Abstract
After a brief overview on biochemical reactors and associated processes, relevant model types and modeling approaches are discussed. In addition, a number of simple modeling applications focusing on bioreactor design, interfacial mass transfer and reactor control are reviewed.
In Part 2 published modeling and simulation work on biochemical reactors and reviews of related laboratory investigations are presented. Specifically, simulation case studies for gas-liquid reactors and hollow fiber bioreactors are discussed.
In Part 3, it is concluded that mathematical modeling and computer simulation are supportive tools for laboratory bench-scale investigations and are indispensable for the design, optimization, and control of large-scale bioreactors. However, existing models representing the process dynamics and economics of (research) bioreactors have to be greatly improved before the latter goal can be achieved.
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Abbreviations
- Ad :
-
cross-section of the downcomer (cm2)
- Ar :
-
cross-section of the riser (cm2)
- B:
-
biomass concentration (mg l−1)
- BA :
-
dimensionless biomass concentration, B/Y Sf
- c:
-
oxygen concentration in the liquid phase (M mol l−1)
- c* :
-
oxygen concentration in the liquid in equilibrium with air (M mol l−1)
- D:
-
dilution rate (s−1)
- D1 :
-
stoichiometric group, = YsSf/YoxMox (dimensionless)
- DG :
-
oxygen diffusivity in the gas phase (cm2 s−1)
- DL :
-
oxygen diffusivity in the liquid phase (cm2 s−1)
- F:
-
volumetric flow rate (cm3 s−1)
- H:
-
Henry's constant (liter atm/mol)
- J:
-
average volumetric flux density of the mixture (cm s−1)
- JG :
-
gas volumetric flux density (cm s−1)
- JL :
-
liquid volumetric flux density (cm s−1)
- K:
-
dimensionless Michaelis constant, = Km/Sf
- Km :
-
Michaelis constant (mg l−1)
- KLa:
-
volumetric mass transfer coefficient (s−1)
- L:
-
height of the riser (cm)
- Ms :
-
molecular weight of the substrate (g mol−1)
- Mox :
-
molecular weight of the oxygen (g mol−1)
- Ptot :
-
total pressure (atm)
- \(P_{o_2 }\) :
-
oxygen partial pressure (atm)
- QL :
-
liquid volumetric flow rate (l s−1)
- QG :
-
gas volumetric flow rate (l s−1)
- R:
-
reaction group, = LΜ/JL (dimensionless)
- rB :
-
rate of biomass generation (mg l−1 s−1)
- rs :
-
rate of substrate consumption (mg l−1 s−1)
- \(r_{o_2 }\) :
-
rate of oxygen consumption (M mol l−1 s−1)
- S:
-
substrate concentration (mg l−1)
- SA :
-
dimensionless substrate concentration = S/Sf
- StG :
-
Stanton number for the gas phase = (LKLa/JG) (RT/H) (dimensionless)
- StL :
-
Stanton number for the liquid phase = LKLa/JL (dimensionless)
- t:
-
time (s)
- T:
-
temperature (K)
- V:
-
total volume of fermentor (l)
- VG :
-
superficial gas velocity (cm s−1)
- VL :
-
superficial liquid velocity (cm s−1)
- VSG :
-
gas-phase volume of the separator (l)
- VSL :
-
liquid-phase volume of the separator (l)
- YS :
-
stoichiometric coefficient, (g) biomass per (g) substrate
- Yox :
-
stoichiometric coefficient, (g) biomass per (g) oxygen
- Y1 :
-
dimensionless partial pressure of oxygen, \(P_{o_2 } /P_{o_2 o}\)
- Y2 :
-
dimensionless oxygen concentration, C/C*
- z:
-
axial height (cm)
- Î’:
-
ratio of separator volume to total volume (dimensionless)
- γ:
-
ratio of liquid flow rates (dimensionless)
- Ï•:
-
gas hold-up (dimensionless) (fraction of gas volume/total volume)
- η:
-
dimensionless tube length (z/L)
- Μ:
-
specific metabolic rate (s−1)
- θ:
-
dimensionless dilution rate = DL/JL
- ξ:
-
ratio of cross-section of riser to downcomer (dimensionless)
- d:
-
related to the bottom of downcomer
- f:
-
related to the feed
- G:
-
gas phase
- s:
-
related to the gas separator
- T:
-
related to the top of the riser
- O:
-
related to the point of gas injection
- L:
-
liquid phase
- T:
-
310 (K)
- Μ:
-
0.4 (h)−1
- Km :
-
37.5 (mg l−1)
- H:
-
900(atm l−1 mol−1)
- Ys :
-
0.4 (g) biomass per (g) substrate
- L:
-
400–1000 (cm)
- Î’:
-
0.1
- JG :
-
35 (cm s−1)
- Sf :
-
200–775 (mg l−1)
- ξ:
-
4.0
- Yox :
-
1.0/(1.7/Ys−2.05) (g) biomass per (g) oxygen
- a:
-
inner radius of membrane
- A, B:
-
series solution constants (eigenconstants)
- b:
-
outer radius of membrane
- c:
-
substrate concentration
- C:
-
dimensionless substrate concentration
- C:
-
dimensionless bulk substrate concentration
- Cf :
-
idealized effluent bulk concentration (no diffusional resistance)
- D:
-
diffusion coefficient
- h:
-
membrane mass transfer coefficient
- I0 :
-
modified Bessel function of the first kind, order zero
- I1 :
-
modified Bessel function of the first kind, order one
- K0 :
-
modified Bessel function of the second kind, order zero
- K1 :
-
modified Bessel function of the second kind, order one
- Ka, Kb :
-
membrane partition coefficients
- K:
-
membrane partition coefficient ratio
- k:
-
reaction rate constant
- M:
-
the Kummer function
- r:
-
radial position
- X:
-
dimensionless radial position
- z:
-
axial position
- Z:
-
dimensionless axial position
- α:
-
diffusion coefficient ratio
- Î’:
-
hollow fiber radius ratio
- η:
-
effectiveness factor
- λ:
-
Thiele modulus
- λ:
-
eigenvalues
- σ:
-
overall mass transfer resistance
- C0 :
-
inlet concentration
- C3/C0 :
-
relative concentration
- D3 :
-
effective diffusivity in spongy matrix
- k:
-
first order rate constant
- Km :
-
Michaelis constant
- r/b:
-
relative radius
- b:
-
inner radius of spongy matrix
- t:
-
time
- V:
-
maximum reaction rate
- Î’=d/b:
-
relative radius of which there is no substrate concentration gradient
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Kleinstreuer, C., Poweigha, T. (1984). Modeling and simulation of bioreactor process dynamics. In: Bioprocess Parameter Control. Advances in Biochemical Engineering/Biotechnology, vol 30. Springer, Berlin, Heidelberg. https://doi.org/10.1007/BFb0006381
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DOI: https://doi.org/10.1007/BFb0006381
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