Conversion of cellobiose to glucose using immobilized β-glucosidase reactors

Cellobiose is an intermediate in the enzymatic hydrolysis of cellulose to glucose and acts as an inhibitor for the cellulase enzymes. The conversion of cellobiose to glucose was studied with β-glucosidase adsorbed on Amberlite DP-1, a cation-exchange resin. The best overall pH for adsorption and reactor operation was near 5.0. The K_m values increased with increasing enzyme loading due to competitive inhibition. The maximum practical enzyme loading was about 28 units/g resin. The immobilized enzyme was operated continously in both packed bed and fluidized bed reactors, giving half-lives between 200 and 375 h.     

Flow dynamics of immobilized enzyme reactors

Summary Enzymic conversion of glucose to fructose was carried out in a packed bed and in a fluidized bed reactor. The flow dynamics of these two flow systems, loaded with two different types of immobilized loaded with two different types of immobilized glucose isomerase particles, were studied. The theoretical RTD curve calculated from the axial dispersed plug flow model equation was matched to the experimental RTD curve by an optimization technique. The effect of fluid velocity on the extent of liquid dispersion was established. Theoretical predictions on the conversion of glucose to fructose were calculated using three mathematical models, namely, a plug flow model, a continuous stirred tank reactor (CSTR) model and an axial dispersed plug flow model. The experimental results showed that the axial dispersed plug flow model was superior in predicting the performance of both the packed bed and fluidized bed reactor.Abbreviations C Dimensionless concentration - D Dispersion coefficient [cm²/sec] - d _p Mean particle diameter [cm] - E Enzyme concentration [mol/gm] - F Fructose concentration [mol/cm³] - F _e Equilibrium fructose concentration [mol/cm³] - G Glucose concentration [mol/cm³] - G _e Equílibrium glucose concentration [mol/cm³] - G _o Initial glucose concentration [mol/cm³] - Reduced glucose concentration [mol/cm³] - K Equilibrium constant - K _mf Forward reaction rate constant [mol/cm³] - K _mr Reserve reaction rate constant [mol/cm³] - K _m Rate constant [mol/cm³] - L Total length of the reactor bed [cm] - l Length [cm] - Q Flow rate [cm³/s] - r Rate of reaction based on volume of substrate - u Superficial liquid velocity [cm/s] - v Interstitial liquid velocity [cm/s] - V Reactor bed volume [cm³] - V _mf Forward reaction rate constant [mol/s·g enzyme] - V _mr Reserve reaction rate constant [mol/s·g enzyme] - z Dimensionless distance along the reactor - Density [g/cm²]     

Continuous ethanol production by immobilized yeast in a fluidized reactor

Summary In order to minimize the adverse effect of CO₂ gas in a packed bed immobilized yeast reactor, a fluidized bed reactor was used for the continuous production of ethanol from glucose. Immobilized yeast was prepared by entrapping whole cells of Saccharomyces cerevisiae within a Caalginate matrix. It was found that the efficiency of the ethanol production in a fluidized bed reactor was 100% better than that for a packed bed reactor system. The alcohol productivity obtained was 21 g/l/hr in a fluidized bed reactor at 94% of conversion level.     

One-dimensional model of the acid hydrolysis of cellulosic substrates in a solid-liquid cyclone reactor

The use of rotating flow in an annulus is investigated as a means of enhancing the yield of glucose and xylose in the acid hydrolysis of cellulosic slurries. A one-dimensional model of such a cyclone reactor is developed for flow cases, co-current and counter-current flow. For the case of 250°C, 1% w/w acid, the one-dimensional model indicates an increase in the maximum glucose yield from 48.1% in a plug flow reactor to 69.3% in a co-current cyclone reactor, and up to 81.0% in a countercurrent cyclone reactor. The corresponding xylose yields are 91.6% for co-current operation and 97.7% for countercurrent operation. In the co-current case the maximum glucose and xylose yields do not occur at the same location in the reactor; however, in the countercurrent case they do. Although product yields are dramatically improved over those obtained in a plug flow reactor, the product concentrations are lower than would typically be obtained in a plug flow reactor.List of Symbols A cm² cross sectional area perpendicular to radial flow - A _c cm² cross sectional area of slurry inlet - A _c cm² cross sectional area of steam inlet - A _w cm² cross sectional area of water inlet - C _c concentration of cellulose as potential glucose (grams of potential glucose/cm³ of total stream) - C _c ^* grams cellulose/cm³ of solids concentration of cellulose as potential glucose - C _ginitial ^* grams glulose/cm³ of solids concentration of cellulose entering reactor - C _g grams glucose/cm³ of total stream concentration of glucose - C _g ^* grams glucose/cm³ of liquid stream concentration of glucose - C _cinitial ^* grams cellulose/cm³ of liquid concentration of glucose entering reactor - C _xn concentration of xylan as potential xylose (grams of potential xylose/cm³ of total stream) - C _xs grams xyclose/cm³ of total stream concentration of nylose - d _f dilution factor - dr cm radial increment - g cm/s² gravitational acceleration - g ^* centrifugal acceleration proportionality constant - h cm height of cyclone reactor - j cm/s flux - K constant in general equation for vortex flow, Eq. (4.9) - k ₁ 1/s kinetic rate constant of cellulose hydrolysis - k _a 1/s kinetic rate constant of xylan hydrolysis - k ₂ 1/s kinetic rate constant of glucose decomposition - k _2a 1/s kinetic rate constant of xylose decomposition - m vortex exponent - M _steam g/s mass rate of steam addition at outer radius - M _water g/s mass rate of cold water addition at outer radius - n cm³/s empirically determined settling parameter - Q cm³/s net volumetric flow in outward radial direction - Q _tot cm³/s total volumetric flow through reactor - q _c cm³/s volumetric flow of slurry feed - q _s cm³/s volumetric flow of stream feed - q _water cm³/s volumetric flow of cold water feed - r cm radial position - r _c 1/s rate of cellulose hydrolysis - r _g 1/s rate of glucose decomposition - r _i cm inner radius - r _o cm outer radius - r _xn 1/s rate of xylan hydrolysis - r _xs 1/s rate of xylose decomposition - s _mom cm g/s² inlet steam momentum - T _bulk s bulk residence time in reactor - T °C reactor temperature - v _c cm³/g specific volume of slurry feed - v _s cm³/g specific volume of steam - v _w cm³/g specific volume of water - V _f cm/s velocity of liquid as a function of radius - V _i cm/s inlet velocity - V _s cm/s velocity of solids as a function of radius - V _steam cm/s inlet steam velocity to cyclone - V cm/s terminal settling velocity - V _q cm/s tangential velocity - w _mom cm g/s² water inlet momentum - Y grams product out/grams reactant in yield of product - solids volumetric fraction - _f solids volumetric fraction in slurry feed - _i initial solids volumetric fraction of slurry - Pi     

Sustained ammonia production by immobilized filaments of the nitrogen-fixing cyanobacterium Anabaena 27893

Summary Whole filaments of the N₂-fixing cyanobacterium Anabaena ATCC 27893 have been immobilized by entrapment in calcium alginate gel beads. In a continuous flow fluidized bed reactor sustained photosynthesis, N₂-fixation, and ammonia production have been achieved over a 130 hour period, the longest tested.     

Citric acid production by immobilized Aspergillus niger in a fluidized bed reactor

Summary Citric acid production by immobilized of Aspergillus niger in a fluidized bed reactor was performed, evaluating the productivity and the stability of the process when pulsing device was used. The application of a pulsing flow to fluidized bed reactor and the feed nitrogen limited allow to control of bioparticles morphology avoiding bed compactation. When operated at optimum pulsation frequency (0.3 s^–1) the stability of the bioreactor was maintained for more than 30 days, increasing the citric acid production in more than 52.2%.     

Continuous Asymmetric Reduction Of 4-Oxoisophorone By Thermophilic Bacteria Using A Hollow Fiber Reactor

Continuous asymmetric reduction of 4-oxoisophorone by the thermophilic bacterium Thermomonospora curvata JTS321 was examined using three reactor systems: packed bed, fluidized bed and hollow fiber. T. curvata was immobilized in polyacrylamide-hydrazide gels when used in the packed and fluidized bed reactors. Of the three reactor systems, the highest productivity (964 mg.1^-1.h^-1) was observed in the fluidized bed reactor. However, many cells grew outside of the gel matrix, causing product contamination. The productivity of the hollow fiber reactor was 504 mg.1^-1.h^-1; the problem of cell contamination of the product was avoided, as the molecular cut-off of the hollow fibers (400 000) was of an appropriate size to prevent cell leakage to the product stream. We therefore consider that the hollow fiber reactor is most suitable for continuous microbial conversions.     

Hydrogen production with immobilized sewage sludge in three-phase fluidized-bed bioreactors

Municipal sewage sludge was immobilized with a modified alginate gel entrapment method, and the immobilized cells were used to produce hydrogen gas in a three-phase fluidized bed. The hydrogen-producing fluidized beds were operated at different liquid velocity (U(0)) and hydraulic retention time (HRT). The results show that in response to operating liquid velocities, the fluidized-bed system had three flow regimes, namely, plug flow, slug flow, and free bubbling. Pressure fluctuation analysis was used to analyze the hydrodynamic properties in this three-phase fluidized bed when it was under a steady-state production of biogas. With a steady-state biogas production rate (U(g)) of 0.196 mL/s/L, a transition state occurred at a liquid velocity (U(0)) of 0.85 cm/s. As U(0) < 0.85 cm/s, the system was basically a nonhomogeneous fluidized bed, whereas the bed became homogeneous when U(0) was higher than 0.85 cm/s. The fluidized bed can be stably carried out at high loading rates (HRT as low as 2 h). Hydrogen fermentation results show that the maximal hydrogen production rate was 0.93 L/h/L and the best yield (Y(H)2(/sucrose)) was 2.67 mol H(2)/mol sucrose.     

Biodegradation of cellulose by β-glucosidase and cellulase immobilized on a pH-responsive copolymer

Biodegradation of cellulose involves synergistic action of the endoglucanases, exoglucanases and β-glucosidases in cellulase. However, the yield of glucose is limited by the lack of β-glucosidase to hydrolyze cellobiose into glucose. In this study, β-glucosidase as a supplemental enzyme along with cellulase are co-immobilized on a pHresponsive copolymer, poly (MAA-co-DMAEMA-co-BMA) (abbreviated P_MDB, where MAA is α-methacrylic acid, DMAEMA is 2-dimethylaminoethyl methacrylate and BMA is butyl methacrylate). The thermal and storage stabilities of PMDB with immobilized enzymes are improved greatly, compared with those of free cellulase. Biodegradation of cellulose is carried out in a pH-responsive recyclable aqueous two-phase system composed of poly (AA-co- DMAEMA-co-BMA) (abbreviated P_{ADB 3.8}, where AA is acrylic acid) and P_MDB. Insoluble substrate and P_MDB with immobilized cellulase and β-glucosidase (Celluclast 1.5L FG and Novozyme 188, respectively) were biased to the bottom phase, while the product was partitioned to the top phase in the presence of 40 mM (NH₄)₂SO₄. When the degradation reaction of cellulose is carried out with PMDB containing immobilized cellulase and β-glucosidase, the concentration of glucose reaches 4.331 mg/mL after 108 h. The yield of glucose is 50.25% after P_MDB containing the immobilized enzymes is recycled five times.     

Continuous ethanol production by Zymomonas mobilis in a fluidized bed reactor. Part II: Process development for the fermentation of hydrolysed B-starch without sterilization

A continuous fluidized bed reactor operation system has been developed for ethanol production by Zymomonas mobilis using hydrolysed B-starch without sterilization. The operation system consists of two phases. In the first phase macroporous glass carriers in a totally mixed fluidized bed reactor were filled up totally with a monoculture of Z. mobilis by fast computer-controlled colonization, so that in the subsequent production phase no contaminants, especially lactic-acid bacteria, could penetrate into the carrier beads. In the production phase the high concentration of immobilized Z. mobilis cells in the fluidized bed reactor permits unsterile fermentation of hydrolysed B-starch to ethanol at short residence times. This results in wash-out conditions for contaminants from the substrate. Long-term experimental studies (more than 120 days) of unsterile fermentation of hydrolysed B-starch in the laboratory fluidized bed reactor (2.2 l) demonstrated stable operation up to residence times of 5 h. A semi-technical fluidized bed reactor plant (cascade of two fluidized bed reactors, each 55 l) was operated stably at a mean residence time of 4.25 h. Glucose conversion of 99% of the unsterile hydrolysed B-starch was achieved at 120 g glucose/l^–1 in the substrate, resulting in an ethanol concentration of 50 g·l^–1 and an ethanol space-time yield of 13 g·l^–1·h^–1. This is a factor of three compared to ethanol fermentation of hydrolysed B-starch with Z. mobilis in a continuous stirred tank reactor, which can only be operated stably under sterile conditions. Correspondence to: D. Weuster-Botz     

Biodegradation of microcrystalline cellulose in pH–pH recyclable aqueous two-phase systems with water-soluble immobilized cellulase

Product inhibition is a barrier for enzymatic conversion of cellulose into reducing sugar in single aqueous phase. In addition, the difficulty in the recovery of cellulase also leads to high cost for the enzymatic hydrolysis of cellulose. In this study, enzymatic degradation of cellulose was carried out in pH–pH recyclable aqueous two-phase systems (ATPS) composed by copolymers poly (AA-co-DMAEMA-co-BMA) (abbreviated P_ADB3.8) and poly (MAA-co-DMAEMA-co-BMA) (abbreviated P_MDB). In the systems, cellulase was immobilized on pH-response copolymer P_MDB by using 1-Ethyl-3-(3-dimethyllaminopropyl)-carbodiimide hydrochloride (EDC) as cross-linker. Optimized partition coefficient of product in the systems was 2.45, in the presence of 40 mM (NH₄)₂SO₄. Insoluble substrate and immobilized enzyme were biased to bottom phase, while the product was partitioned to top phase. Microcrystalline cellulose was hydrolyzed into reducing sugar, and the product entered into top phase. The yield of saccharification in ATPS could reach 70.57% at the initial substrate concentration of 0.5% (w/v), and the value was 9.3% higher than that in the single aqueous phase. Saccharification yield could reach 66.15% after immobilized cellulase was recycled five times in ATPS.     

Use of a tapered fluidized bed as a Continuous bioreactor

Reactor systems based on tapered fluidized beds are being developed for aqueous bioprocesses in which adhering microorganisms or immobilized active biological fractions are used. The use of a fluidized bed prevents biomass buildup, accommodates particulates in the feed stream, is compatible with gas sparging, and allows easy removal or addition of the active materials. The tapered reactor tends to stabilize the fluidized bed, thus allowing a much wider range of operating conditions. Preliminary experimental results and an empirical mathematical model of the tapered bed indicate that bed stability is associated with a decreasing velocity and void-fraction profile up the bed and the pressure drop across the bed decreases with increasing flow rates. The tapered fluidized bed bioreactor is being evaluated for use in the enzymatic production of hydrogen, microbiological denitrification, and microbiological degradation of coal conversion aqueous waste streams. The enzyme catalyzed conversion of lactose to glucose and galactose was used in the evaluation of the reactor concept.     

Photometabolic production of hydrogen from organic substrates by free and immobilized mixed cultures of Rhodospirillum rubrum and Klebsiella pneumoniae*

A culture of R. rubrum cells apparently contaminated with K. pneumoniae were immobilized by entrapment in agar. This system was used as model for hydrogen production by photometabolic means. Observed results indicated that the contaminant exerted a major influence on the observed results. This preparation, when immobilized and used in a specifically designed reactor with glucose substrate, showed operational half-lives of approximately 1000 hr. The feasibility of using this “mixed” culture for producing hydrogen from acid hydrolyzed cellulose and wood sawdust was also examined.     

Effect of cellulose physical characteristics, especially the water sorption value, on the efficiency of its hydrolysis catalyzed by free or immobilized cellulase

Cellulase, an enzymatic complex that synergically promotes the degradation of cellulose to glucose and cellobiose, free or adsorbed onto Si/SiO₂ wafers at 60 °C has been employed as catalyst in the hydrolysis of microcrystalline cellulose (Avicel), microcrystalline cellulose pre-treated with hot phosphoric acid (CP), cotton cellulose (CC) and eucalyptus cellulose (EC). The physical characteristics such as index of crystallinity (I_C), degree of polymerization (DP) and water sorption values were determined for all samples. The largest conversion rates of cellulose into the above-mentioned products using free cellulase were observed for samples with the largest water sorption values; conversion rates showed no correlation with either I_C or DP of the biopolymer. Cellulose with large water sorption value possesses large pore volumes, hence higher accessibility. The catalytic efficiency of immobilized cellulase could not be correlated with the physical characteristics of cellulose samples. The hydrolysis rates of the same cellulose samples with immobilized cellulase were lower than those by the free enzyme, due to the diffusion barrier (biopolymer chains approaching to the immobilized enzyme) and less effective contact between the enzyme active site and its substrate. Immobilized cellulase, unlike its free counterpart, can be recycled at least six times without loss of catalytic activity, leading to higher overall cellulose conversion.     

Lactate from cultures of Lactobacillus casei recovered in a fluidized bed column using ion exchange resin

Summary Lactic acid produced by continuous culture of L.casei in an upflow packed bed reactor, was recovered with Amberlite IRA 400 in a fluidized bed column. Bed expansions of 1.25 and 2.25 were applied. Reutilization did not alter the capability of net recovery of 0.048 ± 0.01 g lactic acid/g resin. When 2200 cm/h of ascensional velocity was used, (bed expansion of 2.25), the resin adsorbed 39.3% of the initial lactic acid and 63.5% was eluted. This resin supported the highest exchange capacity of 0.126 g lactic acid/g resin. Applying high flow rates, the process has potential industrial applications due to the short time employed.     

Cellulase production by a thermophilic clostridium species

Strain M7, a thermophilic, anaerobic, terminally sporing bacterium (0.6 by 4.0 μm) was isolated from manure. It degraded filter paper in 1 to 2 days at 60 C in a minimal cellulose medium but was stimulated by yeast extract. It fermented a wide variety of sugars but produced cellulase only in cellulose or carboxymethyl-cellulose media. Cellulase synthesis not only was probably repressed by 0.4% glucose and 0.3% cellobiose, but also cellulase activity appeared to be inhibited by these sugars at these concentrations. Both C₁ cellulase (degrades native cellulose) and C_x cellulase (β-1,4-glucanase) activities in strain M7 cultures were assayed by measuring the liberation of reducing sugars with dinitrosalicylic acid. Both activities had optima at pH 6.5 and 67 C. One milliliter of a 48-h culture of strain M7 hydrolyzed 0.044-meq of glucose per min from cotton fibers. The cellulase(s) from strain M7 was extracellular, produced during exponential growth, but was not free in the growth medium until approximately 30% of the cellulose was hydrolyzed. Glucose and cellobiose were the major soluble products liberated from cellulose by the cellulase. ZnCl₂ precipitation appeared initially to be a good method for the concentration of cellulase activity, but subsequent purification was not successful. Isoelectric focusing indicated the presence of four C_x cellulases (pI 4.5, 6.3, 6.8, and 8.7). The rapid production and high activity of cellulases from this organism strongly support the basic premise that increased hydrolysis of native cellulose is possible at elevated temperature.     

Improvement of Process Stability of Microbiological Quinoline Degradation in a Three‐Phase Fluidized Bed Reactor

The biological degradation of quinoline by suspended and immobilized Comamonas acidovorans was studied under continuous and discontinuous operating conditions in a three‐phase fluidized bed reactor. C. acidovorans degrades quinoline into biomass and carbon dioxide. Quinoline and the intermediates of its metabolic pathway are found only by quinoline shockloads. The continuous degradation of quinoline by suspended biomass was only possible, if the dilution rate was less than the growth rate (μ_max =0.42 h^–1) and the concentration of a shockload was less than 1 kg/m³. A concentration greater than 1 kg/m³ led to an irreversible damage of the cells. Hence, two different carrier materials were used for immobilization by attachment, to increase the stability of the process. Using immobilization of biomass on carriers decouples the hydrodynamic retention time and the growth rate of the microorganisms. A comparison of the carrier material showed no differences with respect of activity and stability of the biofilm. The process stability of a three‐phase fluidized bed reactor was increased by immobilized biomass. The degradation of toxic shockloads was only possible with immobilized biomass. A dynamic model has been developed to describe the concentration profile of quinoline, 2‐hydroxyquinoline as metabolite and the suspended biomass. A comparison of the measured and calculated values showed good agreement.     

Cellulose hydrolysis by immobilized <Emphasis Type="Italic">Trichoderma reesei</Emphasis> cellulase

Cellulose hydrolysis by immobilized Trichoderma reesei cellulase in the presence of a low viscosity ionic liquid, 1-ethyl-3-methylimidazolium diethyl phosphate (EMIM-DEP), was investigated. Preparation of the carrier-free immobilized cellulase was optimized with respect to concentration of the cross-linker and the type of precipitant. The addition of 2% (v/v) EMIM-DEP during hydrolysis gave an initial reaction rate 2.7 times higher than the hydrolysis rate with no ionic liquid. The initial yield after 2 h was 0.7 g glucose/g cellulose, and the carrier-free immobilized cellulase (CFIC) was effectively re-used five times.     

Cellulase Enzyme from Aspergillus niger

Cellulase enzyme was produced by a selected strain of Aspergillus niger isolated from deteriorated wood and grown on different carbon sources. Filter paper gave the highest yield, followed by carboxymethyl cellulose (CMC). Cellobiose as well as glucose gave a low yield, while the yield from lactose was negligible. The concentration of filter paper cellulose that induced the maximum yield of the enzyme was 1%. Both soluble cellulose (CMC) and cotton cellulose treated with phosphoric acid (swollen) were easily hydrolyzed by cellulase; an increase in cellulase concentration lead to more hydrolysis of CMC and gave linearity in the reaction velocity. At certain concentrations of the enzyme, increase in CMC concentration, (up to 1%) resulted in more reducing sugar. Beyond this point no more hydrolysis occur.     

Continuous ethanol production by Zymomonas mobilis in a fluidized bed reactor. Part I. Kinetic studies of immobilization in macroporous glass beads

A model has been developed to calculate the ethanol production in a well-mixed fluidized bed reactor. This model takes into account diffusion and the reaction inside porous glass beads and the activity of suspended cells in the fluidized bed reactor. The associated model parameters have been determined from the literature and by kinetic studies with Zymomonas mobilis in a continuous stirred tank reactor. The model permits good predictions of steady-state data in a fluidized bed reactor at residence times longer than 1–1.5 h. The immobilization of Z. mobilis in a fluidized bed reactor results in high ethanol space-time yields of more than 50 g·^–1·h^–1 at a glucose conversion of 80% (glucose in substrate: 120 gl^–1). At 99% conversion a space-time yield of 30 g·^–1·^–1 can be achieved when two fluidized bed reactors operate as cascade.