An enzyme kinetic model for describing fermentation processes

An enzyme kinetic model has been proposed to describe fermentation processes. This type of model was chosen because it is biologically sound, can incorporate all of the important engineering control variables, and can draw upon, in its development, the extensive kinetic literature. An intial qualitative test for this model was made on the gluconic acid fermentation. A necessary check of the model was that Monod's empirical cell growth and yield equations were derived as a special case. The model also offered an explanation for the hysteresis behavior of the gluconic acid production rate as a function of gluconolactone.     

Kinetics of the conversion of glucose to gluconic acid by Pseudomonas ovalis

The concept of a “critical oxygen concentration” is conventionally considered to hold for the submerged aerobic fermentation of glucose to gluconic acid. Above the critical level the fermentation rate is supposedly independent of oxygen concentration. In this work it is shown that, at a given agitation rate, the fermentation is independent of dissolved oxygen when above the critical. However, an increase in the agitation rate results in an increase in the fermentation rate. This increase was shown to be accompanied by an increase in the gluconolactone concentration in the broth. Gluconolactone, an intermediate in the reaction pathway, is hydrolyzed nonenzymatically to gluconic acid. Evidence is presented to suggest that the increased gas-liquid interfacial area brought about by increased agitation causes an increased net rate of lactone formation. This in turn results in an increased rate of hydrolysis of the lactone to gluconic acid. A model is presented hypothesizing that negatively charged cells adsorb at the gas-liquid interface. These cells attract hydrogen ions, causing a lowering of the pH in the film around the bubbles. It is this lowered pH which is considered to bring about increased fermentation rates when the interfacial area is increased. Supporting evidence is presented.     

A multikinetic model approach to predict gluconic acid production in an airlift bioreactor

This paper uses a multikinetic approach to predict gluconic acid (GA) production performance in a 4.5 L airlift bioreactor (ALBR). The mathematical model consists of a set of simultaneous firstorder ordinary differential equations obtained from material balances of cell biomass, GA, glucose, and dissolved oxygen. Multikinetic models, namely, logistic and contois equations constitute kinetic part of the main model. The main model also takes into account the hydrodynamic and mass transfer parameters. These equations were solved using ODE solver of MATLAB v6.5 software. The mathematical model was validated with the experimental data available in the literature and is used to predict the effect of change in initial biomass and air sparging rate on the GA production. It is concluded that the mathematical model incorporated with multikinetic approach would be more efficient to predict the change in operating parameters on overall bioprocess of GA production in an ALBR.     

Dynamic modelling of aerobic bioprocesses in gel particles with immobilised cells

A dynamic model for aerobic growing cells immobilised into gel beads is developed and its operation is illustrated for the case of gluconic acid production by a strictly aerophilic strain of Gluconobacter oxydans. The model consists of both kinetic and mass transfer equations predicting the time course of bulk and intraparticle concentrations of substrates, products, and biomass. The model includes a product inhibition term. The parameter values are taken from own studies and from the literature. A sensitivity analysis of the model shows that the most significant parameters for the process are the biotransformation rate constant, the specific cell growth rate in the bulk, and the Thiele modulus for glucose. The computer simulation reveals that depending on the parameter values the gel particles might perform as a source or a sink of the product, thus enhancing or retarding the net process. For a specific parameter selection, the biotransformation in the pellets can prevail compared with the bulk in the beginning of the process as long as the direction of the product diffusion flux is from the beads toward the bulk. Since the process in the free culture dominates, the system is more sensitive to parameters associated with the bulk phase (aeration rate, specific microbial growth rate, oxygen uptake rate). The model can be applied for prediction and fast evaluation of the performance of aerobic processes accomplished by immobilised growing cells.     

Reaction kinetics of cephalexin synthesizing enzyme from Xanthomonas citri

In enzymatic synthesis of cephalexin from D-alpha-phenylglycine methyl ester (PGM) and 7-amino-3-deacetoxy-cephalosporanic acid (7-ADCA) using alpha-acylamino-beta-lactam acylhydrolase from Xanthomonas citri, it was found that this enzyme catalyzes all three reactions including PGM hydrolysis, cephalexin synthesis, and cephalexin hydrolysis. Based on our experimental results, a mechanistic kinetic model for cephalexin synthesizing enzyme system having acyl-enzyme intermediate was proposed. From this kinetic model, the reaction rate equations for three reactions were derived, and the kinetic parameters were evaluated. A good agreement between the simulation results and the experimental results was found.     

Numerical simulation of a glucose sensitive composite membrane closed-loop insulin delivery system

Closed-loop insulin delivery system works on pH modulation by gluconic acid production from glucose, which in turn allows regulation of insulin release across membrane. Typically, the concentration variation of gluconic acid can be numerically modeled by a set of non-linear, non-steady state reaction diffusion equations. Here, we report a simpler numerical approach to time and position dependent diffusivity of species using finite difference and differential quadrature (DQ) method. The results are comparable to that obtained by analytical method. The membrane thickness directly determines the concentrations of the glucose and oxygen in the system, and inversely to the gluconic acid. The advantage with the DQ method is that its parameter values need not be altered throughout the analysis to obtain the concentration profiles of the glucose, oxygen and gluconic acid. Our work would be useful for modeling diabetes and other systems governed by such non-linear and non-steady state reaction diffusion equations.     

Modelling and off line optimization of batch gluconic acid fermentation

Summary The role of mathematical modelling and off line optimization for a batch fermentation process is described. The fermentation of gluconic acid by Acetobacter suboxydans ATCC 621 was studied. The model is based on a series of batch experiments in which the temperature was the only variable. The differential equations of the models were derived from these experiments to give the kinetic parameters and the parametric models varying with the temperature. The fermentation was optimized using Pontryagin's maximum principle. This gave the temperature profile of fermentation.Abbreviations x, g, l, S, c, P The concentration of cell mass, glucose, lactone, gluconic acid, 5-ketogluconic acid and total acidic products respectively - r₁, r₂ E₁ or E₂ enzyme in complex/total E₁ or E₂ enzyme content - a, b E₁ and E₂ enzyme content of unit quantity of biomass - k_i and K_j Rate constants - _max Maximum specific growth rate - y_x z₁=r₁x z₂=r₂x Yield coefficient of biomass with respect to growth on glucose - z₁ r₁x - z₂ r₂x     

Sorbitol production in charged membrane bioreactor with coenzyme regeneration system: II. Theoretical analysis of a continuous reaction with retained and regenerated NADPH

A theoretical model was constructed in order to study charged membrane bioreactors (CMBRs). In this model, it was postulated that a native nicotinamide coenzyme NADP(H) can be partially retained by a charged membrane in continuous operation. A multienzyme system composed of NADPH-dependent aldose reductase (AR) and glucose dehydrogenase (GDH) was used for the production of sorbitol and gluconic acid from glucose and for the conjugated enzymatic regeneration of NADP(H). Both enzymes were studied with respect to their reaction kinetics. AR was determined to obey the Theorell-Chance mechanism. GDH reaction was approximated by the initial velocity equation of the sequential Bi-Bi mechanism since the reverse reaction could be neglected. Significant inhibitions of both enzymes by sorbitol, gluconic acid, and glucose were observed, and the mode of inhibition was estimated to modify the velocity equations. The differential equation system for each component was derived and numerically analyzed according to the model. The theoretical model elucidated several features of the CMBR. (1) When compared at the same productivity, higher retainment was found to bring about a higher coenzyme turnover number, indicating that the feed coenzyme concentration can be reduced. (2) Under constant conversion, a contradictory relationship between turnover number and residence time arises if the feed concentration of a coenzyme varies. The theoretical model predicts that there is a practically optimal concentration for using NADP(H) efficiently. This concentration was consistent with that yielding the estimated minimum total cost. (3) In this system, excess-GDH-to-AR activity was required because of differences in their kinetic constants. The amount of regeneration enzyme required can be reduced by the accumulation of excels NADPH due to coenzyme retainment. (4) Comparison with an ideal repeated batch reaction revealed that the continuously operated CMBR was vastly superior with respect to productivity as well as operation ability.     

Kinetic studies of the reactions catalyzed by glucose-6-phosphate dehydrogenase from Leuconostoc mesenteroides: pH variation of kinetic parameters

The specificity and kinetic parameters of the reactions catalyzed by glucose-6-phosphate dehydrogenase from Leuconostoc mesenteroides has been examined under a range of conditions in order to elucidate details about the mechanism of action of this enzyme. The rate of oxidation of glucose 6-phosphate is inhibited by the addition of various organic solvents. However, the low, inherent glucose dehydrogenase activity of this enzyme was stimulated under these conditions, and was further activated by divalent anions that were observed to be inhibitors of the glucose 6-phosphate dehydrogenation. From an examination of the pH variation of the enzyme kinetic parameters two groups on the enzyme that appear to be involved in the binding of the phosphate group of the sugar substrate have been detected. An enzyme catalytic group, probably a carboxylic acid, has been identified that accepts the proton from the hydroxyl group at carbon-1 of the sugar substrate during its oxidation to a lactone. The ionization of a group on the enzyme with a pK of 8.7 resulted in an increase in the maximum velocity of the glucose-6-phosphate dehydrogenase activity of the enzyme as a consequence of a pH-dependent product release step that is no longer rate limiting at high pH. Stabilization of gluconic acid-delta-lactone against nonenzymatic hydrolysis by organic solvents has allowed the kinetic parameters of the reverse reaction to be reliably measured for the first time in a narrow pH range.     

A rapid method of evaluating permeabilizing activity against Pseudomonas aeruginosa

A rapid (< 30 min) spectrophotometric method has been used to assess the ability of chemical agents to permeabilize the outer membrane of Pseudomonas aeruginosa. When permeabilized, the cells are rendered readily sensitive to lysozyme, an enzyme that is normally excluded from the peptidoglycan of this organism. In addition to ethylenediamine tetraacetic acid, substances showing permeabilizing activity were citric, isocitric, malic and gluconic acids (but not gluconic acid lactone) and sodium polyphosphate.     

Optimization of gluconic acid synthesis by removing limitations and inhibitions

The optimization task was performed using the gluconic acid synthesis by the Acetobacter methanolicusMB 58 strain. The microorganisms were grown continuously on methanol as the growth substrate. After finishing the growth process by the deficiency of N and P, the gluconic acid synthesis was started by adding glucose. The synthesis process was performed continuously. The oxygen transfer rate depended on the gluconic acid concentration. During the growth process, the oxygen transfer rate reached a value of about 13 g O₂ · kg^?1 · h^?1using a 30-l glass fermenter equipped with a 6 blade stirrer and fully baffled. This rate declined to a value of between 2 and 5 g O₂ · kg^?1 · h^?1 in the presence of gluconic acid concentrations above 150 g gluconic acid · kg^?1medium. The yield (g gluconic acid · g^?1glucose) depended on the gluconic acid concentration and amounted to y = 0.7 in relation to 150 g gluconic acid · kg^?1medium and y = 0.8 in relation to 200 g · kg^?1medium, respectively. The fermenters were coupled with ultrafiltration moduls (Fa. ROMICON and Fa. SARTORIUS). The biomass concentrations amounted from 5 to 40 g dry mass kg^?1medium. The ultrafiltration modules retained the biomass within the fermentation system. A glucose solution (30 to 50 weight percent glucose) was continuously dosed into the fermenter. The retention time was chosen between 2 and 30 h. The gluconic acid synthesis rate reached values of up to 32 g gluconic acid · kg^?1 · h^?1. Within a range of up to 250 g gluconic acid · kg^?1medium, the acid concentration had no influence on the enzyme activity.     

A Procedure for gluconic acid synthesis with bacteria made continuous by means of an auxiliary substrate

A method is introduced which makes a continuous oxidation of glucose to glucose acid possible. This method is based on the auxiliary-substrate concept and co-metabolism, respectively. Micro-organisms (e.g. Acinetobacter calcoaceticus), which cannot assimilate glucose, but merely oxidize it, are grown continuously on a heterotrophic substrate (e.g. acetate). While growing they simultaneously synthesize gluconic acid. The productivity of the gluconic acid synthesis with a given strain depends on the dilution rate and the mixing proportion. Since growth and product synthesis are closely connected and growth yield is very much higher due to an auxiliary substrate effect in the presence of glucose than on the heterotrophic substrate alone, this method is suitable for SCP production as well. The productivity of gluconic acid production is controlled at a certain dilution rate by the mixing proportion of the growth substrate and glucose.     

Bioconversion of waste office paper to gluconic acid in a turbine blade reactor by the filamentous fungus Aspergillus niger

Gluconic acid production was investigated using an enzymatic hydrolysate of waste office automation paper in a culture of Aspergillus niger. In repeated batch cultures using flasks, saccharified solution medium (SM) did not show any inhibitory effects on gluconic acid production compared to glucose medium (GM). The average gluconic acid yields were 92% (SM) and 80% (GM). In repeated batch cultures using SM in a turbine blade reactor (TBR), the gluconic acid yields were 60% (SM) and 67% (GM) with 80-100 g/l of gluconic acid. When pure oxygen was supplied the production rate increased to four times higher than when supplying air. Remarkable differences in the morphology of A. niger and dry cell weight between SM and GM were observed. The difference in morphology may have caused a reduction of oxygen transfer, resulting in a decrease in gluconic acid production rate in SM.     

Bioconversion of grape must into modulated gluconic acid production by Aspergillus niger ORS-4.410

AIMS: Analysis of regulators for modulated gluconic acid production under surface fermentation (SF) condition using grape must as the cheap carbohydrate source, by mutant Aspergillus niger ORS-4.410. Replacement of conventional fermentation condition by solid-state surface fermentation (SSF) for semi-continuous production of gluconic acid by pseudo-immobilization of A. niger ORS-4.410. METHODS AND RESULTS: Grape must after rectification was utilized for gluconic acid production in batch fermentation in SF and SSF processes using mutant strain of A. niger ORS-4.410. Use of rectified grape must led to the improved levels of gluconic acid production (80-85 g l(-1)) in the fermentation medium containing 0.075% (NH4)2HPO4; 0.1% KH2PO4 and 0.015% MgSO4.7H2O at an initial pH 6.6 (+/-0.1) under surface fermentation. Gluconic acid production was modulated by incorporating the 2% soybean oil, 2% starch and 1% H2O2 in fermentation medium at continuously high aeration rate (2.0 l min(-1)). Interestingly, 95.8% yield of gluconic acid was obtained when A. niger ORS-4.410 was pseudo-immobilized on cellulose fibres (bagasse) under SSF. Four consecutive fermentation cycles were achieved with a conversion rate of 0.752-0.804 g g(-1) of substrate into gluconic acid under SSF. CONCLUSIONS: Use of additives modulated the gluconic acid production under SF condition. Semi-continuous production of gluconic acid was achieved with pseudo-immobilized mycelia of A. niger ORS-4.410 having a promising yield (95.8%) under SSF condition. SIGNIFICANCE AND IMPACT OF THE STUDY: The bioconversion of grape must into modulated gluconic acid production under SSF conditions can further be employed in fermentation industries by replacing the conventional carbohydrate sources and expensive, energy consuming fermentation processes.     

Cytochrome P-450-catalyzed hydroxylation and carboxylic acid ester cleavage of Hantzsch pyridine esters

Cytochrome P-450 (P-450)-catalyzed oxidation of 2,6-dimethyl-4-phenyl-3,5-pyridinedicarboxylic acid diethyl ester gives rise to 2,6-dimethyl-4-phenyl-3,5-pyridinedicarboxylic acid monoethyl ester and to 2-hydroxymethyl-6-methyl-4-phenyl-3,5-pyridinedicarboxylic acid diethyl ester, identified in this work. A pyridine hydroxymethyl diester of the sort of the latter compound is novel; under acidic or dehydrating conditions the diester is readily converted to a cyclic lactone (2-hydroxymethyl-6-methyl-4-phenyl-3,5-pyridinedicarboxylic acid 5-ethyl ester lactone). 2,6-Dimethyl-4-phenyl-3,5-pyridinedicarboxylic acid monoethyl ester was not hydroxylated to form this hydroxymethyl compound or lactone, but 1,4-dihydro-2-hydroxymethyl-4-phenyl-6-methyl-3,5-pyridinedicarboxyli c acid diethyl ester was enzymatically oxidized to give both products. The rates of oxidative carboxylic ester cleavage and methyl hydroxylation varied among individual forms of P-450 tested. Experiments with 2H and 3H labels were used to estimate an intrinsic kinetic deuterium isotope effect of 15 for ethyl ester cleavage by rat liver P-450PB-B in a reconstituted system. Rat liver microsomal systems showed kinetic deuterium and tritium isotope effects of 8 and 11, respectively, and this deuterium isotope effect was not attenuated in either intra- or intermolecular competitive experiments. When deuterium was present in the ethyl (ester) groups, increases in the rate of 2-methyl hydroxylation were observed in rat liver microsomes and with purified P-450 beta NF-B (but not with P-450PB-B). Deuteration of the methyl groups gave rise to kinetic isotope effects of 7-11, but no increases were seen in the rates of ester cleavage. These studies and those on rates of substrate disappearance indicate that isotopically sensitive branching (metabolic switching) observed in these systems is not necessarily bidirectional.     

Continuous production of gluconic acid by immobilized Gluconobacter oxydans cell bioreactor

Summary Living Gluconobacter oxydans cells were attached on fibrous nylon carrier. Free gluconic acid was directly continuously produced in an aerated tubular immobilized-cell bioreactor for at least 6 months, with a volumetric productivity of at least 5 g/lh at 100 g/l substrate glucose and about 80 g/l product gluconic acid concentrations. The highest volumetric productivity in respect to glucose concentration was obtained with 175 g/l glucose, with about 120 g/l product gluconic acid level. With self-directing optimization procedure in respect to maximum product gluconic acid level, productivities as high as about 12–15 g/lh were obtained at relatively high substrate feed rate of 0.166 l/lh and relatively low aeration rate of 0.5 l/lmin. The highest glucose conversion of about 96% was obtained with a long residence time, at the lowest substrate feed rate used at a relatively low aeration rate, resulting however in a significant increase in ketogluconic acid production.     

Kinetic investigation of a solvent-free, chemoenzymatic reaction sequence towards enantioselective synthesis of a β-amino acid ester

A solvent-free, chemoenzymatic reaction sequence for the enantioselective synthesis of β-amino acid esters has been kinetically and thermodynamically characterized. The coupled sequence comprises a thermal aza-Michael addition of cheap starting materials and a lipase catalyzed aminolysis for the kinetic resolution of the racemic ester. Excellent ee values of >99% were obtained for the β-amino acid ester at 60% conversion. Kinetic constants for the aza-Michael addition were obtained by straightforward numerical integration of second-order rate equations and nonlinear fitting of the progress curves. A different strategy had to be devised for the biocatalytic reaction. Initially, a simplified Michaelis-Menten model including product inhibition was developed for the reaction running in THF as an organic solvent. Activity based parameters were used instead of concentrations in order to facilitate the transfer of the kinetic model to the solvent-free system. Observed solvent effects not accounted for by the use of thermodynamic activities were incorporated into the kinetic model. Enzyme deactivation was observed to depend on the ratio of the applied substrates and also included in the kinetic model. The developed simple model is in very good agreement with the experimental data and allows the simulation and optimization of the solvent-free process.     

Process optimization of continuous gluconic acid fermentation by isolated yeast-like strains of Aureobasidium pullulans

This study was focused on the optimization of a new fermentation process for continuous gluconic acid production by the isolated yeast-like strain Aureobasidium pullulans DSM 7085 (isolate 70). Operational fermentation parameters were optimized in chemostat cultures, using a defined glucose medium. Different optima were found for growth and gluconic acid production for each set of operation parameters. Highest productivity was recorded at pH values between 6.5 and 7.0 and temperatures between 29 and 31 degrees C. A gluconic acid concentration higher than 230 g/L was continuously produced at residence times of 12 h. A steady state extracellular gluconic acid concentration of 234 g/L was measured at pH 6.5. 122% air saturation yielded the highest volumetric productivity and product concentration. The biomass-specific productivity increased steadily upon raising air saturation. An intracellular gluconic acid concentration of about 159 g/L (0.83 mol) was determined at 31 degrees C. This is to be compared with an extracellular concentration of 223 g/L (1.16 mol), which indicates the possible existence of an active transport system for gluconic acid secretion, or the presence of extracellular glucose oxidizing enzymes. The new process provides significant advantages over the traditional discontinuous fungi operations. The process control becomes easier, thus offering stable product quality and quantity.     

Modeling and kinetic analysis of the reaction system using whole cells with separately and co-expressed D-hydantoinase and N-carbamoylase

We developed a kinetic model that describes a heterogeneous reaction system for the production of D-p-hydroxyphenylglycine from D,L-p-hydroxyphenyl-hydantoin using D-hydantoinase of Bacillus stearothermophilus SD1 and N-carbamoylase of Agrobacterium tumefaciens NRRL B11291. As a biocatalyst, whole cells with separately or co-expressed enzymes were used. The reaction system involves dissolution of substrate particles, enzymatic conversion, racemization of the L-form substrate, and transfer of the dissolved substrate, intermediate, and product through the cell membrane. Because the two enzymes have different pH optimum, kinetic parameters were evaluated at different pH for the reaction systems. The model was simulated using the kinetic parameters and compared with experimental data, and it was found that the kinetic model well describes the behavior of the reaction systems using whole cells with separately and co-expressed enzymes. Factors affecting the kinetics of the reaction systems were analyzed on the basis of the kinetic model. In the reaction system with separately expressed enzymes, racemization rate and transport of the reaction intermediate (N-carbamoyl-D-p-hydroxyphenylglycine) were revealed to be the limiting factors at neutral pH, resulting in accumulation of intermediate in the reaction medium. At alkaline condition, on the other hand, inhibition of N-carbamoylase by ammonia was severe, and thereby the reaction rate significantly reduced. In the co-expressed enzyme system, accumulation of intermediate was negligible in the reaction medium, and the improved performance was observed compared to that with separately expressed enzymes. The present model might be applied for the optimization and development of the reaction system using two sequential enzymes.