-------
Table 5 (continued).  SUMMARY-OF STEADY-STATE MEASUREMENTS
Frloary Secondary Secondary
Steady* affluent effluent af Quant Return
•tate VSS, MLVSS. TSS. VSS. elutlge
Date period
2BS«p71 7
29Scp7l 7
10ct7l 7
30ct7l 7
40ct71 7
50ct71 7
60ct71 7
70ct71 7
90ct71 7
100ct71 7
110ct71 7
*So»71 8
10Nov71 a
UXovTl 8
23Nov71 8
24Nov71 8
25Sov71 8
26Nov71 8
29Nov71 8
lJjn72 9
2Jan72 9
SJan72 9
6Jan72 9
8Jan72 9
10Jan72 9
12JJD72 9
Secondary
affluent
total COO
Date Bg/1
28Sep71 112
29Sep?l 107
10ct71 109
30et71 120
40ct71 120
50«l71 127
6Oct71 101
70ct71 114
90ct71 @9
JOOesJJ 114
110ce71 —
?Ni>v7l 132
10::ow71 141
SiNov71 13S
2JSjv71 126
24Kov71 120
25Sow71 137
26Kov71 140
29Sov71 146
Uan72 \Q1
2Jsn72 132
5Jan72 168
6Jan7J i74
8Jan72 316
10Jan72 196
12Jan72 132
ag/1 og/1 Dg/1
79 1060 26
84 1190 19
240 1260 19
49 1010 46
63 1020 34
71 830 35
81 1080 17
65 1140 19
72 840 41
109 1050 12
137 950 IS
88 3280 28
106 3280 23
39 2530 40
61 2080 39
60 1890 36
96 2370 57
81 2050 30
29 1770 31
205 1190 62
104 1040 66
99 960 114
104 1280 65
76 1050 74
94 960 64
92 1380 55
Secondary Secondary
•ffluunt affluent
„ soluble total BOO,
COD, tag /I BS/1 .
86 34
80 23
71 23
78 19
84 23
85 26
77 23
. 84 19
71 23
102 21
108 $«-( —
113 36
110 32
102 29
89 31
83 37
93 32
106 5f,T 41
11? '«•' ' 28
Q8 41
79 30
82 46
107 48
109 28
106 &/; 30
117 «^> 18
ng/l
18
16
12
36
' 31
27
13
18
20
11
10
25
22
36
27
26
44
23
22
29
66
97
57
67
39
52
Secondary
offluene
oolublo
SOD. os/1
18
14
11
14
12
20
12
13
14
17
27
24
20
18
13
14
20
23
21
17
19
21
28
21
24
IS
Prioary Prleary
effluent affluant
total COD. total BOD.
VSS. ag/1 og/1
3030
3120
2950
2690
2690
2610
2710
2850
2800
2730
2550
8620
8870
6840
4830
5330
5740
5780
4450
3060
2570
1770
3630
3210
2380
3150
Prtmery
•ffluaae
glowrate o
13 ^
230
230
252
239
248
234
240
238
241
237
234
233
260
251
23$
237
234
236
237
233
249
200
234
230
173
230
337
358
582
307
319
364
339
380
333
347
395
403
382
317
321
303
332
3Z6
276
491
365
353
393
363
363
404
Raturn
oludgo
flowrsta
B3/hlr
136
136
136
123
125
123
123
127
127
127
127
136
136
131
134
136
136
136
134
131
131
136
148
108
108
114
a8/l
153
120
156
120
78
114
105
96
87
108
144
113
116
88
96
79
111
114
79
150
152
105
156
84
128
113
tfaeea
oludga
„ ilwroeo D
QJ/hr
3.6
3.6 .
3.6
3.3
3.7
3.4
3.6
3.3
3.7
3.6
3.7
1.4
1.3
1.4
l.S
1.3
1.3
1.3
1.3
4.S
4.1
4.0
4.1
4.1
4.1
4.1.



























Aaraiion
tank
voluna
eP
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
240
260
                            53

-------
        u
in

3a£<2
ri.6Dec70
17Dec70
18Dec70
19Dec70
20Dec70
21Dec70
31Dec70
2Jan71
t, 3Jan7l
5Jan71
15Jan71
16Jan71
17 Jan 71
18Jan71
^=-15Apr71
16Apr71
18Apr71
(__19Apr71
9May71
llMay7l
12May71
13ffcay7l
14May7i
16May71
17Ksy71

Ejydraulie
ffesideaea
6i®g0 I0
day
0.215
0.215
0.215
0.215
0.215
0.215
0.215
0.215
0.215
0.215
0.172
0.172
0.174
0.174
0.110
0.117
0.103
0.103
0.071
0.067
0.076
0.075
0.076
6.07S
0.073
Table 6.
,/
Isao X
cell
ag®0 .
®e» 
0.253
0.296
0.268
0.314
0.250
0.260
0.206
0.178
0.613
0.593
0.942
0.725
0.572
©.443
Oo4S5
Loading
LvCODC
0.494
0.532
0.468
0.411
0.382
0.429
0.737
0.696
0.613.
0.656
0.849
0.777
0.448
0.413
0.795
0.895
0.793
1.00
1.58
1.96
2.41
2.70
2,44
1.67
1.79
velocity B
LvBODd
0.308
0.332
0.413
0.137
0.206
0.273
0.347
0.198
0.200
0.200
0.285
0.318
0.292
0.334
0.267
0.279
0.225
0.207
0.649
0.654
1.01
0.762
0.636
0.455
0.541
COB removal
a££ieieffleys
*
73
* J
62
50
61
67
68
50
80
73
85
64
71
68
S5
78 '
76
75
78
76
76
84
S4
73
77
79
BOD removal
sffieicaeyo
I
91
84
89
76
86
§9
90
87
86
92
89
93
92
94
94
93
92
86
94
91
93
95
90
.93
90
Steady-
o£a£e
period
1
1
1
1
1
1
j.
1
1
1
2
2
2
2
3
3
3
3
4
4
• 4
4
4
4
4
                                          1.92
                                                        '•7

-------
Table 6 (continued).  SUMMARY OF STEADY-STATE PERFORMANCE PARAMETERS
Date
19May71
20May71
21Way71
23May71
24May71
25May71
28May71
29May71
16Aug71
17Aug71
20Aug71
23Aug71
24Aug71
25Aug71
26Aug71
28Aug71
29Aug71
30Aug71
31Aug71
5Scp71
'.Sep71
9Sep71
HSep71
12Sep71
13Sep71
14Sep71
16Sep71
17Sep71
19Sep71
lydraulle
residence
day
0.073
0.073
0.073
0.073
0.073
0.073
0.070
0.070
0.040
0.040
0.042
0.041
0.043
0.040
0.040
0.038
0.030
0.041
0.040
0.039
0.042
0.041
0.039
0.041
0.041
H.f)41
U.04U
0.040
0.040
Ksass
call
age 5
8cr day
1.36
1.35
1.51
1.57
1.57
1.29
1.27
1.20
0.545
0.625
0.700
0.788
0.692
0.508
0.754
0.776
0.817
0.753
0.715
0.874
0.775
0,848
0.812
0.411
0.719
0.871
0.740
0.806
0.860
Removal velocity,, Loading velocity „
^cooa 'BOD vcoflc VBOD
1.53
1.83
2.56-
1.96-
1.66
1.78.-
2.76'
1.76/
3.42
2.37
2.70
3.63
3.15
3.18
3.20
3.53
2.75
2.60
5.23
3.07
3.07
3.37
3.44
4.08
4.20
3.94
3.82
3.07 o,
3.12,
0.499
0.567
0.693
0.754
0.718
0.812
0.519
0.625
1.41
1.01
1.25
1.78
1.62
1.73
1.96
1.64
1,29
1.45
1.54
1.71
1.50
1.43
1.05
1.73
1.46
1.86
1.78
, 1.77
1.22
1.91
2.19
3.11
2.28
2.04
2.16
3.16
2.23
4.46
3.29
3.68
4.57
4.06
4.24
4.20
4.44
3.77
3.49
6.19
3.82
3.86
4.17
4.80
5.20
5.60
4.78
4.61
3.95
3.80
0.481
0.606
0.736
0.803
0.771
0.868
0.542
0.661
1.57
1.07
1.42
2.01
1.92
1.94
2.20
1.82
1.49
1.36
1.64
1.87
1.74
1.60
1.24
1.90
1.64
2.06
1.94
2.04
1.39
COD removal BOD removal steady-
efficiencyc, efficiency, state
I Z period
80
84
82
86
81
82
87
79
76
72
73
79
78
75
76
80
73
74
84
81
80
81
72
78
75
82
83
78
82
93
94
94
94
93
94
96
94
90
95
88
89
84
89
89
90
86
84
94
91
86
89
88
91
89
90
92
87
87
5
5
5
5
5
5
5
5
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6
6

-------
                             Table 6 (continued).   SUMMARY OF STEADY-STATE PERFORMANCE PARAMETERS
Wl



Dace

20Sep71
28Sep71
29Sep71
10ct71
30ct71
40ct71
50ct71
60ct71
70ct71
90ct71
100ct71
110ct71
9Nov71
10Nov71
14Nov71
23Nov71
2«Nov7l
25Nov71
26Nov71
2SNov71
Uan72
2Jan72
5Jan72
6Jan72
8Jan72
10Jan72
12Jan72
Hydraulic
residence
tins, e0
day

0.041
0.040
0.040
0.040
0.042
0.040
0.043
0.042
0.042
0.041
0.042
0.042
0.039
0.038
0.040
0.042
0.0/.2
0.043
0.042
0.042
0.039
0.040
0.050
0.043
0.040
0.058
0.040
(sag COD FQEOved)/
C te EC
19 applied)/
Mean
cell
age,,
eeo day

'0.881
0.493
0.556
0.649
0.434
0.337
0.482
0.590
0.569
0.407
0.589
0.562
1.81
1.74
1.38
1.63
1.44
1.35
1.60
1.60
0.538
0.388
0.364
0.456
0.353
0.486
0.535

Stessove
qCODs
\f\faf

3.26
5.96
5.88
10.2
5.40
5.73
6.64
5.86
6.19
7.52
5.55
7.24
2.29
2.16
2.14
2.63
2.74
2.34
2.56
2.11
8.57
6.86
5.69
5.24
6.06
4.64
5.21
'(qs m,VSS)(day).
'Ins EMS§)
(day) o

1 velocity.
W


1.31
3.21
2.24
2.90
2.50
1.61
2.24
2.08
1.74
2.10
2.06
2.95
0.697
0.762
0.696
0.940
0.815
0.900
1.03
0.778
2.83
3.19
1.76 •
2.34
1.50
1.88
1.78
J («g BOD re
lag B9B> a$

Loading
LvCODc


4.13
8.01
7.57
11.7
7.24
7.78
8.67
7.58
7.95
9.56
7.86
9.96
3.19
3.03
3.15
3.63
3.80
3.28
3.78
3.70
10.4
8.76
7.42
7.20
8.66
6.55
7.34 .
tanked) /(mf
lgiMc3d)/(jl£


velocity j, 000 reaoval
LvBODd efficiency.


1.42
3.64
2.53
3.13
2.83
1.90
2.71
2.35
2.01
2.50
2.44
3.63
0.885
0.921
0.874
1.09
0.991
1.11
1.32
1.06
3.19
3.65
2.21
2.86
2.00
2.31
2.05
j. MLVSS) (day)
1 MLVSS) (day)
Z
J-
79
74
78
88
75
74
77
77
78
79
71
73
72
71
68
72
72
71
68
57
02
78
77
73
70
71
71
o -
O

BOD reaoval
efficiency,,
2

92
88
88
93
88
85
82
88
86
84
84
81
79
33
80
86
. 82
82
78
73
89
83
80
'HZ-
75
©a
87



Steady-
state
period

«
7
7
7
7
7
7
7
7
7
7
7
©
3
C
8
e
Q '
• i
Q
9
9
9
.9
. S>
*
©

-------
concentration depends solely on the performance of the solids separation
system, effluent soluble substrate concentration was assumed to be the
limiting substrate concentration for the kinetic analysis.
Secondary Effluent Quality
    As mentioned previously, the secondary effluent substrate and solids
concentrations depend on the growth characteristics of the activated
sludge and the solids separation system performance, respectively.  In
this study, because the system was deliberately operated from a very
low-rate system to a high-rate system, the secondary effluent substrate
concentration varied with the system growth rate.  Secondary effluent
total BOD concentrations (Table 5) varied widely from 7 to 61 mg/1 and
no consistent trend could be delineated.  However, secondary effluent
soluble BOD  (Table 5) varied from 4 to 28 mg/1 and appeared to be a
function of  system growth rate.  This relationship will be discussed sub-
sequently in the kinetic analysis section.
     Secondary effluent  total suspended solids  in this study ranged from  2
to 114 mg/1  and volatile suspended solids varied from 2 to 97 mg/1 (Table
5),  despite  the use of  low—13 ra3/(m2) (day) [315 gal/(ft2) (day) ]—overflow
rates  in the secondary  clarifier.  No correlation could be drawn between
secondary effluent total or volatile suspended solids and system growth
characteristics.  The relationship between  secondary effluent solids con-
centration  and  solids separation system performance will be discussed sub-
sequently under the  evaluation of solids separation systems.
Active Biomass  Parameters—ATP  and  Dehydrogenase Activity
     In addition to  the  mixed  liquor volatile  suspended  solids  (MLVSS),
 adenosine  triphosphate  (ATP)  and dehydrogenase activity (measured  as
 triphenyl  formazan,  TF9 formed  per  hour) were used  to estimate the active
 biomass concentration,,   Although complete  daily ATP and dehydrogenase
 activity measurements were not  conducted throughout the study  period,
 11 steady-state ATP and dehydrogcmase activity measurements  were performed,
 and are reported in Table  7.
                                   57

-------
                       Table 7.  STEADY-STATE ACTIVE ORGANISM CONCENTRATION MEASUREMENTS
00
Steady °state
Date period
18 May 71
19 May 71
24 May 71
25 May 71
17 Aug 71
24 Aug 71
28 Aug 71
4 Oct 71
5 Jan 72
6 Jan 72
10 Jan 72
4
5
5
5
6
6
6
7
9 .;••;,.,;•.
9
9
ATP/MLVSS, . Effluent soluble Effluent soluble
(wg ATP)/ Dehydrogenase/MLVSS , COD, BOD 8
(mg MLVSS) (yg TF)/(mg MLVSS)(hr) Bag/1 mg/1
0.47
0.58
0.49
0.51
0.78
0.72
0.80
1.02
1.22
1.24V- v-
1.01
52.6
27.7
37.4
43.7
54.6
32.6
42.1
73o7
68.0-
50.4
72.6
72
70
79
70
81
59
66
84
82
107
106
10
6
11
10
5
20
13
12
. . 21
28
24

-------
    Previous research studies (References 21 and 22) have reported ATP
content and dehydrogenase activity of activated sludge as viability
measurements.  These studies found that the ATP content ranged from 0.2
to 0.3 (ug ATP)/(mg MLVSS) (Reference 21) and dehydrogenase activity
ranged from 31 to 83 (mg TF)/(g MLVSS) (hr) (Reference 22).  The ATP
content of the MLVSS in this study 10.47 to 1.24 (ug ATP)/(mg MLVSS)]
was higher than previously reported values s while the dehydrogenase ac-
tivities  [27.7 to 73.7 (ug TF)/(mg MLVSS) (hr)] were about the same as
the values reported by Ford, et al,   (Reference 22).
    ATP and dehydrogenase activity measurements were used in the kinetic
analyses and the performance characteristics based on ATP and dehydro-
genase activity are listed in Table 8.  These characteristics included
substrate (BOD and COD) removal velocity based on ATP and dehydrogenase
activity, net growth rate and effluent soluble substrate  (BOD and COD)
concentrat ions .
KINETIC ANALYSIS AND KINETIC CONSTANTS
    The kinetic characteristics of tho accelerated high-rate activated
sludge system were evaluated with respect to  the following  equations  and
kinetic coefficients and  constants:
     (1)   The cell continuity equation,

                             1/6C = Yq -  kd
    where Y  « yield coefficient
          k, ° decay constant.
     (2)   Michaelis-Menten  (Monod) equation,
                                         .
                                    s    1
                  maximum BOD removal velocity

           y » Yq = maximum specific growth rate

           K0 ° half -saturation constant.
            D

                                     59

-------
Table 8.  STEADY-STATE PERFORMANCE CHARACTERISTICS BASED ON ATP AND DEHYDROGENASE ACTIVITY
Date
18 May 71
19 May 71
24 May 71
25 May 71
17 Aug 71
24 Aug 71
28 Aug 71
4 Oct 71
5 Jan 72
6 Jan 72
10 Jan 72
Steady-state
period
4
5
5
5
6
6
6
7
9
9
9
qCOD(ATP)9 qBOD(ATP),
(mg COD removed ) (mg BOD removed)
(yg ATP) (day)
3.64
:.64
3.38
3.48
3.04
4.38
4.42
5.62
4o67
4.23
4.59
(yg ATP) (day)
1.07
0.774
1.47
1.59
1.29
2.25
2.05
1.58
1.45
1.89
1.86

day
0.521
0.738
0.638
0.774
1.60
1.45
1.29
2.24
2.75
2.19
2.06

-------
    (3)   Modified Michaelis-Menten (Monod) equation,
                                 - KCOD>
                      (K.-KCOD)
where     ^coD = raax*mum COD removal. velocity
          *    *
          p a Yq => maximum specific growth rate
          K  = half-saturation constant
           8
          K  n » nonbiodegradable COD concentration.
Evaluation of Cell Continuity Equation
    The cell continuity equation,  l/ec = Yq - k,, was used to estimate
the yield coefficient and decay constant.  Two substrate measures, BOD
and COD, were used as substrate parameters, and  the active biomass con-
centration parameters were expressed as mixed liquor volatile suspended
solids, ATP content and dehydrogenase activity.
MLVSS as Active Biomass Parameter—
    Least-square regression analyses of all steady-state measurement.!; re-
sulted in a yield coefficient of 0.793 (mg MLVSS produced) /(mg BOD removed)
as shown in Figure 4, and 0.293 (mg MLVSS produced)/ (mg COD removed), as
shown in Figure 5.  Although reasonable estimates of yield coefficients
were obtained with highly significant correlation coefficients
(R =» 0.865 for BOD basis and 0.871 for COD basis), relatively high nega-
tive decay constants were obtained (k, = -0.119  and -0.164 day   based
                                     a
on BOD and COD, respectively).  From a statistical regression stand-
point j, one of the primary causes  for the negative k,  appears  to  be  the
                                                                      -1
widely scattered data points  for  net growth rates greater  than  106  day
(cf.  Figures 4 and 5),  Consequently,  the  total  variation,, i.e.,, the sum
of the squares of the deviation of the values  of net  growth  rate from the
mean  net growth rate value „  of  these data  points could  markedly  affect
both  the slope  (yield coefficient) and  the intercept  (decay  constant) of
the cell continuity  equation (Equation  16) „
                                    61

-------
     3.0



     2.0



     2.1



     2.4



7    2.2
 S=»
 «S

"**   2.0



J3   i.g




~   1.0



§-   1.4



|   1.2


H3   | f)
era   l.w
I    I   1   i   I   1   !   I
S.  I    1   !
                       ©
                          STIW-STflTi

                          ITSaei-SlftTS
         JLJLJLJUUULJ
.2 8.4 0.6 0.8 1.0 1.2  1.4 LI !.§ 2.J  2.2 2.4 2.0  2.1 3.0 3.2-3.0  3.1 3.


         iii igam VELOCITY.

-------
 3=.
 fO
ts

C—
                                                     = 0.293 q
                                                  _ Q 293 (mg MLVSS produced)
                                                          (mg COD removed)
                                                   kd  = -0.164 day

                                                        (R = 0.871)
                                                   STEADY-STATE EXPERIMENTS AT HIGH  RATE
                                                   STEADY-STATE EXPERIMENTS AT LOW RATE
Figura   5.
                              34       56       78

                               REMOVAL VELOCITY, q      (mg COD removed)
                                                  COD,  (mg MLVSS) (day)

                Riot  of  cell  continuity using  COD  as substrate
                                                                              10
n

-------
    To check this possibility„ regression analyses tyes-s ©ad® on
values of nin© sEeady~Qtate periods0  Yield coefficients of 00922
(rag MLVSS produced)/(sag BOS rsaoved) „ as shcam in Figure 60 and 00328
(mg MLVSS produced)/ (@g COD removed) „ as ©ho*m in Figure 7B was1© obtained
with identical9 highly significant correlations  (R o 0,981,, p > 0099),
These values of yield coefficients are within the range reported by many
workers  (References 23D 24 and 25).. From the reported da£©0 it appears
that the yield coefficients of 0050  to 0,97 (mg  MLVSS)/(rag BOD removed)
and 0032 to 0.&6  (mg MLVSS)/(mg COD  removed) are applicable to the acti-
vated sludge treatment system of  domestic wastetrater.
    Corresponding values  of decay constants in the cell continuity equa=
                                                            —1
tion (Figures  6 and 7) Here found to be  0.027 and -0,023 day   based  on
BOD and  CODS respectively„  The decay constant of 0,027 day"  based on
BOD is of  the  same magnitude as reported decay rates.  Heukelekian at aJ0
(Reference  26) reported  a decay rate for activated sludge  of  00055 day
and Jenkins and Menar  (Reference  25) reported  a  decay rate of 0,015 day
                                         — 1
    The  negative  decay value, -0.023 day  based on  COD9 appears  to be
questionable,,  although negative values  for decay rates have been  reported
for bacterial  systems  (References 23 and 27),  Theoretically„ according
to the cell continuity  equation0  the value  of  k, should be positive rather
than negative.  The possibilities of varying decay rates and  varying  yield
coefficients  caused by  the temperature  variation in  mixed  liquor  (17  to
26°C)  through  the 15-month study  period may have caused a  negative k. to
result upon linear  regression  analysis,  Mo attempt  Has made  to evaluate
the effect of  temperature on these kinetic  characteristics due  to limited
and  incomplete data.
ATP and  Dehydrogenase as Active  Bioaiass Parameters
    The  yield  coefficients and  decay rates  based on  11  ATP and  dehydro-
genase activity measurements  were obtained  from regression analysis of
the  cell continuity equation,,  which are presented  in Figures  8D  9P 10
and  11,

-------
3.0
     2.5
     2.0
1.5
1.0
0.5
         1 = 0.922 q   -0.0273
         8C        BOO

         y _ g 922 (mg MLVSS produced)
                   (rag 800 removed)
          hd= 0.0273 day
                      -I
                  = 0.981)
0.5
                        ODD
                                                 •STEADY-STATE EXPERIMENTS AT HIGH RATE
                                                 o STEADY-STATE EXPERIMENTS AT LOW RATE
                                                                       1
                                         1.0               1.5               2.0
                                         VELOCITY,  q      (mg  BOD  removed)
                                                   BOD,  (mg  MLVSS)  (day)
                                                                                       2.5
Figure  @
        Cell  continuity equation for  mean  steady-state values  usinp  BOD as
                              substrate parameter

-------
ea
^    2
              T~     r
i       f
                • STEBP-STATE EX PER HOTS AT HIGH RATE
                o STEADV-STATE EXPERJBEIiTS AT LOI RATE
                                            1 = 0.328 D   +
                                          I     •  I
                7   Odll  e@s?t8nui ty aquation for  m@m §^®adlj/=i

-------
3.0
2.0
1.0
   i       r
                         !    '   I

                           * 0.439
                      (ATP)
                          dug ATP produced)
                          (rag BOD removed)
   «d = -o.
i       r
                  = 0.377)
i       r     T
          i       i      j	i
                                                     i       i       r	i
  0.2     0.4     0.®    O.B     1.0    1.2     1.4     1.6     1.8     2.0     2.7

             100 KEiOVAL  VELOCITY,

'igure   '
                    Plot  of cell  continuity  equation using-BOD-and ATP

-------
S3
•si
<33>
IUVJ1


0=
0=
^   LI
0=
                r~~i
    Fiiurt  I

-------
                      3.0
                      2.0
vO
                 C9
                      1.0
                                      I
I
        1 =24.3q(
0.834
                                                                rm
                                                                UF>
                                                                         (TF)
                                                                    = 24 3 0"E TF produced)
                         BOD
                                                                        '1
                                                            kd = -0.834 day
                                                                   (R= 0.417)
  0.01           0.02
BOD REMOVAL VELOCITY, q
                                                                0.03
                          0.04
                                                                   (mg BOD  removed)
                                                                   (/Jg TF/hr) (day)
                              Figure  10   Plot  of cell  continuity  equation using
                                        BOD and dehydrogenase activity
                                                                                         r)
             0.05

-------
     3.0
                       I       I       f
     2.0
•a:
-------
    Based on ATP measurements, as shown In Figure 8, a yield coefficient
of 0.661 (ug TF produced)/(mg BOD removed) and a decay rate of -0.439
day   were observed with a poor correlation coefficient  (R m 0.377).
Using COD as the substrate measure, as shown in Figure 9, a yield coeff-
icient of 0.629 (yg ATP produced)/(tog COD removed) and & large positive
decay of 1.045 day"  were obtained, with good correlation (R <= 00709).
    Poor correlation was observed using dehydrogenase activity as an ac-
tive biomass measure, as shown in Figure 108  A yield coefficient of 24.3
(ug TF produced)/(rag BOD removed)(hr) and a decay rate of -0.834 day"
were obtained (R = 0.417).  A good correlation (R » 0.678), however,
existed for the cell continuity equation based on dehydrogenase activity
and COD removal velocity, as shown in Figure 11.  The yield coefficient
and decay rate were 21.0 (pg TF produced)/(mg COD removed)(hr) and  -0.092
day  , respectively.
Evaluation of Substrate Removal Velocity and Substrate Concentration
Relationships
    Two different approaches were used  to evaluate  the substrate  removal
velocity and substrate concentration  relationships.  These approaches
were:
     (1)   By direct nonlinear regression analysis of  the Michaelis-Menten
           (Monod) relationship, q = qS^/(K  •*• S.)0  to determine  the maxi-
          mum BOD removal velocity, q,  and  half-saturation constant
           constant, K   and
                     5
     (2)    By direct nonlinear regression  analysis of  a modified  Michaelis-
           Menten  (Monod) equation,  assuming a certain  fraction of the  COD
           is nonbiodegradable0  namely,
                          	 COD'
                      q B TK—I~K—) + (s
                          (8   KCOD} * (S1
 where       ^    = nonb*°degradable <'•'>!) ^ont-pr.i ration
                                     71
-------
    To evaluate the Michfi®li@~Hsnt®n  (Monod) kinetic model ©ad its -modi-
fied equation  (Equation 34) 0 all ©t@®dy°state aessuresaeat® t?®ffe used in
the regression analyses,.  A poor correlation and uxir@a@oaal>ls estisaat© of
kinetic constants resulted, however;,  primarily dwe to %?ide scatter in the
data points , especially for HBeasur
-------
 (O
 €/»
 DO
                                                *  STEADY-STATE AT HIGH RATE
                                                  STEADY-STATE AT LOS? RATE
                                                    -4 13 (ag BOO removed)
                                                  BOO" '   (gig aiVSS)
                       10               20
                        EFFLUENT SOLUBLE SOD.
Fi
 hi
 12   Plot of ^lichagl is-^@nten  (Monod)
rate  activated  sludge  system using
        30              40
iOD,  f"1*/1)
   equation  for accelerated
    as substrate parameter
-------
iguire
 EFFUJiOT S
ftiehMli-s-^@nft@n (Nonod)- equation using BOD and ATP
-------
    Using dehydrogenase activity as an active biomass measure, a maximum
BOD removal rate of 0,101 (mg BOD removal)/(ug TF/hr)(day) and a half-
saturation constant of 39.9 (mg BOD)/I were obtained, as shown in Figure
14.  The maximum specific growth rate based on dehydrogenase activity
was estimated to be 2.45 day  .  Because of scattered data and a limited
numbei of data points, kinetic characteristics based on dehydrogenase
activity were inconclusive,

Modified Michaelis-Menten (Monod) Equation
    When COD was used as the substrate concentration parameter, a certain
amount of COD, Kr__, was assumed to be nonbiodegradable to activated sludge,
    Direct nonlinear regression analysis of the modified Michaelis-Menten
(Monod) equation (Equation 34) gave a maximum removal rate, q, of 8.35
(mg COD removed)/(mg MLVSS)(day)9 a half-saturations, KSS1 of 94,9 (mg COD)/I
and a nonbiodegradable COD of 19,9 mg/ls as shown in Figure 15.  The best-
fit equation that results is

                             8,35  (S,     -  19.9)
                                    1COD                            (35)
                        N   75°° +  CS1COD -  19°9)
    Multiplication of the maximum COD removal  rate0 q, by the yield co-
efficient „ Y9 produces a maximum specific growth rate of 2,74 day   based
on COD,  Although the kinetic  constants  q and  y appear to be slightly on
the low side., the values are realistic.
    Steady-state measurements  and  performance  parameters based  on ATP and
dehydrogenase activity also were evaluated with the modified Michaelis-
Menten  (Monod)  equation.  The  best-fit  equations obtained  are shown in
Figures  16  and  17  and are as followsi
                                                                   06)
                         ATP   949 + (S     + 6.5)
 and                    qTF  ° 942
                                     
-------
o
IS
 (So)
-------
ae
o-
53=
D=-
O
o
                                                            _  8.35(S, MD-19.9)
                                                        C00  (94.5 -
                                                                            C(JD
                                                                               - 19.9)
                                                        }   . 8 35 (mg COD removed)
                                                        COD   '   (rag MLVSS) (day)
                                                        Ks = 94.5  (rag COD)/I
                                                           •  STEADY-STATE AT HIGH RATE
                                                           o  STEADY-STATE AT LOW RATE
   Fii
                                EFFLUENT SOLUBLE  COD, Sj CQD  mg/l
                Plot  of modified  Michaelis-Menten (Monod)  equation  for accelerated
               -rate  activated sludge system using COD  as  substrate parameter
-------
C9
               ©
               &
               e
               =!>
               MJI
               CM
                        Flips'© II
                                                   usen'g
-------
•sj

V£>
          &
03

E
    0.14



    0.13



    0.12



    0.11






3  0.08
            o
t—

o
          •s*
          o
          •m
          —  ^CSO (TF)" (833 + 8.
    0.00



    0.07



    0.08



    0.03






    0 03



    0.02
                                             I

                                  o.§§4(sf CDO
                                                  -e-8.i)
                         a       - 0 584 dag COD
                          COP (TF)    '    (ajg TF/hr) (day)
                           - S33 (ag C00)/l
                            I
                                  I
                                                 I
                                          I
I
10      20




Figure n
                                30
                                                                          80
                                                    40       50      80       70

                                               EFFLUENT SOLUBLE COO.  S,  COQ mg/l


                                        Plot of modified Michael is-Menten (Morrod)  equation

                                                      and dehydrogenase  activity
                         100
no
-------
    Because of scattered data points (see Figures 16 and 17), both K
                                                                    3
and KCQJQ values, calculated on the basis of ATP and dehydrogenase activity „
appear to be unrealistic,.  Using previously determined ATP and dehydro=
genase activity yield coeffieients0 iae.9 Y T  <=> 0.629 (yg ATP produced)/
(rag COD removed) and ¥„_, » 2100 (\tg TF produced/hr)/(mg COD ressoved), the
maximum specific growth rate values Here estimated to be unrealistic
(27o4 and 12»3 day   based on ATP and dehydrogenase activity, respectively)

Summary of Accelerated High-Rate Activated Sludge System Kinetic
Characte ris tica  •
    Based upon both  theoretical analyses and practical considerations„
these studies confirm that one of the most important characteristics of
the activated sludge process  affecting both performance and operating
characteristics is the active biological biomass in the system*  Thusp
it is imperative that accurate estimates of the total active biological
bioroass in the system be obtained.  Three active biomass parameters—
MLVSS, ATP and dehydrogenase  activity—were considered in  the kinetic
evaluation of the  accelerated high-rate activated sludge system  for com-
parative purposes.
    Tables 9 and 10  summarize the kinetic characteristics  of the accel-
erated high-rate activated  sludge system based on ATP and  dehydrogenase
activity as  the  active biomass measures.  Because only  11  steady-state
ATP and dehydrogenase  activity measurements Here obtained  during the
study period,  the  kinetic  characteristics,  obtained  from regression anal-
ysis, appear  to  be questionable  on  a  statistical basis.
MLVSS as Active  Biomass  Parameter—
    Reasonable  estimates of kinetic constants  and kinetic  relationships
were  obtained using MLVSS  as  the  active  biomass measure.   A sumaary of
the most  probable*values for  the kinetic  constants  and  coefficients Y,
k.o q,  Ms,  K  and $LnT> are  presented in Table  11,   For  the  purpose  of
  u         8       (*U1)
comparison,  the reported values  of  activated  sludge  process kinetic  cci-
stants  are suosnacized in Table 12.
                                   80
-------
Table 9.  EVALUATION OF CELL CONTINUITY EQUATION USING ATP AND DEHYDROGENASE
                    ACTIVITY AS ACTIVE BIOMASS PARAMETERS
                             BOD as substrate parameter
                        Yield            Decay        Correlation
    Active biomass   coefficient9      constant,     coefficients
      parameters          Y           k, day              R
         ATP           0.661             -0.439          0.377
                      ATP produced)
                     ^
                  (mg BOD removed)


    Dehydrogenase     24.3               -0.834          0.417
      activity    (pg TF produced)
                  (mg BOD removed) (hr)
                        COD as substrate parameter
                   Yield            Decay        Correlation
                coefficient.     constanta      coefficient,
                     Y           k, day-1            R
                  0.629            1.045            0.709
               (pg ATP produced)
               (mg COD removed)
                 21.0             -0.092            0.678
                 ^ TF produced)
               (mg COD removed) (hr)
                                      81
-------
  Table  10.   EVALUATION OF MICHAELIS-MEHTEN  (MONOD)  EQUATION USIHG
         AND  DEHYDROGENASE ACTIVITY  AS  ACTIVE BIOMASS
   Active biomasa
     parameter
                          BOD as substrate parameter
               Maximum BOD
            removal velocity, q
       ATP             2.30


   Dehvdrogenase
      activity         0.101
(mg  BOD  removed)
 (yg ATP)(day)


    BOD  removed)
     TF/hr)(day)
                    Half -saturation
                                K
                                       5.1 mg/1


                                      29.9 mg/1
                      COD as substrate parameter
          Maximum COD
       removal velocity, q      constant, K
                   Ha If-saturation   Nonbiodegradable
                                        COD,  K
                                                         COD
     43.5
      0.584
    COD removed)
 (ug ATP)(day)


fag  COD removed)
     TF/hr)(day)
     942 mg/1
     933 mg/1
-6.5 mg/1


-8.9 mg/1
I
                                    82
-------
               Table 11.   SUMMARY OF MOST PROBABLE KINETIC GROWTH CONSTANTS OF ACCELERATED HIGH-
                                         RATE ACTIVATED  SLUDGE SYSTEM
        Kinetic  constants
                                                           Substrate parameter
            BOD
                                    COD
oo
        Yield  coefficient,Y
Decay constant, kd

Maximum substrate
   removal velocity„
 0.922
(mg MLVSS produced)
(rag BOD  removed )
                                            0.027 day
                                                     -1
                                            4.13
      (mg BOD removed)
       (mg :TLVSS)(day)
 Q 32g(jng MLVSS produced)
      Gng COD removed)


-0.023 day"1


      (mg COD removed)
                        8.35
                                                                                (mg  MLVSS)(day)
        Maximum specific
           growth rate,  \i

        Half-saturation
           constants,  K
                      s
                                                     -I
 3.81  day
26.4   mg/1
                                        -1
                        2.74  day
                       94.9   mg/1
       Nonbiodegradable  substrate
           concentrations,
                              19.9   mg/1
-------
                               Table 12.  ACTIVATED SLUDGE PROCESS KINETIC CONSTANTS
oo
Source
Heukelekian
Gram
Stack
Servici-Sogan
rtcWhorter-
Heukelekian
Eckho f f -Jenkins
Eckenf elder
Dryden
Haas-Pearson
Jenkins-Menar
Hopwood-Downing
Gram
Jenkins-Garrison
Eckhoff-Jenkins
MiddJebrook et al.
Reference
26
30
33
34
35
23
12
36
32
25
24
30
38
23
28
* . -1 K ._
q^ day s^ mg/1
Substrate BOD BOD
Domestic sewage
Skim milk 5.1 100
Glucose 3.0 355
Carbohydrates
Domestic sewage
Synthetic sewage
Pharmaceutical
Chemical
Domestic sewage
Domestic sewage
Domestic sewage
Domestic sewsg©
Domestic sewage
Domestic sewage
Domestic sewage
Y kd ,
SOD COD day"'1
0.50 0.055
0.48 0.045
0.42 0.087
0.34
0.33
0.46 0.08
0.645 0.37
0.77 0.2
0.45 0.05
0»53 0.33 0.001 - 0.015
0.97
.0.53
0.32 0.04
0.33 0.05
0.34 0.016
-------
Yield Coefficient—The yield coefficientB Ys defined as activated sludge
produced per unit of substrate removed, was found in this study to be
0.922 (mg MLVSS produced)/(mg BOD removed) and 00328 (mg MLVSS produced)/
(mg COD removed).  These yield values are in excellent agreement with yield
coefficients reported by many workers (References 22, 23 and 24), viz.,
6.50  to 0.97  (mg MLVSS  produced)/(mg  BOD removed) and 0.32  to  0.46
 (mg MLVSS  produced)/(mg COD  removed).  Middlebrooks  
-------
due to small magnitude  of  the decay  term,  (4) varying decay rat® as a
function of specific growth rate and temperature and (5) analytical
error,
Maximum Substrate Removal  Velocity and Maximum Specific Growth Rat_e°-The'
maximum substrate removal  velocity,  q, is  a growth constant calculated
from the M±chaelis=Menten  (Monod) kinetic  model and relates to maximum
specific growth rate, y =  YPO  Very  few workers have employed the
Michaelis-Menten  (Monod) equation in activated sludge kinetic analysis
                                     A     A
and therefore there are few imported q and M values „  Gram's data
(Reference  30) permit estimation of  a q of 3.0 (mg BOD removed) / (tag solids)
(day) and Benedek and Horvath (Reference 31) reported a q of 506 (mg COD
removed) / (mg solids) (day) .
    In this study, the  Michaelis-Menten (Monod) equation regression anal-
ysis yielded estimates  of  qB viz0, 4.13 (mg BOD removed)/(mg MLVSS)(day)
and 60 35 (mg COD removed) /(mg MLVSS)(day)0 The corresponding values of
maximum specific growth rates were 308l and 2.74 day  „ respectively 0
Theoretically, values of p calculated on a BOD or COD basis should be
identical.  The values  of  qrrir. and wrr.n  based on COD appear to be slight-
                                     \s UIJ
ly below expected values.   Comparing  the  daily steady-state  substrate
removal velocities  (see  Table 6) with the corresponding  values  of  q0 it
appears that  it was  possible to operate this  activated sludge system at
a very high growth  rate  (note especially  Steady=State Periods 7 and 9,
Table 6)0
Half-Saturation Constant and Nonbiodegradable Substrate  Concent rgttlon — •
The half-saturation constant, K „  is  the  limiting substrate  concentra~
                                8
tion which can support activated sludge growth at half the maxisaum growth
rate.  Again, very  limited information is available in the literature on
K  values for activated  sludge systems.  Pearson and Haas  (Reference  32)
 s
reported their best  estimates of K values of 80 (mg BOD) /I  and 225 (mg
COD) /I for the Whit tier  Narrows conventional  activated sludge plant 0
    From regression analysis of the Michaelis-Menten (Monod) ®quation0
the Kg in this study ware found to be 26.4 (mg BOD)/1 and 940S>  (ag COD)/i
Comparison with Kg  verlues reported by Pearson and Haas indicate® tha£  the

                                  86
-------
ratios of K  values from the two studies based on BOD (0.33) and COD
           s
(0.42) are very close.  It should be noted that the K  value is specific
for different waste characteristics, different environmental factors and
different activated sludge systems.  The relatively low values of K _.-
                                                                   SoUL)
and K _» indicate that both BOD and COD are adequate substrate parameters,
although BOD appears to be a better parameter than COD,  It also appears
that the organic substrate concentration expressed as BOD or COD was the
rate-limiting factor in the accelerated high-rate activated sludge system.
    In the modified Michaelis-Menten (Monod) equation (Equation 34), a
certain amount of COD is assumed to be nonbiodegradable in the system*
The nonbiodegradable COD concentration is specific for each organism
(activated sludge) and wastewater.  For the accelerated high-rate system
treating the wastewater from the City of ChinoB the nonbiodegradable COD
concentration is estimated to be about 20 mg/1.

SYSTEM KINETICS WITH OXYGEN TRANSFER

    The oxygen transfer requirements of an activated sludge system can
be expressed as the sum of oxygen  consumption for substrate utilization
and the oxygen requirements for sludge oxidation as follows;

                            U - aqX  + bk                            (38)
where     U  =  rate  of oxygen consumption
          a  =  oxygen requirements  per  unit  substrate removed
          b  =  oxygen requirements  per  unit  cell  oxidized
          q  =  substrate  removal velocity
          k. =  endogenous respiration rate
          X. =  mixed liquor  volatile suspended  solids concentration.

     To estimate the  quantity of oxygen  transferred  to the mixed  liquor
by the mechanical aerator,  the relationship  between oxygen  transfer rate
and aerator  power consumption should be identified. The oxygen  transfer
                                    87
-------
 rate is & function of the oxygen transfer coefficient,, the jpwes coasussp-
. £ion0 tejBBZKsrEfcuE1® sad the dissolved oxygen concentration gj?®di©a£ afc £h<2
 interface sad isa £h® bulk ©ix motor  efficiency
               k  s oxygen transfer ratep mass  0^  transferred/power inp.uto.
 For the EIMCO-SIMCAR aerators „  the gear  reduction efficiencyD  C,s  is
 approximately 0094; the motor efficiency is approximately 00925  and the
 oxygen transfer  rate Has  estimated to be in the range from 00610 to
 2»13 (kg 02)/(kw-hr consusaed)   1105  to 305 (Ib 02)/(hp-hr consumed)]
 (Reference 39).  '
     Based on several assumed values  for  the oxygen transfer capacities
 of the EIKCO-SBCCAR aerators such  as 0092,, 10220  10520 1083 ©nd 2013
 (kg 02)/(kw-hr coasisaed)  [loS,,  200,  2050 3»0  and  3»5 (Ib 0^ transferred)/
 (hp-hr consusasd)3 p the estiraated values  of the aeration coefticierats "a"
 and "bk " are susg^arised  in Table  13» Th® "a" values ranged from 0013.)
        d                                                  "•
 to 0«304 (rag 02)/{mg COD  removed)  or 0,328 to 00766 (mg 02)/(iag SOD re-
 moved) and the "b&d" values ranged from  0.311 to  00755 (mg 02)/(mg MLVSS)
                   . t
-------
                    Table  13.  OXYGEN  TRANSFER KINETIC CONSTANTS IN AEROBIC BIOLOGICAL PROCESSES
oo
vO
Substrate
Skim milk
Domestic sewage
Pr.iu and paper
Chemical
Kraft pulp
Domestic sewage
(this study)
11
it
it
11
Source
Gram (Reference 30)
Downing (Reference 40)
Eckenfelder (Reference 12)
Dryden (Reference 36)
Hazeltine (Reference 37)
Assumed oxygen transfer rate
2.13 (kg 02)/(kw-hr)
1.83 (kg 02)/(kw-hr)
1.52 (kg 02)/(kw-hr)
1.22 (kg 02)/(kw-hr)
0.92 (kg 02)/(kw-hr)
"a"
BOD COD
0.40
0.50
0.52
0.35
0.50
0.766 0.304
0.657 0.250
0.548 " 0.217
0.438 0.174
0.328 0.130
"hlf "
BOD
0.065
0.100
0.089
0^20
0.10
0.755
0.647
0.540
0.432
0.324
day
COD
_
-
-
-
-
0.725
0.62
0.518
0.414
0.311
-------
    Many workers (Seference© i20  30 and 40) have reported 'V md "bk.90
                                                                      &
values on a SOT  baoi®.   The typical values obtained fosr fchs coefficient
"a" range 2ro®-0-033 to 0080 (sag 02)/(tag BOD) for difftuserafc ©yafchefcic
substrates and Oo5  (tag 09)/(m§ BOD) for domestic semge (Inference 41).
                         A
Unfortunately 0. ©d published information is available for co©££ici©a£ ""a1"
values based on,COD as substrate  parameter.  Meanwhilep £hs: reported
"bk," values raag©  fgota 0,065 to  002 (mg .0»)7(mg MLVSS)(day)0
   Q             4                          &
ing to "b" value® of 100 to 1.44  (mg 02)/(tag MLVSS) „
    Comparing  the calculated "a"  and "bk," values with th© s©poirt©d
in Table  13B itxappears that "a"  and "bkd" values of 0.438  (sag 0'2)/(®g BOD
removed)  and 00<|32  (sag 0,)/(mg MLVSS) (day) 8 respectivelyB based on an
                <*•        «•
oxygen transfeffkrate of 1»22 (kg  02)/(kH=hr consumed) [2.0 (Ib 07)/(hp-hr)]
are close to reported values.  Table 14 presents the estimated oxygen trans-
fer rates based  upon 1022 (kg 02)/(to-hr consumed) [200 (Ib 0
transfer  rate  sn\d substrate (BOD.and COD) removal velocities0  this
of oxygen transferred ranged from 00210 to i096 (mg 02)/(mg MLVSS)(d©y)
and is a  linear  function of substrate removal velocities'g <5BOjj and <5COD9
as shown  in  Figures 18 and 19 0 respectively0
    Ths "bk."  values estimated from this study are high coaparod with
           Cl   *^
values reported1-'in  the literature 0  There are several explamsfciotas for
the high  "bk.1" valuess  (1) the assumed ossygen transfer coeff£c£emt oif
0.92  to 2.13 (kg 02)/(kw-hr)  [105  to 3»5  (Ib @2)/(hp=hr)] is sa over°
simplified  assumption because  the  oxygen  transfer  coefficient is not COSB
stant and is  a 'function of aerator type0  temperature and. oxygen conceta=
                 't                  •
tration gradient between the interface and in the mixed liquor g (2) this
negative  value of decay rate0  k.„  may influence the ordinate intercept
(bk,) of  the oxygen requirements equation (Equation 38) j and (3) the
decay rate  may vary with substrate removal rate or with specific growth
               } *
rate  such that  the assumption  of a linear relationship between oxygen
                >
requirements and substrate  removal rate  is questionablep especially ©t
low  rates o       ,-
                                     90
-------
                             Table 14.  OXYGEN TRANSFER KINETIC DATA AND SLUDGE VOLUME INDEX
ve
ec
16Dec70
17Dec70
18Dec70
19Dec70
20Dec70
21Dec70
31Dec70
2Jan71
3 Jan 71
5Jan71
15Jan71
16Jan71
17Jan71
18Jan71
15Apr71
16Apr71
18Apr71
19 Apr 71
9May71
1 l^lay 71
12May71
13May71
14May71
16May71
Power
II&&© ^£ui|p t£ «L OKA p
_
-
-
—
-
-
- '
678
654
677
794
567
670
719
489
478
562
384
432
460
477
459
475
441
T®rap@r©£<
•c

—
—
-
-
-
—
—
_
-
_
_
_
-
19.5
20.0
18.0
18.5
20.0
20.5
20.5
20.0
20.0
20.0
BOD removal
velocity s q,
ares, (mg BOD removed)
(mg MLVSS)(day)
0.281
0.278
0.366
0.104
0.176
0.242
0.312
0.173
0.172
0.18.4
0.25?
0.296
0.268
0.31'V
0.250
0.260
0.206
0.178
0.613
0.593
0 = 942
0.725
0.572
0.423
COD removal
velocity s q,
(mg COD removed)
(mg MLVSS)(day)
0.347
0.329
0.234
0.249
0.257
0.291
0.367
0.560
0.451
0.560
0.542
0.551
0 . 305
0.270
0.619
0.676
0.592
0.783
1.20
1.49
2.04
2.26
1.90
1.28
Oxygen transfer
rate, U,
(og 02)
(mg HLVSSHdayJ
JIL
. -
-
-
-
-
-
0.294
0.303
0.243
0.255
0.210
0.239
0.231
0.490
0.590
0.669
0.491
0.818
0.915
0.940
0.777
0.919
0.785
Sludge
volume
index
_
-
-
-
-
-
-
293
2'J2
251
234
233
257
.252
87
90
93
169
189
226
227
229
176
207
-------
Table 14 (continued).   OXYGEN TRANSFER KINETIC DATA AND SLUDGE VOLUME INDEX
Bae©
16Msy71
17May71
18May71
19May71
20May71
21£2sy71
23£3ay71
24May71
^ Cl^9 A W 7 1
^ jpjUfl y / i
28May71
29May71
16Aug71
17Aug71
20Aug71
23Aug71
24Aug71
25Aug71
26Aug71

29Aug71
30Aug71
31Aug71

f
BOB removal
. COD removal
velocity o q0
) -(tag; COD r-esaow
• °^s£rrf e;
r
Sludge
fe^=te ° i®d©s
441
470
471
457
488
474
446
446
464
473
• 464
372
382
377
380
435
425
433
543
363
448
. 478
20.0
20 J)
20.0
20.0
20.0
20.5
20.0
21.0
21.0
20.0
20.0
26.0
26.0
. 25.0
24.0
25.0
24.5
24.5
23.0
24.0
24,0
24.0
0.423
0.485
0,504
0,449
0..567
0.693
0.754
0.718
0.812
0.519
0.625
1.41
1.01
1.25
1.78
1.62
1.73
1.96
1.64-. .
1.29
1.15
1.54
1.28
1.42
1.71
1.53
1.B3
2956
0.96
1.66
1.78
2.76
1.76
3.42
2.37
2.70
3.63
3.15
3.18
3.20
. . 3.53
2.74
2.60
5.23
0.785
0.835
0.908
0.769
0.862
0.796
0.696
0.676
0.813
0,807
0.859
9,834
0,748
0.900
0.902
1.22
1.03
1.07
1.21
0..89
loOO
1.11
207
218
204
' 217
200
213
206
184
193
206
196
72
87
113
124
88
100
121
168
• '175
138
365
-------
                         Table 14  (continued).  OXYGEN TRANSFER KINETIC DATA AND  SLUDGE VOLUME  INDEX
u>
Power
consumption
Date kw-hr
5Sep71
6Sep71
9Sep71
115ep71
12Sep71
13Sep71
14Sep71
16Sep71
17Sep71
19Sep71
20Sep71
28Sep71
29Sep71
10ct71
30ct71
40ct71
50ct7l
60ct71
70ct71
90ct71
100ct71
110ct71
484
281
374
372
389
398
382
387
375
392
374
365
371
400
390
440
395
426
414
383
395
388
BOD removal
velocity, q,
TesjperatureB (mg BOD removed)
°C
23.0
23.5
25l5
24.0
25.5
26.0
26.0
25.5
25.5
23.5
24.0
23.5
23.0
23.0
22.0
23.0
23.0
23.0
23.5
23.0
23.4
23.5
(mg MLVSS)(day)
1.71
1.50
1.43
1.05
1.73
1.46
1.86
1.78
1.78
1.22
1.30
3.21
2.24
2.90
2.50
1.61
2.24
2.08
1.74
2.10
2.06
2.95
COD removal
velocity, q,
(mg COD removed)
(mg MLVSS)(day)
3.07
3.07
3.37
3.44
4.08
4.20
3.94
3.87
3.08
3.12
3.26
5.96
5.88
10.2
5.40
5.73
6.64
5.86
6.19
7.52
5.55
7.24
Oxygen transfer
rate, U,
(mg 02)
(mg MLVSS)(day)
1.03
0.671
0.970
1.09
1.09
1.27
1.02
9.978
0.699
0.928
0.862
1.49
1.35
1.36
1.65
1.85
1.73
1.70
1.57
1.96
1.62
1.76
Sludge
volume
index
412
323
171
168
184
199
272
935
549
577
463
581
483
434
756
724
826
708
696
283
707
808
-------
                        Table 14 (continued).  OXYGEN TRANSFER KINETIC DATA AND SLUDGE VOLUME  INDEX
VO
Power
consumption,
Date kw~hr
9Nov71
10Nov71
14Nov71
23Wov71
24Mov71
25Nov71
26Nov71
29Nov71
2Jan72
5Jan72
6Jan72
8Jan72
10 Jan 72
12Jan72
390
413
388
408
408
408
391
378
381
393
394
379
378
377
BOD removal
velocity , q,
Temperature 0 (mg BOD removed)
°C
21.0
21^0
21.0
20.0
20.0
20.5
20.0
21.0
18.0
17.0
17.0
18.5
18.0
18.0
(mg MLVSS)(day)
0.697
0.762
0.696
0.990
0.815
0.900
1.03
0.778
2.83
1.76
2.34
1.50
1.88
1.78
COD removal
velocity p q»
(mg COD removed)
(mg MLVSS) (day)
2.29
2.16
2.14
2.63
2.74
2.34
2.56
2.10
8.57
5.69
5.24
6.06
4.64
5.21
Oxygen transfer
rate, Us Sludge
(mg D£) volume
(mg W.VSS)tday
0.511
0.541
0.659
0.843
0.926
0.740
0.821
0.916
1.37
1.77
1.32
•1.55
1.69 '
1,17
) index
104
86
422
71
93
110
146
276
=
39
39
25
35
33
-------
tao
 CM

C3


 t>0
                                 a = 0.438 (Rig




                                 bkri =0.432 (mg 07)/(rog IU?SS)
                                   U o          i
                             VELOCITY  a     (tag  JOB  removed)
                                     i  TO* iRip*  V™ " ™*  Rtrir II/Aif"^T™™7TT^^^TC
Figure  IS   Re I at ionslnip
                                            oiiygso  transfer

                                   removal  velocity
                                   95
-------
=3
o
SO
 Cry.
es
(VAJ)
(UL,
c=
ivn
• = 8.1M (Bg B2)/(B| S8B
    = 0.414 (si 02)/(Q8
           '(B-= f.PI)
-------
NUTRIENT REQUIREMENTS AND REMOVAL
    In addition to organic substrate (carbon source), organisms require
a complex set of nutrients and micronutrients for cellular growth-  The
principal nutrients required for activated sludge are nitrogen and
phosphorus.  Therefore, nitrogen and phosphorus requirements„ removal
efficiencies and removal velocities are of primary concern in activated
sludge process analysis.
    Table 15 presents data on the total and dissolved nitrogen species
(Kjeldahl, ammonia, and nitrite and nitrate) and phosphorus species
(total phosphate and orthophosphate) in the primary  and secondary effluents^
Nitrogen
     The concentrations of various total and dissolved nitrogen species
(Kjeldahl, ammonia, and nitrite and nitrate) in the  primary and secondary
effluents were relatively constant during  the 15-month study period, as
shown in Table 15„  Average total and  dissolved nitrogen  concentrations
in  the primary and secondary effluents are summarized in  Table 16„
Kjeldahl nitrogen represented 99„8 percent or 38.8 mg/1 as N of the
average total nitrogen content  (38.9 mg/1  as N) in the primary effluent,
and consisted of 59.2 percent ammonia  (23.0 mg/1 as  N) and 40.6 percent
organic nitrogen (15.9 mg/1 as  N)„  The average dissolved nitrogen  frac-
tion in the  primary effluent  (33.6 mg/1 as N) was approximately 86,4
percent of  the total in which 86,2 was dissolved Kjeldahl nitrogen, which
consisted of 59.2 percent ammonia  (23.0 mg/1 as N) and 27 percent organic
nitrogen  (10.6 mg/1 as N).  Only minor amounts of combined dissolved ni-
 trite and nitrate  (0.08 mg/1  as N) were present in the primary effluent.
In  the  secondary effluent,  average  total Kjeldahl nitrogen  (29,9  mg/1  as  N)
comprised 97,1 percent of the total nitrogen  (30.8 mg/1  as N)0 and  average
dissolved Kjeldahl nitrogen (27,9 mg/1 as  N) comprised 9006  percent of the
 total nitrogen.  Ammonia  in the secondary  effluent was present totally as
 dissolved  ammonia  (20.9 mg/1  as N).   The average  dissolved nitrate  and
 nitrite increased  from 0.08 to  0,90 mg/1 as N.  This indicates  that a  minor
 degree of nitrification  took place  even  at the high  organic  loading veloc-
 ities and growth rates experienced  by the  system.
                                  97
-------
         Table 15 „   STEADY-STATE NITROGM AS® PHOSPHORUS
KJoldohl
ofterosen « eg ' 1 oo K
Date
16Dec70
17Dec70
180ec70
190GC70
20Dsc70
210QC70
31D@c70
2Jan71
3Jan71
5Jan71
15Jan71
16Jan71
17Jan71
18Jan71
15Apir71
16Apr71
18Ap?71
19Apr71
9Say71
IVlayTl
12May71
13May71
14May71
16May71
17May71
18Hay71
19May71
20May71
2 Way 71
23May71
24May71
25May71
26May71
29May71
16Aug71
17Aug71
20Aug71
23Aug71
24Aug71
25Aug71
26Aug71
28Aug71
29Aug71
30Aug71
31Aug71
A
27.1
38.1
44.0
33.3
38.9
37.6
39.9
30.3
34.7
38.0
47.1
50.4
43.8
31.8
40.3
41.8
37.5
40.0
35.1
37.5
44.3
51.7
43.8
37.5
38.2
40.2
40.8
40.8
46.3
42.0
40.2
39.6
45.7
37.7
38.4
35.3
37.1
36.5
35.3
38.4
37.1
38.9
24.8
34.0
45.2
a
.
-
-
-
-

-
_
-
-
-
-
- .
-
_
-
-
-
_
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
32.3
31.6
30.9
35.3
31.5
34.7
32.2
- .
24.1
29.1
34.0
C
31.0
36.2
38.9
31.8
31.1
30.5
31.4
33.2
32.4
25.3
42.4
33.2
30.5
36.5
_
-
-
-
27.1
27.7
24.6
28.9
34.1
28.8
29.8
28.0
30.4
29.8
31.7
26.8
29.8
29.8
31.7
28.6
30.3
27.8
27.8
30.3
27.8
30.3
25.4
27.2
30.3
30.3
27.2
0
34.2
38.1
47.3
33.8
31.8
32.4
30.7
30.7
31.4
28.0
33.8
31.8
28.5
31.8
31.5
32.0
28.9
28.3
25.8
27.1
23.4
28.3
31.7
27.7
29.6
28.0
28.6
29.8
29.2
26.8
30.4
28. &
28.0
25. 6
22.9
23.3
24.3
24.8
23.5
22.9
21.7
24. S
25.4
26.6
26.6
E3R/1 OS W
A
23.3
21.3
23.6
21.0
23.3
18.8
32.2
25.7
23.7
27.6
28.6
20.9
25.6
21.6
23.9
•>
24.9
-
22.2
-
-
23.1
-'
24.0
-
-
-
23.6
-
23.4
-
- ..
'. =
—
c,
•-
«•
-
-
-
22.0'
-
21.7
-
-
C
24.2
28.1
29.4
23.0
23.0
_«.
20.7
25.0
23.7
22.7
20.9
22.9
16.9
18.6
23.0
-
23.1
-
20,3
=
-
19.1

22. 0
-
-
-
21.6
-
21.3
-
-
-
-
_ .
-
-
-
-
-
17.0
•=•
17.0
-
-
D
24.7
28.4
29.4
23.0
23.3
21.7
22.1
24.3
24.1
23.6
22.6
23.6
17.3
17.9
23.3
- »
23.1
-
20.0
-
-
16.6
-
22.5
-
-
-
21.6
-
20.4
-
-
-
-
_
-
-
-
-
-
17.9
-
16.4
-
-
Hit
a&
OB/1
B
0.04
0.01
0.00
0.02
0.25
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.30
0.11
~
0.00
-
0.00
=
—
0.01

0.01
-
-
-
0.00
-
-
-
-
-
-
•
-
-
-
-
-
0.04
-
0.00
-
-
ffGfce 6
EiiEQ D
as N
0
.
-
-
-
-
»
0.00
0.50
0.00
0.66
1.23
2.11
1.61
1.16
0.11
-
0.00
-
0.03

-
0.04
-
0.49
-
-
-
0.002
-
-
-
-
0
-
—
-
- -
-
-
-
0.67
-
0.84
-
-
Uoeol Ktocfjhoea o
OQ/I as P
~S
11.8
10.3
1@.@
15.3
20.0
21.5
20.0
23.3
16.0
15.4
18.5
19.0
27.5
24.0
18.8
23.0
20.8
17.3
10.3
10. S
17.8
24.0
23.0
13.3
21.0
21.5
22.0
20.0
20.0
21.0
20.0
13.3
13.8
23.0
24.3
20.0
13.8
15.8
16.5
23.8
19.0
19.3
17.5
20.0
20.0
tf C
17.6
° 20.S
- 13.0
- 14.0
- 17. @
- 13.8
'- 16.0
- 17.3
- IS .8
- 18.7
- 3$.S
- 19.0
- 21.0
- 22.0
- is. 8
- 15.3
- 14.5
- 13.3
CS> <30
- 13.8
'- 12.5
S.3
14.8
- 13.3
- 21.0
- IS. 3
- 14.8
- 14.3
- 14 o5
- 11.5
•- 13.0
- 12.0
- 12,8
- 14.8
22.0 18.8
20.0 13.3
11.8 12.3
13.4 13,0
15.8 15.1
23.0 17.3
19.0 19,5
17.0 11.0
1&.9 14. Q
20.0 13.1
20.0 13.3
y
._
»
13. Q
12. Q
217.0
13.3
16.0
13.3
IA.Q
18.2
22,5
16,3
17,0
19,0
17,5
2J.S
12,3
13.0
9.3
IX©
8.3
7,3
14, S
14.3
18, S
13. Q
13.3
11.5
13.8
8,4
14.3
§.@
9.5
12. §
16.9
13.3
11.0
12.7
12.8
11.3
14,4
10.9
11.3
11.8
12.4
 Total  in primary affluent .

B
 Dissolved in primary affluent.
Total in secondary effluent.


Dissolved in oscondory effluent<
-------
     Table  15 (continued),   STEADY-STATE NITROGEN AND
                PHOSPHORUS CONCEOTuATIONS
Orehophosphate»
   mg/1 as P
 B       D
 Mixed lic-jor
    total
   nitrogea
Dg/1 as NST
 Mixed liquor
     total
   phosphorus,
ag/1  as Pf~
9.0 15.5
10.0 12.0
17.0 11.0
16.0 12.5
12.0 11.5
-
11.8 9.4
-
_ _
-
-
-
-
-
-
-
- •
12. 1 7.6
-
9.4 6.9
-
-
»
-
«.
-
-
-
-
-
10, 1 S.6
-
9.1 9.1
-•
-
364
309
276
248
430
372
374
362
273
247
271
311
267
276
280
255
284
237
276
258
264
248
283
249
241
277
220
241
246
243
244
276
215
246
233
10.6
10.4
9.0
7.3
10.0
10.7
10.4
10.8
12.0
11.5
12.4
12.3
12.0
11.4
11.6
11.4
U.I
9.7
10.8
9.4
9.3
10.1
11.2
10.7
12.6
12.6
12.2
13.3
16.0
13.0
14.1
14.2
12.3
12.7
12.7
54.5
18.0
67.5
81.0
120
102
161
144
165
80.2
186
107
70.0
101
88.7
95.5
105
99.2
128
90.2
56.2
61.0
101
101 .
53.2
122
69.7
36.1
40.5
74.5
51.0
71.5
130
101
71.2
i.e
0.61
2.2
2.C
2.E
2.9
4.4
4.3
7.5
3.7
8.5
4.2
3.2
4.2
3.7
4.3
4.1
4.1
5.0
3.3
2.0
2.5
4.0
4.3
2.8
5.6
3.9
1.0
2.6
4.2
2.9
3.7
7.4
5.2
3.4_
                             99
-------
Table 15 (continued),,  STMDY-SE&TB MISS0GHH MB
          PHOSPHOKUS COBSCPWS&SIONS
Kjcldohl AcnijaiaD aitsite,,
aittfOKQn. as/ 1 ao H
Bato
SSsj>71
6Sap71
9Ssp71
IS. Sop 71
13S3p71
13Sap71
14§@p71
IS Sap 71
17Sop71
lSSap71
20Sap71
28Sag>7!
2iSap71
10ee71
30c£71
40ce71
30ct71
60ce71
7Cce71
S0ce71
X00ce71
Il0ce7l
9Hov7i
10Hov71
14Rov71
23Hov71
24KoWl
258&W71
26Kov71
29Ko^71
Uaa72
2Joa72
SJosa72
SJon72
SJoa72
16Joa72
12Joia72
*»««.
\oeol
A
33.1
31.8
33.7
33.1
36.2
32.4
31.1
32.4
42.6
29.2
30.3
36.9
36.3
61.1
36.3
33.6
35.6
36.3
39.3
36.3
33.7
36.3
44.1
41.4
43.0
39.7
38.1
43.0
44.4
37.7
42.3
43.3
39.9
46.6
41.1
41.7
49.0
33.8
in guric
B
25.4
.30.5
30.3
29.2
•29.2
23.6
28.6
28.6
38.8
26.7
29.9
33.1
24.4
41.1
33^7
32.5
32.3
33.7
3^.4
31.2
30.5
31.8
39.2
38.1
35.3
35.9
33.6
39.2
37.7
34.1
33.1
34.3
33.7
40.3
33.3
41.7
47.8
33.3
C
23.5
27.3
22.2
25.4
24.3
27.2
22.9
25.4
26.7
21.6
27.3
29.2
31.2
31.8
24.2
26.7
26.1
27.4
26.7
31.8
24.8
23.5
35.9
31.4
31.6
30.9
31.4
32.5
35.9
31.7
31.4
33.3
36.3
36.9
32.7
38.1
38.7
29.9
9
21.6
24.8
21.0
22.2
20.3
24.2
21.6
23.5
25.4
21.6
24.2
24. 8
28.0
30.5
24.2
21.6
25.3
27.4
26.7
26.7
22.9
24.8
33.1
28.1
28.1
28.1
27.0
28.1
33.5
29.8
26.0
29.0
29.6
31.4
29.6
32.1
36.9
27.9
airy G?21uene.
Mooolvod in prieJK
y sfOuenfc.
os/1 ao B ea/1
A
20.3
=
•>
~
19.4
-
-
19.4
-
16.1
=
24.8
-
c,
22.6
-
-
=
23.9
0 .
22.3
-
—
-
24.8
=
=
25.1
-
0
_
23.0
_
23.1
.
. =
-
23.0
C
16.3

-
-
16.8
-
-
16.3
-
13.9
-
21.0
-
„
19.7
-
_
=
19.4
-
17.5
-
—
_
21.0
_
-
20.4
-
-
_
19.1
=
20.6
_
-
-
20,9
CToeol in
9 B
15.9 0.03
_
= 0.02
= . =
17.2 0.3S
_
*.
18.4 0.31
= =
16.3 0.21
«
21.0 0.00
= =
_ <=
19.7 0.22
.
o = '
0 = .
19,1 0.32
= »
16.2 0.66
_
^ «»
_ =
21.0 0.00
= =
=
20.4 0.00
_ =
= =,
• - =
19.1 0.09
- =
20.3 0.00
• <. =
= =
«,
20.9 0.08
oecoadosy o
. as M
9
0.79
'-
1.41
-
l.GO
=
o
0.27
•=•
1.22
- •
-
-
„
1,44
-
=
=
2.76
=
4.23
-
.—
-
0.63
=
=
1.32 •
-
_
=
0.83
-
0.48
<=.
=
=
@.90
Q2 lu3EB£.
to£a£ pboophaee,,
£20/1 QB.P
A
13.3
21.0
23.2
17.8
15.8
13.3
13.8
12.0
16.8
18.3
16.8
11.3
26.5
23.0
13.3
IS. 3
18.3
13.0
14.0
16.3
16.3
17.3
17.3
17.3
22.4
13.3
11.2
16.3
13.3
13.3
14.3
13.3
7.1
9.7
W.4
17.3
11.2
17,8

u
14.3
18.3
21.0
17.3
13.8
13.8-
14.8
9.0
13.3
18.3
16. §
10.5
18.3
i3.a
12.3
14.3
13.0
13.0
14.0
. 14.®
12.8
13.3
14.3
14.3
20.4
12.2
11.2
14.3
12.2
14.3
11. 2
9.2
7.1
6.3
13,3
10.2
ll.2
14.0

C 9
3.4 6.8
17.8 14.4
25.2 13.4
17,8 14.7
13.8 11.3
16.3 16.0
13.3 13.1
11.5 10.8
12.0 9.S
14.3 9.4
11.3 O.O
13.5 11.3
23.3 16.8
11.5 11.5
11.3 10.8
14.3 12.3
11.0 11.0
9.0 9.5
9.0 8.5
11.5 11.0
12.3 13.8
12.3 12.8
12.8 11.5
13.0 13.0
11.3 11.3
13.5 13.3
13.3 12.3
.14.8 11.8
12.8 13.3
13.8 13.8-
9.7 9.2
Aio2 JiAoW
8.3 f>.2
8.2 7.4
12.2 11.7
12.2 11.8
13.8 7.6
14.7 12.9

B ''
Biooolved in oocCTitoiry oSfflKaae.
                100
-------
Table 15 (continued).   STEADY-STATE NITROGEN AND
          PHOSPHORUS CONCENTRATIONS
Mixed liquor
Orthophosphate, total
mg/1 as P nitrogen.
B
12.5
—
11.8
_
12.5
_
_
9.4
_
10.8
-
_
-
—
13.0
-
-
-
10.8
-
13.8
—
_
-
8.9
-
-
7.4
-
-
-
13.3
-
7.9

-
-
D mg/1 as
9.1 238
228
9.1 294
232
7.6 184
189
211
9.1 216
283
9.6 " 217
245
136
146
190
9.1 134
124
131
146
8.4 134
149
11.0 132
116
333
334
9.2 an
240
240
8.9 275
233
- • §08
130
10.7 119
123
5.9 131
123
122
149
N Z
-1.8
12.7
17.7
15.8
12.0
14.0
13.1
12.7
16.7
11.9
13.2
14.8
12.3
15.1
13.3
12.2
13.3
13.6
13.6
17.7
12.5
12.3
10.2
13.2
10.7
11.6
. 12.6
11.6
11.3
11.7
10.9
11.5
12.9
11.8
11.7
12.7
10.8
Mixed liquor
total
phosphorus.
mg/1 as 1
45.7
70.2
89.5
81.5
108
43.0
45.5
53.5
49.6
62.3
61.8
30.0
32.6
79.5
47.0
50.2
31.3
37.0
42.2
28.0
41.7
28.7
66.4
39.2
37.2
58.9
63.4
34.1
31.0
42.8
35.8
33.6
22.0
36.8
37.7
35.2
36.8
> ;.
2.3
3.9
5.4
5.5
7.0
3.2
2.8
3.2
2.9
3.4
3.3
2.S
2.7
<§.3
4.6
4.9
3.2
3.4
3.7
3.3
4.0
3.0
2.0
1.6
2.3
2.8
3.3
2.6
2:3
2.4
3.0
3.1
2.3
2.9
3.5
3.7
2.5
   11.3      9.62          12.2              3.6
                      101
-------
             Table 16.  AVERAGE NITROGEN AND PHOSPHORUS CONCENTRATIONS IN PRIMARY AND SECONDARY EFFLUENTS
o
N>
Nutrient
• * . \.t
Nitrogen
Total Kjeldahl nitrogen
Dissolved Kjeldahl nitrogen
Total ammonia nitrogen
Dissolved ammonia nitrogen
Dissolved nitrate and nitrite nitrogen
Total dissolved nitrogen
Total nitrogen
Phosphorus
Dissolved orthophosphate
Total dissolved phosphate
Total nhosrahafta
Primary effluent
Concentration^
mg/1 as N

38.8
33.5
23.0
- •
0.08
33.58
38.88

11.3
14.8
17.8
Percent,
%.

99.8
86.2
59.2
- . '
0.2
86.4
100.

63.5
83.2
100
Secondary
effluent
Concentrationp Percent,
mg/1 as P %

29.9
27.9
20.9
20.9
0.90
28.80
30.8

9.62
12.9
14.7

97.1
90.6
. 67.9
67.9
2.9
93.5
100

65.4 .
87.7
100
-------
     Nitrogen removal by the activated sludge process is accomplished by
the synthesis of nitrogen in the activated sludge and possibly by deni-
trification.  It is assumed that both the dissolved and particulate nitro-
genous forms in the primary effluent are available for biosynthesis.
Because most solids in the secondary effluent are biological cells, excess
nutrients are assumed to be present only in soluble forms.
    Table 17 presents the nitrogen removal efficiencies and removal vel-
ocities of various nitrogen species.  Removal efficiencies for the various
nitrogen species were relatively constant when the system was operated
at high rates.  However, the removal efficiencies varied widely when the
system was operated at low rates, i.e., 1/6C » 0,036 to 0.071 day"  .
Approximately 27 percent of the total Kjeldahl nitrogen and 22 percent
of the dissolved Kjeldahl nitrogen was removed by activated sludge.,
Based on grab sample measurements during a three-day period, only 8,2
percent of the ammonia present was incorporated into cell material.  It
appears that the nitrogen supply in the primary effluent was in gross     '
excess of that required for activated sludge growth| hence, nitrogen was
not the limiting nutrient in this study.
    The net yield coefficient with respect to specific nutrient can be
defined as the net amount of cells produced per unit amount of nutrient
removed s, or

                               ,    ,    FX_ + F  (X  - X0)
                  _  cells produced  =   2    wv r    2'             (   }
                n   nutrient removed       F(SQ - S^

                                    VX
 here                    6   °  py       , - rr^-                      (18)
                         c    FX2 "*" Fw(Xr  ~   2*
                                 F(SQ  -  S}
                             
-------
Table 17 „  KUMIEM 1S2QWAL VELOCITIES AS©
Dote
17Bac70
18Bac70
19 Da c 70
20Dac70
21Bsc70
31Bsc70
2Jon71
3Jon71
5Jan71
15Jan71
16Jan71
17Jaa71
18Jan7i
15Ap?71
16Apr71
18Apr71
19Apir71
9May71
llMay71
12May71
13May71
14May71
16May71
17Kay71
18ftey71
19Kay7i
20Hay71
2 Way 71
23May71
24May71
25May71
28Msy71
29Msy71
16Aug71
17Aus71
20Au871
-23Aug71
24Aug71
25Aug71
26Aug71
28Aug71
29Aup/l
30Aus71
31Aug71

' Yoeal B
KJaldehi
0°
0°.0024
6.0110
0.6086
0.0190
=0.0007
0.6064
0.0150
0.0225
0.0364
0..0286
0.
0.0. 8$
0.0240
=©.©220
0.0336
0.0559
0.@629
=0. 125
0.124
0.0712
0.0531
0.0490
0.071S
O.OS52
0.0617
0.0911
0.0753
0.0472
0.0612
0.0998
0.0741
0.202
0.134
0.162
0.157
0.180
0.218
0.222
0.195.
-OJB087
0.0933
0.253
Hue rfLi
lioBolvsd
Kjeldahi

c,
-
=
-
«-•
-
0
=
=
=
=
=
-
-
-
-
-
0
-
-
=
-
-
=
•>
—
0.129
0.0921
0.0305
©.141
0.124
0.166
0.131
"
=0.0247
0.0315
©. 10&
sat soeovol
sss..
=0.0141
=0.0114
=0.0032
0.
-0.0047
0.0023
0.0025
=0.0007
0.0060
0.0101
-0.0070
0.0155
0.0062
0.0012
-
0.004®
-
0.0112
-
-
0.0343
~
0.0081
—
—
-
0.0100
-
0.0148
-
-
-
-
-
-
-
-
-
-
0.0705
-
0.0775
-
-
{q3
vole ty, (QB
Toeal
phosphate
0.0063
0.0048
0.0046
0.0295
0.0092
0.0183
0.0023
=0.0042
=0.0067
0.0049
0.0196
0.0084
0.0027
0.0183
0.0222
0.0123
O.GO&O
0.0302
0.0058
do® £03
0.0483
0.0243
0.0124
0.0431
0.0433
0.0476
0.0330
0.0624
0.023Q
0.0230
0.0524
0.0623
0.0963
0.0760
0.0369
0.0415
0.0566
0.173
0.0662
0.116
6.0906
0.103
0.104
K or P pocsrc
> MLVSS) (dCR?I
Total
dlosolved
phosphate
-
-
-
-
-
-
-
_
-
•
"
'
-
-
•
-
<*
- .
_
-
- -
-
=
-
-
-.
"
0.0660
0.0761
0.0105
0.0362
0.0439
0.162
O.OS63
0.0952
0.106
0.1036
0.1036
;a«35)
i
,=£-
I
=
=
=0.0110
=0.0039
©002.12
®.0®5S
O.QOli
=
©<,6@&6
=
=
-
. =
="
=
=
=
c.
=
O.Q252
•>
@.OH26
=
"
•*
• —
=
=
=
=
=
o
©.§21$
0
• o.
=
=
                                 104
-------
Table 17 (continued).  NUTRIENT REMOVAL VELOCITIES
              AND REMOVAL EFFICIENCIES

Nutrient
Total Dissolved
Kjeldahl Kjeldahl
nitrogen nitrogen
-26
0
-7.5
4.2
2
14
22
-1.3
9.5
26
28
37
35
0
22
23
23
29
26
28
47
45
28
26
23
30
2V
27
37
36
24
28
39
32
40
33
33
32
33
40
42
36
2.4
22
41
-
-
v
-
-
-
.
_
-
_
-
-
-
.
-
-
- •
-
--
-
_
«•
<*
~
-
"
°
=
-
30
26
20
30
26
34
32
-
i.4
8.6
22
removal efficiency, Z
Ammonia
nitrogen
-6.0
-32
-25
-9.5
0
15
4.7
5.4
-1.7
14
21
-18
32
17
2.5

7.2
-
9.9
-
-
28
-
6.2
-
-
«=>
7.7
«,
13
.=
.= '
«,
-
=
=
=
-
=
=
21
=
24
=
-
Total Dissolved
Total dissolved ortho-
phosphate phosphate phosphate
12
19
15
58
20
43
7.5
-18
-22
13
38
21
- 6.9
33
40
25
9.7
26
52
70
35
24
10
36
J/
42
31
60
26
34
49
44
30
34
20
20
22
52
24
44
35
41
38
-
-
-
-
-
-
-
-
-
-
-
-
-
.
-
•
-
-
-
-
-
—
-
-
=
-
-
-
-
23
34
6.8
18
19
50
24
39
33
41
38
-
-
-
-
-
-72
-20
35
22
4.2
-
20
-
-
-
-
-
-
-
-
«*
—
37
-
27
-
—
—
—
-
-
-
-
-
-
15
-
0.
-
-
                          105
-------
Table 17 (continued) „  MJTRIMT REMOVAL
              AKD RMOVAL EFFICIMCIES
Dots
5Sap71
6Sep71
9Ssp71
HSep71
12Sap71
12Sep71
14Sep71
16Sep?l
17Sep71
19Sep71
20Sep71
28Sep71
29Sep71
10ct71
3Oct71
40ct71
50ct71
60ct71
70ct71
90ct71
100ct71
H0ct71
9Nov71
10Wov71
14Nov71
23Mov71
2«Nov71
25Mov71
26Mov71
29Hov71
!Jcn72
2Jon72

Total
KjaWehl
0.144
0.0921
0.18?
0.188
0.232
0.149
0.145
0.131
0.234
0.104
0.0831
0.288
0.5L63
O.S23
0.286
0.342.
0.240
0.199
0.268
0.276
0.244
0.290
O.OS61
0.106
0.148
0.131
0.139
0.147
0.126
0.106
0.346
0.348
RuStrieat SSEOVO! •
DiooolvsS
KjeidaJjl Aeasaia
fflitroBea sigffogsn
0.0473 0.0549
0.0732
0. 141
0.121
0.142 0.0349
O.§300
0. 107
0.0730 0.0146
0. 199
0.0699 0.0281
0.0752
0. 1®§
0.123
0.211 - ' .
0.224 0.0684
0.26®
0. 167
0. 141
0.161 0.100
0.129
0.172 0.138
0.177
0.0478
0.07%
0.0716 0.0377
0.0394
O.OQ2Q
o. aao
0.04S3
0.0377
0.194 • -
0.132 0.0933
ifrw

Total
0.106
0.0869
0.175
0.0533
0.0713
=0.0127
0.0412
0.0176
0.103
0.122
0.076S
0.
0.203
0.230
0.106
0.146
0.174
0.123
0.115
0.152
0.0566
0.114
0.0434
0.0341
0.110
0.
-0.0138.
0.0444
0.
15). 020 1
0.108
0.0839
j N or P trecB^
Jan I3.VSS) Was?
Total
diooolvsd
0.0939
0.0314
0.1129
0.0448
0.0397
=0.0400
0.0260
-0.0264
0.0563
0.122
0.0766
=0.0190
0.0317
0.0461
0.0334
0.0437
0.0945
0.123
0.113
0.0@S2
-0.0226
0.0126
0.0219
0.0103
0.0906
-0.0124
-0.0130
0.0247
-0.0127
0.0067
0.0423
°0.0623
3«a>
)
Pto5£o
©.©423
<=
Oo®4@i
=
@.©770
=
=
0.0344

©.©iSS •
o
0
=
=
§o@f21
0. .
ca
a
0.0S03
= •
OoG^^i4
=
0
=
-a.ooss
=
c,
-*@o016f
=
=
=
@.©S2S
                           106
-------
Table 17 (continued).   NUTRIENT REMOVAL VELOCITIES
              AND REMOVAL EFFICIENCIES.

Total
Kjeldahl
nitrogen
35
22
38
33
44
25
30
27
40
26
21
33
21
50
33
39
28
24
32
26
32
32
25
32
35
29
29
35
24
21
38
33
Nutrient
Dissolved
Kjeldahl
nitrogen
15
19
31
24
30
15
2*
18
34
19
19
25
17
26
28
33
22
19
22
14
25
22
16
26
20
22
20
28
11
13
26
16
removal efficiency, %
Ammonia
nitrogen
22
-
-
-
11
-
<=•
5.1
«,
8.8
0
„
~
_
13
_
-
-
20
-
27
-
~
-
15
-
-
19
-
-
»
17
Total
• phosphate
56
31
47
17
28
-4.6
17
10
43
49
34
0
37
50
39
33
40
37
39
32
15
26
34
25
50
0
-9.8
28
0
8.8
36
23
Total
dissolved
phosphate
52
21
36
15
18
-16
11
-20
2o
49
34
-7.6
8.2
17
12
14
27
37
39
21
-7.8
3.8
20
9.1
45
-9.0
-9.8
17
-9.0
3.5
18
-28
Dissolved
ortho-
phosphate
27
'
23
-
39
_ .
=
3.2
.
11
_
_
-
_
30
„
• „
«
22
_
20
-
—
.
3.4
_
a
-20
.
-
-
20
                             107
-------
Based on these net growth expressionsp the net yield coe£ficisnts oL
various nitrogen species were  computed to be as follows;

                 v   _ii*       pan MLVSS produced)      .      '  •
                            (mg KJeldshl. nitrogen removed)
                       20  i  ,_	(mg MLVSS produced)
                            '    total ammonia nitsogen removed)
Because no nitro§©a  eaaiyses  were  made  directly  on  the  cells0 the nitrogen-
content in the  activated sludge was  estimated  from  the  difference between .
total particulate  aad dissolved nitrogen concentrations determined on  the
mixed liquoro   The calculated total  nitrogen concentrations  in  the activa-
ted sludge are  listed in Table 15„  The concentrations  varied between  7=3
and 16.8 percents  with an average  of 12.2 percent.   This  average nitrogen
content of activated sludge corresponds to a nitrogen yield  coefficient  of
8021  (mg BiLVSS  produced)/(mg  total nitrogen removed) 0  These yield values
and nitrogen  content appear to be  realistic estimates of  the nitrogen  con-
version and are within the range of  reported values which vary  from  5<>6
to  1204 percent (References 280 420  43  and 44) „
Phosphorus
    Daily steady-state total  phosphate  and total dissolved phosphate
•measurements  were  made on the primary, and secondary effluents,,  Dissolved
orthophosphate  Has determined on  three-day grab  samples of the  primary
and secondary effluents,,  These results are presented in Table  3,50   Total
phosphate expressed  a& P ia the primary effluent varied from 701  to  26 05
with  an average of 1708 mg/1  as P  and the total  dissolved phosphate
ranged from 70i to 23„ with an average  of 14 „ 8 mg/!0  On the other hand0
the total dissolved  phosphate in  the secondary effluent varied  from  6»8
to  2205D with an average of 1209 mg/l0  and the' total phosphate  varied
from  802 to 36»50  with an average  of 14„7 mg/1 as P0  From thrse=day grab
sample analysesD dissolved orthophosphate expressed as  P varied from 704
to  UoOp with an average of 1103 mg/lj,  in the primary effluentg and  509
to  15050 with an average of 9062 mg/1,,  in the secondary effluent0

                                     108
-------
    Table 17 also presents the phosphate removal efficiencies and remov-
al velocities which were calculated based on the assumptions that both
the particulate and dissolved phosphate in the primary effluent are
available for biosynthesis and excess phosphates are present in the
soluble forms in the secondary effluent.  Approximately 27.8 percent of
total phosphate or 16.1 percent of total dissolved phosphate was removed
by activated sludge.  Based on three-day grab sample analyses, 12 percent
of dissolved orthophosphate was incorporated into cell material.  It
appears that phosphorus supply in the primary effluent was in gross
excess of the phosphorus required for cellular growth; hence phosphorus
was not the limiting nutrient in this study.
    The net yield coefficients (Equation 40) based oh phosphorus were
found to be as follows:
        _,    ...	(mg MLVSS produced)
        I         	—	
         n     *  (mg total dissolved phosphate as P removed)

        Y  = 28 r	(mg MLVSS produced)	
         n        (mg dissolved orthophosphate as P removed)

Since no phosphorus analyses  were made on  activated sludge,,  the  phosphorus
content in the activated sludge was  estimated from the  difference  between
total particulate and dissolved phosphorus concentration made  on the  mixed
liquor„  The estimated  phosphorus contents in the activated sludge varied
from 0061 to 7039 percent with an average  of 3o60 percent (Table 15)»
This average phosphorus content of  activated sludge corresponds  to a  phos-
phorus yield coefficient of 2708  (mg MLVSS produced)/(mg phosphorus removed)
    Reported values of  phosphorus content  in activated  sludge  range from
2  to 3 percent  (Reference 25)„  The slightly high phosphorus content  of
cells noted in  this study may have  been  caused by greater phosphate up-
take rate and greater phosphorus  storage„   Excess phosphate uptake was
observed by Toerien et  al<, (Reference 7) in an algal growth  kinetic study
under phosphorus  limitation using Selenastrtsa capricoxnutum as a tes£
organism,,

                                   109
-------
    In the treatueat of several nutrient°d«i'ici@nt industrial wastes „
Helmers et &10  (Sfflference  45)  determined rainteal qusratiti®® of nitrogen
and phosphorus  of 40 (mg M)/(§.BOD  reeoved)  and 6
This is approximately  equivalent  to a BOD'sNsP  ratio of  150§5s:
the BODsHsP ratio %?®s  150s48s22 in  the  primary effluent„ it is obvious
that neither nitrogen  nor  phosphorus was a limiting nutrient  la  this
process o  Although  in  the  absence of typical values of  half-=s©turatiom
constants of nitrogen  and  phosphorus (K M  and  K _) „ it  is  conceivable
                                        S ™      o&
that the nitrogen and  phosphorus  concentrations in the  aeration
effluent  (S-.,  or S.J)  were, much greater than the K    or K    values; that
           JLw     JLtt                              8K      SJr
is, S.M » K ... and  S.- »  K Bo Thus,  the  nitrogen aad  phosphorus  reraoval
     IN     SK      Li?     8"
velocities  (q., or qn)  were zero-order  with respect to S,M  or  S.^o   Conse-
             fj     f                                   J.W      JL*
quentlys  the Michaelis=-Menten (Monod)  model (Equation 3)  for  ffiitsogen  or
phosphorus as  a limiting nutrient is not  applicable.   Furthermore0 since
other macronutrients and raicr©nutrients are usually  present in sufficient
quantity  in domestic sewage9 the  organic  substrate measured as BOD or  C00
appeared  to be the  sole growth limiting factor in this  study,

SOLIDS  SEPARATION

    The activated sludge process  incorporates  soluble and particulate
materials into a mass  of biological solids which must be separated fro&
the process effluent.   Sludge settling and compacting characteristics  ar@
a primary requisite to successful operation of the activated sludge pro=
cesso   One of  the objectives of this study was the evaluation of selects^
alternative solids  separation systems„  The selected systems iacludsd
vibratory screening,, enhanced gravity sedimentation„ dissolved air flot®=
tion and  pressurised 'hydro-centrifugal screening,,
Sludge  Settling Characteristics
     Several sludge characteristics are of importance in determining
 settleability0   These sludge characteristics are particle siss distribution
 particle shape D  particle density„ particle surface charge asud sludge voiusas
 index,,   The project was too limited to continuously monitor all of
                                    110
-------
sludge characteristics and correlate them with sludge settleability and
activated sludge operating parameters.  However, some qualitative analy-
ses can be summarized.
    Sludge volume index measurements were made on mixed liquor under
presumed steady-state conditions and are presented in Table 14.  Sludge
volume index varied from 25 at an organic loading rate of 2.00 (mg BOD)/
(rag MLVSS)(day) to 935 at an organic loading rate of 1.94 (mg BOD)/
(mg MLVSS)(day).  Figure 20 shows the variations of sludge volume index
with BOD loading and COD loading rates.  No apparent relationships can
be developed from these widely scattered data.
    It was observed that at low organic loading rate, e.g., less than
1.0 (mg BOD)/(mg MLVSS)(day) or 3.0  (mg COD)/(mg MLVSS)(day)8 the col-
loidal materials in the primary effluent were effectively flocculated
by activated sludge.  At higher organic loadings, the flocculating capac-
ity of the activated sludge apparently was insufficient to flocculate all
colloidal particles causing a very turbid secondary effluent.
    Qualitative morphological microscopic examinations revealed that the
percentage of  filamentous organisms  present in activated sludge increased
with  increased sludge volume index;  also increases in organic loading
tended to stimulate the growth of filamentous organisms„
Vibratory Screening
    A set of SWECO vibrating screens, equipped with three interchangeable
screen materials, was incorporated into the facility.  The three screens
supplied with  the units included 0.044- and 0.037-mm opening  (325- and
400-mesh) stainless steel plain weave screens„ and a 0.014- by 0.105-tiuu
opening  (720-  by  140-mesh) dutch twilled stainless ste*. I screen.,  Each
screen was equipped with  a fine spray washing system for removal of
trapped materials.
    The  screens were  tested  under varying operating conditions which
included  screen size  opening, speed  of  vibratory motor, solids and hy-
draulic  loading rates  and the angle  between  top and bottom vibratory
                                   111
-------
1
                1     of
                       o
                        o
                     o
                      o
                 ©  o
                                    0©
                                                             7     •  S
11     13
-------
weights.  Table  18  presents  the screen performance characteristics and
operating conditions.  Average values  of solids removal efficiencies and
filtration rates are summarized  in Table 19.  The  speed of the vibratory
motor, in the narrow range of 1,100 to 1,500 rpm,  and the angle between
vibratory weights were not found to have a significant effect on per-
formance and were discounted from further consideration.
    Average solids  removal efficiencies from the effluent stream with  the
0.044- and 0.037-mm opening  (325- and  400-mesh) screens were 38 and 49
                                                       3   2
percent, at average filtration  rates of 16.6 and  16.0 m /(m )(day)
                    2
 [408 and 393 gal/(ft )(day)]» respectively, which  are considered  to be un-
acceptable performance.   Suspended solids recovery with these screens  was
too low to return sufficient solids to the aeration tank.  Average solids
removal efficiencies with the 0.014- by 0.105-ram  opening  (720- by  140-mesh)
screen  averaged  91  percent (a value approaching the performance of gravity
                                                  32
settlers) at an  average  filtration rate of 2.98 m /(m )(day)  [73.2 gal/
 (ft2)(day)].
    Hydraulic  capacities of  the vibratory screens  are presented  in Figures
 21, 22  and 23.   Normalized filtration  ratesD which are  the  ratio  of fil-
 tration rate to  hydraulic loading  rates were plotted against  the  corres-
 ponding solids loading rates for each  screen size0  The hydraulic capac-
 ity of  the 0.044-mm opening  (325-mesh) screen  depicted  in Figure  21 ap-
 pears  to be nearly  independent  of  solids  loading  rate.
    Normalized filtration rates of the 0.037-mm opening (400-mesh) screen
 generally  decreases as solids  loading  rates  increased,,  as shown  in Figure
 22o   Results were  erratic, but  this  smaller mesh  size was apparently more
 susceptible  to hydraulic head losses  caused by suspended  solids  and hy-
 draulic loading than the 00044-mm  opening  (325-mesh) screen.
    Whereas  the  solids removal  efficiency of  the  0,014- by  Ool05-mm open-
 ing (720-  by  140-mesh) screen was  acceptable,,  the filtration rate was
 far from acceptable at the  suspended solids  concentrations  applied.  At
                                                2        '            2
 solids loading rates on the  order  of 97.9 kg/(m)(day)  [20,0 lb/(ft )(day)]s
 generally  less than 10 percent  of  the applied  hydraulic flow passed through
 the filters,  as shown in Figure 23.
                                   113
-------
Table 18.
Solids
T.:st loading sate,,
HiBBber kg/ (s^) (day)
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
34.2
24.7
33.0
20.5
28.4
14.8
17.5
117
132
89.7
108
79.8
30.2
59.7
30.2
71.3
50.2
111
93.
76.
50. 
-------
Table 18 (continued).  VIBRATORY SCREEN PERFORMANCE DATA
S.Uids
Test loading rate,
Number kg/ (m2) (day)
46
47
48
49
SO
51
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73
74
75
76
77
78
79
80
81
82
83
84
85
86
87
88
89
193
206
52.6
55.0
105
109
114
106
76.2
88.8
76.8
81.4
53.9
53.5
88.0
51.0
98.2
70.4
104
58.6
92.4
61.7
97.2
76.1
121
30.2
25.0
19.0
104
120
131
115
98.2
118
62.8
37.9
36.6
93.0
81.3
103
67.5
86.4
93.0
101
Filtration
Filtration rate/
rate, hydraulic
m/(m) (day) loading ratio
39.9
55.4
13.0
13.7
23.6
23.9
25.8
24.2
18.1
19.7
17.6
21.0
14.4
14.0
20.5
12.3
24.4
16.4
25.8
16.0
26.2
13.4
26.3
15.8
27.9
8.06
5.70
7.77
27.0
10.6
17.1
28.7
10.6
28.4
7.98
9.73
2.03
1.42
0.24
3.79
0.41
2.24
0.98
0.81
0.73
0.95
0.85
0.85
0.91
0.88
0.92
0.93
0.97
0.90
0.90
0.96
0.94
0.96
0.86
0.91
0.94
0.91
0.93
0.90
0.94
0.65
0.94
0.84
0.94
0.59
0.68
0.86
0.75
0.29
0.45
0.86
0.37
0.72
0.36
0.88
0.23
0.06
0.01
0.13
0.02
0.09
0.04
0.03
Solids
Influent Effluent removal Screen
suspended suspended ef f tciency, o^erJ ng,
eolids, mg/1 solids, ag/1 X j
3540
3540
3440
3440
4050
4050
4050
4070
4070
4070
3930
3730
3530
3680
3680
3780
3780
3720
3720
3320
3520
3490
3490
4070
4070
2230
3000
2100
2880
3340
3460
3450
3500
3010
2880
2440
4050
4070
3930
3730
3780
!3780
4070
4070
2420
2920
2480
1680
3500
2770
3110
3200
3170
2830
2550
3100
2990
1790
2620
2440
2550
2350
2140
2160
2100
2150
2660
2760
3100
860
83d
1040
1180
1640
1840
1950
2030
232C
1400
330
300
180
130
160
90
100
168
130
31.6
17.5
27.9
51.2
13.6
31.6
23.2
21.2
22.1
30.5
35.1
17.0
15.3
51.4
28.8
35.5
32.5
36.9
32.7
38.1
40.5
38.4
23.7
32.1
23.8
61.4
72.3
50.2
59.0
50.7
46.6
43.5
42.0
22.8
51.6
90.4
92.6
95.6
96.7
95.7
97.6
97.4
95.9
96.8
44
44
44
-44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
44
37
37
37
37
37
37
37
37
37
14 x 105
14 x 105
14 a 105
14 a 105
14 a 105
14 a 105
14 a 105
14 n 105
14 a 105
14 a 105
                              115
-------
Table 19.  SUMMARY OF VIBRATORY SCREEN PERFORMANCE
Screen
Mesh Opening ,
Number u
325 44
400 37
20 x 140 14 x 105
Average
influent
solids
concentration „
mg/1
3,395
2,997
3,780
Average
solids removal
efficiency,
38.0
49.0.
91.0
Average
filtration
ratep
m3/(m2)(day)
17.3
16.0
2.97
-------
     100
Eft
     70
X
     10
••'. °J«, ."* ' ..'.'* /-'v. • -l ' '
— oo 9° * .
0 «••••.
— . ° • . • , •
__ o
— »
1 1 1 1 1 II 1
1 20 40 SO 60 100 120 140 160
1 1 .
^^mm

—
	
	
1 1
160 200
                              SOLIDS LOADING RATE, kg/(m2) (day)
               gure  21   Hydrau! ie  capacity of  vibratory 0%
                                    (325-fnesh)  screen
opening
-------
                                  !        I
1    ~~T
09
            t/VJ)
            •
            1UJ1
                                                                '© 3348
                                                                        m
                                                         sh)  scree
-------
100

 90

 80

 70

 60

 50

 40

 30

 20

 10
1
         3440
       • 4050
I
2880



               © 3730

• 3780 L 393Q9  4°9 °4070
                                                            I
                                                          T
                                                         T
                                                          NUMBERS REFER TO
                                                          INFLUENT SUSPENDED
                                                          SOLIDS CONCENTRATION
          20
        40
        80
                            SOL IOS

   Figure 23   Hydraulic capacity
    100      120     140
    RATE.  kg/(m2)  (day)

of. vibratory 0.014-1
f  140-fliesh)  screen
                                              180
200
-------
    Because the attainment of relatively high filtration rates could raot
be achieved with the type of vibratory screening provided for 'this study0
the testing of the vibratory screens was discontinued in-favor of an«=.
hanced gravity ssdiwsntatiosu
Enhanced Gravity Separation
                 i
    During the studies of the accelerated high-rate activated sludge
system^ suspended solids removal from the mixed liquor Has accomplished
by two circularD 1608»ra (55-ft) diameter gravity settlers,  Both settlers
were operated in-parallel during each steady-state period and their per=
formance Has determined from analyses drawn from a common effluent sump
and a common return solids sump.  Table 20 summarizes average operating
parameters and performance characteristics of .the gravity settlers dur-
ing the steady-state activated sludge process operations0  .
    The effect of hydraulic SUE face  loading rate on gravity settler per-
formance is shown in Figure 24„  The hydraulic surface loading rate var-
ied between 5,0 and 13,3 m3/(m2)(day)  [123 and 327 gal/(ft2)(day)] in
the tests at Chino*  These surface loading rates are much lower  than
                                      32                   2
those usually used,, i0e0£, about  32,6 m  /(m )(day)  [800 gal/(ft ) (day) ]
for conventional activated sludge processes,  With the exception of the
single high value point„ effluent suspended solids appeared to be  little
affected by.hydraulic  surface  loading rates in the range studied,,  Al-
though return sludge solids concentrations generally decreased with in-
creasing hydraulic  surface loading  rates„  the large variations of  con-
centrations encountered  in the extremely narrow  range  of surface loading
rates between  12..2  and 13,4 m3/(m2)(day)  [300 and  330  gal/(ft2)(day)]
indicate the  influence of a  factor  other  than surface  loading rate,
    The effect of mean cell age  on  gravity settler performance is  shown
                   V. v                             .               .
in Figure  25„  Return  solids  concentration  from  the  gravity settlers
indicated  a marked  increase with increasing mean cell  age.  The  five
widely spread  return solids  concent rations.„  indicated  in Figure  ?4 in
                                                         '32,
the narrow range of hydraulic  Loading  ratesp  12.3  and  13.4 nt  /(m )(dayj
                    2
 [300  and  330  gal/(f6  )(day)]„  achieve  greater significance  in their
apparently closer  relationship to mean  cell  age.   Effluent  uuspended

                                 120
-------
Table 20.  GRAVITY SETTLER PERFORMANCE
Steady-
state
run
1
et
3
4
5
6
7
8
9
-•irface
-'.cacine rai:es
nrV(m~)(day)
.9.89
12.3
5.01
7.20
7.45
13.1
13.0
13.3
12.6
Solids
loading rate »
kg/ (m2) (day)
33.2
47.4
23.0
20.5
24.0
28.4
18.1
37.7
17.6
Mean
cell age »
day
32.4
16.6
3.17
1.58
1.39
0.737
0.525
1.57
0.446
Suspended Solids
mg/1
Tn fluent Effluent
3,370 38
3,860 47
4,610 29
2,850 26
3.180 40
2,180 31
1,380 25
2,810 38
1,390 71
Return
sludge
solids,
mg/1
6,270
9,600
8,770
7,250
8,100
5,070
3,560
7,060
3,590
-------
......  .C9
           70
§0
           10
                                  1       I       I       I
                          a

                        *^^
                         K
                                                              tf
         i      I       ?      8
                        4   iff@ef
                                                8      10


                                                  . BflTI,  fii
                                                               o    jj
                                                                                           @.f
                                                                                           5,



                                                                                           4,
                                                                                           2..I
-------
U)
                 E
                t/v,
                          TTTTTl
I   I   I  I  I  II
   RETURN  SOllDS.
                                                                LUUL
                                                                     10
                                         r
                      20    30  40
  2     345
   WM CELL A6E,
cell  age  on gravity settler  performance
10.000

 9.000

 8,000

 7,000

 8,000

 5,000
                                                                                           4.000   -j
                                  3,000
                                  2,000
                                  i.ooo
                                  0
-------
solids concentrations,, on the other hand,, indicated only a very slight
increase from 30 to 40 mg/1 with increasing sludge age,  It would appear „
therefore 0 that it is possible to achieve acceptable effluent solids con-
centrations with a gravity settler over a vary wide,, i0eop two order© of
saagnitude,, range of \tnatn cell
    To get an indication of the potential advantage of slowly stirring
the settling sludge to effect  a greater sludge compaction, one gravity
settler was equipped with 6035=cra  (2o5-i.no) vertical angle pickets spaced
38.1 cm (15 in0) apart on the  traveling suction arm and extended to within
61 cm  (24 in0) of  the water surface,,  Both settlers were  then operated with
identical feeds ancJ feed rates during Steady-State Runs 3 through 90  The
sludge blanket in  the picket-equipped gravity settler was observed to be
30 to  61 cm  (12 to 24 in0) lower than in the other settler,  A common
sludge sump  for the two settlers prevented ready  analytical verification
of the improved compact ion 0
Pressurized  Eydro°d®nfcrifugal  Screens
     It is believed that vibratory  screening  could be  successfully  used  as
an activated sludge* separation system if  a continuous  cleaning of  screen
surface and  a pressure mechanism were provided 0   Consequently B a greater-
practical filtration  rate  and  higher 'solids  removal  rate  could be
achieved o  A device -consisting of  a screen mounted on discs which  can be
spun in a pressure vessel  appears  to have  potential  as a  mechanical  solids
separation system  for the  high-rate activated sluUge  process 0
     A small  uastewater concentrator was  loaned  from  SWECO for  evaluation o
The  screening surface is mounted  on a vertical  spinning circular cage
with the feed distributed  from- the inside  toward ehe scff®era0   As £he
liquid passes through the  screen  from  the  centrifugal force,,  the solids
are  transported down .-the screen by gravity and  collected  separately 0  A
cleaning cycle is  also built  into the  unit to eliminate grease binding,,
     Unfortunately,, within  the scop® of  this  project p  this eoncspfc  and
umit could not be  tested  or  evaluated;  however „  the  need  for research is
indicated,                                        -  -         •
                                  124
-------
Dissolved Air Flotation
    Dissolved air flotation was selected as an alternative separation
system because it provides larger compactive forces for concentrating
separated materials as compared to conventional gravity clarification.
    The pilot flotator leased from EIMCO was 1.53 m (5 ft) in diameter
and was equipped with a float skimming system, bottom rakes and a draw-
off for settled solids.  The unit was also equipped with EIMCO's stand-
ard two-stage pressurization system for dissolving air in a recycle
stream drawn from the effluent of the unit.  The hydraulic loading of
this flotator was between 20.3 and 122 m /(m)(day) [500 and 3,000 gal/
   2
(ft )(day)] with relatively good suspended solids capture.  If a coagu-
lant aid and polymer were added properly, the solids in the effluent
were well flocculated and could be easily removed by granular media fil-
tration.
    One test run was made on the pilot flotator which was operated at
approximately 81«4 m /(m )(day)  [2,000 gal/(ft )(day)] with 20 percent
effluent recycle.  The ferric chloride dose used was approximately 150
mg/1,, the polymer was  1.0 mg/1 of Calgon Catfloc and the pH of the re-
cycle stream was 8.3.
    The effluent suspended solids concentration was 22 mg/1 with a vola-
tile portion of 5 mg/1.  The low magnitude of volatile suspended solids
would indicate that the solids were  ferric chloride floes rather than
activated sludge solids*.  It appears  that  the flotation system could  be
effective in separating activated sludge.  Moreover,, it is expected  that
a  considerable amount  of phosphate compounds  could be  removed.
    This air flotation solid separation program was only  designed  to
indicate its general feasibility and potential in activated sludge sepa-
ration application.  Complete system evaluation of dissolved  air flotation
is indicated.
                                  125
-------
                              SECTION VIII
                  DESIGN AND  OPERATIONAL  IMPLICATIONS

    The design and operation of domestic waste treatment plants have
evolved largely from practical experience with full-scale systems„
Theoretical analysis has been directed largely to explaining the phenom-
ena observed in practice.  To date such  analysis has not been• fully
applied to either design or  operation of real systems<,  Such a dileraffla
results from the  interaction of several  pertinent considerations0  On®
of the major factors has been the lack of adequate theoretical bases for
analysis of the process.  A  second, and  possibly more important„ factor
has been the poor communication between  the  theoretician concerned pri-
marily with the theory  and performance criteria of the  process and the
practitioner who  is concerned largely with compliance with traditional
treatment  concepts and  effluent quality  or performance  criteria estab-
lished by  regulatory agencies.
    Complete kinetic description  of  the  activated sludge process  that has
been derived from actual plant data would permit evaluation of the  th®o=
retical model and would make possible more accurate  predictions of  process
performance as well as  indicate opportunities  for improved process  design
and operation.  One of  the great  advantages  of using a  rational kinetic
model to describe the activated sludge process is that  it considers both
the microbial kinetic characteristics„ which are a function of the  co®-
plex biological system  operative„  as well as the effect of physical fac=
tors such  as the  hydraulic residence  time, cellular  recycle„ oxygen trans-
fer rates  and the cellular residence  time-   These latter factors  are  af-
fected by  the intentional sludge  wasting rate, the settleability  of the
mixed liquor and  the effectiveness  of  the solids separation system,,

                                   126
-------
KINETIC DESCRIPTION OF ACCELERATED HIGH-RATE ACTIVATED SLUDGE SYSTEM
    The results from this study have yielded a kinetic description of the
accelerated high-rate activated sludge system and what appear to be reas-
onable values for the kinetic constants and coefficients which can be
utilized in the analysis and design of waste treatment systems, especially
for high-rate activated sludge systems.
    The kinetic analyses suggest that the net growth rate of activated
sludge, 1/6 , in a high-rate process is a linear function of the sub-
strate removal velocity, q, and a constant endogenous respiration rate,
kd» or
                            l/8  = Yq -
                               c
In terms of BOD as the rate-limiting substance,
                       l/ec - 0.922 q    - 0.027
 and  in  terras of COD af the rate-limiting substance,

                            - 0.328 q-S-  0,023
    The kinetic  analysis  also  suggests  that  the  organic substrate  concen-
 tration, expressed aslBOD or biodegradable COD,  was  the growth  limiting
 factor in  the  system and  the Micahaelis-Menten  (Monod) model  can be  suc-
 cessfully  employed to  describe the  substrate removal velocity and  sub-
 strate concentration relationship,  viz,,
                                     qs,
 or                               4o1 S1BOD
                           qBOD = 26
                                   127
-------
                         8°*  (S1COD * 20)
                  ?COD ~ 75 + (S     - 20)
    It is believed that much valuable  information wa© developed during
the investigationp not only regarding  theoretical concept®  aad th©ir.
application to the actual process j, but also with respect  to performance
parameters amd operational control of  the  process 6   Table 21  cougars©
values of the design ®ad performance parameters for  £h© accQl@?at©4
high=rate system studied at Chino with other  activated sludg® g>soeees®@0
    The accelerated high=rate  activated sludge process was  characterized
by extremely high loading velocities„  varying from 002 £o 306 (tag BO®)/
(rag MLVSS)(ddy)«  The system was  operated  and produced high quality
effluents (effluent soitsfol® BOB ranged from 5 to 28  eag/1) and .high p?o»
cess efficiencies (75 to 95 percent BOB removal).
    The most significant finding  of this investigation is that  activated
sludge systems can be designed to handle high organic loading©  up to 3»6
(mg BOD)/(sag MLVSS)(day) with  conventional gravity separators operating
                             32                   2
at an overflow rate of  13»4 m  /(m )(day) [330  gal/(ft ) (day)].  Th©  capa-=-
bility of operating the system at the  unusually  low  sssaa  csll ©g© of -003
day demonstrates  the feasibility  of utilizing the high growth=rat©
tial of activated sludge as a  means of removing  oic§gmlc ma&drial© from
wastewater,,  Howevers the oraly practical solids  separation  systsa
able at presen't is a gravity settling  uraito   Sssearch asaid dowei©pkiat
improved gravity  and mechanical cell separators  K©sssiiiB©  ss&
practical need for improved biological treatment sy©e©sss0
                                   128
-------
               T.=>b.le  21..  DESIGN AND OPEFATIONAL  PARAMETERS FOR
                           ACTIVATED  SLUDGE  PROCESSES
                                                         High-rate       China
                      Conventional         Contact       aeration3     demonstration
Parameter          activated  sludge    stabilization -     (optimuta)      (opt.imum)
Mean cell age,
6C, day
BOD loading, l^p
(mg BOD)
(mg MLVSSKday)
MLVSS, Bg/1
Hydraulic resi-
dence time, 6,
hr
Recycle ratio
BOD removal
efficiency, %
5
0.2
1,500
4
0.1
85
to 15
to 0.5
to 3,000
to 8
to 0.3
to 95
5 to 10 -
0.2 to 0.6 1.9
1,000 to 3,000 2,500
(4,000 to lO.OOOr
0.3 to 0.7 0.7
(1.5 to 5)b
0.25 to 1.25 0.56
80 to 90 89
0.4 to 1.0
2.0 to 3.5
600 to 1,000
0.9
0.3 to 0.5
85 to 95C
Secondary clari
 fier overflow
 rate,
 mV(m2)(day)
32.6
32.6
32.6
                                                                          l3.4
sFisret stags performance of two-stage activated  sludge plant (Reference 48).

  Solido stabilization unite

  Soluble BOD removal efficiency.

 Actual operating overflow rate, no optimum tratQ obtained ,
                                  129
-------
APPLICATION OF SYSTM KINETICS
    Inspection of  the cell  continuity equation  (Equation  16) sad
£Jich®0100-ft ) tank for the con-
ventional process„
    Because  of  the prssent dependence upon gravity cell separa£ion0 the
                                   33
high-rat® process  requires© a 685=®  (240200=ft ) secondary settling wait
                    3         •  3
compared to  © 283-a  (IOD000=ft )  unit for eh©' convsneional psocesso '
Hith the d©velibpmesit of compact, hi^h«=rate ssechanical cell separators •
and eh® repl®c<3E3at of eh® larger  gravity s®eelia§ mmi£©0 a coapact
high^rate ac£iv®£csd sludg® plant wieh £h® potential for substantially '
      o^sffali costs could b® realised0
                                  130
-------
Table 22.  DESIGN COMPARISON BETWEEN CONVENTIONAL AND HIGH-RATE
               CHINO ACTIVATED SLUDGE PROCESSES
Design data
and criteria
F, m3/sec
SQ, (mg BOD) /I
YB (mg MLVSS produced)
(mg BOD removed)
kd, day'1
K , (mg BOD) /I
s
*.
QD (mg BOD removed)
(mg MLVSS) (day)
X-, (ing MLVSS)/!
X29 (mg VSS)/!
F B m3/sec
Xr0 (mg VSS)/i
ap (mg 0_)/(mg BOD removed)
bkd!> (mg 02)/(mg MLVSS) (day)
Secondary overflow rate,
m3/(m2)(day)
Effluent BOD, Slt(mg BOD)/!
BOD removal velocity, q.
Conventional
activated
sludge plant
0.0438
200
0.5
0.05
100
3.0
2,000
30
0.0110
7 9000
0.5
0.1
32.6
20
0.5
Demonstration
activated e ludge
plant, Chino
0.0438
200
0.92
0.027
26
4.1
1,000
30
0.0219
4,000
0.44
0.43
13.4
20
1.78
   (mg BOD removed)
   (mg MLVSS)(day)
                                  131
-------
Table 22 (eomt&nu@d) „  DESIGN COMPARISON SET&JEEM
                             .  Conventional
Design dafca            '          activated
and erifceria
Process efficiency:, Ep %
!*„„ (mg BOD applied)
(mg MLVSS) (day)
Mean eell age9 6CP day
Aeration Sank volunta^
V__ ^
s, ra-3
Hydraulic residence tiats 0
8 „ hr
Sludge wasting rate8
F , m3/day
Sludge production Eates
90 90
O.S6 1.98
5.0 . Oo62
.682 .382
4.3 ;.. i.4-
22.8 127
272 617
      (kg VSS)/day

 Oxygen  requirements;,
      (kg 02)/day                   317
Secondary clarifier surf ace
 areaD m^

Secondary clarifier volume „        283                     685
  areaD m                           116                    281
                                     132
-------
                            SECTION IX
                             GLOSSARY

a     Oxygen requirement per unit substrate removed
h     Oxygen requirement per unit cell oxidized
C^    Gear reduction efficii-ncy
C     Aerator motor efficiency
E     Substrate or nutrient removal efficiency
F     Influent flow rate
Fr    Return activated sludge flowrate
F     Waste activated sludge flowrate
xj    Decay rate
kt    Oxygen transfer rate
K _   Nonbiodegradable COD concentration
K     Half-saturation constant
 O
Lv    Substrate loading velocity
q     Substrate or nutrient removal velocity
q     Maximum substrate or nutrient removal velocity
Rf    Return sludge ratio
SQ    Influent substrate or nutrient  concentration
BI    Effluent substrate or nutrient  concentration
SVI   Sludge volume index
U     Rate  of oxygen consumption
V     Volume of aeration tank
Xfi    Influent cell concentration
X^    Mixed  liquor cell concentration
X2    Effluent cell concentration
X     Return activated  sludge  cell concentration
Xw    Waste  activated sludge cell  concentration
Y     Yield  coefficient
Yn    Net yield  coefficient
\i     Specific  growth rate
n     Maximum  specific  growth  rate
0     Hydraulic  residence  time
 Q     Mean cell  ape
                                      133
-------
                                 »o. „
                           3330  12>13
2.   Moraod0 JoD Etedhcigeiss  stsg  la Cgoioeances d@a Cmlfctagqia Bac£Qg&oiBst®a'n  Paris,
                 Ci@B 1942
 3e   M@a©d9 J., "The Growth of Bacterial Cultures9" Aim,, l@Vo McgobAol. 0 _3e

           •0
               .Ao ThQ  Case fog Coatiauoua Flow (Ch®BO@£s£) Kia®£ic
     of Fiamkeoa - Ntatgieafc Ggg^th Ralafcionehipa iia Enaerophieation M®lysaa
     Prepared for Join£ ladysery Govarmogct Coiaffil££©a Meseiag  o®, Algae
              ,, Oiicsgo, Illinois , 1968             '       •
 50   Fsraclj, ZoB "Theoretical Analysis of Continuous Ciaieisff©  Sys£®!EsB" In:
     Theoretical and Methodological Basis fog Consiauonaa Guitar® of Micgo-           '
     oggamistss 0 Ed. 1=  Malek and Z. F@nelD Acsdesdc Press 9 Kew York;, 1966            <

 6.   Stewart 0 MoJ.0 Reaction Kinetics amd Operational Pagaffi@g®r@ of ContianiotBa       ;
     Flow Aaaerobic Fermentation Procesaes. SSRL Publication No. 4S IER' Series
     90 „ University of  California, Berkeley, 1958
 7»   Toari@n0 DoF.0  MusngB CoH>g ^adi«sky0 J.9 P®ffirsonp  E.'A.  ®ad Scherfig0 'J.
     Fisaal Report..,-  ProvJaional Mgai Mgiay ProcsdagsSj,  SHIL  Report Ho._ 7i-6p
     Sanitary Bngineering Esssareh L©boi?©tosy9 Uai^o  of  Calif onai©0 B©rk
-------
13.  Lawrence, A.W. , and P.L. McCarty,  Kinetics of Methane Fermentation in
     Anaerobic Waste Treatment,  Dept. of Civil Engineering, Stanford Univ., 196'

14.  Agardy, F.J., Cole, R.D. , and Pearson, E.A. ,  Kinetic and Activity Param-
     eters of Anaerobic Fermentation Systems,  Fi rs t Annual Report „ Berkeley:
     Sanit. Eng.  Research Lab., Univ. of Calif., 1963

IS.  Metcalf and Eddy, Inc.,  Wastewater Engineering;  Collection. Treatment.
     Disposal,  McGraw-Hill Series in Water Resources and Environmental Engin-
     eering, 1925

16.  Standard Methods fpt the Examination of Water and Wastewater, 13th Ed. ,
     American Public Health Association, AWWA, WPCF, New York, N.Y., 1971       •

i7.  FWPCA Methods for Chemical Analysis of Water and Wastes, FWPCA, Division
     of Water Quality Research Analytical Quality Control Laboratory, Cincinnati
     Ohio, 1969

18.  Patterson, J.W., Brezonik, P.L., and Putnam, H.D., "Measurement and Sig-
     nificance of Adenosine Triphosphate in Activated Sludge,"  Environmental
     Science and Technology . Vol. A,  1970

19.  Beutler, E. , and Baluda, M.C., "Simplified Determination of Blood Adenosine!
     Triphosphate Using the Firefly System," Blood. Vol. 23. 1964

20»  Baer, R.M. 9 "Computer Program COMMON G2 CAL NLIN, Nonlinear Regression/'
     Computer Centert University of California, Berkeley, 1967«


218  Patterson, J.W., Brezonik, P.L. , and Putnam, H.D., "Sludge Activity Par-
     ameters and Their Application to Toxicity Measurements in Activated Sludge,'
     Paper presented  at the 24th  Industrial Waste Conference, Purdue Univ., 1969

22»  Ford, D.L. , Eckenfelder, W.W. ,  and Yeng, T. , "Dehydrogenase Enzyme as a
     Parameter of Activated Sludge Activities," Proc. 21st Annual Industrial
     Waste Conference,, Purdue Univ. ,  1966

23.  Eckhoff, D.W.,  and Jenkins,  D. ,  Activated  Sludge Systems; Kinetics ct  the
     Steady  and Transient States,  SERL Report No. 67-12, Sanitary Engineering
     Research Laboratory, Univ.  of Calif., Berkeley,  1967
24.  Hopwood, A. P.,  and  Downing, A. I,., "Factors Affedi'.^  the Rate of Production
     and  Properties  of Activated Sludge  in Plants Treating Domestic Sewage,"
     J. Indus t. Sewage Purification.  Part 5,  1965

250  Jenkins, D. ,  and Menar,  A.B., The Fate of  Phosphorus  in Sewage Treatment
     Processes; Part 1,  Primary Sedimentation and Activated  Sludge,  SERL Report
     67-6,  Sanitary  Engineering Research Laboratory,  Univ. of Calif., Berkeley,
     1967
                                       135
-------
260   Heukel@kiaa| H. „  Orford9 H.E. „  and Manganeiii,, Ro 8  "Factors Affecting fch@
      Quantity of Sludge Productioa in the Activated Sludge ProeesSj,"  Sew, ..and
      Indus trial Wastes. £3, 945 9 1951

270   Shea, T.Go,'¥oA.  Pretorius, R.D. Col©, and E.A. Pears©ffl9 Kiaetica of
      Hydrogen Assimilation in Methane Fermentation. SERL Report No.  68-7 ,
      Sanitary Engineering Research Laboratory, Univ. of  Calif. s Berkeley 0
      1968

 28a   Middlebrooks, E.J.,  Jenkins,  D. , Heal,. J. , and Phillips, J. s  "Kinetics
      and  Effluent Quality in Extended Aeration," Water Research, J3»  39 *>
 290   Stewart,  M. J. ,  and Ludwig,  H.F. ,  "Theory of the MAS  Waste=-water Treat-
      ment  Process,,"  Water and Sewage Works,  109, 97 , 1962

 30e   Gram, A.L. ,  Reaction Kinetics of  Aerobic Biological  Processes.  Sanitary
      Engineering  Research Laboratory^  University of California,  Berkeley,
      No. 2, IER Series 90, 1956

 31.   Beneder,  P., and Horvath, I., "A  Practical Approach  to  Activated  Sludge
      Kinetics," Water Research,,  J., 1907

 32.   Pearson,  E.A. ,  and Haas, P.,  Kinetics  Analysis of Whittier Narrows Water
      Reclamation  P^ant .  Report  to Los Angeles County  Sanitation Districts,
      1967

 330   Stack, V.T.  and Conway, R.A. „ "Design Data for Cosipletely-Mised Activated
      Sludge Treatment s"  Sew, and Ind. Wastes , 31, No.  10S  1959

 340   Servicij,  J.A.' and Began,, RoH.9."Free Energy as a  Parameter  in Biological
      Treatment,"   Proc. ASCEn 89 . S.A. 3D pp0 17-40 1963

 350   McWhorter, T.R. , and Heukelekian , H., "Growth and Endogenous . PhAses in
      the Osidation of Glucose B"  Proc. Intl. Conf. .on  Water Follution
      Research , Vol.  2^, pp. 419-345 , Pergaoon Press 1962
 36,   Dryden, F.E.S Barrett, P.M., Kissinger, J.C., and Eckenftslder, W.W.,
      "Treatment of Fine Chemical Wastes by. High-Kate Activated Sludg©9"
      Proc. 9th Purdue Industrial Waste Conference, Purdue Uraiv
-------
 39.   EIMCO Research and Development Center,  EIMCO-SIMCO Ae rat or',  Palatine,
      Illinois

 40.   Downing, A.L., Tomlinson, T..G. and Truesdale, G.A., Effect of
      Inhibitions on Nitrification in the Activated Sludge Process, 1961

41.   Pearson,  E.A.,  "Kinetics  of  Biological  Treatment,"  Presented at  Special
      Lecture  Series,  Advances  in  Water  Quality  Improvement,  University  of
      Texas, Austin,  Texas  1966

42.   McKinney, R.E.,  "Biological  Oxidation of Organic  Matter,"  in Advances  in
      Biological Waste Treatment,   W.W.  Eckenfelder, Jr.  and  J.  McCabe,  eds.,
      1960

43.   McKinney, R.E.  and Horwood,  M.P.,  "Fundamental Approach to the Activated
      Sludge Process.  I., Floe  Producing Bacteria," Sewage and  Industrial
      Wastes.  24. 117, 1952

44.   Greenberg, A.E., Klein,  G. ,  and Kaufman, W.J., "The Effect of Phosphorus
      on the Activated Sludge  Process,"  Sewage and Industrial Wastes,  27, 1955

45.   Helmers, E.N., et^ al.,   "Nutritional Requirements in the  Biological
      Stabilization of Industrial  Wastes.  Ill,  Treatment with  Supplementary
      Nutrients," Sewage and Industrial  Wastes,  24, 1952

46.   Simpson, R.W., "Activated Sludge Modification," Water and Sewage
      Works. 106, 421-426, 1959
                                         137
-------
                               SECTION XI
                                APPENDIX
                     NONSTANDARD ANALYTICAL METHODS

ABENDSINE TRIPHOSPHATE
    The emission of light by  fireflies is known as biolianinescones and
                                                                     t
is an energetic reaction deriving  energy from the hydrolysis of ATP to
ADP and inorganic phosphate.  The  amount of light produced by firefly
extract is directly proportional to  the amount of ATP added.  The reac-
tion involves  the enzyme luciferase8  the bioluoinescent  compound luci-
ferin, and ATP.  Lucif erin  and ATP react in the presence of lucif erase
and' magnesium  ions to form  an enzyme luciferine adenosine monophosphate
complex and  Inorganic phosphate.   The complex is oxidized to pxyluciferyl=
adenylateD followed by  the  release of a quantum of  light„ In the presence
of an arsenate buffer,  there  is an initial burst of  luminescence followed
by an intermediate level of light  emission  that decays steadily with time,,
Procedure
(1)  A 10~ml sample is  added  to 40 ml of Trie buffer in  a 50-ml voluaiet-
     ric flasko
(2)  The ATP is extracted by  immediately placing  the solution in a bo|.l=
     ing water bath for 15  minutes and then transferring it  £o an ice
     bath  for  cooling,
(3)  The volume of the  sample is  restored  to  50 ml  and  the patticulate
     matter  is removed  by  centrifugation or filtration,,
(A)  2 ml  of ATP extract  is added  to 2 ml  of  firefly extract „  The mix-
     ture  is mixed by shaking it  for 15  seconds and at  exactly  two
     minutes the light  emission is measured using  a Turner Flizoiro®s£©Eo
                                   138
-------
DFHYDKOUENASL ACTIVITY
    Triplit-nyl tetrazoliura chloride (TTC) is reduced to Triphenyl forma-
zan 
-------