Evaluation of D-amino acid oxidase from Rhodotorula gracilis for the production of alpha-keto acids: a reactor system

The study reports on the development of a bioreactor for the production of alpha-keto acids from D,L- or D-amino acids using Rhodotorula gracilis D-amino acid oxidase. D-Amino acid oxidase was co-immobilized with catalase on Affi-Gel 10 matrix, and the reactor was operated as a continuous-stirred tank reactor (CSTR) or stirred tank with medium recycling conditions. The optimum substrate concentration and quantity of biocatalyst were determined (5 mM and 1.2 mg/L, respectively). Under optimum operating conditions, product formation was linearly related to both substrate and enzyme concentration, showing the system to be highly flexible. Under these conditions, in a stirred tank, over 90% conversion was achieved in 30 min with a maximum production of 0.23 g of pyruvic acid/day/enzyme units. Product was recovered by ion exchange chromatography. The operational stability of the reactor was high (up to 9.5 h of operation without loss of activity) and the inactivation half-life was not reached even after 18 h or 36 bioconversion cycles. This represents the first case of a reactor developed successfully with a D-amino acid oxidase. (c) 1994 John Wiley & Sons, Inc.     

Modeling and simulation of enzymatic gluconic acid production using immobilized enzyme and CSTR–PFTR circulation reaction system

Objectives

Production of gluconic acid by using immobilized enzyme and continuous stirred tank reactor-plug flow tubular reactor (CSTR–PFTR) circulation reaction system.

Results

A production system is constructed for gluconic acid production, which consists of a continuous stirred tank reactor (CSTR) for pH control and liquid storage and a plug flow tubular reactor (PFTR) filled with immobilized glucose oxidase (GOD) for gluconic acid production. Mathematical model is developed for this production system and simulation is made for the enzymatic reaction process. The pH inhibition effect on GOD is modeled by using a bell-type curve.

Conclusions

Gluconic acid can be efficiently produced by using the reaction system and the mathematical model developed for this system can simulate and predict the process well.

     

Kinetic Modeling of Acetophenone Reduction Catalyzed by Alcohol Dehydrogenase from <Emphasis Type="Italic">Thermoanaerobacter</Emphasis> 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 (k_d=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.     

Scale-up of enzymatic production of lactobionic acid using the rotary jet head system

Enzymatic oxidation of lactose to lactobionic acid (LBA) by a carbohydrate oxidase from Microdochium nivale was studied in a pilot-scale batch reactor of 600 L working volume using a rotary jet head (RJH) for mixing and mass transfer (Nordkvist et al., 2003, Chem Eng Sci 58:3877-3890). Both lactose and whey permeate were used as substrate, air was used as oxygen source, and catalase was added to eliminate the byproduct hydrogen peroxide. More than 98% conversion to LBA was achieved. Neither enzyme deactivation nor enzyme inhibition was observed under the experimental conditions. The dissolved oxygen tension (DOT) was constant throughout the tank for a given set of operating conditions, indicating that liquid mixing was sufficiently good to avoid oxygen gradients in the tank. However, at a given oxygen tension measured in the tank, the specific rate of reaction found in the RJH system was somewhat higher than previously obtained in a 1 L mechanically stirred tank reactor (Nordkvist et al., 2007, in this issue, pp. 694-707). This can be ascribed to a higher pressure in the recirculation loop which is part of the RJH system. Compared to mechanically stirred systems, high values of the volumetric mass transfer coefficient, k(L)a, were obtained when lactose was used as substrate, especially at low values of the specific power input and the superficial gas velocity. k(L)a was lower for experiments with whey permeate than with lactose due to addition of antifoam. The importance of mass transfer and of the saturation concentration of oxygen on the volumetric rate of reaction was demonstrated by simulations.     

Conversion of benzylpenicillin to 6-aminopenicillanic acid in a batch reactor and continuous feed stirred tank reactor using immobilized penicillin amidase

A rate equation has been derived to describe the hydrolysis of benzylpenicillin to 6-aminopenicillanic acid by penicillin amidase. The integrated from of the rate equation has been shown to predict satisfactorily the progress of the reaction in a batch reactor using either soluble or immobilized penicillin amidase. The rate equation was also used to predict the performance of a continuous feed stirred tank reactor containing immobilized enzyme. There was good agreement with experimental measurements.     

Parallel substrate feeding and pH-control in shaking-flasks

An intermittent feeding system for shaking-flasks was developed to close the gap between batch operated shaking-flasks and fed-batch operated as well as pH-controlled stirred tank reactors. A precise syringe pump was connected via a substrate distribution system to individual 2/2-way miniature valves, one for each of up to 16 shaking-flask. The shaking-flasks were equipped with pH-probes. A process computer controls the intermittent feeding of substrates by tracking predefined individual feeding profiles as well as the base (or acid) addition for individual pH-control of the shaking-flasks. Higher concentrations of aerobic cells with higher cellular activities were achieved in fed-batch operated and pH-controlled shaking-flasks as compared to the conventional batch operation. Physiological effects of an intermittent feeding were studied in a stirred tank reactor with a recombinant E. coli strain, which expressed the GDP-mannose-pyrophosphorylase enzyme under the control of the lac-promoter.     

Modeling and simulation of a pressure-swing reactor for the conversion of poorly soluble substrate by immobilized enzyme: the case of d-hydantoinase reaction

An immobilized enzyme reactor system for converting poorly soluble substrate is proposed. In this stirred batch reactor, the solid substrate and immobilized enzyme suspensions are separated by a microporous filter. The advantage of separating the solid substrate from immobilized enzyme is that the fouling and breakage of the immobilized enzyme usually encountered in the stirred tank reactor can be prevented. Pressure swing can be applied to enhance the mass transfer between the two compartments. The hydrolytic reaction converting the poorly soluble substrate p-hydroxyphenylhydantoin (pHPH) into soluble N-carbamoyl-p-d-hydroxyphenylglycine (CpHPG) by immobilized d-hydantoinase is carried out in this reactor. The performance of this pressure-swing reactor is studied by simulation using a simple kinetic model. The pressure-swing operation increases the overall production rate significantly. The pressure swing also makes the reactor perform better for converting the solid substrate at higher concentration.     

Stirred Tank Two-Liquid Phase Biocatalytic Reactor Studies: Kinetics, Evaluation and Modelling of Substrate Mass Transfer

Kinetic measurements of the benzyl acetate hydrolysis by pig liver esterase in a two-liquid phase stirred tank reactor were made at a variety of aqueous phase enzyme concentrations and stirrer speeds. All experiments were performed in an inverted liquid-liquid system at a high phase ratio. The results were explained in terms of the aqueous phase bulk reaction model developed from previous Lewis cell studies. An algorithm is presented for the indirect measurement of the substrate mass transfer coefficient and consequently a model was developed to predict reaction rates. While the model describes the kinetics effectively, and could therefore be used to predict reactor behaviour, no difference was observed between kinetic measurements made at a stirrer speed of 750 and 1000 rpm.     

Continuous alpha-amylase production using Bacillus amyloliquefaciens adsorbed on an ion exchange resin

Summary A method for the continuous production of extracellular alpha amylase by surface immobilized cells of Bacillus amyloliquefaciens NRC 2147 has been developed. A large-pore, macroreticular anionic exchange resin was capable of initially immobilizing an effective cell concentration of 17.5 g DW/1 (based on a total reactor volume of 160 ml). The reactor was operated continuously with a nutrient medium containing 15 g/l soluble starch, as well as yeast extract and salts. Aeration was achieved by sparging oxygen enriched air into the column inlet. Fermentor plugging by cells was avoided by periodically substituting the nutrient medium with medium lacking in both soluble starch and yeast extract. This fermentor was operated for over 200 h and obtained a steady state enzyme concentration of 18700 amylase activity units per litre (18.7 kU/l), and an enzyme volumetric productivity of 9700 amylase activity units per litre per hour (9.7 kU/l-h). Parallel fermentations were performed using a 2 l stirred vessel fermentor capable of operation in batch and continuous mode. All fermentation conditions employed were identical to those of the immobilized cell experiments in order to assess the performance of the immobilized cell reactor. Batch stirred tank operation yielded a maximum amylase activity of 150 kU/l and a volumetric productivity of 2.45 kU/l-h. The maximum cell concentration obtained was 5.85 g DW/l. Continuous stirred tank fermentation obtained a maximum effluent amylase activity of 6.9 kU/l and a maximum enzyme volumetric productivity of 2.73 kU/l-h. Both of these maximum values were observed at a dilution rate of 0.345 l/h. The immobilized cell reactor was observed to achieve larger volumetric productivities than either mode of stirred tank fermentation, but achieved an enzyme activity concentration lower than that of the batch stirred tank fermentor.     

Lipase catalysed hydrolysis of ricebran oil by free and immobilised enzyme system in batch stirred reactor

A change of the reaction rate was observed for the lipasecatalysed hydrolysis of ricebran oil in a batch stirred tank reactor using immobilized lipase enzyme as compared to free enzyme. The reactor rate was observed to be controlled mainly by factors like temperature, pH, initial enzyme concentration, initial substrate concentration and initial products concentration.     

Design of a tubular loop bioreactor for scale-up and scale-down of fermentation processes

Microorganisms traveling through circulation loops in large-scale bioreactors experience variations in their environment such as dissolved oxygen concentration and pH gradients. The same changes are not experienced in small bioreactors, and it is suggested that herein lies one of the major reasons for the problems encountered when translating fermentation data from one scale to another. One approach to study this problem is to look at the circulation loop itself. The present work concerns an attempt to simulate the circulation loops inside stirred tank reactors, using a tubular loop reactor specially constructed for the purpose. The reactor carries a number of ports and probes along its length for the determination of concentration gradients within. The broth is circulated around the loop by the use of peristaltic pumps, and the circulation time (t(c), s) is used as a measure of simulated reactor size. The reactor system has been evaluated using the citric acid fermentation by Aspergillus niger as a test process. Acid production and fungal morphology, in terms of the mean convex perimeter of mycelial clumps quantified by image analysis, were used as the parameters of evaluation for the two systems in comparison. From comparative experiments carried out in 10 and 200 L stirred tank bioreactors, it appears that the loop reactor simulates the corresponding stirred tank representing a valuable tool in scaling up and scaling down of fermentation process.     

A process for bioconversion of cephalosporin C by Rhodotorula gracilis D-amino acid oxidase

Summary A process for the production (in a stirred tank reactor) of glutaryl-7-ACA from cephalosporin C using immobilized D-amino acid oxidase is described. Results so obtained under optimal conditions (1.2 mg coupled enzyme/L, pH 8.5, 2 mM cephalosporin C) point to a system which shows high conversion efficiency and a remarkable operational stability. No exogenous H₂O₂ is requested to shift the reaction equilibrium toward glutaryl-7-ACA production, nor any side product is detected. The immobilized system productivity was 54 g/day/mg of enzyme. This process represents the first reported case of a reactor successfully developed with a DAAO for bioconversion of cephalosporin C.     

Study of microencapsulated urease in a continuous feed,stirred tank reactor

Urease, (urea amidohydrolase, EC 3.5.1.5) co-encapsulated with haemoglobin in cellulose nitrate membranes was found to exhibit apparent Michaelis-Menten kinetics; however, a steadily increasing apparent Michaelis-Menten constant over the lifetime of the preparation was observed. The activity of the enzyme in a continuous feed stirred tank reactor (CSTR) was investigated and correlated with a mathematical model derived from basic Michaelis-Menten kinetics. Plots relating substrate conversion to feed substrate concentration and tank reactor capacity were constructed and found to be accurate to less than 15% error under the experimental conditions studied.     

Study of gaseous substrate fermentations: carbon monoxide conversion to acetate. 2. Continuous culture

The fermentation of gaseous substrates such as CO, H(2), and CO(2) may be performed in a continuous stirred tank reactor, as well as the traditional batch reactor. In this article, the conversion of carbon monoxide by Peptostreptococcus productus is demonstrated in a stirred tank reactor under both mass transfer-controlled and nonmass transfer-controlled conditions. Utilizing a non-steady-state procedure, intrinsic rates are evaluated under non-mass transfer-controlled conditions in a time period of only 5-6 hours. A steady-state procedure was used to evaluate CSTR performance under mass transfer-controlled conditions. The mass transfer coefficient was calculated, followed by the development of a model to predict CSTR behavior for this gas phase substrate.     

Strategies for the design and operation of enzymatic reactors for the degradation of highly and poorly soluble recalcitrant compounds

The presence of recalcitrant compounds in both wastewaters and soils is an important environmental problem. Oxidative enzymes from white-rot fungi have been successfully utilised for the in vitro degradation of xenobiotics, such as the azo dye Orange II and the polycyclic aromatic hydrocarbon anthracene (compounds with high and low solubilities, respectively). Two different reactor configurations are proposed: (i) an enzymatic membrane reactor for the treatment of soluble compounds, consisting of a continuous stirred tank reactor coupled to an ultrafiltration membrane to facilitate the retention and recycling of enzyme; and (ii) a two-phase enzymatic reactor for the degradation of poorly soluble compounds, consisting of an immiscible solvent, which contains the contaminant at high concentrations, and the aqueous phase containing the enzyme and cofactors involved in the catalytic cycle. In this paper, factors affecting the design and operation of both systems are discussed, and experimental results concerning the efficiency and stability of the processes are presented.     

The effect of bovine serum albumin on batch and continuous enzymatic cellulose hydrolysis mixed by stirring or shaking

Bovine serum albumin (BSA) was applied as a model non-catalytic protein to enzymatic hydrolysis of Avicel and dilute acid pretreated corn stover at different reaction conditions to improve the understanding of its ability to enhance cellulose hydrolysis. Addition of BSA improved the 72 h hydrolysis yields in shake flasks by up to 26% for both substrates by reducing de-activation of the exoglucanases and by facilitating reductions in particle size and crystallinity during a magnetically stirred pre-incubation step. The enzyme stabilizing effect of BSA addition was most striking for batch hydrolysis in a stirred tank reactor, with glucose yields increasing by 76% after 72 h for Avicel and by 40% after 145 h for corn stover. Application of BSA to continuous hydrolysis for a mean residence time of 24h gave 33% and 40% higher glucose yields for corn stover and Avicel compared to the controls.     

Strategies for the design and operation of enzymatic reactors for the degradation of highly and poorly soluble recalcitrant compounds

The presence of recalcitrant compounds in both wastewaters and soils is an important environmental problem. Oxidative enzymes from white-rot fungi have been successfully utilised for the in vitro degradation of xenobiotics, such as the azo dye Orange II and the polycyclic aromatic hydrocarbon anthracene (compounds with high and low solubilities, respectively). Two different reactor configurations are proposed: (i) an enzymatic membrane reactor for the treatment of soluble compounds, consisting of a continuous stirred tank reactor coupled to an ultrafiltration membrane to facilitate the retention and recycling of enzyme; and (ii) a two-phase enzymatic reactor for the degradation of poorly soluble compounds, consisting of an immiscible solvent, which contains the contaminant at high concentrations, and the aqueous phase containing the enzyme and cofactors involved in the catalytic cycle. In this paper, factors affecting the design and operation of both systems are discussed, and experimental results concerning the efficiency and stability of the processes are presented.     

The production of high-content fructo-oligosaccharides from sucrose by the mixed-enzyme system of fructosyltransferase and glucose oxidase

Summary A technique to produce high-content fructo-oligosaccharides by the mixed- enzyme system of fructosyltransferase and glucose oxidase was investigated. The mixed-enzyme reaction was carried out in a stirred tank reactor containing 40 %(w/v) sucrose with 10 unit of fructosyltransferase and 10 unit of glucose oxidase per gram sucrose for 25 h, at 40 °C and pH 5.5. Highly concentrated fructo-oligosaccharides up to 90 % was obtained by the mixed-enzyme system.     

Lipase-catalyzed selective synthesis of monolauroyl maltose using continuous stirred tank reactor

Monolauroyl maltose was synthesized by an immobilized lipase that catalyzed condensation of maltose and lauric acid in acetone using a batch reactor or a continuous stirred tank reactor. Mono- and di-lauroyl maltoses were identified by FT-IR, ¹H NMR, ¹³C NMR and MS. Monolauroyl maltose was selectively synthesized in a continuous stirred tank reactor and no diester was detected. The highest concentration of monolauroyl maltose at 28 mmol/l was obtained in 250 ml acetone when maltose was added at 4 g/d and the molar ratio of lauric acid to maltose was fixed at 4:1 at a flow rate of 0.15 ml/min for both influx and effluent without supplement of fresh molecular sieve.     

Biodiesel synthesis in a solvent-free system by recombinant Rhizopus oryzae: comparative study between a stirred tank and a packed-bed batch reactor

A simultaneous synthesis of biodiesel, as fatty acid methyl esters, and monoacylglycerols catalysed by the recombinant Rhizopus oryzae lipase immobilized by adsorption on Relizyme OD/403M is presented. The use of this 1(3)-positional specific lipase prevents the formation of glycerol as a by-product, thus avoiding its drawbacks. The synthesis was carried out in a solvent-free system and it has been studied in two different reactor systems: stirred tank and packed-bed reactor. Stirred tank reactor presented a high-initial reaction rate and achieved a 33.6% yield, which corresponds to a value of 50.4% of the maximum yield that can be achieved with a 1(3)-positional specific lipase. In packed-bed reactor there was a smaller initial reaction rate, but it was achieved a 49.1% yield, which corresponds to a 73.6% of the maximum yield. When a second batch is performed, the yield decreased only 4% when packed-bed reactor is employed whereas a drastic decrease is observed in a stirred tank operation. Therefore, packed-bed reactor showed a best performance and minor damage to the biocatalyst.