Mathematical modeling of diffusion and reaction in the hydrolysis of vegetable protein in an immobilized enzyme recycle reactor

Experimental investigation is by far the most effective approach for studying the behavior of physical systems. However, an enzymatic solubilization of vegetable protein is a complex combination of intrinsic problems, of which many are not easily adaptable to experimental investigation. Experimental designs to study enzyme vegetable protein reactions yield data which describe the extramembraneous activity of the immobilized enzyme. In a continuous recycle immobilized enzyme reactor, the microenvironment concentration of the substrate or product in the membrane phase, or the concentrations along the reactor axial length in the bulk phase are not discernible to the experimenter. However, the knowledge of such concentration profiles is important in weighing the significance of such factors as intermembrane diffusion, enzyme loading, wet membrane size, and the mode of operation of the reactor. The simulation of mathematical models, which describe the physical system within the constraints imposed, yields information which is vital to the understanding of the process occurring in the reactor. The kinetics and diffusion of an immobilized thermophilic Penicillium duponti enzyme at pH 3.4-3.7 and 50 degrees C was modeled mathematically. The kinetic parameters were evaluated by fitting a model to experimental data using nonlinear regression analysis. Simulation profiles of the effects of reactor geometry, substrate concentration, membrane thickness, and enzyme leading on the hydrolysis rate are presented. From the profiles generated by the mathematical model, the best operational reactor strategy is recommended.     

Preparation and characterization of epoxy-functionalized magnetic chitosan beads: laccase immobilized for degradation of reactive dyes

Cross-linked magnetic chitosan beads were prepared by phase-inversion technique in the presence of epichlorohydrin under alkaline condition, and used for covalent immobilization of laccase. The activity of the immobilized laccase on the magnetic chitosan was about 260 U (g/dry beads) with an enzyme loading of about 16.33 ± 0.39 mg [(g/dry beads) mg/g]. Kinetic parameters, V _max and K _m values were determined as 21.7 U/mg protein and 9.4 μM for free enzyme, and 15.6 U/mg protein and 19.7 μM for the immobilized laccase, respectively. The operational and thermal stabilities of the immobilized laccase were improved compared to free counterpart. The immobilized laccase was operated in a batch reactor for the decolorization of reactive dyes from aqueous solution. The laccase immobilized on magnetic chitosan beads was very effective for removal of textile dyes from aqueous solution which creates an important environmental problem in the discharged textile dying solutions.     

Production of pullulanase by free and immobilized cells of <Emphasis Type="Italic">Bacillus licheniformis</Emphasis> NRC22 in batch and continuous cultures

The production of extracellular pullulanase by Bacillus licheniformis NRC22 was investigated using different fermentation modes. In batch culture maximal enzyme activity of 18 U/ml was obtained after 24 h of growth. In continuous fermentation by the free cells, maximal reactor productivity (4.15 KU/l/h) with enzyme concentration of 14.8 U/ml and specific productivity of 334.9 U/g wet cells/h was attained at a dilution rate of 0.28/h, over a period of 25 days. B. licheniformis NRC22 cells were immobilized on Ca-alginate. The immobilization conditions with respect to matrix concentration and cell load was optimized for maximal enzyme production. In repeated batch operation, the activity of the immobilized cells was stable during the 10 cycles and the activity remained between 9.8 and 7.7 U/ml. Continuous production of pullulanase by the immobilized cells was investigated in a packed–bed reactor. Maximal reactor productivity (7.0 KU/h) with enzyme concentration of 16.8 U/ml and specific productivity of 131.64 U/g wet cells/h was attained at dilution rate of 0.42/h. The enzyme activity in the effluent started to decline gradually to the level of 8.7 U/ml after 25 days of the operation.     

Effect of particle loading on GM-CSF production by Saccharomyces cerevisiae in a three-phase fluidized bed bioreactor

Continuous production of a recombinant murine granulocyte-macrophage colony-stimulating factor (MuGM-CSF) by immobilized yeast cells, Saccharomyces cerevisiae strain XV2181 (a/a, Trp1) containing plasmid palphaADH2, in a fluidized bed bioreactor was studied at a 0.03 h(-1) dilution rate and various particle loading rates ranging from 5% to 33% (v/v). Cells were immobilized on porous glass beads fluidized in an air-lift draft tube bioreactor. A selective medium containing glucose was used to start up the reactor. After reaching a stable cell concentration, the reactor feed was switched to a rich, nonselective medium containing ethanol as the carbon source for GM-CSF production. GM-CSF production increased initially and then dropped gradually to a stable level. During the same period, the fraction of plasmid-carrying cells declined continuously to a lower level, depending on the particle loading. The relatively stable GM-CSF production, despite the large decline in the fraction of plasmid-carrying cells, was attributed to cell immobilization. As the particle loading rate increased, the plasmid stability also increased. Also, as the particle loading increased from 5% to 33%, total cell density in the bioreactor increased from 16 to 36 g/L, and reactor volumetric productivity increased from 0.36 to 1.31 mg/L.h. However, the specific productivity of plasmid-carrying cells decreased from 0.55 to 0.07 mg/L.g cell. The decreased specific productivity at higher particle loading rates was attributed to reduced growth efficiency caused by nutrient limitations at higher cell densities. Both the reactor productivity and specific cell productivity increased by two- to threefold or higher when the dilution rate was increased from 0.03 to 0.07 h(-1). (c) 1996 John Wiley & Sons, Inc.     

Methane production from wastewaters by immobilized methanogenic bacteria

A methanogenic population was immobilized onto agar gel, polyacrylamide gel, and collagen membrane. Agar-gel-entrapped methanogenic microorganisms gave the highest activity. The optimum agar concentration was between 1.5 and 3% (w/v), and the optimum microbial content was 20 mg wet cells/g gel. The optimum conditions for methane production by immobilized whole cells were pH 7.0–7.5 and 37–45°C. The rate of methane production was initially 1.8 μmol/g gel/hr. Methane productivity was gradually increased and reached a steady state (4.5μmol/g gel/hr) after 25 days of incubation. The immobilized methanogenic microbial population continuously evolved methane over a 90 day period. No difference in methane productivity was observed after three months of storage at 5°C. Methane was also produced by immobilized whole cells under aerobic conditions. Furthermore, carbohydrates, such as glucose, in wastewater completely decomposed by immobilized whole cells.     

Continuous production of L-phenylalanine by transamination

L-Phenylalanine was produced continuously from L-as-partate and phenylpyruvate by transaminase from a newly screened Pseudomonas putida strain. The process was carried out with an isolated enzyme in homogeneous phase in an enzyme membrane reactor and with immobilized whole cells in a stirred tank reactor, respectively. Due to the difference in transport resistance, the productivity of the free enzyme in homogeneous phase (72 mmol/L h) was about 3 times higher than the productivity achieved using immobilized cells. However, a better stability of the biocatalyst was observed with immobilized cells.     

A feasible enzymatic process for D-tagatose production by an immobilized thermostable L-arabinose isomerase in a packed-bed bioreactor

To develop a feasible enzymatic process for d-tagatose production, a thermostable l-arabinose isomerase, Gali152, was immobilized in alginate, and the galactose isomerization reaction conditions were optimized. The pH and temperature for the maximal galactose isomerization reaction were pH 8.0 and 65 degrees C in the immobilized enzyme system and pH 7.5 and 60 degrees C in the free enzyme system. The presence of manganese ion enhanced galactose isomerization to tagatose in both the free and immobilized enzyme systems. The immobilized enzyme was more stable than the free enzyme at the same pH and temperature. Under stable conditions of pH 8.0 and 60 degrees C, the immobilized enzyme produced 58 g/L of tagatose from 100 g/L galactose in 90 h by batch reaction, whereas the free enzyme produced 37 g/L tagatose due to its lower stability. A packed-bed bioreactor with immobilized Gali152 in alginate beads produced 50 g/L tagatose from 100 g/L galactose in 168 h, with a productivity of 13.3 (g of tagatose)/(L-reactor.h) in continuous mode. The bioreactor produced 230 g/L tagatose from 500 g/L galactose in continuous recycling mode, with a productivity of 9.6 g/(L.h) and a conversion yield of 46%.     

Immobilization of penicillin G acylase on macro-mesoporous silica spheres

In this study, macro-mesoporous silica spheres were prepared with a micro-device and used as the support for the immobilization of penicillin G acylase (PGA). To measure the enzymatic activity, the silica spheres with immobilized PGA were placed into a packed-bed reactor, in which the hydrolysis of penicillin G was carried out. The influences of the residence time, the initial concentration of the substrate, the accumulation of the target product 6-aminopenicillanic acid, and the enzyme loading amount on the performance of the immobilized PGA were investigated. The introduction of macropores increased the enzyme loading amount and decreased the internal mass transfer resistance, and the results showed that the enzyme loading amount reached 895 mg/g (dry support), and the apparent enzymatic activity achieved up to 1033 U/g (dry support). In addition, the immobilized PGA was found to have great stability.     

Immobilized Cyclodextrin Glycosyl Transferase for the Continuous Production of Cyclodextrins

Cyclodextrin glycosyl transferase (E.C: 2.4.1.19) from Bacillus, macerans and from a Bacillus sp. isolate was immobilized by two methods, viz. to epoxy-activated Sepharose and to alkylamine silica treated with glutaraldehyde. Because of the ready availability, low cost ($0.01/g), good surface area (30 M²/g) and ease of operation of a continuous cylindrical reactor, the high silica fabric was chosen. The immobilized enzyme had a pH optimum shifted to the alkaline side (from 6.5 to 7.5) and had a reduced temperature optimum (from 60°C to 50-55°C). Reuse efficiency showed 65% reduction in the overall activity of the immobilized enzyme after 10 cycles of 48 h each. Continuous operation at 55°C of a cylindrical reactor of 141 ml capacity, using the immobilized enzyme (80 g of high - silica fabric containing 114 mg of purified enzyme) gave a maximum productivity of 10.2 g of cyclodextrins L^-1 h,^-1, at a dilution rate of 0.32 h^-1 and a substrate concentration of 20 g L^-1. The half life of the biocatalyst was found to be 22 days, which could be further improved by using a lower operating temperature. Over the useful life time of the immobilized biocatalyst (22 days), the total Cyclodextrin produced was of the order of 88 Kg.     

High production of D-tagatose, a potential sugar substitute, using immobilized L-arabinose isomerase

An L-arabinose isomerase of Escherichia coli was immobilized using covalent binding to agarose to produce D-tagatose, a bulking sweetener that can be economically used as a sugar substitute. The immobilized L-arabinose isomerase stably produced an average of 7.5 g-tagatose/L.day for 7 days with a productivity exceeding that of the free enzyme (0.47 vs 0.30 mg/U.day). Using a scaled-up immobilized enzyme system, 99.9 g-tagatose/L was produced from galactose with 20% equilibrium in 48 h. The process was repeated two more times with production of 104.1 and 103.5 g-tagatose/L. D-Tagatose production using an immobilized L-arabinose isomerase has a high potential for commercial application.     

Immobilization and stabilization of d-hydantoinase from Vigna angularis and its use in the production of N-carbamoyl-d-phenylglycine. Improvement of the reaction yield by allowing chemical racemization of the substrate

This work reports the immobilization of a multimeric d-hydantoinase (DHTase) from Vigna angularis (E.C. 3.5.2.2.) on agarose beads activated with glyoxyl groups aiming to improve its stability via multipoint covalent attachment. The final reduction with sodium borohydride resulted in a drop in enzyme activity that could be decreased by adding Zn²⁺ or Mg²⁺. The optimal preparation with high activity (58 % recovered activity) and stability (around 86-fold more stable than the free enzyme) was obtained by DHTase immobilization on glyoxyl agarose for 24 h at 25 °C and pH 10.05, and a borohydride reduction step in the presence of 10 mM Zn²⁺ (DHTase-Glx). The enzyme was almost fully immobilized on glyoxyl agarose (19.8 mg/g of support) when offering 20 mg/g. This immobilized biocatalyst was used to catalyze the hydrolysis of d,l-phenylhydantoin under substrate racemization conditions, which produced 99 % of N-carbamoyl-d-phenylglycine after 9 h reaction.     

Enzymatic synthesis of esters using an immobilized lipase

Various esters were synthesized in nearly anhydrous hexane from alcohols and carboxylic acids using a lipase from Candida cylindracea. The enzyme was immobilized on a nylon support and protein loadings as high as 10 mg/g were obtained. The activity of the immobilized enzyme was maximum in a range of temperatures from 25 to 37 degrees C. Ethylpropionate was formed from ethanol and propionic acid at a rate of 0.017 mol/h g immobilized protein. Different esters were formed at comparable rates and equilibrium conversions could generally be approached in less than 10 h in a batch reaction system. The immobilized lipase catalyst was quite stable and retained about one third of the initial activity after repeated experiments during the course of 72 days. A stirred tank continuous flow reactor was used successfully for the continuous production of esters.     

Tagatose production by immobilized recombinant Escherichia coli cells containing Geobacillus stearothermophilus l-arabinose isomerase mutant in a packed-bed bioreactor

Using immobilized recombinant Escherichia coli cells containing Geobacillus stearothermophilus l-arabinose isomerase mutant (Gali 152), we found that the galactose isomerization reaction was maximal at 70 degrees C and pH 7.0. Manganese ion enhanced galactose isomerization to tagatose. The immobilized cells were most stable at 60 degrees C and pH 7.0. The cell and substrate concentrations and dilution rate were optimal at 34 g/L, 300 g/L, and 0.05 h(-1), respectively. Under the optimum conditions, the immobilized cell reactor with Mn2+ produced an average of 59 g/L tagatose with a productivity of 2.9 g/L.h and a conversion yield of 19.5% for the first 20 days. The operational stability of immobilized cells with Mn2+ was demonstrated, and their half-life for tagatose production was 34 days. Tagatose production was compared for free and immobilized enzymes and free and immobilized cells using the same mass of cells. Immobilized cells produced the highest tagatose concentration, indicating that cell immobilization was more efficient for tagatose production than enzyme immobilization.     

Mechanism for reversible inactivation of immobilized β-galactosidase from Bacillus circulans during continuous production of galacto-oligosaccharides

Summary The specific activity-dependent stability of the immobilized -galactosidase-2 (-d-galactoside galactohydrolase, EC 3.2.1.23) from Bacillus circulans during the continuous production of galactooligosaccharides from lactose was studied. This was done by measuring the elution pattern of saccharides from the various immobilized Merckogel (controlled pore silica gel) columns and the amount of saccharides remaining in the gel. It was suggested that oligosaccharides produced were trapped inside the three dimensional enzyme aggregate with the immobilized enzyme having a specific activity of 240 units/g of wet gel, causing gradual inactivation, while the immobilized enzyme with 15 units/g of wet gel was stable since the oligosaccharides were not accumulated.Free -galactosidase-2 was stable during continuous reaction in a membrane reactor.     

Kinetic evaluation of biotransformation of benzaldehyde to L-phenylacetylcarbinol by immobilized pyruvate decarboxylase from Candida utilis

Biotransformation of benzaldehyde to L-phenylacetylcarbinol (L-PAC) as a key intermediate for L-ephedrine has been evaluated using immobilized pyruvate decarboxylase (PDC) from Candida utilis. PDC immobilized in spherical polyacrylamide beads was found to have a longer half-life compared with free enzyme. In a batch process, the immobilized PDC generally produced lower L-PAC than free enzyme at the same concentrations of substrates due to increased by-products acetaldehyde and acetoin and reduced benzaldehyde uptake. With immobilized PDC, L-PAC formation occurred at higher benzaldehyde concentrations (up to 300 mM) with the highest L-PAC concentration being 181 mM (27.1 g/L). For a continuous process, when 50 mM benzaldehyde and 100 mM sodium pyruvate were fed into a packed-bed reactor at 4 degrees C and pH 6.5, a productivity of 3.7 mM/h (0.56 g/L . h) L-PAC was obtained at an average concentration of 30 mM (4.5 g/L). The half-life of immobilized PDC reactor was 32 days. (c) 1996 John Wiley & Sons, Inc.     

Ethanol fermentation in a magnetically fluidized bed reactor with immobilized Saccharomyces cerevisiae in magnetic particles

Ethanol fermentation by immobilized Saccharomyces cerevisiae cells in magnetic particles was successfully carried out in a magnetically stabilized fluidized bed reactor (MSFBR). These immobilized magnetic particles solidified in a 2 % CaCl(2) solution were stable and had high ethanol fermentation activity. The performance of ethanol fermentation of glucose in the MSFBR was affected by initial particle loading rate, feed sugar concentration and dilution rate. The ethanol theoretical yield, productivity and concentration reached 95.3%, 26.7 g/L h and 66 g/L, respectively, at a particle loading rate of 41% and a feed dilution rate of 0.4 h(-1) with a glucose concentration of 150 g/L when the magnetic field intensity was kept in the range of 85-120 Oe. In order to use this developed MSFBR system for ethanol production from cheap raw materials, cane molasses was used as the main fermentation substrate for continuous ethanol fermentation with the immobilized S. cerevisiae cells in the reactor system. Molasses gave comparative ethanol productivity in comparison with glucose in the MSFBR, and the higher ethanol production was observed in the MSFBR than in a fluidized bed reactor (FBR) without a magnetic field.     

Continuous ethanol production from pineapple cannery waste using immobilized yeast cells

The cells of Saccharomyces cerevisiae ATCC 24553, were immobilized in k-carrageenan and packed in a tapered glass column reactor for ethanol production from pineapple cannery waste at temperature 30 degrees C and pH 4.5. The maximum productivity was 42.8 g ethanol 1(-1) h(-1) at a dilution rate of 1.5 h(-1). The volumetric ethanol productivity of the immobilized cells was ca. 11.5 times higher than the free cells. The immobilized cell reactor was operated over a period of 87 days at a dilution rate of 1.0 h(-1), without any loss in the immobilized cell activity. The maximum specific ethanol productivity and specific sugar uptake rate of the immobilized cells were 1.2 g ethanol g(-1) dry wt. cell h(-1) and 2.6 g sugar g(-1) dry wt. cell h(-1), respectively, at a dilution rate of 1.5 h(-1).     

Immobilization of Kluyveromyces marxianus cells containing inulinase activity in open pore gelatin matrix: 2. Application for high fructose syrup production

Batch and continuous production of high fructose syrup from Jerusalem artichoke tubers has been studied using yeast cells immobilized in open pore gelatin matrix. In a batch reactor, the hydrolysis was 93% ($\text{d}\text{-fructose/}\text{d}\text{-glucose}\text{= 90/10}$) and 42 mg d-fructose per ml was produced from the artichoke tuber extract by immobilized cells in 3 h. The same immobilized cells were recycled and used repeatedly for 10 batch cycles starting with fresh juice at the beginning of each cycle. It was found that immobilized cells were extremely stable and the percent hydrolysis was almost constant for all 10 batch cycles. In a continuous reactor using an immobilized cell concentration of 65.7 g (dry wt) l^?1 of total working bioreactor volume, the percent hydrolysis was found to remain constant at ～100% at dilution rates <1.26 h^?1, but beyond that it decreased. Volumetric productivity attained its maximum value at D = 2.08 h^?1 and was found to be 100 g l^?1 h^?1. This was achieved at a feed sugar conversion of 80%. At 90% conversion and D = 1.66 h^?1, the productivity was found to be 90 g l^?1 h^?1. Continuous operation of the immobilized cell bioreactor at a constant dilution rate of 1.65 h^?1 for 240 h resulted in only 2% loss of original activity.     

L-DOPA production from tyrosinase immobilized on nylon 6,6

The production of L-DOPA immobilized on chemically modified nylon 6,6 membranes was studied in a batch reactor. Tyrosinase was immobilized on nylon using glutaraldehyde as a crosslinking agent. The effects of membrane pore size and glutaraldehyde concentration upon enzyme uptake and L-DOPA production were investigated. Enzyme uptake was unaffected by glutaraldehyde concentration; approximately 70% uptake was observed when 25% w/v (group 1), 5% (group 2), and 3% (group 3) glutaraldehyde were used, indicating that glutaraldehyde was in excess. Similarly, uptake was the same for membranes with 0.20 and 10 mum pore sizes.Membranes produced using different levels of glutaraldehyde exhibited dramatically different capacities for L-DOPA production, despite the fact that enzyme uptake was equivalent. Membranes from groups 2 and 3 (5% and 3% glutaraldehyde) produced L-DOPA at a rate of 1.70 mg L(-1) h(-1) over 170 h in a 500-mL batch reactor. However, no free L-DOPA was detected when group 1 membranes were used. Experimental evidence suggests that L-DOPA was produced, but remained bound to these membranes via excess glutaraldehyde left over from the immobilization process. Membrane pore size also effected L-DOPA production; less production was observed when 10-mum membranes were used, despite equivalent enzyme uptake. The observed difference in production may be due to differences in the pore density on the two types of membranes which could affect the access of the substrate to the immobilized enzyme.The results of these studies indicate that tyrosinase can be effectively immobilized on nylon 6,6. L-DOPA production was optimal when 0.20-mum-pore-size membranes were activated with 3-5% glutaraldehyde. Stability studies indicated a 20% reduction in activity over 14 days when the immobilized enzyme was used under turnover conditions. (c) 1996 John Wiley & Sons, Inc.     

Continuous D-tagatose production by immobilized thermostable L-arabinose isomerase in a packed-bed bioreactor

D-Tagatose was continuously produced using thermostable L-arabinose isomerase immobilized in alginate with D-galactose solution in a packed-bed bioreactor. Bead size, L/D (length/diameter) of reactor, dilution rate, total loaded enzyme amount, and substrate concentration were found to be optimal at 0.8 mm, 520/7 mm, 0.375 h(-1), 5.65 units, and 300 g/L, respectively. Under these conditions, the bioreactor produced about 145 g/L tagatose with an average productivity of 54 g tagatose/L x h and an average conversion yield of 48% (w/w). Operational stability of the immobilized enzyme was demonstrated, with a tagatose production half-life of 24 days.