLANT
The Department of Civil Engineering at the University of
Lowell operates a 30.3 cu m/day (8,000 gal/day) Davco extended
aeration package plant for research and instruction. The plant
is located on the University campus on the banks of the Merri-
mack River, near a 30 inch diameter brick combined sewer outfall.
The sewer serves several University dormitories, the student
union, a cafeteria, and a number of homes in Lowell. The process
is shown schematically in Figure 3, and operating parameters are
shown in Table 5. Sewage was pumped continuously from the out-
fall sewer to a weir box that provides the plant with a constant
inflow and returns excess flow back to the sewer, upstream of
the pump intake. Septage was continuously mixed in a tank and
fed by an airlift pump that was on a timed intermittent schedule.
The plant air system consists of a single air compressor which
17
-------
feeds four coarse bubble-diffusers in the aeration basin, and
provides air for sludge return, clarifier scum removal and _
septage feeding. Sludge wasting was monitored by pumping mixed
liquor from the aeration basin to a graduated waste-measurement
box.
RETURN SLUDGE
SEPTAGE
STORAGE
CLARIFIER
WASTE
MEASUREMENT
BOX
SEWER
SAMPLING LOCATIONS
Figure 3. Process schematic for the University of Lowell plant.
18
-------
TABLE 5. UNIVERSITY OF LOWELL PILOT PLANT PROCESS DIMENSIONS
Flow rate for extended aeration: 30.3 cu m/day (1,070 cu ft/day)
(8,000 gals/day)
Flow rate for conventional process: 109.0 cu m/day
(3,850 cu ft/day) (28,800 gals/day)
Aeration Tank
Volume: 30.2 cu m (1,070 cu ft) (8,000 gals)
Detention time extended aeration: 24 hrs
Detention time conventional process: 6.7 hrs
Settling Tank
Surface area: 5.9 sq m (63 sq ft)
Volume: 15.5 cu m (547 cu ft) (4,090 gals)
Detention time extended aeration: 12.3 hrs
Detention time conventional process: 3.4 hrs
Overflow rate extended aeration: 5.17 cu m/sq m-day
(127 gpd/sq ft)
Overflow rate conventional process: 18.6 cu m/sq m-day
(457 gpd/sq ft)
19
-------
SECTION 4
MONITORING PROGRAM
SUMMARY OF PROCEDURES
A three phase experimental program was conducted at each of
the three plants. Initially, plants were monitored seven days
per week for periods of two to three weeks without septage ad-
dition. During this first phase of the study, samples were
collected and laboratory tests performed, while incoming septage
was stored for later use. Phase 1 was designed to acquire a
data base prior to septage addition.
During the second stage of testing, septage was added at
constant rates for periods of several days to three weeks. The
objectives were to monitor process performance and effluent qual-
ity under various loading levels, and, if possible, to stress
the plants with large quantities of septage. The two municipal
plants were fed as much septage as could be obtained and stored.
The University plant was stressed to failure, both in the con-
tinuous loading Phase 2 and in the slug loading experiments con-
ducted under Phase 3. During Phase 3, Medfield and Marlborough
were slug-loaded daily for a series of two to four day periods.
Composite and grab samples were collected at locations in
the plants on daily, biweekly, and weekly schedules. Sampling
locations were set and analysis schedules were designed to
follow solids, organics, nitrogen, phosphorus and other consti-
tuents through the plants.
Table 6 summarizes chemical analyses performed at the Uni-
versity of Lowell laboratory, and, when appropriate, at sampling
locations at the three wastewater treatment plants. The table
is a general overview of the analytical work; individual ana-
lytical results are given in the appendices. Sampling points
at each plant are shown in Figures 1, 2, and 3. The analytical
methods used are summarized in Table 7.
MONITORING PROGRAM AT MEDFIELD
Table 8 is a summary of tests conducted at Medfield during
the fall of 1977. The daily routine at Medfield during Phase 1
consisted of obtaining plant operating data for the preceding
20
-------
TABLE 6. SCHEDULE OF SAMPLES AND ANALYSES
Plant
Medfield
Marlborough
U. of Lowell
Sample Frequency
Daily (D)
Semi-weekly (SW)
Weekly (W)
Type of Sample
Composite (C)
Grab (G)
Analyses
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile
Solids
Suspended Solids
-P
G
0)
d
rH
m
G
H
X
X
X
D
C
X
X
X
X
X
X
X
0)
rc$
.p
Q.
0
CO
X
X
X
D
G
X
X
X
X
X
X
ry Effluent
(0
e
-H
M
P-i
X
D
C
X
X
X
X
X
X
X
dary Effluent
£
o
o
(L)
U2
X
X
X
D
C
X
X
X
X
X
X
X
4->
G
Q)
d
H 0)
m M tn
m o T3 -p
W d d c
>i -H co oj 4J cu
nJ G (U G CU fq
X
X
D
W
G
X
X
X
X
X
X
X
(U
fd
u
X
X
D
W
G
X
X
Volatile Susp.
Solids
X XX X X X X
(continued)
X
X
21
-------
TABLE 6. (continued)
Ammonia-N
Nitrate-N
Total Kjeldahl N
Total Phosphorus
Grease
pH
Temperature
Alkalinity
Dissolved Oxygen
D.O. Uptake
Settlometer
Capillary Suction
Time
Turbidity
Metals
0)
rH
4-1
H
X
X
X
X
X
X
X
X
X
X
OJ
tn
rd
4->
CD
CO
X
X
X
X
X
X
X
X
iittary Effluent
j_i
PH
X
X
X
X
X
X
X
X
X
X
condary Effluent
0)
CO
X
X
X
X
X
X
X
X
X
X
X
rtiary Effluent
0)
E-i
X
X
X
X
X
X
X
X
X
X
X
J-l
o
D1
-H
CD
X
s
X
X
X
X
X
X
X
X
X
Q) SH
jji CU
t3 4-) 4->
rH M (0 TZi "rl
CO CD 4J 0) Cm CD
d fd a -P
t_i ^/ ^_i K/l ^J*| rj ^_j
3 OCD UTi 34-1
4J -rl fli -r| 3 U rH X
rjj ,£3 XlH rO-H rd
rt E-iCO EHCO >fa O
X X
X X
X XX
X
X X
X
X
X
X X
X XX
Oxidation Reduc-
tion Potential X
day, collecting samples, and conducting analyses. Influent and
effluent samplers (Isco Model 1680) composited four samples each
hour into a container. Quantities from each of the twenty-four •
containers were composited in a large container proportioned in
accordance with the recorded plant flow record. Grab samples of
mixed liquor and returned sludge were also taken daily. Cake,
thickened sludge, thickener and vacuum filter supernatant were
taken whenever the plant wasted solids, about once each week.
Samples were returned to the University laboratory within two
hours of collection.
22
-------
TABLE 7. ANALYTICAL PROCEDURES
Analyses
Std. Methods
Sect.*
EPA Tech.
Transfer Sect.**
Comments
COD-Total 508
COD-Soluble 508
BOD-Total 507
BOD-N Suppressed 507
Total Solids 208A
Total Volatile Solids 208E
Suspended Solids 208C
Volatile Susp. Solids 208E
Ammonia-N
Nitrate-N 419B
Total Kjeldahl-N 421
Total Phosphorus 425E
Grease
pH 424
Temperature 212
Alkalinity 403
Dissolved Oxygen 422F
D.O. Uptake 213B
Settlometer 213C
Capillary Suction Time
Turbidity 214A
ORP
Chromium 301A
Cadmium 301A
Copper 301A
Nitrate 301A
Lead 301A
Zinc 301A
00340
00340
00310
00310
00500
00505
00530
00535
00610
00625
00556
00400
00010
00410
00299
01034
01027
01042
01067
01051
01092
sample fil-
tered(0.45 Tim)
added 10 ml
of 3.0M
NH4C1 to
300 ml BOD
bottle
Orion Model
95-10
Orion Model
92-07
Persulfate
Digestion
Separatory
Funnel
Corning
YSI Model 54
Triton
Hach
Corning
*American Public Health Association, Standard Methods for the
•Examination of Water and Wastewater(Washington, D.C., 1976.)
**Environmental Protection Agency, Technology Transfer, Manual
of Methods for Chemical Analysis of Water'and Waste, \Lvi\) .
23
-------
TABLE 8. TEST PERIODS AND SEPTAGE LOADING AT MEDFIELD
Type of Consecutive
Phase Loading Loading Days*
Average
Septage Load-
Starting Completion ing - % of
Date Date Daily Flow
1
2A
3A
2B
3B
No Loading
Continuous
Shock
Continuous
Shock
3
7
4
- _-r -- _-_ . -*•__ r.
22
21
+ 2
+ 1
+ 1
8/22
9/13
10/14
11/1
11/14
9/12
10/3
10/18
11/8
11/18
2
1
3
2
0
.0
.8**
.8
.6**
* Indicates number of days septage fed plus the monitored
recovery period.
** Percent of average daily flow is shown. Shock loading
duration and application rates are detailed in the text,
Temperature, pH, and dissolved oxygen were measured at
sampling locations. Settlometer and dissolved oxygen uptake
tests were conducted in the plant laboratory.
The routine was continued during the continuous septage
feed study, Phase 2, with the addition of daily septage sampling
from the aerated grit chamber. Septage was also sampled as it
was discharged from hauling trucks in an effort to exert some '
control of septage solids and organic concentration.
A schematic of the septage feed system used at Medfield is
shown in Figure 4. Septage was discharged from haulers' trucks
to a screening box used to remove hair and plastic materials.
Screen wire was 2 inches on-center; anything less clogged with
hair from a single load. Vibrating screens were not available.
In Phase 2A screened septage was pumped from the aerated grit
chamber to a weir box on a 15 minute cycle. The pumping period
was about seven minutes. In Phase 2B the weir box was eliminated
and the cycle increased to 30 minutes. The quantity pumped from
the aerated grit chamber each day was determined by measuring
changes in liquid level.
During the first shock load test, Phase 3A, the drain plug
was pulled in the aerated grit chamber, sending 18.9 cu m
(5,000 gals) "of septage to the raw sewage lift station. This
was repeated on the second day, followed by 25.4 cu m (6,700
24
-------
'FP,
SEPTAGE
SEPTAGE
PUMP F
WEIR BOX
V
(.
OUTLET
CHANNEL
PHASE 2A
INLET
SEWER
SEWAGE
SEPTAGE
SEPTAGE
PUMP
i/OKVf
OUTLET
CHANNEL
PHASE 2B
INLET
SEWER
SEWAGE
Figure 4. Septage feed systems - Medfield.
gals) on the third day. The pumps returned the slugs of septage
to the 56.8 cu m (15,000 gals) aerated grit chamber compartment
containing sewage. The mixture was then displaced from the grit
chamber by incoming sewage over a period of about four hours.
The rate of septage input to aeration tank 1 based upon total
solids analyses during Phase 3A is shown in Figure 5. The total
solids curve is representative of septage displacement from the
aerated grit chamber to the aeration basins.
AM 10 AM 11 AM 12 NOON
TIME
1 PM
2 PM
Figure 5. Influent total solids - Medfield - Phase 3.
25
-------
During the second shock load test, Phase 3B, portable pumps
and a septage hauling truck were used to pump septage directly
from the septage compartment of the aerated grit chamber and
from the primary tank to the aeration tank inlet. The plant
was loaded on each of four successive days; 29.5 cu m (7,780
gals) on each of the first three days and 37.9 cu m (10,000
gals) on the fourth day.
MONITORING PROGRAM AT MARLBOROUGH
A three phase monitoring program was initiated at the Marl-
borough Easterly wastewater treatment plant during the spring
of 1978. The testing schedule is shown on Table 9. Monitoring
began after winter snow-melt when infiltration had subsided,
plant flows were down and septage deliveries on the upswing.
During Phase 1 the plant was monitored for 17 days without sep-
tage addition beginning on April 17. Composite samples of plant
influent, primary effluent, secondary effluent and final effluent
were collected for analyses every day during the period. Grab
samples of mixed liquor and returned sludge were also taken
daily from both the secondary treatment process (first stage)
and the nitrification process (second stage). Combined primary
and secondary sludge, and cake and vacuum filtrate were sampled
whenever the plant wasted solids.
TABLE 9. TEST PERIODS AND SEPTAGE LOADING AT MARLBOROUGH
Phase
Type of
Loading
Consecutive
Loading Days*
Starting
Date
Completion
Date
Average
Septage
Loading
% of Flow
1 No Loading 22
2A Continuous 3
2B Continuous 1,75
3A Shock 3 + 2
3B Shock 2+1
4/17
5/8
5/16
5/30
6/7
5/7
5/10
5/18
6/2
6/9
0
1.25
2,14
0.83
2.05
* Indicates number of days septage fed plus the monitored
recovery period.
During Phase 2 septage was fed continuously. Septage sam-
ples were collected daily, as were the composite and grab sam-
ples taken during Phase 1. An effort was made to obtain septage
samples that were representative of the entire mass of material
fed during a particular test, either by mixing holding tanks or
by sampling various locations in a tank.
26
-------
The septage storage and feed system used for continuous and
shock loading is shown on Figure 6. The system consisted of a
227 cu m (60,000 gal) storage basin that had been used as an
aeration basin for an old plant that previously existed on the
site. The aeration system was used to mix the septage. A
gasoline-motor-driven sludge pump was used to transfer septage
from storage to one 53 cu m (14,000 gal) aerated grit chamber
compartment. The plant grit chamber is a dual-compartmented
unit; one side is normally used as a septage receiving tank.
VALVE
SEPTAGE
WET
WELL
V
V
PRIMARY
CLARIFIER
TRANSFER
PUMP
Figure 6. Septage feed system - Marlborough.
Septage was discharged from the grit chamber to a manhole,
and from there to a 22.7 cu m (6,000 gal) wetwell adjacent to
the secondary clarifiers. The 15.2 cm (6 inch) wetwell centrif-
ugal pump was cycled on a time clock enabling controlled input
to the primary clarifier during Phase 2.
During the first continuous loading test, 110 cu m (29,000
gal) of septage were fed over a period of 24 hours. The wet-
well pump discharged 2.27 cu m (600 gal) in each cycle. It
cycled on for one minute every 30 minutes. Septage held in
storage and that provided by incoming trucks during this test
period enabled three days of continuous feeding. During the
second Phase 2 test, a high input by haulers plus accumulated
storage enabled feeding a total of 375 cu m (99,000 gal) over a
period of 42 hours. This was equivalent to feeding the plant a
truckload of septage every half hour, twenty-four hours per day
for close to a two day period.
27
-------
The first shock loading test began on May 30 and was re-
peated on the following three days. The entire contents of the
aerated grit chamber compartment, the transmission piping and
the wetwell, 79.5 cu m (21,000 gal) were discharged to the pri-
mary clarifier in a period of 30 minutes. During the second
test this was repeated on each of two days, but, in addition to
the 30 minute discharge of 79.5 cu m (21,000 gal), an added 68.1
cu m (18,000 gal) of septage was pumped at the same time from
storage. The pumped discharge took two hours. On the second
day of this test, an additional 45.4 cu m (12,000 gal) was also
fed during the afternoon. The last continuous and shock loadings
were the maximum loadings possible at the plant with available
storage and pumping facilities. These loadings far exceeded nor-
mal or potential input to the plant.
A principal objective at Marlborough was to determine the
effects of high level septage addition on primary clarification
and septage solids reduction in primary clarification. To ac-
complish this goal, primary clarifier samples were taken at a
mid-location near the surface, at mid-depth, near the bottom,
and at the effluent weir. Samples were initially collected at
one-half hour intervals, followed by longer intervals as the
effects of a shock load passed through the basin.
RESEARCH AT THE UNIVERSITY PILOT PLANT
Septage research at Lowell began during 1976 under a grant
from the Commonwealth of Massachusetts, Department of Environ-
mental Quality Engineering. The work was conducted at the Uni-
versity pilot plant which, at that time, was operated as an
extended aeration process. Continuous loading tests were con-
ducted with long aeration basin retention and high mixed liquor
solids concentration. This initial study has been combined with
this research, and the results of loading the extended aeration
process are given in subsequent sections of this report. The
test schedule is shown on Table 10. The sewage and septage feed
systems are shown on Figure 7.
During 1977 and 1978 the University plant was slug loaded
in the extended aeration mode of operation and was also operated
as a conventional facility, i.e., with an aeration basin reten-
tion period and mixed liquor solids concentration, akin to con-
ventional processes, but without primary clarification.
Extended Aeration Mode of Operation
Plant operation in the extended mode began by seeding with
22.7 cu m (6,000 gals) of mixed liquor obtained from the Bil-
lerica, Massachusetts extended aeration plant. The initial in-
fluent flow was 30.3 cu m (8,000 gals) per day.
28
-------
FEED
OVERFLOW
LGE
1
_^
' »-
»
N r
EFFLUENT &
WASTE SLUDGE
MANHOLE
S-^
SEPTAGE
FEED
(/SCREENS
',
III c
1,
i
OVER-
FLOW
r^
AIR
LIFT
*
•
4*
* f
• *
V
, i
* ^
*
*
9 J
' /»
*
•~N
DAM
-PUMP
SEWAGE FEED SYSTEM
SEPTAGE FEED SYSTEM
Figure 7. University of Lowell pilot plant feed systems.
After seven weeks of operation in this baseline mode, Phase
2 was begun and 75-7 liters/day (20 gals/day) of septage was
introduced to the plant. While feeding septage, mixed liquor
suspended solids, mixed liquor settleability, aeration basin
dissolved oxygen, and effluent COD values were determined. BOD
tests were run on influent, effluent, and septage samples.
Microscopic inspections were frequently performed on the mixed
liquor to determine sludge condition and to aid in operation.
Influent sewage samples were composited over 24 hour periods;
.all other samples were grab.
The septage feed rate was increased by steps and the pro-
cess allowed to stabilize at each selected feed rate. Process
stability was determined by effluent COD and turbidity and
sludge settleability. Increases were made over a five month
period in accordance with the schedule shown on Table 10.
Sludge was returned to the aeration tank at four times the
influent flow rate to minimize excessive retention in the
29
-------
TABLE 10. TEST PERIODS AND SEPTAGE LOADINGS
AT UNIVERSITY OF LOWELL PILOT PLANT
Phase Mode
3A
3B
1
2A
2B
3A
3B
Extended
Aeration
Extended
Aeration
Conventional
Conventional
Conventional
Conventional
Conventional
Type of
Loading
Shock
Shock
No loading
Continuous
Continuous
Shock
Shock
Consecutive
Loading Days*
3 + 2
3 + 2
17
12
6
3 + 2
2 + 2
Starting
Date
7/25
8/ 1
3/12
3/29
4/10
5/ 3
5/18
Septage
Loading
% of Flow
1.33
2.63
0
0.42
0.82
1.04
1.82
*Indicates number of days septage fed plus the monitored recovery
period.
clarifier. Sludge wasting was controlled by settleability.
Settling requirements limited mixed liquor suspended solids
concentration. As a result, F/M ratios rose with increasing
septage loading.
Two series of shock loadings were investigated in Phase
3: 1.3% and 2.6% of the total daily sewage flow rate. Each
series consisted of imposing the shock once a day for three
consecutive days and monitoring the recovery period for either
one or two days.
Conventional Mode of Operation
An approximation of conventional activated sludge operation
was studied by increasing the influent flow rate. The average
aeration basin detention time was just over six hours. At
the increased flow rate the final clarifier detention time,
about three hours, exceeded conventional operation.
Two periods of continuous loading were performed, followed
by two shock loading periods. Loadings are shown on Table
10.
Sewage pump failures occurred frequently prior to Phase
3, causing problems in the aeration tanks, which, in turn,
resulted in loss of the clarifier blanket during shock loading.
30
-------
SECTION 5
RESULTS AT MEDFIELD
PHASE 1 - BASELINE FOR COMPARISON
The first phase of research at Medfield provided a baseline
of information which was used to evaluate the effects of septage
addition. During this three week period, septage was withheld
from the, plant. Sewage flow was only 14% of the design flow
rate; aeration basin and final clarifier detention times were
long, and loading parameters were low. Low sewage loading en-
abled large inputs of septage during subsequent phases of the
research in contrast with the experiments at Marlborough,
where the plant was fully loaded prior to septage addition.
Process Characteristics
Solids concentration in the aeration tanks at Medfield are
normally maintained at comparatively high levels. As a result,
the mean cell residence time, SRT (total microbial mass/rate of
withdrawal) is considerably longer than the 20 to 30 day periods
generally used for extended aeration plant design. Mean cell
residence time and various other process parameters which charac-
terize the operation at Medfield during Phase 1 are shown on
Table 11. For comparison, design parameters commonly used for
extended aeration process design are also included on this
table.
The combined effects of high mixed liquor solids concentra-
tion and low organic input are expressed in the food-to-micro-
organism ratio, F/M, which.at 0.018 kg BODs/kg MLVSS-day is con-
siderably below the range normally experienced at extended
aeration plants. High oxygen utilization, 4.5 kg 02/kg BOD5
(Ib 02/lb BODc) is also a result of low organic loading and the
basal metabolism requirements of the large mass of organisms
maintained under aeration.
During Phase 1 the plant operated well along the endogenous
respiration phase of the growth curve. Rotifers and ciliates
were in abundance.
Metcalf and Eddy, Inc. Wastewater Engineering, McGraw Hill,
New York, 1972, pg. 498.
31
-------
TABLE 11. PROCESS CHARACTERISTICS - MEDFIELD PHASE 1
Characteristic
Phase 1
Average Values
Design Parameters
Used for Extended
Aeration Process*
Flow Rate, Q, cu m/sec (mgd)
Sludge Return Rate, Qr,
cu m/sec (mgd)
Qr/Q
Aeration Basin Retention, hrs
Mixed Liquor Volatile Susp-
Solids, mg/1
Mixed Liquor Volatile Susp.
Solids, mg/1
F/M, kg BOD5/kg MLVSS-day
Loading, gm BOD^/cu m-day
(Ib BOD/1000 cu ft-day)
Mean Cell Residence, SRT, days
0,009 (.206)
0.018 (.420)
2,0
37.6
7580
4570
0.018
83.3(5.2)
88
0.75-1.5
18-36
0.05-0.15
160-400(10-25)
20-30
Oxygen Utilization, kg 02/kg BOD 4.5
Oxygen Utilization, kg 0_/kg COD 2.2
*Metcalf and Eddy, Inc., Wastewater Engineering (New York:
McGraw-Hill, 1972):498.
Influent Wastewater Characteristics
Characteristics of raw sewage sampled and analyzed during
Phase 1 are shown on Table 12. The analytical results depict a
typical residential community discharge, devoid of industrial
wastes, but with some ground and surface water infiltration.
The organic, solids, nitrogen and phosphorus concentrations
shown in Table 12 characterize the plant influent as weak domes-
tic sewage.6 Standard deviations shown in Table 12 indicate
variability in composite samples. The total average daily input
to the plant during Phase 1 was 110 kg (242 Ib) of organic mater-
ial expressed as BOD^ or 215 kg (474 Ib) expressed as total COD.
Daily total solids and total volatile solids input were 348 kg
(766 Ib) and 144 kg (318 Ib), respectively.
Metcalf and Eddy, Inc. Wastewater Engineering, McGraw Hill,
New York, 1972, pg. 231.
32
-------
TABLE 12. INFLUENT, EFFLUENT, THICKENER SUPERNATANT
AND VACUUM FILTRATE CHARACTERISTICS - MEDFIELD - PHASE 1
x = Mean Values
s = Standard Deviations
Characteristics Influent
COD-Total, mg/1
COD-Soluble, mg/1
BOD5-Total, mg/1
BOD5-N Suppressed,
mg/1
TOC, mg/1
Total Solids, mg/1
Total Volatile
Solids, mg/1
Suspended Solids,
mg/1
Volatile Susp.
Solids, mg/1
Total Kjeldahl-N,
mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus,
mg/1
Grease, mg/1
PH
Temperature , C
Alkalinity, mg/1
as CaC03
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
X
276
87
141
93
75
446
185
108
85
26
13
0
10.6
74
7.1
18
136
0.04
0.20
0.13
0.10
0.59
0.37
s
78
23
22
24
.10
64
43
56
48
3.3
1.7
0
3.7
72
0.2
1.0
11.6
0.02
0.28
0.03
0.04
0.10
0.28
Vacuum
Thickener Filter
Effluent Supernatant Filtrate
X
19
17
3.6
1
13
336
78
4.0
2.8
0.2
7.2
0,7
4.5
7.3
19
0.03
0.15
0.06
0.10
0-15
0.22
S X S
6,1 26 4.4
5.8
2.2 4.4 3.7
0,6 0,7
16 12 3.5
27 329 20
25 71 12
1.8 1 1.9
1.5 1 1.9
0.2
0.7
0.1
0.7
0.1
1.5
0.03 0.03 0.03
0.14 0.01 0.02
0.01 0.07 0.03
0.07 0.09 0.01
0.09 0-45 0.53
0.19 0.23 0.22
X
358
120
101
91
768
381
83
55
0.02
0.08
0.15
0.10
0-23
1.31
s
118
19
114
84
26
19
0-03
0.08
0.04
0.09
0-20
1.40
33
-------
Effluent Quality Prior to Septage Addition
Medfield produces an exceptionally clear, low solids, low
BOD5 effluent. Average characteristics of secondary effluent
produced by the plant are shown on Table 12. The tabulated
values reflect effluent quality prior to tertiary sand filtra-
tion and chlorination. During Phase 1 the plant removed 97%
of the influent BOD5, 93% of the COD, and 96% of the suspended
solids. Effluent quality and plant performance were exemplary.
Sodium aluminate is added prior to final clarification for
phosphorus removal. Total phosphorus concentrations are normally
kept below 1 mg/1, in accordance with regulatory requirements,
and, during Phase 1, averaged 0.7 mg/1.
Heavy metal concentrations in effluent wastewater were be-
low influent levels, and were consistent with metal quantities
incorporated into the vacuum filter cake. (Table 12).
Effluent and influent metal concentrations were within recommend-
ed drinking water standards.
Figure 8 shows low ammonia-N levels during the entire Phase
1 period. The ammonia nitrogen curve indicates that ammonia was
completely converted to nitrates during the no-septage load per-
iod, except for a slight increase in ammonia concentration during
the brief initial period, when the remnants of a clean-out oper-
ation were still in the system. Several days before the Phase 1
study was initiated, septage stored in the plant aerated grit
chamber was fed to the plant. Complete conversion of ammonia to
nitrate is expected in a system carrying 4,570 mg/1 of mixed
liquor volatile suspended solids, with an 88 day cell residence
time. Under these conditions the growth rate of heterotrophic
organisms is comparatively low, below the maximum growth rate
of autotrophic nitrifying bacteria. This enabled the existence
of nitrifiers in sufficient concentration to completely oxidize
ammonia in the wastewater. As a comparison, treating an influ-
ent containing 26 mg/1 of total kjeldahl nitrogen in a carbon
oxidation-nitrification system (single stage activated sludge
or extended aeration), ammonia break-through in the effluent
would be expected when the cell residence time is reduced to
about 5 days. "7 The growth rate of Nitrosomonas and the extent
of nitrification in a system is dependent not only upon the
growth rate of heterotrophic organisms, but also upon environ-
mental factors—principally, dissolved oxygen, pH, temperature
and alkalinity. During the entire monitoring period at Medfield,
pH remained between 6.8 and 7.2, and temperature averaged 19°C.
These conditions are excellent for growth. Alkalinity in the
Process Design Manual for Nitrogen Control, U.S. Environmental
Protection Agency, Technology Transfer, 1975, pp. 3-17.
34
-------
•N
Z
o
u>
o
I 1 I I I i , !
RETURN SLUDGE WASTED
DISSOLVED OXYGEN
BASIN 2
23 2k 25
26 27 28 29 30 31
AUGUST 1977
4567
SEPTEMBER 1977
9 10 11 12
DATE
Figure 8. Effluent nitrogen and Basin 2 dissolved oxygen - Medfield - Phase 1.
-------
influent wastewater was always sufficient for the synthesis of
bacterial cells. However, dissolved oxygen in the aeration ba-
sins and the final clarifier were quite low—often well below
2 mg/1. Septage addition prior to the initiation of Phase 1 may
have depressed dissolved oxygen levels sufficiently for the
slight rise in ammonia shown in Figure 8 between August 24 and
August 28. Dissolved oxygen, pH, temperature, and alkalinity
values are shown on Appendix Table B-3.
The effect of dissolved oxygen on nitrification has been
modeled using the Monod relationship:
DO
K
'O,
DO
where y = Nitrosomonas growth rate, day
-1
-1
y = peak Nitrosomonas growth rate, day
DO = dissolved oxygen, mg/1
K = half-saturation constant for oxygen, mg/1
2
With a value of 1.3 assumed for Ko28, the rate of ammonia con-
version would be 43% of the peak rate at 1 mg/1, and 28% and 13%
at 0.5 mg/1 and 0.2 mg/1, respectively.
The following equation for bacterial synthesis and ammonia
oxidation shows the relative quantities of ammonia converted
either to nitrifiers or oxidized to nitrates:
+ 1.8302 + 1.98HC03 -»•
0.98NO" + ]
1.041H20
The equation shows the relative unimportance of autotrophic
synthesis in removing ammonia from a system. However, hetero-
trophic synthesis utilizes considerably more nitrogen. Cell
yield (kg of mixed liquor volatile suspended solids produced un-
der aeration per kg of 6005 removed) averaged 0.4 during Phase
1. This value is based upon BOD,- reductions from 141 mg/1 in
the influent to 4 mg/1 in the secondary effluent, and sludge
production equal to 43 kg/day (95 Ib/day) on a dry weight basis.
Process Design Manual for Nitrogen Control, U.S. Environmental
Protection Agency, Technology Transfer, 1975, pp. 3-12.
36
-------
assuming cell nitrogen content equal to 14%9/ nitrogen incor-
porations into heterotrophic cells would utilize 7.7 mg/1 of
available ammonia nitrogen from solution. Clearly, the fate of
the remaining 15 to 18 mg/1 of ammonia removed during Stage 1
was a transformation to nitrates.
Denitrification routinely occurs at Medfield and is asso-
ciated with low dissolved oxygen in the aeration tanks and the
final clarifier. Figure 8 shows nitrate nitrogen increasing
from negligible concentrations at the initiation of testing to
about 2 mg/1 at the end of a week, increasing rapidly to 8 mg/1
in a three day period, followed by values between 6 mg/1 and
8 mg/1 for the balance of the period. Increases in the conver-
sion of nitrates to nitrogen gas and subsequent loss to the at-
mosphere generally coincides with decreasing dissolved oxygen
levels. A comparison of dissolved oxygen levels in basin 2 and
nitrate levels in the effluent shows this relationship.
A year after the completion of Phase 1 at Medfield, the
plant was revisited on July 24, 1978. Nitrate concentrations
were measured in three aeration basin compartments and in the
final clarifier. The effluent NO3-N concentration from basins 1,
2 and 4 were 3.6 mg/1, 1.5 mg/1 and 0.65 mg/1, respectively.
Dissolved oxygen levels in basins 2, 3 and 4 were between 0.8
and 1.5 mg/1 near the surface, and essentially absent near the
bottom of the tanks. Water temperature and plant loading were
about the same as during Phase 1. Clearly, the plant nitrifies
in the first aeration basin and denitrifies to some extent in
the remainder of the basins.
Mixed Liquor and Secondary Sludge
Average mixed liquor characteristics, x, are shown in Table
13. Standard deviations, s, in recorded data are also listed.
High total solids concentrations maintained during Phase 1 and
throughout the experimental period at Medfield caused nitrifi-
cation and denitrification, by reducing the heterotrophic growth
rate, and by keeping mixed liquor oxygen levels low.
Dissolved oxygen uptake was determined on samples taken
from basin 3, chosen as an average value location. Low measured
uptake values, an average of 15 mg/l/hr, were a result of the low
F/M ratio. A disadvantage of maintaining high mixed liquor
solids was increased air requirements. However, the two speed
surface aerators used at Medfield give little flexibility for
reducing aerator power consumption.
9Schroeder, Edward D., Water and Wastewater Treatment, McGraw
Hill, Inc., New York, 1977, pg. 182.
37
-------
TABLE 13. MIXED LIQUOR AND SECONDARY SLUDGE CHARACTERISTICS
MEDFIELD - PHASE
Characteristic
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Suspended Solids, mg/1
PH
Temperature, °C
Alkalinity, mg/1 as CaCO^
D.O. Uptake, mg/l-hr
Dissolved Oxygen Basin #1, mg/1
Dissolved Oxygen Basin #2, mg/1
Dissolved Oxygen Basin #3, mg/1
Dissolved Oxygen Basin #4, mg/1
Dissolved Oxygen Clarifier, mg/1
Settlometer, 30 min
Capillary Suction Time, sec
Mixed
Liquor
X
7910
4670
7580
4570
7.0
20
241
15.0
4.7
1.2
1.0
1.0
1.2
695
s
263
219
271
214
.11
1.2
34
5.5
1.2
0.6
0.6
0.6
0.6
71
Secondary
Sludge
x s
9830 1979
5850 1262
803 47
9.1 0.6
Settlometer test results are given in Appendix Table B-3.
Samples for this analysis were taken from the end of aeration
basin 4. Only small variations in values were observed during
Phase 1. The mixed liquor settled slowly, sweeping material
from suspension, and producing a clear supernatant.
Secondary clarifier sludge was returned to aeration basin 1
at an average rate of 0.018 cu m/sec (0.42 mgd) or twice the
average influent flow rate. At this high return rate, solids
buildup was minimal in the clarifier; total solids in the return
sludge averaged 9,830 mg/1. While this value is comparatively
high for extended aeration plant operation, it is not much
greater than the mixed liquor concentration.
Sludge Dewatering
Thickener supernatant and vacuum filter filtrate were re-
turned to the head end of the plant weekly during Phase 1. Chem-
ical characteristics of these liquids are shown on Table 12.
The thickener produced an extremely high quality supernatant.
38
-------
Filtrate from the vacuum filter was high in organic content - on
a par with strong domestic sewage; but the small quantity pro-
duced had little impact on secondary treatment. Table 14 shows
solids concentrations in thickener sludge and vacuum filter
cake. Nalco type 7120 liquid polymer was used both in the
thickening and dewatering processes. The coil-spring filters
produced cake containing about 12% solids. This relatively wet
cake is characteristic of polymer treatment. Total solids
wasted during Phase 1 averaged 185 kg/day (407 Ib/day). Vola-
tile solids were 60% of the total.
TABLE 14. THICKENER SLUDGE AND VACUUM FILTER CAKE -
MEDFIELD - PHASE 1
Thickener Vacuum Filter
Parameter Sludge Cake
Total Solids, percent 5.6 12.2
kg/day 185
(Ib/day) (407)
Total Volatile Solids, percent 3.4 7.4
kg/day 115
(Ib/day) (253)
Volume, cu m/day 5.36
(gal/day) (1420)
Capillary Suction Time, sec 12.1
Metals, mg/kg dry cake
Cadmium 38
Chromium 306
Copper 1240
Nickel 179
Lead 1330
Zinc 1080
A solids balance for Phase 1 is shown on Table 15. The
table shows average results obtained on three days during Phase
1, when solids were wasted: August 30, September 6, and Septem-
ber 15. The August 30 wasting contained septage solids dis-
charged prior to the Phase 1 period. The difference between
total volatile solids input and output is biological sludge pro-
duction. This difference, Yobs/ was 43 kg/day (95 Ib/day) or
0.4 kg of mixed liquor volatile suspended solids produced per
kg of BOD5 removed.
39
-------
TABLE 15. VOLATILE SUSPENDED SOLIDS BALANCE
MEDFIELD - PHASE 1
Sample
Volatile Suspended Solids
Influent, kg/day
(Ib/day)
Septage, kg/day
(Ib/day)
Change in MLVSS in Basin, kg/day
(Ib/day)
Secondary Effluent, kg/day
(Ib/day)
Cake, kg/day
(Ib/day)
Biological Sludge kg/day
Production /-n_/j \
(Ib/day)
Totals, kg/day
(Ib/day)
Input
66
(146)
8
(17)
0
(0)
43
(95)
117
(258)
Output
0
(0)
2
(5)
115
(253)
117
(258)
The observed yield coefficient reflects bacterial decay as
well as production. The observed coefficient, YO^S, is related
to a growth-yield coefficient, Y, that depicts growth only by:
obs 1 + k,8
d c
where
k-, = microorganism-decay coefficient, time
0 = mean cell residence time = SRT
Utilizing the kinetic decay coefficients for aerobic treatment
of domestic wastes, k^ = 0.05 days ~1, and the actual Phase 1
mean cell residence time, OG = 88 days, and computed observed
yield coefficient, Y0ks = 0.4, gives a growth yield coefficient,
Y, of 2.16. This value exceeds reported Y values (0.5 kg of
MLVSS produced/kg BOD_ removed) by a factor of four. It is
probable that the 88 Say cell retention time used for this com-
40
-------
putation overestimates the effective retention time under aero-
bic conditions. Low dissolved oxygen in aeration basins 2,
3 and 4 resulted in comparatively low time of solids under
aeration.
PHASE 2 - CONTINUOUS FEEDING
Process Characteristics
Process characteristics for the continuous septage feed
studies, Phases 2A and 2B, are shown on Table 16. The baseline
data are included for comparison. Continuous feeding was
approximated by introducing small quantities of septage every
15, 30 or 60 minutes throughout a test period.
During Phase 2 influent sewage flow increased slightly
over the average Phase 1 rate, causing slightly lower aeration
basin hydraulic retentions and lower Qr/Q values. During Phase
2A, the plant was fed septage at a rate equal to 2% of the aver-
age sewage flow, on a volumetric basis. The organic loading to
the plant doubled: loading increased from 83.3 to 152 gm BODc/
cu m-day (5.2 to 9.5 Ib BOD5/1000 cu ft,- day). This Phase 2A
value is at the low end of a range of organic loadings exper-
ienced at extended aeration plants (see Table 11). Solids
wasting was increased during Phase 2, and as a result, mixed
liquor volatile suspended solids did not increase above Phase 1
levels. The combination of increased organic loading and con-
stant mixed liquor solids concentrations is reflected in the
F/M ratio, which doubled.
In Phase 2B the feed rate was 3.6% of the sewage flow rate.
This resulted in a three-fold increase in organic loading and
F/M ratio. Organic loading during Phase 2B was near the upper
limit of values normally experienced at extended aeration
plants, but because of high solids retention in the aeration ba-
sins, the F/M ratio was considerably below conventional values.
Mean cell residence time for Phase 2 also reflects high mixed
liquor solids retention.
Influent Sewage and Septage
Sewage characteristics changed little throughout the Phase
1 - Phase 2 period. Average values for sewage shown on Tables
17 and 18 are similar to values shown for Phase 1 on Table 12.
Daily variability, represented by standard deviations presented
in Table 17 and 18, were considerably greater than differences
in average values shown for each phase. Based upon these in-
fluent data, Phase 1 is considered a valid baseline for an
appraisal of the effects of septage addition in Phase 2.
Septage characteristics are also shown on Table 17 and 18,
as are the computed combined sewage and septage characteristics
41
-------
TABLE 16. PROCESS CHARACTERISTICS AND LOADING -
MEDFIELD - PHASES 1 & 2
Characteristic
Flow Rate, Q, cu m/day
(mgd)
Septage Feed Rate, cu ro/day
(gpd)
Septage/Sewage, percent
Sludge Return Rate, Qr, cu m/sec
Cmgd)
Qr/Q
Aeration Basin Retention, hrs
Mixed Liquor Susp. Solids, mg/1
Mixed Liquor Volatile Susp. Solids,
rag/1
F/M, kg BOD5/kg MLVSS-day
BOD5, kg/day
(Ib/day)
COD-Total, kg/day
(Ib/day)
COD-Soluble, kg/day
(Ib/day)
Total Solids, kg/day
(Ib/day)
Total Volatile Solids, kg/day
(Ib/day)
Loading, gm BOD,-/cu m-day
(Ib BOD5/10QO cu ft-day)
Mean Cell Residence, days
Phase 1
780
Q.206
0
0
0
0.018
0.420
2.Q
37.6
7,580
4,570
0,018
110
(242)
215
(474)
68
(149)
348
(766)
144
(318)
83,3
(5.2)
88
Phase 2A
893
0.236
17.8
4,700
2,0
0,017
0.398
1.7
32.2
7,610
4,610
0.033
217
(478)
508
(1120)
137
(3011
508
(11201
241
(532)
152
09.5)
59
Phase 2B
1,094
0.289
39.4
10,400
3.6
0.020
0.457
1.6
25.9
7,670
4,770
0.055
279
(614)
1005
(2215)
161
(355)
968
(Z135)
609
(1343)
245
(15.3)
36
The computed concentrations are based upon average daily flow
rates and average characteristics of both sewage and septage.
Septage variability is well documented and is discussed in
Section 1. Storage at the plant tended to attenuate wide fluc-
tuations in organic and solids concentrations, but it also di-
minished the strengths of the stored septage due to solids sep-
42
-------
TABLE 17. SEWAGE AND SEPTAGE - MEDFIELD - PHASE 2 A
Combined Sewage
Characteristic Sewage Septage and Septage *
COD-Total, rag/1
COD-Soluble, mg/1
BOD5-Total, rag/1
BOD5~N Suppressed, mg/1
TOC, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Susp. Solids,
mg/1
Total Kjeldahl-N, rag/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Grease, mg/1
PH
Temperature, C
Alkalinity, mg/1 as CaCO
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
X
3Q8
118
155
115
71
448
189
114
86
26
15
0
11
61
7,0
17
3 145
0.0.2
0.12
0.22
0.18
0.20
1.65
s
118
53
54
34
8,0
75
64
77
53
4.0
•2.5
0
2,6
35
0.2
1.1
14
0.01
0,03
0.10
0.08
0.15
3.12
X
13,190
1,750
4,450
3,460
6,110
4,110
4,580
3,380
213
73
0
127
4,340
6.9
18
515
0.05
0.60
4,17
0.29
0.88
4.62
s
13,500
1,340
3,780
3,070
3,530
2,370
3,120
2,210
65
21
0
50
2,980
0.4
2.2
219
0.02
0.43
2.61
0.13
0.50
2.84
X
558
150
238
180
558
265
201
150
30
16
0
13
144
7,0
17
152
0.02
0.13
0.30
0.18
0-21
1.71
Calculated from sewage and septage quality data and relative
proportions of each waste
aration This occurred in the primary tank used for storage as
well as in the grit chamber. Nevertheless, by purposely obtain-
ing strong septage at Medfield, a moderately strong liquid was
fed during Phase 2. Septage COD averaged about 13,000 mg/1 in
Phase 2A and 16,000 mg/1 in Phase 2B. It is interesting to note
that soluble COD was a small fraction of the total—about 10%
43
-------
SEWAGE AND SEPTAGE - MEDFIELD - PHASE 2B
Characteristic
COD-Total, rag/1
COD-Soluble, mg/1
BOD5-Total, mg/1
BOD^-N Suppressed, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Susp. Solids,
mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
pH
Temperature , C
Alkalinity, mg/1 as CaC03
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Sewage
X
308
1Q6
122
77
414
210
100
86
24
16
0.6
7.3
15
136
0.05
0.07
0.08
0.04
0.26
0.23
s
98
67
39
22
78
58
94
69
4.8
3.3
0.1
0.3
0.5
15
0.07
0.01
0.01
0.03
0.12
O.Q6
—
Combined Sewage
Septage and Septage
X
16,100
1,080
3,510
1,800
12,440
9,140
11,140
8,300
278
69
7.2
12
665
0.06
0.27
2.43
0.26
1.40
5.51
s
14,500
410
3,300
674
15,590
11,320
15,360
11,130
233
6.3
0.3
1.0
187
0.03
0.23
1.40
0.18
0.57
4,01
X
887
142
246
140
855
538
505
388
33
:is
7.3
15
155
0.05
0.08
0.16
0.05
Q.3Q
0.41
for both periods. This result is consistent with the operation
of septic tanks, in which soluble organics are displaced into a
leaching field, while the major liquid fraction pumped from tanks
is recent influent sewage. Association of organic content with
suspended solids was observed in the majority of septage samples.
However, some septage samples were encountered, during the course
of the study,that were comparatively clear, but yielded surpris-
ingly high COD values.
Septage solids data shown in Tables 17 and 18 are consis-
tent with the COD data. Septage volatile suspended solids aver-
aged 86% of the total volatile solids. These results suggest
that primary clarification should be an effective process for
septage solids separation from a combined sewage/septage influent
44
-------
to a municipal plant. In fact, this result is confirmed by
studies at Barnstable, Massachusetts10 and by our research at
Marlborough, presented in Section 6 of this report.
In comparison with sewage, septage nutrient/carbon ratios
are low, but not below levels that tend to inhibit bacterial
growth. BOD5:N:P ratios for sewage and septage at Medfield
were 13.3:2.5:1 and 35:1.7:1, respectively. Nitrogen is TKN-N,
and phosphorus is total phosphorus. The combined septage and
sewage had a BODs:N:P relationship of 18.3:2.3:1. These values
are well within growth limiting ratios of about 60iS:!.11
\
Septage brought to Medfield contained considerable quanti-
ties of grease. In Phase 2A the 2% input of septage more than
doubled the grease load on the plant. Septage had little effect
on pH, alkalinity, or metal concentrations at Medfield. Compari-
son of sewage and combined influent on Tables 17 and 18 show
only negligible increases in concentrations.
Phase 2 data are presented in detail in Appendices C and
D. The reader is encouraged to review the data in total as a
means of gaining insights into the impact of septage on this
treatment facility, which plots and statistical parameters do
not provide.
Effluent Quality
Changes in effluent quality caused by the continuous addi-
tion of septage are shown on Table 19. Total and soluble COD
average values appear to increase with septage addition. BOD5,
total solids, suspended solids, and volatile suspended solids
data suggest that septage at the 2% and 3.6% levels did not
affect effluent quality. Only the average total volatile solids
for Phase 2B appears higher than baseline values. On September
23, the return sludge pumps at Medfield were inadvertently turn-
ed off over night. This caused a reduction in mixed liquor sus-
pended solids shown on Appendix Table C-4 and increased solids
and organic concentrations in the secondary effluent. Data that
reflect the effects of this malfunction are not included in the
average values shown on Table 19. To determine if septage
actually increased effluent organic concentrations, one-way
Guttenplan, Steven D.,"The Establishment of a Septage Re-
ceiving and Handling Program for the Town of Barnstable, Mass.",
Journal of the New England Water Pollution Control Association,
Part 1,. Volume II, 1977, pp. 1-10.
11Clark, N.W., Viessman, W., and Hammer, M.J., Water Supply and
Pollution Control, International Textbook Co., Toronto,
1971, pg. 269.
45
-------
analysis-of-variance tests were conducted on data shown in
Appendices B-2, C-3 and D-3. Phase 1 was compared with Phase_
2A and 2B data. The results of these computations are shown in
Table 20.
TABLE 19. EFFLUENT QUALITY -
MEDFIELD - PHASES 1 & 2
Characteristic
Phase 1
Phase 2A
Phase 2B
COD-Total, mg/1
COD-Soluble, mg/1
BOD5~Total, mg/1
BOD5~N Suppressed, mg/1
TOG, mg/1
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Susp. Solids, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Grease, mg/1
pH
Temperature, °C
Heavy Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
X
19.5
17
4
1
13
336
78
4
3
0.2
7.2
0.7
4.5
7.3
19
0.03
0,15
0.06
0.10
0.15
0.22
X
27
20
3.7
1.0
6.3
326
68
3,2
2.0
2.7
4.1
1.4
3.9
7.1
18
0.02
0.13
0.14
0.11
0.03
0.70
s
11
7.3
2.7
0.9
4.2
45
22
2.7
1.9
2.0
3.5
0.7
0.6
0,3
1.3
0.01
0.04
0.09
0,01
0.05
1.40
X
31
26
2.5
1.4
316
115
2.4
2.1
0,4
12.8
7.4
14.1
0.01
0.05
0.03
0.01
0.08
0.41
s
5.0
7.4
1.0
0.8
68
42
1.4
J-,4
0.2
1.8
0.3
0.9
0.0.1
0.04
0.01
0.01
0.02
0.46
The observed F ratio for total COD is larger than the criti-
cal value of F at the 99% level. The assumption that septage
addition did not increase the concentrations of organic material
in secondary effluent cannot be rejected. Analysis-of-variance
computations for the solids data support the contention that the
effluent was not affected, with the exception of the Total Vola-
46
-------
TABLE 20. ANALYSIS OF VARIANCE RESULTS - MEDFIELD
Parameter
Computed F F ** k-1
Degrees of Freedom
* n,-l*
i
COD-Total
COD-Soluble
BOD5-Total
BOD5-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Suspended Solids
7.61
4.98
0,99
0.69
0.65
8.83
2.04
1.88
5.12
5.12
5.40
5.15
5.10
5.11
5.10
5.10
2
2
2
2
2
2
2
45
45
29
44
49
48
49
49
* k = the number of data groups (3 in all cases)
* n. = total number of measurements
**
Dixon and Massey, Introduction to Statistical Analysis,
(McGraw Hill, New York):398.~~
tile Solids results (and this result is based only upon Phase 2B
data). There was no significant difference between Phase 1 and
Phase 2A total volatile solids values.
If septage affected effluent quality during continuous
feeding at 2% and at 3.6%, the effects were barely measureable.
It is concluded that septage did not diminish effluent quality.
Statistically, the long periods of monitoring, particularly
Phase 2A, provide an adequate basis for this conclusion.
Effluent quality was well within regulatory requirements. Grease
and heavy metal concentrations in the effluent were unaffected
by septage addition.
Nitrogen
Ammonia and nitrate concentrations varied during Phase 2
in response to septage loading, aeration basin dissolved oxygen
levels, bacterial population response, and changes in mixed
liquor volatile suspended solids concentration. The latter was
dependent upon sludge production and wasting. Figures 9 and 10
show ammonia nitrogen and nitrate nitrogen concentrations as
a function of time. In Phase 2A the aerator in basin 1 was on
high; the remaining aerators in basins 2, 3, and 4 were kept on
the low setting. During Phase 2B, the aerators in basins 1 and
2 were on high; the remainder on low.
47
-------
Z
o
ex
00
UJ
o
Z
o
RETURN SLUDGE
WASTED
DISSOLVED OXYGEN
BASIN 2
0
13 14 15 16 17 18 19 20 21 22 23 24 25 26
SEPTEMBER 1977 DATE
Figure 9. Effluent nitrogen and Basin 2 dissolved oxygen
27 28
30
123
OCTOBER 1977
Medfield - Phase 2A.
-------
15
14
13
12
11
10
9
8
7
O 6
5
4
O
K
LU
O
1 r
RETURN SLUDGE
WASTED
31 1
OCTOBER
NITRATE - N
-DISSOLVED OXYGEN
BASIN 2
AMMONIA - N
345
NOVEMBER
DATE
Figure 10.
Effluent nitrogen and Basin 2 dissolved oxygen
Medfield - Phase 2B.
49
-------
In Phase 2A the ammonia began to increase in the plant
effluent three days after initiation of loading. It reached a
maximum of 6.1 mg/1 as N, three days later, and declined there-
after. Throughout this phase of monitoring, nitrification was
never complete. The three day period prior to the initial in-
crease provided sufficient time for a process response to the
impact of increased organic loading. The initial rise also co-
incides with solids wasting on September 15. Similar responses
do not occur on other wasting days. Apparently, wasting did
not significantly reduce nitrifying bacterial populations.
Nitrate nitrogen concentrations in secondary effluent de-
clined steadily during Phase 2A from levels above 8 mg/1 during
the first several days of loading, to less than 1 mg/1 near the
end of the test period. Denitrification exhibited in Phase 2A
is associated with dissolved oxygen levels in basins 2, 3, and
4. Dissolved oxygen in basin 2 declined steadily from 1.9 mg/1
on September 13 to 0.45 mg/1 six days later on September 19.
Thereafter, dissolved oxygen was very low or nonexistent in
basins 2, 3, and 4. Dissolved oxygen values during this period
are shown on Appendix Table C-4.
Phase 2B was conducted one month after completion of 2A.
During the intervening month, the plant was shock loaded with a
slug of septage (Phase 3A). During the week of continuous load-
ing, Phase 2B, the plant nitrified completely. This was
accomplished at almost twice the previous loading.
Nitrification and Denitrification - An Explanation
While nitrification was essentially completed in the first
aeration basin during Phase 1, increased organic loading in
Phase 2 apparently inhibited nitrification in this basin. During
Phase 2A the nitrifiers were further inhibited in basins 2, 3,
and 4 by low dissolved oxygen levels; nevertheless, considerable
ammonia oxidation did occur. In Phase 2B increased oxygen input
to basin 2 (high aerator setting) increased dissolved oxygen
levels in basins 2, 3, and 4. This is shown on Figure 10 and
in Appendix Table D-5. Figure 10 shows the results of increased
dissolved oxygen in basins 2, 3, and 4 - complete nitrification
demonstrated by low ammonia concentrations and a marked re-
duction in denitrification, shown by high nitrate levels.
Phosphorus
In Phase 1 phosphorus averaged 10.6 mg/1 in the influent
sewage (See Table 21). This was equivalent to an input of 8.3
kg/day (18.2 Ib/day). The addition of 48.1 I/day (12.7 gal/day)
of a 19% solution of sodium aluminate, 9.1 kg/day (20.1 Ib/day),
as A12C>3 reduced phosphorus in the effluent to 0.7 mg/1, 0.5
kg/day (1.2 Ib/day). Approximately 1.2 kg of sodium aluminate
were used per kg of phosphorus removed in the processes.
50
-------
TABLE 21. PHOSPHORUS REMOVAL
MEDFIELD - PHASES 1 & 2
Phase 1 Phase 2A
Influent
Septage
Effluent
Phosphorus Removed
A12O3 Used
Al O./P, kg/kg*
**
A1203/P, kg/kg
A1+++/P, kg/kg**
- - — ' •*
8,3
0.54
7.8
9.1
1.2
1.5
0.79
(18
(1
(17
(20
-2)
.2)
.0)
.1)
10.
2.
1.
11.
10.
0
3
3
0
3
0.
1.
0.
(22
(5
(2
(24
(22
94
13
60
.1)
-0)
.9)
-2)
.8)
*Based upon total phosphorus removal
**Assuming 2 mg/1 P incorporation into cells, BOD/Ps:90/l
Assuming 2 mg/1 of phosphorus taken up by organisms based upon
a 90:1, C:P ratio in sludge-^, the ratio of A12O3 to phosphorus
precipitated increases to 1.5 or 0.79 as A1+++:P. This compares
with estimates of 0.87 as A1+++:P.13
In Phase 2A, phosphorus derived from septage and a higher
sewage flow increased input to the plant to 11.0 kg/day. Dur-
ing this phase of operation sodium aluminate feed was insuf-
ficient, and effluent phosphorus concentrations averaged 1.5
mg/1. Again, assuming 2 mg/1 cell uptake, Al2O3:P, and Al~l~~l~+:P
ratios were 1.13 and 0.60, respectively. These values are lower
than both Phase 1 and reported values, and are a direct result
of the high effluent concentrations, i.e., the remaining frac-
tion of phosphorus would require proportionally more aluminate
for removal.
Based upon an average of 190 mg/1 of phosphorus in septage,
0.23 kg of A1203 are required per cu m of septage (0-39 lb/1000
gal). For commercially available sodium aluminate solution
(19% A^Og) , 1.2A of sodium aluminate solution is required per
cu m of septage (1.2 gal/1000 gal).
12
Fair, Geyer and Okun, Water and Wastewater Engineering, Wiley,
New York, 1968, pp. 34-6.
Process Design Manual for Phosphorus Removal, U.S. Environ-
mental Protection Agency, Technology Transfer, 1971, pp.3-4.
51
-------
Dissolved Oxygen
Sludge wasting during Phase 2 compensated for septage
solids, either added with septage or produced in the aeration
basins from the soluble septage fraction. Table 22 shows mixed
liquor solids concentrations and alkalinity unchanged throughout
Phase 1 and Phase 2. Basal metabolism oxygen requirements are
thus assumed constant for the period, and changes in oxygen de-
mand are attributed to septage addition.
TABLE 22. MIXED LIQUOR CHARACTERISTICS - MEDFIELD - PHASES 1&2
Characteristic
Total Solids, mg/1
Total Volatile Solids,
Suspended Solids, mg/1
Volatile Susp. Solids,
PH
Temperature, °C
Phase Phase
1 2A
mg/1
mg/1
Alkalinity, mg/1 as CaCO-,
D.O. Uptake, mg/l-hr
Dissolved Oxygen Basin
Dissolved Oxygen Basin
Dissolved Oxygen Basin
Dissolved Oxygen Basin
#1, mg/1
#2, mg/1
#3, mg/1
#4, mg/1
Dissolved Oxygen Clarifier, mg/1
Settlometer, 30 min
X
7910
4670
7580
4570
7.0
20
241
15.0
4.7
1.2
1.0
1.0
1.2
695
X
8050
4750
7720
4670
6.9
18
241
20.6
3.5
0.5
0.5
0.5
0.5
705
s
369
249
354
241
0.3
1.7
30
5.8
1.1
0.4
0.3
0.4
0.4
41
Phase
2B
X
7990
4880
7770
4780
7.3
14.2
225
13.5
2.0
3.6
2.9
2.3
1.1
439
s
263
143
238
138
0.4
0.8
70
4.2
1.4
1.1
1.1
1.1
1.0
40
Dissolved oxygen levels in the aeration basin were affected
by septage loading and aerator setting. In basin 1 dissolved
oxygen dropped from an average of 4.7 mg/1, in Phase 1, to 3.5
in Phase 2A and finally to 2.0 mg/1 in Phase 2B. During Phase
1 basins 2, 3, 4 and the clarifier held an average of 1 mg/1
of dissolved oxygen. However, with the same aerator settings
these basins just barely held their dissolved oxygen during
Phase 2A. Basins 2, 3, and 4 would not have remained aerobic in
Phase 2B had the basin 2 aerator stayed on the low setting.
52
-------
Based upon dissolved oxygen and temperatures in basin 1,
computations using the expression:
dO
2 =
dt
K(C - C)
o
show a 37% increase in oxygen utilization in basin 1 between
Phase 1 and Phase 2A, and a 90% increase between Phase 1 and
Phase 2B, where:
dO
= rate of oxygen utilization, mg/l-day
"
K = oxygen transfer coefficient, day
C = oxygen saturation concentration, a function of
temperature, mg/1
C = measured dissolved oxygen concentrations, mg/1
A 13% increase was observed in basins 2, 3, and 4 in Phase 2A.
Dissolved oxygen uptake measured directly in basin 3 in-
creased by 37% in Phase 2A from an average of 15.0 mg/l-hr to
20.6 mg/l-hr. In Phase 2B dissolved oxygen uptake averaged 13.3
mg/l-hr in basin 3 and 16.7 in basin 1. These values are com-
parable to the Phase 1 average uptake rates .
It is apparent that the principal BOD5 fraction was exerted
in the first two basins and that measured uptake rates in basin
3 do not reflect this demand. This is particularly true in
Phase 2B with increased air input to basin 2. Measured dis-
solved oxygen uptake values in basin 1 are time dependent and
vary as a surge of sewage or septage enters the basin. Dis-
solved oxygen levels attenuate these effects and are a better
indication of oxygen utilization.
Using dissolved oxygen levels, the information included in
Table 23, and the following equation, oxygen utilization was
computed for the septage added in Phase 2A.
dO,
^
dF
II
do,
dF
dO,
t.
dF
dO.
kg On/kg BODC= 2 /BOD^ = K
7 ~ dt~ b
where,
= K
(C - C) - (C - C)
3 II S I
"
-------
TABLE 23. DISSOLVED OXYGEN UTILIZATION - MEDFIELD - PHASES 1 & 2
Phase 2B
Pre-loading & During
Phase 1 Phase 2A Recovery Period Test
Basin #
Dissolved
Oxygen, C,
mg/1
Saturation
D.O., Cs,
mg/1
, kg/day
2, 2",
1 3&4 1 3&4 1 2 3&4 1 2 3&4
4.7 1.0 3.1 0.5 4.6 5.3 4.2 1.6 3.4 2.4
9.1 9.1 9.5 9.5 10.2 10.2 10.2 10.3 10.3 10.3
, ,-,
-, kg/day
87.4 39.3
26.7 36.1
106
134.4 87.4 83.0
41.1 26.7 50.8
138
ABOD (Differ-
ence Phases
1 & 2)
kg/day
kg 02/kg BOD5
A COD (Phase
1-2)
kg O2/kg COD
kg 02/kw-hr
Ib O2/hp-hr
increase due to increased sewage inflow)
(Cs ~ Oj = dissolved oxygen deficit in Phase 1.
The reaeration coefficient K was calculated from Phase 1 oxygen
uptake measurements and equals 43.7 day"1.
Based upon dissolved oxygen deficits in the four aeration
basins, dissolved oxygen utilization attributed to the incre-
mental septage load was 0.59 kg 02/kg BODs. The Phase 1 oxygen
utilization for sewage was 4.5 kg 02/kg BOD5, but most of this
was for cell respiration.
1.22
2.01
0.59
284
0.22
1.42
2.33
0.86
626
0.19
0.67 0.94
1.10 1.55
54
-------
If the five-day biochemical oxygen demand value, BODs, for
septage is assumed to be 68% of the ultimate demand BODL, then
oxygen utilization was 0.4 kg 02/kg BODL. The 68% is an average
value for domestic sewage and has not been verified for septage.
The turbine aerators at Medfield are rated at 7.46 kw (lOhp)
at 1800 rpm (high setting) and 1.86 kw (2.5 hp) at 900 rpm
(the low setting). The four units produced an average of 1.2 kg
02/kWh(2.0 Ib 02/hp-h) during Phase 1 and 1.4 kg 02/kWh (2.3
Ib/hp-h) during Phase 2A. This compares with design values for
activated sludge processes between 1.5 kg O2kWh (2.5 Ib 02/hp-h)
and 2.4 kg O2/kWh (4.0 Ib 02/hp-h).14
Oxygen utilization for Phase 2B could not be determined by
comparison with Phase 1 because of the change in speed of the
basin 2 aerator. For Phase 2B a comparison was made between
average dissolved oxygen levels during loading and values ob-
tained just prior to and following the loading period. This
analysis yielded values of 0.74 kg 02/kg BODs and 0.9 kg 02/kWh
(1.6 Ib 02/hp-h).
In conclusion, it appears that conventional oxygen require-
ments and transfer design parameters used for the treatment of
domestic sewage at extended aeration plants may be applied to
the treatment of sewage and septage. Conventional parameters
are conservative for the Medfield operation.
Thickener Supernatant and Vacuum Filtrate Quality
Organics and solids concentrations in flotation thickener
supernatant did not increase with septage addition. A compari-
son is shown on Table 24. Supernatant quality with or without
septage addition was similar to secondary effluent. Increases
in heavy metals concentrations shown on Table 24 are attributed
to sample variation and the limited data base. Unless septage
is derived from industrial sources, concentrations of metals in
thickener supernatant, vacuum filter filtrate or sludge cake
should not change appreciably with septage addition.
Table 25 shows an increase in vacuum filtrate organic and
solids concentrations between Phase 1 and Phase 2. An analysis-
of-variance of filtrate and supernatant data indicates no signi-
ficant difference between Phase 1, Phase 2A and Phase 2B data.
However, the statistical analysis is based upon a small number
of samples.
Schroeder, Edward D-, Water and Wastewater Treatment, McGraw
Hill, New York, 1977, pg. 115.
55
-------
TABLE 24. THICKENER SUPERNATANT CHARACTERISTICS
MEDFIELD - PHASES 1 & 2
Characteristic
COD-Total, mg/1
BOD5-Total, mg/1
BOD.--N Suppressed, rag/1
TOC, mg/1
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Susp. Solids, mg/1
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Phase
1
X
26
4.4
0.7
12
329
71
1
1
0.03
0,01
0.07
0.09
0.59
0.23
Phase
2A
X
25
1.4
1.3
313
51
8.6
5.6
0.02
0.51
0.16
0.12
0.21
1.21
s
5.2
0.6
0.9
21
14
12
10
0.01
0.64
0.12
0.02
0.19
0.98
Phase
2B
X
35
4.5
2.1
303
71
7.0
4.0
0.01
0.05
0.03
0.03
0.11
0.28
s
3.2
2.4
0.3
32
20
7.8
2.6
0.01
0.03
0.01
0.01
0.03
0.02
Sludge Production
In Phase 1 the plant produced 185 kg/day (407 Ib/day) of
dry solids. The 2% septage addition increased production to
260 kg/day (571 Ib/day) and the 3.6% addition increased it to
309 kg/day (679 Ib/day}. Total solids, volatile solids, and
heavy metal concentrations are shown in Table 26.
Table 27 shows a volatile solids mass balance for Phase 2.
Volatile solids production increased from 43 kg/day (95 Ib/day)
in Phase 1 to 77 kg/day (168 Ib/day) in Phase 2A and to 143 kg/
day C317 Ib/day) in Phase 2B. The Phase 1 and 2A estimates are
each based upon1three weeks of data, while Phase 2B is based
upon one week of data and a single wasting period. Thus the
Phase 2A data are used for sludge production estimates.
Increases in the quantity of solids wasted daily from the
plant are compared on Table 28 for Phase 2A with increases in
organic and solids loading. There appears to have been a direct
one-to-one relationship between the increase in BOD5 and soluble
COD, and volatile suspended solids production in the aeration
basins. It also appears that the increase in septage and sewage
total solids caused a corresponding rise in cake production.
56
-------
TABLE 25. VACUUM FILTRATE CHARACTERISTICS
MEDFIELD - PHASES 1 & 2
Characteristics
Phase
1
Phase
2A
Phase
23
COD-Total, mg/1
BOD -Total, mg/1
BODj--N Suppressed, mg/1
TOC, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Susp. Solids,
mg/1
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
x
358
120
101
71
768
381
83
55
0.02
0.08
0-15
0-10
0.23
1.31
x
970
398
243
143
1290
658
1170
717
0.02
0.19
0.30
0.10
0.51
1.70
600
19
6.4
392
1440
893
0.02
0.06
0.22
0.01
0.32
1.18
x
1140
383
160
742
918
590
0.04
0.08
0.55
0.07
0.74
1.36
696
77
33
660 1390 815
484
760
481
0.01
0.01
0.42
0.01
0.06
0.97
Settlometer Tests
Settlometer tests in conjunction with mixed liquor and re-
turn sludge solids concentration analysis, sludge blanket depth
measurements, and sludge volume index (SVI) determinations are
used to regulate sludge return rates and sludge wasting. Process
control using the "West" method requires the addition of a re-
turn sludge centrifuge test.-'-5
Figure 11 is a characteristic plot of settled sludge volume
as a function of settling time. Average curves for Phases 1 and
2 are shown. The level of mixed liquor solids carried at
Medfield was atypical of extended aeration plants. As a result
the settling was slow, compaction was limited and the average
curves are considerably above conventional measurements. Sett-
ling improved slightly after each wasting period as shown on
15 Alfred W. West, Return Sludge Flow Control, (National Waste
Treatment Center: U.S. EPA, September 1960).
57
-------
TABLE 26, THICKENER SLUDGE AND VACUUM FILTER CAKE
MEDFIELD - PHASES 1 & 2
Thickener Sludge
Phase I 2A 2B
Total Solids, percent 5,6 4.6 4.0
kg/day
Ub/day)
Total Volatile Solids, 3.4 2.8 3.0
percent kg/day
(Ib/day)
Volume, cu m/day 5.36
(gal/day) 1420
Capillary Suction Time, 12.1 14.7 7.0
sec
Metals, mg/kg dry cake
Cadmium
Chromium
Copper
Nickel
Lead
TABLE 27. VOLATILE SUSPENDED SOLIDS
MEDFIELD - PHASE 2
Vacuum Filter
1
12,2
185
407
7.4
115
253
38
306
1240
179
1330
BALANCE
2A
12,0
260
571
7.4
164
361'
22
166
792
75
389
Cake
2B
11.8
309
679
5.2
270
596
33
108
735
83
622
PHASE 2A
Sample Input Output
Influent, kg/day 78
(Ib/day) (172)
Septage, kg/day 53
(Ib/day) (118)
Change in MLVSS, kg/day 42
(Ib/day) (93)
Secondary
Effluent, kg/day 2
(Ib/day) (4)
Cake, kg/day 164
(Ib/day) (361)
Sludge kg/day 77
Production (Ib/day) (168)
Totals, kg/day 208 (208)
(Ib/day) (458) (458)
PHASE
Input
95
(209)
208
(458)
143
(317)
446
(984)
2B
Output
174
(384)
2
(4)
270
(596)
446
(984)
58
-------
TABLE 28 - SOLIDS RATIOS - MEDFIELD - PHASE 2A
Ratio
Phase 2A/Phase 1
Cake Solids Production
Total Solids
Total Volatile Solids
Influent Sewage and Septage
Total Solids
BOD 5
COD-Soluble
Sludge Production
Mixed Liquor Volatile
Suspended Solids
1.41
1.43
1.46
1.98
2.02
1.79
1000
900
800
700
600
Q
<
a: 500
£ 400
UJ
3 300
I-
200
100
0
co
PHASE 1
PHASE 2
10
1
20 30 40
TIME, MIN,
50
60
Figure 11. Settlometer Readings - Medfield - Phases 1 and 2
59
-------
Figures 12 and 13, but because of the high solids concentration,
changes in settlometer readings were never a useful indication
of meeting requirements.
1000
900
CD
I
RETURN
SLUDGE
WASTED
LU
to 400
I
I
I
I
23 25 27 29
AUGUST
31
468
SEPTEMBER
10 12
DATE
Figure 12. Mixed liquor 30-minute settlometer readings
Medfield - Phase 1.
900
O
CO
600
500
400
I I I I
I RETURN I
•SLUDGE WASTED!
Ill I-
I
I
I
I
I
13 15 17 19 21 23
SEPTEMBER
DATE
25 27 29
1 3
OCTOBER
Figure 13. Mixed liquor 30-minute settlometer readings
Medfield - Phase 2A.
60
-------
Sludge Dewatering
In Phase 2 solids fed to the thickener and vacuum filter
increased in direct proportion to the total solids in the added
septage. Septage addition resulted in increased polymer use,
again, in proportion to the quantity of solids added. Vacuum
filter cake was unaffected by septage addition but septage did
reduce the percent of solids in the thickener float (See Table 26).
This was caused by an increase in wasted sludge suspended solids
concentration above Phase 1 levels. The average return sludge
solids concentration on the wasting days was 10,850 mg/1 in
Phase 2 as compared with 8,970 mg/1 in Phase 1. The increased
solids caused a 17% reduction in the air to solids ratio which
reduced the float solids content from 5.55% to 4.62%.16
Sludge dewatering was determined during Phase 1 and 2 by
observing the cake produced weekly and by conducting Capillary
Suction Time,CST, measurements on returned and thickened sludge.
The measuring device was a Type 130 Triton CST apparatus. The
device measures the dewaterability of sludges by monitoring the
time it takes to extract a unit volume of water by capillary
suction.
Samples of returned sludge collected prior to thickening
in both phases had low CST values: this indicates excellent de-
waterability. Individual measurements are plotted on Figure 14.
The increase in solids in Phase 2 had no effect on CST values,
nor did the nature of the sewage/septage mixture affect returned
sludge CST.
Figure 14 also shows a reduction in thickened sludge CST
values with increasing septage addition. This was probably a
result of decreasing solids concentration. Whether or not sep-
tage improved sludge dewaterability is debatable—certainly it
did not diminish dewaterability.
PHASE 3 - SHOCK LOADING
In Phase 3, the plant was slug loaded daily with quantities
of septage which averaged 1.8% of the daily sewage flow rate
during the first three-day test, and 2.6% during a second four-
day test. The percent rate of septage feed based upon actual
sewage and septage flow rates was 10-13% during Phase 3A and
60-75% during Phase 3B. The methods used to shock the plant were
presented in a description of the monitoring program at Medfield
(Section 4 of this report).
16U.S. Environmental Protection Agency, Process Design Manual
for Sludge Treatment and Disposal, 1974, pp. 4-21.
61
-------
03-
O
0
LLJ
ID
a.
LU
en
2 -
1 -
THICKENED SLUDGE
5 10 15
CAPILLARY SUCTION TIME (SEC)
Figure 14. Septage feed vs. capillary suction time - Medfield.
Shock loading affected many aspects of the Medfield process:
mixed liquor concentrations, protozoan growth, effluent quality,
and particularly dissolved oxygen concentrations. Changes
occurred quickly and recovery was rapid. The effects of each
shock on the system are shown in detail in Appendices E and F.
Influent Sewage and Septage
Average influent sewage and septage characteristics during
Phase 3 are shown on Table 29. Sewage flow into the plant in-
creased 58% over the Phase 1 levels. The increase was primarily
caused by storm water infiltration into the Medfield sewerage
system. This conclusion is supported by a comparison of Phase
1 and Phase 3 COD, BODs and solids data. The Phase 3 averages
are considerably below Phase 1 levels. During Phase 3 the plant
received about the same sewage solids and organic load as during
Phase 1, but hydraulic detention times were reduced by 37%.
Strong septage was selected and transported to Medfield for
the Phase 3 study. Analyses of material used for each test are
included in the Appendices. Generally, the septage had a COD in
the 28,000 mg/1 range, BOD5 of about 5,000 mg/1, and total
solids, 14,000 mg/1. The exception was the third day of Phase
3A, when 37.9 cu m (10,000 gal) of septage sediment that had
accumulated during the previous tests were pumped into the plant.
This miasmic liquid had a COD of at least 60,000 mg/1.
Effluent Quality
Between 7 a.m. and 8 a.m. sewage flow sharply increased at
Medfield, and remained comparatively high each morning. This is
62
-------
TABLE 29. SEWAGE AND SEPTAGE CHARACTERISTICS
MEDFIELD - PHASE 3
Phase
Flow, cu m/day
mgd
Sept age/Sewage
COD-Total, mg/1
COD-Soluble, mg/1
BOD5-Total, mg/1
BOD--N Suppressed, mg/1
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
PH
Alkalinity, mg/1 as CaC03
Temperature , C
Sewage
3A 3B
1,240
0.33
191
84
51
387
143
89
73
13
14
7.4
135
1,220
0.32
230
77
72
50
386
138
87
72
21
23
0.6
137
14
Septage
3A 3B
1.5-2.0
39,400
1,740
5,590
4,310
12,800
10,100
11,000
8,870
57
147
6.9
460
2.4-3.1
27,200
2,000
5,100
3,980
14,100
10,700
12,870
9,860
400
176
377
a common occurrence at treatment plants. The effects of this
surge of sewage were: a rise in the F/M ratio, increased dis-
solved oxygen uptake rates, lower D.O. in the aeration basins,
and initially higher D.O. levels in the secondary clarifier.
Flow from the clarifier abruptly increased. Initially, clari-
fier effluent organic content is low, reflecting extended treat-
ment during the night. The increased flow shortens the hydraulic
retention time during the morning hours, and results in diminish-
ed effluent quality late in the day. The effects of septage
addition are viewed in light of this normal early morning fluc-
tuation.
Changes in secondary effluent COD and BOD5 during the two
shock loading periods are shown on Figures 15 and 16. The BOD5
data plotted on both of these figures show no definite increases
associated with shock loading. The slight perturbation in these
63
-------
50
40
2 30
DC
0
O
O
20 —
10 -
9AM 9AM 9AM 9AM 9AM
10/14 10/15 10/16 10/17 10/18
TIME
Figure 15. Effluent BOD and COD - Medfield - Phase 3A.
60
50
40
< 30
20
O
o 10
I '
COD
BODC
9AM 9AM
11/14 11/15
9AM 9AM
11/16 11/17
TIME
9AM
11/18
Figure 16. Effluent BOD and COD - Medfield - Phase 3B,
64
-------
data appear to be random. Throughout the two periods, BOD-
levels were at least as low as during Phase 1.
Phase 1 effluent total COD averaged 20 mg/1, and effluent
soluble COD averaged 18 mg/1. During Phase 2, effluent total COD
increased slightly to an average of 32 mg/1, and soluble COD
increased to 24 mg/1. The overall effect of shock loading in
Phase 3 was again a slight deterioration in effluent quality:
total COD increased to about 32 mg/1 in Phase 3A, and to 40 mg/1
in 3B. Soluble COD data for Phase 3B averaged 23 mg/1.
Peak COD concentrations in Phase 3 generally occurred five
to seven hours after the morning sewage surge and septage input.
Recovery was rapid and a second increase in COD values was not
observed after the early evening sewage flow surge, which was
less pronounced.
Secondary effluent total and suspended solids data are
plotted on Figure 17 and 18. In Phase 1 total and suspended
solids in the effluent averaged 336 mg/1 and 4.0 mg/1, respec-
tively. Only total solids data following the first two shocks
during Phase 3B (Figure 18) show values significantly above the
Phase 1 levels.
500
400
o
"- 300
LU
O
O
O
200
100
J ' ' ' |
I 1
1 ^ ^ I ' ' ' I
SHOCK LOADINGS
TOTAL SOLIDS
SUSPENDED SOLIDS
i i j^ j i J
9AM 9AM 9AM 9AM 9AM
10/14 10/15 10/16 10/17 10/18
TIME
Figure 17. Effluent total solids and suspended solids - Med-
field - Phase 3A.
The results of organic and solids analyses, just reviewed,
indicate that secondary effluent quality was little affected by
the introduction of comparatively large quantities of septage.
65
-------
Increases in COD observed daily during Phase 3 were caused pri-
marily by flow surges. It is suggested that had septage been
added several hours before the morning surges, the impact upon
effluent quality would have been more pronounced.
(SI
o
z
o
o
500
400
300
200
100
-i r
t i
i 1 1 1 r
SHOCK
LOADING
TOTAL SOLIDS
•SUSPENDED SOLIDS
I . , , I . .
9AM 9AM 9AM 9AM 9AM
11/14 11/15 11/16 11/17 11/18
TIME
Figure 18.
Effluent total solids and suspended solids -
Medfield - Phase 3B.
Nitrogen
Ammonia data for Phase 3 are given in Appendix Tables E3
and F3. During Phase 3A, effluent ammonia nitrogen levels never
exceeded 0.1 mg/1. During the three-day shock loading period,
nitrate nitrogen levels steadily declined from 15 mg/1 to 5 mg/1,
Complete conversion of ammonia to nitrates occurred throughout
the test period. Denitrification began on the second day, and
was coincident with the drop in basin 2 dissolved oxygen levels.
This is shown on Figure 19. The principal effect of the slug
load was a rapid reduction in mixed liquor dissolved oxygen
levels, which resulted in a gradual increase in nitrate reduc-
tion over the course of the test.
Nitrification and denitrification processes seen in Phase
3A were repeated in Phase 3B. The large quantities of septage
used in Phase 3B only slightly inhibited nitrification. These
data are plotted in Figure 20. Dissolved oxygen levels dropped
dramatically after each shock load, and denitrification again
increased steadily during the four-day period.
66
-------
DISSOLVED OXYGEN
BASIN 2
10/17
9AM
10/18
Figure 19. Effluent nitrogen and Basin 2 dissolved oxygen
Medfield - Phase 3A.
I ' •
SHOCK
LOADING
_ DISSOLVED OXYGEN
BASIN 2
9AM 9AM
11/14 11/15
9AM
11/16
TIME
9AM 9AM
11/17 11/18
Figure 20.
Effluent nitrogen and Basin 2 dissolved oxygen
Medfield - Phase 3B.
67
-------
Dissolved Oxygen
The introduction of a large slug of septage caused an
initial decline in basin 1 dissolved oxygen. The initial de-
mand is the weighted average of the anaerobic slug diluted in
the 302 cu m (80,800 gal) basin. Septage did not cause an ini-
tial mixed liquor dissolved oxygen reduction to a value less than
given by:
D'°- initial . VOLbasin
D-°-final =
This was determined experimentally in the laboratory. For
example, the 29.5 cu m (7,780 gal) of septage introduced on
three days of Phase 3B caused an initial 9% drop in the pre-shock
dissolved oxygen concentration. The major observed decline in
oxygen levels was caused by a rapid increase in dissolved oxygen
uptake .
Figures 21 and 22 show the rapid increase in dissolved oxy-
gen uptake rates experienced after each shock loading. These
curves vividly demonstrate the treatability of septage in sys-
tems treating domestic sewage. The effect of the shock load
was most pronounced in the first aeration basin. Rates increas-
ed in Phase 3B, Figure 22, from 10 to 15 mg/l-hr to 25 to 45mg/l-
hr. The high uptake rates lasted for about six to eight hours
and declined thereafter. On each day of the Phase 3 shock per-
iod, the uptake rate ascended to a higher value than on the pre-
vious day, and returned to a higher value preceding the next
shock. The basin 3 data shown in Figures 21 and 22 show a two-
hour lag in response to the shock loadings, and slighter increas-
es than experienced in the first basin. Basins 1 and 2 obvious-
ly did the "lion's share" of the work.
Settling
Thirty-minute settlometer results for basins 1 and 4 are
shown on Figures 23 and 24. In each case, septage solids in-
creased the settling rate and markedly diminished supernatant
quality. In Phase 3A thirty-minute settlometer readings changed
from 650 ml/1 to about 550 ml/1.
Average settlometer curves for the entire monitoring period
are shown on Figure 25. Figure 25 is a plot of settled sludge
volume as a function of time. Generally, the curves show that
settling rates and sludge compaction increased with septage
additions.
Values obtained after shock loading the plant with 29.5 cum
(7,780 gal) of septage on November 16, 1977 are shown on
68
-------
9AM 9AM 9AM 9AM
10/14 10/15 10/16 10/17
9AM
10/18
TIME
Figure 21. Basin 3 dissolved oxygen uptake - Medfield - Phase 3A.
oe
i
LU
x
o
_
O
V)
to
45
40
35
30
25
20
15
10
0
I ,.,.., I ,....,,
•BASIN 3
' ' L
1
I . .
_L
9AM 9AM 9AM 9AM 9AM
11/14 11/15 11/16 11/17 11/18
TIME
Figure 22. Basin 1 and 3 dissolved oxygen uptake - Medfield
Phase 3B.
69
-------
900
z
— 800
LU
LU
700
600
500
LU
co 400
"—'
SHOCK LOADING
BASIN 4
' ' L.
J L
1
9AM 9AM 9AM 9AM 9AM
10/14 10/15 10/16 10/17 10/18
TIME
Figure 23. Thirty-minute settlometer reading Basin 4 - Med-
field - Phase 3A.
O
UU
CO
900
800
700
600
500
400
-i—i r
T—i 1—i—r
i i
SHOCK
LOADING
BASIN 4
9AM 9AM 9AM 9AM 9AM
11/14 11/15 11/16 11/17 11/18
TIME
Figure 24. Thirty-minute settlometer reading Basins 1 and 4
Medfield - Phase 3B.
70
-------
1000
900
800
cj
o
o
LU
tD
Q
_1
CO
Q
LU
CO
700
600
500
400
300
200
100
—BASIN 1
PHASE
3B
— 2B
I
0 5 10 15 20 25 30 45 60
SLUDGE SETTLING TIME (MIN)
Figure 25. Average settlometer readings Basin 4 - Medfield.
Figure 26. Settlometer supernatant turbidity levels increased
shortly after the shock loading for the sample taken from basin
1. A similar increase in turbidity occurred with the basin 3
sample after a lag period reflecting septage displacement
through the aeration tanks. Deterioration in supernatant qual-
ity was visually apparent as septage was added to the system.
71
-------
17
16
15
14
13
12
11
10
£ 7
6
5
4
1
0
i—i—rfi—'
BASIN 1
/ \
SHOCK LOADING AT 8:30 AM
1
1
1
1
1
7am 8 9 10 11 NOON 1pm
NOVEMBER 16, 1978
TIME
4 5pm /7am
11/17
Figure 26. Settlometer supernatant turbidity - Medfield - Phase 3B
72
-------
SECTION 6
RESULTS AT MARLBOROUGH
PHASE 1 - BASELINE FOR COMPARISON
Operating Parameters
During Phase 1 the plant received an average sewage flow of
0.12 cu m/sec (2.7 mgd) . This was slightly more than 50% of the
design flow rate. Since only one half of the treatment train
was in use, all operating clarifiers and aeration basins were
hydraulically loaded at their design capacities.
Phase 1 consisted of a ten-day monitoring period, followed
by a single day of inadvertant septage addition, a three-day re-
covery period and an additional seven days of no-septage moni-
toring. Process characteristics for Phase 1 are shown in Table
30.
Influent Characteristics
Average values and associated standard deviations for all
influent parameters monitored during Phase 1 are shown in
Table 31. Influent organic, nitrogen and phosphorus concentra-
tions characterize the wastewater as weak sewage. Total and
suspended solids concentrations classify it as a medium strength
sewage. Heavy metal concentrations were near or below values
recommended for drinking water standards. Measured concentra-
tions were relatively uniform throughout the monitoring period
except for the solids data, and standard deviations for these
were near or exceeded mean values, indicating large variability.
Primary Clarification
Removals of total BOD and suspended solids by primary clari-
fication averaged 17% and 52%, respectively, during Phase 1. COD
and total solids reductions averaged 22% and 33.5%, respectively,
These values, shown on Table 32, are lower than would be expec-
ted for a system operating at an overflow rate of 29 cu m/sq
m-day (712 gal/sq ft-day). The results were due to the weak
strength of the sewage.
17Metcalf and Eddy, Inc., Wastewater Engineering, p. 231,
73
-------
TABLE 30. PROCESS CHARACTERISTICS
MARLBOROUGH - PHASE 1
Characteristic
Mean Value
Flow Rate, Q, cu in/sec (mgd)
Sludge Return Rate, Stage #1, Qr, ,
cu m/sec (mgd)
Sludge Return Rate, Stage #2, Qr2 ,
cu m/sec (mgd)
Qr2/Q
Aeration Basin Retention, Stage #1, hrs
Aeration Basin Retention, Stage #2, hrs
Mixed Liquor Suspended Solids, Stage #1, mg/1
Mixed Liquor Vol. Susp. Solids, Stage #1, mg/1
Mixed Liquor Suspended Solids, Stage #2, mg/1
Mixed Liquor Vol. Susp. Solids, Stage #2, mg/1
F/M, kg BOD5/kg MLVSS/day, Stage #1
F/M, kg BOD5/kg MLVSS/day, Stage #2
F/M, kg TKN/kg MLVSS/day, Stage #2
Loading, Stage #1, gm BOD,-/cu m-day
(Ib BOD5/1000 cu ft-day)
Loading, Stage #2, gm BOD^/cu m-day
(Ib BOD5/1000 cu ft-day)
Loading, Stage #2, gm TKN/cu m-day
(Ib TKN/1000 cu ft-day)
Mean Cell Residence, Stage #1, SRT, , days
Mean Cell Residence, Stage #2, SRT2 , days
Oxygen Utilization, Stage #1, kg 09/kg BOD,.
^ D
Oxygen Utilization, Stage #1, kg 0,,/kg COD
Oxygen Utilization, Stage #2, kg 0,,/kg BOD,-
£' 3
Oxygen Utilization, Stage #2, kg O2/kg COD
Oxygen Utilization, Stage #2, kg 02/kg TKN
0.12 (2.7)
0.06 (1.4)
0.22 (5.0)
0.50
1.83
5.11
5.11
1490
1070
3420
2170
0.42
0.024
0.037
470
(29.3)
51.3
(3.2)
80.2
(5.0)
2.4
>60
1.15
0.53
18.5
9.7
10.2
Nitrogen and phosphorus concentrations were unaffected by
sedimentation. While there were some reductions in the concen-
trations of cadmium, chromium and copper, there was a small
74
-------
TABLE 31. INFLUENT, PRIMARY EFFLUENT,
SECONDARY EFFLUENT AND FINAL EFFLUENT
MARLBOROUGH - PHASE 1
Characteristics
COD - Total, mg/1
COD - Soluble, mg/1
BOD5 - Total, mg/1
BOD- - N - Suppressed
mg/1
Total Solids, mg/1
Total Volatile Solids
mg/1
Suspended Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Grease, mg/1
Alkalinity, mg/1 as
CaCO3
PH
Dissolved Oxygen, mg/1
Temperature
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Influent
x s
317
90
120
87
716
468
221
200
20
16
1.0
5.6
129
112
6.8
3.3
10
0.02
0.04
0.20
0.04
0.07
0.27
75
24
40
37
506
493
376
366
6.5
2.8
0.3
2.1
11
21
0.3
1.0
1.4
0.02
0.09
0.05
0.03
0.06
0-09
Primary
Effluent
x s
247
78
100
73
476
193
106
72
27
17
1.0
5.5
211
136
6.8
2.3
9.4
0.01
0
0.17
0.06
0.27
1.00
134
36
64
48
194
72
104
41
9.5
5.5
0.5
2.7
169
45
0.4
2.1
2.5
0.02
0
0.07
0.05
0.33
1.90
Secondary
Effluent
x s
55
37
11
4.1
358
111
10
7.6
17
13
3.2
1.0
52
89
6.8
4.4
10
0.02
0
0.75
0.05
0.14
0.72
17
Final
Effluent
x s
12
5
3
.1
.0
108
4
3
4
2
1
0
0
1
2
0.
1.
0.
0.
1.
68
.6
.8
.1
.8
.0
.5
19
31
.3
.6
.9
02
0
78
04
06
43
2
0
39
30
.6
.8
463
6
8
2
0
.9
.3
.1
.5
101
121
6
5
1
0
0
6
5
Q.
0.
0.
0.
0.
.7
.8
.7
.7
17
.7
13
50
.8
.9
10
01
0
09
05
09
13
7
6
0
0
4
0
0
1
2
0.
0.
0.
0.
0.
61
.9
.1
.9
.9
.5
.6
11
31
.4
.7
.5
01
0
05
04
12
06
increase in nickel. Lead and zinc both exhibited substantial
increases in average values but standard deviations for these
data exceeded the mean values.
75
-------
TABLE 32. MIXED LIQUOR
MARLBOROUGH - PHASE 1
Mixed Liquor
1st Stage
Mixed Liquor
2nd Stage
First
Compartment
Mixed Liquor
2nd Stage
Last
Compartment
Characteristic
Total Solids, mg/1
Total Volatile
Solids, mg/1
Suspended Solids,
mg/1
Volatile Susp.
Solids, mg/1
pH
Temperature , C
Alkalinity, mg/1
as CaCO.,
D. 0. Uptake,
mg/l-hr
Dissolved Oxygen, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N , mg/1
Nitrate-N, mg/1
Settlometer,
30 minutes ,ml/l
X
1,820
1,160
1,490
1,070
6.8
10
132
20
7.4
121
15
0.9
149
s
489
365
517
379
0.3
1.1
34
6.1
1-3
33
3.9
0.1
35
X
3,800
2,230
3,320
2,140
6.9
10
185
46
0.7
185
2.3
12
5
353
197
367
182
0.4
0.8
55
19
0.3
22
1.6
3.8
X
3,950
2,330
3,510
2,210
6.8
10
184
15
8.0
163
1.7
15
258
s
412
254
399
255
0.3
0.8
42
4.0
0.9
68
1.1
5.3
12
Secondary Treatment
Organic loadings on the secondary process (Stage 1) were
typical of conventional operations. The F/M ratio was 0.44 and
volumetric loading averaged 0.50 kg BOD5/cu m-day (31 Ib BODc/
1000 cu m ft-day). The ratio was typical of conventional
operation, even with the weak sewage, because of the low mixed
liquor suspended solids concentration (1,490 mg/1) and the
short aeration basin detention time (5.1 hours).
BOD removal in the secondary system averaged 89%. Removal
from influent to secondary effluent was 91%. Suspended solids
76
-------
removals, from influent to secondary effluent, averaged 95%,
eliciting a secondary effluent concentration of 10 mg/1.
Nitrogen loss or incorporation into cell tissue was very
small, amounting to only 1 mg/1. Ninety-five percent of the in-
fluent nitrogen was in the secondary effluent. This small
usage is not typical and cell incorporation of 5 to 6 mg/1 would
have been expected for this strength sewage. Nitrification
began in the secondary system (Stage 1), raising nitrates from
1 mg/1 in the influent to 3.2 mg/1 in the secondary effluent.
Aluminum sulfate added to the secondary aeration basins
for phosphorus removal, coupled with biological assimilation,
reduced phosphorus levels to 1.0 mg/1.
Dissolved oxygen levels remained high throughout Phase 1,
averaging 4.4 mg/1. Heavy metals (Cd, Cr, Ni, Pb and Zn)
remained at low concentrations. Only copper showed an increase
in average value from primary to secondary effluent. Again
variability in the copper concentration data was high.
Nitrification Stage
The nitrification stage (Stage 2) further reduced organic
concentrations: overall plant BOD5 removal was 98%. Nitrifica-
tion was essentially completed with final effluent nitrate
nitrogen, TKN and ammonia nitrogen averaging 17, 1.7 and 0.7
mg/1, respectively. From influent to final effluent only
1.6 mg/1 of nitrogen were assimilated.
Dissolved oxygen levels during Phase 1 (5.9 mg/1) and mixed
liquor volatile suspended solids concentrations (2,170 mg/1)
were both conducive to good nitrification system operation.
Solids retention time, SRT, for the nitrification system was not
calculated because of infrequent sludge wasting, but the SRT
was certainly in excess of the recommended 10-20 days.18 Both
temperature (10°C) and pH (6.8) were below values recommended
for optimum nitrification but the other parameters (D.O., MLVSS,
and SRT) offset the effect of low temperature and pH. The
BODs/TKN ratio for the influent to the nitrification stage was
0.65, a value which would support a relatively high fraction
of nitrifying organisms.
Solids Production
A volatile suspended solids, VSS, balance for Phase 1 is
shown in Table 33. Items included in the balance are influent
VSS, VSS removed with the vacuum filter cake, changes in mixed
18
Ibid., p. 667.
77
-------
liquor volatile suspended solids inventory for each of the
aeration stages and the production of VSS by conversion of waste
organics to cells. Production was the computed difference be-
tween inputs and outputs. A balance of VSS was preferred to a
total suspended solids balance because of the large amounts
of ferric chloride and lime used in waste sludge conditioning.
TABLE 33. VOLATILE SUSPENDED SOLIDS BALANCE
MARLBOROUGH - PHASE 1
Sample
Volatile
Input
Suspended Solids
Output
Influent, kg/day
(Ib/day)
Effluent, kg/day
"(Ib/day)
Change in MLVSS, kg/day
Stage #1, (Ib/day)
Change in MLVSS, kg/day
Stage #2, (Ib/day)
Cake, kg/day
(Ib/day)
Biological Sludge kg/day
Production, (Ib/day)
Totals , Kg/day
(Ib/day)
953
(2,102)
12
(27)
672
(1,482)
1,637
(3,611)
23
(50)
(211)
465
1,404
(3,096)
1,638
(3,611)
The sludge yield factor, based upon computed sludge produc-
tion values, was 0.29 kg of VSS produced per kg of BOD5 removed.
This value is lower than the expected value, Y
equation:
obs1
given by the
obs
k,e
d c
where the mean cell residence time, 6C, was 2.4 days in the sec-
ondary system and published values for the endogenous decay rate,
k,, and yield without decay, Y, are 0.055 days~l and 0.5 kg VSS
78
-------
produced per kg BOD5 removed. The equation given an expected
Yobs of 0.44. The difference in expected and recorded yield
factors is most likely due to a change in the solids inventory
carried in the clarifiers between wasting periods.
Heavy metals were concentrated in the filter cake with con-
centrations on a dry solids basis, ranging from 0.01% for cad-
mium to 0.73% for zinc.
Vacuum filter filtrate at Marlborough was a strong waste
stream with obnoxious characteristics. It has high COD, BOD,
TKN, and ammonia concentrations as well as a high pH. Metal
concentrations were low, probably as a result of hydroxide pre-
cipitation. The odor of this is as unpleasant as that of v
septage. CSee Tables 34 and 35.) Ferric chloride and lime usage
averaged 152 kg/day (334 Ib/day) and 2,950 kg/day (6,486 lb/
day), respectively.
PHASE 2 - CONTINUOUS FEEDING
Process Characteristics
Operating parameters for the constant feed studies, Phases
2A and 2B, are shown on Table 36. Influent flow averaged 0.103
cu m/sec (2.3 mgd) during Phase 2A and 0.12 cu m/sec (2.75 mgd)
during Phase 2B. These flows were close to the average Phase
1 flow rate, 0.12 cu m/sec (2.7 mgd). In each of the Phase 2
studies mixed liquor solids concentrations and clarifier and
aeration basin retention times were similar to Phase 1 values.
Processes were operated at near hydraulic design capacities.
Septage loading averaged 110 cu m/day (29,000 gals/day) in
Phase 2A. The test lasted three days with a septage volume
equal to 1.25% of the average daily sewage flow rate. The
organic material added by septage was mostly removed in primary
clarification. As a result, organic loading, mean cell residence
time and oxygen utilization in the secondary and nitrification
stages were almost identical to baseline values (Compare
Tables 30 and 36). Increased loading due to septage organics
passing the primary clarifier was offset by a 15% reduction in
sewage flow.
In Phase 2B 375 cu m (99,000 gals) of septage were added
over a period of 42 hours. The septage volume was 2.14% of
the average daily sewage flow rate. Process characteristics
shown on Table 36 indicate that septage did not increase
secondary and nitrification process loading during this period.
Influent Characteristics
Sewage characteristics for Phase 2 are shown in Tables 37
and 38 and can be compared with baseline values in Table 31.
79
-------
TABLE 34. RETURN SLUDGE AND COMBINED SLUDGE
MARLBOROUGH - PHASE 1
Characteristics
Returned
Sludge
1st Stage
x s
Returned
Sludge
2nd Stage
x s
Combined
_Sludge
x s
COD-Total, mg/1
COD-Soluble, mg/1
BCD-Total, mg/1
BOD-N Suppressed
Total Solids, mg/1, % 3,640 1,650 5,920 931 47,100 13,200
Total Volatile Solids,
mg/1, % 2,550 1,420 3,520 548 30,100 8,700
Suspended Solids, mg/1 3,180 1,660 5,450 925 44,200 12,500
Volatile Susp. Solids
mg/1 2,390 1,420 3,420 547 28,000 8,250
PH
Total Kjeldahl-N, mg/1 284 179 324 105 l.,540 657
Ammonia-N, mg/1 16 6.2 3.6 3.2 225 157
Nitrate-N, mg/1 1.7 3.1 12 5.8 6.4 3.4
Total Phosphorus, mg/1 1,010 338
Capillary Suction Time, sec 14 8.2 8.3 1.2 359 103
Metals, rag/kg dry cake
Cadmium 0.45 0.18
Chromium 7.50 3.85
Copper 29.90 14.21
Nickel 3.47 1.43
Lead 9.97 3.55
zinc 26.38 13.43
Sewage was weak during the test with small increases observed
during the Phase 2B period. In this second constant feed test
COD increased 12%, BOD 41%, suspended solids 23% and TKN 270%
over baseline values. Total solids decreased 21%.
Characteristics of septage used in Phase 2 and calculated
concentrations of the combined sewage and septage influent are
also shown on Tables 37 and 38. The septage was quite strong.
It effectively doubled the organic and phosphorus loading on the
80
-------
TABLE 35. VACUUM FILTER FILTRATE AND CAKE
MARLBOROUGH - PHASE 1
Characteristics
COD-Total, mg/1
COD-Soluble, mg/1
BOD-Total, mg/1
BOD-N Suppressed
Total Solids, mg/1, %
Total Volatile Solids,
mg/1, %
Suspended Solids, mg/1
Volatile Susp. Solids,
mg/1
pH
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Vacuum
Vacuum Filter
_Filtrate _ Cake
X S X S
5,080
4,170
3,250
2,720
7,880
2,230
927
227
12.1
662
381
14
25
960
1,110
1,050
1,210
1,710 25.6 3.3
697 9.3 1.6
193
41
0.1
933
143
5,7
18
Metals, mg/1,
mg/kg dry cake
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
0.06
0.04
0.40
0.37
0.47
0.87
0.02
0.10
0.05
0.08
0.07
1.00
121
1,231
4,142
735
1,726
7,339
19
443
771
100
336
1,470
plant in Phase 2A. Solids and nitrogen loading increased by
about 30%. Septage nearly tripled the COD loading in Phase 2B
and doubled the solids and phosphorus loads.
Primary Effluent
A comparison of Tables 37 and 39 shows the effects of pri-
mary clarification on the combined sewage-septage influent for
81
-------
TABLE 36. PROCESS CHARACTERISTICS
MARLBOROUGH - PHASE 2
Phase . 2A 2B
Flow Rate, Z, cu m/sec (mgd) 0.103 (2.3) 0.12 (2.75)
Septage Feed Rate, cu m/day (gpd) 110 (29,000) 216 (57,000)
Septage/Sewage, % 1.25 2.14
Sludge Return, Stage #1,
cu m/sec (mgd) 0-067 (1.5) 0.07 (1.6)
Sludge Return, Stage #2,
cu m/sec (mgd) 0.245 (5.6) 0.28 (6.4)
Aeration Retention, Stage #1, hrs 5.91 4.91
Aeration Retention, Stage #2, hrs 5.91 4.91
MLSS , Stage #1, mg/1 1,197 1,480
MLVSS, Stage #1, mg/1 947 1,150
MLSS , Stage #2, mg/1 3,409 3,417
MLVSS, Stage #2, mg/1 2,147 2,180
F/M, kg BOD5/kg MLVSS-day, Stage #1 0.45 0.54
F/M, kg BOD5/kg MLVSS-day, Stage #2 0.017 0.017
F/M, kg TKN/kg MLVSS-day, Stage #2 0.034 0.034
Loading, Stage #1, gm BOD,-/cu m-day 423 625
(Ib BOD5/1000 cu ft-day? (26.4) (39.0)
Loading, Stage #2, gm BOD^/cu m-day 35.8 36.9
(Ib BOD5/1000 cu ft-dayl (2.23) (2.3)
Loading, Stage #2, gm TKN/cu m-day 74.1 73.8
(Ib TKN/1000 cu ft-day) (4.62) (4.6)
Mean Cell Residence, Stage #1, days 2.5 3.69
Mean Cell Residence, Stage #2, days >6Q >60
Oxygen Use, Stage #1, kg 02/kg BOD5 1.11 0.69
Oxygen Use, Stage #1, kg 02/kg COD 0.42 0.40
Oxygen Use, Stage #2, kg 02/kg BOD5 31.7 17.31
Oxygen Use, Stage #2, kg 02/kg COD 13.2 13.20
Oxygen Use, Stage #2, kg 02/kg TKN 14.1 8.45
Phase 2A. Solids added with septage increased both suspended
and total solids concentrations in the primary effluent. Pri-
82
-------
TABLE 37. SEWAGE, SEPTAGE AND COMBINED INFLUENT
Characteristic
COD-Total, mg/1
COD-Soluble, mg/1
BOD5~Total, mg/1
BOD^-N Suppressed, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Grease, mg/1
pH
Temperature , C
Alkalinity mg/1 as CaC03
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Sewage
x s
305
96
129
112
707
537
280
234
26
20
1.3
5.5
171
6.9
12
132
0.01
0
0.19
0
0.05
0.29
62
25
8.1
15
245
310
118
117
0,7
1.4
0.3
1.2
66
0
0
2.3
0.01
0
0,04
0
0.07
0.01
Septage
x s
24,500
7,410
5,900
16,970
12,420
14,530
10,780
730
170
480
1,643
6.4
830
0.02 0.02
2.0 0.74
18.3 4.1
0.78 0.14
2.9 0.76
4.9 1.8
Combined
Sewage and
Septage *
602
218
183
907
683
455
363
35
22
11
189
6.9
142
0.01
0.02
0.41
0.01
0.08
0.35
*Calculated concentrations
mary effluent suspended solids averaged 199 mg/1 during Phase
2A and only 106 mg/1 in Phase 1. COD values were much higher
during the period but total BOD5 did not change. Septage caused
an increase of about 22% in TKN levels and 64% in ammonia.
Phosphorus levels in primary effluent were unaffected by septage
addition.
83
-------
TABLE 38. SEWAGE, SEPTAGE AND COMBINED INFLUENT
MARLBOROUGH - PHASE 2B
Characteristic
COD-Total, mg/1
COD-Soluble, mg/1
BOD5-Total, mg/1
BODj--N Suppressed, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Susp. Solids,
mg/1
Total Kjeldahl-N, mg/1
Ammon i a-N , mg/ 1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Grease, mg/1
pH
Temperature , °C
Alkalinity, mg/1 as CaCO.,
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Sewage
x s
354 115
73 14
169 44
120 7.8
564
308
272
246
54 16
13 2.1
0.9 0.3
5.3 2.8
209
6.7 0.1
12 0
117 7.8
0
0
0.20
0
0.18
0.28
Combined Sewage
and
Septage Septage *
X X
27,500
11,180
8,450
18,940
14,450
15,270
12,160
640
100
220
3,121
4.6
0
0.08
1.0
13.4
0.16
2.0
15.0
905
393
289
937
595
577
488
66
15
9.7
268
6.7
115
0
0.02
0.48
0
0.22
0.59
*Calculated concentrations
The primary clarifier removed 49% of the combined influent
COD, 53% of the BOD5 and 56% of the suspended solids, in
Phase 2A. This compares with Phase 1 COD, BOD5 and suspended
solids removals of 22%, 17%~and 52%, respectively.
84
-------
TABLE 39. PRIMARY EFFLUENT, SECONDARY EFFLUENT
AND FINAL EFFLUENT
MARLBOROUGH - PHASE 2A
Characteristic
COD-Total , mg/1
COD-Soluble, mg/1
BOD5~Total, mg/1
BODg-N Suppressed, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Susp. Solids,
mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
» Grease, mg/1
pH
Temperature , °C
Dissolved Oxygen, mg/1
Alkalinity, mg/1 as CaCO3
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Primary
Effluent
x s
310
98
103
69
592
298
199
137
33
28
0.9
5.4
135
7.2
12
2.0
192
0
0
0.20
0.05
0.09
0.56
16
26
13
4.8
57
91
25
15
0.9
7.0
0.1
5.4
35
0.1
0
1.9
2.0
0
0
0.06
0.07
0.12
0.05
Secondary
Effluent
x s
62
52
8.7
2.6
395
158
18
9
18
17
4.4
0.8
35.2
7.1
13
2.1
106
0.02
0
0.06
0.05
0.08
0.12
24
18
6.9
0.6
54
23
4.4
6
0.5
2.1
0.5
0.1
0.2
0
1.4
30
0.02
0
0
0.03
0.11
0.01
Final
Effluent
x s
45
38
1.6
1.1
479
237
18
15
2.0
0.5
20
1.4
6.2
6.9
13
5.5
46
0.02
0
0.17
0
0.06
0.68
4.3
2.3
0.7
0.1
23
12
12
10
0.3
0.2
0.6
0.8
0.9
0.2
0
0.5
7.8
0.02
0
0.13
0
0.08
0.30
At the 2.14% loading, Phase 2B, primary effluent was only
slightly stronger than concentrations measured during Phase 1.
Primary effluent concentrations are shown in Table 40 Table
41 shows a comparison of Phase 2B and Phase 1 influent and
85
-------
TABLE 40. PRIMARY EFFLUENT, SECONDARY EFFLUENT
AND FINAL EFFLUENT
MARLBOROUGH - PHASE 2B
Characteristic
COD-Total, mg/1
COD-Soluble, mg/1
BOD5-Total, mg/1
BODt--N Suppressed, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended' Solids ,
mg/1
Volatile Susp. Solids,
mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus,
mg/1
Grease, mg/1
PH
Dissolved Oxygen,
mg/1
Temperature, °C
Alkalinity, mg/1
as CaCO.,
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Primary
Effluent
x s
255
80
128
76
477
206
143
101
20
0.8
6.1
6.9
1.4
13
156
0
0
0
64
15
28
20
60
92
31
38
5.8
0.1
0.5
914
0.2
0.9
1.0
6.7
0
0
.16
.10
.14
8.6
Secondary
Effluent
x s
46
33
7.8
1.9
364
82
10
7.3
13
2.7
0.9
51
6.7
3.0
14
98
0.
0.
0.
0.
0.
0.
4.5
15
3.4
0.4
22
57
0.6
1.2
6.0
0.7
0.6
.2
0.2
1.2
0.6
18
03
50
09
11
07
21
Final
Effluent
x s
38
34
1.7
0.6
489
164
13
8.0
1.0
18
1.0
24
6.5
5.7
13
38
0.
0.
0.
2.4
10
0.5
0.5
14
62
4.0
2.6
1.0
2.5
0.4
.8
0.1
0.7
0.7
2.9
0
0
07
10
0
32
86
-------
TABLE 41. RATIOS OF CHARACTERISTICS
MARLBOROUGH - PHASES 2A & 2B
Characteristics
COD-Total, mg/1
COD-Soluble, mg/1
BOD5-Total , mg/1
BOD5~N Suppressed, mg/1
Total Solids, mg/1
Total Vol. Solids, mg/1
Suspended Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N , mg/1
Total Phosphorus, mg/1
Alkalinity, mg/1
as CaCO-,
Influent
Phase 2A Phase 2B
Phase 1
1.90
1.82
2.10
1.27
1.46
2.06
1.82
1.75
1.38
1.96
1.27
Phase 1
2.85
3.28
3.32
1.31
1.27
2.61
2.44
3.30
0.94
1.73
1.03
Primary
Phase 2A
Phase 1
1.26
1.26
1.03
0.95
1.24
1.54
1.88
1.90
1.22
0.90
0.98
1.41
Effluent
Phase 2B
Phase 1
1.03
1.11
1.28
1.04
1.00
1.07
1.35
1.40
1.22
1.18
1.11
1.15
primary effluent characteristics. The ratios listed on Table
41 clearly show that a three-fold increase in combined influent
COD, BOD5 and suspended solids yielded almost no increase in
primary effluent COD and about a 30% increase in BOD5 and sus-
pended solids.
Efficiency of removal in Phase 1 and in Phase 2B is con-
trasted in Table 42. Low percent removals shown for Phase 1
were due to the weak strength of the sewage. The high percen-
tages shown for Phase 2B on Table 42 indicate that a large
fraction of the organic material in septage is associated with
suspended solids which are readily settled in primary clarifica-
tion.
Secondary Treatment
A comparison of Tables 31 and 39 shows that a septage/
sewage feed ratio of 1.25%, Phase 2A, caused no noticeable
deterioration in secondary effluent quality. Secondary effluent
suspended solids increased but remained well within regulatory
standards, averaging 18 mg/1. In contrast, the total BOD5
87
-------
TABLE 42. EFFICIENCY OF PRIMARY CLARIFIERS
MARLBOROUGH - PHASES 2A & 2B
Percent Removal
Characteristics Phase 1 Phase 2A Phase 2B
COD-Total, mg/1
COD-Soluble, mg/1
BODr-Total, mg/1
BOD,--N Suppressed, mg/1
Total Solids, mg/1
Total Vol. Solids, mg/1
Suspended Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, rag/1
Ammonia-N, mg/1
Total Phosphorus, mg/1
22
13
17
16
34
59
52
64
-35
- 6
2
49
53
62
35
56
56
62
6
-27
51
72
67
74
49
65
75
79
50
-33
37
dropped about 20% to 8.7 mg/1. Efficiencies of BODn and sus-
pended solids removal in the secondary treatment units alone
averaged 92% and 91%, respectively, during Phase 2A.
The aerator settings remained the same during Phases 1
and 2A but average secondary effluent dissolved oxygen levels
dropped from 4.4 to 2.1 mg/1. This was unexpected since the
F/M ratios were the same (0.45 for Phase 2A and 0.42 for Phase
1) as were dissolved oxygen uptake rates (18 mg/l-hr for Phase
2A and 20 mg/l-hr for Phase 1). The difference in dissolved
oxygen concentration was probably caused by surges in influent
flow, transferring high D.O. water from the aeration basin to
the secondary clarifier. Oxygen measurements were not taken at
exactly the same time each morning.
Mixed liquor volatile suspended solids were 12% lower dur-
ing Phase 2A, averaging 947 mg/1. This value is low when com-
pared with conventional activated sludge practice, but effluent
quality remained excellent. Mixed liquor data are shown in
Table 43.
In Phase 2B, primary effluent BOD loading and the F/M
ratio were higher than in Phase 1 and 2A. The F/M ratio
(0.54 kg BOD5/kg MLVSS-day) was about 25% higher than that used
for conventional activated sludge processes. Mean cell resi-
dence time increased from 2.4 and 2.5 days during Phases 1 and
88
-------
TABLE 43,, MIXED LIQUOR
MARLBORQUGH - PHASE 2A
Mixed Liquor Mixed Liquor
2nd Stage 2nd Stage
Mixed Liquor First Last
1st Stage Compartment Compartment
Characteristics x s x s x s
Total Solids, mg/1 1,630 234 3,837 221 3,853 792
Total Volatile Solids,
mg/1 1
Suspended Solids, mg/1 1
Volatile Susp. Solids,
mg/1
pH
Temperature, °C
Alkalinity, mg/1 as CaCO,.
D. 0. Uptake, mg/l-hr
Dissolved Oxygen, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1 .
Settlometer, 30 mi n , ml/1
,110
,197
947
6.9
13
154
18
6.5
131
17
1.1
123
223
196
181
0.1
0
15
2.1
1.0
22
4.0
0.4
2.9
2,327
3,450
2,130
6.7
13
180
66
0.6
198
2.2
14
129
425
175
0.1
0
11
6.0
0.3
37
1.7
2.5
2,337
3,367
2,163
6.7
13
167
11
7.8
223
0.8
17
223
512
773
480
0.1
0
6.1
2.1
0.8
22
0.6
1.7
5.8
2A, respectively, to 3.7 days in Phase 2B. Average character-
istics of the secondary effluent are shown in Table 40. In
every case, contaminant levels were equal to or less than those
of Phase 1, despite the addition of septage at a septage/sewage
ratio of 2.14% BOD and suspended solids removal efficiencies
in the secondary treatments alone averaged 94% and 93%, res-
pectively.
There was a drop in the effluent dissolved oxygen from 4.4
mg/1 in Phase 1 to 3.0 mg/1 in Phase 2B. This change can be
attributed to the change in temperature from 10°C in Phase 1
to 14°C in Phase 2B.
The mixed liquor volatile suspended solids concentration
was about the same in Phases 1 and 2B and settleability remained
good (SVI averaged 127 ml/gram). The increase in the F/M ratio
in Phase 2B did not raise the oxygen utilization rate; in fact,
there was a slight decrease from Phase 1 of about 15%. These
data are shown in Table 44.
89
-------
TABLE 44. MIXED LIQUOR
MARLBOROUGH - PHASE 2B
Mixed Liquor Mixed Liquor
2nd Stage 2nd Stage
Mixed Liquor First Last
1st Stage Compartment Compartment
Characteristics x s x s x
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Susp. Solids
mg/1
PH
Temperature , °C
Alkalinity, mg/1 as CaCO-,
D. 0. Uptake, mg/l-hr
Dissolved Oxygen, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Settlometer, 30 minutes.ml,
1,870
1,270
1,480
1,150
6.9
13
140
17
6.1
177
14
0.9
/I 188
389
303
272
221
0.2
0.6
14.8
2.7
1.2
32
5.6
0-2
42
3,337
1,960
2,933
1,887
6.6
13
134
32
0.5
247
5.1
13
1,947
1,182
1,896
1,157
0.1
0.6
11
29
0.2
56
5.1
4.2
4,307
2,557
3,900
2,473
6.6
13
156
11
8.2
293
1.0
15
213
284
112
252
55
0.2
0.6
13
1.4
0.1
104
0.3
4.4
5.8
Nitrification Stage
Performance of the nitrification stage in Phase 2 was
almost identical to that of Phase 1. The only exception was a
slight increase in suspended solids and in the fraction of total
volatile solids. Nitrification was almost complete with the
effluent averaging 18 to 20 mg/1 nitrate-N and containing only
2.0 mg/1 TKN and 0.5 to 1.0 mg/1 ammonia-N.
Final effluent quality was not affected by the addition of
the septage, with the possible exception of the grease content,
which was significantly higher in Phase 2 than during background
monitoring. It should be recognized that this conclusion is
based on only one grease analysis during Phase 2B.
90
-------
Biological Solids Production
Throughout Phases 1, 2A and 2B no intentional sludge wast-
age occurred from the nitrification section of the plant. Pri-
mary sludge and excess first stage activated sludge were rou-
tinely wasted. Because of the short duration of Phases 2A
and 2B, meaningful solids balances could not be made.
Since organic loadings on secondary and nitrification
stages were not increased by addition of septage up to 2.14%, no
increase in excess activated sludge was expected. Increases in
primary effluent concentrations shown in Table 41 were caused
by corresponding increases in influent sewage levels. The
increased solids handled by the plant were derived from suspen-
ded solids added to the primary clarifier by septage. For
Phase 2A this increase amounted to 1,597 kg/day (3,514 Ib/day)
and for Phase 2B, 3,300 kg/day (7,260 Ib/day). Using the data
for SRT and MLSS in Stage #1, septage increased wasted solids
by 54% during Phase 2A and 100% during Phase 2B.
Characteristics of the return sludge, combined sludge,
vacuum filter filtrate and cake were similar during septage
addition phases. Data are shown in Tables 45, 46 and 47.
Conditioning of sludge was accomplished using ferric
chloride and lime. Operating records indicated an average
ferric chloride dosage of about 3% on a dry solids basis. This
was a typical value. In contrast, lime dosage averaged 60%
based on dry solids. This usage is six to eight times normal
values.
PHASE 3 - SHOCK LOADING
The first shock loading test at Marlborough, Phase 3A,
lasted three days. At 7 a.m. each morning 79.5 cu m (21,000
gals) of septage was added to the primary clarifier within a
period of thirty minutes. Sewage flow during this test averaged
9,590 cu m/day (2.53 mgd). The septage/sewage flow ratio was
0.83% on a total daily quantity basis. The instantaneous
septage/sewage ratio for the thirty-minute period of septage
addition was about 30%.
The second shock loading test, Phase 3B, lasted two days.
At 7 a.m. each morning 148 cu m (39,000 gals) of septage were
released from storage: 79.5 cu m (21,000 gals) during the first
thirty minutes and the remainder over the next one and one-half
hours. In addition, 45.4 cu m (12,000 gals) were added at
2 p.m. on the second day. The septage/sewage ratio was 1.8% on
the first day and 2.3% on the second day.
91
-------
TABLE 45. RETURN SLUDGE AND COMBINED SLUDGE
MARLBOROUGH - PHASE 2A
Characteristic s
Total Solids, mg/1
Total Vol. Solids, mg/1
Susp. Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
CST, sec.
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Return
Sludge
1st Stage
x s
2,700 373
1,860 335
2,260 361
1,640 351
206 34
18 1.0
1.2 0.3
11 1.4
0.78 0.25
12.6 4.8
46.2 3.1
5.0 1.1
13.5 2.3
15.3 0.64
TABLE 46. RETURN SLUDGE AND
Return
Sludge
2nd Stage
x s
6,710 364
4,120 151
6,210 341
3,920 181
335 9.9
1.5 1.0
13 3.2
8.0 0.9
0.07 0.01
0 0
0.38 0.01
0.29 0.02
0.46 0.06
0.51 0.14
Combined
Sludge
x s
63,780 4,270
35,510 2,770
58,960 4,920
42,360 2,840
1,820 317
152 109
12 1.7
1,870 601
309 154
150 18.4
1,057 344
4,529 354
631 166
1,817 51.6
9,463 5,008
COMBINED SLUDGE
MARLBOROUGH - PHASE 2B
Characteristics
Total Solids, mg/1
Total Vol. Solids, mg/1
Susp. Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
CST, sec.
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Return
Sludge
1st Stage
x s
3,220 546
2,240 353
2,520 62
2,130 312
261 78
12 2
0.9 0.2
18 9.4
Return
Sludge
2nd Stage
x s
5,990 754
3,667 601
5,520 709
3,547 575
412 40
2.3 0.9
11 5.8
8.7 0.4
Combined
Sludge
x s
68,090 7,040
36,720 1,820
62,670 5,630
33,720 1,460
1,980 40
300 40
13 2.6
1,230 475
327 97
0.60 0.05
11.2 0
42.8 0.38
2.40 0.28
9.60 0.35
13.3 1.61
92
-------
TABLE 47. VACUUM FILTER FILTRATE AND CAKE
MARLBORQUGH - PHASE 2A & 2B
Characteristic s
2A - Vacuum Filter
Filtrate Cake
x s x
2B - Vacuum Filter
Filtrate Cake
x s x
COD-Total, mg/1
COD-Soluble, mg/1
BOD5-Total, mg/1
BOD5-N Sup. , mg/1
Tot. Solids, mg/1, (%)
Tot. Vol. Solids,
mg/1 (%)
Susp. Solids, mg/1
Vol. Susp. Solids,
mg/1
PH
Total Kjeldahl-N,
mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Tot. Phosphorus, mg/1
Metals, mg/1, mg/kg
dry cake
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
4,880
4,000
2,897
2,590
8,000
2,390
893
267
12
420
410
93
12
0.07
0
0.38
0.29
0.46
0.51
149
79
443
265
478
340
436
97
0
16
42
25
3.3
0.01
0
0.01
0.02
0.06
0.14
(25.1)
( 8.8)
150
1,057
4,529
631
1,817
9,463
8,090
2,030
1,030
350
11.9
383
347
13
15
0.05
0
0.38
0.28
0.35
1.61
269
711
259
26
0.1
0
50
3.5
8.4
(26.6)
( 9.3)
189
1,891
4,312
605
2,043
6,052
Sewage and Septage Characteristics
Phase 3 sewage was characteristic of a weak to moderate
strength domestic waste and similar to influent monitored during
the baseline period. Average values for both shock load periods
are shown on Table 48. These values can be compared with base-
line characteristics on Table 31.
Average septage characteristics for the period are also
shown on Table 48. Septage used for the two tests was compara-
tively strong with COD and total solids averaging 28,500 mg/1
and 17,400 mg/1, respectively. Daily septage and sewage charac-
teristics values for Phase 3 are given in Appendix Tables 1-1
and 1-2.
Primary Effluent
An effect of large septage inputs to a primary clarifier
is apparent in Figures 27 through 30. In all cases organic
and solids concentrations in the primary effluent increased
93
-------
TABLE 48. SEWAGE AND SEPTAGE CHARACTERISTICS
MARLBOROUGH - PHASE 3
Characteristics
COD-Total, mg/1
COD-Soluble, mg/1
BOD-Total, mg/1
BOD-N Sup. , mg/1
Total Solids, mg/1
Tot. Vol. Solids, mg/1
Susp. Solids, mg/1
Vol. Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Alkalinity, mg/1 as CaCO_
PH
X
334
99
116
64
503
269
209
188
35
19
1.2
126
6.7
Sewage
s
50
43
28
21
76
101
158
150
15
2.6
0.5
11
0.1
Septage
X
28,500
7,950
6,660
17,400
12,700
15,200
11,400
637
213
900
5.4
600
500
400
300
y 200
z
o
o 100
9AM
9AM
9AM
9AM
5/30
5/31
TIME
6/1
6/2
Figure 27.
Primary effluent COD and BOD
3A.
Marlborough - Phase
94
-------
1100
1000
900
800
700
2 60°
500
o
o
400
300
200
100
T T
SHOCK
LOADING
9AM 9AM
6/7 6/8
TIME
9AM
6/9
Figure 28. Primary effluent COD and BOD- - Marlborough -
Phase 3B.
very shortly after beginning the feeding operation. Figures 27
and 28 show that COD and BOD5 values increased significantly
within one hour of beginning the test, reached a maximum value
within one and one-half and two hours, and declined to back-
ground levels within four to six hours. Total and suspended
solids data on Figures 29 and 30 show the same result. Peak
values were reached in about one-third the clarifier design
retention time. Septage addition was directly related to peak
concentrations. Peak COD and BODg values during Phase 3B were
about twice as high as during Phase 3A. While the short time
95
-------
700
600
^ 500
Z
O
— 400
OL
LLJ
O
z
o
o
300
200
100
0
TOTAL SOLIDS
SUSPENDED SOLIDS
9AM 9AM 9AM
5/30 5/31 6/1
TIME
9AM
6/2
Figure 29. Primary effluent total and suspended solids
Marlborough - Phase 3A.
increase in organic and solids concentrations observed during
Phase 3 were dramatic, the impact on 24-hour composited samples
was not significant.
Dilution and clarification in the primary clarifier were
analyzed by considering the shock load a step input and by
comparing the effluent peak values with the theoretical con-
centration of the step input. If material were conserved and
moved in pl~ug flow, the ratio of input concentration to peak
concentration would be 1.0. Calculation of the step input
concentration was done by mass balance over the one-half hour
loading period. Septage-sewage chemical characteristics ob-
viously are not conservative in the liquid fraction, but ratios
would be much higher if the mixture followed a plug flow mode.
For example, a typical suspended solids influent to effluent
ratio for sewage is 0.2 to 0.4. For the sewage-septage mix-
ture this ratio would probably be somewhat lower because of the
heavy nature of some septage suspended solids, but not as low
as the calculated value, 0.1, unless significant short circuit-
ing and/or intermixing existed.
96
-------
9AM
6/7
9AM
6/8
TIME
9AM
6/9
Figure 30. Primary effluent total and suspended solids
Marlborough - Phase 3B.
Primary Clarification
During Phase 3B samples were taken from the primary clari-
fier before shock loading and periodically after loading.
Samples were taken from a point one-half the distance from inlet
to effluent weir and at depths of 0.3, 1.5, and 3.0 meters. In
addition, samples were taken at the same times from the effluent
weir. All samples were analyzed for total solids.
Septage was introduced during Phase 3B at the rate of 2.65
cu m/min (700 gpm) for the first 38 minutes and then at 0.56
cu m/min (150 gpm) for the following 82 minutes.
Figure 31 shows total solids concentrations found as a
function of depth of the various sampling times. It can be
97
-------
0.0
05
QC
CJ 1.0
<
li-
ce
2.0
Q.
LU
Q
3.0
7AM
I
1 I I
SEPTAGE LOADING
- 7:40, 700 GPM
00, 150 GPM
NOON
10AM 9AM SAM 7:30AM 8:30AM
I
I
200 400 600 800 1000 1200
TOTAL SOLIDS CONCENTRATION (MG/I_)
1400
Fig-are 31. Primary clarifier total solids profiles -
Marlborouqh - Phase 3,
seen that the concentration levels increased with depth through-
out the loading period (between 7 a.m. and 9 a.m.). Peak values
occurred near the end of the loading period. After 8:30 a.m.
concentrations steadily declined and were comparatively more uni-
form with depth.
In Figure 32 concentration values are plotted against time.
Effluent concentrations reach a maximum at the same time as
those taken at the intermediate depth. This indicates that a
significant amount of mixing and short circuiting occurred. The
time to reach maximum values was about two-thirds of the theo-
retical detention time.
98
-------
SEPTAGE LOADING
7:00 - 7:40, 700 GPM
7:40 - 9:00, 150 GPM
3.0 METER DEPTH
EFFLUENT
400
200
I
7AM
SAM
9AM
10AM
TIME
11AM
NOON
Figure 32. Primary clarifier total solids distribution
Marlborough - Phase 3.
Further substantiation of this non-ideal behavior is shown
in Figures 33 and 34. Figure 33 shows two effects of impulse
loading on a sedimentation tank: ideal plug flow and displace-
ment with dispersion. Figure 34 shows a similar dimensionless
99
-------
2.5
2.0
c/c,
1.5
1.0
0.5
0.0
IDEAL PLUG FLOW
DISPLACEMENT AND
DISPERSION
I
0.5 1.0 1.5 2.0
TIME / DETENTION TIME (t/T)
Figure 33. Clarifier effluent responses to a pulse input,
plot of Phase 3B data. While the septage loading was not truly
an impulse input, the resulting effluent curve (Figure 34) is
similar to that of a system exhibiting a large amount of dis-
persion.
The data suggest that as septage enters the clarifier,
a portion of the solids rapidly falls to lower levels, causes
100
-------
o
o
o
CO
Q
O
CO
P 0.2
LU
CO
Q
o.i
LU
UJ
/
- /
- /
/
-/
V i
/ E SEPTAGE ADDED
1
1
I
1
150
125
O
100 g
Q
Q
75 <
50
25
LU
CD
<
I-
o.
LU
0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6
TIME / DETENTION TIME (t/j)
Figure 34. Primary clarifier, effluent total solids/influent
total solids - Marlborough - Phase 3,
turbulence and creates density currents which mix the septage•
with the tank contents. This effect produces the rapid rise
in effluent solids concentration.
Although short circuiting occurred, the primary clarifier
performed very well from the standpoint of suspended solids
101
-------
removal. Considering an eleven-hour period, beginning with the
shock load, the clarifier received 3,890 kg (8,550 Ibs) of in-
fluent suspended solids and passed only 727 kg (1,600 Ibs) over
the weir. The removal efficiency was 81 percent. The high
removal efficiency is a result of a significant removal of heavy
particles associated with septage. .At the end of this eleven-
hour period, suspended solids levels in the effluent had fallen
to values similar to pre-shock conditions.
Secondary Treatment
The impact of septage on the secondary process at Marl-
borough is shown on Figures 35 through 46. Detailed results
are presented in the Appendix Table 1-4.
Effluent COD levels in Phase 3 were generally higher than
observed during Phase 1, but septage seems to have had little
impact on this observation, since pre-shock and post-shock levels
were also high. Figures 35 and 36 show that in three days
COD increased significantly after septage addition. The elevated
COD may have represented refractory organics associated with
septage but may also have been caused by morning sewage flow
surges. In any event, COD increases were of small magnitude and
not accompanied by corresponding increases in BOD,.,
/-^ 120
_J
Sp 100
g 80
I—(
K
5 60
LU
O
40
o
<-> 20
I ' ' ' I
SHOCK
LOADING
9AM 9AM 9AM 9AM
5/30 5/31 6/1 6/2
TIME
Figure 35. Secondary effluent COD and BOD^ - Marlborough -
Phase 3A.
102
-------
100
80
2 60
<
OC.
o
o
40
20
9AM
6/7
II
SHOCK
LOADING
COD
BOD,. —
9AM
6/8
TIME
9AM
6/9
Figure 36. Secondary effluent COD and BOD^ - Marlborough -
Phase 3B.
The influence of the septage was most evident in the efflu-
ent solids data shown on Figures 37 and 38.
600
^-v
<^ 500
^ 400
Z
O
< 300
LU
O
200
O 100
9AM
5/30
TOTAL SOLIDS
SUSPENDED SOLIDS
9AM
9AM
9AM
5/31
TIME
6/1
6/2
Figure 37. Secondary effluent total and suspended solids
Marlborough - Phase 3A.
103
-------
<•-> 600
_l
•^
3 500
z
O 400
o: 300
O
O
O 200
100
0
^ "I
SHOCK
LOADING
TOTAL SOLIDS
SUSPENDED SOLIDS _
Uf . . 1 ^ . , I .
9AM
9AM
9AM
6/7
6/8
TIME
6/9
Figure 38. Secondary effluent total and suspended solids
Marlboroiagh - Phase 3B.
There was a definite increasing trend in 'the effluent total
solids concentrations during both test periods. Late in the
afternoon of the second day of both tests, solids concentrations
reached maximum values. Primary effluent maximum concentrations
of total and suspended solids occurred two to three hours prior
to the peak secondary effluent concentrations.
Nitrogen data for Phase 3 are plotted on Figures 39 and 40.
Septage appears to have increased effluent TKN and ammonia
levels in both tests. But influent sewage concentrations were
higher than baseline values during Phase 3. Secondary effluent
nitrate nitrogen decreased about 1 mg/1. The rapid increase
in ammonia concentration shown on Figures 39 and 40 was caused
by both septage and surges of sewage flow.
Shock loading had a pronounced effect on mixed liquor dis-
solved oxygen (Figures 41 and 42). Within five hours of impos-
ing a shock, dissolved oxygen had fallen to a minimum for the
day. Mixed liquor temperatures were higher in Phase 3 than in
Phase 1 (17°C versus 10°C) and as a result dissolved oxygen
levels were lower, even with the increased aerator output in
Phase 3. Increased mixed liquor solids added to the dissolved
oxygen demand in Phase 3B.
104
-------
30
2 20
o
z
o
o
10
0
I
T 1 T
SHOCK
LOADING
TKN
'AMMONIA-N
NITRATE-N
9AM 9AM
5/30 5/31
9AM
9AM
6/1 6/2
TIME
Figure 39. Secondary effluent nitrogen - Marlborough - Phase 3A.
30
O
Z
O
O
20
10
I II
I
SHOCK
LOADING
AMMONIA-N
NITRATE-N
9AM
6/7
9AM 9AM
6/8 6/9
TIME
Figure 40, Secondary effluent nitrogen - Marlborough - Phase 3B.
105
-------
8
7
_l
"cB 6
^
z 5
O
I—*
i4
i-
13
z
0 2
O Z
9AM
9AM
9AM
9AM
5/30
5/31
TIME
6/1
6/2
Figure 41. Mixed liquor dissolved oxygen, first stage
Marlborough - Ph.a,se 3A,
9AM
9AM
9AM
6/7
6/8
6/9
TIME
Figure 42. Mixed liquor dissolved oxygen, first stage
Marlborough - Phase 3B.
106
-------
Dissolved oxygen uptake data, shown on figures 43 and 44,
also show the impact of septage, Peak values occurred three
to five hours after septage addition. Average dissolved oxygen
uptake rates were similar in Phases 3A and 1 but Phase 3B
average values were higher than all preceding tests. This was
not caused by septage but rather by comparatively high mixed
liquor solids concentration.
LU (£.
e? x
> i
x _i
a
n i
CD
30
20
tu
GO I-
— • CL
a ra
10
I
SHOCK
LOADING
I I I .1:1.1
I I 1
9AM 9AM
5/30 5/31
9AM
9AM
6/1
6/2
TIME
Figure 43. Mixed liquor dissolved oxygen uptake, first stage -
Marlborough - Phase 3A.
A striking rise in settlometer data was observed in Phase
3A. Thirty-minute values are shown on Figure 45. Over the
three days, settlometer readings increased 50%, from 120 ml/
liter to 180 ml/liter, in a linear manner. Shortly after
septage additions (within two hours) settlometer readings had
fallen slightly, 10 ml/liter to 20 ml/liter, and then increased
throughout the day. For each day after the shock period began,
the highest settlometer readings were obtained just before ini-
tiating that day's shock load. This was caused by long night-
time periods of low feed and extended aeration time. SVI
varied from a low of 75 to a high of 110 ml/g - an excellent
settling range. The increase in settlometer readings over the
three-day period was caused by an increase in mixed liquor
suspended solids from 1,070 mg/1 to 1,540 mg/1. The percent
107
-------
40
II I Q£
CD X
Zll 30
20
CD
as:
_J LU
O^
V) <
CO h-
—• O.
Q Z>
10
9AM
6/7
SHOCK
LOADING
9AM
6/8
TIME
9AM
6/9
Fig-are 44. Mixed liquor dissolved oxygen uptake, first stage -
Marlborough - Phase 3B.
en 200
< 150
Of.
o
100
50
0
-t I I
I ' ' r
SHOCK
LOADING
CO
9AM 9AM 9AM 9AM
5/30 5/31 6/1 6/2
TIME
Figure 45, Thirty-minute settlometer, first stage - Marlborough-
Phase 3A.
108
-------
of volatiles of the mixed liquor suspended solids remained almost
invariant at 73% over the entire period.
A similar increase in thirty-minute settlometer readings
was observed in Phase 3B. The increase, 40 ml, was small but
the trend was real. The average value, 158 ml per gram, was
essentially the same as in Phase 1 (Figure 46).
^ 250
ID
| 200
<
LU
ce
LU
I-
UJ
s
o
150
100
50
UJ
co 0
I II
' I
SHOCK
LOADING
9AM 9AM 9AM
6/7 6/8 6/9
TIME
Figure 46.
Thirty-minute settlometer, first stage
borough - Phase 3B.
- Marl-
Nitrification Stage (Stage 2)
Excellent tertiary treatment was achieved in Phase 3.
Final effluent COD, BODs and suspended solids concentrations
were about the same as those of the baseline period. Values
are plotted on Figures 47 through 50. Effluent total volatile
solids were 30% higher in Phase 3A than in Phase 1, but returned
to Phase 1 levels in Phase 3B. Peak total solids concentrations
occurred at the same time as those in secondary effluent, three
to five hours after primary effluent concentrations were at
maximum. This indicates that the concentration perturbations
monitored were caused by hydraulic surges in sewage flow and not
by septage input.
Nitrate nitrogen concentrations in final effluent were four
to five mg/1 higher in Phase 3 (17 mg/1 Phase 1; 20.7 mg/1 Phase
3A-' 21 7 mg/1 Phase 3B) . The rise in nitrates reflected similar
109
-------
70
60
50
40
< 30
DC
LU 20
O
O 10
SHOCK
LOADING
BODc
9AM 9AM 9AM
5/30 5/31 6/1
TIME
9AM
6/2
Figure 47. Final effluent COD and BOD- - Marlborough - Phase 3A.
<
cc.
O
70
60
50
40
30
20
o 10
^ ' I
SHOCK
LOADING
COD
I , . , I . , .
9AM 9AM
6/7 6/8
TIME
6/9
Figure 48. Final effluent COD - Marlborough - Phase 3B,
110
-------
^-v 600
_1
ar 500-
O 40°
»—»
»-
1$ 300
O
z
o
200
100
SHOCK
LOADING
TOTAL SOLIDS
SUSPENDED SOLIDS
9AM 9AM 9AM
5/30 5/31 6/1
TIME
9AM
6/2
Figure 49. Final effluent total and suspended solids
Marlborough - Phase 3A.
600
500
400
-------
increases in secondary effluent TKN values. Increased nitrifi-
cation was a result of the additional food provided to nitrify-
ing organisms by septage and an increased sewage ammonia source.
Ammonia nitrogen and TKN averaged 0.63 mg/1 (S = 0.41) and 2.5
mg/1 (S = 0.49) respectively in Phase 3 (Refer to Appendix Table
1-5) .
Most of the nitrification at Marlborough was accomplished
in the first compartment of the plant's nitrification section.
This is substantiated by mixed liquor nitrate values, dissolved
oxygen levels, and the dissolved oxygen uptake rates (See
Figures 51 through 54). Settlometer readings were relatively
constant throughout Phase 3 (Figures 55 and 56). For the load-
ing applied in Phase 3 the nitrification stage was not measurably
influenced by septage addition.
Figure 51.
o
1-^
H-
<
I-
LU
o
8
7
6
5
4
3
S 2
1
o
I '
I I
SHOCK
LOADING
LAST
COMPARTMENT
COMPARTMENT-
9AM
9AM
9AM
9AM
5/30
5/31
TIME
6/1
6/2
Dissolved oxygen, first and last compartment,
second stage - Marlborough - Phase 3A.
Dissolved oxygen uptake rates in the first compartment
showed significant variations between early morning and later
in the day. For example, the 7:00 a.m. values averaged 14.6
mg/l-hr, while samples collected between 8:00 a.m. and 6:00 p.m.
112
-------
o
t—»
h-
LU
U
z
o
o
9
8
7
6
5
4
3
2
• i
-I tl
9AM
6/7
1 • I
SHOCK
LOADING
.--LAST
COMPARTMENT
FIRST
COM-'*'
'ARTMENT-
9AM
6/8
TIME
9AM
6/9
Figure 52. Dissolved oxygen, first and last compartment, second
stage - Marlborough - Phase 3B.
averaged 83 mg/l-hr. Septage did not affect the culture, but
rather the normal increase in daily flow displaced large quan-
tities of secondary clarifier liquid between 7:00 and 8:00 a.m.
113
-------
o;
:r
i
a.
LLJ
X
o
Q
LU
o
CO
CO
I— i
Q
110
100
90
80
70
60
50
40
30
20
10
0
LT'T"T
SHOCK
LOADING
I
9AM
9AM
9AM
9AM
5/30
5/31
TIME
6/1
6/2
Figure 53. Dissolved oxygen uptake, first compartment, second
stage - Marlborough - Phase 3A.
114
-------
110
QC
I
_[j 90
^
O
S 80
<
Q.
70
60
LLJ
£ 50
X
O
0
LU
40
30
J2 20
10
-I II
I
SHOCK
LOADING
9AM 9AM 9AM
6/7 6/8 6/9
TIME
Figure 54. Dissolved oxygen uptake, first compartment, second
stage - Marlborough - Phase 3B.
115
-------
150
z
Q
<
UJ
100
50
LU
CO
I
I I
SHOCK
LOADING
9AM
9AM
9AM
5/30
5/31
TIME
6/1
9AM
6/2
Figure 55. Thirty-minute settlometer, last compartment,
second stage - Marlborough - Phase 3A.
150
UJ
oc
100
50
CO
I
9AM
6/7
I
' ' '
T
SHOCK
LOADING
I ... I , , . I
9AM
6/8
9AM
6/9
TIME
Figure 56. Thirty-minute settlometer, last compartment, second
stage - Marlborough - Phase 3B.
116
-------
SECTION 7
RESULTS AT LOWELL - EXTENDED AERATION
PHASES 1 AND 2
During Phase 1 no septage was fed. Mixed liquor suspended
solids stabilized at 4,000 mg/1 and the plant achieved excellent
solids and organic removals. In Phase 2 septage was fed contin-
uously, except on two occasions. An accidental overfeed and
snow storm upset the plant in mid-March 1977. Air compressor
and pumps were off for thirty hours and septage was not fed to
the plant for a six-day period. The second interruption in sep-
tage feed occurred near the end of Phase 2 in early May 1977.
On one weekend, a truckload of septage containing a solvent
smelling like paint thinner was fed to the plant for a full day.
The impact on the plant lasted six days. Effluent, during this
upset, was cloudy, had a COD of 640 mg/1, and smelled like the
solvent. Microscopic inspection of the mixed liquor indicated
that the usual population of higher organisms (rotifers, proto-
zoa, etc.,) was not present, but the presence of well-flocculated
solids indicated that the bacterial population had remained via-
ble. The dissolved oxygen uptake rate did not change.
Sewage and Septage Characteristics
During periods when the students occupied the dormitories
the sewage was characteristic of a weak to moderate strength
waste with an average COD of 373 mg/1. When the students were
on vacation the strength of the sewage dropped significantly,
with the influent COD averaging only 142 mg/1. Periods of re-
duced sewage strength occurred from December 22, 1976 to January
14, 1977 and March 14, 1977 to March 20, 1977.
Feed rate and characteristics of septage used for the study
at Lowell are shown in Figure 57. COD varied from 3,400 mg/1
to 46,000 mg/1. Septage strength declined during the winter
months, and increased after mid-March. Haulers stated that much
of the pumping done in the Lowell area in the winter is routine
periodic work for apartment houses, restaurants, etc.
Food/Microorganism Ratio
Settleability of bacterial floes in the secondary clarifier
acted as a constraint on the maximum permissible solids concen-
117
-------
5000
4000
a
O 3000
2000
LU 1000
PHASE 1
PHASE 2
"— N
>
Q 2000
"V.
_l
1500
Q
LU
LU
LL. 1000
LU
0
-------
o:
O co
Z3Q
Gf ~
~ _J
_l O
co
Ul Q
X LJLJ
- Q
s: z
LU
a.
CO
Z3
V)
8000
6000
4000
2000
0
PHASE 1
PHASE 2
LU
>- Z
H --
a: _J
« i-
x h-
I- LU
CO
800
600
400
200
0
12000
P Q 800°
Z> UJ
_IH
w ^ 4000
2:
0
NOV
J—U
1 I J ll
DEC JAN FEE MAR
MONTH
APR
MAY
Figure 58. Mixed liquor suspended solids, settleability, and
sludge wastage - Lowell - Extended aeration Phases
1 and 2.
119
-------
Dissolved Oxygen Requirements
Septage addition dramatically increased the demand for oxy-
gen in the aeration tanks. By mid-February, at a septage/
sewage feed ratio of 1.5%, the aeration system did not supply
enough air to maintain adequate dissolved oxygen levels. The
compressor output was increased and conditions improved within
hours. The air supply was adequate until the end of the experi-
ment, when once again dissolved oxygen levels were low, this
time at a septage feed ratio of 6.3%.
Measured values of oxygen uptake rate compared favorably
with oxygen requirements calculated from standard equations.
As an example, data are shown in Table 49 for a septage/sewage
flow ratio of 3.1%.
TABLE 49. OXYGEN UTILIZATION AT SEPTAGE/SEWAGE RATIO OF 3.1%
LOWELL - EXTENDED AERATION - PHASE 2
Characteristic Calculated Values
Solids Retention Time, days 20
Mixed Liquor Susp. Solids, mg/1 3,500
Aeration Tank Volume, cu m(gal) 30.3 (8,000)
Septage BODL, mg/1 10,000
Septage Feed Rate, cu m/day 0.95
(gal/day) (250)
Sewage Feed Rate, cu m/day 30.3
(gal/day) (8,000)
Influent BODL, mg/1 300
D.O. Uptake Rate, mg/1-hr-gm 4.5
Effluent BODL, mg/1 15
O2/day, kg/day 11.4
(Ib/day) (25.2)
Theoretical oxygen requirements based upon food utilization and
cell wasting:
02/day = BODL - 1.42 (Volatile Solids wasted)
10.6 kg/day (23 Ib/day)
Treatment Efficiency
Septage was treated with sewage in Phase 2 without dimin-
ishing effluent quality, at rates up to 3% of the sewage flow.
At this septage feed rate, organic loading on the plant was
doubled and the plant received twice its design organic loading.
At a septage input of 4.4% of the sewage flow rate there was a
120
-------
slight increase in effluent COD and effluent color. Dissolved
oxygen in the aeration basin fell below 1 mg/1. Severe dis-
ruption occurred after several days at a septage feed rate of
6.3%. The effective treatment range of this plant could have
been extended by increasing the air supply, since low dissolved
oxygen was the cause of the disruption. The range might also
have been extended by wasting more frequently, thereby reducing
endogenous (oxygen) requirements. Effluent COD is shown in
Figure 59.
Q
o
o
3
_l
U.
U.
200
180
160
140
120
100
80
60
40
20
PHASE .1
I
I
I
I
I
NOV DEC JAN FEE MAR APR
MONTH
MAY
Figure 59. Effluent COD - Lowell - Extended aeration Phases 1
and 2.
Figure 60 shows the impact of the combined sewage and sep-
tage influent on treatment efficiency. Effluent COD increased
linearly with increasing influent strength. However, the effi-
ciency of COD removal remained almost constant prior to process
failure. The plant achieved better than 90% COD removal through-
out Phase 2.
121
-------
100
90
80
Z 70
LLJ
0
DC
UJ 60
a.
<
o
a
o
o
50
40
30
20
10
0
0
I
I
200
150
100
50
Q
O
O
LU
500 1000 1500
COB I NED INFLUENT COD (MG/0
2000
Figure 60. COD removal efficiency - Lowell - Extended aeration
Phases 1 and 2.
EXTENDED AERATION - PHASE 3
Phase 3 consisted of two separate shock tests: septage
volumes were fed equal to 1.33% and 2.63% of the average daily
sewage flow rate. The plant was shock loaded in a period of 5
to 10 minutes in each test.
Mixed Liquor
Mixed liquor suspended solids averaged about 3,000 mg/1
during the first shock loading. This was about 500 •=- 1,000 mg/1
less than concentration measured during Phases 1 and 2. The
dissolved oxygen uptake rate prior to shocking was about one-
half the values measured during the latter stages of Phase 2.
This was caused by a reduction in available sewage flow. Dor-
mitories were closed for summer recess and septage had not been
fed for some time.
122
-------
Addition of septage in Phase 3A caused a two-fold increase
in dissolved oxygen uptake rate within one hour. The higher rate
was maintained for at least six hours after the shock. By the
following morning the uptake rate had returned to pre-shock
levels. Settleability was not affected by septage addition.
During Phase 3B there was a substantial increase in mixed
liquor suspended solids, beginning at 2,800 mg/1 and climbing to
3,800 mg/1 at the end of the monitored recovery period. Oxygen
uptake was low at the start of the test, but one hour after the
shock it had again increased significantly. The uptake rate re-
mained higher after 24 hours than it had in the first shock
period, but was still lower than its Phase 2 level.
Only a slight loss of settleability occurred at the 2.63%
loading.
Oxygen Concentrations
The first aeration basin absorbed the impact of the shock
load in both Phase 3 tests. The initial oxygen reduction was
simply the result of the introduction of a significant quantity
of anaerobic material. Subsequent reduction was caused by the
high uptake rate. Dissolved oxygen levels remained high in the
second basin. Clarifier dissolved oxygen levels remained high
during Phase 3A but fell and were slow to recover in Phase 3B.
The most severe lowering of dissolved oxygen occurred within one
hour of shocking in both aeration basins, but was delayed in the
clarifier until two or three hours after loading. During Phase
3A the septage strength increased each day, but there was little
noticeable difference in the dissolved oxygen response. Re-
covery was essentially complete within four to six hours. In
Phase 3B there was a residual effect on the clarifier. Dissolved
oxygen levels at corresponding times after shocking were lower
on the second day than on the first, and lower yet on the third
day. This happened even though the septage strength decreased
steadily from the first to the third day.
Effluent Quality
Effluent COD was only marginally affected by septage at the
1.33% loading. It rose to a peak about three to four hours af-
ter loading, but returned to very low values twenty-four hours
after each Phase 3A shock. The pre-shock COD was 32 mg/1 and
the maximum value was 48 mg/1 (occurring on the first day). As
the test proceeded, the maximum level each day decreased, al-
though the septage strength increased. The biological culture
readily accepted septage as a food source.
Suspended solids remained below 20 mg/1, with the one ex-
ception three hours after shocking on the second day. The
123
-------
concentration rose to 48 mg/1 and dropped to 16 mg/1 in one hour.
Nitrification was not noticeably interrupted during Phase 3A.
Effluent quality was seriously degraded in the second shock
loading test, Phase 3B. On the first day of shocking, effluent
COD rose from 36 mg/1 to a high of 269 mg/1. By the next morn-
ing, the level had nearly returned to the previous starting
value. On subsequent days, a marked increase in effluent COD
was not experienced because the organic loading was significantly
decreased as the test proceeded, although the hydraulic loading
remained constant. The septage organic loading the first day
was 49.6 kg (109 Ibs) of COD, on the second day it was 32.4 kg
(71.5 Ibs), and on the third day, it was 5.8 kg (12.9 Ibs).
In contrast, the sewage fed during the three days averaged
4.3 kg (9.4 Ibs) of COD applied per day.
Effluent suspended solids showed the same trend as COD,
rising significantly on the first day, but returning to low
levels (generally less than 12 mg/1) for the remainder of the
test.
The shock of the first day of Phase 3B inhibited the cul-
ture's ability to nitrify; and by the morning of the second day
no nitrates were found in the effluent. Nitrates did not re-
appear until the first morning of the recovery period, and had
only risen to about one-third of the starting value at the end
of the test.
Shock loading at the 1.3% level did not affect effluent
quality even in the first few hours after addition. Increasing
the shock to 2.63% did result in deterioration of effluent
quality for several hours following the input, but the effect
was short lived.
124
-------
SECTION 8
RESULTS AT LOWELL - CONVENTIONAL MODE OF OPERATION
PHASE 1 - BASELINE FOR COMPARISON
Operating Parameters
During seventeen days of baseline monitoring, the influent
sewage flow rate averaged 110 cu in/day (29,100 gpd) , the aerator
detention time was 6.6 hours, and the clarifier detention time
averaged 3.3 hours. The aeration time was typical of conven-
tional practice, but the clarifier detention time was 50% in
excess of conventional practice. Students occupied the dormi-
tory facilities for ten days of the Phase 1 period, but were
on vacation for seven days in the middle of the period. Process
characteristics for the period are shown in Table 50.
TABLE 50. PROCESS CHARACTERISTICS
LOWELL - CONVENTIONAL MODE - PHASE 1
Characteristic Value
Flow Rate, Q, cu m/day (gpd) 111 (29,3001
Aeration Basin Retention, hrs 6.55
Mixed Liquor Susp- Solids, mg/1 2427
Mixed Liquor Volatile Susp. Solids, mg/1 1893
F/M, kg COD/kg MLVSS-day 0.4
Loading, gm COD/cu m-day 101
(Ib COD/1000 cu ft-day) (6.3)
Mean Cell Residence, SRT, days 10
Oxygen Utilization, kg 02/kg COD 1.22
Influent Characteristics
Influent organic and solids concentrations characterize the
waste as weak sewage. Average values for all monitored para-
meters are shown in Table 51. Both the COD and suspended solids
125
-------
TABLE 51. INFLUENT AND EFFLUENT
LOWELL - CONVENTIONAL MODE - PHASE 1
Characteristic
COD-Total , mg/1
COD-Soluble, mg/1
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Susp. Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Alkalinity, mg/1 as CaCO-
PH
Temperature , °C
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Influent
x s
206
458
164
112
85
18
8
1.5
7.3
108
6.8
14
0
0
0.11
0
0.08
0.14
108
104
65
81
49
7.7
3.9
0.9
6.3
19
0.2
1.5
Effluent
X S
50
39
379
97
14
10
5
2..1
8.7
2.1
60
6-7
10.7
0.02
0
0.07
0
0.09
0.12
22
12
83
31
20
16
3.6
3.0
2.1
0.4
26
0.2
1.0
values were significantly lower when the students were off
campus. Ammonia, TKN, and phosphorus concentrations also fell
during the vacation period. The system was fed at the rate of
22.9 kg COD-day(50.35 Ib/day) or 0.75 kg COD/cu m-day (47.0
Ib COD/1,000 ft3-day).
Effluent Characteristics
The plant functioned well during Phase 1 with effluent COD
averaging 50 mg/1, and suspended solids averaging 14 mg/1. Low
TKN (5 mg/1) and ammonia nitrogen (2.1 mg/1) levels and moder-
ately high nitrate nitrogen values C8,7 mg/1) indicate that
nitrification was nearly complete during this monitoring period,
Phosphorus values were low, averaging 2.1 mg/1. Dissolved
oxygen levels were satisfactory during most of Phase 1; they
126
-------
dropped below 1 mg/1 on only two occasions. Treatment efficiency
averaged 75% based on COD removal and 88% with respect to sus-
pended solids removal. Average effluent values are shown in
Table 51.
Mixed Liquor Characteristics
Mixed liquor suspended solids were maintained at an average
of 2,430 mg/1, which is typical of conventional operation. Vola-
tile suspended solids averaged 1,890 mg/1 and suspended solids
were about 78% volatile (See Table 52).
Dissolved oxygen uptake rates averaged 28.9 mg/l/hr or
15.3 mg/1/hr-gram of volatile suspended solids. This value is
somewhat lower than those generally found in conventional treat-
ment processes and indicates that the process was lightly fed.
The F/M ratio was 0.40 (COD basis) and 0.19 (BOD5 basis). All
mixed liquor samples were taken from the second aeration basin.
The solids retention time was maintained at 10 days by
daily wasting 800 gallons of mixed liquor directly from the
aeration basin. Settleability remained marginally acceptable
throughout this phase, with the half-hour settlometer reading
averaging 665 ml/1. The sludge volume index, SVI, was 274 ml/gm.
Oxygen concentrations within the aeration basins remained above
1 mg/1 except on two occasions when they fell to 0.5 mg/1.
PHASE 2 - CONTINUOUS LOADING
Operating Parameters
The sewage flow rate during the twelve days of Phase 2A
averaged 109 cu m/day (28,740 gal/day). This was 1.3% less than
the Phase 1 flow rate. Students were in attendance throughout
the period and this produced a stronger influent waste. Deten-
tion times in the aeration basin and clarifier were the same as
those of Phase 1. Phase 2B was conducted over a seven-day period
at an average sewage flow rate of 103 cu m/day (27,210 gal/day)
or 6.5% less than Phase 1. Process characteristics are shown in
Table 53.
Influent Characteristics
Raw sewage COD values were higher during Phase 2A than dur-
ing Phase 1. Suspended solids concentrations were low, aver-
aging only 78 mg/1. These and other parameters, which charac-
terize the sewage as a weak to moderate domestic waste, are
shown in Table 54. Influent sewage imposed an average daily
loading on the system of 27.5 kg (60.6 Ib) of COD/day or 0.91
kg COD/cu m-day (56.7 Ib COD/1,000 cu ft-day).
127
-------
TABLE 52. MIXED LIQUOR
LOWELL - CONVENTIONAL MODE - PHASE 1
Characteristic s
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Susp. Solids, mg/1
Alkalinity, mg/1 as CaCCU
D. 0. Uptake, mg/l-hr
Dissolved Oxygen, mg/1
Location A at surface
A near bottom
B at surface
B near bottom
C at surface
C near bottom
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Settlometer, 30 minutes, ml/1
Settlometer, 60 minutes, ml/1
PH
Temperature , °C
Metals, mg/1
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Mixed Liquor
x s
2,436
1,727
2,427
1,893
87
29
3.4
3.2
3.6
3.4
5.0
4.8
172
2.9
8.9
666
483
6.6
12
0
0
0
1
243
174
285
272
21
13
1.5
1.5
1.6
1.7
2.2
2.2
14
3.6
2.0
71
53
0.1
0.9
.03
0
.63
.10
.43
2.0
The septage to sewage flow ratio averaged 0.41 percent dur-
ing Phase 2A and the septage had an average COD value of 13,640
mg/1. Septage increased the COD loading on the plant by 7.5
kg/day (16.5 Ib/day) or 0.25 kg/cu m-day (15.4 lb/1,000 cu ft-
day). Total organic loading (septage plus sewage) averaged 35.9
128
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TABLE 53. PROCESS CHARACTERISTICS
LOWELL - CONVENTIONAL MODE - PHASE 2
Characteristics
Flow rate, 0, cu in/day ,
(gpd)
Septage Feed Rate , cu in/day
(gpd)
Septage/Sewage , %
Aeration Basin Retention, hrs
Mixed Liquor Suspended Solids, mg/1
.Mixed Liquor Volatile Suspended
Solids, mg/1
F/M, kg COD/kg MLVSS-day
Loading, gm COD/cu m-day
(Ib COD/1000 cu ft-day)
Mean Cell Residence, SRT, days
Oxygen Utilization, kg 0,,/kg COD
Phase 2A
814
(28,740)
3.4
(120)
0.42
6.65
3,120
2,370
0.59
149
(9.3)
10
0.78
Phase 2B
771
(27,210)
6.2
(220)
0.81
7.0
2,870
2,330
0.57
179
(11.1)
10
0.77
TABLE 54. SEWAGE, SEPTAGE, AND COMBINED INFLUENT
LOWELL - CONVENTIONAL MODE - PHASE 2A
Characteristics
COD-Total mg/1
Total Solids, mg/1
Total Volatile Solids,
Suspended Solids, mg/1
Sewage
x s
253
460
mg/1 190
78
Volatile Suspended Solids,
mg/1 69
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
23
12
1.2
(continued)
96
74
57
42
39
0.8
2.7
0.4
Combined
Sewage
and
Septage Septage
X S X
13,643
3,918
3,038
1,756
1,254
329
73
12,230
1,943
1,626
658
721
89
41
—
309
474
202
85
74
24
12
—
129
-------
TABLE 54. [continued)
Sewage
~~~~~Combined.
Sewage
and
Septage Septage
Characteristics
x
x
X
Total Phosphorus, mg/1
Alkalinity, mg/1 as CaC03
PH
Metals, mg/1:
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
5.6
135
7.0
2.1
10
0.6
87
312
7.2
8
141
0.2
5.9
136
0
0
0.09
0.05
0.15
0.07
0
0
0.02
0.02
0.13
0.06
0.06
0.26
11.4
0.30
0.62
2.6
0.08
0.38
3.6
0.14
0.14
0.14
0
0
0.14
0.05
0.15
0.08
kg COD/day (77.1 Ib COD/day) or 1.16 kg/cu m-day (72.1 lb/1,000
cu ft-day). This represents a 53% increase over Phase 1.
Total solids loading averaged 50.7 kg/day (112 Ib/day) of
which 1.8 kg (4 Ib) were added by the septage. Septage added
only 0.14 kg/day (0.3 Ib/day) to the 2.45 kg/day (5.4 Ib/day)
of nitrogen in the sewage.
During Phase 2B the septage flow was 0.81% of the sewage
flow rate. Septage organic, solids, nitrogen and phosphorus
levels were, in all cases, higher than for the septage of Phase
2A (See Table 55).
Organic loading averaged 40.4 kg (89,1 Ib) COD/day or 1.33
kg/cu m-day (83.3 lb/1,,000 cu ft-day), a 77% increase over
Phase 1. Of this total 24.9 kg COD/day (54.9 Ib COD/day) were
added by the sewage and 15.5 kg/day (34.2 Ib/day) by the sep-
tage. Solids loading was 53.6 kg/day (118 Ib/day) of which 18
percent was added by the septage.
The septage increased the total loadings of TKN, ammonia
and phosphorus by 11.6%, 6.1% and 22.1%, respectively. As in
Phase 2A, the septage increased COD loadings more than any
other monitored parameter (62%).
130
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TABLE 55. SEWAGE, SEPTAGE, AND COMBINED INFLUENT
LOWELL - CONVENTIONAL MODE - PHASE 2B
Characteristics
COD-Total, mg/1
Total Solids, mg/1
Total Volatile Solids,
mg/1
Suspended Solids, mg/1
Volatile Suspended
Solids, mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Alkalinity, mg/1 as
CaC03
PH
Metals, mg/1:
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Effluent Characteristics
Sewage
x s
242 117
427 56
153 45
66 31
56 27
24 6.2
13 5.6
2.5 1.5
4.2 0.2
119 21
6.6 0.4
0
0
0.07
0.04
0.06
0.07
Septage
x s
18,640 15,732
11,507 14,292
8,364 9,940
9,903 13,841
7,440 10,020
346 288
98 79
-
113 15
708 349
6.7 0.5
0.24
2.00
820
0.80
11.20
57.00
Combined
Sewage
and
Septage
x
390
516
219
145
115
27
14
5.1
124
6.6
0
0.02
6.65
0.05
0.15
0.53
Overall treatment during Phase 2A produced an effluent with
a lower COD (30 vs. 50 mg/1) and a lower SS (4 vs. 14 mg/1)
than during Phase 1. TKN and ammonia were also lower during this
phase while nitrate concentrations were slightly higher. Total
solids, total volatile solids, phosphorus and alkalinity were
almost identical in both phases. The only indication of an ad-
verse effect caused by the septage addition at 0.41% was a de-
131
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cline in effluent dissolved oxygen from 3.0 mg/1 in Phase 1
to 0.5 mg/1 in Phase 2A. Treatment efficiencies averaged
90% and 95% for COD and suspended solids removal, respectively,
Average effluent values are shown in Table 56.
TABLE 56. EFFLUENT
LOWELL - CONVENTIONAL MODE - PHASE 2
Characteristics
COD-Total , mg/1
COD-Soluble, mg/1
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Suspended Solids,
mg/1
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Total Phosphorus, mg/1
Alkalinity, mg/1 as CaCO.,
PH
Temperature , °C
Dissolved Oxygen, mg/1
Metals, mg/1:
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Phase
X
30
22
357
92
4.0
3.6
1.9
1.3
9.6
2.5
63
6.7
12
0.5
0
0
0.07
0
0.02
0.01
2A
s
8.9
6.3
42
27
3.0
3.0
0.4
0.3
1.5
0.5
6.7
0.2
0.5
0.3
0
0
0.02
0
0.04
0.04
Phase 2B
x s
126
26
410
130
52
48
3.5
1.6
5.5
2.9
73
6.6
13
0.4
0
0
0.09
0
0
0.06
152
3.8
112
91
85
79
1.1
0.7
1.9
0
14
0.1
0.7
0.5
Based upon average effluent total COD and suspended solids
values (126 and 52 mg/1, respectively) it would appear that
septage significantly degraded effluent quality in Phase 2B.
132
-------
However, soluble COD values remained at about the same level
measured during Phases 1 and 2A. Soluble COD values indicate
the system was capable of handling septage at the rates applied
during this phase. Based on total COD removal and suspended
solids removal, treatment efficiency fell to 67% and 64%,
respectively. Dissolved oxygen levels in the effluent were
very low, averaging 0.4 mg/1.
Normal organic loadings on conventional activated sludge
processes range between 0.32 and 0.64 kg BOD/cu m-day. Assuming
a COD:BOD ratio of 2.5:1 for combined sewage and septage, the
plant was loaded at the rate of 0.3, 0.46> and 0.53 kg BOD/
cu m-day for Phases 1,2A and 2B, respectively. Thus, loadings
throughout these three phases covered the typical range.
The Lowell plant performed very well in the conventional
mode during Phase 1 and Phase 2A (septage fed at 0.41%) . In-
creasing the loading to 0.81% (Phase 2B) resulted in degrada-
tion of effluent quality. This loss of treatment efficiency
was caused by overtaxing capabilities of the oxygen transfer
system. It is felt that the system would have satisfactorily
treated septage at 0.81% if higher oxygen levels could have
been maintained. Although treatment efficiency was excellent
during Phase 2A, data indicate septage was stressing the oxygen
system near its limits.
Lack of primary clarifiers significantly increased organic
loadings on the aeration system and led to system overload and
effluent quality degradation.
Mixed Liquor Characteristics
Mixed liquor suspended solids concentrations during Phase
2A were one-third higher than those measured during the base-
line period (3,170 vs. 2,430 mg/1). This is also true of mixed
liquor total solids, total volatile solids and volatile sus-
pended solids concentrations. Alkalinity and TKN in mixed liquor
were about 50% higher during Phase 2A than they were during
Phase 1, while ammonia was about the same in both phases and
nitrates were slightly lower. Table 57 shows average values for
Phase 2.
Dissolved oxygen uptake values averaged 35 mg/l-hr or
15.2 mg/1-hr-gram of volatile suspended solids as compared with
29 mg/l-hr or 15.3 mg/1-hr-gram during Phase 1. It is obvious
that the increase in overall oxygen uptake rate was due to the
higher volatile suspended solids concentration carried in the
mixed liquor during Phase 2A. Dissolved oxygen levels averaged
1 mg/1 throughout the aeration basins.
Mean cell residence time was held at 10 days. The F/M
ratio averaged 0.34 (COD basis) or 0.16 (BOD5 basis assuming a
133
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TABLE 57. MIXED LIQUOR
LOWELL - CONVENTIONAL MODE - PHASE 2
Characteristics
Total Solids, mg/1
Total Volatile Solids, mg/1
Suspended Solids, mg/1
Volatile Suspended Solids,
mg/1
Alkalinity, mg/1 as CaCO3
D.O. Uptake, mg/l/hr
Dissolved Oxygen, mg/1:
Location A, at surface
Location A, at bottom
Location B, at surface
Location B, at bottom
Location C, at surface
Location C, at bottom
Total Kjeldahl-N, mg/1
Ammonia-N, mg/1
Nitrate-N, mg/1
Settlometer, 30 min.,ml/l
Settlometer, 60 min.,ml/l
PH
Temperature , °C
Metals, mg/1:
Cadmium
Chromium
Copper
Nickel
Lead
Zinc
Phase
X
3,230
2,440
3,170
2,370
129
36
1.1
0.8
1.0
0.9
1.2
1.0
240
2.4
6.8
686
514
6.5
13
0.03
0.50
1.64
0.09
1.22
9.03
2A
s
438
430
276
450
46
7
0.4
0.3
0.3
0.3
1.4
1.3
39
0.9
3.7
124
104
0.3
0.5
0.01
0.50
0.41
0.02
0.08
9.58
Phase
X
3,190
2,525
2,870
2,330
145
43
2.4
2.2
2.3
2.1
0.9
0.7
221
2.3
3.6
880
740
6.5
14
2B
s
413
286
396
365
33
21
2.4
2.4
2.3
2.3
1.2
1.2
29
1.5
2.2
16
44
0.2
0.5
134
-------
COD/BOD5 ratio of 2:1 for the combined influent and septage).
This loading was lower than that of Phase 1 even though sep-
tage was added, because of the increased mixed liquor suspended
solids carried during Phase 2A. Loadings were at the low end
of recommended values for conventional activated sludge pro-
cesses.
Sludge settleability was acceptable with the one-hour
settlometer reading, averaging only 6% above Phase 1 values.
The SVI averaged 216 ml/gram. However, as Phase 2A progressed,
settleability declined. The clarifier had at times (prior to
this phase) shown a tendency to unload solids. This was not a
continuous happening, but occurred on some days for short
periods of time. The effluent suspended solids data indicate
that the clarifiers did not unload solids during this phase,
but the settlometer data indicate it may have been tending this
way. Whether septage was the cause is not discernable from
the data.
During Phase 2B, mixed liquor suspended solids (2,870 mg/1)
were midway between Phase 1 and Phase 2A average values. The
volatile suspended solids were about the same as for Phase 2A,
2,330 mg/1. Alkalinity was again higher for this phase than
for Phase 1. Ammonia nitrogen remained approximately the same
as in previous phases, however, nitrate levels fell to approxi-
mately one-half those of Phase 2A and about 40% of Phase 1
values. TKN values were lower than Phase 2A as,would be ex-
pected, since both the total solids and suspended solids con-
centrations were less. It is interesting to note that the ratio
of total solids to TKN averaged 14.2, 13.5 and 14.4 for Phases
1, 2A and 2B, respectively. Values are shown in Table 57.
Dissolved oxygen uptake rate averaged 43 mg/l-hr or 18.5
rag/1-hr-gram VSS. This rate is about 20% higher than in the
previous two phases and was due to an elevated food concentra-
tion. However, the standard deviation of this data was three
times that of Phase 1 and 50% higher than in Phase 2A.
Mean cell residence time was held at 10 days. The F/M
ratio was 0.53 based upon COD and 0.25 based upon BOD5. This
loading was within the range recommended for conventional
processes and was the highest applied during continuous feeding
operations.
Throughout this phase dissolved oxygen levels remained
near 1 mg/1 or less, except on occasions when the influent pump
clogged and sewage feed slowed. It is apparent that this situa-
tion occurred on two of the nine days of the test. Oxygen
levels were approximately the same as those of Phase 2A and much
lower than during Phase 1. This indicates that the pilot plant
may have been approaching its oxygen transfer limitation.
135
-------
Sludge settleability began to degrade during Phase 2B
with the one-hour settlometer reading averaging 740 ml/1. This
value is much higher than the 514 ml/1 of Phase 2A and 483 ml/1
for Phase 1. SVI for this phase averaged 307 ml/gram.
PHASE 3 - SHOCK LOADING
Influent - Sewage Plus Septage
Phase 3 began two weeks after the completion of Phase 2B.
In the interim sewage feed was maintained but septage was
withheld. Prior to initiating Phase 3, the process began to
deteriorate because of severe influent pump plugging problems.
This condition resulted in periods of reduced feed or no feed
at all. Loadings became erratic and unknown and the culture
suffered substantially. Settleability was poor and on several
occasions the blanket in the clarifier rose to the surface
and unloaded solids over the weir.
The influent COD averaged 378 mg/1 and that of the septage,
23,600 mg/1. The process was shock loaded with 41.3 kg (91 Ib)
of sewage COD combined with 26.8 kg (59 Ib) of septage COD, on
each of three days. The total solids loading was 58.6 kg
(129 Ib) per day. Septage contributed 49.9 kg (110 Ib) and
sewage 8.6 kg (19 Ib) each day. It took one hour to feed each
shock load. During the one-hour period the loading on the
system was equivalent to 644 kg (Iy420 Ib) of COD per day and
212 kg (468 Ib) total solids per day.
The raw sewage was typical of a moderate strength domestic
waste. Septage volumetric loading represented 1.04 percent of
the daily flow on each of the three days. Values are shown in
Appendix Tables M-l and M-2.
Effluent Characteristics
A composite sample collected during the twenty-four hours
preceding the first day's shock had a suspended solids concen-
tration of 114 mg/1, indicating that clarifier operation was
still unbalanced. After loading on the first day, hourly sam-
ples showed low suspended solids (15 mg/1 or less) for the next
three hours rising to 40 mg/1 in the fourth hour and 60 mg/1 in
the sixth hour. However, they had returned to 15 mg/1 the
following morning. Effluent total COD showed the same trend,
but soluble COD remained low throughout, as did the BOD values.
On the second day, suspended solids remained low for two
hours following the shock and then rose to between 700 and 800
mg/1, falling to 136 mg/1 the next morning. They continued to
fall until the sixth hour after shocking on the third day. At
this time the blanket in the clarifier again reached weir level
and spilled solids in the effluent. Total COD again followed
136
-------
the same trend with soluble COD remaining low throughout,
averaging 32 mg/1 with a standard deviation in the twenty sam-
ples of 11.5 mg/1.
Nitrification was severely inhibited. Prior to shocking,
the nitrate concentration was 9.0 mg/1 and fell steadily
throughout the first and second days to a low of 0.7 mg/1. Re-
covery began on the morning of the third day, but again dropped
to the previous lows two to three hours after loading. Nitrates
recovered to only 1.7 mg/1 three days after termination of the
shock loading.
Unfortunately, phosphorus levels were not determined on the
first day of the shock. Beginning on the second day, effluent
phosphorus levels were less than 1 mg/1 and showed a definite
influence on the septage within three hours rising to 15.5 mg/1.
On the third day, wash through of phosphorus was continuing and
again the septage increased effluent values noticeably within
three hours.
Alkalinity and pH remained constant throughout the test.
Variations in TKN were similar to changes in COD and suspended
solids. Process disruption was severe at the 1% septage feed
rate of this phase. This was due to the poor condition of
mixed liquor and limitations in oxygen transfer.
Mixed Liquor Characteristics
Mixed liquor suspended solids concentration dropped from
1,670 mg/1 at the beginning of the test to 1,240 mg/1 at the
end of the three-day shock period. Compared with conventional
operation these values are low.
Dissolved oxygen uptake rates were stimulated by the addi-
tion of septage. On the first day, the uptake rate climbed
from 8.2 mg/l-hr (5.0 mg/1-hr-gram VSS) to a high of 41.1 mg/1-
hr (25.3 mg/1-hr-gram VSS). The pre-shock value was character-
istic of a very lightly loaded system. The latter value is
typical of conventional process return sludge. The second and
third day values rose to the same maximum value of 32.6 mg/l-hr-
gram VSS.
The one-hour settlometer readings averaged 640 ml/1.
While this value is typical of some of the other phases, it is
a poor rate at low mixed liquor suspended solids concentrations.
The SVI averaged 522 ml/gram, indicative of a poorly settling
sludge. In all phases of the conventional loading study, SVI
values were well above the 100 ml/gram level usually considered
desirable.
Before initiating Phase 3, aerators were adjusted to direct
the major air flow to the first aeration basin. This was done
137
-------
in anticipation of a heavy oxygen demand in the first basin. As
a result, when the shock loads were applied, dissolved oxygen
levels in the first basin were reduced to between 2 and 3 mg/1
within one hour and then began to recover. However, the second
basin dropped to below 1 mg/1 within one hour and remained at
this low level until run completion with one exception on the
third morning. Clarifier dissolved oxygen concentrations re-
mained under 1 mg/1 throughout the test and in most cases were
zero. It is concluded that the 1% loading in Phase 3 produced
severe oxygen depletions in the plant.
138
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SECTION 9
MICROBIOLOGY
MICROBIOLOGICAL STUDIES
Microscopic analyses were performed in all phases of the
monitoring program at both Medfield and Marlborough. At Med-
field microbiological communities were identified in mixed
liquor, return sludge, and in secondary effluent. Unicellular
algae and protozoan species and microscopic metazoan species
were enumerated in a Sedgwick-Rafter cell.
Organisms were not counted during the Marlborough study.
The predominant forms and relative abundance of particular
indicator groups were noted. In addition, floe characteristics
were observed and recorded.
Analyses of Medfield samples were conducted by faculty
and graduate students in the University of Lowell, Department
of Microbiology. Marlborough samples were analyzed by a biolo-
gist with wastewater treatment plant operating experience.
MEDFIELD - MICROSCOPIC STUDIES
Medfield microfauna consisted of various protozoan types.
The "Micro-flagellates" found in mixed liquor and return sludge
were designated as flagellates with characteristic cell sizes
of 5 to 20y range. The term "macroflagellate" was used to
classify flagellated protozoans with cell sizes in the 30y and
greater size range. Euplotes and Colpoda were frequently seen
free swimming ciliates, both in mixed liquor and return sludge.
Colpoda were occasionally seen in secondary effluent. Ciliates
of small size, less than 20y , were lumped under the classi-
fication of microciliates. Lionotes, another ciliate, were
also seen in mixed liquor and return sludge. This species
appears to be quite sensitive to alterations in the treatment
plant loading and showed acute sensitivity to shock loading.
Vorticella, a sessile ciliated protozoan, appeared in low to
moderate numbers in mixed liquor and return sludge, and were
very infrequently observed in the effluent stream. Suctorians,
a less frequently found stalked ciliate, have similar distribu-
tion to the vorticella, and like vorticella, indicate a mature
stable community. Rotifers, a metazoan species, similarly
indicate a more mature stable community and, like lionotes and
the sessile ciliates, show sensitivity to insult. Sarcodinian
139
-------
protozoa were occasionally observed, but these amoeboid forms
were not recorded due to the great difficulty in distinguishing
the population density within the sludge particulates. Armored
amoebas were similarly overlooked, as the difficulty in distin-
guishing live individuals from dead individuals led to the
decision to eliminate them from practical consideration.
Occasional vorticella, nematodes and rotifers were recorded
in the effluent.
Effluent flora was categorized by green filamentous algae:
scenedesmus, a non-motile green algae, and pennate and navi-
culate diatoms. Large spirochetes were seen with moderate fre-
quency.
Species number, numbers of individuals within each species
and total number of individuals in counted samples provided
input for computerized calculation of the Shannon Weiner
Species Diversity Index, defined as:
H = -T. (i^/N) log (n±/N)
where n. = the number of individuals of the i
species
N = total number of individuals in a sample.
A high H value is indicative of a diverse, stable, healthy
community.
Results
Plots were made of the number of species, S; total number
of individuals, N; and species diversity, H, of each of the
samples observed. Figures 61 through 71 show the relationships
of these parameters over the time course of the study. Data
on species composition and distributions within samples are
provided in the appendices on data sheets entitled Microbiologi
cal Indices.
Medfield - Phase 1
Phase 1 monitoring conducted from August 25, 1977 through
September 12, 1977 provided baseline data under conditions of
normal operations. Control phase operations showed inherent
levels of fluctuation in the measured parameters and provided
indication of the effects of normally experienced variations
in flow rate and sewage concentration.
Mixed liquor data indicated a species diversity index, H,
which centers about a mean of 1.85; number of organisms in the
samples average 72 individuals per 1 ml sample distributed
140
-------
within an average of seven species for the thirteen days of
sampling microorganisms. These data, presented in Figure 61,
show an initial depression in diversity, the cause of which may
have been the septage cleanout operation, which preceded Phase
1. A major holiday weekend, September 3 through 5, coincides
with a lowering of numbers and increase in species diversity.
These aberrations show subsequent recovery over the next four
days. A rain storm of September 9, 1977, which increased flow
rate of raw sewage by 39%, is associated with a second re-
duction in diversity. Of particular interest here is the be-
havior of population densities of the ciliates, euplotes and
colpodas. Return sludge (Figure 62) shows similar aberrations
following the holiday period and the rain storm. Secondary
effluent as monitored over the period appeared to be more
stable (Figure 63). Data are shown in detail in Appendix Table
B-6.
The relative sensitivity of normal, non-septage-loaded con-
ditions in the Medfield plant may be a result of the relatively
light sewage load received at the plant.
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DATE
— DIVERSITY INDEX
I I I I I 1 I I I I I I I I
Figure 61. Microbiological indices, mixed liquor - Medfield -
Phase 1.
Medfield - Phase 2
Phase 2 studies of mixed liquor, return sludge and secon-
dary effluent (Figures 64, 65 and 66) show a consistent res-
ponse pattern. Mixed liquor shows an average species number of
141
-------
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Figure 62. Microbiological indices, return sludge - Medfield
Phase 1.
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SPECIES
ORGANISMS (X20)
DIVERSITY INDEX
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DATE
9/11 9/13
Figure 63.
Microbiological indices, effluent - Medfield -
Phase 1.
142
-------
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— ^DIVERSITY INDEX
I I I I I I I
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9/14 9/16 9/18 9/20 9/22 9/24 9/26 9/28 9/30 10/2 10/4
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Figure 64. Microbiological indices*mixed liquor - Medfield -
Phase 2A.
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Figure 65.
Microbiological indices, return sludge - Medfield -
Phase 2A.
143
-------
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Figure 66.
Microbiological indices, effluent - Medfield -
Phase 2A.
7.7 with a standard deviation of 1.75 throughout the course of
Phase 2 constant loading. The species diversity averaged 2.01
(standard deviation was 0.37), and the number of organisms aver-
aged 107 organisms per ml with a standard devia'tion of 65.5.
This high standard deviation is the result of step-like changes
in the number of individual organisms per sample. Data are
presented in Appendix Tables C-7 and D-8.
While number of species is quito constant, a major shift
in the numbers of individuals appears on September 20 followed
by a slight decline on September 21 and a precipitous decrease
on September 22. Species most conspicuously affected are the
ciliates and rotifers. Changes in fauna appear to be asso-
ciated with a temperature change of over 3°C over September 19th
to 20th, followed by a shut-down on September 23 of the return
sludge pumping operation. Complete recovery of the community
was not observed as the colpoda and euplotes species did not
reestablish former population densities. It is apparent,
however, that the mixed liquor community assumed a new, stable
equilibrium composition as the newly established equilibrium
persisted for the remaining ten days of the study. Return
sludge and effluent communities showed similar changes over
144
-------
the septage addition period. These microbiological data appear
to correlate quite closely with certain chemical parameters
(particularly nitrogen data).
In Phase 2B, little change was observed in either mixed
liquor or in the effluent. Figure 67 indicates the relative
stability of the situation.
11
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ORGANISMS
SPECIES
DIVERSITY INDEX
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11/1 11/3 11/5 1J/7 11/9
DATE
11/8
Figure 67.
Microbiological indices, effluent - Medfield
Phase 2B.
Medfield - Phase 3
During Phase 3A, microbiological indicators were monitored
intensively over the time course of the daily loadings. Over
the 24-hour period the typical response was one of reduction
in overall numbers of organisms, reduction in species, but no
significant reduction in species diversity. Slight trends to-
ward recovery in numbers and species were observed, but full
recovery was observed only once and only in species number
(Figure 68). The reduction in species and numbers with the
maintenance of species diversity levels around 2 indicates
145
-------
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° 8 10 12 2 4 "8 10 12 2 4 8 10 12 2 4 6868
10/14 10/15 10/16 10/17 10/18
DATE
Figure 68. Microbiological indices, mixed liquor - Medfield - Phase 3A.
-------
that the more common species were affected most adversely by
the process. Lionotes were observed to be very sensitive to
shock loading and decreased from an initial density of 50.5% of
the total population to an ending density of 5.5% of the total.
This species demonstrated a strongly regressive decrease
over the course of the shock loadings. Rotifers and spiro-
chetes showed less intense regression rates.
Phase 3 effluent showed daily reductions in number, species
and diversity. An interesting occurrence in this phase was a
reduction in the floral species composition. Green algae,
scenedesmus and the pennate and naviculate diatoms were elimin-
ated. The fauna constituents of the effluent did prevail,
however. Figure 69 illustrates this. Biological parameter
trends in basin 1, the receiving basin, show a similar pattern
as illustrated in Figure 70.
In Phase 3B, higher concentrations of septage applied
daily showed equivalent results with daily decreases in all
parameters followed by recovery toward the end of the day
(Figures 71 and 72). This loading program did not appear to
alter significantly the communities' abilities to recover from
septage insult. Secondary effluent shows similar recoveries.
Appendix Tables E-9 and F-7 show the test results.
MARLBOROUGH MICROSCOPIC ANALYSES
Floe characteristics and indicator organism populations
were monitored during the baseline and septage addition periods
at Marlborough. Six parameters were used to describe floe
characteristics: color, size, texture, edge condition, inter-
space clarity and the presence of filamentous forms. Micro-
organism species used as indicators of process performance and
sludge age were free swimming and stalked ciliates, flagellates
and rotifers.
Floe Characteristics
A 'good" quality sludge in a conventional activated sludge
process usually has floe that is small to medium in size,
fairly uniform in shape with well defined edges, slightly
granular in texture, and golden brown in color. The interspaces
between the floe are clear, and filamentous organisms, while
generally present, are not overly abundant. A good sludge
settles slowly, occupying about 350 ml in a settlometer after
thirty minutes of settling, and produces an effluent low in
suspended solids and BOD.
An overoxidized or "old" sludge tends to be characterized
by small granular floes of high density with jagged edges,
irregular shape, and a dark grey color. It has a low respira-
tion rate and settles very rapidly in the secondary clarifier.
147
-------
oo
8
7
6
5
4
3
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1 1 1
SPECIES
- O O
— —
ORGANISMS
(X10)
DIVERSITY INDEX
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LO/17
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DATE
Figure 69. Microbiological indices, effluent - Medfield - Phase 3A.
-------
o:
LU
PQ
11
10
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7
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ORGANISMS
(X10)
A
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DIVERSITY INDEX
I
- o -
10 11 12 1
10/16
7 8
10/17
7 8
10/18
DATE
Figure 70. Microbiological indices, mixed liquor - Medfield -
Phase 3A.
In the conventional process the formation of an old sludge
generally results in a turbid effluent with a high SS concen-
tration. Typical causes of old sludge are excessive aeration
tank detention time, low influent organic loadings and in-
sufficient wasting.
A highly filamentous floe is indicative of a potential
sludge bulking condition. The occurrence of excessive fila-
mentous growth can result from various adverse conditions in
the process. These include organic and hydraulic overloads,
too long or too short a sludge age, dissolved oxygen problems,
PH problems, toxicity, and industrial shock loadings.
149
-------
C£
8
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5
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INDIVIDUALS
(X10)
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DIVERSITY"
INDEX
1 1
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MON. 11/14/77
6 10 2 6
TUBS. 11/15/77
1
1
- O--O-
1
6 10 2 6 6 10 2 6 10
WED. 11/16/77 THURS.11/17/77 FRI. 11/18/77
DATE
Figure 71. Microbiological indices, mixed liquor - Medfield - Phase 3B.
-------
8
7
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5
a:
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Ul
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SPECIES
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INDIVIDUALS
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DIVERSITY
INDEX
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MON. 11/14/77
6 10 2 6
TUBS. 11/15/77
6 10 2 6 6 10 2 6
WED. 11/16/77 THURS.11/17/77 FRI.11/18/77
DATE
Figure 72. Microbiological indices, secondary effluent - Medfield - Phase 3B.
-------
Microorganisms
A "good" activated sludge from the conventional process
operated at a mean cell residence time of five to ten days
usually has representatives from many protozoa species. There
is generally a high concentration of both the free swimming and
stalked ciliates: the latter is usually the predominant form.
Free swimming flagellates are generally present in relatively
high numbers. These are found in greater abundance in unstabil-
ized sample sludge, i.e., short mean cell residence time. Roti-
fers may or may not be present. Their presence is usually
indicative of the highly stable conditions associated with a
long mean cell residence time.
Non-ideal or adverse process conditions create a variety of
changes in the relative distribution of indicator groups. A
young sludge condition will cause a predominance of the free
swimming forms, both ciliates and flagellates. An old, well
stabilized sludge may be entirely lacking in the free swimmers
and have an abundance of stalked ciliates and rotifers.
Changes in organic loading can disrupt the distribution of
organisms.
Phase 1 - Results
In the first stage aeration tanks, floe characteristics
and indicator organism populations were typical of a well-run
conventional process with a slightly long mean cell residence
time. The results are shown in Table 58. The floe was well
defined, medium to small in size, slightly granular in texture,
grey-brown in color, and contained few filamentous forms. The
predominant indicator group was the stalked ci.liated protozoa.
Free swimming flagellates were consistently present in suffi-
cient numbers to cause turbidity in the floe interspaces, but
were not in the abundance usually found in a young sludge. Free
swimming ciliates were very few in number, and no rotifers
were detected.
In both compartments of the nitrification process (Tables
59 and 60) floe characteristics and organism populations indi-
cated a highly stabilized condition. In the first compartment
floe was very small and granular, with jagged edges and a golden
brown color. The interspaces were clear but the floe was
highly filamentous. In the last compartment floe conditions
were very similar to the first except that filamentous forms
were even more numerous. During the course of the Phase 1
study, the quantity of filamentous forms slowly decreased.
Their presence in the sludge mass did not appear to cause any
adverse effects in the process and probably helped by slowing
the settling rate of what would otherwise have been a very
rapidly settling sludge. The predominating indicator group
152
-------
TABLE 58. MIXED LIQUOR MICROBIOLOGICAL INDICES
AND FLOC CHARACTERISTICS - MARLBOROUGH
FIRST STAGE
PHASE
2A
Floe Characteristics
Color
Size
Texture
Edges
Interspaces
Filamentous
Grey
Grey-
Brown
2B
Yellow-
Grey
Brown
Yellow-
Grey
Brown
Small to Medium - -
Fairly Granular - -
- Well Defined - -
Slightly Turbid - -
- - Few ------
Species
Free Swimming
Flagellates
Free Swimming
Ciliates
Numerous
Few
Fairly
Numerous
Numerous
------- Few -----------
Stalked Ciliates ----- Predominant --------
Rotifers None - - - - None - - Few - r- - Few -
TABLE 59. MIXED LIQUOR MICROBIOLOGICAL INDICES
AND FLOC CHARACTERISTICS - MARLBOROUGH
SECOND STAGE - FIRST COMPARTMENT
PHASE
2A
2B
Floe Characteristics
Color
Size
Texture
Edges
Interspaces
Filamentous
______ Golden Brown -------
______ very Small --------
_____ Very Granular --------
Jagged - - Jagged - - Fairly - -Fairly Well
Well Defined Defined
------- Clear ----------
Numerous ------- Fairly Numerous
(continued)
153
-------
TABLE 59. (continued)
PHASE
1 2A 2B 3
Species
Free Swimming Fairly
Flagellates Few - - - - Few - - - Few - - -Numerous
Free Swimming
Ciliates ________ pew ---------
Stalked Ciliates -------- Few ---------
Rotifers _______ predominant -------
TABLE 60. MIXED LIQUOR MICROBIOLOGICAL INDICES
AND FLOC CHARACTERISTICS - MARLBOROUGH
SECOND STAGE - LAST COMPARTMENT
PHASE
1 2A 2B 3
Floe Characteristics
Color _______ Golden Brown ____--
Size _____ very Small to Small -----
Texture Very Very Fairly Well Fairly Well
Granular Granular Defined Defined
Edges ________ jagged --------
Interspaces ________ clear ---------
Filamentous Fairly Numerous Fairly Fairly
Numerous Numerous Numerous
Species
Free Swimming Fairly
Flagellates - Few - - - Few - - - - Few - - Numerous
Free Swimming
Ciliates - None - - None - - - Few _ _ Few
________ pew __________
Rotifers _______ Predominant -------
in both compartments was the rotifers. No free swimming flagel-
lates, and very few free swimming and stalked ciliates were ob-
served.
154
-------
Phase 2 - Results
Septage addition in Phase 2 did not adversely affect either
floe or indicator organism population characteristics in the
first stage process. Floe characteristics, including color,
crispness of edges, and degree of turbidity in the interspaces,
if anything, improved. Indicator organism populations remained
stable and the occasional appearance of rotifers again indicated
improved floe quality. No significant detectable changes in
floe or indicator organism characteristics were observed in
either nitrification stage compartment. A very slight increase
in the free swimming flagellate population was not considered
to be significant.
Phase 3 - Results
No significant changes in floe characteristics or indicator
organism populations were observed in the first stage. Floe
remained healthy in appearance and showed no signs of disrup-
tion or stress. One noticeable change observed in indicator
organism characteristics was an increase in the size of the
stalked ciliates.
No significant changes were detected in the floe charac-
teristics observed during Phase 3 loadings in either nitrifi-
cation compartment. A slight increase in free swimming flagel-
late concentration in both compartments was the only change
observed in the indicator organism population and was not re-
garded as significant.
155
-------
SECTION 10
ECONOMICS OF SEPTAGE TREATMENT
COST OF TREATING SEPTAGE AT MUNICIPAL PLANTS
Septage treatment costs for municipal wastewater treat-
ment plants were divided into three categories: incremental
operation and maintenance costs, capital costs for equipment
and structures, and disposal site land costs. The emphasis
of this cost analysis is the operation and maintenance costs
associated with treatment at Medfield and Marlborough. These
costs are applicable to similar processes and scales of treat-
ment. A general discussion of capital costs is presented, but
capital costs are site specific. Sludge disposal at land fills
or by other means is not discussed, but must be included in
septage treatment cost estimates. Land disposal is a signi-
ficant and costly problem in some communities, while in other
communities ample space is available for septage sludge disposal
at a minimal cost.
OPERATING AND MAINTENANCE COSTS FOR TREATING SEPTAGE AT MEDFIELD
Records at the Medfield plant for the period prior to ini-
tiation of the research program indicated a fairly consistent
addition of about 0.5%, by volume, of septage. This level of
addition did not cause any modifications in plant operation, nor
any disruption in performance. However, it was a substantial
contribution to plant organic and solids loading and provided a
baseline condition for estimating the cost of septage treatment.
The baseline condition is shown in Table 61. Three separate
methods were used to estimate operating and maintenance costs;
each was based upon a separate set of assumptions.
Method 1 - Budget Item Cost Distribution
The operating budget of the plant was divided into thirteen
accounts as shown on Table 62. Each of the accounts was appor-
tioned between four characteristics of the wastewater: flow,
organic loading, total solids, and phosphorus. Both BOD and
COD were used as measures of wastewater organic content.
The cost distribution for Method 1 is shown on Tables 62
and 63. It was fairly easy to apportion power and chemical
costs with reasonable accuracy, and these two budget items
156
-------
TABLE 61. MEDFIELD TREATMENT PLANT AVERAGES AND YEARLY TOTALS
Parameter
Influent
Septage
Yearly Totals
Flow
Organic Loading
BOD
COD
Total Solids
Phosphorus
1,135 cu in/day
(0.30 mgd)
138 mg/1
(156.6 kg/day)
293 mg/1
(332.5 kg/day)
437 mg/1
(496 kg/day)
10.9 mg/1
(12.4 kg/day)
1,740 cu m/yr
(460,000 gal/yr)
4,664 mg/1
(8,115 kg/yr)
14,564 mg/1
(25,340 kg/yr)
11,549 mg/1
(20,100 kg/yr)
127 mg/1
(221 kg/yr)
416,400 cu m
(HOxlO6 gal)
65,300 kg/yr
(144,000 Ib/yr)
147,000 kg/yr
(324,000 Ib/yr)
201,000 kg/yr
(443,000 Ib/yr)
4,740 kg/yr
(10,440 Ib/yr)
TABLE 62. PERCENT DISTRIBUTION - MEDFIELD - METHOD 1
Electrical
Chemical
Supplies
Outside Services
Clean Sewer
Travel
Uniforms
Telephone
Heat
Truck Fuel
Motor Repair
Consultant
Personnel
% Cost
Based
on Flow
36
10
30
33
100
30
33
30
15
10
15
% Cost
Based on
Organic
Loading
21
30
33
30
33
30
15
20
25
% Cost
Based
on Total
Solids
Loading
42
17.6
30
33
30
33
30
65
100
100
60
55
% Cost
Based on
Phosphorus
Loading
1
72.4
10
1
10
1
10
5
10
5
represent more than 40% of the total cost. The distribution of
salaries, representing an additional 35% of overall costs, were
based upon operator judgment. Some of the other ten budget
items are specific to one characteristic of the wastewater, but
157
-------
TABLE 63. COST DISTRIBUTION - MEDFIELD - METHOD 1
Ul
CO
Electrical
Chemical
Supplies
Outside
Services
Clean Sewer
Travel
Uniforms
Telephone
Heat
Truck Fuel
Motor
Repair
Consultant
Personnel
TOTAL
TOTAL
TOTAL
ANNUAL
COST,
$
21,306
23,686
7,000
2,650
1,000
250
650
588
8,100
115
300
4,000
38,376
108,021
FLOW
$/cu m
0.0185
0.0057
0.0051
0.0021
0.0024
0.0002
0.0005
0.0004
0.0029
0.0010
0.0139
0.0527
$/l,000 gal
0.1995
ORGANIC
$/kg BOD $/kg COD
0.0685
0.0322
0.0134
0.0011
0.0033
0.0027
0.0186
0.0123
0.1469
0.2990
$/lb BOD
0.1356
0.0345
0.0143
0.0060
0.0005
0.0015
0.0012
0.0083
0.0054
0.0653
0.1370
$/lb COD
0.0621
Solids
$/kg SS
0.0445
0.0207
0.0105
0.0044
0.0004
0.0011
0.0009
0.0262
0.0006
0.0015
0.0119
0.1051
0.2278
$/lb SS
0.1033
Phosphorus
$/kg P
0.0450
3.6184
0.1477
0.0056
0.0053
0.0014
0.0124
0.0855
0.0844
0.4049
4.4106
$/lb P
2.0003
-------
most can only be distributed arbitrarily according to someone's
most reasonable estimate, with due regard to floor space occu-
pied, or in proportion to power consumed, etc. Justification is
essentially subjective for these costs.
Unit costs of removal for each wastewater characteristic
given on Table 63 were applied to average characteristics
of septage. Values shown on Table 64 were computed in accor-
dance with:
C = E(v + wBOD + y-SS + z-P)
or
C = £(v + x-COD + y-SS + z-P)
where C = the cost of treatment per cu m (1,000 gal) of septage
BOD = the organic loading in kg/cu m (lb/1,000 gal) as bio-
chemical oxygen demand
COD = the organic loading in kg/cu m (lb/1,000 gal) as chemi-
cal oxygen demand
SS = the suspended solids concentration in kg/cu m (lb/
1,000 gal)
P = the phosphorus concentration in kg/cu m (lb/1,000 gal)
v = cost per cu m (1,000 gal) of liquid
w = cost per kg (lb) of BOD
x = cost per kg (lb) of COD
y = cost per kg (lb) of suspended solids
z = cost per kg (lb) of phosphorus.
Table 64 shows that the operation and maintenance cost of
treating septage at Medfield was about $5.00 per cu m($18.50 per
1,000 gal). This estimate is based upon an initial assumption
that all functions and processes at a treatment facility are
necessary and contribute to the treatment of septage, i.e.,
the cost of treating an increment of organics, for example, is
the same for sewage and septage. Method 1 is considered ex-
tremely conservative and the costs shown overestimate septage
treatment expenses.
A second method was employed in which a different initial
assumption was made.
Method 2 - Limited Budget Cost Distribution
Fundamental to the second method is the assumption that
many budget cost items are independent of septage addition.
These items were not included in the septage treatment cost
determination.
159
-------
TABLE 64. BUDGET ITEM COST DISTRIBUTION - METHOD 1
Component
COD
BOD
SS
P
FLOW
Strength Unit Component
kg/cu m Treatment Cost,$/cum
mg/1 (lb/1,000 gal) Cost ($/l,000 gal)
14,564 14.6
(121.5)
4,664 4.7
(38.9)
11,549 11.6
(96.3)
127 0.13
(1.06)
__
S0.1370/kg
($0.0621/lb)
$0.2990/kg
($0.1356/lb)
$0.2278/kg
($0.1033/lb)
$4.4106/kg
($2.0003/lb)
$0.0527/cu m
($0. 1995/1, 000 gal)
2.00
(7.55)
1.41
(5.27)
2.64
(9.95)
0.57
(2.12)
0.05
(0.20)
TOTALS
Based on COD:
(COD + SS + P + Flow)
Based-on BOD: (BOD + SS + P + Flow)
= $5.26/cu m
($19.82/1,000 gal)
= $4.67/cu m
($17.14/1,000 gal)
Items included in the estimate were increased in various
ways. Electrical costs were increased by whole machine units,
i.e., power for an additional aerator, thickener or vacuum
filter was put in service for septage treatment. Chemical costs
were increased as flow, suspended solids, and phosphorus were
increased. The personnel costs expanded incrementally by the
addition of an additional staff member. Small increases in
fuel and motor repair accounts were included for completeness.
This approach is somewhat dependent upon economics of
scale. It is very unlikely that a large plant having many
operators would experience anything approaching the 33% manpower
increase called for in the Medfield case, where allowance for an
additional full-time staff member was made on a three-man base.
Some discrepancy might also be expected in the electrical bud-
get if operational flexibility were allowed. This analysis
did not allow variation in equipment use overtime; a rather ex-
treme position in any circumstances. It is felt that the
cost determined by this method is conservative for those items
budgeted. The cost of treating septage, based upon the above
assumptions, was $3.07/cu m ($11.62/1,000 gal). The results of
the second analysis are shown in Table 65.
Method 3 - Incremented Effort Cost Evaluation
The results of the third cost analysis are also shown in
Table 65. Base annual costs were actual costs incurred at
160
-------
TABLE 65. PLANT COST COMPONENT DISTRIBUTION
Base Annual
0.5% Septage
Electrical '
Chemicals
Truck Fuel
Motor Repair
Personnel"^
Total
Incremental
Cost
Cost
Condition
$21,306
23,686
115
300
38,376
83,783
Incremented Item*
Method 2
2% Septage Cost
$22,802
28,329
158
413
51,168
102,871
19,088
Incremented
Efforts**
Method 3
$21,848
29,092
158
413
45,929
97,440
13,657
Cost/cu m $3.07 $2.04
(Cost/1,000 gal) ($11.62) ($7.72)
Incremental volume of septage was 6,210 cu m/yr (1.64x10
gal/yr)
**Measured flow and septage volumes during testing were
908.4 cu m/day(0.24 mgd) and 18.35 cu m/day (4,848 gpd),
respectively
tElectrical power costs were $0.0066/kw-h
ttPersonnel costs were computed on the basis of $49.20/man-day
Medfield. The same limited inventory of item cost categories
was used as in Method 2. In Method 3 approximations were made
of the change in effort induced by a 2% septage loading. These
estimates were based upon the constant loading tests (Phase 2).
There was no constraint to assume whole-unit increments of
costs. The indicated treatment costs are therefore more inde-
pendent of the economics of scale.
Based upon oxygen demand data, aerator output was increased
four hours each day at the 2% loading. Labor costs were in-
creased by four man-hours per day, based upon observation of
the plant operation during the test period (Phase 2).
The cost of treating septage in Method 3 is based upon ex-
perience at Medfield during the test period, and represents a
best estimate of actual incremental costs. The cost was $2.04/
cu m ($7.72/1,000 gal).
Costs of treatment determined by each of the three sets of
assumptions indicate clearly that treating septage along with
domestic wastewater is a relatively expensive undertaking at an
161
-------
extended aeration facility. Septage treatment appears to cost
about eight to twenty-two times as much as sewage treatment at
Medfield.
Costs derived in Method 1 are clearly too high. Results
for this method indicate that the cost of operating the Medfield
plant at a 2% septage loading would increase the cost of opera-
tion by $30,567.00 per year, or by 28.3%.
The second and third methods, which address the costs in
terms of increments of additional expenditure, clearly provide
more realistic representations of the cost. Method 1 assumes a
linear relationship between cost and waste characteristics.
Only that part of the chemical costs for phosphorus removal
closely approximates a linear model. Most other costs are
essentially constant below a certain threshold (undefined),
and then begin to respond in a way that has not been studied.
Although Method 1 is not representative, it serves to indicate
an upper limit.
Analyses 2 and 3 appear to show a reasonable range of costs,
The cost would be larger at a small plant that might have a
proportionally larger increment of cost due to putting on more
staff, or because the machine time increment was large when
processing septage at 2%.
A major portion of the cost of treating septage at Med-
field is associated with oxidizing septage organics in the aera-
tion basins. A conventional plant with primary clarification
could expect to treat septage for less than experienced in an
extended aeration mode of treatment.
MA.RLBOROUGH - ECONOMIC IMPACT OF SEPTAGE ADDITION
Septage additions at Marlborough were attenuated by the
primary clarifier to such an extent that no significant increase
in loadings were experienced by secondary or nitrification
processes. As a result, increased operating expenses asso-
ciated with accepting septage were reflected only in solids
handling and disposal costs.
Items considered in ascribing costs to solids handling and
disposal include; 1) chemicals, 2) vacuum filter manpower,
3] utilities, 4} vacuum filter maintenance - including fil-
ter cloth, 5) the solids disposal truck driver, and 6) the solids
disposal site equipment operator. Capital equipment depre-
ciation and disposal land costs are not included, thus, the
following estimates are for additional operating costs only.
Estimates of present manpower requirements for the solids
train,vacuum filter maintenance and cloth life were provided by
the plant superintendant, as were the manpower requirements
162
-------
associated with the various elevated solids levels. Chemical
costs were taken from present bid prices obtained at Marlborough.
Cost projections have been made using the incremented effort
method described in the Medfield study.
Table 66 shows unit costs and projected total solids treat-
ment costs of 10, 50 and 100% over present levels for solids
handling.
TABLE 66. SOLIDS HANDLING AND DISPOSAL UNIT COSTS AND ESTIMATED
INCREASES AS A FUNCTION OF SOLIDS LOADING INCREASE - MARLBOROUGH
Item
Unit Cost
Usage Increase
Increase in Solids Processed
10 50 100
Chemicals
Lime
Ferric
Chloride
Vacuum Filter
Manpower
Vacuum Filter
Maintenance
Vacuum Filter
Cloth
Solids Disposal
Truck Driver
Disposal Site
Equipment
Operator
Utilities
$0.0018/kg 10%
(7.85/ton)
$0.0497/kg 10%
(218.80/ton)
$7.05/man-hour 0
$150/yr 10%
$1800/yr 10%
$ 7.0 5/man-hour 0
$7.05/man-hour
$2755/yr
(3% of total
Utilities Budget)
50%-
50%
day
50%
50%
day
week
20%
100%
100%
3 man-hrs 6 man-
hours
day
100%
100%
1 man-hr 2 man-
hours
day
6 man-hrs 12 man-
hours
week
40%
163
-------
Suspended solids data from Phases 2A and 2B indicate that
a septage loading of 1.25% increased solids wasting by 54%,
while a loading of 2.14% increased wastage by 100%. Therefore,
the percentage increase in solids wasted is about 50 times the
septage loading expressed as a percentage of flow. Since
Marlborough presently accepts approximately 0.16% of its total
flow as septage, increases in septage solids input of 10, 50
and 100% would correspond to total septage loadings of 0.36%,
1.16%, and 2.16%, respectively.
Total operating costs for solids handling and disposal at
the various loadings are shown in Table 67. The relatively
low cost of treating these levels of septage, when compared to
the Medfield study, is a result of treating septage primarily
in the solids train.
CAPITAL COSTS
Physical facilities for receiving, storing, feeding and
treating septage are site specific. Capital costs from loca-
tion to location can be expected to vary considerably.
An engineering design for a septage receiving station,
located at a municipal treatment facility, would be based upon
a number of considerations. These would include:
a. Anticipated septage loading, sewage flow rate and
variability in septage hauling schedules
b. Is the receiving station to be constructed at an
existing waste treatment plant or at a new plant?
c Are primary clarifiers available "or planned for com-
bined sewage and septage solids removal?
d. Is there capacity for septage treatment in secondary
and tertiary processes?
e. Sludge dewatering procedures and operating schedules
A receiving station is required at all plants handling
septage. Facilities exist that consist of nothing more than
paving for truck egress and a discharge manhole leading to a
grit chamber, a primary clarifier, or an aeration basin.
This type of an arrangement is not nearly adequate. A receiv-
ing tank should be designed to permit feeding a plant septage
at desired rates and on a schedule that is in harmony with
solids wasting and dewatering operations. Holding facilities
should be sized to permit septage flow attenuation and flexi-
bility for plant operation and maintenance. Septage should be
kept in suspension within a holding tank - air mixing is
recommended. Mechanical grit removal equipment is necessary.
Holding facilities and unloading areas should be covered and
ozonation is suggested for odor control.
It is conceivable that septage holding tanks would be
preceded by bar racks, but if screening devices are proposed,
164
-------
TABLE 67. PRESENT AND PROJECTED COSTS OF
SOLIDS HANDLING AND DISPOSAL - MARLBOROUGH
Item
Chemicals
V.F. Man-
power
V.F. Cloth
& Maintenance
Utilities
Present
Yearly
Cost
$16,650
29,330
1,950
2,755
10%
Increase
in Susp.
Solids
Handled
18,315
29,330
2,145
2,755
50%
Increase
in Susp.
Solids
Handled
24,975
34,830
2,925
3,305
100%
Increase
in Susp.
Solids
Handled
33,300
40,330
3,900
3,860
Disposal
Truck Driver 14,670
Disposal Site
Equipment
Operator
5,870
14,670
5,870
16,500
8,070
18,340
10,270
Total 71,225 73,085
TSS Increase
Ib/year 174,700
Cost of Extra
Solids
?/metr~ic ton 24.24
($/ton) £21.99)
Cost of
Treatment
$/cu m 0,26
($/1000 gal) Cl.OQ)
Cat 11,000 mg/1 TSS)
90,605
110,000
873,400 1,746,800
48.95
(44,40}
0,54
(2,04)
48,95
C44.40)
0,54
(2,04}
they must be chosen with considerable care, based upon document-
ed experience with septage. Septage can be settled in a grit
chamber, but unlike sewage grit, settled septage solids are
highly organic and must be put through a dewatering and stabili-
zation process. There are obviously any number of designs
possible for receiving facilities and capital costs would vary
accordingly. Capital costs for septage handling will also
165
-------
include the cost of large diameter mains and pumps to facili-
tate septage transmission without clogging.
Dewatering process costs can be the major capital_expendi-
ture associated with septage handling. An average capital cost
estimate for total sludge handling for sewage sludge is about
$132/cu m ($0.50/gal) of daily sewage flow.iy Based upon a
septage to sewage solids ratio of 50:1, the capital cost for
total solids handling for sludge derived from septage is
$6,600/cu m ($25,000/1,000 gal) of average daily septage input
to a plant.
There would be a significant capital cost for aeration
equipment for secondary treatment of septage with sewage.
Since septage addition does not add appreciably to plant flow
rate, final clarifier design can be based upon sewage loading.
However, aeration tank size must be based upon the organic con-
tent of the combined sewage and septage influent to the secon-
dary process. A considerable reduction can be made in aeration
equipment and aeration tank size if a large portion of the in-
coming septage solids are removed in a grit chamber or primary
f-* ~\ -^ -V* -1 -P "I ^^ -V*
clarifier.
19
Tihansky, Dennis P., "Historical Development of Water Pollu-
tion Control Cost Functions", Journal of Water Pollution
Control Federation, Vol. 46, May 1974, pp. 813.
166
-------
SECTION 11
SYNTHESIS OF RESULTS
DESIGN PARAMETERS
Septage Strength
Domestic septage is about fifty times as strong as domestic
sewage. A 2% addition of septage, on the average, doubles
solids and organic loading on the treatment facility. Septage
is a readily treatable waste at extended aeration and conven-
tional activated sludge plants. Mixed liquor bacteria are well
adapted to assimilate septage; oxygen uptake rates increase
rapidly as septage is added to an aeration basin. Septage does
not exert an initial oxygen demand other than that caused by
dilution of an anaerobic material in a partially aerated mixed
liquor.
Domestic septage and sewage obviously derive from the same
source, but in some respects, the properties of septage differ
from those of sewage. Concentrations of solids, organics, and
nutrients are obviously much higher; ratios of nitrogen and phos-
phorus to carbon tend to be lower than found in domestic sewage.
Chemical characteristics of septage are extremely variable
and commercial and industrial wastes are, at times, hauled with
domestic septage. Septage can contain grit, plastic material,
and large amounts of hair that clog conduits and wear out equip-
ment designed for handling sewage. Raw septage is difficult to
dewater unless acidified, chemically treated with coagulants or
mixed with raw or secondary sludge.
Design parameters for septage-sewage mixtures are given in
the following sections.
Dissolved Oxygen Requirements
The aeration basins utilized for this study were fed septage
in various ways, at a number of loading rates. The four aera-
tion basins at Medfield were fed raw septage directly from
holding tanks. The basins operated in series and mixed liquor
solids concentrations were maintained at high levels.
First stage aeration basins at Marlborough were fed efflu-
ent from a primary clarifier receiving a combination of sewage
167
-------
and septage. The mixed liquor solids content of these basins
was comparatively low, and the basins were operated in parallel.
The nitrification stage (second stage) basins at Marlborough
were not affected by septage addition. Non-oxidized remnants
of septage added to the first stage were not found in secondary
effluent.
The Lowell aeration basins were fed septage directly,
while operating both as an extended aeration and conventional
activated sludge facility.
The three plants were loaded both at constant rates and
with pulse inputs. Lowell and Marlborough were loaded to near
design capacity with sewage prior to septage addition. Med-
field was very lightly loaded prior to septage addition, and
had ample capacity for the large quantities of septage dis-
charged directly to its aeration basins. Marlborough also
received large quantities of septage, but at this plant the
heavily loaded aeration facilities were protected by primary
clarifiers that proved to be extremely effective in removing
septage from the waste/water stream.
Dissolved oxygen utilization during the constant feed
tests at Medfield was between 0.59 and 0.74 kg 02AgBODs.
At Marlborough, utilization was between 0.69 and 1.11 kg
02/kg BOD5. Oxygen utilization based upon COD was more con-
sistent at the two plants, averaging 0.21 kg O2/kg COD at
Medfield and 0.41 kg O2/kg COD at Marlborough. At Lowell,
oxygen utilization was 0.78 kg 02/kg COD when the plant operated
as a conventional process and 0.58 kg 02/kg COD when it was
operated in the extended aeration mode.
Oxygen utilization at treatment facilities depends upon
mixed liquor solids concentrations, process loading, and, in
general, plant operation. The above dissolved oxygen utili-
zation estimates covered a wide range of operating conditions,
and yet remained within the range of normal experience. Per-
haps more germane, septage did not markedly change oxygen
utilization rates experienced with sewage alone. The trend
usually observed during the course of this research was an
improvement (or decrease) in oxygen utilization per kg of COD
or BOD, with septage addition.
The implication for designing constant-feed systems for
septage is that oxygen demand can be estimated based upon
parameters used for high strength sewage. Total oxygen utili-
zation either for design or determining excess plant capacity,
should be based upon average septage BOD, COD values, or, as
an approximation, fifty times the value for sewage.
Assume, for example, that septage were added at a constant
rate to a plant, doubling the organic loading, but not apprecia-
168
-------
bly changing the hydraulic loading. Oxygen requirements based
upon the equation,
O (kg ) = Food utilized _ "1 ("organisms wasted"
per day J L per
would approximately double. This, of course, assumes that
wasting would be doubled to maintain a constant mixed liquor
solids concentration, and that the BOD rate-constant is the same
with or without septage. However, there is no reason to suppose
that oxygen transfer efficiency will remain the same after sep-
tage addition. Increased food addition to a biological oxida-
tion process generally lowers dissolved oxygen levels and im-
proves transfer rates. Dissolved oxygen uptake rates increased
significantly in Phase 2A at Medfield (2% constant septage feed
for 3 weeks) and in the conventional mode tests at Lowell.
Oxygen transfer at Medfield increased from 1.2 to 1.4 kg O^/kw-h
(2.0 to 2.3 Ib/hp-h).
In conclusion, air requirements for activated sludge and
extended aeration facilities can be based upon COD or BOD input
to the secondary process and anticipated oxygen transfer effi-
ciencies.
Shock loading can place a severe demand on a plant's aera-
tion capacity. This was seen at Medfield and at Lowell. At
Lowell, aeration capacity limitation finally upset the plant.
At Marlborough the primary clarifier took the brunt of the
septage input, diminishing the need for increased air capacity.
The initial oxygen demand caused by a shock load is the
volumetric ratio of septage to mixed liquor, multiplied by the
mixed liquor dissolved oxygen concentration. This demand is
relatively minor. The major decline in dissolved oxygen (90%
or more during this study) was caused by rapid increases in
oxygen uptake rates. The general effects at Medfield were very
low oxygen levels or a loss of mixed liquor dissolved oxygen for
short periods of time, rapid recovery, and little or no effect
upon effluent quality. However, if the quantity of septage
is large enough, or if the loading is repeated too often, upset
occurs as was experienced at the Lowell plant.
A plant can take at least twice as much septage if fed
continuously than if shock loaded. This is based upon air re-
quirements. If septage were not fed during periods of high
sewage inflow, plant capacity would be further increased.
Sludge Production
The constant loading at Medfield provided a record of
sludge wasting that enabled correlation between septage charac-
teristics and cake production. There was, at Medfield, a direct
169
-------
relationship between total solids in combined sewage-septage
influent and cake production. A 46% increase in total solids
input in Phase 2A at Medfield resulted in a 41% increase in
cake solids production. A 100% increase in BOD^ and soluble
COD at Medfield caused a corresponding 79% increase in produc-
tion of mixed liquor volatile suspended solids.
Secondary sludge derived from a combination of sewage and
septage at Medfield, or with primary sludge containing septage
plus secondary sludge at Marlborough, did not affect vacuum
filter performance. Chemical addition per unit weight of
sludge did not vary and sludge cake characteristics remained
unchanged.
The thickening process at Medfield changed perceptibly
with increasing waste return sludge concentration—thickened
sludge concentration declined. There was no change in the
vacuum filter filtrate or in thickener supernatant.
Thickener and vacuum filter design for combined septage
and sewage treatment can be based upon the solids and organic
content of the combined plant influent, plant process charac-
teristics, i.e., biological sludge production and the effi-
ciency of primary clarification, and conventional thickener
and vacuum filter design criteria.
Aeration Process Loading
Design parameters normally used for conventional and exten-
ded aeration plants appear to apply to plants receiving
quantities of septage between 1 and 3% of the sewage flow.
Typical values are shown in Table 68.
TABLE 68. TYPICAL DESIGN PARAMETERS*
Conventional Extended
Activated Sludge Aeration
Mean Cell Residence Time,
0 , days 5-15 20-30
C
Food-to-microorganism Ratio,
U, kg BOD5/kg MLVSS-day 0.2-0.4 0.05-0.15
Mixed Liquor Suspended Solids,
MLSS, mg/1 1,500-3,000 3,000-6,000
Volumetric Loading,
kg BOD5/cu m .32-.64 .16-.40
(Ib BOD5/1000, cu ft) (20-40) (10-25)
*Metcalf and Eddy, Wastewater Engineering, McGraw Hill, New
York, 1972, p. 498.
170
-------
Volumetric loading, kg BOD5/cu m (Ib BOD5/1,000 cu ft)
shown in Table 68 are considered conservative; while septage
increases organic loading, it does not significantly increase
hydraulic loading. Effluent quality is dependent upon mean
cell residence time or the F/M ratio. Since the recycling
rate is adjustable, treatment efficiency is theoretically inde-
pendent of hydraulic retention. However, in practice, a mini-
mum volume is required.
Primary Clarification
Primary clarifiers handling septage should be designed
conservatively. Either surface loading or detention time
criteria, customarily used for design, pertain to hydraulic
loading and conventional values are based upon experience
with domestic sewage.
Mixing of sewage and septage tends to diminish solids con-
centration differences at the inlet to a primary clarifier.
Differences are greatly minimized if septage is fed at low
constant rates instead of injecting slugs.
Septage solids appear to settle well in primary clarifiers.
In the constant feed tests at Marlborough, 69% of the sus-
pended solids load was removed from the wastewater stream by
the primary clarifier. The heavy solids in septage appear
to enhance settling. Density currents created by septage-
ladened water did not upset clarification,but rather carried
material more quickly to the clarifier bottom. This was ob-
served during shock loading at Marlborough when 79.5 cu rn
(21,000 gal) of septage was input to the 1,318 cu m (345,000
gal) clarifier in a period of 30 minutes.
While septage does not appear to cause excessive short
circuiting under constant septage feeding, accumulation of
anaerobic solids at the bottom can cause upset. This has
been a problem at Marlborough when sludge containing septage
accumulated too rapidly or was not wasted quickly enough,
particularly during summer months.
This research did not provide optimum design criteria for
clarifiers treating septage and sewage. However, the Marl-
borough clarifier, loaded at design hydraulic capacity with
sewage, functioned adequately while heavily loaded with septage.
The critical elements in clarifier design for combined
sewage and septage solids removal are effluent quality, sludge
removal and surface skimming. Settling and efficiency of re-
moval appear to be enhanced by septage. Septage can add
large quantities of grease solids which can quickly coat the
surface of a clarifier. Particular attention should be paid to
skimming mechanism design if septage addition is planned.
171
-------
Removing settled solids rapidly requires not only ade-
quate mechanisms but also adequate pump and dewatering capa-
city. Removal rate requirements can be quite high if septage
is slug loaded or a plant accepts and treats many loads of
septage on a particular day.
Secondary Clarification
Septage addition did not affect secondary clarification at
either Medfield or Marlborough. Clarifier upset experienced
at the University of Lowell plant was caused by oxygen defi-
ciency at high septage loading. When mixed liquor samples
were aerated during these high loading tests at Lowell, mixed
liquor settled well in settlometers. Secondary clarifier
design based upon conventional surface loading rates is
recommended.
GUIDELINES FOR SEPTAGE ADDITION
Septage Handling and Receiving
Large quantities of septage are not easily handled at
wastewater treatment plants, unless provisions are available or
provided to accommodate the unique physical characteristics of
septage. Septage can contain large quantities of grit, hair
and stringy material. It is highly odoriferous and is a
health hazard. The combination of these characteristics makes
it a difficult material to handle, particularly at small
plants where wastewater flows through small diameter conduits
and pumps. Generally, pumps that pass grit without wear tend
to clog with hair and string; grinder pumps that cut the hair
obviously can't handle grit. The 15 cm (6 inch) centrifugal
transfer pump used at Marlborough pumped about a thousand
cubic meters (several hundred thousand gallons) of septage
without clogging. The 8 to 10 cm (3 to 4 inch) submersible
pumps, centrifugal pumps and plunger pumps used at Medfield
clogged repeatedly. Fixed screens, with wire at 7 cm
(3 inches) on center clogged readily with septage hair. Vibrating
screens have been used successfully in experimental work. 2^
Handling the immense quantities of septage used in the
course of this study left researchers with a very clear
realization of the difficulties inherent in feeding septage at
controlled rates. As a general rule screening is not recommend-
ed, and where feasible, gravity flow through large diameter
20
A. J. Condren, "Pilot Scale Evaluations of Septage Treatment
Alternatives", U. S. EPA, EPA-600/2-78-164, September
1978.
172
-------
pipes is preferred. If pumping is necessary, small quantities
should be pumped intermittently at high rates with large pumps.
Pumping once every 15 to 30 minutes is suggested.
Septage is not sewage. Personal contact with septage while
cleaning screens and unclogging pumps or pipes is highly
undesirable. Designers cannot expect operators to perform
tasks that are objectionable and hazardous. When septage
handling at a plant is troublesome, haulers are turned away.
Continuous and Slug Loading
There are distinct advantages and disadvantages to both
constant and shock loading septage at municipal plants. Con-
stant loading places less of a demand on clarifier and aera-
tion facilities. Septage can be fed during low sewage-flow
periods, reducing the wide diurnal fluctuations of organic
loading normally found at wastewater treatment plants.
Constant loading requires construction and maintenance of
storage facilities and a septage transfer system that works
at low flows. This is by no means a simple task. Gravity flow
systems are best,but any flow control restriction easily
plugs with septage. A well-engineered gravity system is most
desirable and should be considered by design engineers. In-
termittent pumping with large size pumps is feasible.
A number of treatment plants now use a modified constant
flow system. Septage is discharged from trucks into an aerated
grit chamber. Sewage is bled into the chamber, diluting and
slowing displacing the septage. Each incoming septage load
displaces an equal quantity of the diluted mixture. This type
of system is better than direct discharge but obviously it can
be improved upon.
Storage provides an opportunity to pretreat septage. Pre-
treatment might include grit removal, aeration, grease removal
and chemical treatment of industrial loads of septage. Agita-
tion and oxygen exchange normally provided in aerated grit
chambers will neither keep all septage solids in suspension
nor render septage aerobic. Aeration does drive off dissolved
gases and will cause odor problems not experienced with quies-
cent holding tanks. Aeration also atomizes the septage
liquid, putting potentially infectious bacteria and viruses
into the air. Septage discharge, storage and pretreatment is
best accomplished in closed tanks with proper ventilation and
provision for odor control. Solids removal equipment should
be designed for a suspended solids concentration of about 10,000
mg/1. Septage holding and feeding tanks must be provided with
large capacity sludge removal equipment.
173
-------
Operation Control Strategies
Control strategies differ, depending upon the size and type
of plant accepting septage. The most cost effective way of
handling septage is to move it to the dewatering stage with as
little dilution as possible, i.e., wasting as much as possible
from a primary clarifier or combining with primary and secondary
sludge directly. This latter alternative has not been thorough-
ly investigated nor demonstrated at a plant, but research to
date indicates that it is certainly worth considering. The
approach does not require utilization of plant aeration capa-
city, which is often a limiting factor.
When aeration capacity or primary clarifiers are available,
combining septage and sewage at a plant inlet has distinct
practical advantages. Odor problems associated with storage
of septage alone are avoided and transmission problems, e.g.,
clogging, are minimized.
Much can be accomplished in septage treatment by regulating
hauling schedules and by feeding at times of relatively low
process loading.
174
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APPENDIX A
TABLE A-l
MEDFIELD TREATMENT PLANT PROCESS DIMENSIONS
Design Plow Rate:
Average Flow During Test Period:
Aerated Grit Chamber
Number of Units:
Number of Units in Use:
Length x Width x Height:
Volume:
Detention Time During Test Period:
Detention Time at Design Flow:
Primary Sedimentation Basins
Number of Units:
Number of Units in Use:
Length x Width x Height:
Volume:
Detention Time at Design Flow:
Overflow Rate at Design Flow:
Aeration Tanks
Number of Units:
Total Number of Compartments:
Number of Compartments in Use:
Compartment Length x Width x Depth:
Compartment Volume:
Detention Time During Test Period:
Detention Time at Design Flow:
Final Clarifiers
Number of Units:
Number of Units in Use:
Diameter:
Depth:
Volume:
Detention Time During Test Period:
Detention Time at Design Flow:
Overflow Rate During Test Period:
Overflow Rate at Design Flow:
0.066cu m/sec (l.Smgd)
0.012cu m/sec (0.28mgd)
2
1
4.6m x 4.6m x 2.7m (15ft x 15ft x 9ft)
56.8cu m (2005cu ft) (ISOOOgals)
1.29hra
0.48hrs
None (Used for Septage Storage)
25.3m x 4.6m c 2.7m (83ft x 15ft x 7ft)
247cu m (8715cu ft) (65200gals)
2.03hrs
24.5cu m/sq m-day
9.1m x 9.1m x 3.7m (30ft x 30ft x 12ft)
306cu m (lOSOOcu ft) (SOSOOgals)
7.08hrs
1.29hrs
2
1
12.2m (40ft)
2.7m (9ft)
316cu m (11310cu ft) (84600gals)
7.25hrs
2.71hrs
8.87cu m/sq m-day (219gpd/sq ft)
24.4cu m/sq m-day (602gpd/sq ft)
175
-------
TABLE A-2
MARLBOROUGH TREATMENT PLANT PROCESS DIMENSIONS
Design Flow Rate:
Average Flow During Test Period:
Aerated Grit Chamber
Number of Units:
Number of Units in Use:
Length x Width x Height:
Volume:
Detention Time at Design Flow:
Storage Tanks (Old Aeration Tanks)
Number of Units:
Number of Units in Use:
Length x Width x Height:
Volume:
0.24cu m/sec (5.5mgd)
0.145cu m/sec (3.5mgd)
2
1
7.6m x 3.7m x 2.5m (25ft x 12ft x 8.1ft)
70.3cu m (2194cu ft) (16400gals)
Detention Time During Test Period: 0.12hrs
0.14hrs
2
0
18.3m x 3.7m x 2.4m (60ft x 12ft x 8ft)
165cu m (5760cu ft) (99000gals)
Primary Settling Tanks
Number of Units:
Number of Units in Use:
Diameter:
Depth:
Volume:
Detention Time During Test Period: 2.56hrs
Detention Time of Design Flow: 1.54hrs
Overflow Rate During Test Period:
Overflow Rate at Design Flow:
2
1
21.3m (70ft)
3.7m (12.2ft)
1318cu m (47000CU ft) (352310gals)
35.leu m/sq m-day (857gpd/sq ft)
29.1m/sq m-day (715gpd/sq ft)
Aeration Tanks 1st Stage
Number of Units: 2
Total Number of Compartments: 4
Number of Compartments in Use: 2
Compartment Length x Width x Height: 24.2m x 12.2m x 3.7m (30ft x 40ft x 12ft)
Compartment Volume: 1089cu m (38400cu ft) (287200gals)
Detention Time During Test Period: 4.18hrs
Detention Time at Design. Flow: S.Olhrs
(continued)
176
-------
TABLE A-2 (continued)
Secondary Clari£ier
Number of Units:
Number of Units in Use:
Diameter:
Depth:
Volume:
/
Detention Time During Test Period:
Detention Time at Design Plow:
Overflow Rate During Test Period:
Overflow Rate at Design Flow:
Aeration Tanks 2nd Stage
Number of Units:
Number of Units in Use:
Number of Compartments per Unit:
Unit Length x Width x Height:
Unit Volume:
Detention Time During Test Period:
Detention Time at Design Flow:
Nitrification Settling Tanks
Number of Units:
Number of Units in Use:
Diameter:
Depth:
Volume:
Detention Time During Test Period:
Detention Time at Design Flow:
Overflow Rate During Test Period:
Overflow Rate at Design Flow:
2
1
27.4m (90ft)
3.7m (12ft)
288cu m(76200cu ft) (570000gals)
4.15hrs
4.98hrs
21.leu m/sq m-day (519gpd/sq ft)
17.7cu m/sq m-day (432gpd/sq ft)
2
1
4
24.4m x 24.4m x 3.7m (80ft x 80ft x 12ft)
2178cu m (76800cu ft) (574465gals)
4.2hrs
S.Ohrs
4
2
24.4m (80ft)
3.7m (12ft)
288cu m (76200cu ft) (570000gals)
4.15hrs
5.04hrs
13.4cu m/sq m-day (328gpd/sq ft)
11.leu m/sq m-day (274gpd/sq ft)
177
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TABLE A-3
UNIVERSITY OF LOWELL PILOT PLANT PROCESS DIMENSIONS
Flow Rate for Extended Aeration:
Flow Rate for, Conventional Process:
Aeration Tank
Number of Units:
Number of Sections:
Length of Each Section:
Width of Each Section:
Depth of Each Section:
Volume of Each Section:
Detention Time of Unit - Extended Aeration:
3Q.3CU m/day (1070cu ft/day) (8000gals/day)
109.Ocu m/day (3850cu ft/day) (28800gals/day)
1
2
2.01m (6.6ft)
2.74m (9.0ft)
2.74m (9.0ft)
15.leu m (534.6cu ft) (4000gals)
24.0hrs
Detention Time of Unit - Conventional Process: 6.7hrs
Settling Tank
Number of Units:
Diameter:
Depth:
Volume:
Detention Time - Extended Aeration:
Detention Time - Conventional Process:
Overflow Rate - Extended Aeration:
Overflow Rate - Conventional Process:
1
2.73m (8.96ft)
2.64m (8.67ft)
15.45CU m (597cu ft) (4090gals)
12.27hrs
3.41hrs
5.17cu m/sq in-day (127gpd/sq ft)
18.6cu m/sq m-day (457gpd/sq ft)
178
-------
Date
Day
Flow Rate., mgd
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Organic Carbon
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorus
Grease
PH
Temperature , °C
Alkalinity, CaCO,
•Labor Day
8/22
Mon
.227
232
83
130
71
80
479
166
64
64
22.9
13.9
.02
7-7
138
8/23
Tues
.203
254
87
110
95
78
432
222
67
26
12.1
.01
126
7.2
17
140
8/24
Wed
.276
373
103
170
94
89
458
173
184
172
25-5
11.2
.025
17-5
7-3
17
133
8/25
Thur
.238
247
87.6
139
81
400
156
82
67
13.1
.01
7.2
17
140
8/26
Fri
.232
266
75-^
69
63
408
166
61
44
13.4
.03
7.3
17
125
8/27
Sat
.200
286
75-^
69
74
424
188
94
82
11.5
.035
7.0
17
133
APPENDIX B
TABLE B-l
MEDFIELD - PHASE I (no septage)
INFLUENT (mg/1)
8/28 8/29 8/30 8/31 9/1 9/2 9/3
Sun Mon Tues Wed Thur Fri Sat
.165 .199 .226 .209 .192 .198 .157
119 273 1?4 390 202 362 319
4.3.7 115 79.1 108 91.3 80.7 66.9
144 127
39 70 68 133 89 107 103
62 93 68 78 69
339 427 366 422 4-01 532 447
112 183 184 175 137 234 178
37 48 18 204 46 178 146
18 39 9 148 33 148 110
27-4 21.6
9.4 12.4 12.5 12.3 13.7 13.2 10.3
.06 .04 .04 .07 .04 .0? .07
5-8 10.5
24.8
7.0 7.1 7.3 6.7 7.0 6.8 7.1
17 18 18 is 17 19 18
99 137 130 1/1.2 141
9/4
Sun
.129
240
66.9
107
98
66
429
146
141
106
13.6
• 07
9/5 9/6
Mon Tues
.129 .189
361 395
95.2 115
168 170
134 127
90 73
546 496
297 231
211 165
159 142
30.8
14.2 13.4
.04 .02
11.5
9/7 9/8
Wed Thur
.195 .242
289 296
111 111
133 150
101 114
67
408 483
170 191
104 115
84 93
25.2
13.3 15.4
.02 .01
10.0
9/9 9/10 9/11 9/12 x
Fri Sat Sun Mon
.340 .203 .180 .205 .206
117 283 259 34-0 276
36.4 85.0 72.9 134-
141
95 74 88 117 92.5
465 391 ^21 630 446
180 141 162 266 184.5
141 62 100 119 108
105 51 75 92
29.1 26
14.5 15-0 14.3 16.8 13.2
.11
.03 .02 0
11.0
7.1 7.1 7.1 7.0 7.1 7.0 7-2 7-1 7.2
18 18 18 17 18 1? 2L 19 17
138 14-4 136 132 145 IV? 155
-------
TABLE B-2
MEDFIELD - PHASE I (no septage}
SECONDARY EFFLUENT (mg/l)
00
o
Date
Day
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Organic Carbdn
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Ammonia-N
Nitrate-N
Total Phosphorus
Gres.se
pH
Temperature, °c
Sodium Aluminate, gal
* Grab samples taken 8/23 through 9/7
$ Composite samples taken 9/7 through 9/12
8/23
Tues
16
16
7.8
6.6
372
62
4.4
3.8
0
0.8
.61
7.5
19
15.4
8/24
Wed
19.8
15-9
6.6
2.4
6.6
312
3.4
1.4
.56
.22
5-0
7.4
19
15.4
8/25
Thur
23.8
27.8
5.5
1.5
4
287
55
6.6
3-9
.54
.21
.41
7.3
19
8/26 8/27
Fri Sat
27.9 23.8
19.9 23.8
3.9
0.9 1.1
6.5 6
327 312
90 70
4.8 4.3
4.3 2.6
•39 .11
1.73 2.2
7.1 7.4
18 19
17.6 17.6
8/28
Sun
27.8
23.8
0.8
6
311
75
3.2
2.0
.06
1.86
7.0
19-5
13.2
8/29
Mon
15.9
19.8
1.2
23
345
120
5.4
3.7
0
2.6
7.2
21
17.6
8/30
Tues
23.7
19.8
1.1
13.5
347
92
3.8
2.8
.17
1.3
.77
7-3
21
17.6
8/31
Wed
19.8
15.8
0.6
318
138
1.7
1.7
.65
3.8
4.0
7.3
20
8.8
9/1
Thur
23.9
23.9
0.4
4.5
320
86
4.3
2.1
.28
6.75
.68
7.1
20
9/2
Fri
15-9
11.9
0.6
5
355
97
8.0
6.7
.11
7-85
7.4
21
19.8
9/3
Sat
15.8
11.8
1.6
i.O
5
343
51
5.2
3.9
.11
6.0
7.2
22
17.6
9/4
Sun'
15.8
15.8
2.1
0.6
3
309
41
5.0
3.3
.22
5-9
7.3
20
13.2
9/5 9/6 9/7 9/7 9/8 9/9 9/10 9/11 9/12 x
Mon Tues Wed Wed Thur Fri Eat Sun Mon
19.7 23.8 19.8 27.7 15.8 16.2 8.1 4.0 23.7 19.5
7.9 19.8 15.8 23.7 15-8 16.2 12.1 4.0 23.7 17.5
1.6 2.3 2.5 2.2 3.6
0.8 0.3 0.5 0.4 2.7 1.2 1.1 0.7 1.0
25 8 72 10.5 14.5 12.9
330 397 316 308 368 339 334 346 378 336
38 100 69 77 HO 63 78 57 75 78.3
4.5 4.3 4.2 0.6 4.5 5.3 1.6 0.6 1.8 4.0
3.4 2.8 3.9 0.6 3-3 4.2 1.1 0 1.1 2.85
.11 .19 .06 0 .01 .17 .11 0 .22 .18
7.4 8.2 7.2 7.0 6.8 7.5 .7.6 7.75 7.72 4.93
.74 .68 .78 .67
7.2 7-3 7-3 7.2 7..4 7.5 7.4 7.4
19 17 19 18 16
15.4 15.4 17.6 13.2 13.2
-------
00
TABLE B-3
MEDFIELD - PHASE I (no septage)
MIXED LIQUOR (mg/1)
Date 8/23 8/24 8/25 8/26 8/27 8/28 8/29 8/30 8/3! 9/1 9/2 9/3 9/4 9/5 9/6 9/7 9/8 9/9 9/10 9/11 9/12
Day Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Fri Sat Sun Mon
Total Solids 9140 7880 8320 8680 8130 8320 8770 7760 8100 8010 7880 7930 8100 8520 7680 7990 7890 7520 7700 7790
Total Volatile Solids 6820 4730 5050 5290 4850 5080 5300 4610 48104810 4620 4540 4580 5110 4480 4690 4590 4400 4990 4530
Suspended Solids 8490 8620 7710 8010 8410 7850 7540 7590 7740 8160 7350 7680 7540 7180 7340 7450
Volatile Susp. Solids 5260 5890 5190 5020 5080 4620 4530 4450 4490 5000 4390 4610 4500 4320 4940 4480
PH
Temperature, °C
Alkalinity, CaCO-j
D.O. Uptake, mg/l/hr
Dissolved Oxygen
Basin #1
#2
#3
#4
Clarifier
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
7-1
20
246
12.6
5.9
.65
.75
1.1
1.2
980
950
920
890
860
830
750
670
7.2
19
245
18.3
2.1
.45
.70
1.10
1.6
920
850
790
730
670
620
510
450
7.1
19
229
6.9
4.0
.8
1.0
.8
1.0
960
920
870
830
790
750
640
560
7.0
18
223
24.0
3.9
1.3
1.0
.9
1.2
960
910
870
830
790
750
640
560
6.9
19
284
9.3
4.3
1.6
1.6
1.5
1.5
950
900
870
830
800
760
650
610
7.0
20
306
14.7
4.9
-5
.3
.2
.3
950
900
860
815
770
735
7.2
21
283
14.9
4.2
.5
.4
-5
.4
950
900
860
815
770
74o
640
560
7.0
21
255
27.0
3.5
.8
.8
• 7
.9
950
900
870
830
790
760
650
570
7.0
20
223
17.6
4.0
1.25
1.20
1.10
1.20
950
870
800
730
670
620
510
460
7.0
20
242
11.2
4.1
1.2
1.0
1 .0
1.25
890
790
700
630
570
530
450
400
6.9
21
244
16.4
4.1
0.8
0.5
0.4
0.6
950
900
840
790
740
690
580
510
6.9
22
16.8
3.2
0.8
0.5
0.5
0.7
950
900
840
780
720
670
560
490
7.0
20
15-1
4.9
0.9
0.6
0.6
1.2
950
905
850
810
760
720
610
530
7.1
19
233
10.1
4.3
1-3
1.05
1.0
1.25
960
910
870
820
775
730
610
540
7-0
19
245
12.3
6.2
1.8
1.75
1.75
2.1
950
900
860
820
780
735
630
550
7.1
20
257
15.0
5.6
0.6
0.25
0.3
0.4
970
910
860
800
750
700
575
500
6.8
19
221
9.2
*K7
0.5
0.1
0.2
0.1
955
900
840
780
74o
680
560
490
6.9
18
164
26.7
6.3
2.4
2.1
2.05
2.0
960
900
850
790
74o
690
570
500
6.9
19
12.6
5.7
1.9
1.1
1.0
1.2
950
880
830
770
700
660
6.9
19
13.5
5-9
1.7
1.2
1.1
1.1
920
830
730
660
590
550
460
6.8
, 17
192
10.6
6.65
2.6
2.5
2.3
2.3
950
900
840
780
720
670
560
490
-------
TABLE B-4
MEDFIELD - PHASE I
SECONDARY RETURN SLUDGE (mg/L)
CO
Tues Wed Thur Fri
Sat
Sun
11720 8560 60?0 104-10 7400 10390 5980
6940 5330 3540 6310 4510 6300 3590
Date
Day
Total Solids
TVS
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
Flow Rate, ragd .42? .430 .407 .453 .417 -374
Capillary
Suction Test
8/29 8/30
Mon Tues
5980 8080
3590 4860
.428 .431
8/31 9/1 9/2 9/3 9A
Wed Thur Fri Sat Sun
9280 11860 14910 10630 11040
5590 7020 94-10 6230 6330
970
920
870
840
790
750
650
570
.403 .411 .453 .430 .42?
9.7'
9/5 9/6 9/7
Mon Tues Wed
9550 9860 10970
5400 5750 6510
970
940
910
870
850
820
740
675
.374 .433 .441
9.1
9/8
Thur
9900
5860
970
945
920
890
870
84-0
765
700
.4-29
8.5
9/9 9/10 9/11 9/12
Fri Sat Sun Mon
9330 104-30 10320 9820
5440 6135 6000 5720
.469 .418 .370 .421
-------
TABLE B-5
MEDFIELD - PHASE I (no septage)
THICKENER AND VACUUM FILTER(mg/l except Sludge and Cake Values)
THICKENER
Date
COD-Total
BOD-Total
BOD-N Suppressed
Total Organic Carbon
Total Solids
Total Volatile Solids
Total Susp. Solids
Total Vol. Susp. Solids
Capillary Suction Test
Volume, gal
Supernatant Sludge
8/30 9/6 9/15 8/30 9/6 9/15
27-7 27.7 20.0
7 1.8
0.7
10
307
72
0
0
15
332
82
3-3
3-:
3^7 5.83$ 5.26 5.62
58 3.57 3.15 3-35
0
0
15.75 20.95 10-5
40^80*39570*31350* 6770* 8230* 7660*
VACUUM FIITER
Filtrate Cake
8/31 9/9 9/15 8/31 9/9 9/15
328 257 488
120
101 222
77 104
640 856 809 12.69^ 11.35 12.62
284 438 421 7.73 6.82 7.60
55 89 106
34 61 70
Conditioned Sludge
Capillary Suction Test
15.5 10.9 9.8
•Total Supernatant and Sludge
183
-------
Date
Mixed liquor
Total No. Organisms (N)
Total No. Species (S)
Diversity Index (H)
No. Organisms
Vortioella
Colpoda & Euplotes
Micro Flagellates
Macro Flagellates
Rotifers
Diatoms
Lionotes
Micro Ciliates
Suctorians
Nematodes
Spirochetes
Effluent
Total No. Organisms (N)
Total No. Species (S)
Diversity Index (H)
No, Organisms
Ciliates
Green Filaments
Micro Flagellates
Macro Flagellates
Scenedeswus
Colpoda
Pennates
Naviculum
Rotifers
Paramecium
Nematodes
Vorticella
TABLE B-6
MEDFIEID - PHASE I (no septage)
MICROBIOLOGICAL INDICES (mg/1)
8/25 8/26 8/29 8/30 8/31 9/1 9/2 9/5 9/6 9/7 9/8 9/9 9/12 9/13
73
4
.95
11
58
3
1
Iii4
7
1.47 2,
39
91
1
3
2
4
83
7
.15
28
27
16
1
7
2
2
65
9
2.18
18
20
20
2
1
1
1
1
1
77
7
2.12
28
27
1
7
4
1
9
44
7
2.33
14
14
4
5
1
1
5
48
8
1.93
17
22
1
1
4
1
1
1
78
7
1.84
8
48
9
3
7
1
2
29
9
2.79
7
8
1
1
3
1
1
3
29
8
1.94
_
18
1
1
1
3
1
1
25
4
1.15
1
19
2
3
70
6
1.76
-
44
6
4
9
2
166
7
1.64
25
110
4
1
7
10
171
7
1.48
12
122
1
2
7
8
9 19
30
6
1.67
5
3
1
1
19
22
6
2.05
7
3
1
1
1
9
15
5
2.11
6
3
2
3
10
7
2.72
1
1
2
1
2
(continued)
184
-------
TABLE B-6 (continued)
Date 8/25 8/36 8/29 8/30 8/31 9/1 9/2 9/5 9/6 9/7 9/8 9/9 9/12 9/13
Return Sludge
Total No. Organisms (N)
Total No. Species (s)
Diversity Index (fl)
No. Organisms
Vortioella
Colpoda & Euplotes
Micro Flagellates
Macro Flagellates
Rotifers
Diatoms
Lionotes
Micro Ciliates
Suctorians
Nematodes
Spirochetes
92
6
88
5
82
2
1
4
1
114
6
1.01
14
92
4
1
2
1
93
6
1.92
11
37
34
8
2
1
98
5
1.92
33
41
10
10
4
76
7
2.25
18
33
3
7
5
2
8
64
7
2.23
21
24
5
2
4
2
6
45
6
1.84
7
27
2
3
3
3
59
4
1.51
15
33
10
1
29
7
1.68
1
19
1
1
1
5
1
5^
8
1.95
33
2
5
5
2
5
1
1
71
11
2.36
21
30
1
3
5
1
5
2
1
1
1
90
8
2.42
18
53
4
3
6
2
4
142
7
1.33
1
107
4
6
14
1
9
156
6
1.42
11
113
1
7
10
14
185
-------
APPENDIX C
TABLE C-l
MEDFIELD - PHASE HA (continuous loading)
SEPTAGE (mg/1)
Date 9/13 9/14 9/15 9/16 9/17 9/18 9/19 9/20 9/21 9/22 9/23 9/24 9/25 9/26 9/27 9/28 9/29 9/30 10/1 10/2 10/3
Day Tues Wed Thur Fri Sat- Sun Mon Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Fri Sat Sun Mon
COD-Total 8730 5200 3080 4580 4680 2780 4-620 3560 8480 30000 lino 11030 34600 14-560 6960 9200 7550 58180 24-Soo 9170 14120
COD-Soluble 1120 1520 880 1360 880 2130 1417 1260 5180
BOD-Total " 2350 9300 12200 2190 2670 1620 1500 2130 3810 10000 3810 1845
BOD-N Suppressed 1500 2250 2320 2325 3970 2820 810 9600 10100 2790 2610 1280 1710 1640 10000 3450 1180 1980
Total Solids 6210 314-0 2500 2620 2980 2510 3150 2770 5230 5980 6010 5780 13650 8830 4750 4450 5450 12260 13530 7560 8930
H
CO Total Volatile Solids 4750 2300 16?0 1780 1920 1700 2170 1910 3650 4200 4240 4130 8890 5570 2920 2650 3600 6280 10230 5600 6710
CFi
Suspended Solids 5530 2450 1490 1310 1900 1650 1950 1750 3310 4050 5130 3750 10340 6690 3010 2810 3930 10620 11400 5850 7330
Volatile Susp. Solids 4440 2000 1190 1080 620 1320 1610 1290 2800 3550 3540 3110 7000 4860 2250 2060 2980 5620 9160 4650 5920
Total Kjeldahl-N 174 153 146 165 208 304 213 z^ 183 3^°
Ammonia-N 50.4 37-3 22.4 79.5 74.2 56.0 73.9 58.2 73.9 69.4 94.1 77.3 109 86.2 72.8 81.8 70.6 115 72.8 91.8 60.5
Total Phosphorus 220 60 200 110 105 120 120 160 120 105 95 120 215 87 70
Grease 590 6320 5?lTO 6260 6500 400
pH 6.9 6.9 7.1 7.1 7.1 7.1 7.1 7-3 6.5 6.9 6.8 6.6 8.1 7.3 7.2 6.7 6.7 6.0 6.3 6.4 6.8
Temperature, °C 20 17 22 18 23 21 19 16 16 18 14 16 18 18 18 18 15 18 19 18 16
ORP -710 -800 -785 -780 -540 -780 -585 -750 -580 -830 -580 -680 -560 -750 -570 -610 -680
Volume, gal 4-030 5970 534-0 4-700 3910 4220 5320 5220 4210 1+780 4900 4-300 4670 4870 5050 4840 4770 4220 4340 3860 4630
JS of Daily Flow 2.13 2.61 2.68 2.03 2.08 2.37 2.44- 2.04 1.85 2.17 2.14 1.94 2.27 1-50 1.90 1.88 1.90 1.69 1.62 1.51 1.60
Alkalinity 303 400 364 450 426 1149 745 631 599 439 495 490 335 381
-------
TABLE C-2
MEDFIELD - PHASE IIA (continuous loading)
INFLUENT (mg/1)
CO
Date
Day
Flow Rate, mgd
COD-Total
COD-Soluble
BCD-Total
BOD-N Suppressed
Total Organic Carbon
-J Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Amroonia-N
Nitrate-N
Total Phosphorus
Grease
pH
Temperature, °C
Alkalinity
9/13
Tues
.189
298
119
119
76
Wl
176
74
68
19.1
0.0
7-3
17
166
9/14
Wed
.229
328
100
126
79
4-57
1?8
110
92
27.2
17.0
0.0
9.2
79.2
7.2
17
153
9/15
Thur
.199
312
148
123
69
414
145
64
48
17.8
0.0
7.2
7.0
17
150
9/16
Fri
.232
672
198
697
410
353
259
36.1
17.8
0.02
16.5
7.2
18
160
9/17
Sat
.188
198
77.4
52
368
120
37
35
24.9
16.3
0.0
7.1
17
9/18
Sun
.178
230
87
87
379
126
59
52
14.3
0.0
7.1
19
145
9/19 9/20 9/21
Won Tues Wed
.218 .256 .228
327 395 372
48 154 180
141
72 194 128
66 76
488 450 444
244 196 165
253 159 100
186 99 74
23.8 24.9
11.4 13.9 15-3
0.0 0.0 0.0
13.0 9.8
83.2
6.8 7.2 7.1
18 17 15
118 129 145
9/22
Thur
.220
272
116
158
122
65
446
164
66
66
17.4
0.04
7.3
16
159
9.23
Fri
.229
413
270
482
217
120
89
27.2
18.0
0.0
11.0
7.1
17
9.24
Sat
.221
409
155
237
178
507
259-
141
107
14.7
0.0
11.0
6.8
16
9.25
Sun
.206
222
95
99
117
56
438
182
63
44
22.1
13.4
0.0
11.5
6.7
14
143
9.26
Mon
.324
456
100
208
154
78
496
235
209
124
23.0
12.0
0.0
10.7
7.4
17
126
9.27
Tues
.266
204
72
72
88
377
115
70
59
13.2
0.0
10.7
20
7-5
17
143
9.28 9.29 9.30 10.1 10.2 10.3 10.4 x
Wed Thur Fri Sat Sun Mon Tues
.257 .251 .261 .268 .256 .290 .236
296 257 249 189 197 172 308
84 76 83 83 150 82
147 176 114
107 119 111 103 77 105
46o 443 483 341 347 425
159 193 205 135 179 174
112 86 109 30 67 121
83 82 25 59 99
23.0 24.6
14.1 15.1 15.7 10.9 10.2 14.1 14.8
0.0 0.0 0.0
16.2 11.5 12.5 9.0 8.5
7.0 7.1 6.7 6.7 6.6 7.0 7.0
17 17 16 16 16 18 15
158 157 153 129 122 148
-------
H
00
Date
Day
COD-Total
COD-Soluble
BCD-Total
BOD-N Suppressed
Total Organic Carbon
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Ammonia-N
Nitrate-N
Total Phosphorus
Grease
pH
TABLK C-3
MEDFIELD - PHASE IIA (continuous loading)
SECONDARY EFFLUENT (mg/l)
Temperature ,
Na0 '
j , gal
9/13
Tues
11.9
11.9
0.5
4.5
353
72
0.9
0.4
.06
9.0
1.2
7.3
18
1 £ li.
9/14
Wed
20.0
20.0
1.9
5
332
^5
2.8
2.5
.62
8.4
1.1
4.4
7.2
18
9/15
Thur
12.0
16.0
1.8
6.5
349
98
2.8
1.6
• 30
12.5
2.1
7-1
18
TO {*
9/16
Fri
24.0
24.0
326
121
2.4
2.2
1.8
6.5
2.1
7-3
18
_^
9/17
Sat
43.8
13.8
0.3
292
3^
0.8
0.6
5.4
4.6
7-2
18
.1 1 •>-
9/18
Sun
24.0
15.8
0.6
5
280
39
1.5
l.l
5-2
6.1
2.0
7.2
21
9/19 9/20 9/21 9/22
Mon Tues Wed Thur
19.9 19.8 32.0 24.0
19.9 19.8 16.0 24.0
1.9 1.8
0.2 0.7 0.9 0.4
3 5 16.5
293 269 308 339
56 47 65 60
3-3 3.7 3-3 1.5
2.0 2.6 2.2 1.5
5.2 6.1 5.6 3-5
6.5 5.6 2.3 1.7
2.1 2.3 2.4
4.0
7.3 7-3 6.8 6.8
19 19 15 16
— ^ « R 1 1 n f, f.
9/23
Fri
135-
35.7
3.2
1.8
7.5
330
68
2.7
1.5
5-0
2.5
2.4
7.2
16
R R
9/24
Sat
67.5
27.8
4.1
0.9
6
351
83
3.1
1.6
*.5
2.7
1.9
7-5
15
R «
9/25
Sun
43-7
39-7
2.4
0.7
5-5
378
96
1.8
0.8
2.1
1.6
1.6
6.7
13
H H
9/26
Mon
32.0
28.0
2.8
0.4
5
306
69
2.7
0.8
2.2
1.5
1.8
7.3
18
1 e It.
9/27
Tues
32.0
24.0
8.6
3.0
332
79
8.6
6.7
3-5
0.2
0.9
3.2
7.6
18
1 n
-------
TABLE 0-4
MEDFIELD - PHASE IIA
MIXED LIQUOR (tng/1)
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, °C
Alkalinity
00 D. 0. Uptake1, mg/l/hr
Dissolved Oxygen
Basin #1
Basin #2
Basin #3
Basin #4
Clarifier
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
9/13 9/14
Tues Wed
8160 8160
4yifO 4790
7750 7830
4640 4?10
6.9 7-3
17.5 18.5
205 188
10.4 12.9
6.0 2.8
1.9 1.05
1.7 0.8
1.9 0.7
1.8 0.8
950 950
900 900
850 840
850 790
750 735
690 680
500 560
460 490
9/15 9/16
Thur Fri
7760 7880
1)490 4630
7460 7550
4450 4570
6.3 6.9
18 18
200 250
17.1 11.8
4.3 4.8
0.9 0.7
0.6 0.6
0.6 0.45
0.7 0.3
960 960
910 910
860 860
810 810
760 760
700 710
580 590
490 510
9/17 9/1-8
Sat Sun
7750 7840
4630 4520
7420 7540
4550 4450
7.1 7.2
18 22
244
16.8 23.3
5.05 4.45
0.7 0.45
0.7 0.40
0.6 0.40
0.65 0.35
960 940
910 880
830 830
810 775
725 760
710 675
580 560
500 490
9/19 9/20
Mon Tues
7590 8150
43^0 4810
7360 7870
4310 4790
7.0 7.1
19 18
252 235
20.4 20.9
2.9 3.4
0.6 0.4
0.5 0.4
0.5 0.35
0.4 0.3
960 950
910 900
860 850
810 800
750 790
715 710
600 600
510 520
9/21 9/22
Wed Thur
8330 7570
4880 4490
8060 7260
4850 4400
7.0 6.5
16 17
216 220
18.9 15-7
3.6 3-8
0.4 0.4
0.3 0.45
0.3 0.4
0.5 0.5
965 950
930 900
880 850
830 805
760 410
740 710
610 590
530 500
9/23
Fri*
5700
3300
5350
3260
7.0
18
186
1*1.5
7.8
0.8
0.7
0.65
0.8
800
620
510
450
410
380
340
325
9/24 9/25
Sat Sun
8200 7910
4890 4750
7860 7530
4800 4640
7.1 6.8
14 15
23.0 22.6
2.5 2.8
0.2 0.3
0.2 0.2
0.1 0.2
0.2 0.2
920 940
850 910
780 870
720 830
660 790
620 750
,520 640
470 550
9/26 9/27
IV!on Tues
8650 8300
5180 4890
8250 8000
5100 4870
6.8 7.4
17 19
209 224
20.2 27.4
3.8 2.4
0.5 0.8
0 . 45 0.9
o . 45 0.9
0.55 1.1
980 950
940 900
900 855
860 810
820 770
780 730
690 620
590 540
9/28 9/29
Wed Thur
7250 7770
4280 4640
6930 ?420
4250 4560
7.0 6.9
18 17
280 266
25.7 21.4
2.4 1.5
0.2 0.2
0.2 0.2
0.2 0.2
0.4 0.3
940 960
890 900
845 850
800 800
755 750
710 690
600 585
510 500
9/30 10/1
Fri Sat
8020 8080
4760 4?00
7680 7770
4630 4590
6.7 6.8
16 18
268 256
23.3 28.6
4.0 2.7
0.4 0.3
0.4 0.3
0.3 0.3
0.4 0.5
960 960
915 910
860 860
810 815
760 770
710 725
600 610
510 525
10/2
Sun
8500
5000
8010
4890
6.7
19
272
28,2
2.4
0.4
0.2
0.4
0.5
950
900
860
800
740
680
560
500
10/3 10/4
Mon Tues
8530 8600
5080 5200
8210 8300
4960 5140
6.5 6.9
17 16
268 283
33-2 17.3
3.4 4.2
0.3 0.2
0.3 0.2
0.2 0.3
0.4 0.2
960 955
920 915
880 860
840 815
800 765
760 720
640 600
510 520
*Sludge return off, 3pm to Sam
-------
TABLE C-5
MEDFIELD - PHASE IIA (continuous loading)
SECONDARY RETURN SLUDGE (mg/1)
Date
Day
Total Solids
TVS
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
4-5 minutes
60 minutes
Flow Rate, mgd
Capillary
Suction Test
Date
Day
Total Solids
TVS
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
Flow Rate , mgd
Capillary
Suction Test
9/13
Tues
9700
5630
960
930
900
870
840
790
630
580
.1+21
9.25
9/27
Tues
12020
7090
990
970
955
940
920
900
855
'800
>33
9/14 9/15
Wed Thur
10070 9910
5840 5760
980
960
935
910
880
830
770
690
.438 .448
8.75
9/28 9/29
Wed Thur
8250 10930
4860 6560
970
940
915
890
870
84-0
770
690
.392 .4-20
10.9
9/16 9/17 9/18 9/19 9/20 9/21
Fri Sat Sun Mon Tues Wed
9770 10000 10060 12130 10610 1074-0
5650 5900 5830 6970 5310 6290
980
960
9*1-0
915
895
870
810
750
.417 .450 .34.8 .403 .399 .395
9.1 8.5
9/30 10/1 10/2 10/3 10/4
Fri Sat Sun Kon Tues
10380 11050 11720 11550 114-90
5750 6360 6930 6890 6950
.4-19 .493 >00 .4-33
10.1
9/22 9/23 9/24- 9/25 9/26
Thur Fri Sat Sun Mon
9760 35060 9120 9190 11030
5770 20750 5^30 5550 6570
970
94-5
920
890
865
84-0
710
690
.128* .413 .37^ .359 -382
10.5
*Return sludge pump off from 2pm to 7am
190
-------
vo
H
TABLE C-6
MEDFIELD - PHASE IIA (continuous loading)
THICKENER AND VACUUM FILTER
(mg/1)
Date
Day
COD-Total
BCD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Total Susp. Solids
Total Vol. Susp. Solids
Capillary Suction Test
Volume, gal
Date
Day
COD-Total
BOD-Total
BOD-N Suppressed
Total Organic Carbon
Total Solids
Total Volatile Solids
Total Susp. Solids
Total Vol. Susp. Solids
Capillary Suction Test
* Total Supernatant and Sludge
9/21
Wed
2k,
1.9
1.5
286
3^
6
s 3
25100*
9/26
Kon
20
0.2
0.2
297
66
3^
28
14190
Filtrate
9/26 9/28
Mon
563
384
247
143
893
460
166
Is 9^
Wed
1660
411
238
2050
1110
2820
1?40
Supernatant Sludge
9/27 9/28 10/3 10/4 10/5 9/21 9/26 9/27 9/28
Tue
24
1.6
2.1
325
69
3
0
19260
10/5
Wed
688
921
404
512
318
Wed Mon Tue Wed Wed Mon Tue Wed
20 24 28 - 35
1.4 1.7 1.7
1.5 0.2 2.0
319 318 297 3^8 ^.5953 ^-68 4.28
48 60 45 36 2.70f° 2.80 2.64
3 o 0 14
0008
11.4 21.5 19.2 12.5
12850 19920 11220 17710 8560 8670
VACUUM FILTER
Cake Cond. Sludge
9/26 9/28 10/5 9/26 9/28 10/5
lion Wed Wed Mon Wed Wed
12.23S 12.0?S 11.955
7.375 7.W 7-W
10/3 io/4 10/5
Mon Tue Wed
4.78 4.85 4-53
3.00 3.05 2.79
13.6 10.5 14.3
13400
8.0 10.6
-------
TABLE C-7
MEDFIEID - PHASE IIA (continuous loading)
MICROBIOLOGICAL INDICES
Date 9/14 9/15 9/16 9/19 9/20 9/21 9/22 9/23 9/26 9/27 9/28 9/29 9/30 10/3 10/4
Return Sludge
Total No.Organisms (N) 216 193 179 196 130 105 93 13 86 88 79 96 59 76 108
Total No. Species (S) 10 98888778988777
Diversity Index (H) 1.51 1.61 1.82 2.16 2.25 2.36 2.15 2.50 2.12 1.94 2.63 1-82 1.96 2.26 1.87
No. Organisms
Vorticella
Colpoda & Euplotes
Micro Flagellates
Macro Flagellates
Rotifers
Diatoms
Lionotes
Micro Ciliates
Suctorians
Nematodes
Spirochetes
Mixed Liquor
Total No.Organisms (N) 205
Total No. Species (S)
Diversity Index (H)
No. Organisms
Vorticella
Colpoda & Euplotes
Micro Flagellates
Macro Flagellates
Rotifers
Diatoms
Lionoteg
Micro Ciliates
Suetorians
Nematodes
Spirochetes
Effluent
Total No.Organisms (N)
Total No. Species (S)
Diversity Index (H)
No. Organisms
Ciliates
Green Filaments
Micro Flagellates
Macro Flagellates
Scenedesmus
Colpoda
Pennates
Naviculum
Rotifers
Parmecium
Nematodes
Vorticella
192
32
155
i
5
6
2
6
3
1
5
) 205
8
1.81
37
124
2
2
6
12
3
19
21
10
2.91
1
1
2
1
1
7
3
3
2
1
20
129
2
1
4
1
7
1
28
196
9
2.03
24
112
7
1
5
5
13
2
27
19
109
1
3
6
7
4
30
199
10
1.95
22
102
3
4
5
1
5
1
1
55
71 29 15
72 58 41
332
4 3 18
20 9 2
677
3
2 1
17 19 19
198 115 109
797
2.11 2.07 1.93
,68 16 21
65 61 55
312
949
6 3 1
1
5 8 1
1
42 20 20
92
7
1.31
3
1
4
12
2
69
1
38
29
2
9
5
2
8
23
3
.84
19
2
2
33
8
2.84
5
5
4
4
3
8
3
1
1 33 55
28 8
5 3
126
1 5 2
213
2 1
1
1 1
2 14 9
32 65 144
889
2.36 2.22 1.90 2,
1 25 87
9 15 15
122
417
3 3 8
1 1
1 2
1
1 2
12 16 21
118
11
2.83
4
11
10
10
21
15
39
2
3
1
2
23 61
13 7
9 1
4 8
10 5
2 2
2 1
16 11
57 68
7 7
,15 2.35
7 25
10 5
1 5
3 4
8 6
1
3
27 20
24
11
3.30
4
2
2
2
2
3
4
2
1
1
1
34
5
3
2
5
1
9
53
8
2.23 1
26
5
1
4
7
1
1
8
36 64
5 1
6 8
5 4
9 13
2 3
13 15
58 83
6 10
.90 2.34
29 30
3 8
2 2
4 4
3 3
1
1
4
1
17 29
33
8
2.82
3
6
9
4
2
4
2
3
-------
APPENDIX D
TABLE D-l
MEDFIELD - PHASE IIB (continuous loading)
SEPTAGE (mg/1)
Date
Day
Volume, gal
% Daily Flow
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
pH
Temperature, °C
Alkalinity
11/1
Tue
11,010
3.6?
11,380
475
3,510
2,215
10,500
8,540
9,115
7,545
125
68
6.9
14
625
11/2
Wed
11,281
4.04
8,700
1,345
2,775
2,400
4,170
3,015
3,030
2,285
174
70
7.6
12
11/3
Thur
7,933
2.46
14,415
940
2,000
1,510
8,280
5,900
6,890
4,920
273
70
6.9
12
559
11/4
Fri
11,062
4.10
4,590
1,090
1,440
880
3,030
2,100
2,100
1,645
132
80.
7-3
11
11/4
Sat
11>150
4.76
10,625
940
1,507
1,260
5,220
3,900
4,020
3,160
195
60
483
11/6
Sun
9,993
4.18
12,850
940
2,550
2,520
6,695
4,740
5,435
3,900
258
64
7.4
12
688
P . Ill i
11/6 11/7
Sun Kon
10,238
3.88
16, 940 48,000
1,805
10,800
10,520 47,275
7,680 34,335
9,255 45,510
6,990 33,130
792
72
7.2
12
970
X
10,380
15,938
278
69
193
-------
TABLE D-2
MEDFIELD - PHASE IIB (continuous loading)
INFLUENT (mg/1)
Date 10/31
Day Hon
Flow Rate, ragd .288
COD-Total 269
COD- Soluble 79
BOD- Total
BOD-N Suppressed
Total solids
TVS
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N 62.5
Nitrate-N
pH
Temperature, °C
Alkalinity
11/1
Tue
.300
85
62
349
131
66
60
15
.48
11/2
Wed
.279
269
99
99
69
337
195
60
58
21
22
.75
7.7
14-. 0
11/3
Thur
.322
494
86
166
94
573
308
301
231
24
16
• 5<*
7.4
14.0
14-9
llA
Fri
.270
307
86
177
113
403
194
14
13-5
33
14
.6
7.0
15.0
154
11/5
Sat
.234
207
55
418
186
58
55
20
12
.5
7.6
15.0
125
11/6
Sun
.239
297
240
96
57
386
265
91
86
21
13
• 53
130
11/7
Mon
.264
271
71
108
69
429
192
113
101
22
17
.63
7.0
15.0
122
11/8
Tue
.403
249
40
99
72
419
193
134
88
25
14
• 75
7.2
114
X
.289
295
119
77
23.7
20.6
• 59
TABLE D-3
MEDFIELD - PHASE IIB
SECONDARY EFFLUENT (mg/1)
Date
Day
COD-Total
COD-Soluole
BOD-Total
BOD-N Suppressed
Total Solids
10/31 11/1
Mon
41.5
29.6
l.l
0.3
Tue
4.4
3-1
191.1 289.2
Total Vol. Solids 100.5 198.0
Suspended Solids 1.7 2.4
Volatile Susp.Solids 0.5 1.9
Ammonia-N 0.14 0.46
Nitrate-N 9.5 12.5
pH
Temperature, °C
11/2 11/3 11/4 11/5 11/6 11/7 11/8 x
Wed Thur Fri Sat Sun Mon Tue
33.6 27.3 29.0 33.2 25.4 29.5 29.7 31.2
35.0 11.7 21.0 33.2 23.4 27.5 27.7 26.1
2.7 1.8 2.7 3.2 1.6 2.7 2.2 2.5
1.6 1.0 1.5 1.3 0.6 1.3 1.7 1.4
232.0 332.0 341.5 392.0 391.0 351.0 323.3 316.0
92.7 81.0 104.0 86.0 135.0 162.0 76.7 115.0
5.2 1.1 3.1 1.0 1.6 3.9 1.8 2.4
4.9 1.1 2.9 l.o 1.6 3.6 1.4 2.1
0.34 0.65 0.32 0.16 0.19 0.66 0.41 0.37
13.0 ll.o 12.0 14.0 14.0 15.0 14.5 12.8
7.7 7.5 7.1 7-4 7.1
13.0 14.0 15,0
194
-------
TABLE D-4
MEDFIELD - PHASE IIB
MIXED LIQUOR (mg/1)
Date 11/1 11/2 11/3 U/4 11/5 11/6 11/7 11/8 H/9 11/1 11/2
Basin No. #4
Total Solids 7690 7940 7940 7640 8150 8360 8180 7990 7740 7380 7800 7690
Total Volatile Solids 4660 4890 4920 4750 4960 5100 4890 5010 4760 4430 4830 4700
Suspended Solids 7480 7700 7660 7330 7790 8030 7890 7660 74?0 7180 7570 7530
volatile Susp. Solids 4560 4720 4840 4680 4820 4960 4860 4860 4640 4340 4790 4690
pH 6.8 7.9 7.4 7.17.5 7.0 7.0
Temperature,°C 13,5 13-0 14.0 14.5 15-0 15.0 15.0 16.0
Alkalinity 16? 162 300 269 200 147 17°
Settlometer
5 min
1 0
15
20
25
30
45
60
Settling column
5 min
10
15
20
25
30
45
11/6 11/7 11/B 11/9
7330 7970 8360 8190 8630
4560 4840 5100 5010 5*H° 5630
7030 7640 8030 7870 8210 8740
4410 4?10 4960 4940 5310 5480
2?5 312 206 166
920
840
750
680
560
460
420
950
900
830
770
705
650
520
450
930
860
790
710
640
585
470
430
940
850
780
675
630
570
475
430
940
850
750
660
600
550
450
400
910
860
770
690
630
575
450
430
900
840
770
700
650
600
500
450
910
820
740
660
600
540
450
400
890
770
640
560
510
475
410
380
930
860
770
700
610
580
460
420
940
870
800
?40
670
620
490
420
920
820
725
640
570
510
420
370
920
790
650
550
510
480
400
370
900
800
700
620
550
510
430
390
750
600
520
470
440
410
350
340
900
820
740
660
600
550
460
420
900
800
700
620
570
520
450
410
94o
870
810
740
680
620
500
430
54.0 34.9 28.6 28.6 28.6
130.2 106.4 117,5 104.8 111.1
208.0 177.8 200.0 190.5 196,9
288.9 247.7 288.7 273.1 285.1
396.9 336.6 374.7 377.8 362.0
479.4 417.5 460.4 460.4 441.3
717.6 654.1 700.0 685.8 666.8
930.3 857.3 420.8 892.2 822.3
25.4
85-7
152.4 149.2
368.3 374.7
28.6 w.5
79.4 133.14.
228.7
222.3 222.3 308.0
298.5 298.5 396.9
485.8
562.0 587-4 7^6.1
746.1 771.5 965.2
-------
TABLE D-5
MEDFIELD - PHASE IIB
DISSOLVED OXYGEN
Date
Day
Time
D.O. Uptake
Basin # 3
#1
Dissolved Oxygen
Basin #1
#2
#3
,_ #4
VD Clarifier
cn
11/1
Tue
7:30
a.m.
6.6
6.2
5.6
5.2
3.3
11/1
Tue
1:00
p.m.
9.0
22.8
1.7
5.0
4.6
4.2
3.6
11 /2
Wed
8:30
a.m.
10.8
11.4
3-3
4.7
3.9
3.1
1.6
11/2
Wed
12
noon
1.5
4.1
3.3
2.7
1.2
11/2
Wed
3:50
p.m.
0.9
2.9
2.2
1.3
0.8
11/3
Thur
8:30
a.m.
13.8
10.5
2.8
4.0
2.9
2.2
0.8
11/3
Thur
12:20
p.m.
1.5
2.5
2.0
1.3
0.7
11/4
Fri
8:00
a.m.
20.4
20.4
1.4
3.8
2.9
2.1
0.8
11/4
Fri
12
noon
1.6
3.0
2.3
2.0
0.7
U/5
Sat
9OO
a.m.
10.8
23.1
2.6
3.0
2.2
1.7
0.2
11/5
Sat
1:30
p.m.
1.1
2.3
1.8
1.2
0.2
11/5
Sat
3:45
p.m.
0.7
2.5
1.6
1.2
0.2
11/6
Sun
9iOO
a.m.
17.7
20.7
3-5
4.3
3.0
2.5
0.9
11/7
Mon
9sOO
a.m.
11.7
15.0
0.3
3-7
3.3
2.7
0.9
11/7
Mon
1:00
p.m.
0.8
3-3
2.4
1.9
0.6
11/7
Mon
3;OC
p.m.
0.4
2.6
1.7
1.1
0.4
1.1/8
Tue
7OO
a.m.
11.7
12.6
3.9
5.0
4.0
3.3
1.1
11/9
Wed
7:30
a.m.
13.8
14.1
3.3
4.7
3-9
3.2
1.4
11/10
Thur
7:30
a.m.
5-0
5-2
4.3
3-7
1.6
Date 11/1
Day Tue
Total Solids 11700
Total Volatile Solids 7300
Suspended Solids 11460
Volatile Suspended Solids 7170
Flow Rate, mgd .419
Capillary Suction Test 10.3
TAB1E D-6
MEDFIELD - PHASE IIB
SECONDARY SIUDGE
11/2 11/3 H/4 11/5 H/6 11/7 H/8 11/9
Wed Thur Fri Sat Sun Won Tue Wed
9200 8300 12010 9020 10370 10960 8210 9390
5610 5140 7360 5370 6290 6760 5070 5730
8960 8040 11570 8600 9010 10660 7900 9130
5600 5030 7160 5230 6200 6700 4970 5690
.344 .767 .408 .441 .431 .412 .463
7.5 7.0 7.5 8.3 8.0 7.9 6.4 7.3
-------
TABLE D-7
MEDFIELD - PHASE IIB
THICKENER AND VACUUM FILTER
Date 11/2
Day Wed
COD-Total 39-5
BCD-Total 3.4
BOD-N Suppressed 1.7
Total Solids 280
Total Volatile Solids 53
Total Susp. Solids 2.0
Volatile Suspended Solids 2.0
Capillary Suction Test
Volume 38170*
Date
Day
COD-Total
BCD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids 1300
Total Susp. Solids
Volatile Susp. Solids
Capillary Suction Test
* Total Supernatant and Sludge
THICKENER
'grnatant
11/3
Thur
35.0
2.9
2.2
290
68
3.0
3-0
19200*
e
11/9
Wed
11/8
Tue
31.4
7.3
2.3
340
93
16
7.0
40090*
VA
11/3
Thur
11/2
Wed
3.12%
1.14JS
8.4
10360
Sludge
11/3
Thur
3.18
1.17
5-4
4670
CUUM FILTER
Cake
11/4
Fri
11/9
Wed
11/8
Tue
5.66
3.61
7.1
11/3
Thur
1931
426
193
2330
1300
1790
1140
Filtrate
Fri
875
303
144
1000
475
564
381
Cake
11/9 H/3 H/4
Wed Thur Fri
617
285
137
850 11.9* 12.8*
450 7.2^ 4.6^
400
250
Cond. Sludge
11/9 11/3 11/4 11/9
Wed Thur Fri Wed
10.8?? 5.5?* 5.7?? 6.6^
3.9 3.2$ 2.1?S 2.4"5
6.8
7.1 14.1
197
-------
TABLE D-8
MEDPIEID - PHASE IIB
MICROBIOLOGICAL INDICES
Date 11 /I
Total No. Organisms 88
Total No. Species 7
2.26
Diversity Index
No. of Organisms
Vorticella
BASIN #1
11/3 U/5 U/7
82 75 96
867
2.15 1.9 1.72
EFFLUENT
33
Colpoda and Euplotes 15
Micro Flagellates
Macro Flagellates
Rotifjrs
Diatoms
lionotes
?'licro Ciliates
Suctorians
Nematodes
Spirochetes
12
20
3
32
9
21
39
k
11
16
k
62
12
11/9
66
7
2.06
•11
7
Ciliates
Green Filaments
Micro Flagellates
Macro Flagellates
Scenede sinus
Colpoda
Pennates
Naviculum
Rotifers
Paramecium
Nematodes
Vorticella
11/8
14
5
2.07
198
-------
TABLE D-9
Phase I
Date 8/24 8/26 8/31
Septage Loading %
Influent
Copper (mg/1)
Nickel
Chromium
Zinc
Cadmium
Lead
Secondary Effluent
Copper (mg/1)
Nickel
Chromium
Zinc
Cadmium
Lead
Septage
Copper (mg/1)
Nickel
Chromium
Zinc
Cadmium
Lead
.12
•15
0
• 90
0
.50
.04
.22
.40
.43
0
.20
.15
.0?
0
.18
.04
.64
.05
.0?
.10
.10
0
.08
.08
.14
.24
.41
.02
.61
.05
.07
.17
.50
.02
.10
MEDFIELD - HEAVY METALS
INFLUENT, EFFLUENT AND SEPTAGE
1 1 A
9/2 9/7 9/9 9/14 9/16 9/21 9/23
2.61 2.03 1.85 z.14
.16
.09
.75
.32
.05
.74
.07
.13
0
.09
.05
• 32
.14
.06
.09
.23
.05
.46
.07
.05
.15
.12
.02
.10
.15
.11
.12
.17
.05
.57
.06
.05
.07
.09
.0?
.10
.27
.15
.09
.17
.01
.36
.23
.13
.21
•13
.01
0
6.44
.25
.45
7.30
.07
• 50
• 37
.28
.15
.33
.04
.19
.14
.10
.13
.23
.01
0
2.56
.17
1.30
2.28
.03
1.50
.18
.09
.10
.97
.01
0
.15
.10
.10
.10
.01
0
2.49
.19
.21
2.17
.04
• 95
.25
.28
.14
8.00
.01
• 38
.24
.10
.12
3.56
.02
0
9/28
1.88
.09
.11
.10
.13
.02
.10
.03
.11
.10
.09
.02
.10
1.83
.34
.33
3.29
.05
.27
9/30
1.69
.16
.14
.14
• 32
• 03
.14
.04
.10
.10
.08
.02
.10
7-52
.50
.70
8.05
.06
1.20
11/2
4,04
.07
.02
.07
.28
0
,40
.04
0
.09
.94
0
.09
3.42
.38
.43
8.38
.08
1.80
IIB
11/5
4,76
.09
.04
.07
.24
.13
.19
.03
0
.04
.14
.01
.10
1.44
.13
.11
2.64
.04
1.00
11/9
.07
.07
.08
.17
.02
.20
.03
.02
.02
.14
.01
.06
199
-------
Phase
Date
Septage Loading
Thickener Supernatant
TABLE D-10
MEDFIELD - HEAVY METALS
THICKENER AND VACUUM FILTER
I IIA
8/30 8/31 9/6 9/9 9/15 9/16 9/22 9/26 9/27 9/28 10/3
2.1? 1.50 1.90 1 .88 1.60
I IB
10/5 H/2 H/3 H/8 11/9
4.04 2.46 4.76
Copper (mg/1) .07
Nickel .10
Chromium 0
Zinc .06
Cadmium 0
Lead .71
Vacuum Filter Filtrate
Copper (mg/1)
Nickel
Chromium
Zinc
Cadmium
Lead
Cake
Copper (mg/kg of DryCake)
Nickel
Chromium
Zinc
Cadmium
Lead
.06
.10
0
.56
.05
0
.11
.02
.15
.89
0
• 38
1260
235
440
154-0
29
1759
.ob
.08
0
.19
.05
1.07
• 15
.09
0
.18
.05
• 30
1190
102
285
1179
68
1995
.11
.09
.ok
.12
.01
0
'.18
.20
.10
2.88
.02
0
1280
201
193
532
16
2k2
.20 .06 .03
,11 .11 .13
.10 .34- 1.78
2.32 .51 .96
.01 .01 .03
o .17 .39
.15
.10
.15
2.90
.02
.20
631
66
132
1447
26
197
.24- .33
.14 .10
.32 .10
2.53 .73
.03 .01
0 ,25
.20
.11
.26
1.67
.04
.83
952
83
199
795
17
580
.09
.13
.44
• 19
.04
.44
•55
.10
.15
.54
.01
.50
.03 .02
.03 .03
.09 .03
.29 .26
0 0
.10 .15
.85
.06
.09
2,04
.03
.70
668
89
80
1354
27
606
.04
.02
.04
.28
.02
.09
.25
.08
.07
.67
.04
.78
802
76
153
1731
38
637
200
-------
APPENDIX E
TABLE E-l
MEDFIELD - PHASE IIIA (shock loading)
SEPTAGE (mg/1)
Date
Day
V olume, gal
Percent of Flow
Loading Time
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volati
Suspended Solids
Volative Su
Airanonia-N
Total Phosphorus
pH
Alkalinity
Date
Day
Flow Ratei mgd
COD-Total
Total Solids
Total Volatile
Suspended Solids
Volatile S
Airanonia-N
Total Phosphorus
pH
Temperature
Alkalinity
BOD-Total
BOD-N Suppressed
lo/i^ 10/15
Fri
5000
1.5
Sat
5000
1.9
9iOOam 9 i 20am
28950 29130
id
Solids
Is
ided Solids
is
MEDFIELD -
Solids
ds
Solids
"US
'c
1790
6080
3980
16700
13310
15100
12180
56
155
6.9
480
TABLE E-2
PHASE IIIA (shock
INFLUENT (mg/1)
10/4 10A5
Fri Sat
.33 -27
295
479
220
146
120
13.1
14
7.*
165
84
C1
1690
5100
4640
8850
6890
6930
5550
^5
165
440
loading)
10/16
Sun
.3^
86
277
65
31
26
7.3
104
10/16
Sun
6700
2.0
9 i 10am
60000
71
120
6.9
10/17
Mon
.37
108
335
105
112
66
6.4
6.9
67
51
36
10/18
Tue
132
356
75
10
10
3.6
7.3
7.1
201
-------
TABLE E-3
MEDFIELD - PHASE IIIA (shock loading)
SECONDARY EFFIUENT (mg/1)
Date
Time
AT after shook, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Ammonia-N
Nitrate-N
Total Phosphorus
pH
Temperature, °C
Alkalinity
Friday 10/14 Friday 10/14
a.m. p.m. p.m.
9:00 10:00 11:00 12:00 1:00 2:00 3:30 3:00 3:30 4:30 $lJO 6:30 7:30 8:30 9:30 10:30
0 1 2 3 4 55-5 6 6.5 7.5 8.5 9-5 10.5 11.5 12-5 13.5
31.5 35-4 27.6 35.4 27.6 51.2 43.3 23.6 55.1 31.5 31.5 23.6 51.2 51.2 35.3 51.2
Saturday 10/15
a.m. p.m.
9:20 10:20 11:20 12:20 1 i 20
0
27
.6
351
90
7
6
0
14
7
.7
.2
.0
.0
.0
.8
.5
15
78
15
2
.5
• 5
329
93
6
5
0
14
1
7
• 3
.8
.4
.0
.1
.0
.2
15
72
4
0
.2
.4
317
7
7
0
14
1
7
44
.4
.0
.0
.1
.0
.3
14
77
27.6
2.0
0.5
317
48
4.4
4.0
0.0
14.1
.9
7.0
14
75
27
.6 27.6 39-4 19.7 31.5 23.6 15-7 11.8 15-7 23.6 15.7 11.8
2.0
O.g
261 333 341 315 332
34
7
6
<
10
7
.7 56
.0
.6
.1 <.l <.l <.l
.8 14.0 14.5 13-3 14.0 14.1 14.0 14.7 14.0
.9 .9 -9 .9 .9 .9 -9 .9 .8
.2 7.0 6.9 6.9 6.9
14
341 373 325
69-3
5.0
2.8
<.l
14.2 15.0 12.0
.9 .8 .8 .8
7.4
12
1234
27.5 27-5 27.5 31.4
1.6 2.0
0.8 0.8
297 300 317 325
32.0 62.7 58.7 73.3
1.8 5-6 2.2 6.8
1.2 3.8 1.4 4.2
10.8 11.8
.7 .9 1.0
7.3 7.4 7.2 7.4
14 14 15 15
74 72
(continued)
-------
TABLE E-3 (continued)
Date
Time
AT After Shock, hrs.
COD-Total
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Ammonia-N
Nitrate-N
Total Phosphorus
pH
Temperature, °C
Alkalinity
Saturday 10/15
p.m. '
p.m. '
2:20 3.20 4:20 5:20 6:20 7:20 8.20 9:20 1 0 1 20 11:20 12:
5.0 6.0 7.0 8.0 9.0 10.0 11.0 12.0
23.9 51.0 27.9 31.9 12.0 15.6 19.9 23.9
Sunday 10/16
a.m.
a.m.
20 1:20 2:20 3:20 4:20 5:20 6:20 ?:20
13.0 14.0 15-0 16.0 1?.0 18.0 19.0 20.0 21.0
23.9 23.9 19.9 8-°
326 300 332 331 335
52.0
4.2
3.2
<.l <.l <.l <.l <.l
13.0 12.0 11.5 12.3 12.1 12.2 11.0 12.0 13.3 12.0
1.0 1.0 1.0 1.21.2
7.2
79
325
12.0
319
= 30
11.3
9:10 10:10
0 1.0
31.0 35.3
.9
320 321
64.0 61.3
5.8 6.8
3.8 4.2
11.5 10.0 9.1
1.0 1.0
7-3 7.4
13 13
79 79
(continued)
-------
TABLE E-3 (continued)
NJ
O
Date
Time
AT After Shock, hrs.
COD-Total
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Airanonia-N
Nitrate-N
Total Phosphorus
pH
Temperature, °c
Alkalinity
a „ Sunday 10/16 Sunday 10/16 Monday 10/1?
a>mp p'm> p.m. a.m.
11:1012:10 1 ilO 2:10 3:10 4:10 5:10 6:10 7:10 8:10 9:1010:1011:1012:10 1:10 2ilO 3:10 4:10 5=10 6:10 ?:10
2.0
3.0 4.0 5.0 6.0 7.0
9.0 10.0 11.0 12.0 13.0 14. 0 15.0 16-0 17-0 18.0 19.0 20.0 21.0 22.0
47.1 12.1 20.2 28.3 36.4 28.3 28.3 40.5 36-^ 28.3 20.2 28.3 32.4 24.3 20.2 24.3 36.4
353
319
61.3
5.4
3.4
<.l
8.8
0.9
7.4
14
78
0.3
0.3
331
44.0
3.0
1.4
<.l
10.3
0.8
7.5
15
1.8
0.4
327
50.7
6.6
3.8
<.l
10.0
1.0
7.6
15
2.0
0.4
313
50.7
6.6
3.8
<.l <.l
9.5 9.0 8.6 8.2
0.9 0.8 0.8 0.8
. 7.6
14
345 327
.1 .1
7.6 7.4 7.3 6.9 6.7
0.8
6.5
.1
5-2
28.3
341
.1
5.0
0.5
.2
0
.1
4.0
(continued)
-------
TABLE E-3 (continued)
Date
Time
AT After Shock, hrs.
COD-Total
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Ammonia-N
Nitrate-N
Total Phosphorus
pH
Temperature, C
Alkalinity
Monday 10/17
a.m. p.
8:00 8:30 9:00 10:00 11:00 12:00 1:00
344
23.3 23.8 24.8 25.8
40.0 27.9 53.7
319
36
5-0
3.8
0.9
7.0
14
26.8
25.9
0.4
4.0
1.0
0.9
0.11 0.04
3.5 3.2
1.0 0.8
7 = 30
34.3
19.9
3.1
0.3
268
67
6.2
4.6
0.06
4.8
0.9
Tue 10/18
a.m.
8:00
46.8
23.9
0.9
0.4
279
83
1 .2
1.2
0.12
4.2
0.9
7.1
13
94
205
-------
TABLE E-4
MEDFIELD - PHASE IIIA (shock loading)
DISSOLVED OXYGEN (mg/1)
Date
Time
AT After Shock
Basin #1
#2
#3
#4
Clarifier
Date
tvj T ime
O
CTi AT After Shock
Basin #1
#2
#3
#4
Clarifier
Date
Time
A T After Shock
Basin #1
#2
#3
#4
Clarifier
^
va
9:00
0
6.2
5.9
5.7
5-5
3-5
°Jl
8:55
0
6.2
6.2
5.o
4.7
2.7
Friday
.m.
10:00 11:00 12:13
1.0
2.6
6.2
6.4
6.1
4.2
9:25 9
.25
5.8
6.0
5.2
4.8
2.7
Monday 10/17
a
9:20
24.17
3.9
1.9
1.2
0.5
0.3
.m. p
10:30 7
25-33 34
1.6
2.9
2.1
1.1
0.8
2.0 3.22
2.8
4.7
4.8
4.8
2.9
Sunday
:55 10:25'
.75 1.25
0.3 0.4
5-3 3-1
5.0 3.0
4.5 2.7
2.8 2.7
10/14
12:45 2:00
3.75 5.0
2.4 2.2
2.4 3.3
2.8 3.0
2.8 2.6
2.8 1.9
10/16
m.
10:55 11:25
1.75 2.25
0.5 0.5
1.4 0.6
1.7 0.4
0.7 0.2
2.1 1.5
J L
^\/ Saturday
p.m.
3:00 4:00
6.0 7.0
2.6 2.1
4.3 3.8
3.5 3.5
3.2 3.3
2.0 2.4
11:55 12:25
2.75 3.25
0.6 0.7
0.7 1.1
0.4 0.2
0.2 0.2
0.5 0.2
— V
9:20
0
5-3
4.9
4.7
4.3
2.8
12:55
3.75
0.8
1.1
0.6
0.2
0.2
9:50
0.5
1.2
4.7
4.7
3.9
2.1
1:25
4.25
0.6
1.7
0.6
0.2
0.1
10i20
1.0
1.2
4.8
4.4
3.8
2.3
1 = 55
4.75
0.6
1.9
0.6
0.2
0.1
a.m.
11:05
1.75
1.9
4.7
4.2
3.7
2.8
2:25
5.25
0.7
1.2
0.5
0.2
0.1
11:20
2.0
2.8
4.9
4.1
3.5
2.9
2:55
5.75
0.8
1.6
0.5
0.2
0.1
12:20
3.0
1.6
4.6
4.2
3.6
2.6
3 = 25
6.25
0.8
1.8
0.7
0.1
0.1
12:50
3.5
1.4
4.6
4.0
3.8
p.m.
3:55
6.75
0.8
1.9
0.8
0.2
0.2
10/15
1:20
4.0
1.6
4.3
4.2
3.2
2.4
4:25
7.25
0.8
1.9
1.1
0.5
0.3
2:20
5.0
1.1
4.5
3.7
3.2
2.2
4:55
7.75
0.9
2.0
1.0
0.6
0.3
p.
2:50
5.5
0.7
4.1
3.9
3.6
2.4
5:25
8.25
1 .2
1.7
1.0
0.6
0.4
m.
3:15
5.9
1.1
3.6
3.5
3.2
2.2
5:55
8.75
1.6
1.6
1.1
0.5
0.4
3:45
6.4
0.3
4.1
3.7
3.0
2.5
8:25
11.25
2.1
2.2
1.4
1.1
0.5
4:45
7.4
1.1
5.0
4.2
3-6
2.3
8:45
11.58
2.1
2.2
1.4
1.0
0.5
Tuesday 10/18
.m. a.m.
:25 7:25
.25 46.25
3.0 4.9
2.8 4.2
2.2 2.8
1.5 2.0
0.7 l.o
-------
TABLE E-5
MEDFIELD - PHASE IIIA (shock loading)
MIXED LIQUOR BASIN 1 AND If- (mg/1)
Date
Time
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature , C
to Alkalinity
0
-J D.O. Uptake
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
10/13 10/14
a ,m0 a.,m. p.m..
9:00 9:20 10:30 11:20 12:20 1:20
8230 8080 8150 8150 8050 8060
4820 46?0 4840 4890 4650 4750
7970 7750 7830 7840 7740 7770
4780 4580 4720 4750 454-0 4650
7.1 7.1 6.9 7.1 6.9 6.8
15 15 15 14 14 14
190 185 170 175 260 270
3:20
8190
4840
7890
4740
7.8
945
880
820
750
695
640
520
450
8.9
940
880
820
760
700
645
520
450
8.4
940
880
810
740
680
620
500
440
8.0
930
870
810
730
580
500
430
8.4
920
850
780
700
630
580
470
420
9.6
940
880
740
680
620
470
440
15.6
2pm
930
845
750
670
600
550
460
420
10/15
a.m. p.m.
9:20 10:20 11:20 12:20 1:20 3:20
8050 8270 8340 8480 8230 8680
4200 4880 4920 5050 4930 5160
7780 7980 8050 8180 7910 8370
4120 4840 4830 5010 4910 5110
7.2 7.3 7.4 7,2 7.3 7.2
13 13 14 14 14 14
7-5 8.4 10,5 8.3 9.0 9.3
9^5 9i|.o 920 940
890 880 800 890
840 820 710 830
780 ?60 640 765
725 700 575 715
6?0 650 530 660
540 530 460 530
4?0 460 415 460
10/16
a.m.
9:10 10:10 11:10 12:10
8320 8640 8930 8990
4930 5090 5300 5330
8010 8320 8620 8630
4880 5030 5260 5290
7.2 7.2 7.4 7.5
12 13 14 15
220 210 210
8.1 8,4 20.6 22.8
10/17 10/18
p.m. a.m. a.m.
1:10 3:10 7:30 7:30
8660 9140 9460 9030
5160 5J90 5660 5380
8350 8820 9160 8720
5120 5360 5650 5350
7.6 7.6 6.9 7.0
15 14 14 13
230
17.4 18.2 13.3 14.8
940
880
815
750
695
640
520
460
900
810
730
660
600
550
480
430
940
885
830
775
720
665
550
480
910
820
735
660
560
480
450
930
865
810
740
690
630
515
460
950
900
830
7?0
710
650
550
480
8feO
765
675
600
550
510
450
410
920
850
790
720
660
610
500
450
950
£00
640
765
730
680
555
4PO
94P
S&o
820
760
700
640
520
450
* Basin #3
+ Basin #4 near discharge point
-------
TABLE E-6
MEDFIELD - PHASE IIIA (shock loading)
MIXED LIQUOR BASIN #1 (rag/1)
Date
Time
D.O. Uptake
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
Total No. Organisms
Total No. Species
Diversity Index
10/16
a.m.
9-.10 10:10 11:10
8.4 42.6 57.6
900
800
730
640
590
560
490
480
102
9
2,41
p.m.
12:10
43.2
930
860
740
650
590
550
500
460
1 :10
32.4
900
780
6;<5
610
560
520
460
420
]
3:10
30.3
940
900
850
700
740
690
560
480
83
10
2.75
.0/17 1
a.m.
7:30
22.2
940
880
810
750
690
640
515
450
90
90
2.20
LO/lb
a.m.
7:30
11.7
940
880
815
750
685
630
500
450
65
6
2.25
No. Organisms
Vorticella 4
Colpoda & Euplotes 27
Micro Flagellates 6
Macro Flagellates 23
Rotifers 4
Diatoms 1
lionotes 33
Micro Ciliates
Suctorians 1
Nematodes
Spirochetes 3
9
15
4
24
8
1
16
1
1
3
28
1
28
7
21
1
7
23
15
12
•7
208
-------
TABLE E-7
MEDFIELD - PHASE IIIA
SECONDARY SLUDGE (mg/1)
Date 10/13 10/14 10/15 10/16 10/17 10/18
Total Solids 10860 10200 15700 12020 16400 14300
Total Volatile Solids 6440 5940 9160 7130 9870 8670
Flow Rate,mgd .428 .320 .400 .349 .420
Capillary Suction Test 7.4 8.1 7.7 9.7 9.3
TABLE E-8
MEDFIELD PHASE IIIA (shock loading)
THICKENER AND VACUUM FILTER
THICKENER VACUUM FILTER
Supernatant Sludge '•'iltrate Cake
Date 10/17 10/19 10/17 10/19 10/18 10/20 10/18
COD-Total 17.9 359
BOD-Total 1.2 180
BOD-N Suppressed 0.7 50
TotaL Solids 336 5-0?S 564 13-0",
Total Volatile Solids 5^ 1.99? 225 8.13?
Total Susp. Solids 198
Total Vol. Susp. Solids 128
Capillary Suction Test 9.8
Volume, gal 14350 11250 7940 484?
209
-------
TABLE E-9
MEDFIELD - PHASE IIIA (shock loading)
MICROBIOLOGICAL INDICES
Date 10/13
Time
AT After Shook
Mixed Liquor
Total No. Organisms 205
Total No. Species 8
Diversity Index 1.57
No. Organisms
Vorticella
Colpoda & Euplotes
Micro Flagellates
Macro Flagellates
Rotifers
Diatoms
Lionotes
Micro Ciliates
Suctorians
Nematodes
Spirochetes
Effluent
Total No. Organisms
Total No. Species
Diversity Index
No. Organisms
Ciliates
Micro Flagellates
Macro Flagellates
Scenede sinus
Colpoda
Pennate s
Naviculum
Nematodes
10/14
10/15
9:20
0
191
9
2.06
4
28
6
29
12
1
104
1
6
44
7
2.13
7
4
4
2
23
3
a.m.
10:20 11:20 12:20
1 2 3
136 159 146
9 10 9
2.11 1.86 1.95
2 1
16 14 17
432
16 35 34
7 3 10
211
76 92 77
1
1
111
13 8 3
p.m.
1:20 3:20 9:20
460
121 166 138
768
1.94 1.94 2.12
537
27 33 33
481
15 25 22
5 11 7
1
64 86 63
1 4
44 58
7 7
1.82 2.24
27 28
2 3
4 10
3
1 3
7 7
1 4
2
a.m.
10:20 11:20 12:20
123
154 117 128
989
2.13 1.99 2.09
124
34 20 20
821
25 15 21
9 10 9
111
72 64 67
112
333
p.m.
1:20
4
121
7
2.00
3
27
18
9
60
2
2
(continued)
210
-------
TABLE E-9 (continued)
Date
Time
AT After Shock
Mixed Liquor
Total No. Organisms
Total No. Species
Diversity Index
No. Organisms
Vorticella
Colpoda & Euplodes
Micro Flagellates
Macro Flagellates
Rotifers
Diatoms
Lionotes
Micro Ciliates
Suctorians
Nematodes
Spirochetes
Effluent "
Total No. Organisms
Total No. Species
Diversity Index
No. Organisms
Ciliates
Micro Flagellates
Macro Flagellates
Scenedesmus
Colpoda
Pennates
Naviculum
Nematodes
10/16
a.m. p.m.
3:20 9:10 10:10 11:10 12:10
10/1? 10/18
a.m. a.m.
1:10 3:10 7:30 7>JO
0
1
104
8
1.96
2
22
2
19
3
1
53
2
42
6
2.14
19
it.
10
4
3
2
95
10
2.60
2
25
6
17
6
2
29
1
1
6
44
6
2.29
15
9
2
2
9
7
102
9
2.40
3
28
3
22
4
3
34
3
1
105
9
2.41
1
31
6
31
6
2
23
1
4
90
9
2.43
2
27
4
19
5
2
27
1
3
95
9
2.46
2
29
5
21
5
2
26
1
4
89
9
2.38
2
25
3
18
6
2
30
1
2
44
5
1.23
32
2
8
1
66
8
2.49
3
22
5
18
4
2
10
2
27
6
2.31
7
1
3
6
8
2
55
7
1.94
4
22
22
1
1
3
2
17
3
1.58
5
6
6
211
-------
APPENDIX F
TABIE F-l
MEDFIELD - IrfASE IIIB (shock loading)
SEPTAGE (mg/1)
TABLE F-2
MEDFIELD - PHASE IIIB (shock loading)
INFLUENT (mg/1)
to
M
to
Date
Day
Volume, gal
% of Flow
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Alkalinity
11/14
Mon
7770
2.5
18810
870
3600
3000
12750
9720
11870
9170
319
72
11/15
Tue
7780
2.4
23700
3980
11640
8880
10480
8110
373
428
11/16
Wed
7780
2.4
33460
1580
4500
3325
16270
12240
14930
11270
377
358
11/17
Thur
10000
3.1
32870
3540
7200
5625
15830
12050
14180
10870
532
280
346
Date
Day
Flow Rate, mgd
COD-Total
COD-Soluble
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Temperature, °C
Alkalinity
BCD-Total
BOD-N Suppressed
1/14
Mon
.314
460
128
70
62
21.8
14
150
69
45
11/15
Tue
.330
240
59.1
347
157
122
92
21.3
0.5
132
80
60
11/16
Wed
.323
220
94.5
352
128
70
62
19-3
23
0.7
14
130
67
45
11/17
Thur
.322
15
-------
Date
Time
AT After Shock, hrs
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
K3 Total Solids
l*> Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Temperature °C
pH
Turbidity
TABLE F-3
MEDFIELD - PHASE IIIB (shock loading)
SECONDARY EFFLUENT (mg/l)
Monday
a .
1:20
51.2
15.8
3.8
1.4
463
98.7
12.4
7.6
1.7
0.7
14.2
13
7.8
5.0
.m.
e
Hi
o
o
®
K
: LOADII
o
o
5
9:00
1.0
43.3
27.6
4.0
1.6
443
72.0
8.4
5.8
1.1
15.1
4.6
11/14
10:
2
47
23
3
00
.0
.2
.6
.6
1.6
437
68
6
5
1
15
.0
.4
.6
.1
.0
4.9
P
11:00
3
39
3
.0
.4
.4
1.7
423
78
10
6
0
15
4
.7
.0
.0
.4
.1
.8
.m.
12:00
4.0
47.2
39.4
4.5
1.7
461
216
10.8
10.4
1.1
14.0
5.2
2:00
6.0
55-1
39.4
4.6
1.3
456
188
13.2
12.0
2.0
1.0
15.0
4.4
4:00
8.0
51.2
31.5
4.3
2.1
473
232
14.0
14.0
1.3
14.9
5-5
5sOO 6100
9.0
35.9
19.9
3.5
1.6
416
125
13.6
12.4
0.3
16.2
4.8
8:00 11 :00
12.0 15.0
43.8 43.8
12.0 12.0
0.3 0.3
16.0 15.9
Tuesday 11/15
a.m.
2:00 5:00 7OO
p.m.
OO 10:30 11:30 12:30 2:30
F=
18.0 21.0 23.5 « 1.0 2.0 3.0 4.0 6.0
o
43.3 ^ 47.2 43.3 43.3 27.6 27.6
00
27-6
-------
TABLE F-3 (continued)
Date
Time
AT After Shock, hrs
COD-Total
COP-Soluble
BCD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Temperature, °c
PH
Turbidity
Tuesday 11/15
Wednesday 11/16
4:00
7-5
27.6
13-5
4:30
8.0
55.1
11.8
4.8
3.6
435
108
12.0
7.2
2.4
• 35
14.0
4.0
p.m.
5:00 7:00 8:00. 9:00 10:00 11:00 1:00 3:00 4:00 5:00 6:00 7:
8.5 10.5 11.5 12.5 13.5 14.5 16.5 18.5 19.5 20.5 21.5 23
35.4 27.6 27
11
3
1
30
.0
.6
.8
.4
.9
355 333 315 351 319
49 76 47 117
12.4 12.0 6.8 2.0 4
12.0 11.6 6,4 1.6 4
1
13-2 14.1 14.0 13.4 13.2 13
7
2
.4
.0
• 5
.3
13
.8
.5
g
a
o
CO
®
M
O
O
(—1
SHOCK
9OO
1 .0
31-5
19-7
3.2
1.1
305
27
5-2
4.8
12.5
2.8
a.m.
10:30 11 :30
2.0
35.4
27.6
2.9
0.9
303
36
2.8
2.4
12.2
2.5
3-0
47.2
31-5
3-5
0.9
327
69.3
4.8
3-6
12.2
2.3
12:30
4.
43.
27.
3.
0.
0
3
6
4
8
p.m.
2:30
6.0
47.2
31.5
2.2
0.5
316 34o
54.
5.
4.
12.
7
2
0
0
2.0
82.7
6.4
4.8
12.1
3-1
4:30
8.0
55-1
35-4
3.2
1.2
336
69.3
6.0
4.8
12.0
3-5
(continued)
-------
TABLE F-3 (continued)
Date
Time
AT After Shock, hrs
COD-Total
COD-Solut>le
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids 70.7
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Temperature, °C
pH
Turbidity
Date
Time
AT After Shock, hrs
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Temperature, °C
PH
Turbidity
6:30
10.0
35.4
27.6
3-5
1.0
328
70.7
11.2
8.0
12.0
3.7
Wednesday 11/16
p.m.
8:00 11:00 1:00 3:00 6:00 7:
27
15
3
1
a.m.
30
.6
.8
.1
.2
327
57
3
3
1
0.6 0.5 0.6 0.7 0.4 o
11.5 11.2 11.1 10.8 10.3 10
7
2
-3
.2
.2
.3
.3
.0
.2
.4
6
cfl
o
o
CO
®
£;
H
Q
•ad
O
U
O
X
c/i
'9:00
1.
31.
27.
2.
0.
0
5
6
8
9
327
60.
5.
5.
0.
10.
3.
0
2
2
3
0
7
Thursday
10:00 11:00
2
35
27
4
2
.0
.4
.6
.2
.0
316
68
2
2
0
10
2
.0
.8
.8
.8
.0
.7
3.0
35.7
19.7
4.4
1.5
308
56.0
5.6
5.6
0.8
9.8
3.8
11/17
12:00
4
47
19
4
2
.0
.6
.7
.2
.3
292
66
6
6
1
9
3
. 7
.8
.4
.3
.4
.8
2:00
6.0
43.3
23.6
5.1
2.4
292
21.0
7.2
6.4
2.0
1.8
9.0
4.6
Thursday 11/17
p.m.
4:00 6:00 7:00
Friday 11/18
a.m.
?:00 10:30 12:00 1:30 3:00 5:00 6:30 ?:30 8:00
-3.7
H.5
5.4
2.5
288
6.8
6.0
1.5
8.8
4.7
35.4
31.5
6.0
2.2
295
5.6
5.2
1.7 2.0 2.0 1.8 2.5 2.4 2.1
8.8 8.2 8.1 8.1 8.1 8.6 7.8
4.5
35.4
31.5
3.7
1.7
1.0
1.8 1.8 2.0
7.7 7=3 7.0
14.2
14.2
28.3
44.0
1.6
1.2
215
-------
CTi
TABLE F-4
MEDFIELD - PHASE IIIB (shock loading)
DISSOLVED OXYGEN (mg/1)
Aerator Settings
Date #1 #2 #3 #4
Sun 11-13 High High low low
Won 11-14 High High Low Low
Tue 11-15 High Low Low Low
Wed 11-16 High High Low Low
Date
Time
AT After Shock
Basin # 1 (H)
# 2 (H)
#3 (1)
#4(L)
Clarifier
Date
Time
AT After Shock
Basin # 1 (H)
#2(L)
#3(1)
#4(1)
Clarifier
a.m.
7:20
Before
6.8
7.6
6.9
6.6
5.4
a.m.
7:20
6.9
6.1
5.6
5-5
5.0
6
cti
0
0
03
®
O
w
e
a
0
CO
®
V
X
OQ
9:00
1.0
2.4
6.3
6.3
6.1
5.3
9:00
0.5
2.7
3.3
3.2
3.4
4.7
9:30
1.5
1.5
5.8
5-7
5.6
5-3
9:30
1.0
1.9
1.2
1.7
1.8
3.8
Monday 11/14/77
10:00 10:35 11:00 11
2.0 2.5+ 3.0
1.5 3-6 3.3
5.5 5.7 5.3
5-3 5-4 5.1
5.1 4.9 4.7
5-2 5.6 5-3
Tuesday 11/15/77
Thur 11-1? High
:30
3.5
3.2
5.3
5.2
4.8
4.4
10:00 10:30 11:00 11:30
1.5 2.0 2.5
2.2 3.2 3.7
0.5 0.3 0.5
0.6 0.2 0.3
0.7 0.3 0.2
3.1 2.5 1.7
3.0
3.6
0.4
0.5
0.2
1.1
noon
12:00
4.0
3-9
5.5
5-3
5.3
4.4
noon
12:00
3.5
3.2
0.6
0.2
0.2
1.0
12:30
4.5
3.9
5-6
5.2
4.8
4.1
12:30
4.0
2.9
0.3
0.2
0.2
0.5
p.m.
1 :00
5.0
2.7
5.3
5-2
4.9
4.2
p.m.
1 :00
4.5
2.7
0.5
0.2
0.2
0.2
1:30
5-5
1.9
5-3
5.2
4.7
4.2
1:30
5.0
2.5
0.3
0.2
0.2
0.3
2iOO
6.0
2.4
5-7
5-1
4.7
4.1
2:00
5-5
2.6
0.4
0.2
0.1
0.2
2:30
6.5
2.8
5.4
4.9
4.6
4.1
2:30
6.0
2.2
0.5
0.2
0.2
0.1
3:00
7.0
3.4
5-3
4.8
4.3
4.0
3:00
6.5
1.9
0.2
0.4
0.2
0.1
High
3:30
7.5
2.3
4.8
4.4
4.0
3-5
300
7.0
1.9
1.1
0.2
0.3
0.2
L ow I ow
4:00
8.0
3.3
5-3
4.5
4.0
3.7
4:00
7-5
1.8
1 .0
0.4
0.3
0.4
5:00
9.0
3.7
5.5
5.0
4.6
3.7
4:30
8.0
1.8
0.5
0.5
0.4
0.4
6:00
10.0
4.0
5.7
5.2
4.8
3-7
5OO
9.0
2.2
1.6
0.7
0.7
0.5
6:30
10.0
2.4
1.8
0.8
0.7
0.5
(continued)
-------
TABLE F-4 (continued)
K)
Date
Time
AT After Shock
Basin # 1 (H)
#2 (H)
#3 (1)
#4 (I)
Clarifier
Date
Time
AT After Shock
Basin # 1 (H)
#2 (H)
# 3 U)
# ''• (1 )
Clarifier
Wednesday 11/16/77
a.m.
7:30
7.4
7.1
5-7
5.1
3.7
9:00
A 0.5
01
o 1.6
£ 4.5
® 4.3
g 3.8
o
M 3-3
Thursday
a.m.
7OO
6.9
6.5
4.8
3-9
2.0
8:00
e- 0
a
§ 5-0
-------
TABLE F-5
MEDFIELD - PHASE IIIB (shook loading)
MIXED LIQUOR (mg/l)
Date
NJ
Time
AT After Shock
Total Solids
Total Vol. Solids
Suspended Solids
Volatile Susp Solids
Alkalinity
Settlometer
5 minutes #4
10 minutes
15 minutes
20 minutes #1
25 minutes
30 minutes
45 minutes
60 minutes
Settling Column (#4)
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
D.O. uptake mg/l/hr
a.m.
7:30 9:00
1.0
7780 8360
4390 4800
7380 7970
4340 4740
467 422
900 910
830 840
750 760
680 700
620 630
570 580
460 470
410 420
10:00
2.0
8210
4710
7880
4640
436
910
840
770
690
620
570
460
400
11:00
3-0
7970
455.0
7600
4510
428
910
750
640
580
530
500
430
390
, (mm settled)
8.3 * 8.4
8.1
8.1
- a ^
noon p
12:00 2
4.0
8380
4900
7960
4500
382
890
800
720
650
580
540
440
390
p.m.
1 :00
41.3
111.1
181.0
254.0
330.2
403.2
627.1
831.9
8.4
.m.
: 00
6.0
394
900
790
690
610
550
510
430
380
8.5
4:00 a>m'
3:30 4:30 5:30 7OO
7.5 8.5 9.5
8340 8260
4810 4670
7940 7870
4750 4590
374 417
940
850
780
700
630
570
470
410
8.4 8.8 7.2 8.7
9:00
1 .0
8340
4870
7970
4830
420
910
750
640
570
520
480
400
360
22.9
10:00
2.0
420
930
860
770
700
630
580
470
410
20.7
11:00
3.0
8340
4860
7980
4800
378
930
840
750
670
600
550
460
400
23-3
noon
12:00
4.0
432
900
800
700
610
550
510
430
390
21.9
p.m. l±;00
2:00 3OO 4:30 5OO
6.0 7.5 8.5 9.5
8840 7740
5080 14,500
8420 7400
5650 J|4io
390 336
810
620
550
490
450
420
370
340
20.8 21.1 20.5 19.8
(continued)
-------
TABLE F-5 (continued)
Basin #3
Basin #1
N>
Date Tuesday 11/15/77
a.m.
Time fiJO 9:30 10:30
AT After Shock
Total Solids
Total Vol. Solids
Suspended Solids
Volatile Susp. Solids
Alkalinity 320
Settlometer
5 minutes Basin #4 930
10 minutes & 810
15 minutes Basin #1 780
20 minutes 700
25 minutes 630
30 minutes 570
45 minutes 470
60 minutes 420
Settling Column., mm settled
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
D.O. Uptake 7.7
1.0
8360
5080
8000
4970
252
920
800
700
610
550
510
430
400
7.6
2.0
8260
5000
7920
4850
302
840
770
680
620
550
500
430
390
9.8.
11:30
3.0
8410
5100
8070
4960
294
920
830
770
700
640
580
470
410
10.1
p.m.
12:30
4.0
7970
4540
7550
4460
298
920
840
770
690
620
560
460
400
1:
12
93
160
231
303
374
581
774
9.6
2:30
6.0
7880
4440
7420
4380
282
910
810
710
630
570
530
440
400
00 p.m
.7
.7
.3
.8
.2
.7
.0
.7
10.1
4:30
8.0
7830
4500
7490
4410
298
920
840
750
670
590
550
46o
410
17.5
a.m.
7OO
8490
5030
6130
4940
292
750
620
550
500
460
430
390
330
9.1
9OO
1 .0
286
730
580
520
470
440
400
350
320
25.0
10:30
2.0
8140
5060
7820
5010
270
770
670
590
540
490
460
400
370
20.3
11:30
3.0
9120
5480
8800
5430
280
830
650
550
490
450
420
370
340
25.8
p.m.
12:30
4.0
8400
4810
8090
4710
306
890
740
620
560
510
470
4oo
370
25.2
2:30 4:30
6.0 8.0
7/00 8500
i|Jj,10 4950
7360 8170
4350 4900
276 290
900 890
750 800
640 730
570 650
530 580
490 540
410 440
370 390
21.3 26.8
( continued)
-------
TABLE K-5 (continued)
Basin #3
Basin #1
Date
Time
AT after shock
Total Solids
Total Vol. Solids
Suspended Solids
Volatile Susp. Solids
Alkalinity
Settlometer
5 minutes Basins
10 minutes #4
15 minutes
20 minutes &
25 minutes
30 minutes $'-
45 minutes
Wednesday 11/16/77
a.m.
7:.30 9:30 10:30 11 130
8930
5370
8660
5350
242
920
850
780
700
630
580
470
60 minutes 420
Settling Column, mm settled
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
D.O. Uptake
12.1
Settlometer Supernatant
Turbidity, Ntu 3.2
1.0
8770
5220
8600
5200
208
900
810
720
650
590
530
440
390
10.8
5.1
2.0
8690
5240
8450
5220
202
850
750
650
590
540
440
390
14.1
4,4
3.0
7390
4420
7020
4340
268
840
710
610
540
490
450
390
350
13.3
6.7
p.m.
12:30 2:30
4.0 6.0
7890 7380
4810 4460
7570 7040
4750 4380
240 264
890 900
790 780
690 670
610 590
540 530
500 490
410 410
370 370
p.m.
1 :00
44.5
123.8
200.0
282.6
358.8
450.9
704.6
923.9
13.7 12.8
12.0 9.0
4:30 5:30 6:30
8.0 9.0 10.0
8060 8030
4770 4780
7750 7740
4730 4740
216 220
880
690
580
520
480
44o
390
350
13.0 11.4
6.5
a.m.
7:3° 9OO
1 .0
8400 7860
5110 4880
8140 7580
5050 4830
228 194
920 840
860 660
770 560
710 500
640 450
590 420
480 360
430 320
12.5 24.2
5-3 17
10:30 :
2.0
7950
4960
7760
4910
216
680
570
500
450
420
350
320
25.3
12
p.m.
LI :30 12:30
3.0
8050
^750
7720
4690
216
710
550
480
430
390
370
330
300
24.8
12
4.0
8080
4840
7770
4760
244
720
560
490
450
400
380
340
300
23.0
13
2:30
6.0
8070
4860
7650
4740
252
720
550
470
430
400
370
330
310
24.6
8
4:30 5:30
8.0 9.0
7380
4310
7070
4260
232
85C
7U
61 C
54C
500
470
400
360
28.3 23.1
8.5
6:30
10.0
7940
4690
7640
4640
242
(continued)
-------
TABLE F-5 (continued)
Date
Time
AT After Shock
Total Solids
Total Vol. Solids
Suspended Solids
Volatile Susp. Solids
Alkalinity
Settlometer
5 minutes
10 minutes
15 minutes
^j 20 minutes
M 25 minutes
30 minutes
45 minutes
60 minutes
Settling Column
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
D.O.. Uptake
Thursday 11/17/77
a.m.
7OO 9:00 10:00
6830
4050
6540
4210
234
900
780
680
600
550
510
440
400
1.0
5700
3400
5420
3370
228
930
850
770
700
620
570
480
430
2.0
8440
5140
8140
5090
204
920
850
770
700
630
570
460
410
Basin #3
noon
11:00 12:00
3-0
8740
5310
8440
5250
206
860
730
610
550
500
470
410
380
4.0
224
870
74o
640
560
510
480
410
380
p.m.
2iOO
6.0
7600
4460
7290
4390
860
690
580
520
480
440
390
360
4:00
8.0
7990
4760
7740
4750
920
810
710
630
570
530
420
380
p.m.
1:00
15.0
15.4
13.5
19.2
25.
104.
181.
260.
336.
415.
644.
847.
17.2
4
8
0
4
6
9
5
7
18.5
19.2
Basin #1
Friday 11/18/77
a.m. a.m. noon p.m, p.m. a.m.
4:00 6:00 8:00 7OO 9:00 10:00 11:00 12:00 2:00 4:00 6:00 8:00
8.0 10.0 24.0 1.0 2.0 3.0 4.0 6.0 8.0 10.0 24.0
7990 8210 8310 8210 7710 8600 7270 8450 8270 8320 8080 8080
4760 4800 4890 4840 4900 5310 4370 5120 4920 4950 4790 4680
7740 7960 8100 7930 7420 8310 6980 8170 8000 8070 7840 7850
4750 4800 4890 4820 4640 5160 4310 5010 4890 4930 4750 4650
226 240 250 260 234
950
890
830
770
710
650
530
450
900
790
700
620
550
500
420
380
900
770
680
600
550
500
420
380
900
780
670
600
540
500
420
390
850
730
650
570
520
480
410
380
890
760
650
560
510
470
410
370
900
770
670
590
530
490
420
380
920
810
710
630
570
530
440
390
940
880
810
740
680
620
500
430
Settlometer Supernatant
Turbidity, Ntu 4.5 3.8
5.0
Basin #4
19.2 18.4 10.4 16.3 38.4 24.2 32.5 40.4 46.9 32.7 13.
Basin #1
3.5 23
5.5 8.5
-------
TABLE F-6
MEDFIELD - PHASE IIIB
SECONDARY SLUDGE (mg/1)
Date 11/14*11/15 11/16 11/1? 11/18
Day Won Tue Wed Thur Fri
Total Solids 11980 6350 10000 14090 8430
Total Vol. Solids 6830 3600 5896 8510 4940
Suspended Solids 11520 5?40 9720 13360 8190
Volatile Susp. Solids 6760 3320 5830 8440 4930
Plow Rate, mgd .406 .462 .435 .412 .494
Capillary Suction Test 7.2 7.1 6.1 6.4 6.6
*Samples collected at 7'30 a.m.
to TABLE F-7
to
tO MEDFIELD - PHASE IIIB (shock loading)
MICROBIOLOGICAL INDICES
Mixed Liquor Basin #1
Date Monday 11/14/77 Tuesday 11/15 Wednesday 11/16 Thursday 11/1? Friday 11/18
Time ?:30 9:0011:00 4:00 7130 90011:30 4>30 7 = 30 9OO 2:30 ?:30 9:0012:00 8:00
No. of Individuals (N) ?1 39 65 55 ?4 39 42 45 41 31 38 66 49 38 39
No. of Species (S) 557773455 314.4334
Diversity Index (H) 1.49 1.22 1.94 1.40 1.02 0.76 0.80 0.98 1.26 0.75 0.96 1.21 0.65 0.87 0.75
Secondary Effluent
Date Monday 11/14/77 Tuesday 11/15 Wednesday 11/16 Thursday 11/17 Friday 11/18
Time 7:20 lliOO 2:00 4:00 7 :JO 11:30 4:30 7:30 11:30 2:30 7OO 12:00 8:00
No. of Individuals (N) 19 24 32 33 18 21 19 30 25 27 5 8 21
No, of Species (S) 446634464 433 5
Diversity Index (H) 1.80 1.74 1.91 1.54 1.22 1.64 1.06 1.64 1.29 1.20 1.37 1.06 1.84
-------
KJ
NJ
LO
Date
Day
Flow Rate,cu m/sec
ragd
COD-Total
COD-Soluble
BOD-Total
POD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorus
Grease
Alkalinity
pH
Temperature, °C
APPENDIX G
TABLE G-l
MARLBOROUGH - PHASE I
INFLUENT (mg/1)
M/17
Mon
0.13
(2.9)
230
70
45
32
340
192
71
68
24.6
12
1.4
2.1
4/17
Mon
0.13
(2.9)
296
109
111
53
528
278
67
64
19.3
15
0.8
7.7
100
6.2
8.0
4/18
Tues
0,12
(2.8)
188
89.8
115
87
584
330
358
312
21.6
15
1.0
7.8
237
90
6.3
8.1
4/19
Wed
0.12
(2.8)
297
73.4
185
121
2070
1840
1690
1630
23.0
15
0.9
5.9
103
6.4
9.5
4/20
Thur
0.14
(3.2)
286
159
147
129
350
182
57
55
20.4
16
1.1
6.5
118
6.5
8.9
4/21
Fri
0.14
(3.1)
259
74.5
46
36
532
360
88
78
16.0
13
1.0
5.7
97
6.5
9.0
4/22
Sat
0.14
(3.2)
180
66.7
60
45
320
118
40
14
17.1
12
0.9
2.7
98
7.1
10.0
4/23
Sun
0.13
(3.0)
345
83.4
106
84
876
686
140
130
27
16
1.1
5.7
99
7.1
9.8
4/24
Mon
0.13
(3.0)
319
114
100
53
444
244
128
102
19.9
16
1.2
3.8
74
6.6
9.9
4/25
Tues
0.12
(2.7)
408
102
153
123
432
182
122
118
28.8
20
1.7
4.9
80
7.1
9.9
4/26
Wed
0.12
(2.8)
337
89.1
1022
746
104
90
24.6
18
1.1
7.1
121
110
6.6
9.9
5/1
Mon
0.11
(2.6)
373
100
112
85
834
222
253
237
23.2
20
0.9
7.3
126
6.8
10.8
5/2
Tues
0.11
(2.5)
462
55.3
141
106
280
4
264
238
26.3
16
0.4
5.8
130
6.9
10.8
5/3
Wed
0.10
(2.3)
344
106
142
136
1912
1600
132
128
27.7
18
0.8
5.5
141
131
7.0
10.8
5/4
Thur
0.10
(2.3)
372
68
147
132
678
428
74
10
30.5
19
0.9
129
6.9
11.5
5/5
Fri
0.10
(2.3)
325
103
144
54
672
458
94
66
12
0.8
10.0
124
134
7.2
11.0
5/6
Sat
0.11
(2.4)
410
79.7
155
107
524
316
142
104
19
0.9
3.3
148
7.2
12.0
5/7
Sun
0.11
(2.4)
267
71.7
129
90
4P4
232
156
14b
25.8
20
0.9
3.8
129
7.0
13.2
*Grab Sample
-------
to
S3
TABLE G-2
MARLBOROUGH - PHASE I
PRIMARY EFFLUENT (mg/lj
Date
Day
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Airanonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
** Temperature, °C
** Dissolved Oxygen-Top
** Dissolved Oxigen-Bottom
Grease
4/17
Mon
284
73.9
101
63
436
186
104
88
18
0.5
6.4
105
6.3
i
:tom
4/17
Mon
125
148
172
110
582
262
53
40
37.2
20
2.4
14.6
98
6.3
1.3
4/18
Tues
180
78.1
60
39
314
100
70
52
24.9
10
1.9
3.1
74
6.3
9
8.6
17.8
4/19
Wed
182
73.4
84
50
360
160
78
64
22.4
17
0.7
5.2
128
6.7
9
0.4
4/20
Thur
218
51.6
94
65
316
130
48
46
23.5
14
0.8
5.6
130
6.4
9
3.5
4/21
Fri
157
50. 9
39
30
304
46
37
17.4
15
0.9
4.0
128
6.7
9
5.3
4/22
Sat
126
39.2
27
310
122
46
34
14.0
12
0.8
1.6
73
6.8
9
1.2
4/23
Sun
196
66.7
48
25
328
140
58
46
20.2
13
0.8
6.0
105
6.8
9
1.1
4/24
Mon
193
55.1
71
44
388
156
56
60
16.5
14
0.7
5.4
118
6.9
9
1.1
4/25
Tues
204
74 .5
82
53
378
166
66
60
20.5
15
1.2
5.2
118
7.1
9
3.9
4/26
Wed
194
77. 5
388
156
44
40
31.1
16
1.5
4.2
94
6.9
10
2.2
287
5/1
Mon
627
100
57
46
898
232
84
80
29.1
18
0.8
5. 5
183
7.2
10
2.9
0.5
5/2
Tues
221
87
77
51
488
174
92
80
28,6
21
0.8
4.6
185
7.6
10
1.4
5/3
Wed
434
184
154
151
610
254
210
154
45.0
36
0.7
6.4
223
7.2
12
2.9
0.4
51.6
5/4
Thur
472
64
285
180
962
394
470
176
44.8
17
0.8
203
7.0
11
1.6
5/5
Fri
274
63.5
147
142
614
264
220
126
16
0.7
5.3
192
7.3
11
0.6
0.4
329
5/6
Sat
120
47.8
52
31
386
170
54
40
15
0.8
129
6.9
11
0.5
0.2
5/7
Sun
247
67.7
147
83
508
216
116
80
27.2
15
0.8
4.5
164
6.8
12
0.4
0.1
* Grab sample
** Measured in the primary clarifier
-------
TABLE G-3
MARLBOROUGH -
SECONDARY
*4/17
Mon
73.9
50.6
15.0
8.4
278
30
16
; 13
15.9
12
1.0
1.5
78
6.4
4/17
Mon
81.7
62.3
19.1
9. 5
354
72
10
8
16.8
13
3.5
1.8
73
6.3
3.6
4/18
Tues
78.1
50.8
8.1
5.2
372
110
19
14
15.0
12
3.7
1.8
73
6.3
10
2.1
4/19
Wed
27.0
19.3
13.8
6.2
310
46
10
8
14.7
11
3.5
0.3
68
6.3
10
3.5
4/20
Thur
43.7
31.7
15.0
7.6
284
76
2
1
15.1
11
3.4
0.7
67
6.5
10
4.8
4/21
Fri
58. S
47.1
11.2
2.4
348
132
12
8
12.7
15
1.0
0.8
70
6.8
10
7.6
4/22
Sat
82.4
54.9
3.3
1.1
270
68
7
2
9.7
12
3.1
0.7
55
6.8
10
3,9
PHASE
I
EFFLUENT (mg/1)
4/23
Sun
43.1
35.3
•6.7
260
76
1
1
10.2
10
3.4
0.7
42
6.7
10
5.7
4/24
Mon
47.2
35.4
3.0
1.2
324
70
7
6
13.7
10
2.9
0.6
58
6.9
10
5.6
4/25
Tues
47.1
39.2
8.1
2.7
302
124
9
6
13.3
14
3.8
0.5
71
7.0
10
4.9
65.4
4/26
Wed
58.1
42.6
348
84
9
8
16.4
18
3.4
1.7
97
7.0
10
4.8
29.1
5/1
Mon
34 .6
26.9
16.5
£ 1
758
108
7
5
16.2
13
4.0
0.7
119
6.9
11
4.5
5/2
Tues
55. 3
27.7
5.1
4 1
364
34
10
9
14.8
13
3.6
0.5
120
7.1
11
5.5
5/3
Wed
62.5
31.3
19.7
6.0
372
224
8
6
27.3
21
3.5
0.8
145
7. 3
11
5.3
23.1
5/4
Thur
72
40
15.6
7.2
388
84
13
11
20.7
16
3.2
133
7.0
12
0.4
5/5
Fri
55.6
31.7
12.4
3.9
370
64
17
12
13
3.7
0.2
130
7.2
12
4.2
37.9
5/6
Sat
39.8
27.9
4.3
1.9
356
132
12
8
13
1. 3
1. 3
114
7.1
12
4 .1
5/7
Sun
35.9
19.9
12.6
2.7
388
122
11
10
16.8
15
5. 0
1.5
92
6.9
13
5. 3
Date
Day
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
tO Suspended Solids
NJ
(Jl Volatile SUSP- Solids 13
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
** Temperature, C
** Dissolved Oxygen
Grease
*Grab Sample ** Measured in the first stage final clarifier
-------
TABLE G-4
MARLBOROUGH - PHASE I
FINAL EFFLUENT (mg/1)
Date *
Day
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids'
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Artmonia-N
Mitrate-N
Total Phosphorous
Alkalinity
PH
** Temperature, C
** Dissolved Oxygen
Grease
4/17
Mon
42.8
23. 3
5.4
1.5
374
62
35
21
2.1
0.6
16
1.5
45
6.6
^ Adding alkaline waste to
4/17
Mon
46.7
46.7
1.7
1.5
448
106
3
2
2.1
0.3
19
2.0
26
6.1
7.0
second
4/18
Tues
43.0
43.0
4.4
1.7
474
182
18
12
2.4
0.5
19
1.5
29
6.2
10
9.1
4.4
stage
4/19 4/20
Wed Thur
43.5 47.6
34.8 43.7
2.6 2.1
1.4 0.9
412 378
166 100
8 5
7 4
1.4 1.8
0.6 1.3
17 17
0.5 0.7
41 30
6.3 6.5
9 10
6.3 5.5
4/21
Fri
43.1
31.4
1.0
1.0
368
42
1
1
1.0
<.5
18
0.4
32
6.7
10
4.8
4/22
Sat
39.2
27.5
2 .5
1.0
410
128
5
2
1.4
0.1
17
0.3
52
7.3
10
5.4
4/23
Sun
35.3
31.4
1.4
0.5
388
96
1
1
0.8
0.2
16
0.4
42
7.0
10
6.8
4/24
Mon
23.6
19.7
1.9
0.4
400
92
2
2
1.0
0.7
17
0.2
39
7.0
10
6. 5
* Grab sample
4/25 4/26
Tues Wed
47.1 42.6
27.5 34.9
2.6
0.7
340 516
86 80
3 3
2 2
1.1 1.5
0.3 0.3
17 19
0.2 0.6
^91 ^148
7.5 7.4
10 10
7.0 5.8
8.9
** Measured
5/1
Mon
26. 9
23. 1
7.8
776
84
3
2
1, 4
0.4
16
0.4
46
6.6
10
6.6
j n the
5/2
Tues
35.6
15.8
0.5
462
106
11
10
1.4
0. 1
15
0.3
57
7 . 2
10
6.3
second
5/3
Wed
35.2
31. 3
1.1
0.2
506
106
2
1
2.2
0.2
19
0. 3
58
7.0
10
6. 5
25.4
stage
5/4
Thur
44
32
1.1
0.2
542
186
5
3
1.8
0.2
26
56
6. 7
11
0.8
final
5/5
Fri
31.7
27.8
1.1
0.8
544
210
11
6
0.4
24
0.2
58
6.9
11
5.3
5/6
Sat
35.9
23.9
6.1
0. 5
486
190
10
2
1.6
18
0.1
52
7. 0
11
4.5
5/7
Sun
35.9
23.',
0. 3
0.1
510
228
2
1
1.8
1.0
22
0. 1
40
6.9
12
f .6
clarif ier
-------
N>
TABLE G-5
MARLBOROUGH - PHASE
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Suspended Solids
PH
Temperature, °C
Alkalinity
D.O. Uptake, mg/l-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-M
Nitrate-N
Settlometer (Avg. 3 values)
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
4/17
Mon
2140
1450
1900
1360
6.4
9
123
19.7
6.7
14
0.8
350
265
215
190
180
175
165
160
160
4/18
Tues
2880
1980
2590
1920
6.4
9
125
30
7.7
11
0.9
385
295
265
245
235
220
210
195
190
4/19
Wed
2580
1750
2290
1690
6.3
10
127
30.2
7.4
202
15
0.8
325
255
220
195
180
175
165
160
155
4/20
Thur
2230
1430
1980
1360>
6.4
10
105
17.6
7.9
11
0.9
210
"165
145
135
130
130
120
115
115
4/21
Fri
1890
1250
1650
1200
6.5
10
127
27.2
4.0
128
13
1.0
330
260
230
210
200
190
185
175
165
MIXED
4/22
Sat
2470
1610
2170
1530
6.7
10
125
23.8
7.5
143
14
0.9
345
260
235
210
200
195
190
180
175
I
LIQUOR (mg/1)
4/23
Sun
1320
865
1060
820
6.7
9
95
16.3
8.4
115
14
0.7
245
190
170
155
150
145
140
135
135
4/24
Mon
1390
830
1100
790
6.8
10
92
15.5
8.1
89
13
0. 9
195
155
145
140
135
130
125
115
115
4/25
Tues
1400
880
1050
800
6.9
10
91
18.5
8.0
98
12
1.0
190
150
135
130
125
125
125
120
120
4/26
Wed
1430
370
1100
680
6.9
10
103
13. 6
7.5
87
13
1.1
195
150
140
135
125
125
125
125
120
4/27
Thur
1600
1020
1270
950
6.9
11
104
12.5
8.0
17
0. 9
185
145
135
130
130
130
125
125
120
5/2
Tues
1310
770
930
640
6.8
11
155
14.8
8.6
12
0.9
145
115
110
110
105
105
100
95
95
5/3
Wed
1640
960
1270
900
7.1
12
171
12.8
8.5
111
20
0. 7
155
120
110
105
100
95
90
90
90
5/4
Thur
1910
1160
1480
1030
7. 0
12
204
28.2
4.1
27
0.9
180
150
140
135
130
125
120
115
115
5/5
Fri
1830
1170
1430
1000
7.1
11
166
15.5
7.6
15
0.8
230
185
175
165
160
160
155
150
150
5/6
Sat
1610
940
1130
860
7.1
12
178
19.3
7. 3
123
17
0. 6
215
175
160
150
145
140
130
130
130
5/7
Sun
1300
810
940
680
7. 0
12
155
16.2
9.1
115
17
1. 0
185
140
125
125
120
120
115
115
115
-------
TABLE G-6
MARLBOROUGH - PHASE I
MIXED LIQUOR - SECOND STAGD - FIRST COMPARTMENT (mq/1)
Date 4/17 4/18 4/19 4/20 4/21 4/22 4/23 4/24 4/25 4/26 4/27 5/2 5/3 5/4 5/5 5/6 5/7
Day Won Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Tues Wed Thur Fri Sat Sun
Total Solids 3820 3480 3940 3560 3270 4060 2780 3900 4130 3750 3890 4100 4070 3980 4030 3970 3950
Total Volatile Solids 2260 2050 2350 2120 1950 2440 1700 2340 2360 2190 2190 2470 2390 2300 2420 2190 2280
Suspended Solids 3500 3100 3520 3190 2930 3630 2510 3500 3610 3290 3350 3670 3600 3520 3580 2510 3500
Volatile Susp. S'olids 2140 1970 2260 2050 1900 2330 1670 2280 2240 2030 2090 2390 2290 2200 2300 2090 2100
pH 6.5 6.3 6.2 6.4 6.6 7.0 7.0 6.9 7.5 7.6 7.4 6.8 6.8 7.0 77 6.8 6.8
Temperature, °C 9 9 9 10 10 10 10 10 10 11 11 10 11 11 11 11 12
M Alkalinity 118 139 144 142 145 215 167 138 205 279 332 181 194 231 169 173 174
00
D.O. Uptake, mg/l-hr 37.8 60.0 24.0 56.8 60.0 40.6 15.1 37.2 60.0 19.6 35.1 12.6 57.6 65.5 60.0 66.7 66.7
Dissolved Oxygen 1.1 1.6 1.0 0.6 0.7 0.7 0.7 0.8 0.8 0.7 0.7 0.6 0.7 0.5 0.5 0.5 0.3
Total Kjeldahl-N 148 185 174 174 174 193 215 182 218
Ammonia-N 2.4 0.9 1.5 3.5 6.5 2.6 3.1 2.0 1.1 3.2 0.9 1.4 0.6 1.0 0.3 3.8 4.2
Nitrate-N 12.5 10 12.5 9.5 6.5 6.0 8.0 13 9.8 15.5 13.5 14.5 17.5 18 17 9.5
-------
TABLE G-7
MARLBOROUGH - PHASE I
MIXED LIQUOR - SECOND STAGE - LAST COMPARTMENT (mg/1)
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, °C
Alkalinity, CaCO3
D.O. Uptake, mg/l-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
4/17
Man
3930
2440
3600
2370
6.8
9
136
15.7
8.5
1.7
480
380
330
300
280
260
260
250
240
4/18
Tues
4120
2470
3720
2360
6.3
9
140
17.3
9.2
0.4
15
460
400
300
280
260
250
240
230
220
4/19
Wed
4210
2480
3770
2380
6.2
9
169
16.4
8.6
1.6
12
480
380
330
300
280
260
250
230
230
4/20
Thur
4000
2340
3600
2160
6.8
10
152
15.3
8.1
1.5
15
480
370
300
290
270
260
250
230
220
4/21
Fri
3830
2290
3500
2170
6.5
10
147
14.4
6.5
145
2.7
14
450
350
300
270
260
250
230
210
200
4/22
Sat
3750
2240
3350
2170
7.0
10
207
19.1
8.7
174
4.8
4.9
450
350
300
300
270
250
240
220
220
4/23
Sun
3970
2380
3580
2280
6.9
10
180
14.3
8.4
162
2.9
7.0
490
380
330
300
280
270
250
250
250
4/24
Mon
4060
2430
3630
2310
6.8
10
137
14.2
8.4
176
2.1
10
470
370
310
280
270
250
235
220
210
4/25
Tues
4280
2460
3790
2380
7.4
10
218
15.9
8.6
171
1.3
14
500
350
330
300
270
260
240
230
220
4/26
Wed
4100
2400
3560
2220
7.5
11
266
28.4
7.8
204
1.6
13
470
360
300
280
260
250
240
220
215
4/27
Thur
4150
2310
3580
2210
7.2
11
282
11.5
8.3
0.6
17
420
340
290
270
250
240
230
220
210
5/2
Tues
4170
2480
3700
2410
6.8
10
183
14.3
8.7
0.7
15
480
360
330
290
270
250
230
220
210
5/3
Wed
2750
1570
2320
1520
6.8
11
202
11.9
7.7
0.8
15.5
450
365
320
285
270
260
240
230
225
5/4
Thur
4490
2680
4010
2540
6.8
11
193
13.2
5.5
251
1.1
27
520
410
360
320
295
280
250
235
230
5/5
Fri
3190
1900
2750
1680
6.7
11
193
10.0
7.8
0.3
21
490
390
380
310
285
270
250
240
235
5/6
Sat
4050
2260
3580
2130
6.7
11
159
13.2
7.5
120
1.7
20
420
330
290
270
250
240
220
210
210
5/7
Sun
4060
2470
3610
2280
6.7
12
159
14.1
8.5
227
2.4
12
450
350
300
260
240
230
220
220
210
-------
to
Date
TABLE G-8
MARLBOROUGH - PHASE I
RETURNED AND COMBINED SLUDGES (mg/1)
4/17 4/18 4/19 4/20 4/21 4/22 4/23 4/24 4/25 4/26 4/27 4/28
Sludge Returned to First
Stage Aeration
Total Solids 4400
Total Volatile Solids 3100
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Aramonia-N 1.4
Nitrate-N 13.5
Capillary Suction Time,38.4
sec
Return Rate,cu m/sec 0.06
mgd
(1.4)
Sludge Returned to
Second Stage Aeration
Total Solids 5680
Total Volatile Solids 3380
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N 11
Nitrate-N 8
Capillary Suction Time, 7.6
sec
Return Rate,cu m/sec 0.21
mgd
(4.8)
4860 5350 4890 7810 5370 3720 3410 3450 2230 3290
3500 3710 3370 6770 3590 2520 2340 2340 1540 2230
4330 4970 4590 7210 4960 3410 3090 2920 1780 2940
3350 3600 3280 6490 3440 2400 2240 2220 1510 2160
325 766 300 274 190 204 258
15.5 8.4 18 17 20 17 11 12 13 13
0.9 1.2 0.7 0.9 1.0 2.0 1.0 1.0 1.8 0.8
26.6 15.2 13.0 14.7 17.3 9.0 8.4 9.2 8.6
0.06 0.07 0.06 0.06 0.05 0.05 0.06 0.05 0.05 0.05
(1.4) (1.5) (1.4) (1.4) (1.2) (1.2) (1.3) (1.2) (1.2) (1.1)
6270 6240 6820 6330 5860 5430 6020 6380 5900 6350
3860 3780 4080 3850 3470 3220 3680 3740 3390 3660
5890 5880 6430 5800 5440 4880 5550 5620 5360 5830
3790 3700 3970 3650 3360 3030 3570 3630 3390 3580
386 570 286 274 277 257 330
1.9 1.5 2.1 1.5 7839 2.1 3.8
15 8.7 13 8.0 2.1 3.3 8.0 14 8.5 15
8.1 7.2 7.7 9.0 9.8 9.5 7.4 7.3 8.1
0.21 0.21 0.20 0.21 0.21 0.21 0.22 0.22 0.22 0.22
(4.8) (4.7) (4.6) (4.8) (4.9) (4.9) (5.0) (5.0) (5.1) (5.0)
(•continued)
5/1 5/2 5/3 5/4 5/5 5/6 5/7
1840 2090 2360 1220 3080 2530
1080 1250 1480 810 2070 1720
1420 1740 1840 960 2693 2070
950 1190 1300 770 1910 1480
165 171 182
16 30 22 13 19 20
0.8 10.8 1.2 0.8 0.8 0.9
11.2 8.1 7.7 11.4 8.1 9.7
0.07 0.07 0.08 0.08 0.07 0.07
(1.6) (1.5) (1.7) (1.7) (1.6) (1.6)
6290 6290 6180 2600 5500 6400
3710 3720 3580 1590 3300 3870
5770 5820 5680 2260 5050 5940
3510 3630 3500 1560 3140 3690
316 176 364
1.1 1.6 2.2 0.2 1.5 3.8
13 13 22 21 18 5.2
11.7 8.2 7.3 7.7 7.7 7.9
0.24 0.23 0.23 0.23 0.23 0.24
(5.5) (5.3) (5.3) (5.3) (5.3) (5.4)
-------
Date
TABLE G-8, (continued)
4/17 4/18 4/19 4/20 4/21 4/22 4/23 4/24 4/25 4/26 4/27 4/28
5/1 5/2 5/3 5/4 5/5
Combined Primary, First
and Second Stage Sludges
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Capillary Suction Time,
sec -.
Sludge Wasted, 10 liters
103gal
23930
16660
22770
16010
1019
225
a
850
268
84
(22.1)
58030
33530
52740
30280
2027
1030
252
105
(27.8)
58100
40180
54530
38050
2027
74
(19.6)
57670
37170
54240
34880
1036
222
1240
468
110
(29.1)
49460
32870
45860
30580
358
70
4. 9
431
98
(26.0)
49950
32550
46960
30550
1697
200
9.0
1180
386
83 69
(22.0) (18.D
46360
25470
43440
23650
150
5.5
425
232
73 138 95
(19.3) (36.5) (25.2)
57460
35990
53620
33520
2173
560
10
1360
499
78 96
(20.5) (25.4)
26270
15070
23880
14420
1994
150
0.8
332
84
(22.1)
5/6
-------
TABLE G-9
MARLBOROUGH - PHASE I
VACUUM FiLi'fER (mg/1)
Date
Day
Vacuum Filter Filtrate
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Vacuum Filter Cake
Total Solids, %
Total Volatile Solids,'
Quantity, kg/day
Ib/day
Ferric Chloride,
kg/day
Ib/day
Lime, kg/day
4/18
Tues
2960
2210
1260
780
3470
522
627
217
2770
300
50
27.6
i; 7.5
(283)
2126
4686
4/20
Thur
5250
3090
8530
2160
966
248
12.1
403
600
24
26.4
7.8
5566
12270
(394)
3382
7455
4/21
Fri
4880
4050
7870
2270
716
258
12.1
364
380
21
24.8
10.4
3552
7833
(271)
3575
7881
4/24
Mon
6270
5920
3900
4140
8640
2710
930
ISO
12.0
21.6
10.6
5820
12830
(332)
3483
7678
4/25
Tues
5510
4610
3540
2760
8370
2640
1060
284
12.1
325
290
22.0
11.2
4205
9270
(381)
3092
6816
4/26
Wed
5610
4860
3960
3630
8660
2940
1180
262
12.0
176
550
10
22.2
11.0
4001
8820
(344)
2222
4899
4/27 4/28 5/1 5/2
Thur Fri Mon Tues
4350
3580
2590
1680
8210
2080
740
160
12.3
342
340
30.0
7.8
3086 3151 9240 5520
6804 6947 20370 12170
(283) (271) (344) (369)
2995 2125 6956 3961
6603 4686 15336 8733
5/4
Thur
5700
5040
4350
3700
9330
2430
1130
232
12.2
251
210
18
6.5
25.7
10.2
5375
11850
(406)
2705
5964
5/5
Fri
5200
4200
3160
2380
7860
2280
990
204
12.1
30.4
7.6
4105
9050
(332)
3865
8520
232
-------
co
Phase
Dates
Start
Completion
Total Volume, liters
(gals)
Feed Rate, liter/day
% Daily Flow
COD-Total
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
pH
Alkalinity
Total Phosphorous
Grease
APPENDIX H
TABLE H-l
MARLBOROUGH - PHASE II
SEPTAGE (mg/1)
*IIIA *IIB
5/8 - 5/10 5/16 - 5/18
Mon 8a.ra. Tues 7a.in.
Thur 8a.m. Thur la.m.
333100 375000
(88000) (99000)
109800 215750
(29000) (57000)
1.25 2.14
24500 27500
7410 11180
5900 8450
16970 18940
12420 14450
14530 15270
10780 12160
730 640
170 100
6.4 4.6
830 0
480 220
1643 3121
Phase
Date
Day
Flow Rate, cu m/sec
mgd
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
Temperature, C
Grease
TABLE H-2
MARLBOROUGH - PHASE II
INFLUENT (rag/1)
IIA
5/8
Mon
0.11
(2.4)
376
124
136
128
146
120
26.9
21
0.8
135
6.9
12
5/9
Tues
0.10
(2.3)
263
90.2
120
110
534
318
324
228
25.5
20
1.4
6. 3
131
6.9
12
124
5/10
Wed
0.10
12.3)
277
75.1
130
99
880
756
370
354
26.0
18
1.2
4.6
131
6.9
12
218
5/11
Thur
0.11
(2.4)
285
138
98
650
382
348
316
26.4
22
0.7
8.5
134
6.8
12
5/15
Mon
0.11
(2.5)
344
160
177
125
896
646
354
298
28.3
20
0.6
5.5
126
6.8
12
IIB
5/16
Tues
0.12
(2.7)
435
82.4
200
125
42.3
14
0.7
7.3
122
6.7
12
5/18
Wed
0.12
(2.8)
272
63.0
138
114
564
308
272
246
65.0
11
1.1
3.3
111
6.6
12
209
* Average values for samples collected during test periods
-------
TABLE H-3
MARLBOROUGH - PHASE II
PRIMARY EFFLUENT (mg/1)
Phase
Date
Day
Composite or Grab Time
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
to Total Volatile Solids
U>
it* Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkal in ity
pi I
**Tcmperature
"^Dissolved Oxygen-Top
Bottom
Grease
IIA
5/8
Mon
Com
327
128
108
69
630
206
170
133
32.5
21
0.9
192
7.1
12
0.7
0.3
5/9
Tues
Com
306
82.4
88.5
64.5
620
388
212
122
34.2
35
1.0
1.5
190
7.2
12
4.2
0. 3
160
5/10
Wed
Com
296
83.0
113
74
526
300
216
152
33.6
28
0.8
9.2
194
7.2
12
1.0
0. 3
110
5/10 5/10 5/11
Wed Wed Thur
8am 5pm Com
277 443 289
58.6
122 40.5
21.0
526
182
148
88
45.3
18 18
1.0 1.2 1.2
6.5
191
7.3
13
1.8 0.5
0.2
5/15
Mon
Com
420
96
197
108
690
346
284
220
40.0
23
0.7
10.3
177
6.9
5/16
Tues
Com
255
94.1
108
61.5
516
268
152
112
41.4
24
0.8
6. 5
164
6.8
12
0.4
0.3
5/16
Tues
1pm
332
145
147
123
620
268
132
90
65.9
31
0.9
4.8
230
8.6
5/16
Tues
7pm
379
160
185
155
530
250
60
48
37.2
28
1.0
7. 5
132
6.7
2.4
5/17
Wed
3am
371
180
152
125
472
236
112
72
14.6
12
1.2
3.8
111
6.4
5/17
Wed
7am
325
153
173
110
460
228
88
78
25. 5
15
1.1
6.1
104
6.4
IIB
5/17
Wed
1pm
488
284
239
224
524
188
142
100
66.4
25
0.8
8.0
199
7.3
5/17
Wed
5pm
341
158
170
152
438
156
94
68
26.9
14
0.6
8.8
135
6.7
1.7
5/17
Wed
9pm
413
111
213
177
518
236
140
100
25.2
15
0.8
11.0
111
6.5
5/17
Wed
Com
318
82.4
147
90
508
250
168
132
29.4
17
0.8
6. 3
152
6.7
14
2. 2
0.3
914
5/18
Thur
Com
191
63. 5
409
100
108
58
28.6
17
0.9
5.6
153
7.1
13
1.5
0. 5
** Measured in the primary clarifier.
-------
TABLE H-4
MARLBOROUGH - PHASE II
SECONDARY EFFLUENT (mg/1)
fO
UJ
Ul
Phase
Date
Day
Composite or Grab Time
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
**Temperature
**Dissolved Oxygen
Grease
"Measured in the primary clarifier.
5/8
MOD
Com
86.3
70.6
7.2
2.4
376
134
23
3
17.6
15
5.0
110
6.9
13
4.1
5/9
Tues
Com
39.2
35.3
2.7
2.1
456
180
16
15
17.2
16
4.0
0.8
74
7.2
13
2.0
IIA
5/10 5/10
Wed Wed
Com Sam
59.3 83.0
51.4 67.4
16.2 7.0
3.2 3.1
352
160
15
9
18.2
19
4.3 1.2
0.7
134
7.1
13
2.2
35.2
I IB
5/10 5/11
Wed Thur
5pm Com
59.3 54.7
43.0
11.6
1.4
352
76
24
13
19.3
12
1.4 5.0
0.6
139
7.5
13
0.2 1.9
5/15
Mon
Com
60
52
12.9
3.5
360
112
6
4
18.8
18
4.0
1.3
103
6.8
13
3.2
5/16
Tues
Com
43.1
15.7
5.4
2.2
388
100
11
8
14.3
19
2.2
1.4
117
6.8
13
3.7
5/16
Tues
1pm
78.1
43.0
4.8
2.2
342
80
9
6
15.0
21
1.2
2.1
117
7.0
5/16
Tues
7pm
58.6
39.1
4.2
1.0
404
122
7
6
9.5
17
1.2
1.4
142
7.1
1.7
5/17
Wed
3am
62.5
39.0
6.6
1.8
364
106
10
7
13.0
12
0.9
1.2
93
6.5
5/17
Wed
7am
35.3
27.5
8.2
2.6
354
96
19
11
12.9
11
1.1
1.7
93
6.4
5/17
Wed
1pm
90.5
47.5
6.4
4.8
328
15
11
15.4
13
0.9
0.1
93
6.5
5/17
Wed
5pm
59.4
59.3
6.2
4.2
306
11
10
16.5
12
1.0
1.0
115
6.7
0.6
5/17
Wed
9pm
64.8
43.5
4.4
2.0
358
34
11
6
14.3
12
1.0
1.0
98
6.4
5/17
Wed
Com
51.2
39.4
10.2
1.6
358
128
10
6
13.4
13 '
2.5
0.3
86
6.5
14
1.6
51.2
5/18
Thur
Com
43.7
43.7
346
18
10
8
16.6
7
3.5
0.9
87
6.9
14
3.6
-------
TABLE H-5
MARLBOROUGH - PHASE II
FINAL EFFLUENT (mg/1)
Phase IIA IIB
Date 5/8 5/9 5/10 5/10 5/10 5/11- 5/15 5/16 5/16 5/16 5/17 5/17 5/17 5/17 5/17 5/17 5/18
Day Mon Tues Wed Wed Wed Thur Mon Tues Tues Tues Wed Wed Wed Wed Wed Wed Thur
Composite or Grab Time Com Com Com Sam 5pm Com Com Com 1pm 7pm 3am 7am 1pm 5pm 9pm Com Com
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids 244
to
J^ Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
Temperature
Dissolved Oxygen
Grease
47.0
35.3
1.3
1.1
454
244
18
13
2.2
0.6
20
37
6.7
12
5.9
47.0
39.2
1.1
1.0
500
224
7
7
2.1
0.2
19
0.8
51
7.0
13
5.6
6.8
39.5 43.5
39.5 31.6
2.4 9.9
0.8
482
244
30
26
1.7
0.6
20 22
2.0
50
7.0
13
5.0
5.5
39.5 31.2
31.2
1.4
0.1
504
100
34
22
1.7
0.5
21 24
1.0
41
6.9
13
3.4 5.3
44
44
1.0
0.7
498
228
8
7
2.7
0.7
21
2.1
30
6.6
13
5.3
39.2
35.3
1.3
0.2
494
200
14
11
3.4
1.7
20
1.4
35
6.5
12
5.3
35.2
35.2
7.8
0.6
474
108
16
13
0.2
19
1.5
47
6.8
35.2
27.3
8.0
1.0
442
154
19
10
2.0
0.8
20
0.1
38
6.5
4.3
46.9
35.2
10.4
1.3
484
294
16
12
2.8
0.9
0.9
51
6.8
27.5
23.5
8.8
1.7
566
232
31
18
2.9
0.9
18
0.6
51
6.5
51.2
35.4
7.3
1.4
338
58
38
28
3.6
0.3
14
0.3
52
6.5
51.2
43.3
7.6
1.1
372
72
10
8
2.2
0.6
15
0.4
45
6.5
6.0
43.3
39.4
8.2
2.0
436
96
21
10
3.1
0.4
16
0.6
42
6.3
35.4
23.6
2.0
0.9
500
200
9
6
2.0
18
0.6
40
6.6
5.2
24.8
39.7
43.
474
92
17
7
2.2
0.3
15
0.9
40
6.5
13
6.5
-------
TABLE H-6
MARLBOROUGH - PHASE II
MIXED LIQUOR - FIRST STAGE (mg/1)
Phase
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, C
Alkalinity
D.O. Uptake, mg/l-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
5/8
Mon
1360
860
970
780
7.0
13
143
15.8
7.6
13
0.8
180
140
125
125
120
120
110
105
105
5/9
Tues
1760
1290
1310
1140
6.8
13
171
20.0
5.7
115
18
0.9
215
165
155
140
135
1.5
120
120
115
1 1 A
5/10
Wed
1770
1180
1310
920
7.0
13
149
18.6
6.1
146
21
1.5
215
175
155
145
135
125
115
115
115
IIB
5/11
Thur
1670
1010
1270
880
7.0
13
182
14.4
6.7
123
24
1.1
205
160
140
135
130
125
120
120
110
5/12
Fri
1320
810
1270
760 •
6.9
14
169
17.6
7.1
90
14
1.2
200
165
150
135
135
130
120
120
120
5/16
Tues
1570
1080
1250
980
7.0
13
150
13. -6
7.3
154
20
0.8
235
205
180
170
160
155
140
130
130
5/17
Wed
1730
1110
1410
1070
6.7
14
123
18.6
4.9
9
1.1
260
210
195
185
180
175
160
155
145
5/18
Thur
2310
1620
1780
1400
6.9
13
147
17.7
6.2
199
13
0.9
405
310
275
260
250
235
220
215
210
237
-------
TABLE H-7
MARLBOROUGH - PHASE II
MIXED LIQUOR - SECOND STAGE - FIRST COMPARTMENT (2A) (mg/1)
Phase
Date 5/8
Day Mon
Total Solids 4080
Total Volatile Solids2470
Suspended Solids 3930
Volatile Susp. Solids2300
pH 6.8
Temperature 13
Alkalinity 168
D.O.Uptake, mg/l-hr 67.3
Dissolved Oxygen 0.9
Total Kjeldahl-N
Ammonia-N 1.0
Nitrate-N 12
5/9
Tues
3730
2290
3300
2140
6.7
13
190
60.0
0.6
224
1.4
17
IIA
5/10
Wed
3650
2220
3120
1950
6.7
13
181
72.0
0.3
171
4.2
14
5/11
Thur
3850
2220
3360
2110
6. 9
13
166
75.8
0.4
218
2.6
17
5/12
Fri
4110
2510
3730
2370
6.6
13
181
86.8
0.6
213
3.8
16
5/16
Tues
4260
2540
3790
2410
6.5
13
145
65.1
0.4
311
11
18
I IB
5/17
Wed
4650
2740
4250
2690
6.7
14
123
21.2
0.7
227
2.8
10
5/18
Thur
1100
600
760
560
6.5
13
135
9.9
0.3
204
1.6
12
238
-------
TABLE H-8
MARLBOROUGH - PHASE II
MIXED LIQUOR - SECOND STAGE - LAST COMPARTMENT (2B) (raq/1)
Phase
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature
Alkalinity
D.O. Uptake, mg/l-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
5/8
Mon
4180
2510
3720
2410
6.8
13
160
9.0
8. 7
0.4
15
430
330
280
250
240
230
210
200
200
5/9
Tues
2950
1760
2480
1610
6. 7
13
171
10.2
7.5
238
0.6
18
400
300
270
240
230
220
200
190
190
IIA
5/10
Wed
4430
2740
3900
2470
6.7
13
177
13.0
7.2
207
1.5
18
390
300
270
250
230
220
200
200
5/11
Thur
4500
2640
3990
2500
6.8
13
161
10.9
7.8
227
1.1
21
440
320
280
250
240
230
210
200
200
5/12
Fri
4040
2420
3650
2260
6. 7
13
169
13.2
7.9
202
1.8
20
440
340
290
260
240
230
220
200
200
5/16
Tues
4490
2680
4020
2510
6. 7
13
160
12.5
8.1
412
1.3
20
400
300
270
250
230
220
200
200
200
IIB
5/17
Wed
4450
2530
4070
2500
6.6
14
166
10.3
8.3
221
1.3
12
490
300
260
240
230
210
200
200
190
5/18
Thur
3980
2460
3610
2410
6.4
13
141
10.0
8.2
246
0. 7
13
400
300
260
240
220
210
200
200
200
239
-------
TABLE H-9
MARLBOROUGH - PHASE II
RETURNED AND COMBINED SLUDGES (mg/1)
Phase
Date
Day
Sludge Returned to First
Stage Aeration
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Amraonia-N
Nitrate-N
Capillary Suction Time,
sec
Return Rate, cu m/sec
(ragd)
5/8
Mon
2270
1480
1840
1240
18
1. 5
9.6
0.07
(1.6)
5/9
Tues
2900
1970
2460
1810
182
17
1. 0
10.2
0.07
(1.5)
IIA
5/10
Wed
2930
2120
2470
1880
230
19
1.2
12.2
0. 06
(1.4)
5/11
Thur
2520
1680
2100
1580
193
20
1.2
10.1
0.07
(1.6)
5/12
Fri
2710
1820
2530
1700
218
15
1.0
8.7
0.07
(1.6)
5/16
Tues
2890
2010
2540
1930
272
12
1.1
13.2
0.07
(1.6)
IIB
5/17
Wed
2920
2070
2570
1970
179
10
0.9
12.5
0. 07
(1.5)
5/18
Thur
3850
2650
3450
2490
333
14
0.7
29.2
0.07
(1.6)
Sludge Returned to Second
Staqe Aeration
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Capillary Suction Time,
sec
Return Rate, cu m/sec
(mgd)
6930
4190
6430
4050
0.4
9
8.9
0.24
(5.5)
6290
3950
5820
3710
328
2.0
15
8.0
0.25
(5.5)
6910
4230
6390
3990
342
2.2
14
7.2
0.25
(5.7)
5500
3250
5010
3140
283
2.9
18
8.4
0.26
(6.0)
7600
4540
7280
4510
400
3.6
13
8.7
0.27
(6.1)
6280
3620
5730
3460
451
3.4
17
8.2
0.26
(6.0)
6550
4290
6100
4160
372
1.6
5.5
8.8
0.30
(6.9)
5130
3090
4730
3020
414
2.0
10
9.0
0.28
(6.3)
(continued)
240
-------
TABLE H-9 (continued)
Phase
Date 5/8
Day Mon
Combined Primary, First
and Second Stage Sludges
Total Solids 27160
Total Volatile Solids 17530
Suspended Solids 25340
Volatile Susp. Solids 16400
Total Kjeldahl-N 1100
Ammonia-N 160
Nitrate-N 10
Total Phosphorous 500
Capillary Suction Time, 347
sec
IIA
5/9 5/10 5/11
Wed
60230 68510
33040 38500
54680 64310
30040 35590
1860 1480
26 220
13 10
2300
131 388
Thur
62590
34990
57950
31760
2110
210
13
1450
408
5/12
Fri
81710
32730
75760
30580
1814
260
9
6800
101
5/16
Tues
IIB
5/17 5/18
Wed Thur
67510 61360 75410
35580 35750 38820
61610 57640 68750
32510 33320 35340
2010 1954
340 300 260
12 16 11
1250 1700 950
426 323 233
241
-------
TABLE H-10
MARLBOROUGH - PHASE II
VACUUB FILTER (rng/1)
Phase
Date
•Day
VACUUM FILTER FILTRATE
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
VACUUM FILTER CAKE
Total Solids, %
Total Volatile Solids, t
Quantity, kg/day
(Ib/day )
Ferric Chloride, kg/day
( Ib/day)
Lime , kg/day
( Ib/day )
IIA
5/8
Mon
3030
2350
2050
1630
7450
2100
1190
310
12.0
250
29. 0
7.0
5394
(11892)
167
(369)
4831
(10650)
5/9
Tues
4770
4060
3040
2820
7830
2090
760
290
12.0
409
10.5
26.6
9. 3
8308
(18315)
190
(418)
4444
(9789)
5/10
Wed
5050
4030
2400
2300
7630
2760
540
160
12.0
431
440
75
16
25.0
9.0
7317
(16131)
173
(381)
2705
(5964)
5/11
Thur
4820
3910
3250
2650
8540
2320
1380
350
380
110
10
23.7
8.0
7117
(15690)
179
(394)
3671
(8094)
5/12
Fri
3870
3440
3570
2190
6900
1230
630
210
12.2
375
240
8
26.5
10.9
5903
(13013)
145
(320)
3768
(8307)
5/16
Tues
4080
3120
2480
1980
7780
1990
750
370
12.0
340
10
24
26.1
6.7
5356
(11807)
167
(369)
3188
(7029)
IIB
5/17
Wed
4000
3100
2540
1860
8260
2760
1080
360
11.9
300
17
13
25.4
10.6
5242
(11556)
151
(332)
3671
(8094)
5/18
Thur
4500
3150
8230
1340
1260
320
11.9
383
400
13
7.5
28.2
8.6
6090
(13428)
156
(344)
3478
(7668)
242
-------
TABLE H-ll
MARLBOROUGH - PHASES I AND II
HEAVY METALS (mg/1)
Phase
Date 4/18
Septage Loading % Flow
Influent
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
Primary Effluent
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
Secondary Effluent
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
Final Effluent
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
Septage
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
.16
.04
0
.28
.03
.14
.30
.04
0
.37
.04
1.0
.08
.06
0
.20
.03
.18
.10
.07
0
.17
0
0
4/20
0.22
0
0
0.19
0
0.07
0.10
0
0
0.15
0
0.06
0.09
0
0
0.23
0.03
0.10
0.06
0
0
0.11
0
0
4/25
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
.15
. 04
0
.15
.03
.06
.13
.05
0
.13
0
.26
.07
0
0
.17
.03
.12
.20
.11
0
.07
.02
.07
I
4/27
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
.17
.07
0
.38
.03
.09
.17
.04
0
.14
. 02
.13
.07
0
0
.17
.03
.10
.07
0
0
.19
0
0
5/2
0.18
0.05
0
0.22
0
0.13
0.15
0.05
0
0.68
0.02
0.08
0.07
0.05
0
0.14
0
0.07
0.08
0.04
0
0.05
0
0.10
5/4
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0,
0,
0.
0.
21
0
0
40
0
0
16
06
0
26
0
.08
.09
0
0
.15
0
,25
.08
.04
0
.18
.02
.16
5/5
0.
0.
0.
0.
0.
0.
0.
5.
0.
4
0.
3.
0.
0.
0.
0.
30
07
25
27
03
0
21
16
0
29
0
26
.8
06
0
96
0
15
06
07
0
0
33
0
0
0
0
0
0
0
0
0
0
0
0
0
IIA
5/9 5/10
1.25
.16
0
0
.29
.02
0
.15
.10
0
.59
0
0
.06
.03
0
.11
.03
0.0
.26
0
0
.46
.03
0.0
15.4
0
1
3
0
2
.68
.48
.60
.08
.36
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
21
0.
2.
6.
3.
22
0
0
28
0
10
24
0
0
52
0
17
06
07
0
13
0
16
07
0
0
89
0
12
.2
88
52
10
0
44
IIB
5/17
2.14
0.
0.
0.
0.
0.
8
0.
0.
0.
0
0.
0.
0.
0.
0.
0.
13
0.
1
15
0.
2.
20
0
0
28
0
18
16
10
0
.6
0
14
09
11
.5
21
03
07
07
10
0
32
0
0
.4
16
.0
.0
08
00
(continued)
243
-------
TABLE H-ll (continued)
Phase
Date
Septage Loading
Vacuum Filter Filtrate
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
Combined Sludge
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
Cake rag/kg dry cake
Copper
Nickel
Chromium
Zinc
Cadmium
Lead
4/18
0.37
0.35
0
0. 42
0.04
0.35
7.1
2.00
5.50
22.8.
0.22
4.21
3305
736
1471
8337
128
1178
4/20
0.42
0.40
0
0.50
0.08
0.50
34.8
3.90
1.3
43.6
0. 50
13.60
4393
744
908
7261
109
1815
4/25
0.45
0.50
0
0.55
0. 07
0.50
33.8
3.83
12.5
42.0
0.43
7.30
4806
915
1526
9612
108
1678
I
4/27 5/2
0.33
0.31
0.25
0. 38
0.07
0.45
19.0
1.46
7. 5
22. 9
0.26
11.60
3106
613
958
7163
146
1987
5/4
0.45
0.28
0
2.90
0.04
0. 54
39.6
4.64
10.0
15.1
0.60
10.48
4964
685
1834
5673
98
2127
5/5
0.40
0.35
0
0.44
0.05
0.45
45.2
5.00
8.20
11.9
0.68
12.64
4275
717
690
5985
138
1572
5/9
1
0.37
0.30
0
0.41
0.07
0.42
48.4
5.80
16. 0
15.7
0. 96
15.12
4779
748
813
13004
163
1853
IIA
5/10
.25
0. 38
0.27
0
0.61
0.06
0. 50
44 . 0
4.28
9.2
14.8
0.60
11.8
4279
513
1300
5921
137
1780
I IB
5/17
2.14
0.38
0.28
0
1.61
0.05
0.35
42.8
2.40
11.2
13.3
0.60
9.60
4312
605
1891
6052
189
2043
244
-------
Phase
Date
Start Shock
Length of Shock, min
Total Volume, gal
% of Avg. Daily Plow
% of Flow During Shock
COD-Total
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
PH
Alkalinity
APPENDIX I
TABLE 1-1
MARLBOROUGH - PHASE III
SEPTAGE (mg/1)
IIIA
5/30 5/31 6/1
7 am 7 am 7 am
30 30 30
21000 21000 21000
0.81 0.84 0.84
55 59 61
-t— 32260 >-
-* — 7800 —>-
~> 4970 >-
-f- -21160 —>-
—— 15300 *-
-«— 19610 =-
—- 14450 -••-*-
— 540 —>
-s 190 -f
•a— 5.8 *-
-«— 744 —*-
6/7
7 am
110
39000
1.8
22
21900
6080
5700
11390
8050
8910
6630
616
260
5.2
959
IIIB
6/8 6/8
7 am 2 pm
120 15
39000 12000
2.3
19 55
31200
9980
9300
19590
14660
17130
13140
756
190
5.3
1000
245
-------
Phase
Date
Day
Flow Rate, mgd
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Airanonia-N
Nitrate-N
Alkalinity
pH
TABLE 1-2
MARLBOROUGH - PHASE III
INFLUENT (mg/1)
5/29
Man
2.5
362
50.6
147
78
590
410
560
520
26
16
1.2
117
6.6
IIIA
5/30
Tues
2.6
298
78. 4
117
63
420
200
200
190
26
18
1.2
127
6.7
LI IB
5/31
Wed
2.5
336
72.0
510
260
160
150
62
17
1. 3
130
6.7
6/1
Thur
2.5
311
91.3
78
30
580
330
150
110
19
0.6
108
6.6
6/6
Tues
2. 3
383
108.0
138
86
420
150
140
120
29
21
2.2
140
6. 8
6/7
Wed
2.2
392
112.0
440
170
100
90
41
16
0.9
128
6. 7
6/8
Thur
2.2
254
184.0
98
63
560
360
150
140
25
23
1.1
133
6.8
246
-------
Phase
Date
Day
Time
Time After Shock, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
pH
Tempe ra ture
Dissolved Oxygen-Top
Bottom
TABLE 1-3
MARLBOROUGH - PHASE III
PRIMARY EFFLUENT (mg/1)
III A
5/29
Mon
Cora.
226
66.2
78.0
48.0
392
300
72
52
28.8
19
0.9
141
7.1
5/30
Tues
7am
0
218
105
78.0
60.0
352
150
82
40
32.2
19
1.1
141
7.2
15
1.1
0.4
5/30
Tues
7: 30am
h
206
99.4
75.0
52.5
418
272
56
34
29.1
19
1.0
145
7.2
5/30
Tues
Sam
1
432
179
162
138
538
274
107
79
35.0
21
1. 1
196
7.1
0.4
0.4
5/30
Tues
8: 30am
1*!
440
206
183
144
548
298
104
76
34.2
21
1.0
159
6.5
5/30
Tues
9am
2
366
171
144
120
472
232
154
94
34.7
25
1.0
156
6.7
0.3
0.6
5/30
Tues
10am
3
405
226
185
144
624
332
82
42
43. 7
29
1.2
266
8.5
0.3
0.3
5/30
Tues
llam
4
342
193
176
125
552
196
70
30
42.8
28
0.8
241
8.6
0.3
0.3
5/30
Tues
12 noon
5
342
187
168
126
550
138
74
38
39.8
26
1.3
245
8.6
0.3
0.2
5/30
Tues
2pm
7
388
216
195
155
610
248
86
68
35.3
24
1.6
245
8.6
0.2
0.2
5/30
Tues
4pm
9
310
153
117
104
420
84
32
30
25.2
22
1.6
173
8.2
0.4
0.3
5/30
Tues
6pm
11
333
145
153
104
436
152
84
64
24.6
14
1.0
153
7.2
2.2
0.4
5/30
Tues
9pm
13
353
141
177
131
384
134
78
68
14
1.1
137
7.1
1.5
0.3
5/30
Tues
Com.
247
94.1
114
48.0
432
162
64
60
22
1.3
175
7.0
5/31
Wed
7am
24/0
' 263
114
88.5
76.5
458
210
72
60
21.3
18
1. 3
159
7.0
15
0.2
0.4
5/31
Wed
7:30am
%
235
106
84.0
69.0
398
174
76
70
20
1.2
153
7.0
5/31
Wed
Sam
1
333
123
108
93.0
522
310
118
108
29
1.1
163
6.9
0.2
0.7
(continued)
-------
CO
Phase
Date
Day
Time
Time After Shock, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids 374
Suspended Solids
Volatile Susp. Solids 176
Total Kjeldahl-N
Ammonia-si
Nitrate-N
Alkalinity
pH
Temperature
Dissolved Oxygen-Top
Bottom
5/31 5/31 5/31 5/31
Wed Wed Wed Wed
8:30am 9am 10am 11am 12noon
TABLE 1-3 (continued)
III A
5/31 5/31 5/31 5/31 5/31 5/31 6/1 6/1 6/1
Wed Wed Wed Wed Wed Wed Thur Thur Thur
2pm 4pm 6pm 10:30pm Com. 7am 7:30am Sam
6/1 6/1 6/1 6/1
Thur Thur Thur Thur
:30am 9am 10am 11am
• ih
591
222
204
198
672
374
200
176
29
1.9
179
6.8
2
512
163
180
584
344
112
100
37.8
30
1.8
179
6.9
0.1
0.3
3
369
179
162
132
574
288
116
96
30
1.1
235
7.8
0.2
0.3
4
337
194
192
78.0
562
268
100
96
28
1.5
259
8.3
0.1
0.3
5
365
191
270
90.0
598
268
84
70
45.4
28
1.5
264
8.3
0.1
0.2
7
344
212
168
128
712
260
194
68
30
1.8
278
8.5
1.7
0.2
9
324
100
147
110
654
228
186
70
20
1.0
182
7.3
1.4
0.2
11
296
124
120
84.0
614
196
168
66
18
1.3
161
7.1
1.4
0.2
I5h
348
144
174
135
546
260
154
54
18
0.7
1.2
0.2
24/0
228
76
63.0 81.0
42.0 61.5
452
188
68
62
31.9
23
1.5
164
7.0
16
0.3
0.4
h
264
108
450
198
64
60
21
1.2
157
6.8
1
364
116
96.0
60.0
494
304
168
156
24
1.0
150
6.8
0.1
0.3
1*5
472
124
99.0
75.0
526
288
92
60
24
1. 3*
148
6.6
2
401
163
141
113
594
286
142
124
37.2
28
1. 8
180
7.0
0.3
0.3
3
376
183
141
114
576
246
78
62
38
1.4
235
8.2
0.4
0.3
4
349
206
174
125
560
238
66
54
38
1.5
263
8.5
0.3
0.2
(continued)
-------
to
£*•
VO
Phase
Date
Day
Time 1
Time After Shock, hrs.
COD-Total
COD-Soluble
BOD-Total
Bod-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
PH
Tempe ra ture
Dissolved Oxygen-Top
Bottom
TABLE 1-3 (continued)
III A
6/1 6/1 6/1 6/1 6/1 6/2 6/2
Thur Thur Thur Thur Thur Fri Fri
6/6 6/7
6/7 6/7
Tues Wed Wed Wed
III B
6/7 6/7 6/7 6/7 6/7
Wed Wed Wed Wed Wed
noon
5
381
210
159
128
584
240
63
60
44.5
35
1.4
259
8.7
0. 4
0.2
2pm
7
635
222
177
131
634
294
.54
46
25
1.5
247
8.8
0.9
2.0
4pm
11
290
159
141
110
564
246
78
67
22
0.7
195
8.1
1.2
1.3
6pm
13
508
341
129
102
500
102
86
70
19
2.0
150
6.9
1.5
0.9
Com.
222
74.8
63.0
42.0
516
176
92
62
22
1.2
182
7.0
7am 9 am
24 26
276
98.4
90.0
76.5
536
226
128
120
35.0
22
1.4
142
7.1
16
0.3 0.1
0.3 0.2
Cora.
243
75. 7
84.0
49.5
400
94
50
40
23
0.9
144
7.2
7am
0
247
104
111
73.5
464
172
76
52
33.3
18
1.0
161
7.2
17
0.2
0.3
7: 30am
h
223
104
58.5
458
190
86
38
17
1.1
165
7.2
Sam
1
379
91.6
126
70.5
616
346
248
200
20
1.4
213
6.9
0.1
0.2
8: 30am
l!j
916
290
345
273
848
546
540
492
35
1.2
203
6.9
9am
2
745
295
330
243
718
398
204
184
48.4
31
1.5
208
6.9
0.1
0.2
10am
3
622
275
285
240
694
336
160
140
41
1.2
233
7.1
0.1
0.1
11am
4
450
211
189
165
622
272
100
92
33
0.6
255
8.4
0.2
0.1
12noon
5
438
211
156
112
592
262
84
80
46. 2
38
1.2
251
8.5
0.1
0. 1
(continued)
-------
to
Ul
o
Phase
Date
Day
Time
Time After Shock, hrs. 7
COD-Total
COD-Soluble
BOD-Total
EOD-N Suppressed
Total Solids
Total Volatile Solids 226
Suspended Solids
Volatile Susp. Solids 60
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
PH
Temperature
Dissolved Oxygen-Top 0.2
TABLE 1-3 (continued)
6/7
Wed
2pm
7
384
188
213
122
564
226
74
60
25
1.3
195
7.2
0.2
0.1
6/7
Wed
4pm
9
332
164
216
113
494
210
48
46
19
0.7
166
6.9
0.4
0.2
6/7
Wed
6pm
11
340
184
171
118
526
240
44
42
19
1.2
155
6.8
0.3
0.1
6/7
Wed
Com.
252
88.0
103
93.0
502
274
74
52
21
1.3
179
7.0
6/8
Thur
7am
24/0
248
96.0
99.0
470
230
62
50
30.5
19
1.2
164
7.0
17
0.4
0.3
6/8
Thur
7 : 3 0 am
h
292'
104
105
81.0
476
238
90
74
18
1.3
161
6.4
6/8
Thur
Sam
1
632
240
198
188
668
420
224
162
21
0.6
167
6.7
0.2
0.2
III B
6/8
Thur
8:30am
1*5
1128
440
518
456
962
600
260
196
29
1.0
183
6.4
6/8
Thur
9am
2
1128
484
443
383
970
588
407
293
65.2
34
1.5
215
6.6
0.2
0. 3
6/8
Thur
10am
3
876
420
420
381
842
526
227
166
36
1.7
252
7.0
0.3
0.1
6/8
Thur
11am
4
688
371
368
155
918
452
284
164
45
1.5
271
7.3
0.1
0.1
6/8
Thur
12noon
5
633
270
336
209
722
316
196
108
51.8
40
1.4
243
7.6
0.1
0.1
6/8 6/8 6/8 6/8 6/9 6/9 6/9 6/9
Thur Thur Thur Thur Fri Fri Fri Fri
2pm 4pm 6pm Com. 7am Bam 9am 10am
7/0 9/2 11/4 24/17
488 387 371 309 313
246 191 238 85.9 145
264 252 222 135 150
207 229 183 82.5 113
806 598 490 516 400
332 142 166 192 174
190 80 52 152 46
110 76 50 128 44
36 23 22 31 14
1.3 0.9 1.2 1.0 1.2
260 174 167 201 150
7.8 6.8 6.9 7.2 6.8
18
0.1 0.1 0.2 0.2 1.0 0.4 0.5
0.1 0.2 0.2 0.3 0.2 0.2 0.2
-------
to
<-" Total Solids
TABLE 1-4
MARLBOROUGH - PHASE III
SECONDARY EFFLUENT (mg/1)
Phase IIIA
Date 5/29 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/31 5/31 5/31 5/31 5/31 5/31
Day Mon Tues Tues Tues Tues Tues Tues Tues Tues Tues Tues Tues Wed Wed Wed Wed Wed Wed
Time Comp 7am Sara 9am 10am 11am noon 2pm 4pm 6pm 9pm Comp 7am Sam 9am 10am 11am noon
Time after shock, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
50.6
46.7
8.4
0.0
266
32
9
3
17.4
15
4.1
116
7.1
0
54.5
54.5
7.2
326
172
15
5
18.9
18
0.1
135
7.3
17
3.8
1
62.3
23.4
6.4
0.4
350
166
11
6
19.0
16
1.8
140
7.0
2.8
2
113
42.8
10.4
1.6
304
20
10
5
18.5
17
1.6
139
7.0
3.0
3
70.0
54.5
9.6
1.6
296
58
8
3
19.5
16
1.5
149
7.0
2.5
4 5
31.1
31.1
8.0
2.8
318
52
6
2
21.7
20
1.5
163
7.1
1.7 0.9
7
62.7
51.0
8.6
3.2
354
88
20
13
23.4
20
1.9
186
7.4
0.2
9
59.5
58.8
9.0
2.3
352
56
25
15
23.5
24
1.5
197
7.4
0.4
11
79.4
47.1
10.0
3.5
332
34
22
13
21.7
19
1.8
199
7.4
1.0
14
71.4
54.9
13.4
2.4
202
22
4
3
19.2
19
2.0
186
7.4
0.4
55.6
47.1
10.2
2.0
332
94
24
16
18
4.0
142
7.1
24/0
79.4
47.1
5.6
1.7
358
92
10
9
17.9
17
1.7
160
7.1
17
1.5
1
67.5
54.9
9.0
3.0
376
150
9
9
19
1.5
166
7.2
1.6
2
60.0
36.0
7.0
2.4
356
106
13
11
18
1.8
163
7.3
2.4
3 i
56. 0
44. 0
7.2
2.4
374
114
5
3
17.2
18
1.7
159
7.3
2.2 1.8
i 5
60.0
40.0
11.2
9.3
438
122
6
5
22
1.8
168
7.2
1.5
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
pH
Temperature , C
Dissolved Oxygen
(continued)
-------
TABLE 1-4 (continued)
C71
Phase
Date
Day
Time
Time after shock, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
PH.
Temperature , C
Dissolved Oxygen
IIIA
5/31 5/31
Wed Wed
2 pm 4 pm
7 9
76.0 72.0
56.0 48.0
13.8 9.0
3.3 2.1
516 538
114 88
43 45
14 11
22 22
1.9 2.0
176 209
7.2 7.3
1.5 0.8
5/31
Wed
6pm
11
64.0
44.0
8.8
2.1
528
72
39
10
22
1.8
207
7.3
0.6
5/31
Wed
10:30
pm
72.0
56.0
10.0
2.1
488
122
42
11
20
2.2
0.4
5/31 6/1
Wed Thur
Comp 7am
24/0
60.0
48.0
8.2
2.1
356
100
7
7
20.2
19
1.5
156
7.1
17
0.8
6/1
Thur
8am
1
64.0
48.0
4.4
1.5
364
182
5
5
20
1.4
157
7.3
1.4
6/1
Thur
9am
2
60.0
68.0
4.0
0.6
378
80
19
18
24
U8
158
7.2
1.3
6/1
Thur
10am
3
68.0
48.0
10.6
0.9
366
86
7
7
20.2
18
1.9
153
7.1
1.8
6/1 6/1
Thur Thur
llam noon
4 5
63.5
43.7
6.8
5.4
350
86
1
1
23
1.8
169
7.0
1.1 0.7
6/1
Thur
2pm
7
55.6
27.8
6.0
5.4
452
180
15
14
23.9
21
1.6
179
7.1
0.2
6/1
Thur
4pm
9
67.5
39.7
6.0
7.2
422
162
3
2
23
2.0
203
7.4
0.2
6/1 6/1
Thur Thur
6 pm Comp
11
55.6 43.4
51.6 43.3
8.0 12.2
8.2 11.6
426 430
102 104
7 11
6 5
22 17
2.2 4.7
205 158
7.2 7.1
0.3
6/2
Fri
7am
24
66.9
63.0
10.4
4.5
406
122
7
5
19
1.8
162
7.2
17
2.0
6/2
Fri
9am
26
2.6
(continued)
-------
TABLE 1-4 (continued)
Phase
Date
Day
Time
Time after shock, hrs
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
fO
V Suspended Solids
to
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
PH
Temperature, C
Dissolved Oxygen
I1IB
6/6
Tues
Comp
51.8
43.8
5.4
0.8
406
60
3
2
18
5.5
193
7.4
6/7
Wed
7am
0
43.8
43.8
2.4
462
182
6
2
18.6
16
2.6
210
7.7
16
1.0
6/7
Wed
Sam
1
39.8
35.9
2.0
0.5
414
102
9
2
17
2.2
194
7.9
1.8
6/7
Wed
9am
2
39.8
39.8
2.8
1.2
426
112
2
1
IS
2.3
191
7.8
2.1
6/7
Wed
10am
3
51.8
51.8
2.8
0.2
428
110
3
2
18.2
17
2.0
198
8,1
1.6
6/7
Wed
noon
5
51.8
43.8
5.6
2.0
418
124
4
3
26
3.0
201
7.8
0.2
6/7
Wed
2pm
7
60.0
48.0
5.0
1.8
418
82
. 4
3
23.1
21
2.0
218
7.5
0.2
6/7
Wed
4pm
9
72.0
52.0
5.2
0.8
408
60
1
1
20
2.3
215
7.9
0.2
6/7
Wed
6pm
11
72.0
52.0
3.8
0.8
388
68
1
1
20
1.6
216
7.7
0.2
6/7 6/8
Wed Thur
Comp 7am
24/0
52 . 0 56.0
40.0 44.0
6.6 2.4
0.2 0.3
420 418
108 204
6 9
2 4
16.9
17 16
6.5 2.3
180 181
7.3 7.7
18
0.7
6/8
Thur
Sam
1
48.0
28.0
3.0
468
264
6
2
15
3.2
174
7.6
1.0
6/8
Thur
9am
2
36. 0
28. 0
3.4
0.8
490
176
2
6
19
3.4
181
7.4
0.9
6/8
Thur
10am
3
40. 0
36.0
8.2
4.4
416
226
4
3
17. 9
22
2. 5
183
7. 5
0.1
6/8
Thur
noon
5
78. 1
46.8
9.0
2.9
446
84
17
7
23
2.0
202
7.5
0.1
6/8 6/8
Thur Thur
2pm 4pm
7/0 9/2
66.4 74.0
39.1 51.0
10.6 8.4
3.9 2.1
478 454
66 40
23 11
10 10
23.8
27 21
1.0 0.9
218 228
7.5 7.4
0.1 0.2
(continued)
-------
Phase
Date
Day
Time
Time after shock, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids 440
Total Volatile Solids 36
Suspended Solids 5
Volatile Susp. Solids 5
Total Kjeldahl-N
Aimnonia-N 19
Nitrate-N 1.7
Alkalinity 226
pH 7.6
Temperature, °C
Dissolved Oxygen 0.2
TABLE 1-4 (continued)
IIIB
6/8 6/8 6/9 6/9 6/9
Thur Thur Fri Fri Fri
6pm Comp 7am Sam
11/4 24/17
58.6 46.8 54.7
54.7 43.0 50.8
8.0 8.2 4.2
2.4 2.0 2.3
366
72
1
0
18
6.0
166
7.0
366
86
5
4
14
1.8
184
7.4
18
0.3
6/9 6/9
Fri Fri
9am 10am 11am
0.1
0.4
1.7 1.1
254
-------
TABLE 1-5
MARLBOROUGH - PHASE III
FINAL EFFLUENT (mg/1)
Phase III A
Date 5/29 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/31 5/31 5/31 5/31 5/31 5/31 5/31
Day Mon Tues Tues Tues Tues Tues Tues Tues Tues Tues Tues Tues Wed Wed Wed Wed Wed Wed Wed
Time
Time after shock, hrs.
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
|sj Total Volatile Solids
Ul
12
0.6
316
62
3
2
2. 8
0.6
19
64
6. 8
0.4
Comp
54.9
47.1
1.1
0.4
390
"142
13
11
0.8
19
56
7.0
7am
24/0
39.2
35.3
2.1
0.7
436
146
15
11
2.2
0.3
18
66
6.9
17
3.0
Bam 9am
1 2
44.0
24.0
2.0
0. 3
408
134
11
9
0.7
20
80
7.0
3.4 3.5
10am
3
36.0
28.0
4.0
0.3
428
202
3
3
2. 1
0.8
18
84
7.1
2.4
11am noon
4 5
40.0
32.0
454
156
7
6
0.6
19
77
6.9
1.9 1.4
2pin
7
47.6
47.6
2.1
0. 5
572
148
42
11
2.0
0.4
18
76
7.0
0. 8
(continued)
-------
Phase
Date
Day
Time
Time after shock, hrs.
COD- Total
COD-Soluble
BOD- Total
Bod-N Suppressed
Total Solids
Total Volatile Solids
K, Suspended Solids
Ul
g^ Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Alkalinity
PH
Temperature
Dissolved Oxygen
TABLE 1-5
(continued)
III A
5/31
Wed
4pm
9
55.6
32.0
4.4
0.5
576
124
45
11
0.1
20
65
6.9
0.3
5/31
Wed
6pm
11
44.0
36.0
12
1.3
582
150
42
13
0.2
20
59
6.4
0.3
5/31 5/31
Wed Wed
10:30 Comp
pm
15>s
40.0 44.0
38.0 32.0
12 2.9
1.2 1.7
568 448
184 224
42 3
13 3
1.0 0.6
20 20
54
6.8
0.4
6/1
Thur
7am
24/0
3.2
0.6
464
146
2
1
2.7
0.2
20
59
6.7
17
2.0
6/1 6/1
Thur Thur
Sam 9am
1 2
32.0
36.0
472
168
30
25
0.2
20
52
6.6
2.1 2.3
6/1 6/1
Thur Thur
10am 11am
3 4
43.7
27.8
10.5
0.9
466
160
9
7
2.2
0.2
20
59
6.5
1.2 0.6
6/1
Thur
noon
5
43.7
39.7
5.0
0.2
416
158
1
1
0.8
20
48
.6.2
0.4
6/1
Thur
2pra
7
43.7
31.7
>10.6
0.2
460
246
5
4
2.4
0.7
22
55
6.6
0.2
6/1
Thur
4pm
9
39.7
31.7
10.0
1.6
404
138
4
3
0.6
22
56
6.5
0.3
6/1
Thur
6pm
11
35.7
31.7
^9.2
1.2
464
170
8
7
1.2
26
56
6.4
0.2
6/1
Thur
Comp
-39.4
35.4
1.1
536
202
13
8
2.7
1. 3
23
57
6.5
6/2
Fri
7am
24
51.2
47.2
-9.2
1.1
532
170
10
9
0.8
25
54
6.5
4.3
6/2 6/6
Fri Tues
9am Comp
26
20.0
1.1
0.9
426
60
8
3
0.5
23
89
7.2
4.9
6/7 6/7
Wed Wed
7am 8am
0 1
35.9
43.8
0.4
500
84
8
2
2.2
0.2
23
104
6.6
16
3.0 4.0
(continued)
-------
Phase
Date
Day
Time
Time after shock, hrs
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Arnmonia-N
Nitrate-N
Alkalinity
pH
Temperature, C
Dissolved Oxygen
TABLE 1-5 (continued)
III B
6/7
Wed
9am
2
39.8
27.9
1.1
510
106
6
4
108
6.7
4.0
6/7
Wed
10 am
3
31.9
27.9
20.3
1.4
476
80
5
4
3.1
0. 3
21
106
7.1
2.4
6/7
Wed
noon
5
31.9
23.9
0.4
476
106
5
4
0.4
26
99
7.1
1.8
6/7
Wed
2pm
7
44.0
44.0
0.7
480
98
2
1
2.7
0.5
26
101
6.9
1.2
6/7
Wed
4pm
9
40.0
36.0
1.3
464
74
2
2
0.3
23
100
6.5
0.6
6/7
Wed
6pm
11
44.0
52.0
2.3
456
48
2
2
0.4
24
99
6.3
0.6
6/7
Wed
Comp
28. 0
16.0
1.6
472
150
5
3
0.5
23
96
6.6
6/8
Thur
7am
24/0
24.0
16.0
3.2
480
140
4
2
1.8
0.2
22
90
6.5
18
4.7
6/8 6/8
Thur Thur
8am 9am
1 2
28.0
12.0
9.0
492
128
8
4
0.5
21
91
6.7
5.2 4.0
6/8
Thur
10am
3
36.0
16.0
434
146
7
4
2.0
0.7
24
89
6.6
3.4
6/8
Thur
noon
5
39.1
27.3
2.0
532
114
16
6
1.0
19
85
6.5
2.5
6/8
Thur
2pm
7/0
35.2
31.3
2.0
536
110
16
6
2.1
0.8
17
83
6.5
1.8
6/8
Thur
4pm
9/2
47.0
43.0
1.9
498
50
8
7
0.8
17
81
6.5
0.2
6/8
Thur
6pm
11/4
54.7
35.2
1.4
488
62
5
5
0. 3
19
80
6.5
0.2
6/8
Thur
Comp
43.0
43.0
1.1
456
106
8
7
2.4
2.4
20
82
6.7
6/9 6/9
Fri Fri
7 arn Sam
24/17
39.1
35.2
426
126
4
4
2. 4
1.2
22
81
6.6
18
2.2 2.5
6/9
Fri
9am
2.5
-------
TABLE 1-6
MARLBOROUGH - PHASE III
MIXED LIQUOR - FIRST STAGE (mg/1)
Phase
Date
Day
Time
Time after shock, hrs,
Total Solids
Total Volatile Solids
Suspended Solids
Volatile SUSP. Solids
pH
Temperature, °C
Cv)
J*J Alkalinity
6.0. Uptake, mg/l-hr.
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
III A
5/30
Tues
7am
0
1460
950
1070
740
6.9
16
210
18.8
6.6
134
20
1.0
190
140
130
120
120
115
110
105
105
5/30
Tues
8am
1
16.5
6.4
190
140
130
130
120
120
115
110
110
5/30
Tues
9am
2
1570
930
1220
890
6.9
206
26.3
4.9
112
19
1.1
180
140
130
120
120
110
110
100
100
5/30
Tues
10am
3
24.8
3.8
180
140
130
120
115
110
105
105
100
5/30
Tues
11am
4
1620
980
1160
820
7.0
237
24.9
3.1
129
24
1.1
180
150
140
130
120
120
115
110
110
5/30
Tues
noon
5
18.6
2.1
190
160
140
130
130
120
110
110
110
5/30
Tues
2pm
7
25.1
3.6
200
170
150
140
130
120
120
120
120
5/30 5/30 5/30
Tues Tues Tues
4pm 6pm 8pm
9 I'l 13
1800
1080
1330
940
6.8
343
22.8 20.8
4.5 5.4 5.2
20
1.3
220 220
170 170
160 150
150 140
140 140
130 130
120
120
110
5/31
Wed
7am
24/0
2070
1350
1620
1180
6.7
16
298
20.3
6.4
151
20
1.3
240
190
170
160
150
145
135
135
130
5/31
Wed
Sam
1
19.9
6.4
210
170
150
140
130
130
120
120
120
5/31
Wed
9am
2
17.5
4.8
210
170
150
140
135
130
120
120
120
5/31
Wed
10am
3
21.6
4.8
230
180
160
150
140
140
130
120
120
5/31
Wed
11am
4
25.0
4.5
230
190
170
160
140
140
130
130
130
5/31
Wed
noon
5
23.6
4.1
250
190
170
165
155
145
140
130
130
5/31
Wed
2pm
7
23.9
3.9
240
185
170
160
150
145
140
130
130
5/31
Wed
4pm
9
1980
1160
1400
1010
6.8
343
22.0
3.1
35
1.1
250
200
180
170
160
150
145
140
130
5/31
Wed
6pm
11
22.2
3.6
250
200
180
170
160
150
(continued)
-------
TABLE 1-6 (continued)
Phase
Date 5/31
Day Wed
Time 10:30
pm
Time after shock, hrs. 15%
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, °c
Alkalinity
10 D.O. Uptake, mg/l-hr
^ Dissolved Oxygen 2.6
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
6/1
Tfiur
7am
24/0
2290
1510
1860
1350
6.8
16
300
22.4
5.4
24
1.4
300
240
210
200
185
170
170
160
155
6/1 6/1
Thur Thur
Bam 9am
1 2
18.9 20.9
5.3 3.8
220 220
185 175
160 160
150 150
140 140
140 135
130 130
130 130
130 120
6/1
Thur
10am
3
24.6
3.3
235
200
170
160
150
145
140
130
130
III
6/1
Thur
11am
4
23.8
2.2
240
200
170
160
155
150
140
130
130
A
6/1
Thur
noon
5
25.5
1.5
260
200
180
170
165
150
140
130
130
6/1
Thur
2pm
7
8.9
3.5
250
210
190
170
160
150
140
140
130
6/1 6/1
Thur Thur
4pm 6pm
9 11
2050
1260
1540
1150
6.9
328
24.9 22.2
4.3 5.3
39
1.7
270 270
210 220
195 200
180 180
170 170
160 160
150
140
140
6/2 6/2
Fri Fri
7am 9am
25 27
2320
1560
1910
1390
7.0
16
220
30.0
7.6 7.5
162
20
1.1
300
240
210
200
190
180
170
160
150
6/7
Wed
7am
0
2250
1260
1830
1160
7.3
16.5
191
17.7
5.2
168
17
1.6
370
210
180
165
160
150
140
130
130
6/7
Wed
Sam
1
19.4
5.4
220
180
150
140
135
130
120
115
115
III B
6/7
Wed
9am
2
24. 7
1.6
230
185
160
150
145
140
130
125
120
6/7
Wed
10am
3
28.9
1.0
235
190
170
160
150
140
135
125
120
6/7
Wed
11am
4
31.9
1.4
240
190
170
155
150
145
130
130
125
(continued)
-------
TABLE 1-6 (continued)
Phase
Date
Day
Time
Time after shock, hrs.
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
PH
Temperature, C
Alkalinity
D.O. Uptake, mg/l-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
III B
6/7
Wed
noon
5
30.0
1.2
240
190
170
160
145
140
130
130
120
6/7
Wed
2pm
7
29.0
3.4
250
200
180
165
160
150
140
135
130
6/7
Wed
4pm
9
2560
1520
2120
1430
6.7
364
28.3
4.1
22
1.3
270
220
190
175
165
160
150
140
140
6/7 6/8
Wed Thur
6pm 7am
11 24/0
1960
1100
1540
960
6.8
17.5
284
27.1 22.6
4.1 6.3
14
1.2
270 285
220 235
185 200
175 185
170 180
160 170
155
150
145
6/8
Thur
Sam
1
22.7
6.1
265
200
160
155
150
150
140
135
130
6/8
Thur
9am
2
34.3
1.5
250
200
180
170
155
•150
135
135
130
6/8
Thur
10am
3
34.8
1.3
270
220
195
170
170
160
150
140
135
6/8
Thur
11am
4
36.7
1.1
280
230
200
180
170
170
155
150
140
6/8
Thur
noon
5
34.4
1.0
270
220
200
190
18'0
170
160
150
150
6/8 6/8
Thur Thur
2pm 3pm
7 8
37.5
1.0 1.4
270
240
210
190
185
175
160
155
150
6/8 6/8
Thur Thur
4pm 6pm
9 11
2510
1420
2020
1060
7.2
353
36.4
1.3 2.2
23
1.4
310
250
225
210
200
190
180
170
160
6/9 6/9
Fri Fri
7am Sam
24 25
3010
1880
2650
1770
7.1
18
300
30.8
4.7 5.1
19
1.3
315
255
225
210
190
185
175
170
160
6/9 6/9 6/9
Fri Fri Fri
"9am lOain 11am
26 27 28
5.2 4.9 4.7
-------
N)
a\
Phase
Date
Day
Time
Time, After Shock, hrs.
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, C
Alkalinity
D.O.Uptake, mg/1-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
TABLE 1-7
MARLBOROUGH - PHASE III
MIXED LIQUOR - SECOND STAGE - FIRST COMPARTMENT (mg/1)
111A
5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/30 5/31 5/31 5/31 5/31 5/31 5/31
Tues Tues Tues Tues Tues Tues Tues Tues Tues Tues Wed Wed Wed Wed Wed Wed
7am 8am 9am 10am llam noon 2pm 4pm 6pm 8pm 7am
0 1 2 3 4 5 7 9 11 13 24/0
2730 2280 2290
1710 1270 1290
8am
1
2300
1500
6.8
17
144
1960
1220
6.7
127
1960
1210
6.4
148
28.4 74.0 57.1 94.7 84.4 74.0 101.9 93.1 81.8
1.2 0.8 0.6 0.3 0.3 0.3 0.2 0.3 0.3
165 123
2.1 6.0 9.0
11 11 9.5
1.2
9am 10am llam noon
2345
2640
1570
2220
1440
6.6
16.5
194
8.0 76.1 78.3 85.7 84.4 85.7
0.3 0.3 0.3 0.3 0.2 0.2
126
3.5
15
(continued)
-------
NJ
Phase
Date
Day
Time
Time After Shock,hrs.
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, C
Alkalinity
D.0.Uptake,mg/1-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
TABLE 1-7 (continued)
IIIA
5/31 5/31 5/31 5/31 6/1 6/1 6/1 6/1 6/1 6/1 6/1 6/1 6/1 6/2
Wed Wed Wed Wed Thur Thur Thur Thur Thur Thur Thur Thur Thur Fri
7am Sam 9am 10am 11am noon 2pm 4pm 6pm 7am
1234579
2280
1300
1870
1230
6.5
2pm 4pm 6pm 10:30
pm
7 9 11 15!s 24/0
80.6
0.2
2540
1400
2030
1300
6.4
148
91.5 78.3
0.2 0.3
2480
1480
2080
1350
6.4
17
141
11.0
0.3 0.4
152
11 24
2810
1660
2290
1420
6.5
17
123
11.0 76.1 78.3 83.1 85.7 83.1 90.0 85.7 81.8 11.1
0.3 0.3 0.3 0.3 0.6 0.3 0.4 0.7 0.5
3.0
13
3.7
17
6.5
8.5
1.4
19
6/2
Fri
9am
26
0.9
(continued)
-------
TABLE 1-7 (continued)
Phase
Date
Day
Time
Time After Shock, hrs
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
PH
Temperature, °c
Alkalinity
D.O.Uptake,mg/l-hr
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
6/7 6/7 6/7 6/7 6/7 6/7
Wed Wed Wed Wed Wed Wed
7am Sam 9am 10am llam noon
012345
2240
1310
1760
1190
6.9
16
122
IIIB
6/7 6/7
Wed Wed
2 pm 4 pm
7 9
1970
1140
1520
1080
6.5
191
6/7 6/8
Wed Thur
6pm 7am
11 24/0
2330
1350
1860
1150
6.5
139
6/8 6/8 6/8 6/8 6/8 6/8
Thur Thur Thur Thur Thur Thur
Sam 9am 10am llam noon 2pm
1 2 3 4, 5 7
7.0 74.0 93.1 78.3 79.4 88.5 100.0 93.1 88.5
0.4 0.4 0.3 0.4 0.4 0.3 0.3 0.2 0 4
140
1.6 4.1
20 15
7.4 69.2 85.7 70.1 70.1 73.0 100.0
0.4 0.4 0.4 0.2 0.2 0.2 0.2
4.5
19
(continued)
-------
TABLE 1-7 (continued)
Phase
Date
Day
Time
Time After Shock, hrs
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, °C
Alkalinity
D.O.Uptake, mg/1 hr
Dissolved Oxygen
Total Kjeldahl-N
Anunonia-N
Nitrate-N
6/8
Thur
3pm
0.4
6/8
Thur
4pm
9
2140
1210
1740
880
6.7
18
164
98.2
1.0
8.5
13
6/8
Thur
6pta
11
0.9
6/9
Fri
7am
24
2240
1350
1760
1200
6. 3
18
128
75.8
0.5
136
1.1
17
IIIB
6/9
Fri
Sam
25
0.5
6/9
Fri
9am
26
6/9
Fri
10am
27
6/9
Fri
11am
28
0.4
0.4
0.4
264
-------
Ul
TABLE 1-8
MARLBOROUGH - PHASE III
MIXED LIQUOR - SECOND STftGE - LAST COMPARTMENT (mg/1)
Phase
Date
Day
Time
Time After Shock, hrs
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
PH
Temperature , C
Alkalinity
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
5/30 5/30 5/30
Tues Tues Tues
7am Bam 9am
012
2600
1610
2210
1480
6.6
17
137
7.3 4.3 1.8
151
1.3
13
230 190 190
170 140 135
150 120 120
140 120 110
130 115 110
130 110 105
130 110 100
120 105 100
120 105 100
5/30 5/30
Tues Tues
10am llam
3 4
2370
1370
2080
1340
6. 5
107
1.2 1.2
129
1.5
14
190 190
140 140
120 120
110 120
110 110
110 110
100 110
100 100
100 100
IIIA
5/30 5/30
Tues Tues
noon 2pm
5 7
1.0 0.5
180 200
140 150
120 120
110 120
110 110
105 110
100 110
100 110
100 110
5/30
Tues
4pm
9
1680
980
1350
900
6.6
147
0.8
2.2
12
190
150
120
110
110
110
110
110
100
5/30 5/30 5/31
Tues Tues Wed
6pm 8pm 7am
11 13 24/0
1890
1130
1430
960
6.6
17
185
1.0 0.3 6.2
1.3
17
200 210
150 155
130 140
120 130
110 125
110 120
120
120
120
5/31
Wed
Bam
1
3.5
190
140
130
120
110
110
110
110
110
5/31
Wed
9am
2
1. 5
190
140
120
110
110
110
110
100
100
5/31
Wed
10am
3
1.2
190
145
120
115
110
110
110
110
110
5/31
Wed
llam
4
1. 5
200
150
130
120
110
110
110
110
110
5/31
Wed
noon
5
1.3
210
150
130
120
120
120
110
110
110
(continued)
-------
TABLE 1-8 (continued)
Phase
Date
Day
Time
Time After Shock, hrs
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp- Solids
pH , • ' *•- '• ' "
Temperature, C
Alkalinity '
K) -Dissolved Oxygen
C\ Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
Illft
5/31
Wed
2pm
7
'
0.8
200
145
120
120
110
110
110
105
105
5/31
Wed
4pm
9
2460
1420
1930
1310
6-. 5
130
0.6
2.7
15
190
145
120
115
110
110
110
105
105
5/31 5/31 6/1
Wed Wed Thur
6pm 10:30 7am
pm
11 15*5 24
2258
1350
1840
1200
6^5-
17
1*9
1.2 1.3 5.7
1.1
17
195 220
145 160
130 140
120 130
110 120
110 120
120
120
120
6/1
Thur
Sam
1
2.0
190
140
120
120
115
110
105
105
105
6/1
Thur
9am
26
1.1
190
135
115
110
105
105
100
100
100
6/1
Thur
10am
3
1.2
180
330
110
105
100
100
100
100
100
6/1
Thur
llam
4
1.5
180
130
110
105
100
100
100
100
100
6/1
Thur
noon
5
1.2
190
130
110
105
100
100
100
100
100
6/1
Thur
2pm
7
1.3
190
145
130
120
115
110
110
110
110
6/1 6/1
Thur Thur
4pm 6pm
9 11
2280
1340
1870
1170
1.2 1.3
3.6
8.8
200 190
J',0 140
120 120
110 115
110 110
110 110
110
100
100
6/2
Fri
7am
25
2480
1510
1990
1370
6.5
17
118
6.7 .
0.5
20
220
160
135
135
130
125
120
120
120
f/2
Fri
9am
27
3.3
(continued)
-------
K)
-J
Phase
Date
Day
Time
Time After Shock, hrs
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
pH
Temperature, C
Alkalinity
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
Nitrate-^
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
TABLE 1-8 (continued)
IIIB
6/7
Wed
7am
0
2120
1250
1650
1130
6.8
16
150
7.0
0,9
21
, 6/7
Wed
Sam
1
2.0
6/7 6/7 6/7 6/7
Wed Wed Wed Wed
9am 10am llam noon
1.2 1.3
1.6
1.4
6/7
Wed
2pm
7
1.2
6/7
Wed
4pm
9
2280
1880
2360
1820
6.7
164
1.3
2,2
15
6/7 6/8
Wed Thur
6pm 7am
11 24/0
1620
890
1200
730
6.4
17.5
141
1.3 7.5
120
0.8
20
6/8
Thur
Sam
1
4.0
9am 10am llam noon
2345
2pm
1.
2.9
2.1
1.6
1.4
215 ,190 195 190 185 180 195 190 200 215 190 195 190 185 ISO 195
160 160 140 135 135 135 140 140 190 160 160 140 135 135 135 140
135 120 120 120 120 120 120 125 120 135 120 120 120 120 120 120
130 115 115 110 120. 115 120 120 120 130 115 115 110 120 115 120
120 110 115 110 110 110 120 115 115 120 110 115 110 110 110 120
120 110 110 110 110 110 115 115 110 120 110 110 110 110 110 115
120 110 110 110 110 110 110 115 120 110 110 110 110 110 110
120 110 110 110 110 110 110 110 120 110 110 110 110 110 110
120 110 110 110 110 110 110 110 120 110 110 110 110 110 110
(continued)
-------
TABLE 1-8 (continued)
Phase
Date
Day
Time
Time After Shock, hrs
Total Solids
Total Volatile Solidr
Suspended Solids
Volatile Susp. Solids
pH
Temperature, C
Alkalinity
Dissolved Oxygen
Total Kjeldahl-N
Ammonia-N
ISH i_rate-N
Settlometer
5 minutes
10 minutes
15 minutes
2C minutes
25 minutes
30 minutes
40 minutes
50 minutes
60 minutes
6/8 6/8
Thur Thur
3 pm 4 pm
8 9
2160
1210
1750
870
6.7
18
135
0.9 1.0
1.7
14
190
140
125
120
115
115
115
110
110
IIIB
6/8 6/9 6/9
Thur Fri Pri
6pm 7am Sam
11 24 25
2350
1410
1940
1320
6.4
18
124
1.3 5.0 3.0
127
0.3
17
130
130
120
120
120
120
110
110
110
6/9 6/9 6/9
Fri Fri Pri
9am li'Jam 11am
26 27 28
1.6 1.5 17
268
-------
APPENDIX J
TABLE J-l
MARLBOROUGH - PHASES I, II AND III - SLUDGES WASTED
Phase I
Date 4/17 4/18 4/19 4/20 4/21 4/22 4/23 4/24 4/25 4/26 4/27 4/28 4/29 4/30 5/1 5/2 5/3
Day Mon Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Fri Sat Sun Mon Tues Wed
Sludge Wasted
First Stage, 103 liters 746 15 386 454 454 28B 496 416 295 344 322 435 238 276 363 432 367
(103 gals) (197) (4) (102) (120) (120) (76) (131) (110) (78) (91) (85) (115) (63) (73) (96) (114) (97)
Sludge to
Vacuum Filter, 103liters 84 105 74 110 98 83 69 73 138 95 78
Cn (1° gals) (22.1) (27.8) (19.6) (29.1) (26.0) (22.0) (18.1) (19.4 ) (36.5) (25.2) (20.5)
ID
Phase j- 11 A I1B
Date 5/4 5/5 5/6 5/7 5/8 5/9 5/10 5/11 5/12 5/15 5/16 5/17 5/18 5/19 5/20
Day Thur Fri Sat Sun Mon Tues Wed Thur Fri Mon Tues Wed Thur Fri Sat
Sludge Wasted
First Stage, 103 liters 405 439 432 477 454 568 341 318 318 318 318 318 318 337 348
(103 gals) (107) (116) (114) (126) (120) (150) (90) (84) (84) (84) (84) (84) (84) (89) (92)
Sludge to
Vacuum Filter, 103 liters 96 84 100 134 116 105 84 101 86 88 100 79
(103 gals) (25.4)(22.2) (26.4) (35.4) (30.7) (27.7) (22.3) ( 26 . 7) (22.8) (23.3) (26.4) (20.8)
(continued)
-------
to
-J
o
TABLE J-l (continued)
Phase I IB IIIA
Date 5/21 5/22 5/30 5/31 6/1 6/2 6/3 6/4 6/5 6/6 6/7 6/8 6/9
Day Sun Mon Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Fri
Sludge Wasted
First Stage, 103 liters 473 428 295 273 318 341 318 318 363 318 337 295 375
(10 gals) (125) (113) (78) (72) (84) (90) (84) (84) (96) (84) (89) (78) (99)
Sludge to
'ilter,
(103 gals) (28.0) (20.7)(21.2)(30.0)(20.9) (34.2)(26.3)(19.5) (23.2)
Vacuum Filter, 103 liters 106 78 80 114 79 130 100 74 88
-------
to
-J
I-1
TABLE J-2
MARLBOROUGH - PHASE I, II AND III
SLUDGE QUANTITIES WASTED
Phase
Date
Day
Sludge Wasted
First Stage
1000 liters
1000 gals
Sludge to
Vacuum Filter
1000 liters
1000 gals
Phase
Date
Day
Sludge Wasted
First Stage
1000 liters
1000 gals
Sludge to
Vacuum Filter
1000 liters
4/17 4/18
Mon Tues
746 15
197 4
84
22.1
5/8 5/9
Mon Tues
454 568
120 150
100 134
4/19
Wed
386
102
1 1 A
5/10
Wed
341
90
116
4/20
Thur
454
120
105
27.8
4/21 4/22
Fri Sat
454 288
120 76
74
19.6
I
4/23 4/24 4/25 4/26 4/27 4/28 4/29 4/30 5/1
Sun Mon Tues Wed Thur Fri Sat Sun Mon
496 416 295 344 322 435 238 276 363
131 110 78 91 85 115 63 73 96
110 98 83 69 73 138
29.1 26.0 22.0 18.1 19.4 36.5
5/2
Tues
432
114
95
25.2
5/3
Wed
367
97
78
20.5
5/4
Thur
405
107
96
25.4
5/5
Fri
439
116
84
22.2
5/6 5/7
Sat Sun
432 477
114 126
IIB
5/11
Thur
318
84
105
5/12
Fri
318
84
84
5/15 5/16
Mon Tues
318 318
84 84
101 86
5/17
Wed
318
84
88
5/18
Thur
318
84
100
5/19
Fri
337
89
79
5/20
Sat
348
92
5/21 5/22
Sun Mon
473 428
125 113
106
1000 gals
26.4 35.4 30.7 27.7 22.3
26.7 22.8 23.3 26.4 20.8
28.0
(continued)
-------
TABLE
Phase
Date
Day
Sludge Wasted
First Staqe
1000 liters
1000 gals
Sludge to
Vacuum Filter
1000 liters
J-2 (continued)
IIIA
5/30
Tues
295
78
78
5/31
Wed
273
72
80
6/1
Thur
318
84
114
6/2 6/3
Fri Sat
341 318
90 84
79
6/4 6/5
Sun Mon
318 363
84 96
130
IIIB
6/6
Tues
318
84
100
6/7
Wed
337
89
74
6/8
Thur
295
78
88
6/9
Fri
375
99
1000 gals
20.7 21.2 30.0 20.9
34.2 26.3 19.5 23.2
Phase
Date
Day
TABLE J-3
MARLBOROUGH - PHASE I, II AND 1 I - SLUDGES WASTED
IIIA
5/30 5/31 6/1 6/2 6/7 6/8 6/9
Tues Wed Thur Fri Wed Thur Fri
3470 3110 4290
2060 1810 2680
2940 2660 2870
1840 1600 2520
28 18 14
2.0 2.0 1.0
9.1 11.1 13.6
0.08 0.09 0.07
(1.8) (2.0) (1.5)
3110 3620
1890 2200
2640 3150
1690 2060
Sludge Returned to First Stage Aeration
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
2550
1730
2080
1460
213
23
1.0
Capillary Suction Test, sec 14.9
Return Rate, cu m/sec
mgd
Sludge Returned to Second
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Capillary Suction Test, sec
Return Rate, cu m/sec
mgd
0.07
(1.6)
2660
1770
2180
1570
24
1.5
11.6
0.07
(1.6)
2740
1840
2280
1670
24
1.0
14.4
0.07
(1.7)
2240
1480
1770
1370
230
21
2.1
10.8
0. 07
(1.8)
Stage Aeration
3580
2120
3120
1910
210
3.0
10
5.9
0.09
(2.1)
3720
2160
3340
2090
8.5
14
7.3
0.09
(2.0)
3280
2600
2830
2450
3.0
16
5.7
0.11
(2.4)
2080
1180
1600
1040
2.0
19
6.4
0.11
(2.4)
4.0 1.0
18 17
5.3 5.7
2.0
17
5.7
0.07 0.07 0.09
(1.5) (1.6) (2.0)
272
-------
TABLE J-4
VARIATION OF SOLIDS CONCENTRATION WITH DEPTH IN THE PRIMARY CLARIFIER DURING SHOCK LOADING - PHASE III
TOTAL SOLIDS (mg/1)
Phase
Date
Tim$
7 am Shock
7:30 am
8 am
8: 30 am
9 am
10 am
11 am
12 noon
2 pm Shock
2:15 pm
3:15 pro
4 pm
6 pm
Time
7 am Shock
7:30 am
8 am
8:30 am
9 am
10 am
11 am
12 noon
2 pm Shock
2:15 pm
3:15 pm
4 pm
6 pm
IIIB
6/8
Top
(1 ft. below surface)
544
436
482
707
870
728
672
700
682
Top
(1 ft. below surface)
142
110
176
364
360
252
272
192
200
Middle
(5 ft. below surface)
532
544
914
962
892
848
668
716
704
TOTAL VOLATILE
Middle
(5 ft. below surface)
136
188
452
422
384
406
222
206
264
Bottom
(10 ft. below surface)
386
1204
1088
1506
996
956
732
1436
838
SOLIDS (mg/1)
Bottom
(10 ft. below surface)
86
690
610
842
456
468
292
700
264
Effluent
(in trough)
470
476
668
962
970
842
918
722
806
598
490
Effluent
(in trough)
230
238
420
600
588
526
452
316
332
142
166
273
-------
N)
Date
Day
Flow Rate, gpd
COD-Total
COD-Soluble
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
Temperature, C
Dissolved Oxygen
APPENDIX -K
TftBtE K-l
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION - PHASE I
INFLUENT (mg/1)
3/12
Sun
0400
467
616
316
90
76
30.5
8.0
1.5
88
7.2
3/13
Mon
28800
356
514
274
126
122
7.5
1.6
18
118
7.1
15
7.4
3/14
Tues
28800
286
450
188
173
143
22.7
12.0
1.4
89
7.0
16
6.6
3/15
Wed
26600
217
384
122
82
67
12.0
0.8
8.0
97
6.6
14
8.5
3/16
Thur
27900
316
560
190
358
192
24.2
14.0
1.0
128
6.8
17
6.9
3/17
Fri
28800
257
706
182
156
102
17.0
1.0
116
6.6
14
7.6
3/18
Sat
28800
87
574
192
108
84
8.9
1.0
127
6.7
3/19
Sun
28800
107
402
108
60
32
11.5
4.3
1.1
97
6.8
3/20
Mon
28800
125
55
95
380
116
49
48
4.8
0.8
4.5
108
6.6
13
3.4
3/21
Tues
28800
136
66
376
166
8.3
4.0
1.5
61
6.9
13
7.6
3/22
Wed
28800
128
400
176
43
38
4.2
0.9
3.5
129
6.8
12
9.8
3/23
Thur
28800
108
410
106
68
10.1
4.3
2.6
124
6.7
14
8.4
3/24
Fri
28800
102
57
4.3
2.2
110
6.5
13
7.6
3/25
Sat
28800
129
380
70
18
11
7.0
1.6
118
6.8
3/26
Sun
28800
282
434
176
152
126
17.9
8.1
1.2
92
6.8
3/27
Mon
34600
214
380
150
105
87
6.5
1.5
2.5
103
6.6
6
8.0
3/28
Tues
33100
174
59
368
92
85
62
19.3
11.0
1.5
133
7.2
15
7.5
-------
Ul
Date
Day
COD-Total
COD-Soluble
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
Alkalinity
pH
Temperature,°C
Dissolved Oxygen
TABLE K-2
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION-PHASE I
SECONDARY EFFLUENT (mg/1)
3/12
Sun
73
430
112
21
14
3.6
2.3
12.0
18
6.7
3/13
Mon
54
350
138
7
1
2.1
12.5
2.1
28
6.5
12
3/14
Tues
53
32.0
86
16
15
8.1
6.0
6.5
52
6.6
11
3.5
3/15
Wed
57
334
80
9
5
9.0
7.4
2.8
83
6.9
11
2.3
3/16
Thur
53
61
500
142
3
2
9.6
8.2
5.5
95
7.0
12
0.8
3/17
Fri
56
580
70
2
0
3.2
7.5
61
6.8
12
0.4
3/18 3/19
Sat Sun
32
24
402
96
12
5
2.4
0.0
9.8
61
6.7
3/20
Mon
43
43
5.5
346
76
5
4
0.0
8.0
1.9
61
6.8
10
1.9
3/21
Tues
35
31
3.5
302
100
3
3
1.3
0.2
7.5
95
6.8
10
2.1
3/22
Wed
54
43
338
130
4
4
.1
8.5
2.1
70
6.8
10
4.8
3/23
Thur
31
31
408
102
13
.1
7.5
75
6.8
10
4.3
3/24
Fri
31
3.0
344
56
9
8
.1
7.3
88
6.6
10
4.8
3/25 3/26
Sat Sun
43 31
304
42
8
5
1.4
.1 .1
8.0 9.0
62 56
6.3 6.5
3/27
Mon
31
31
277
86
12
12
1.0
10
1.6
53
6.7
9
5.8
3/28
Tues
116
47
450
140
85
62
8.7
2.0
12
62
6.8
11
1.9
-------
TABLE K-3
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
PHASE I - MIXED LIQUOR (mg/1)
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Alkalinity
pH
Temperature, °C
D.O. Uptake, mg/1- hr
Dissolved Oxygen, mg/1
•^J Location A nr. Surface
A nr. Bottom
B nr. Surface
B nr. Bottom
C nr. Surface
C nr. Bottom
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
3/13
Mon
2100
1460
2280
1780
49
6.8
12
26
6.0
5.8
5.9
5.8
6.8
6.7
171
3.1
11
960
910
840
780
700
650
460
3/14
Tues
2150
1590
1970
1590
48
6.6
12
18
5.8
5.5
5.5
5.2
6.9
6.7
2.5
13
960
900
850
780
720
660
540
460
3/15
Wed
2040
1430
3090
2610
74
6.6
12
63
2.8
2.6
2.5
2.4
4.6
4.6
146
8.0
5.8
950
870
780
710
670
620
500
440
3/16
Thur
2300
1660
2370
1830
100
6.8
12
40
3.7
3.4
3.9
3.4
1.6
1.0
9.0
7.0
960
910
850
790
740
680
570
480
3/17
Fri
2428
1658
1950
1500
106
6.7
12
19
2.7
2.6
2'. 7
2.5
0.8
0.5
168
8.8
6.5
960
920
880
840
780
740
610
540
3/20
Mon
2618
1824
2560
1880
96
6.6
11
23
2.7
2.6
2.8
2.6
4.8
4.9
182
0.0
9.8
980-1
950
900
860
830
790
670
590
3/21
Tues
2518
1730
2490
1930
94
6.5
11
22
2.1
2.1
2.3
1.8
4.2
4.1
0.7
8.5
980
910
810
770
730
600
540
3/22
Wed
2766
2004
78
6.6
11
20
4.9
4.6
4.5
4.4
7.2
6.7
193
0.2
8.5
'960
910
860
800
740
700
560
500
3/23
Thur
2622
1842
2520
2030
104
6.7
12
29
3.1
2.7
2.7
2.5
6.1
5.9
0.2
9.5
950
900
840
780
730
680
570
490
3/24 3/25
Fri Sat
2392
2360 2380
1780
101
6.5
12
20
3.3
3.2
2.9
2.7
6. 0
5.8
171
0.2
8.8
950
860
770
730
680
630
520
460
3/26 3/27
Sun Mon
2692
1898
2540 2575
1910 1930
91
6.6
9
30
2.6
2.6
6.1
6.1
7 .1
7.1
171
0.1
9.8
900
800
710
650
600
560
480
430
3/28
Tues
2608
1846
2470
1950
106
6.7
12
37
0.8
0.7
0.8
0.8
3.3
3.2
2.5
9.0
900
810
740
670
600
550
450
400
-------
APPENDIX L
TABLE L-l
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
PHASE II - SEPTAGE (my/I)
K)
Date
Day
Septage Volume, gpd
% of Daily Flow
COD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Total Phosphorus
Alkalinity
PH
Nitrate-N
3/29
Wed
123
0.43
22090
4500
6810
5140
1800
570
448
145
650
7.1
3/30
Thur
194
0.62
10030
5720
4720
1780
1290
105
210
7. 2
3/31 4/1
Fri Sat
110 137
0. 38 0.48
16800
3900
6690 3680
5510 3060
1850 2510
1100 2420
342
46
80
250
7.6
4/2 4/3 4/4
Sun Mon Tues
0 132 194
0 0.46 0.67
33010 33780
5320
3780
2720
950
330
116
96
276
6.9
4/5
Wed
123
0.43
5620
3462
2600
2310
1760
246
75
334
7.2
4/6
Thur
106
0.41
5300
3530
2720
2640
2130
60
86
269
7.4
4/7
Fri
115
0.40
6270
2740
2120
1950
1660
280
54
4/8
Sat
97
0.34
1880
1480
970
990
760
27
259
7.1
4/9
Sun
106
0. 37
1600
1290
820
780
520
27
245
7.2
4/10
Mon
264
0.92
1310
660
970
500
480
320
109
24
7.3
0.8
4/11
Tues
247
0.96
17760
17260
12070
15720
11040
110
123
613
6.1
4/12
Wed
216
0.78
11220
1950
3960
3020
2760
2270
263
80
566
7.0
4/13
Thur
203
0.67
8590
4530
3570
3060
2520
68
102
273
6.8
4/14
Fri
45490
41770
29410
39230
28830
666
1.6
1332
6.1
0.0
4/15
Sat
159
0.69
34630
5960
4840
3900
3360
213
760
6.3
4/16 4/17
Sun won
229
0. 86
11480 11280
6100 6670
5140 5340
4170 4910
3740 4040
426
188 138
706 500
6.6 7.3
-------
TABLE L-2
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
PHASE II - INFLUENT (mg/1)
Date 3/29 3/30 3/31 4/3 4/4 4/5 4/6 4/7 4/8 4/9 4/10 4/11 4/12 4/13 4/14 4/15 4/16 4/17
Day Wed Thur Fri Mon Tues Wed Thur Fri Sat Sun Mon Tues Wed Thur Fri Sat Sun MOn
Flow Rate, gpd 28800 31400 28800 28800 28800 28800 25600 28800 28800 28800 28800 25600 27600 30100 28800 23000 26600
COD-Total 170 218 239 227 248 216 200 168 379 468 324 295 176 192 191 82 436
COD-Soluble
BOD-N Suppressed
Total Solids
Total Volatile Solids 138
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
NJ
*-J Ammonia-N
CO
Nitrate-N
Total Phosphorus
Alkalinity
pH
Temperature, °C
Dissolved Oxygen
478
138
10
1.3
125
6. 8
15
7.2
170
336
94
45
42
22.4
13
1.2
4. 1
136
7.3
15
6.6
99
466 488
192 194
50 62
37 54
13
1.0
8.0
150
6.9
16
6.3
458
240
78
72
22.4
14.5
0.9
138
6.8
15
6.7
402
202
74
64
15
0.7
4. 8
138
6.8
16
6. 3
414
160
62
60
23.8
11.5
1.0
143
1,6
17
5.9
442
158
61
54
11
1.4
140
6.6
498
230
83
69
12
1.5
132
6. 7
149
620
296
186
168
6.0
2.0
115
6. 7
456
186
102
86
22
4.5
4.3
140
6.8
17
5.4
71
388
136
84
68
21.8
8.0
3.5
104
6.6
17
5.2
486
218
72
68
10
2.7
4.0
127
6.8
16
5.9
392
110
54
50
18.5
20
3.5
85
5.8
18
5.4
450
140
50
40
9.5
0. 7
142
6.7
18
5.8
336
118
10
6
11
0.8
130
6.6
12
7.6
482
216
92
76
30.8
10
1. 8
105
6. 8
15 16
4-4 5.0
-------
TABLE L-3
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
- PHASE II
EFFLUENT (mg/1)
Date
Day
Septage/Sewage, %
COD- Total
COD-Soluble
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
M
^j Ammonia-N
Nitrate-N
Total Phosphorus
Alkalinity
pH
Temperature, °C
Dissolved Oxygen
3/29
Wed
0.43
23.7
19.8
460
116
10
8
1. 3
11.0
54
6.7
12
0.9
3/30
Thur
0.62
35.7
27.8
6.6
316
58
1
1
2.5
1.8
10.0
2.0
61
7.2
12
0.9
3/31 4/3
Fri Mon
0.38 0.46
46.3 38.6
30.9
1.7
380 368
64 126
4 2
2
1.2
9.5
2.9
68
6. 8
13
0. 3
4/4
Tues
0.67
34.9
15.5
338
112
4
4
2.0
1.4
9.5
65
6.8
12
0.3
4/5
Wed
0.43
31.5
27.6
316
130
10
9
1.3
7.5
2.7
74
6.6
12
0.3
4/6
Thur
0.41
27.5
15.7
342
90
3
3
1.7
1.2
7.8
69
6.7
13
0.2
4/7
Fri
0. 40
19.5
330
72
1
1
1.1
8.5
54
6.3
13
0.3
4/8 4/9
Sat Sun
0.34 0.37
19.5 23.4
19.5
1.7
360 358
82 68
4 2
2 2
1.5
1.8 0.8
12.0 10.5
61 64
6.7 6.7
4/10
Mon
0.92
34.7
27.0
382
96
12
9
1.5
7.5
2.9
71
6.6
14
0.2
4/11
Tuea
0.96
47.2
23.6
3.7
314
54
11
9
2.7
1.2
8.0
65
6.6
13
0.4
4/12
Wed
0.78
31.2
27,. 3
358
86
7
7
1.4
5.0
2.9
65
6.6
14
0.3
4/13
Thur
0.67
78.4
27.5
342
78
28
26
4.3
0.8
4.4
60
6.5
14
0.1
4/14
Fri
230
31.1
542
208
68
62
2.9
2.6
14
0.2
4/15
Sat
0.69
31.1
19.5
336
86
1
1
2.0
6.0
75
6.7
13
1.6
4/16 4/17
Sun
0.86
432
13.3
598
304
238
222
1.3
5. 0
99
6.8
12 13
0.3 0.3
-------
TABLE L-4
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION - PHASE II
MIXED LIQUOR (mg/1)
Date
Day
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Alkalinity
PH
Temperature, °C
D.O. Uptake, mg/l-hr
ISJ
Dissolved Oxygen
Location A nr. surface
A" nr . bottom
B nr. surface
B nr. bottom
C nr . surface
C nr. bottom
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
3/29
Wed
2610
1820
1740
1350
110
6.8
13
32
0.6
0.5
0.6
0.4
2.3
1.9
196
2.2
11.0
880
790
700
620
510
420
390
3/30
Thur
2800
1930
2950
2260
130
6.6
13
36
0.9
0.7
0.8
0.7
4.1
3.5
1.4
10.0
940
850
780
710
650
590
480
420
3/31
Fri
2630
1890
2930
2380
112
6.6
13
38
1.0
0.6
0.8
0.7
0.6
0.5
224
3.6
8.0
910
810
730
680
620
580
470
420
4/4
Tues
3680
2800
3480
2780
157
6.8
13
41
1.0
0.7
0.9
0.8
0. 5
0.3
1.5
9.5
950
900
850
820
790
740
620
540
4/5
Wed
3380
2650
3510
2890
127
6.7
13
27
1.8
1.1
1.4
1. 3
0.4
0.4
252
2.5
6.5
970
920
870
830
790
750
640
570
4/6
Thur
3420
2660
3080
2540
139
6.7
14
48
0.9
0.9
1.1
1.2
0.3
0.3
1.5
5.8
980
940
910
870
840
810
680
610
4/7 4/8
Fri Sat
3730 3350
2860 2730
3280 2760
2710 2060
29 168
6.0 6.2
14
31
1.4
1.2
1.4
1.2
0.4
0.3
288
2.8 3.7
8.5 0.9
980
950
920
880
830
700
650
4/9 4/10
Sun Mon
3510 3440
2660 2620
3340 3040
2700 2500
190 100
6.4 6.2
14
24
0.9
0.8
1.1
0.9
0.2
0.2
244
2.1 3.6
1.2 2.9
980
950
930
900
880
780
730
4/11
Tues
3458
2695
3140
2617
101
6.2
14
67
0.7
0.5
1.0
0.8
0.8
0.4
1.6
7.5
990
950
920
900
880
860
800
740
4/12
Wed
3812
2956
3526
2924
145
6.7
D4
27
2.0
1.8
2.2
2.2
0.4
0.3
246
2.0
4.0
980
960
940
920
900
850
800
4/13
Thur
3300
2560
2950
2470
141
6.4
15
55
0.7
0.6
0.8
0.7
0.2
0.2
1.5
4.2
4/14
Fri
3230
2490
2930
2220
185
6.7
15
0.8
0.7
0.8
0.6
0.4
0.2
190
1. 3
1.9
980
950
930
900
880
820
760
4/15
Sat
3036
2262
2582
2158
161
6.4
15
7 . 6
7.4
7.4
7.3
4.0
3.9
5.0
0.8
4/16 4/1S
Sun Sun
@9am ?5pm
2732
2082
2544
1866
187
6.5
14
1.5 4.8
0.9 4.8
0.6 4.8
0.2 4.5
0.3 1.4
0.2 1.0
3.2
2.2
4/17
Mon
2536
1926
2266
1890
138
6.5
14
2.4
2.2
2. 1
2.1
0.6
0.3
202
0.5
5.5
950
910
880
850
820
750
680
-------
APPENDIX M
TABLE M-l
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
SEPTAGE (mg/1)
Date
Day
Volume, gal
Loading Time
COD-Total
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Amraonia-rN
Total Phosphorous
pH
Alkalinity
% of Flow
- PHASE III
5/3
Wed
300
Sam
10395
1200
5888
4688
4522
3820
367
78
6.19
896
r. 04
5/4
Thur
300
Bam
14570
2035
2030
4440
3504
2976
2584
357
170
52
6.23
790
1.04
5/5
Fri
300
Sam
45800
9600
8775
12824
10580
11132
9416
974
360
370
5.81
1580
1.04
5/18
Thur
600
Sam
26587
6188
6188
6198
4802
4364
3554
661
120
187.5
5.58
490
2.08
5/19
Fri
450
9am
11111
4672
3428
2978
2430
319
475
5.78
310
1.56
281
-------
TABLE M-2
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
INFLUENT (mg/1)
- PHASE III
Date
Day
Flow Rate, gpm
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Anunonia-N
Nitrate-N
Total Phosphorous
pH
Temperature, C
Alkalinity
5/3
Wed
20
600
138
154
121
440
190
118
110
26.6
16.5
0.44
6.5
19.0
148
5/4
Thur
20
219
106
89
61
390
144
31
27
24.9
15.0
1.00
6.88
19.5
137
5/5
Fri
20
428
80
90
86
516
326
103
102
33.9
16.0
0.50
6.75
7.02
19.0
148
5/6 5/7
Sat Sun
20 20
266
48
118
90
486
254
118
110
24.6
14.0 12.0
1.05 0.90
4.0
7.15
15.0 17.0
129 130
5/18
Thur
177
79
97
90
404
154
92
72
18.8
3.0
1.8
6.74
18.0
106
5/19
Pri
274
91
420
126
90
62
30.0
17.0
0.85
5.3
6.90
17.0
138
5/20
Sat
211
76
76
38
358
108
78
66
22.1
8.5
0.75
4.3
6.84
17.0
140
5/21
Sun
163
91
58
340
170
28
18
19.3
15.0
1.0
4.2
6.70
20.0
152
282
-------
to
CO
OJ
Date
Day
Time
Time After Shock, hrs
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
pH
Temperature, C
Alkalinity
5/3
Wed
Sam
0
32
Comp
400
Comp
174
Comp
114
Comp
104
0.26
9.00
6.75
14
67
TABLE M-3
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION
PHASE III - EFFLUENT (mg/1)
5/3 5/3 5/3 5/3 5/3 5/4 5/4 5/4 5/4 5/4 5/4 5/5 5/5
Wed Wed Wed Wed Wed Thur Thur Thur Thur Thur Thur Fri Fri
9am 10am 11am noon 2pm Sam 9am 10am 11am noon 2pm Bam 9am
2346
47 1272 1272 1040
39 43 39 63
6 503 945 485
1 203 180 128
12346 24/0 1
51 87 59 79 121 51 47
36 35 28 20 24 23 39
10 19 20 22 20 9 4
6 12 11 15 18 1 1
294 308 330 340 398 288 252 306 992 1194 882
126 162 160 154 206 112 92 84 630 876 566
4 15 11 40 60 15 1.5 3 640 896 800
3 13 10 37 56 13 0.5 1 592 768 708
2.9 9.4 10.4 11.6 10.6 1.5 1.0 4.6 71.7 74.5 56.6
1.45 5.00 8.50 7.50 6.00 0.45 0.24 2.20 4.90 5.00 5.25
7.50 5.00 3.00 2.40 2.00 1.80 1.60 1.00 0.65 0.85 0.70
0.6 0.8 1.8 15.5 18.5
6.80 6.97 7.18 7.06 6.73 7.04 7.02 7.06 6.98 7.02 6.90
15 15 16 17 15 15.5 1" 15..5 16 17
77 96 104 104 104 97 89 99 129 121 122
24/0
116
24
112
14
1
16
12
74
a
472 372
198 174
136 56
108 46
13.0 8.7
2.2 1.1
1.70 2.50
13.0 1.3
6.72 6.76
16 16
93 87
5/5
Fri
10am
2
68
24
62
40
298
94
25
3
6.4
2.0
0.78
4.3
6.91
16
98
5/5
Fri
11am
3
52
40
22
10
306
130
12
10
8.8
3.2
0. 55
10.3
6.88
15.5
91
5/5 5/5 5/6
Fri Fri Sat
noon 2pm Sam
4 6 24
416 1240 369
20 24 32
21 443 165
12 375 47
288 1202 450
92 884 218
16 872 232
3 700 198
40.0 58.2 22.7
2.8 7.1 6.0
0 . 81) 0.62 0.95
4.0 16.5 4.3
7.00 6.77 7.12
15.5 16 15
108 116 105
(continued)
-------
TABLE M-3 (continued)
N3
00
Date
Day
Time
Time After Shock, hrs
COD-Total
COD-Soluble
BOD-Total
BOD-N Suppressed
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
Ammonia-N
Nitrate-N
Total Phosphorous
PH
Temperature, °C
Alkalinity
5/18
Thur
Bam
0
83
59
75
28
398
130
52
46
14.6
10.0
5.0
4.0
6.80
16.0
102
5/18
Thur
9am
1
551
39
285
123
832
462
264
188
41.4
9.0
2.0
7.5
6.96
16.0
106
5/18
Thur
10am
2
976
51
390
171
1052
468
816
392
42.6
11.5
1.4
10.5
6.77
120
5/18
Thur
11am
3
658
51
336
204
726
400
371
300
33.6
14.0
0.95
7.8
6.90
132
5/18
Thur
noon
4
390
51
258
147
516
262
212
168
28.6
13.5
0.95
9.5
6.90
17.0
127
5/18
Thur
2pm
6
389
83
426
198
462
198
416
184
34.7
12.5
1.0
6.5
17.0
5/19
Fri
7am
23/0
123
44
52
20
390
58
66
44
13.3
11.0
1.50
1.0
6.86
16.0
119
5/19
Fri
10am
1
643
64
300
120
846
452
500
352
19.6
14.5
0.90
7.0
6.60
17.0
133
5/19
Fri
11am
2
1659
95
540
158
836
468
513
373
25.5
20.0
0.95
12.0
6.80
18.0
150
5/19
Pri
noon
3
921
52
413
150
870
504
513
387
21.8
16.0
0.70
8.3
6.87
18.0
153
5/19
Fri
1pm
4
246
64
323
68
758
412
413
307
15.4
18.0
0.65
11.3
6.92
146
5/19
Fri
3pm
6
389
60
188
558
.238
252
184
15.4
15.0
0.85
5.0
6.78
19.0
141
5/20
Sat
Sam
23
622
56
180
113
768
410
432
66
36.1
14.0
0.95
7.3
6.80
17.0
134
5/21
Sun
Sam
47
219
32
165
520
342
248
224
98
4.5
6.70
18.0
129
-------
TABLE M-4
UNIVERSITY OF LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION - PHASE III
MIXED LIQUOR (mg/1)
Date
Day
Time
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
K) ' PH
00 o
Ul Temperature, C
Alkalinity
D.O. Uptake, mg/l-hr.
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
5/2 5/3
Tues Wed.
Sam Sam
2020 1672
1542 1266
1670 1414
1420 1218
6.50
15.0
105
8.2
980
950
870
760
710
680
570
510
5/3
Wed
9am
2120
1630
1840
1556
16.0
17.9
970
940
910
850
800
750
640
550
5/3
Wed
10am
1892
1460
1616
1396
16.0
25.5
970
950
890
840
760
710
600
540
5/3
Wed
11am
29.8
970
970
920
890
870
830
700
640
5/3
Wed
noon
16.0
37.6
980
950
920
890
850
810
710
680
5/3
Wed
2pm
16.5
41.4
990
950
890
820
750
700
600
5/4
Thur
Sam
1984
1424
1636
1268
6.82
15.5
122
9.0
990
980
950
930
900
830
750
5/4
Thur
9am
7.07
15.5
126
28.0
1000
970
950
920
900
860
780
710
5/4
Thur
10am
6.97
16.0
128
27.3
1000
970
950
930
890
870
800
730
5/4
Thur
11am
6.89
16.0
124
29.9
1000
970
950
940
900
880
790
710
5/4
Thur
noon
6.94
17.0
132
39.1
990
950
930
830
780
680
600
5/4
Thur
2pm
6.72
17.0
156
41.5
980
950
900
830
770
730
640
550
5/5
Fri
Sam
1564
1208
1268
1068
6.55
16.0
112
19.9
970
950
930
900
880
830
750
690
5/5 5/5 5/5 5/5 5/5
Fri Fri Fri Fri Fri
9am 10am 11am noon 2pm
6.80 6.88 6.80 6.78
16.0 16.0 16.0 16.0 16.0
144 151 144 140 129
30.8 28.4 31.2 34.8 33.2
970 970 970 970 970
930 940 940 950 940
890 910 910 930 910
870 870 900 880
830 850 850 870 850
780 820 830 850 820
680 730 740 780 740
620 650 680 720 610
(continued)
-------
CO
Date
Day
Time
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
PH
Temperature, °C
Alkalinity
D.O. Uptake, mg/l-hr
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
5/6 5/7
Sat Sun
8am Sam
1540 1894
1128 1080
1240 1526
958 1042
15.0 16.0
109
18.1 12.0
950 980
900 960
860 950
820 920
760 900
720 870
620 800
530 730
TABLE M-4 (continued)
5/17 5/18
Wed Thur
Sam Sam
1198 1086
816 696
932 742
700 612
6.60 6.66
16.0
91 119
12.3
970
920
880
830
770
710
620
550
5/18
Thur
9am
1934
1434
1540
1256
6.78
16.0
144
28.7
850
770
670
620
560
480
410
5/18
Thur
10am
6.90
142
24.5
960
870
770
650
600
560
460
400
5/18
Thur
11am
1950
1450
1608
1366
7.04
149
22.4
960
870
770
650
610
580
460
410
5/18
Thur
noon
6.90
17.0
144
22.1
920
830
700
650
600
560
450
410
5/18
Thur
2pm
1628
1192
1286
1022
18.0
23.5
940
880
790
750
690
620
520
450
5/19
Fri
7am
1318
886
992
846
6.89
16.0
147
14.7
940
850
760
690
620
580
490
420
5/19
Fri
10am
846
452
500
352
6.67
17.0
160
47.5
960
880
730
660
610
580
490
420
5/19
Fri
11am
836
468
513
373
6.61
18.0
164
51.2
940
820
700
640
580
540
450
390
5/19
Fri
noon
870
504
513
387
6.59
18.0
153
40.6
880
750
640
580
540
490
400
350
5/19
Fri
1pm
758
412
413
307
6.74
160
51.9
890
740
650
580
520
480
400
350
5/19
Fri
3pm
558
238
252
184
7.45
19.0
189
58.8
890
740
660
580
520
490
5/20
Sat
7am
1468
996
1164
956
6.77
18.0
137
21.2
930
730
610
540
500
460
390
340
5/21
Sun
9am
1156
906
906
780
6.67
18.0
140
20.6
910
720
600
530
480
440
380
330
-------
to
TABLE M-5
UNIVERSITY OP LOWELL PILOT PLANT - CONVENTIONAL MODE OF OPERATION - PHASE III
DISSOLVED OXYGEN (mg/1)
Date
Day
Time
Time
Point
Date
Day
Time
Time
Point
2
A - Top of Tank
B ~ Bottom of Tank
* 3
5/3 5/3 5/3 5/3
Wed Wed Wed Wed
i X* \
4
\^ _/
5/3 5/3 5/4 5/4 5/4 5/4 5/4
Wed Wed Thur Thur Thur Thur Thur
7:50 9am 10am llam noon 2pm 7:50 9am 10am llam noon
after
3A
3B
2A
2B
1A
IB
4A
am
shock, hrs. Before 1.0 2.0 3.0
7.6 | 3.3 4.2 4.6
6.6 g 3.1 3.9 4.2
6.6 °° 2.9 3.9 4.5
6.2 * 2.8 3.8 4.0
o
4.9 £ 0.8 1.2 0.8
4.4 0.8 0.8 0.8
1.0 0.4 0.4 0.2
5/5 5/5 5/5 5/5
Fri Fri Fri Fri
am
4.0 6.0 Before 1.0 2.0 3.0 4.0
4.6 4.3 6.8 g 2.2 3.4 4.6 4.B
10
4.2 4.3 6.4 g 2.2 3.5 4.6 4.8
4.5 4.1 6.2 m 1.9 3.6 4.4 4.4
4.5 4.1 5.8 X 2.0 3.6 4.2 4.6
o
1.0 0.9 2.8 g 0.4 0.6 1.2 0.7
0.8 0.8 2.8 0.5 0.4 0.5 0.6
0.3 0.3 1.0 0.1 0.0 0.0 0.0
5/5 5/5 5/6 5/7
Fri Fri Sat Sun
5/4
Thur
2pm
6.0
4.6
4.6
4.2
4.2
0.8
0.5
0.0
7:50 9am 10am llam noon 2pm Bam 8am
after
3A
3B
2A
2B
1A
IB
4A
am
shock, hrs. Before 1.0 2.0 3.0
6.9 g 1.9 4.2 5.6
(0
6.4 0 1.9 3.9 5.4
o
6.4 m 2.0 4.6 5.7
5.4 "" 1.9 4.2 5.6
2.8 £ 0.3 0.5 0.8
to
1.6 0.2 0.4 0.5
0.3 0.0 0.0 0.0
4.0 6.0 No No
Shock Shock
5.4 4.4 8.0 7.4
5.2 4.4 7.5 7.3
5.3 4.6 8.2 7.8
5.2 4.4 6.0 7.4
1.4 1.0 3.4 5.2
0.8 0.6 2.2 4.0
0.2 0.0 0.3 0.4
(continued)
-------
TABLE M-5 (continued)
Date
Day
Time
Time after shock.
5/18
Thur
7am
hrs. Before
5/18
Thur
9am
l.Q
5/18
Thur
10am
2.0
5/18
Thur
11am
3.0
5/18
Thur
noon
4.0
5/18 5/19
Thur Fri
2pm 7am
6.0 Before
5/19
Fri
10am
1.0
5/19
Fri
11am
2.0
5/19
Fri
noon
3.0
5/19
Fri
1pm
4.0
5/19
Fri
3pm
6.0
5/20
Sat
7am
No
5/21
Sun
9am
No
I c Shock Shock
KJ
00
OO
Point 3A
3B
2A
2B
1A
IB
4A
6.
6.
6.
6.
8.
8.
1.
2 a
ra
,0 o
o
.3 ™
.1 M
u
.0 S,
en
,0
.2
0.
0.
0.
0.
1.
1.
0.
.6
,5
,6
,5
.9
,9
,2
0.4
0.4
0.4
0.4
2.2
2.3
0.0
0.
0.
0.
0.
3.
3.
0.
.6
.6
.6
.6
,8
.7
.0
1.
1.
1.
1.
3.
3.
0.
.2
.0
.2
.0
, 8
,8
.1
0.
0.
0.
0.
3.
3.
0.
4
2
2
2
2
2
5
3.9
3.7
3.4
3. 4
6.8
6. 8
0.5
d
o
o o
" in
ON "
ON
^
-------
00
VD
APPENDIX - N
TABLE N-l
UNIVERSITY OF LOWELL PILOT PLANT - OPERATION IN EXTENDED AERATION MODE - PHASE III
SEPTAGE (mg/1)
Phase
Date
Day
Total Volume, liters
(gallons )
% Daily Flow
COD-Total
Total Solids
Total Volatile Solids
Suspended Solids
Volatile Susp. Solids
Total Kjeldahl-N
pH
Grease
Total Phosphorous
IIIA
7/25
Mon
401
(106)
1.33
19200
9210
7400
9400
6400
487
6.2
17700
250
7/26
Tues
401
(106)
1.33
25280
13540
9500
17800
683
5.4
23720
275
7/27 7/28 7/29
Wed Thur Fri
401 0 0
(106) (0) (0)
1.33
46400
29390
28750
22240
728
5.5
8500
275
8/1
Mon
795
(210)
2.63
62450
34390
29200
29000
27750
1025
6.9
120
8/2
Tues
795
(210)
2.63
40800
11770
9730
6000
6000
381
6.8
60
IIIB
8/3 8/4
Wed Thur
795 0
(210) (0)
2.63
7370
4100
3340
2200
1600
241
6.9
52
B/5
Fri
0
(0)
-------
TABLE N-2
UNIVERSITY OF LOWELL PILOT PLANT - OPERATION IN EXTENDED AERATION MODE - PHASE III
INFLUENT (mg/1)
to
UJ
o
Phase
Date
Day
Flow, liters per day
gallons per day
COD-Total
Suspended Solids
Volatile Suspended Solids
Total Kjeldahl-N
Total Phosphorous
7/25
Won
30280
(8000)
56
23
5. 0
7/26
Tues
30280
(8000)
112
31
29
8.1
6.5
IIIA
7/27
Wed
30280
(BOOO)
127
33
16
11.5
IIIB
7/28
Thur
30280
(8000)
175
53
7/29
Fri
30280
(8000)
323
63
8/1
Mon
30280
(8000)
216
104
100
20.4
3. 9
8/2
Tues
30280
(8000)
100
32
10.1
0.6
8/3
Wed
30280
(8000)
107
46
35
10.9
1.6
8/4 8/5
Thur Fri
30280 30280
(8000) (8000)
211
58
49
-------
TABLE N-3
UNIVERSITY OF LOWELL PILOT PLANT - OPERATION IN EXTENDED AERATION MODE - PHASE III
EFFLUENT (mg/1)
Phase
Date
Day
Time
Time After Shock,hrs
COD-Total
Suspended Solids
NO3-N
pH
IIIA
Shock Shock Shock
7/2517/25 7/25 7/25 7/25 7/25 7/2617/26 7/26 7/26 7/26 7/26 7/2717/27 7/27 7/27 7/27 7/27 7/28 7/29
Mon Mon Mon Mon Mon Mon Tues Tues Tues Tues Tues Tues Wed Wed Wed Wed Wed Wed Thur Fri
10am 11am noon 1pm 2pm 4pm 10am 11am noon 1pm 2pm 4pm 10am 11am noon 1pm 2pm 4pm 10am 10am
012346 24/0 12346 24/0 1 2 3 4 6 24 48
32 28 36 48 48 24 24 28 32 40 28 20 24 32 32 36 36 20 32
2 0 0 2 2 2 9.5 10 11.3 48 16 19 16 12 2 2 11 16 13 18
10.2 11.8 12.4 9.3 9.9 10.6 11.2 10.2 10.5 8.4 8.4
7.1 7.2 7.2 7.1 7.1 7.1 7.3 7.4 7.2 7.1 7.1 7.1
to
vo
Phase
Date
Day
Time
Time After Shock, hrs
COD-Total
Suspended Solids
NO3-N
pH
Shock
IIIB
Shock
Shock
8/118/1 8/1 8/1 8/1 8/1 8/218/2 8/2 8/2 8/2 8/2 8/31 8/3 8/3 8/3 8/3 8/3 8/4 8/5
Mon Mon Mon Mon Mon Mon Tues Tues Tues Tues Tues Tues Wed Wed Wed Wed Wed Wed Thur Fri
10am 11am noon 1pm 2pm 4pm 10am 11am noon 1pm 2pm 4pm 10am llam noon 1pm 2pm 4pm 10am 10am
012346 24/0 12346 24/0 1 2 3 4 6 24 48
36 91 253 269 249 170 44 48 76 84 80 68 20 16 32 32 56 23 16 36
7 32 130 136 104 72 9 4 3 23 3 12 3 3 1 7 9 9 16 28
6.4 7.6 5.6 000000 0.1 2.0
7.3 7.2 7.2 7.0 7.1 7.1 7.3 7.3 7.3 7.3 7.3 7.1 7.3 7.3 7.2 7.2 7.2 7.3 7.3 7.2
-------
TABLE N-4
UNIVERSITY OF LOWELL PILOT PLANT - OPERATION IN EXTENDED AEk«i'ION MODE - PHASE III
DISSOLVED OXYGEN (mg/1)
IO
to
Phase
Date
Day
Time
Time After Shock, hrs
Point 1A
IB
2A
2B
3A
3B
4A
Phase
Date
Day
Time
Time After Shock, hrs
Point 1A
IB
2A
2B
3A
3B
4A
Shoe
7/25
Mon
10am
0
7.7
7.5
6.2
6.1
6.0
6.0
6.0
Shoi
8/1,
Mon
10am
0
7.6
7.4
5.5
5.5
5.4
5.3
6.5
*»•
;k
7/25
Mon
llam
1
4.8
4.5
2.2
2.1
1.9
2.0
4.6
:k
, 8/1
Mon
llam
1
5.7
5.5
2.1
2.1
1.9
1.8
5.0
2 1 /
6
3 \
7/25 7/25 7/25 7/2
Mon Mon Mon Mo
' \
f
* — _S
IIIA
Shock
5 7/2617/26 7/26
n Tues Tues Tues
noon 1pm 2pm 4pm 10am llam noon
234
6.0 7.0 7.2 7.
5.6 6.8 6.9 6.
4.0 5.9 6.1 6.
3.9 5.9 6.1 6.
3.8 5.8 6.0 5.
3.8 5.8 5.9 5.
3.6 4.0 4.4 4.
8/1 8/1 8/1 8/
Mon Mon Mon Mo
6 24/0 1 2
1 7.7 5.2 6.7
7 7.5 4.7 6.2
1 5.9 1.1 3.3
0 5.8 0.9 3.3
9 5.8 0.8 3.2
9 5.7 0.7 3.2
8 6.2 5.1 4.7
IIIB
Shock
1 8/21 8/2 8/2
n Tues Tues Tues
noon 1pm 2pm 4pm 10am llam noon
234
5.5 5.7 5.5 5.
5.4 5.5 5.3 4.
2.6 3.3 3.6 2.
2.6 3.3 3.5 2.
2.5 3.3 3.5 2.
2.5 3.3 3.4 2.
3.9 3.3 2.8 2.
6 24/0 1 2
1 7.1 5.0 5.4
8 6.9 4.7 5.1
7 5.7 0.8 2.1
7 5.5 0.8 2.1
4 5.3 0.7 2.0
4 5.1 0.7 1.9
0 3.8 3.2 2.5
7/26
Tues
1pm
3
7.1
6.9
5.4
5.3
5.3
5.3
4.8
8/2
Tues
1pm
3
5.9
5.5
3.1
3.1
2.8
2.8
2.3
7/26
Tues
2pm
4
7.0
6.7
5.3
5.2
5.2
5.1
4.7
8/2
Tues
2pm
4
5.9
5.6
3.3
3.2
3.1
3.1
2.3
7/26
Tues
4pm
6
7.4
6.9
5.1
5.1
4.9
4.8
5.0
8/2
Tues
4pm
6
5.9
5.6
3.3
3.3
3.2
3.2
2.3
She
7/27
Wed
10am
24/0
8.0
7.8
6.4
6.3
6.1
6.1
6.2
She
8/3
. Wed
10am
24/0
6.9
6.6
4.5
4.5
4.3
4.0
4.4
ck
7/27
Wed
llam
1
5.3
5.2
1.2
1.0
0.8
0.7
5.3
>ck
^8/3
Wed
llam
1
3.7
3.5
0.5
0.5
0.3
0.4
2[8
7/27
Wed
noon
2
6.5
6.4
4.4
4.4
4.3
4.3
4.4
8/3
Wed
noon
2
4.6
4.5
1.4
1.4
1.2
1.1
1.6
7/27
Wed
1pm
3
6.5
6.3
4.7
4.7
4.5
4.5
4.1
8/3
Wed
1pm
3
5.2
5.0
2.6
2.6
2.4
2.4
1.7
7/27
Wed
2pm
4
6.7
6.5
4.8
4.7
4.6
4.6
4.2
8/3
Wed
2pm
4
5.7
5.4
3.4
3.4
3.2
3.2
2.0
7/27
Wed
4pm
6
6.5
6.3
5.0
5.0
4.9
4.9
4.1
3/3
Wed
4pm
6
5.7
5.4
3.4
3.3
3.2
3.2
2.8
7/28
Thur
10am
24
7.5
7.3
5.4
5.3
5.2
5.2
5.2
8/4
Thur
10am
24
6.5
6.2
4.6
4.5
4.5
4.4
3.9
7/29
Fri
lOarn
48
7.8
7.7
6.1
6.0
5.9
5.9
6.5
8/5
Fri
10am
48
6.6
6.5
4.0
3.9
3.8
3.8
4.3
-------
to
10
CO
TABLE N-5
UNIVERSITY OF LOWELL PILOT PLANT - OPERATION IN EXTENDED AERATION MODE - PHASE III
MIXED LIQUOR (mg/1)
Phase
Date
Day
Time
Time After Shock, hrs
Suspended Solids
Volatile Susp. Solids
PH
Temperature , °C
D.O. Uptake mg/1-hr-gm
Settlometer
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
She
7/25
Mon
10am
0
2750
2050
23
2.0
500
390
340
300
280
270
240
230
>ck
7/25
Mon
11am
1
23
5.1
500
400
350
310
290
280
250
320
7/25
Mon
noon
2
23
3.3
510
400
350
310
290
270
240
240
7/25
Mon
1pm
3
23
3.1
500
400
350
310
290
270
250
240
7/25
Mon
2pm
4
23
5.1
540
420
360
330
300
290
260
250
Sh<
7/25 7/26
Mon Tues
4pm 10am
6 24/0
3170
2770
23 23
5.0 1.9
490 610
380 470
340 410
300 360
330
270 310
250 275
250 250
IIIA
DCk
7/26
Tues
11am
1
23
2.9
550
420
360
330
300
290
270
250
7/26
Tues
noon
2
23
2.8
580
440
380
340
310
300
270
250
7/26
Tues
1pm
3
23
2.8
630
480
410
370
340
310
280
260
7/26
Tues
2pm
4
7.4
23
3.0
470
400
350
330
310
280
260
7/26
Tues
4pm
6
23
2.7
520
400
350
320
300
290
270
260
She
7/27^
Wed
10am
24/0
3140
2560
23
1.4
610
465
400
360
330
300
280
250
>ck
7/27
Wed
11am
1
23
3.2
600
470
400
360
330
300
280
260
7/27
Wed
noon
2
23
2.4
550
440
390
350
330
310
280
260
7/27
Wed
1pm
3
23
2.7
620
480
410
370
340
320
300
280
7/27
Wed
2pm
4
7.6
23
3.8
810
630
510
440
390
360
310
280
7/27
Wed
4pm
6
7.1
23
3.5
640
490
410
370
350
330
300
280
7/28 7/29
Thur Fri
10am 10am
24 48
3180 3190
2220 2300
7.9
23 23
1.9 2.6
690 640
530 490
440 420
390 370
350 340
330 320
290 280
280 260
(continued)
-------
TABLE N-5 (continued)
Phase
Date
Day
Time
Time After Shock, hrs
Suspended Solids
Volatile Susp. Solids
PH
Temperature, C
D.O.Uptake mg/1-hr-gm
Settlometer
TUB
Shock
Shock Shock Shock
8/11 8/1 8/1 8/1 8/1 8/1 8/21 8/2 8/2 8/2 8/2 8/2 8/31 8/3 8/3 8/3 8/3 8/3 8/4 8/5
Mon Mon Mon Mon Mon Mon Tues Tues Tues Tues Tues Tues Wed Wed Wed Wed Wed Wed Thur Fri
10am 11am noon 1pm 2pm 4pm 10am 11am noon 1pm 2pm 4pm 10am 11am noon 1pm 2pm 4pm 10am IQam
012346 24/0 12346 24/0 1 2 3 4 6 24 48
2800 3140 3660 3780 3810
2190 2510 2880 2860 2920
7.0 7.8 7.6 7.5 7.6 7.6 7.3 8.0 7.9 8.1 8.0 7.7 7.2 7.8 7.6 7.8 7.7 7.6 8.0 7.8
23 23 24 24 24
1.7 3.8 4.4 4.7 4.9 5.3 3.6 4.8 4.6 4.2 3.9 2.9 4.2 4.7 4.2 4.2 3.6 2.9 2.9
5 minutes
10 minutes
15 minutes
20 minutes
25 minutes
30 minutes
45 minutes
60 minutes
520
410
350
320
290
280
250
230
580
450
390
350
330
300
270
250
590
460
390
360
330
300
270
250
650
500
430
380
350
320
290
260
660
500
440
390
320
290
270
630
480
410
370
340
320
280
260
670
510
430
390
360
340
310
290
590
460
400
370
350
300
280
670
510
440
400
370
340
300
290
660
510
440
400
370
350
320
300
660
500
420
380
350
330
300
280
600
460
400
370
340
330
300
290
740
570
480
430
400
380
340
320
790
630
530
460
420
390
350
320
690
530
460
420
390
370
340
320
690
530
460
420
390
370
340
320
780
600
500
450
410
390
350
320
730
560
470
420
390
370
340
320
850
710
590
510
430
370
340
820
660
550
490
440
410
360
340
-------
TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
. REPORT NO.
EPA-6QQ/2-79-132
3. RECIPIENT'S ACCESSION NO.
TITLE AND SUBTITLE
MONITORING SEPTAGE ADDITION TO WASTEWATER
TREATMENT PLANTS
Volume I; Addition to the Liquid Stream
5. REPORT DATE
November 1979 (Issuing Date)
6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)
Burton A. Segall, Charles R. Ott, and
William B. Moeller
8. PERFORMING ORGANIZATION REPORT NO.
9. PERFORMING ORGANIZATION NAME AND ADDRESS
University of Lowell
Lowell, Massachusetts
10. PROGRAM ELEMENT NO.
1BC611, SOS #6
01854
11. CONTRACT/GRANT NO.
R-805406-01
12. SPONSORING AGENCY NAME AND ADDRESS Cin. , OH
Municipal Environmental Research Laboratory—
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, Ohio 45268
13. TYPE OF REPORT AND PERIOD COVERED
Final:Volume 1,8/77-11/78
14. SPONSORING AGENCY CODE
EPA/600/14
15. SUPPLEMENTARY NOTES
Project Officers:
Steven W. Hathaway (513) 684-7615
Robert P. G. Bowker (513) 684-7620
16. ABSTRACT
The report provides information needed to facilitate septage disposal at
municipal wastewater treatment plants. Research assessed the effects of
septage addition to primary and secondary biological waste treatment
processes. Septage was added to an extended aeration process, a two-
stage conventional activated sludge process, and a pilot plant operated
both as an extended aeration and a conventional activated sludge facility
All processes were monitored during a no-septage feed baseline period,
which was followed by constant feed and slug'feed. Results included
process loading for existing plants, design criteria for new facilities
and cost of treatment of septage. Experience gained in feeding and
treating large quantities of septage is reported.
Septage is readily treated biologically with domestic sewage. The
organic and solids content of septage averages about 50 times that of
domestic sewage. Solids removal in primary clarification is excellent
and in combination with primary or secondary sludge, septage dewaters
well.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTIFIERS/OPEN ENDED TERMS
c. COSATI Field/Group
Waste treatment
Sludge disposal
Septic tanks
Septic tank sludge
Septage treatment
Biological treatment
13B
18. DISTRIBUTION STATEMENT
Release to Public
'-
EPA Form 2220-1 (Rev. 4-77)
Unclassified
321
20. SECURITY CLASS (This page)
Unclassified
22. PRICE
295
-•• US GOVERNMENT PRINTING OFFICE 1980 -657-146/55E8
------- |