Page 744 - Fundamentals of Water Treatment Unit Processes : Physical, Chemical, and Biological

Biological Reactions and Kinetics 699

TABLE 22.9
Kinetic Data
Coefficients
Y (mg Cells=mg
1
1
Source Basis Substrate Culture Substrate) K s (mg=L) b m (day ) b (day )
Schulze (1965) Concentration Glucose E. coli 0.44 95 26
Heukelekian BOD Domestic waste 0.50 0.055
(1951)
Gram (1956) BOD Skim milk 0.48 100 2.5 0.045
Pearson-Haas COD Sewage 0.45 0.05
(1965)
Stack and Conway BOD Glucose 0.42 355 1.26 0.09
(1959)
Lawrence (1975, COD Domestic Activated sludge 0.35–0.45 mg 25–100 mg=L 2–4 0.05–0.10
p. 252) wastewater VSS=mg COD COD
Lawrence (1975, NH 3 NH 3 Activated sludge 0.05 mg=mg N 1.0 mg N=L 0.33 ND
p. 254) oxidation
Gaudy and Gaudy COD Glucose Sewage 0.62 390 7.7 ND
(1980) Glucose Sewage 100 9.1 ND
Lactose 0.47 ND
Sucrose 0.53 ND
COD Sewage Sewage 63 12 ND
Benefield and NH 4 as N NH 4 þ 0.05 mg VSS=mg 0.5–2.0 0.3–0.5 ND
þ
Randall (1980) NH 4 þ
Hao et al. (2009) MLSS Synthetic Seeding from Beijing 0.05
wastewater with WWTP; 30 day
COD ¼ 400 mg=L operation
Hao et al. (2009) NH 4 as N 200 mg NH 4 as Seeding from Beijing 0.08
þ
þ
N=L; to determine WWTP; 30 day
b, zero NH 4 as operation; then
þ
N=L nitrifiers were
predominant
Parker et al.=EPA NH 4 as N NH 4 þ Nitrosomonas in Y(net) 0.15 kg 0.6 mg NH 4 þ 0.18 exp 0.116 ND
þ
(1975) suspended growth cells=NH 4 as N as N=Lat (T-15) day 1
þ
reactor removed 208C 0.32 day 1
at 208C
Parker et al.=EPA NO 3 as N NO 3 =methanol Nitrobacter in Y(net) ¼ Y=(1 þ bu c ); 0.08 mg 1.04 (208C) 0.04

(1975) suspended growth Y ¼ 0.6–1.2 kg NO 3 -N=L

reactor VSS=kg NO 3 -N

removed;
Tchobanoglous Units as Domestic 0.6 mg VSS=mg 60 mgBOD 5 =L 5 0.06
and Burton given wastewater BOD 5 40mgCOD=L
(1991, p. 394)
where As may be seen by the substrate mass balance relation for a
U is the specific substrate utilization rate (kg substrate reactor, Chapter 23, Section 23.2.2.1, U is related to m=Y; the
3
3
degraded=m =s)=(kg viable cells=m ) mass reactor mass balance is, Q(S o S) ¼ [dS=dt]V; and since
S o is the substrate concentration entering the reactor (mg [dS=dt] ¼ (1=Y)[mX], then rearranging gives (m=Y) ¼ (S o S)=
3
substrate=m ) (u X), or
S is the substrate concentration leaving the reactor (mg
3
substrate=m ) m
(22:44)
u is the hydraulic detention time in reactor, V=Q (s) Y
U ¼
3
X is the viable cell concentration in reactor (kg cells=m )
In other words, although U has been used as an empirical
If U is given and if S o , S, and X are specified, then parameter, it is related to fundamental kinetic constants (see
the reactor may be sized based on u (since V(reactor) ¼ Q u). also Tchobanoglous and Burton, 1991, p. 392), The relation