A mathematical model of oxidative deamination of amino acid catalyzed by two D-amino acid oxidases and influence of aeration on enzyme stability.

Two D-amino acid oxidases (DAAO) from different sources (Arthrobacter protophormiae and porcine kidney) were used to oxidatively deaminate D-methionine in the batch reactor. A mathematical model of the process was developed and validated by the experiments carried out without and with oxygen supply by aeration. Kinetic parameters of the model were estimated from the initial reaction rate experiments. Aeration increased the reaction rate in the initial part of the reaction and reduced the time necessary to achieve the final substrate conversion. However, it had a negative influence on the operational stability of enzymes. Operational stability decay rate constants estimated from the experimental data increased with the airflow rate, which indicated lower operational stability of enzymes. It was found that oxygen concentration significantly influenced the stability of DAAO from porcine kidney. Enzyme from microbial source had better operational stability and one order of magnitude lower values of decay rate constants.

Mathematical model for aldol addition catalyzed by two D-fructose-6-phosphate aldolases variants overexpressed in E. coli.

Two D-fructose-6-phosphate aldolase variants namely, single variant FSA A129S and double variant FSA A129S/A165G, were used as catalysts in the aldol addition of dihydroxyacetone (DHA) to N-Cbz-3-aminopropanal. Mathematical model for reaction catalyzed by both enzymes, consisting of kinetic and mass balance equations, was developed. Kinetic parameters were estimated from the experimental data gathered by using the initial reaction rate method. The model was validated in the batch and continuously operated ultrafiltration membrane reactor (UFMR). The same type of kinetic model could be applied for both enzymes. The operational stability of the aldolases was assessed by measuring enzyme activity during the experiments. FSA A129S/A165G had better operational stability in the batch reactor (half-life time 26.7 h) in comparison to FSA A129S (half-life time 5.78 h). Both variants were unstable in the continuously operated UFMR in which half-life times were 1.99 and 3.64 h for FSA A129S and FSA A129S/A165G, respectively.

Aldol addition of dihydroxyacetone to N-Cbz-3-aminopropanal catalyzed by two aldolases variants in microreactors.

Aldol addition of dihydroxyacetone to N-Cbz-3-aminopropanal catalyzed by two d-fructose-6-phosphate aldolase variants, FSA A129S and FSA A129S/A165G, overexpressed in Escherichia coli was studied in microreactors. The presence of organic solvent was necessary due to poor solubility of N-Cbz-3-aminopropanal in water. Hence, three co-solvents were evaluated: ethyl acetate, acetonitrile and dimethylformamide (DMF). The influence of these solvents and their concentration on the enzyme activity was independently tested and it was found that all solvents significantly reduce the activity of FSA depending on their concentration. The reaction was carried out in three different microreactors; two without and one with micromixers. By increasing enzyme concentration, it was possible to achieve higher substrate conversion at lower residence time. Enzyme activity measured at the outlet flow of the microreactor at different residence time revealed that enzymes are more stable at lower residence times due to shorter time of exposure to organic solvent. The reaction in the batch reactor was compared with the results in microreactor with micromixers. Volume productivity was more than three fold higher in microreactor with micromixers than in the batch reactor for both aldolases. It was found to be 0.88Md(-1) and 0.80Md(-1) for FSA A129S and FSA A129S/A165G, respectively.

Effect of different variables on the efficiency of the Baker's yeast cell disruption process to obtain alcohol dehydrogenase activity.

Cell disruption process of dry baker's yeast was studied in this work to obtain maximum activity of alcohol dehydrogenase (ADH). Disruption by ultrasonication, glass beads, and combination of these two methods was compared. A 1.8-fold increase of ADH activity can be achieved by combining glass beads with ultrasonication in comparison to ultrasonication. To achieve maximum volume activity of ADH, the effect of different variables on the cell disruption process was investigated (time, glass bead diameter, mass of glass beads, and ultrasound amplitude). Using the Design-Expert© software, 24 factorial experimental design was performed. Two ultrasound probes were tested: MS 73 and KE 76. Optimal conditions (process variables) for cell disruption process were obtained. Optimal ADH activities after cell disruption with MS 73 and KE 76 probes were 1,890.9 and 1,531.7 U cm⁻³, respectively. Necessary ultrasonication time and ultrasound amplitude should be at the maximum values in the investigated variable range (30 min and 62 %). Bead size should be at maximum (4 mm) when using MS 73 probe and at minimum (0.3 mm) when using KE 76 probe. Partial purification of the enzyme was carried out and it was kinetically characterized using several oxidation and reduction systems.

Evaluation of factors influencing the enantioselective enzymatic esterification of lactic acid in ionic liquid.

In this paper esterification of ethanol and lactic acid catalyzed by Candida antarctica B (Novozyme 435) in ionic liquid (Cyphos 104) was studied. The influence of different variables on lipase enantioselectivity and lactic acid conversion was investigated. The variables investigated were ionic liquid mass/lipase mass ratio, water content, alcohol excess and temperature. Using the Design Expert software 2(3) factorial experimental plan (two levels, three factors) was performed to ascertain the effect of selected variables and their interactions on the ethyl lactate enantiomeric excess and lactic acid conversion. The results of the experiments and statistical processing suggest that temperature and alcohol excess have the highest effect on the ethyl lactate enantiomeric excess, while temperature and water content have the highest influence on the lactic acid conversion. The statistical mathematical model developed on the basis of the experimental data showed that the highest enantiomeric excess achieved in the investigated variable range is 34.3%, and the highest conversion is 63.8% at the initial conditions of water content at 8%; 11-fold molar excess of alcohol and temperature at 30 °C.

Modelling as a tool of enzyme reaction engineering for enzyme reactor development.

Strategy of the development of model for enzyme reactor at laboratory scale with respect to the modelling of kinetics is presented. The recent literature on the mathematic modelling on enzyme reaction rate is emphasized.

Mathematical modeling of maltose hydrolysis in different types of reactor.

A commercial enzyme Dextrozyme was tested as catalyst for maltose hydrolysis at two different temperatures: 40 and 65 degrees C at pH 5.5. Its operational stability was studied in different reactor types: batch, repetitive batch, fed-batch and continuously operated enzyme membrane reactor. Dextrozyme was more active at 65 degrees C, but operational stability decay was observed during the prolonged use in the reactor at this temperature. The reactor efficiencies were compared according to the volumetric productivity, biocatalyst productivity and enzyme consumption. The best reactor type according to the volumetric productivity for maltose hydrolysis is batch and the best reactor type according to the biocatalyst productivity and enzyme consumption is continuously operated enzyme membrane reactor. The mathematical model developed for the maltose hydrolysis in the different reactors was validated by the experiments at both temperatures. The Michaelis-Menten kinetics describing maltose hydrolysis was used.

Mathematical modelling of NADH oxidation catalyzed by new NADH oxidase from Lactobacillus brevis in continuously operated enzyme membrane reactor.

NADH oxidase from Lactobacillus brevis was kinetically characterized in two different buffers: Tris-HCl and glycine-sodium pyrophosphate (pH 9.0). Reaction kinetics was described using the Michaelis-Menten model with product (NAD(+)) inhibition. It was found that this type of inhibition is uncompetitive. Experiments in the continuously operated enzyme membrane reactor revealed a strong enzyme deactivation at two different residence times: 12 and 60 min. A stronger deactivation was observed at the lower residence time in the glycine-sodium pyrophosphate buffer. Enzyme deactivation was assumed to be of the first order. The developed mathematical model for the continuously operated enzyme membrane reactor described these experiments very well. The mathematical model simulations revealed that a high enzyme concentration (up to 30 g cm(-3)) is necessary to obtain and maintain the stationary NADH conversion near 100% for a longer period of time.

Kinetic modeling of acetophenone reduction catalyzed by alcohol dehydrogenase from Thermoanaerobacter sp.

NADPH-dependent alcohol dehydrogenase (ADH) from Thermoanaerobacter sp. was kinetically characterized using reduction of acetophenone as a model. To achieve 98% conversion of acetophenone, cofactor regeneration by oxidation of 2-propanol with the same enzyme was used. The enzyme was stable in the batch reactor. It was enantioselective towards (S)-1-phenylethanol (ee>99.5%). Due to its high deactivation in continuously operated stirred tank reactor (kd=0.0141 min-1) there was no way to keep high conversion of acetophenone at 98%. The deactivation occurred in the repetitive batch as well. A mathematical model for the acetophenone reduction with cofactor regeneration describing the behaviour in a batch, repetitive-batch and continuously stirred tank reactor was developed.