Galactose oxidase. An enzyme with lectin properties.

Galactose oxidase interacts with immobilized D-galactosyl residues and related immobilized and free sugars under the conditions of affinity electrophoresis in polyacrylamide gel and agglutinates sialidase-treated human erythrocytes. The agglutination is also inhibited by D-galactose and its derivatives and is temperature dependent. The sugar binding and hemagglutinating activity are preserved after removal of Cu2+ essential for enzymic activity. These properties are very similar to those of some typical lectins; however, a number of D-galactose specific lectins do not possess any detectable galactose oxidase activity.     

Gallotannin hydrolysis by immobilized fungal mycelia in a packed bed bioreactor.

Hydrolysis of gallotannin to gallic acid by immobilized mycelia of Aspergillus niger MTCC 282, Aspergillus fischerii MTCC 150, Fusarium solani MTCC 350 and Trichoderma viride MTCC 167 in a packed bed bioreactor was studied. Fungal mycelia preinduced with 5 g L-1 gallotannin were immobilized in calcium alginate gel (1.5%) and the resultant beads were packed in a column to a bed volume of 175 mm3. Gallotannin dissolved in distilled water was passed through the column and the eluate was recycled after adjusting pH to 6 with ammonium hydroxide (10%). Maximum hydrolysis of gallotannin was recorded by immobilized mycelia of F. solani and T. viride at 35 degrees and 45 degrees C after 175 and 60 min of residency period respectively. Optimum substrate concentration required for maximum hydrolysis was 10 g L-1 at pH 5 for both the fungi. Immobilized mycelia of A. niger and A. fischerii revealed maximum operational stability. Loss of activity after eighth run was in the order of-A. niger (no loss), A. fischerii (7.5%), F. solani (18%) and T. viride (18%). Stability in terms of retention of enzyme activity after 150 days of storage at 4 degrees C was A. niger (58%), A. fischerii (26.8%), F. solani (83%) and T. viride (85.1%).     

Monomeric sarcosine oxidase: structure of a covalently flavinylated amine oxidizing enzyme.

BACKGROUND: Monomeric sarcosine oxidases (MSOXs) are among the simplest members of a recently recognized family of eukaryotic and prokaryotic enzymes that catalyze similar oxidative reactions with various secondary or tertiary amino acids and contain covalently bound flavins. Other members of this family include heterotetrameric sarcosine oxidase, N-methyltryptophan oxidase and pipecolate oxidase. Mammalian sarcosine dehydrogenase and dimethylglycine dehydrogenase may be more distantly related family members. RESULTS: The X-ray crystal structure of MSOX from Bacillus sp. B-0618, expressed in Escherichia coli, has been solved at 2.0 A resolution by multiwavelength anomalous dispersion (MAD) from crystals of the selenomethionine-substituted enzyme. Fourteen selenium sites, belonging to two MSOX molecules in the asymmetric unit, were used for MAD phasing and to define the local twofold symmetry axis for electron-density averaging. The structures of the native enzyme and of two enzyme-inhibitor complexes were also determined. CONCLUSIONS: MSOX is a two-domain protein with an overall topology most similar to that of D-amino acid oxidase, with which it shares 14% sequence identity. The flavin ring is located in a very basic environment, making contact with sidechains of arginine, lysine, histidine and the N-terminal end of a helix dipole. The flavin is covalently attached through an 8alpha-S-cysteinyl linkage to Cys315 of the catalytic domain. Covalent attachment is probably self-catalyzed through interactions with the positive sidechains and the helix dipole. Substrate binding is probably stabilized by hydrogen bonds between the substrate carboxylate and two basic sidechains, Arg52 and Lys348, located above the re face of the flavin ring.     

Optimal temperature policy for immobilized enzyme packed bed reactor performing reversible Michaelis-Menten kinetics using the disjoint policy.

The optimal temperature policy that maximizes the time-averaged productivity of a continuous immobilized enzyme packed bed reactor is determined. This optimization study takes into consideration the enzyme thermal deactivation with substrate protection during the reactor operation. The general case of reversible Michaelis-Menten kinetics under constant reactor feed flow rate is assumed. The corresponding nonlinear optimization problem is solved using the calculus of variations by applying the disjoint policy. This policy reduces the optimization problem into a differential-algebraic system, DAE. This DAE system defines completely the optimal temperature-time profiles. These profiles depend on the kinetic parameters, feed substrate concentration, operating period, and the residence time and are characterized by increasing form with time. Also, general analytical expressions for the slopes of the temperature and residual enzyme activity profiles are derived. An efficient solution algorithm is developed to solve the DAE system, which results into a one-dimensional optimization problem with simple bounds on the initial feed temperature. The enzymatic isomerization of glucose into fructose is selected as a case study. The computed productivities are very close to that obtained by numerical nonlinear optimization with simpler problem to solve. Moreover, the computed conversion profiles are almost constant over 90% of the operating periods, thus producing a homogeneous product.     

Optimization of a packed bed bioreactor with immobilized cells using experimental design

A central composite design was employed for the optimization of heterogeneous enzymatic hydrolysis of sucrose. The reaction was catalyzed by whole yeast cells of Saccharomyces cerevisiae immobilized in Ca-pectate gel. Bioreactor volumetric productivity was chosen as an optimization criterion, while temperature and gel biomass concentration were optimization parameters. Sucrose inlet concentration of 700 kg m^–3 and outlet conversion of 65% were constant in all experiments. In the temperature range 51–73 °C and biomass concentration range 11–39 kg m^–3 (dry mass of cells), the dependence of bioreactor productivity on the two factors was described by a second order polynom regression equation. No simple optimum was revealed by the experimental design. The bioreactor productivity increased within the whole experimental range of biomass concentration, whereas a temperature optimum was found to be between 60 and 65 °C.List of Symbols b _j jth regression coefficient - c _Si kg m^–3 inlet sucrose concentration - F m³ min^–1 flow rate - F F distribution - f _LF degrees of freedom of lack of fit variance - f _P degrees of freedom of pure error variance - N total number of runs - n ₀ number of runs in the centre of design - P kg m^–3 min^–1 productivity - s _LF ² lack of fit variance - SS _LF lack of fit sum of squares - S _p ² pure error variance - SS _P pure error sum of squares - SS _R total residual sum of squares - V _b m³ bioreactor bed volume - X _O outlet conversion - x ₁ 1st factor - coded temperature - x ₂ 2nd factor - coded biomass concentration - y kgm^–3min^–1 measured response (productivity) - kg m^–3 min^–1 estimated response (productivity) - y _Oi kg m^–3 min^–1 measured response in the centre of design - ¯y ₀ kg m^–3 min^–1 average of response in the centre of design     

Performance of rotating packed disk reactor with immobilized glucose oxidase

Summary Reactor performance was studied to investigate whether a rotating packed disk reactor (RPDR) can be used for the enzymatic oxidation of biochemicals. The disks were packed with calcium alginate beads with immobilized glucose oxidase and catalase, which catalyze the reaction of glucose and oxygen. The production rate of gluconic acid increased with the speed of rotation and the bulk flow rate. An optimum submergence for maximum productivity existed.     

Mathematical modeling of ethanol production by immobilized Zymomonas mobilis in a packed bed fermenter

A mathematical model which describes ethanol production in a packed bed fermenter containing. Zymomonas mobilis entrapped in small spheres of calcium alginate within a packed bed fermenter has been developed. The equations combine simultaneous diffusion and reaction as well as a complex flow pattern to calculate glucose and ethanol profiles in the column type reactor. As part of the study, diffusivity values for glucose and ethanol in cell-loaded calcium alginate were determined. Also a freecell kinetic expression for Z. mobilis at 33 degrees C and ph 6.0 was developed. Comparison of the model with actual experimental results were made showing average deviations of ca. 30-40%.     

Various applications of immobilized glucose oxidase and polyphenol oxidase in a conducting polymer matrix

In this study, glucose oxidase and polyphenol oxidase were immobilized in conducting polymer matrices; polypyrrole and poly(N-(4-(3-thienyl methylene)-oxycarbonyl phenyl) maleimide-co-pyrrole) via electrochemical method. Fourier transform infrared and scanning electron microscope were employed to characterize the copolymer of (N-(4-(3-thienyl methylene)-oxycarbonyl phenyl) maleimide) with pyrrole. Kinetic parameters, maximum reaction rate and Michealis-Menten constant, were determined. Effects of temperature and pH were examined for immobilized enzymes. Also, storage and operational stabilities of enzyme electrodes were investigated. Glucose and polyphenol oxidase enzyme electrodes were used for determination of the glucose amount in orange juices and human serum and phenolic amount in red wines, respectively.     

A heat transfer study on packed bed reactors of immobilized glucoamylase

Enzymes are generally sensitive to temperature changes. Porous glass particles used for glucoamylase immobilization are poor thermal conductors and a non-uniform temperature distribution can conceivably develop in a packed bed reactor of immobilized glucoamylase on porous beads. This study was made to determine experimentally the temperature and concentration profiles in an immobilized glucoamylase column. This work provides a procedure for examining possible heat effects on reactor column performance in enzyme applications.     

Production of structured triacylglycerols by acidolysis catalyzed by lipases immobilized in a packed bed reactor

The aim of this work was to produce structured triacylglycerols (STAGs), with caprylic acid located at positions 1 and 3 of the glycerol backbone and docosohexaenoic acid (DHA) at position 2, by acidolysis of tuna oil and caprylic acid (CA) catalyzed by lipases Rd, from Rhizopus delemar, and Palatase 20000L from Mucor miehei immobilized on Accurel MP1000 in a packed bed reactor (PBR), working in continuous and recirculation modes. First, different lipase/support ratios were tested for the immobilization of lipases and the best results were obtained with ratios of 0.67 (w/w) for lipase Rd and 6.67 (w/w) for Palatase. Both lipases were stable for at least 4 days in the operational conditions. In the storage conditions (5 °C) lipases Rd and Palatase maintained constant activity for 5 months and 1 month, respectively.These catalysts have been used to obtain STAGs by acidolysis of tuna oil and CA in a PBR operating with recirculation of the reaction mixture through the lipase bed. Thus, STAGs with 52–53% CA and 14–15% DHA were obtained. These results were the basis for establishing the operational conditions to obtain STAGs operating in continuous mode. These new conditions were established maintaining constant intensity of treatment (IOT, lipase amount × reaction time/oil amount). In this way STAGs with 44–50% CA and 17–24% DHA were obtained operating in continuous mode. Although the compositions of STAGs obtained with both lipases were similar, Palatase required an IOT about four times higher than lipase Rd.To separate the acidolysis products (free fatty acids, FFAs, and STAGs) an extraction method of FFAs by water–ethanol solutions was tested. The following variables were optimized: water/ethanol ratio (the best results were attained with a water/ethanol ratio of 30:70, w/w), the solvent/FFA–STAG mixture ratio (3:1, w/w) and the number of extraction steps (3–5). In these conditions highly pure STAGs (93–96%) were obtained with a yield of 85%. The residual FFAs can be eliminated by neutralization with a hydroethanolic KOH solution to obtain pure STAGs. The positional analysis of these STAGs, carried out by alcoholysis catalyzed by lipase Novozym 435, has shown that CA represents 55% of fatty acids located at positions 1 and 3 and DHA represents 42% of fatty acids at position 2.     

Experimental behavior of a whole cell immobilized dextransucrase biocatalyst in batch and packed bed reactors

Dextransucrases from Leuconostoc mesenteroides have been used to produce a diversity of controlled structure oligosaccharides with potential industrial applications. This is the case of !(1̄) branched glucooligosaccharides produced by L. mesenteroides NRRL B-1299 dextransucrase. In order to establish an industrial scale process with the immobilized enzyme, a biocatalyst was produced by whole cell entrapment in alginate beads. The main physical and physicochemical properties of the biocatalyst were determined and the hydrodynamic behavior in a packed bed reactor studied. It was possible to produce spherical beads of 0.2 cm diameter containing the insoluble part of L. mesenteroides culture (cells and insoluble polymer) with an activity of 4 IU/g. Immobilization yield reached 93% with an effectiveness factor of 0.995 for particles of d_p < 0.2 cm. Due to the complexity of dextransucrase mechanism and kinetics, data obtained from initial rate measurements failed to describe the results obtained from the batch and continuous reactors. Therefore, apparent K_M and V_max data were used for the reactor modeling. It was found that under the conditions studied, the reaction rate was controlled by external mass transfer limitations.     

Properties of a glucose oxidase covalently immobilized on amorphous AlPO4 support

Glucose oxidase (GOD) was covalently immobilized on amorphous AlPO₄ as well as on an AlPO₄/clay mineral Sepiolite system. Immobilization of the enzyme was carried out through the -amino group of lysine residues through an aromatic Schiff's-base. Activation of the support was obtained after reaction of appropriate molecules with support surface –OH groups. The enzymatic activities of native, and different immobilized GOD systems and filtrates, were followed by the amount of liberated -gluconic acid obtained in the enzymatic β- -glucose oxidation with the aid of an automatic titrator. The kinetic properties of native and immobilized GOD were obtained for glucose concentrations in the range of physiological conditions and at different working conditions such as reaction temperature, reaction pH, and enzyme concentration.

The binding percentage of enzymes was in the 50–80% range, with residual and specific activities in the 65–80% and 90–150% ranges, respectively. No change in the pH optimum and only slight changes in the V_max and K_M kinetic parameters with respect to native GOD were observed, so that not only was little deactivation of enzyme obtained throughout the immobilization process but also that the stability of the covalently bound enzyme in the two supports appeared to have increased with respect to the soluble enzyme. GOD immobilization also increased its efficiency and operational stability in repeated uses on increasing the amount of immobilized enzyme.     

R-mandelic acid production with immobilized recombinant Escherichia coli cells in a recirculating packed bed reactor

A recirculating packed bed reactor (RPBR) was used for efficient production of R-mandelic acid (R-MA) by kinetic resolution of racemic R,S-mandelonitrile (R,S-MN) using the recombinant E. coli cells crosslinked with diatomite (DA)/glutaraldehyde (GA)/polyethyleneimine (PEI). The performance and productivity of RPBR were evaluated by several parameters, including cell load, substrate feeding rate, height diameter (H/D) ratio, reactor structures, and operation stability. The kinetic resolution process showed higher initial reaction rate (1.52?mM/min) and yield (100%) by recycling 100?mL of substrate solution (70?mM) through RPBR packed with 6.0?g immobilized cells at a substrate-feeding rate of 19?mL/min while the H/D ratio was 2.8. The immobilized cells were successfully applied into kinetic resolution of R,S-MN in the RPBR for 50 batches with an average productivity of 4.12?g/L/h for R-MA with >99% of enantiomeric excess.     

A kinetic model for methanogenesis from whey permeate in a packed bed immobilized cell bioreactor

The fermentation kinetics of methane production from whey permeate in a packed bed immobilized cell bioreactor at mesophilic temperatures and pHs around neutral was studied. Propionate and acetate were the only two major organic intermediates found in the methanogenic fermentation of lactose. Based on this finding, a three-step reaction mechanism was proposed: lactose was first degraded to propionate, acetate, CO(2), and H(2) by fermentative bacteria; propionate was then converted to acetate by propionate-degrading bacteria; and finally, CH(4) and CO(2) were produced from acetate, H(2), and CO(2) by methanogenic bacteria. The second reaction step was found to be the rate-limiting step in the overall methanogenic fermentation of lactose. Monod-type mathematical equations were used to model these three step reactions. The kinetic constants in the models were sequentially determined by fitting the mathematical equations with the experimental data on acetate, propionate, and lactose concentrations. A mixed-culture fermentation model was also developed. This model simulates the methanogenic fermentation of whey permeate very well.     

Performance of cell immobilized packed bed bioreactor for continuous fermentation of alcohol

Experiments were conducted in a packed bed bio-reactor consisting of entrapped yeast cells in alginate matrix for continuous production of alcohol. The variables include initial substrate level, reactor diameter, diameter of the bead and residence time. The influence of these parameters on the conversion of substrate was studied. The film and pore diffusional effects were observed by varying the column and bead diameters, respectively. The pseudo first order reaction rate constant was calculated and correlated with the bead diameter. The effectiveness factor and the Thiele modulus were estimated. A correlation was proposed for fractional conversion in terms of operating variables. It is possible to predict the residence time required and volumetric productivity achieved in a bioreactor for any given initial substrate concentration at any fractional conversion obtained.List of Symbols a _m m²/kg surface are per unit mass of catalyst particle - D m diameter of the reactor - D _e m²/s effective diffusivity - d m particle diameter - h m bed height - k m/s first order reaction rate constant - k m³/(kg · s) pseudo first order reaction rate constant - k _in m³/(kg · s) intrinsic reaction rate constant, (=K/gh) - k _m m/s mass transfer coefficient - P kmol/(m³ · s) volumetric productivity - Q m³/s flow rate of the feed - S kmol/m³ substrate concentration at any time - S _o kmol/m³ initial substrate concentration - S _p kmol/m³ substrate concentration on the gel bead surface - t s reaction time - T (kg · cat · s)/m³ space time (weight of the biocatalyst/flow rate of the feed) - v kmol/(kg · cat · s) reaction rate - V _pfr m³ volume of the packed bed reactor - X [1-(S/S _o)] fraction of the substrate converted in to product Greek Symbols effectiveness factor - Thiele modulus - kg/m³ density of the catalyst particle - s residence time, (= D² h/4Q) - voidage     

Evaluation of the effectiveness factor along immobilized enzyme fixed-bed reactors: Design of a reactor with naringinase covalently immobilized into glycophase-coated porous glass

A design equation is presented for packed-bed reactors containing immobilized enzymes in spherical porous particles with internal diffusion effects and obeying reversible one-intermediate Michaelis-Menten kinetics. The equation is also able to explain irreversible and competitive product inhibition kinetics. It allows the axial substrate profiles to be calculated and the dependence of the effectiveness factor along the reactor length to be continuously evaluated. The design equation was applied to explain the behavior of naringinase immobilized in Glycophase-coated porous glass operating in a packed-bed reactor and hydrolyzing both p-nitrophenyl-alpha-L-rhamnoside and naringin. The theoretically predicted results were found to fit well with experimentally measured values.     

Continuous aerobic phenol degradation by defined mixed immobilized culture in packed bed reactors

A defined mixed culture of Pseudomonas putida, Commamonas testosteroni and Candida tropicalis was immobilized by adsorption on polyurethane foam, cocoa-fibers, expanded slate and sintered glass. Packed bed reactors were used for long-term continuous phenol biodegradations. Loading experiments were done to study the impact of the following parameters: (1) hydraulic retention time, (2) dissolved oxygen concentration, and (3) elimination of the oxygen limitation. After the acclimation period (approximately 10 d), the loading test with the individual packings showed the following maximum degradation rates: sintered glass 34, polyurethane foam 12, expanded slate 11.5, and cocoa-fibers 7.7 kg m(-3) d(-1). All these values were reached at a removal efficiency >99 % and with oxygen in excess. Under these conditions, the pH of the diluted unbuffered medium in the reactor effluent was 3.2-4.0 and no incompletely oxidized metabolic intermediates were found. The free cell concentration in the effluent increased after the phenol overloading time period.     

Online immobilized enzyme microreactor for the glucose oxidase enzymolysis and enzyme inhibition assay

An online immobilized glucose oxidase (GOx) capillary microreactor was developed based on an enzymatic redox reaction with 1,4-benzoquinone as an acceptor of electrons, replacing the molecular oxygen typically used in a GOx reaction to achieve direct ultraviolet detection without derivation. A high efficiency of enzymolysis was obtained at 1 mg ml^?1 1,4-benzoquinone for 5 min of incubation at 25 °C, and baseline separation of the substrate and product could be achieved with a resolution of 3.85 by employing 20 mM phosphate buffer (pH 8.0) containing 40 mg ml^?1 sulfated β-cyclodextrin as an additive, a constant voltage of 15 kV, and a detection wavelength of 220 nm. In addition, an online enzyme inhibition study was performed on the immobilized GOx microreactor with metal ions Ag⁺ and Cu²⁺ used as model inhibitors. The results indicate that Ag⁺ (IC₅₀ = 69.16 μM) has a markedly higher inhibitory effect than Cu²⁺ (IC₅₀ = 1.33 mM). The protocol described can be applied in high-throughput screening of enzyme reactions and inhibitors.