Performance of the continuous glucose isomerase reactor system for the production of fructose syrup

Glucose isomerase in the form of heat-treated whole-cell enzyme prepared from Streptomyces phaeochromogenus follows the reversible single-substrate reaction kinetics in isomerization of glucose to fructose. Based on the Kinetic constants determined and the mathematical model of the reactor system developed, the preformance of a plug-flow-type continuous-enzyme reactor system was studied experimentally and also simulated with the aid of a computer for the ultimate objective of optimization of the glucose isomerase reactor system. The enzyme decay function for both the enzyme storage and during the use in the continuous reactor, was found to follow the first-order decay kinetics. When the enzyme decay function is taken into consideration, the ideal homogeneous enzyme reactor kinetics provided a satisfactory working model without further complicatin of the mathematical model, and the results of computer simulation were found to be in good agreement with the experimental results. Under a given set of constraints the performance of the continuous glucose isomerase reactor system can be predicted by using the computer simulation method described in this paper. The important parameters studied for the optimization of reactor operation were enzyme loading, mean space time of the reactor, substrate feed concentration, enzyme decay constants, and the fractional conversion, in addition to the kinetic constants. All these parameters have significant effect on the productivity. Some unique properties of the glucose isomerization reaction and its effects on the performance of the continuous glucose isomerase reactor system have been studied and discussed. The reaction kinetics of glucose isomerase and the effects of both the enzyme loading and the changes in reaction rate within a continuous reactor on the productivity are all found to be of particular importance to this enzyme reactor system.     

Performance of a cyclic operated multicolumns recirculated packed bed batch reactor for 6-APA production

The methodology for designing a multicolumns recirculated packed bed batch reactor (MRPBR) system is developed. The performance of the system employing immobilized penicillin-G amidase (IPGA) for the production of 6-APA is studied. The total IPGA activity in the cyclic operated MRPBR system is maintained within a constant range by periodically replacing the oldest column in the system. The reaction time for each cycle of batch reaction is, therefore, maintained within a constant range by employing a sufficient number of columns and independent on the cycle number. The variations of 6-APA production rate is held to a desired level. The production yield of IPGA increases and 6-APA production rate decreases with the number of column installed in the MRPBR system. Both the production yield and production rate increase with the IPGA lifetime in the system. The production yield can be enhanced significantly by extending the batch reaction time. For a system designed to allow the batch reaction to be completed within 240 min, the production yield of IPGA can be 80% higher than that in the stirred tank reactor (STR) system. However, the 6-APA production rate decreases to 55% of that in STR system.     

Transesterification of palm oil to methyl ester on activated carbon supported calcium oxide catalyst

In this study, methyl ester (ME) was produced by transesterification of palm oil (CPO) (cooking grade) using activated carbon supported calcium oxide as a solid base catalyst (CaO/AC). Response surface methodology (RSM) based on central composite design (CCD) was used to optimize the effect of reaction time, molar ratio of methanol to oil, reaction temperature and catalyst amount on the transesterification process. The optimum condition for CPO transesterification to methyl ester was obtained at 5.5 wt.% catalyst amount, 190 °C temperature, 15:1 methanol to oil molar ratio and 1 h 21 min reaction time. At the optimum condition, the ME content was 80.98%, which is well within the predicted value of the model. Catalyst regeneration studies indicate that the catalyst performance is sustained after two cycles.     

Butanol production by Clostridium acetobutylicum in a continuous packed bed reactor

In this study, we report on a butanol production process by immobilized Clostridium acetobutylicum in a continuous packed bed reactor (PBR) using Tygon^® rings as a carrier. The medium was a solution of lactose (15–30 g/L) and yeast extract (3 g/L) to emulate the cheese whey, an abundant lactose-rich wastewater. The reactor was operated under controlled conditions with respect to the pH and to the dilution rate. The pH and the dilution rate ranged between 4 and 5, the dilution rate between 0.54 and 2.4 h^?1 (2.5 times the maximum specific growth rate assessed for suspended cells). The optimal performance of the reactor was recorded at a dilution rate of 0.97 h^?1: the butanol productivity was 4.4 g/Lh and the selectivity of solvent in butanol was 88%_w.     

Optimization of a reactor assembly for the production of 6-APA from penicillin-V

The design and operation of an industrial penicillin-V deacylation reactor is simulated, using a kinetic expression and mass transport parameters for the immobilized enzyme particles which were determined experimentally in a previous study. It is desirable to use a series of equalsized plug flow reactors with pH control at the entrance to each reactor, and with a possibility of recycling reactant in each reactor. These measures are necessary to avoid a steep pH profile through the reactor; the deacylation reaction is accompanied by an increase of acidity of the reaction medium, and H(+) is a strong inhibitor and may deactivate the enzyme. The optimization study which is carried out at a fixed penicillin conversion of x = 0.99 shows that it is uneconomical to use penicillin feed concentrations above 150mM-175mM, and that the buffer concentration in the reaction medium should not be less than 50mM-75mM. Increasing the number of reactors from 4 to 8 or 10 leads to higher productivity of 6-APA, and a moderate recycle in the first couple of reactors diminishes the sharp decrease in pH which will be found in a straight plug flow reactor operation of the equipment. Higher pumping costs and lower productivity are unavoidable drawbacks of an operation mode where the separation costs for the product mixture are desired to be low.     

Semiparametric inference for a 2-stage outcome-auxiliary-dependent sampling design with continuous outcome

Two-stage design has long been recognized to be a cost-effective way for conducting biomedical studies. In many trials, auxiliary covariate information may also be available, and it is of interest to exploit these auxiliary data to improve the efficiency of inferences. In this paper, we propose a 2-stage design with continuous outcome where the second-stage data is sampled with an "outcome-auxiliary-dependent sampling" (OADS) scheme. We propose an estimator which is the maximizer for an estimated likelihood function. We show that the proposed estimator is consistent and asymptotically normally distributed. The simulation study indicates that greater study efficiency gains can be achieved under the proposed 2-stage OADS design by utilizing the auxiliary covariate information when compared with other alternative sampling schemes. We illustrate the proposed method by analyzing a data set from an environmental epidemiologic study.     

High efficiency bioethanol production from barley straw using a continuous pretreatment reactor

We developed a new pretreatment process for producing high-efficiency bioethanol from a lignocellulosic biomass. Barley straw was pretreated with sodium hydroxide in a twin-screw extruder for continuous pretreatment. The biomass to ethanol ratio (BTER) for optimal pretreatment conditions was evaluated by response surface methodology. Simultaneous saccharification and fermentation (SSF) was conducted to investigate the BTER with 30 FPU/g cellulose of enzyme and 7% (v/v) yeast (Saccharomyces cerevisiae CHY 1011) using 10% (w/v) pretreated biomass under various pretreatment conditions. The maximum BTER was 73.00% under optimal pretreatment conditions (86.61 °C, 0.58 M, and 84.79 mL/min for temperature, sodium hydroxide concentration, and solution flow rate, respectively) and the experimental BTER was 70.01 ± 0.59%. SSF was performed to investigate the optimal enzyme and biomass dosage. As a result, maximum ethanol concentration and ethanol yield were 46.00 g/L and 77.36% at a loading pretreated biomass of 20% with 30 FPU/g cellulose of the enzyme dosage for barley straw to bioethanol. These results are a significant contribution to the production of bioethanol from barley straw.     

Performance of a cutinase membrane reactor for the production of biodiesel in organic media

The enzymatic transesterification of oils with an alcohol, using recombinant cutinase of Fusarium solani pisi microencapsulated in sodium bis(2-ethylhexyl) sulfosuccinate (AOT)/isooctane reversed micelles, was performed in a membrane bioreactor (MBR). A tubular ceramic membrane with a nominal molecular weight cut off of 15,000 Da was used to retain the enzyme, and characterized in terms of rejection coefficients of the reaction components by transmission experiments. The performance of the MBR in a total recirculation-batch mode was compared with results obtained in a stirred batch tank reactor. The continuous operation of the MBR was also evaluated and the influence of the alcohol type and permeate flow rate on conversion degree and productivity (up to 500 g(product) /day/g(enzyme) was attained) were analyzed. Cutinase wild type and mutant T179C were tested for this process and the high long-term operational stability of the cutinase mutant demonstrated its potential as biocatalyst for the enzymatic continuous production of biodiesel.     

Application of polyethylene glycol immobilized Clostridium sp. LS2 for continuous hydrogen production from palm oil mill effluent in upflow anaerobic sludge blanket reactor

A novel polyethylene glycol (PEG) gel was fabricated and used as a carrier to immobilize Clostridium sp. LS2 for continuous hydrogen production in an upflow anaerobic sludge blanket (UASB) reactor. Palm oil mill effluent (POME) was used as the substrate carbon source. The optimal amount of PEG-immobilized cells for anaerobic hydrogen production was 12% (w/v) in the UASB reactor. The UASB reactor containing immobilized cells was operated at varying hydraulic retention times (HRT) that ranged from 24 to 6 h at 3.3 g chemical oxygen demand (COD)/L/h organic loading rate (OLR), or at OLRs that ranged from 1.6 to 6.6 at 12 h HRT. The best volumetric hydrogen production rate of 336 mL H₂/L/h (or 15.0 mmol/L/h) with a hydrogen yield of 0.35 L H₂/g COD_removed was obtained at a HRT of 12 h and an OLR of 5.0 g COD/L/h. The average hydrogen content of biogas and COD reduction were 52% and 62%, respectively. The major soluble metabolites during hydrogen fermentation were butyric acid followed by acetic acid. It is concluded that the PEG-immobilized cell system developed in this work has great potential for continuous hydrogen production from real wastewater (POME) using the UASB reactor.     

Partial linear inference for a 2-stage outcome-dependent sampling design with a continuous outcome

The outcome-dependent sampling (ODS) design, which allows observation of exposure variable to depend on the outcome, has been shown to be cost efficient. In this article, we propose a new statistical inference method, an estimated penalized likelihood method, for a partial linear model in the setting of a 2-stage ODS with a continuous outcome. We develop the asymptotic properties and conduct simulation studies to demonstrate the performance of the proposed estimator. A real environmental study data set is used to illustrate the proposed method.     

Horizontal reactor for the continuous production of ethanol by yeasts immobilized in pectin

Summary Yeast cells (Saccharomyces cerevisiae) were immobilized in pectin gel, incubated 12 h at 30°C and then used for the continuous production of ethanol employing a wedge-shaped horizontal reactor and sugar cane molasses as the carbon source. Under steady state conditions the mean residence time was 1.6 h and the volumetric productivity 40 g EtOH/hl. The gas evolved was easily released. Successive batch incubation in a synthetic medium substantially restored the fermentative capacity of the beads already used in the continuous assay.Departamento de Biotecnología y Bioingeniería, Centro de Investigación y de Estudios Avanzados del IPN, México D.F.Member of the Scientific Researcher's Career of the Consejo Nacional de Investigaciones Científicas y Técnicas (CONICET), Argentina.     

Improvement in the bioreactor specific productivity by coupling continuous reactor with repeated fed-batch reactor for acetone-butanol-ethanol production

In comparison to the different fermentation modes for the production of acetone, butanol and ethanol (ABE) researched to date, the continuous fermentation is the most economically favored. Continuous fermentation with two or more reactor cascade is reported to be the most efficient as it results in a more stable solvent production process. In this work, it is shown that a continuous (first-stage) reactor coupled to a repeated fed-batch (second stage) is superior to batch and fed-batch fermentations, including two-stage continuous fermentation. This is due to the efficient catalyst use, reported through the specific product rate and rapid glucose consumption rate. High solvents are produced at 19.4 g(ABE) l?1, with volumetric productivities of 0.92 g(butanol) l?1 h?1 and 1.47 g(ABE) l ?1 h?1. The bioreactor specific productivities of 0.62 and 0.39 g g?1(cdw) h?1 obtained show a high catalyst activity. This new process mode has not been reported before in the development of ABE fermentation and it shows great potential and superiority to the existing fermentation methods.     

Immobilized salt-tolerant yeasts: application of a new polyethylene-oxide support in a continuous stirred-tank reactor for flavour production

Immobilization of salt-tolerant yeasts considerably decreases the total time required for the flavour development in soy-sauce processes. For immobilization of cells, alginate gel is mostly used as support material. However, alginate is not very suitable for use in soy-sauce processes because alginate is sensitive to abrasion and chemically unstable towards the high salt content of the soy-sauce medium. In contrast, a newly developed polyethylene-oxide gel seems to be more suitable, but this gel has not been used so far for flavour production in a bioreactor with a high salt content. Therefore, this gel was applied with immobilized salt-tolerant yeasts in a continuous stirred-tank reactor, containing more than 12.5% (w/v) salt. In this reactor, the polyethylene-oxide gel particles did not show any abrasion for several days, while alginate gel beads were already destroyed within 1 day. In addition, the polyethylene-oxide gel particles with immobilized salt-tolerant yeasts Candida versatilis and Zygosaccharomyces rouxii showed a good flavour production. From this work, it was concluded that the application of polyethylene-oxide gel in long-term soy-sauce processes is attractive in the case the sticking together of polyethylene-oxide gel particles can be controlled.     

Continuous production of monoacylglycerols from palm olein in packed-bed reactor with immobilized lipase PS

A packed-bed reactor (PBR) system using immobilized lipase PS as biocatalyst was developed for continuous monoacylglycerols (MAG) production. The condition for continuous MAG production using immobilized lipase PS (IM-PS) of 1.5 g (550 U) in PBR (0.68 cm i.d., 25 cm long) was optimized. The effect of molar ratio of glycerol to palm olein, water content in glycerol and residence time on MAG production was investigated. The optimal glycerol to palm olein molar ratio and water content in glycerol were 12:1 and 10% (w/w), respectively. The yield of MAG increased with increasing residence time. At a residence time of 7.5 h gave the highest yield of MAG of 60%. The long-term operation gave the highest yield of MAG 61.5% at 24 h of the operation time with the productivity of 1.61 g MAG/day. A half-life of the long-term process was 35 days of the operation time with the productivity of 0.81 g MAG/day. Furthermore, the large scale of MAG production was performed continuously with IM-PS of 15 g (5500 U) in PBR (1.5 cm i.d., 50 cm long). The highest yield of MAG in large-scale operation of 70.1% and the 11-fold increasing in productivity of 18.3 g MAG/day were obtained at 24 h of the operation time.     

Integrated thermophilic enzyme-immobilized reactor and high-rate biological reactors for treatment of palm oil-containing wastewater without sludge production

Bioprocess and Biosystems Engineering - Bacillus pumilus, the thermophilic microorganism, was used to biosynthesise lipase of specific activity 5173 U. The purified lipase was highly stable in the...     

Process development of continuous hydrogen production by Enterobacter aerogenes in a packed column reactor

Hydrogen bioproduction from agro-industrial residues by Enterobacter aerogenes in a continuous packed column has been investigated and a complete reactor characterization is presented. Experimental runs carried out at different residence time, liable of interest for industrial application, showed hydrogen yields ranging from 1.36 to 3.02 mmol_H2mmol^у_glucose or, in other words, from 37.5% to 75% of the theoretical hydrogen yield. A simple kinetic model of cell growth, validated by experimental results and allowing the prediction of biomass concentration profile along the reactor and the optimization of superficial velocity, is suggested. By applying the developed approach to the selected operative conditions, the identification of the optimum superficial velocity v_0,opt of about 2.2 cm h^у corresponding to the maximum hydrogen evolution rate H£_2g,max, was performed.     

Performance of a two-stage fermentor with cell recycle for continuous production of lactic acid

The performasnce of a recycle two-stage fermentor with cell separators after each stage is analyzed numerically for continuous production of lactic acid. In this system, the bleed broth withdrawn from the first stage is provided to the second fermentor to reuse viable cells in the bleed. Biological rate expressions and parametric values are taken from the literature. The effects of operating parameters on the concentrations of total and viable cells, substrate and product in each stage, the lactic acid productivity and the substrate conversion are examined and discussed. With respect to overall productivity and conversion, it is found that the present fermentor system is more efficient than a conventional chemostat fermentor with cell recycle.     

Effect of catalyst additives on the production of biofuels from palm oil cracking in a transport riser reactor

Catalytic cracking of crude palm oil (CPO) and used palm oil (UPO) were studied in a transport riser reactor for the production of biofuels at a reaction temperature of 450 °C, with residence time of 20 s and catalyst-to-oil ratio (CTO) of 5 g g^?1. The effect of HZSM-5 (differrent Si/Al ratios), beta zeolite, SBA-15 and AlSBA-15 were studied as physically mixed additives with cracking catalyst Rare earth-Y (REY). REY catalyst alone gave 75.8 wt% conversion with 34.5 wt% of gasoline fraction yield using CPO, whereas with UPO, the conversion was 70.9 wt% with gasoline fraction yield of 33.0 wt%. HZSM-5, beta zeolite, SBA-15 and AlSBA-15 as additives with REY increased the conversion and the yield of organic liquid product. The transport riser reactor can be used for the continuous production of biofuels from cracking of CPO and UPO over REY catalyst.     

Sucrose biotransformation by immobilized Phaffia rhodozyma and continuous neokestose production in a packed-bed reactor

The effects of important production variables on the biotransformation of sucrose by immobilized cells of Phaffia rhodozyma were investigated. Cell concentration had negative effect on the maximum concentration of neokestose and the optimal concentration was 16?g/l (calculated by dry weight). The concentration of sucrose had a positive effect on the maximum concentration of neokestose within 1.170?mol/l. Elevating the reaction temperature increased the reaction rate but decreased the maximum concentration of neokestose. Sugar cane juice could be used as an inexpensive substrate for neokestose production. Additionally, a 30-d continuous neokestose production was found feasible in a packed bed reactor, indicating that the cell immobilization with chitosan-coated alginate has the potential for industrial production.     

Study of a reactor model for enzymatic reactions in continuous mode coupled to an ultrasound bath for esters production

Bioprocess and Biosystems Engineering - The main objective of this work was to investigate the enzymatic production of ethyl esters in continuous mode coupled to an ultrasound bath. For...