Abstract
A formal kinetic mathematical model for poly-(3-hydroxybutyrate-co-3-hydroxyvalerate-co-4-hydroxybutyrate) [P(3HB-co-3HV-co-4HB)] terpolyester synthesis from glucose and galactose derived from whey permeate supplemented with γ-butyrolactone by the archaeon Haloferax mediterranei was created. Further, a low structured mathematical model for poly-3-hydroxybutyrate synthesis from whey permeate by Pseudomonas hydrogenovora was developed. In both cases, biosyntheses for obtaining the experimental data used for compiling the models were performed via fed-batch cultivations. The model developed for H. mediterranei consists of 10 differential and 11 algebraic equations, including 27 kinetic constants. The model compiled for P. hydrogenovora encompasses 10 differential and 3 algebraic equations, including 36 kinetic constants. Both models were solved by Runge–Kuta variable step numerical integration with Monte Carlo parameter optimization procedure. Difficulties arising from the modeling of redirection of metabolic fluxes from biomass growth toward polyhydroxyalkanoate synthesis and byproducts are discussed.
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Notes
Trace elements solution (per liter): ZnSO4·7H2O, 100 mg; H3BO3, 300 mg; CoCl2·6H2O, 200 mg; CuSO4, 6 mg; NiCl2·6H2O, 20 mg; Na2MoO4·2H2O, 30 mg; MnCl2·2H2O, 25 mg.
Abbreviations
- S 1 :
-
concentration of glucose
- S 10 :
-
concentration of glucose in feed stream
- S 2 :
-
concentration of galactose
- S 20 :
-
concentration of galactose in feed stream
- S 3 :
-
concentration of γ-butyrolactone
- S 30 :
-
concentration of γ-butyrolactone in feed stream
- N :
-
concentration of inorganic nitrogen source
- NK:
-
concentration of complex nitrogen source
- P 1 :
-
concentration of P-3HB
- P 2 :
-
concentration of P-3HV
- P 3 :
-
concentration of P-4HB
- PHA:
-
concentration of PHA (PHA = P 1 + P 2 + P 3)
- P t max :
-
maximum biologically possible PHA concentration
- X r :
-
concentration of residual biomass
- H :
-
concentration of yeast extract
- MXr :
-
mass of residual biomass in reactor volume
- MS1 :
-
mass of glucose in reactor volume
- MS2 :
-
mass of galactose in reactor volume
- MS3 :
-
mass of γ-butyrolactone in reactor volume
- MP1 :
-
mass of P-3HB in reactor volume
- MP2 :
-
mass of P-3HV in reactor volume
- MP3 :
-
mass of P-4HB in reactor volume
- MPt :
-
mass of total polymer; MPt = MP1 + MP2 + MP3
- MH:
-
mass of yeast extract in reactor volume
- V :
-
working volume
- V 0 :
-
starting volume
- F i :
-
inflow (fed-batch) in time interval “i”
- (t i :
-
time intervals for substrate inflows
- μ (j)max :
-
partial maximal specific growth rates on substrate j=1–3
- q p(j)s(k) :
-
specific production rates of products j=1–3 on substrates k=1–3
- Y x/s(k) :
-
partial yield coefficients for residual biomass on substrates k=1–3
- IPR:
-
mass fraction of Ac-CoA in the residual biomass; IPR = PR/X 1
- IEK:
-
mass fraction of PHB-polymerase in the residual biomass; IEK = POL/X 1
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Acknowledgment
This work was supported by Wheypol Growth EC-Project GRD2-2000-30385.
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Koller, M., Horvat, P., Hesse, P. et al. Assessment of formal and low structured kinetic modeling of polyhydroxyalkanoate synthesis from complex substrates. Bioprocess Biosyst Eng 29, 367–377 (2006). https://doi.org/10.1007/s00449-006-0084-x
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DOI: https://doi.org/10.1007/s00449-006-0084-x