Lipase-catalyzed kinetic resolution of (R,S)-1-phenylethyl propionate in an enzyme membrane reactor

Enzymatic stereoselective hydrolysis of (R,S)-1-phenylethyl propionate was performed in a stirred tank and in a biphasic enzyme membrane reactor. Lipase from Pseudomonas sp. was proved to be a good enantioselective catalyst for this reaction. The enzyme was covalently immobilized in a porous polyamide membrane (flat sheet as well as hollow-fibres) via glutaraldehyde. An influence of membrane hydrophobicity on reactor performance was observed. Initial lipase activity and productivity in the processes were equal to 1.05 × 10^?4, 1.3 × 10^?5 and 1.0 × 10^?5 mole/(h × mg of enzyme) in the case of native lipase, in the aromatic polyamide hydrophobic membrane reactor and in the hydrophilic polyamide-6 membrane reactor, respectively. The influence of some factors such as temperature, pH, buffer concentration, initial substrate concentration and addition of β-cyclodextrin derivatives on reaction rate and enantioselectivity was investigated and discussed. In the enzyme membrane reactor both organic and aqueous phases circulated countercurrently on both sides of the membrane. At a conversion degree of under 55–60%, pure enantiomer of the remaining ester (i.e. > 98%) was obtained.     

Synthesis of esters using a nylon-immobilized lipase in batch and continuous reactors.

Direct esterifications using a nylon-immobilized lipase from Candida cylindracea were carried out in batch and continuous-flow reactors. The immobilized enzyme was effective in catalyzing the synthesis of ethylpropionate, isoamylpropionate, and isoamylbutyrate. With ethanol dissolved in hexane as a substrate, the maximum initial esterification rate was 0.02 mole/(h x g of immobilized protein), but the enzyme was stable only when the substrate concentrations were lower than 0.2 M. With isoamyl alcohol in hexane as a substrate, esterification rates as high as 0.085 mole/(h x g of immobilized protein) were observed and the immobilized enzyme was stable over a much broader concentration range. However, in this case, the use of a solvent, such as hexane, was not necessary for esterification, and the enzyme could be employed in equimolar acid/alcohol mixtures. A packed-bed reactor was operated successfully for the continuous synthesis of esters. The reactor was stable for long periods of time, and the steady-state performance could be accurately predicted on the basis of batch reaction experiments.     

Kinetics of Growth and Substrate Uptake in a Biological Film System

The rates of growth and substrate uptake in a biological film continuous-flow reactor were studied. The experiments were performed with high fluid velocities to bring the reactor operation to the reaction-controlled regime, thus avoiding external diffusional resistances. The glucose uptake experiments were performed with small film thicknesses so that full substrate penetration within the entire film thickness could be obtained. In this way, the catalyst effectiveness factor was 1.0 and the observed rate was the true, or intrinsic, rate. The results of the experiments indicate that both the intrinsic rate of substrate uptake and the rate of film growth are independent of the substrate concentration remaining in the reactor (zero-order reactions). However, the value of the initial substrate concentration when the film is in the early stages of growth defines the magnitude of both the rate of uptake and growth. This effect of the initial substrate concentration follows a saturation-function pattern.     

Changes of lipase-catalyzed lipolytic rates in a batch reactor

A dramatic change of the reaction rate was observed for the lipase-catalyzed hyrolysis of tributyrin in a batch reactor. Immediately after the addition of the enzyme, the lipolysis rate increased continuously until a maximal reaction rate was reached. The duration of the induction was mainly controlled by the bulk enzyme concentration and the reactor stirring speed. The reaction rate dropped sharply after reaching its maximal value. The lipolysis decayed at a rate of about 0.012 min(-1), and was not affected by changes of the stirring speed. This decay was attributed to the fast deactivation of the surface-adsorbed lipase, and possibly to the extremely slow desorption of the inactivated species. For reaction time longer than 120 minutes, the lipolysis decreased at a much slower rate. Several mechanisms for the decay of the lipolysis rate were discussed.     

Entrapment of lipase into K-carrageenan beads and its use in hydrolysis of olive oil in biphasic system

The porcine pancrease lipase was immobilized by entrapment in the beads of K-carrageenan and cured by treatment with polyethyleneimine (PEI) in the phosphate buffer. The retention of hydrolytic activity of lipase and compressive strength of the beads were examined. The activity of free and immobilized lipase was assessed by using olive oil as the substrate. The immobilized enzyme exhibited a little shift towards acidic pH for its optimal activity and retained 50% of its activity after 5 cycles. When the enzyme concentration was kept constant and substrate concentration was varied the K_m and V_max were observed to be 0.18 × 10⁻² and 0.10, and 0.10 × 10⁻² and 0.09 respectively, for free and for entrapped enzymes. When the substrate concentration was kept constant and enzyme concentration was varied, the values of K_m and V_max were observed to be 0.19 × 10⁻⁷ and 0.41, and 0.18 × 10⁻⁷ and 0.41 for free and entrapped enzymes. Though this indicates that there is no conformational change during immobilization, it also shows that the reaction velocity depends on the concentration. Immobilized enzyme showed improved thermal and storage stability. Hydrolysis of olive oil in organic–aqueous two-phase system using fixed bed reactor was carried out and conditions were optimized. The enzyme in reactor retained 30% of its initial activity after 480 min (12 cycles).     

Performance of a β-d-galactosidase hollow fibre reactor

β-d-Galactosidase was immobilized in a hollow fibre ultrafiltration module. The hydrolysis of 2-nitrophenyl β-d-galactopyranoside (ONPG) was significantly affected by enzyme loading, flow rate and substrate concentration. Pretreatment of hollow fibres with a protein was necessary to minimize enzyme inactivation. Residence time distribution studies indicated that the product of the reaction (ONP) was significantly adsorbed by the fibres, which resulted in the reactor taking 10–30 h to achieve steady-state. An equation based on Michaelis-Menten kinetics and a plug-flow model adequately described the performance of the reactor with regard to operating variables, even though some diffusion effects were observed.     

Production of galacto-oligosaccharides by immobilized recombinant beta-galactosidase from Aspergillus candidus

The preparation of galacto-oligosaccharides (GOSs) was studied using the immobilized recombinant beta-galactosidase from Aspergillus candidus CGMCC3.2919. The optimal pH and temperature for the immobilized enzyme were observed at pH 6.5 and 40 degrees C, respectively. Increasing the initial lactose concentration increased the yield of GOSs. The dilution rate was found to be a key factor during the continuous production of GOSs. The maximum productivity, 87 g/L.h was reached when 400 g/L lactose was fed at dilution rate of 0.8/h. The maximum GOS yield reached 37% at dilution rate of 0.5/h. Continuous operation was maintained for 20 days in a packed-bed reactor without apparent decrease in GOS production. The average yield of GOSs was 32%, corresponding to the average productivity of 64 g/L.h, which implied that the immobilized recombinant beta-galactosidase has potential application for GOS production.     

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.     

Production of galacto-oligosaccharides from lactose by Aspergillus oryzae beta-galactosidase immobilized on cotton cloth.

The production of galacto-oligosaccharides (GOS) from lactose by A. oryzae beta-galactosidase immobilized on cotton cloth was studied. The total amounts and types of GOS produced were mainly affected by the initial lactose concentration in the reaction media. In general, more and larger GOS can be produced with higher initial lactose concentrations. A maximum GOS production of 27% (w/w) of initial lactose was achieved at 50% lactose conversion with 500 g/L of initial lactose concentration. Tri-saccharides were the major types of GOS formed, accounting for more than 70% of the total GOS produced in the reactions. Temperature and pH affected the reaction rate, but did not result in any changes in GOS formation. The presence of galactose and glucose at the concentrations encountered near maximum GOS greatly inhibited the reactions and reduced GOS yield by as much as 15%. The cotton cloth as the support matrix for enzyme immobilization did not affect the GOS formation characteristics of the enzyme, suggesting no diffusion limitation in the enzyme carrier. The thermal stability of the enzyme increased approximately 25-fold upon immobilization on cotton cloth. The half-life for the immobilized enzyme on cotton cloth was more than 1 year at 40 degrees C and 48 days at 50 degrees C. Stable, continuous operation in a plugflow reactor was demonstrated for 2 weeks without any apparent problem. A maximum GOS production of 21 and 26% (w/w) of total sugars was attained with a feed solution containing 200 and 400 g/L of lactose, respectively, at pH 4.5 and 40 degrees C. The corresponding reactor productivities were 80 and 106 g/L/h, respectively, which are at least several-fold higher than those previously reported.     

An ultrafiltration membrane bioreactor for the lipolysis of olive oil in reversed micellar media

The enzymatic hydrolysis of olive oil using Chromobacterium viscosum lipase B encapsulated in reversed micelles of dioctyl sodium sulfosuccinate (AOT) in isooctane was investigated in an ultrafiltration ceramic membrane reactor of tubular type, operating in a batch mode. Water concentration was found to be a critical parameter in the enzyme kinetics and hydrolysis yield of the reaction. The size of micelles, recirculation rate, and substrate concentration were found to be the major factors affecting the separation process. A correlation that enables the prediction of final conversion degrees in this bioreactor from the initial reaction conditions was established. (c) 1993 Wiley & Sons, Inc.     

Membrane reactor for enzymatic hydrolysis of cellobiose

A pressurized, stirred vessel attached with an ultrafiltration membrane was used as a membrane reactor, Cellobiose hydrolysis by cellobiase was carried out and theoretically analyzed in terms of steady-state conversion and flow rate through the membrane. When the flow rate exceeds a critical value, a significant fraction of the enzyme inside the reactor is localized in the concentration polarization layer where shear from stirring is high. Consequently, enzyme deactivation inside the concentration polarization layer is accelerated and the conversion decreases due to an exchange of active enzyme in bulk with deactivated enzyme in the polarization layer via convection and back diffusion. Successful operation can be obtained at flow rates lower than the critical point to avoid the polarization and thus the deactivation. It is shown that 6.5 L of 2 mg/mL of cellobiose solution is hydrolyzed to glucose with a conversion of 91% in 20 h with 1.617 mg of cellobiase enzyme, in a reactor attached with a PM 10 membrane of an effective surface area of 39.2 cm².     

β-Galactosidase from Talaromyces thermophilus immobilized on to Eupergit C for production of galacto-oligosaccharides during lactose hydrolysis in batch and packed-bed reactor

The β-galactosidase from Talaromyces thermophilus CBS 236.58 immobilized onto Eupergit C produced galacto-oligosaccharides (GalOS) in batchwise and continuous packed-bed mode of operation. A maximum yield of GalOS of 12, 39 and 80 g l⁻¹ was obtained for initial lactose concentrations of 50, 100 and 200 g l⁻¹, respectively, for batch conversion experiments. The immobilized enzyme could be re-used for several cycles for lactose hydrolysis and transformation. The maximum GalOS concentration of approximately 50 g l⁻¹ was obtained with the dilution rate of 0.375 h⁻¹ in a packed-bed reactor, when using an initial lactose concentration of 200 g l⁻¹. Continuous conversion of lactose in the packed-bed reactor resulted in the formation of relatively more trisaccharides than when employing the immobilized enzyme in discontinuous mode of operation.     

Optimal design for CSTR's in series performing enzymatic lactose hydrolysis

Analytical expressions are derived for the optimal design (based on minimum overall reactors volume) of a series of N CSTR's performing enzymatic lactose hydrolysis. It is assumed that lactose hydrolysis obeys Michaelis-Menten kinetics with competitive product (galactose) inhibition and no enzyme deactivation occurs. The optimum design of a cascade of ideally mixed reactors are compared with equal size reactors and with plug flow reactor required for a given overall degree of lactose conversion. The effect of operating parameters such as temperature, lactose initial (feed) concentration and conversion, enzyme and product initial concentration on the optimal overall holding time are also investigated. Optimization results for a series of N CSTR's up to five are obtained and compared with plug flow reactor.     

The Influence of Fatty Acid and Glycerol on the Kinetics of Fat Hydrolysis by Candida Rugosa Lipase in a Membrane Reactor

The kinetics of lipid-hydrolysis by Candida rugosa lipase was investigated in a membrane reactor and in an emulsion system. Two models were chosen to describe the kinetics of the enzyme:

(1) The hydrolysis of triglycerides to fatty acids was considered to be a chain reaction with the intermediary products di- and mono-glyceride; each step was assumed to be a reversible second-order reaction. The reaction rate constants were determined from batch experiments. The experimental results could be described with this model.

(2) For process optimization and control, a model based on the power law was developed. For this model, the rate of hydrolysis was measured as a function of fatty acid and glycerol concentrations. Relations for the initial rate and equilibrium ester fraction as a function of the glycerol concentration were determined. Further, the reaction rate could be described with the power-law model with a power of 1.75 in the hydrolyzable ester fraction for a wide range of glycerol concentrations. The model with power 1.75 gave much better results when compared to a similar first order model. Although simpler, the first order model can not be used. The power law model was applied in the simulation of a reactor composed of three modules. The fatty acid production rate was calculated for this reactor system as a function of the outgoing glycerol concentration at different conditions.     

Enzymatic production of biodiesel from cotton seed oil using t-butanol as a solvent

The enzymatic production of biodiesel by methanolysis of cottonseed oil was studied using immobilized Candida antarctica lipase as catalyst in t-butanol solvent. Methyl ester production and triacylglycerol disappearance were followed by HPLC chromatography. It was found, using a batch system, that enzyme inhibition caused by undissolved methanol was eliminated by adding t-butanol to the reaction medium, which also gave a noticeable increase of reaction rate and ester yield. The effect of t-butanol, methanol concentration and temperature on this system was determined. A methanolysis yield of 97% was observed after 24h at 50 degrees C with a reaction mixture containing 32.5% t-butanol, 13.5% methanol, 54% oil and 0.017 g enzyme (g oil)(-1). With the same mixture, a 95% ester yield was obtained using a one step fixed bed continuous reactor with a flow rate of 9.6 mlh(-1) (g enzyme)(-1). Experiments with the continuous reactor over 500 h did not show any appreciable decrease in ester yields.     

固定化酶-离子交换组合系统进行青霉素G水解生产6-APA的模型化研究

采用固定化青霉素酰化酶(Penicillin acylase)在反应器中进行青霉素G水解生产6－APA,同时与离子交换柱相组合以连续地去除反应混合液中的苯乙酸。建立了离子变换柱的分格模型(Comparunent model)．在确定了青霉素G和苯乙酸沿柱高的浓度分布的基础上,与描述固定化酶反应器的状态方程相结合,得到了固定化酶－离子交换组合系统的数学模型。在将计算机模拟值与实验值进行验证后,探讨了组合系统中树脂量、循环流速和组合起始时间对青霉素G酶解过程的影响。     

Ceramic membrane microfilter as an immobilized enzyme reactor.

This study investigated the use of a ceramic microfilter as an immobilized enzyme reactor. In this type of reactor, the substrate solution permeates the ceramic membrane and reacts with an enzyme that has been immobilized within its porous interior. The objective of this study was to examine the effect of permeation rate on the observed kinetic parameters for the immobilized enzyme in order to assess possible mass transfer influences or shear effects. Kinetic parameters were found to be independent of flow rate for immobilized penicillinase and lactate dehydrogenase. Therefore, neither mass transfer nor shear effects were observed for enzymes immobilized within the ceramic membrane. Both the residence time and the conversion in the microfilter reactor could be controlled simply by regulating the transmembrane pressure drop. This study suggests that a ceramic microfilter reactor can be a desirable alternative to a packed bed of porous particles, especially when an immobilized enzyme has high activity and a low Michaelis constant.     

Transient response of encapsulated enzymes in hollow-fiber reactor

A mathematical model for the transient response of encapsulated enzymes is developed showing the effects of the outer boundary layer, the encapsulating membrane, the partition coefficient, and diffusion with reaction within the encapsulating medium. The model incorporates both first-order kinetics and Michaelis-Menten kinetics for the reaction rate. Using typical hollow-fiber or microcapsule parameters, the model shows that (a) the partition coefficient affects the overall rate only when the rate-limiting step is diffusion through the membrane, (b) the transient overall effectiveness factor rises sharply with time and approaches an asymptotic value for most situations, and (c) the first-order approximation to Michaelis-Menten kinetics is not valid when the initial outside bulk concentration is higher than the Michaelis constant and the overall rate is reaction limited. The model is compared with experimental data using uricase in a hollow-fiber enzyme reactor configuration. Batch assay and CSTUER (continuous-stirred ultrafiltration enzyme reactor) studies were conducted on the free enzyme to provide some of the parameters used in the model. The CSTUER data fit the case of substrate inhibition kinetics with the apparent Michaelis constant approaching zero. The hollow-fiber reactor was conducted with uricase dissolved in both a buffer solution and a concentrated hemoglobin solution. Diffusivities of the solute were measured in both solutions as was the osmotic pressure of the hemoglobin solution. While experimental data for uricase in buffer solution could easily be matched by the model, that in the concentrated hemoglobin solution could not.     

Steady-state generation of hydrogen peroxide: kinetics and stability of alcohol oxidase immobilized on nanoporous alumina

Alcohol oxidase from Pichia pastoris was immobilized on nanoporous aluminium oxide membranes by silanization and activation by carbonyldiimidazole to create a flow-through enzyme reactor. Kinetic analysis of the hydrogen peroxide generation was carried out for a number of alcohols using a subsequent reaction with horseradish peroxidase and ABTS. The activity data for the immobilized enzyme showed a general similarity with literature data in solution, and the reactor could generate 80 mmol H₂O₂/h per litre reactor volume. Horseradish peroxidase was immobilized by the same technique to construct bienzymatic modular reactors. These were used in both single pass mode and circulating mode. Pulsed injections of methanol resulted in a linear relation between response and concentration, allowing quantitative concentration measurement. The immobilized alcohol oxidase retained 58 % of initial activity after 3 weeks of storage and repeated use.     

Reaction conditions for laccase catalyzed polymerization of catechol

Poly(catechol) was synthesized in batch runs with laccase from Trametes versicolor (ATCC 200801). The polymerization reaction was conducted in a closed, temperature controlled system containing acetone and sodium acetate buffer for pH control. The effects of the solvent mixture, monomer (catechol), enzyme, medium pH and temperature on the polymerization rate were investigated with respect to initial reaction conditions and depletion rate of dissolved oxygen in the medium. Maximum initial reaction rate was attained with 10% (v/v) acetone-sodium acetate buffer at pH 5.0, 25 degrees C, 0.02 U/ml enzyme and 250 mg/l initial catechol and 10 mg/l dissolved oxygen. A general saturation enzyme kinetics response was observed for catechol substrate. Temperature rise supported the rate increase up to 45 degrees C, after which the rate tended to be stable due to a drop in dissolved oxygen concentration as well as enzyme instability.