A study on enzymatic reaction using a liquid emulsion membrane technique

An enzymatic reaction using a liquid emulsion membrane technique was studied to investigate the effects of some experimental variables on the stability of liquid membrane, enzyme deactivation, and transport of substrates and products. The hydrolysis of L-phenylalanine methyl ester by alpha-chymotrypsin was selected as a model reaction system. First, a transport mechanism for the substrates and products across the membrane was qualitatively identified. Second, it was found that the pH of the internal phase was one of the most important variables to determine the enzyme activity in a liquid membrane. Third, the effect of membrane phase which consists of surfactant, carrier, and organic solvent on the emulsion stability was investigated. It was found that the properties of the organic solvents greatly affect the emulsion stability. For an optimum condition, it was possible to reuse the emulsion which consists of membrane phase and internal phase without further separation. It was finally concluded that the enzyme in a liquid membrane retained 60% of its native activity in spite of vigorous mixing during the emulsification step.     

Optical bio-sniffer for ethanol vapor using an oxygen-sensitive optical fiber

An optical bio-sniffer for ethanol was constructed by immobilizing alcohol oxidase (AOD) onto a tip of a fiber optic oxygen sensor with a tube-ring, using an oxygen sensitive ruthenium organic complex (excitation, 470 nm; fluorescent, 600 nm). A reaction unit for circulating buffer solution was applied to the tip of the device. After the experiment in the liquid phase, the sniffer-device was applied for gas analysis using a gas flow measurement system with a gas generator. The optical device was applied to detect the oxygen consumption induced by AOD enzymatic reaction with alcohol application. The sensor in the liquid phase was used to measure ethanol solution from 0.50 to 9.09 mmol/l. Then, the bio-sniffer was calibrated against ethanol vapor from 0.71 to 51.49 ppm with good gas-selectivity based on the AOD substrate specificity. The bio-sniffer with the reaction unit was also used to monitor the concentration change of gaseous ethanol by rinsing and cleaning the fiber tip and the enzyme membrane with buffer solution.     

Continuous production of isovaleraldehyde through extractive bioconversion in a hollow-fiber membrane bioreactor

A membrane bioreactor was developed to perform an extractive bioconversion aimed at the production of isovaleraldehyde by isoamyl alcohol oxidation with whole cells of Gluconobacter oxydans. A liquid/liquid extractive system using isooctane as extractant and assisted by a hollow-fiber hydrophobic membrane was chosen to recover the product. The aqueous bioconversion phase and the organic phase were maintained apart with the aid of the membrane. The extraction of alcohol and aldehyde was evaluated by performing equilibrium and mass transfer kinetic studies. The bioprocess was then performed in a continuous mode with addition of the substrate to the aqueous phase. Fresh solvent was added to the organic phase and exhausted solvent was removed at the same flow rate. The extractive system enabled a fast and selective in situ removal of the aldehyde from the water to the organic phase. High conversions (72–90%) and overall productivity (2.0–3.0 g l⁻¹ h⁻¹) were obtained in continuous experiments performed with different rates of alcohol addition (1.5–3.5 g l⁻¹ h⁻¹). Cell deactivation was observed after 10–12 h of operation.     

A multiphasic hollow fiber reactor for the whole-cell bioconversion of 2-methyl-1,3-propanediol to (r)-beta-hydroxyisobutyric acid

This paper describes the bioconversion of 2-methyl-1,3-propanediol to (R)-beta-hydoxyisobutyric acid (HIBA) by Acetobacter ALEI in a hollow fiber membrane bioreaction system arrangement that allows the integration of three liquid phases: the aqueous bioconversion phase, the organic phase consisting of a solution of trioctyl phosphine oxide (TOPO) in isooctane, and the third phase consisting of a basic stripping solution that allows reextraction of HIBA from the organic phase. A comparison of HIBA mass transfer experiments was carried out in the membrane reactor with two and three phases for different pH and TOPO concentrations. The use of the three-phase arrangement allows the extraction of high quantities of HIBA from the aqueous medium (higher than 85%) independently of the pH, whereas in the two-phase system the percentage of HIBA extracted from the aqueous medium was lower, 42% in the best case, and strongly influenced by the pH. The percentage of the extractive agent TOPO in the organic phase influenced on the mass transfer rate in both bi- and triphasic arrangements. By simply integrating the re-extraction phase in the system it was possible to increase the extraction yield by 2-fold, reduce the amount of TOPO by 4-fold, and operate at the more favorable pH 4. A bioconversion experiment was done in these conditions (pH = 4, TOPO = 5%) to confirm the advantages of including the third stripping solution. Fed-batch operation of the triphasic membrane reactor was maintained for more than 20 h, reaching an HIBA concentration in the stripping solution of 29 g L(-)(1).     

Epoxidation of 1,7‐octadiene by Pseudomonas oleovorans in a membrane bioreactor

A growing cell culture of Pseudomonas oleovorans was used to biotransform 1,7‐octadiene to 1,2‐epoxy‐7,8‐octene in a continuous‐flow bioreactor with an external membrane module. A dense silicone rubber membrane was used to contact an organic phase, containing both the reactant (1,7‐octadiene) and the growth substrate (heptane), with an aqueous biomedium phase containing the biocatalyst. Heptane and octadiene delivery to the aqueous phase, and epoxide extraction into the solvent, occurred by diffusion across the dense membrane under a concentration‐driving force. In addition, a liquid feed of heptane and octadiene was pumped directly into the bioreactor to increase the rate of delivery of these compounds to the aqueous phase. In this system 1,2‐epoxy‐7,8‐octene accumulated in a pure solvent phase, thus, product recovery problems associated with emulsion formation were avoided. Furthermore, no phase breakthrough of either liquid across the membrane was observed. In this system, the highest volumetric productivity obtained was 30 U.L⁻¹, and this was achieved at a dilution rate of 0.07 h⁻¹, 70 m².m⁻³ of membrane area, and a steady‐state biomass concentration of 2.5 g.L⁻¹. The system was stable for over 1250 h. Decreasing the dilution rate led to an increased biomass concentration, however, the specific activity was significantly reduced, and therefore, an optimal dilution rate was determined at 0.055 h⁻¹. © 1999 John Wiley & Sons, Inc. Biotechnol Bioeng 63: 601–611, 1999.     

Effect of beta-galactosidase hydration on alcoholysis reaction in organic one-phase liquid systems

Alcoholysis reactions were performed in organic one-phase liquid systems with E. coli beta-galactosidase to produce heptyl-beta-galactoside from lactose and 1-heptanol. The reaction rate was highly dependent on the amount of water solubilized in the alcohol. A larger amount of water led to a system of two liquid phases in which the alcoholysis rate was 73% faster than in the one-phase system. No hydrolysis reaction of either lactose or product was observed in one-phase liquid systems up to 20 h, independent of the water content. Solubility of lactose in the organic phase increased with the water content in the system and the reaction followed the Michaelis-Menten model. Water activity was calculated for heptanol containing different amounts of water and the obtained values were used to estimate the hydration of beta-galactosidase from known models. Enzyme activity correlated with sorbed water, similar to the behavior reported for lysozyme in low water environments. It is concluded that water contribution to enzyme hydration dominates the rate of reaction compared to its effect on lactose solubilization.     

Kinetically controlled synthesis of ampicillin and cephalexin in highly condensed systems in the absence of a liquid aqueous phase

Advantages of performing penicillin G amidase catalysed synthesis of ampicillin and cephalexin by enzymatic acyl transfer to the β-lactam antibiotic nuclei in a highly condensed system using mainly undissolved substrates, with no apparent aqueous liquid phase, were demonstrated. It was shown that synthesis can be performed in the absence of a liquid phase formed by water or an organic co-solvent. This highly condensed system is formed by a liquid phase given by one of the reactant, the phenylglycine methyl ester (PGM), that remains liquid in these operative conditions and the partially dissolved β-lactam nucleus. Operating in such highly condensed system, the water that causes the hydrolysis of PGM is limited to the water hydrating the support on which the enzyme is covalently immobilised. In this way the reaction system is maintained at a controlled degree of hydration.

In the present work the reaction system was modulated by eliminating the solvent (aqueous or aqueous/organic), reducing the amount of water to the minimum for the biocatalytic activity and using PGM as solvent and reagent at the same time. The synthesis was conducted with equimolar amounts of PGM and the β-lactam nucleus, with a reduced hydrolysis of the activated acyl donor. We have also studied a simple and efficient method for the workup of the reaction where the unreacted reagents can be recovered after selective filtration and precipitation.     

Reaction rate with suspended lipase catalyst shows similar dependence on water activity in different organic solvents.

We have studied the effect of thermodynamic water activity (a W) on the initial rate of esterification catalysed by an immobilised lipase (Lipozyme) suspended in an organic reaction mixture. The catalyst and the organic phase were separately pre-equilibrated to the same aw value. The rate shows similar dependence on aw in reaction mixtures based on five different organic solvents ranging in polarity from pentan-3-one to hexane, and in a liquid reactant mixture. There is a maximum at aw about 0.5, with a decline to 30-70% at aw of either 0.9 or less than 0.01. When the rates are presented in terms of water concentration in the organic phase (or total water content of the system), the maxima for the various solvents come at very different positions, reflecting the widely varying solubilities of water in the organic phase.     

Use of stable emulsion to improve stability, activity, and enantioselectivity of lipase immobilized in a membrane reactor

The enantiocatalytic performance of immobilized lipase in an emulsion membrane reactor using stable emulsion prepared by membrane emulsification technology was studied. The production of optical pure (S)-naproxen from racemic naproxen methyl ester was used as a model reaction system. The O/W emulsion, containing the substrate in the organic phase, was fed to the enzyme membrane reactor from shell-to-lumen. The enzyme was immobilized in the sponge layer (shell side) of capillary polyamide membrane with 50 kDa cut-off. The aqueous phase was able to permeate through the membrane while the microemulsion was retained by the thin selective layer. Therefore, the substrate was kept in the enzyme-loaded membrane while the water-soluble product was continuously removed from the reaction site. The results show that lipase maintained stable activity during the entire operation time (more than 250 h), showing an enantiomeric excess (96 +/- 2%) comparable to the free enzyme (98 +/- 1%) and much higher compared to similar lipase-loaded membrane reactors used in two-separate phase systems (90%). The results demonstrate that immobilized enzymes can achieve high stability as well as high catalytic activity and enantioselectivity.     

Three different examples of enzymatic bioconversion in liquid membrane reactors

Three different examples of enzyme emulsions are presented. The enzymes are immobilized in liquid surfactant membranes. The effect of the organic membrane phase is discussed as well as the influence of the membrane composition on the transport of substrates and products through the membrane. An enzyme emulsion system for the production of l-leucine with continuous co-factor regeneration is described. It is not necessary to increase the molecular weight of the co-factor by linking it to a soluble high molecular weight compound (e.g., PEG), since the coenzyme cannot pass the liquid membrane without a suitable carrier. Also, a product (6-APA) can be enriched in the internal phase of the liquid membrane. The separation effect is not based on differences in molecular weight, but on the chemical behavior of the substances to be separated.     

Technical aspects of separation and simultaneous enzymatic reaction in multiphase enzyme membrane reactors

The technical aspects of the membrane extraction of a compound either from aqueous phase into apolar organic solvent phase or from the apolar phase to the aqueous one and the enzymatic conversion of the solute in a multiphase enzyme membrane reactor are considered. The application possibilities, the selection aspects of membrane material as well as the solvent phase, the water content and its control, the method of the enzyme immobilisation and the operation of the extraction/reaction system are discussed.     

Dynamic interactions between enzyme activity and the microstructured environment

A new approach for the study of an enzyme's relationship with its own reaction medium has been developed. One technique of micellar enzymology is the use of pseudohomogeneous systems composed of surfactant/water/organic solvent. In such systems, the physicochemical properties and textures of the medium depend on the relative ratios of the different components. Enzymes are catalytically active in such systems and up to the present have been studied in different microenvironments, such as micelles, microemulsions and lyotropic liquid crystals. Our purpose was to develop a system in which the enzyme could, by its activity, modify one of the components in such a way that the relative ratios among them changed sufficiently to produce a transition from one phase domain to another. The three components, water (or glucose in water), octanol and octyl-beta-D-glucoside, form a classical ternary water/oil/surfactant system. The relevant phase diagram shows different macroheterogeneous phases and microstructured domains. The enzyme beta-D-glucosidase hydrolyses octyl-beta-D-glucoside to form glucose and octanol. The enzyme was found to change the relative ratios of water (or glucose in water), octanol and octyl-beta-D-glucoside in such a manner that the physicochemical structure of the medium was modified. At the beginning of the reaction beta-D-glucosidase was present in a micellar solution of octyl-beta-D-glucoside in water. As the enzymatic reaction proceeded, the medium became biphasic. One of the two phases was the micellar solution of octyl beta-D-glucoside in water, while the other phase was either a microemulsion or a liquid crystalline phase. In addition the enzyme, through its catalytic activity, was able to modify the physiocochemical properties of the reaction medium.     

Enzymatic resolution of (S)-(+)-naproxen in a trapped aqueous-organic solvent biphase continuous reactor

A trapped aqueous-organic biphase system for the continuous production of (S)-(+)-2-(6-methoxy-2-naphthyl) propionic acid (Naproxen) has been developed. The process consists of a stereoselective hydrolysis of the racemic Naproxen methyl ester by Candida rugosa lipase in a trapped aqueous-organic biphase system. The reaction has been carried out in a laboratory-scale continuous-flow stirred tank reactor (CSTR). The staring material has been supplied in and remaining substrate recovered by organic phase. YWG-C(6)H(5), a poorly polar synthetic support, has been employed to immobilize the lipase and to restrict the aqueous phase. Lipase immobilized on YWG-C(6)H(5) containing aqueous phase has been added into the CSTR to catalyze the hydrolysis. A dialysis membrane tube containing a continuous flow closed-loop buffer has been applied in the CSTR for the extraction of product and recruiting of the aqueous part consumed. Various reaction conditions have been studied. The activity of immobilized enzyme was effected by the polarity of support, the substrate concentration, logP value of organic phase and the product inhibition. At steady-state operating conditions, an initial conversion of 35% has been obtained. The CSTR was allowed to operate continuously for 60 days at 30 degrees C with a 30% loss of activity. The hydrolysis reaction yielded (S)-(+)-Naproxen with >90% enantiomeric excess and overall conversion of 30%.     

Simultaneous extraction and concentration of penicillin G by hollow fiber renewal liquid membrane

In this article, hollow fiber renewal liquid membrane (HFRLM) technique was used for recovery of penicillin G from aqueous solution. The organic solution of 7 vol % di‐n‐octylamine (DOA) + 30 vol % iso‐octanol + kerosene was used as liquid membrane phase, and Na₂CO₃ aqueous solution was used as stripping phase. Experiments were performed as a function of carrier concentration in the organic phase, organic/aqueous volume ratio, pH, and initial penicillin G concentration in the feed phase, pH in the stripping phase, flow rates, etc. The results showed that the HFRLM process was stable and could carry out simultaneous extraction and concentration of penicillin G from aqueous solutions. As a carrier facilitated transport process, the addition of DOA in organic phase could greatly enhance the mass transfer rate; and there was a favorable organic/aqueous volume ratio of 1:20 to 1:30 for this system. The mass transfer flux and overall mass transfer coefficient increased with decreasing pH in the feed phase and increasing pH in the stripping phase, because of variation of the mass transfer driving force caused by pH gradient and distribution equilibrium. The flow rate of the shell side had significant influence on the mass transfer performance, whereas the effect of flow rate of lumen side on the mass transfer performance was slight because of the mass transfer intensification of renewal effect in the lumen side. The results indicated that the HFRLM process was a promising method for the recovery of penicillin G from aqueous solutions. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Simplified cysteine dioxygenase activity assay allows simultaneous quantitation of both substrate and product

A high-performance liquid chromatography (HPLC) method for enzyme activity assays using a hydrophilic interaction liquid chromatography (HILIC) column in combination with an evaporative light scattering detector was developed. The method was used to measure the activity of the non-heme mono-iron enzyme cysteine dioxygenase. The substrate cysteine and the product cysteine sulfinic acid are very weak chromophores, making direct ultraviolet (UV) detection without derivatization rather insensitive; moreover, derivatization of cysteine is often not efficient. Using the system described, underivatized substrate and product in samples from cysteine dioxygenase activity assays could be separated and analyzed. Furthermore, it was possible to quantify cysteic acid, the noncatalytic oxidation product of cysteine sulfinic acid. Acetone was used both to stop the enzymatic reaction by protein precipitation and as an organic mobile phase, making sample preparation very easy and the assay highly reproducible.     

Separation and concentration of L-phenylalanine using a supported liquid membrane

The separation and concentration of L-phenylalanine (L-Phe) using a supported liquid membrane (SLM) is investigated. A cation complex agent, di-2-ethylhexyl phosphoric acid (D₂EHPA), is used as a carrier in the SLM with n-Heptane as a solvent. The reaction order and equilibrium constant in the formation reaction of L-Phe-carrier complex are obtained from the extraction experment. A mathematical model for a carrier mediated counter transport process is proposed to estimate the diffusion coefficient of L-Phe-carrier complex in the liquid membrane. Permeation experiments of L-Phe using a SLM are performed under various operating conditions and optimum conditions for the transport of L-Phe are obtained. Concentration of L-Phe in the strip phase against its concentration is observed. Transport rate of glucose through liquid membrane is less than that of L-Phe in the competitive transport of L-Phe and glucose. And the existence of glucose reduced the transport rate of L-Phe. The performance of separation with continuous strip phase is increased due to the dilution effect in the strip phase.     

Two-stage recovery of S-adenosylmethionine using supported liquid membranes with strip dispersion

We report the selective recovery of S-adenosylmethionine (SAM) from fermentation broths using a two-stage supported liquid membrane system with strip dispersion (SLM-SD). The system utilized two MiniModule^® hollow-fiber membrane modules as microporous supports and an organic membrane solution consisting of the extractants of sodium di-2-ethylhexyl sulfosuccinate (AOT), di-(2-ethylhexyl)phosphoric acid (DEHPA), and trioctylphosphine oxide (TOPO) in the solvent n-octanol. SAM was extracted in the first membrane module. Methionine (Met) was captured by the first stripping solution and further purified in the second membrane module. pH values in the feed phase and the first and second stripping solutions, extractant concentrations, NaCl concentration, and the SAM acceptor in the first stripping solution were optimized. Strip dispersion mixing speed, pressure differences across the membranes, and flow rates of the feed and strip dispersion phases were investigated experimentally. The optimal extractant concentrations were: AOT 2.78 wt%, DEHPA 27.0 wt%, and TOPO 1.61 wt%. The optimal pH values in the feed phase and the first and second stripping solution were 3.0, 2.5, and 1.0, respectively. SAM extraction efficiency of 98.7%, SAM recovery efficiency of 91.8% and Met removal efficiency of 85.4% were achieved within 5 h. Finally, the mass transfer analysis indicated that the mass transfer resistances from the extraction reaction and the membrane phase were predominant.     

Competitive lipase-catalyzed ester hydrolysis and ammoniolysis in organic solvents; equilibrium model of a solid-liquid-vapor system.

Enzymatic ester hydrolysis and ammoniolysis were performed as competitive reactions in methyl isobutyl ketone without a separate aqueous phase. The reaction system contained solid ammonium bicarbonate, which dissolved as water, ammonia, and carbon dioxide. During the reaction an organic liquid phase, a vapor phase, and at least one solid phase are present. The overall equilibrium composition of this multiphase system is a complex function of the reaction equilibria and several phase equilibria. To gain a quantitative understanding of this system a mathematical model was developed and evaluated. The model is based on the mass balances for a closed batch system and straightforward relations for the reaction equilibria and the solubility equilibria of ammonium bicarbonate, the fatty acid ammonium salt, water, ammonia, and carbon dioxide. For butyl butyrate as a model ester and Candida antarctica lipase B as the biocatalyst this equilibrium model describes the experiments satisfactorily. The model predicts that high equilibrium yields of butyric acid can be achieved only in the absence of ammoniolysis or in the presence of a separate water phase. However, high yields of butyramide should be possible if the water concentration is fixed at a low level and a more suited source of ammonia is applied.     

An integrated process: ester synthesis in an enzymatic membrane reactor and water sorption

In the case of such reactions as ester synthesis, water is produced during the reaction. Because these reactions are carried out in hydrophobic solvents an additional (water) phase in the system must not be allowed, i.e. the concentration of water saturation in the organic solvent should not be exceeded. In such a case, the reaction kinetics and product equilibrium concentration undergo undesirable changes because of the partition coefficient of the components and hampered process of product separation. Hence, removal of the water produced in the reaction determines whether the process is successful or not. For this purpose, the integrated process with water sorption in the column with molecular sieves was applied. Integration of the process of synthesis and dehydration of a reaction phase, in which a biocatalyst is suspended and not dissolved as in water solutions, requires holding up of the catalyst in the reactor before directing the stream of reaction mixture to dehydration process. This hold-up and a possibility of multiple use of the catalyst may be accomplished by using a separating barrier, e.g. an ultrafiltration membrane or by permanent fixing of the catalyst to the matrix, e.g. a polymeric membrane. The efficiency and activity of a biocatalyst (lipase CAL-B) immobilized on a polymer membrane by sorption and chemical binding, were determined. A subject of study was the synthesis of geranyl acetate, one of the most known aromatic compound. A hydrophobic (polypropylene) matrix was shown to be a much better carrier in the reactions performed in an organic solvent than a hydrophilic (polyamide) membrane being tested. The reaction kinetics of geranyl acetate synthesis with the use of geraniol and acetic acid as substrates, was described by the equation defining the "Ping-Pong Bi Bi" mechanism that was related additionally to the inhibition of a substrate (acetic acid). The following constants of kinetic equation were obtained k(3)(')=0.344 mol g(-1)h(-1), K(mA)=0.257 mol l(-1), K(mG)=1.629 and K(iA)=0.288 for the native enzyme and v(max,Gel)=111.579 mol l(-1)h(-1), K(mA)=0.255 mol l(-1), K(mG)=1.91 mol l(-1), K(iA)=0.238 mol l(-1) for the one immobilized by sorption on a polypropylene membrane. Half-life time of the native enzyme activity was 204 h and stability of the immobilized preparation was 70 h. With respect to the reaction kinetics and stability of the native enzyme and immobilized preparation, from both types of membrane bioreactor more attractive appears to be the one in which the membrane is used not as a catalyst layer but only as a barrier that immobilizes the native enzyme within the bioreactor volume. When an integrated process proceeds, the method to collect water in the sorption column during the process, appeared to work very well. The reaction proceeded with a very high efficiency (after 120 h alpha=98.2% for native enzyme and 83.2% for immobilized enzyme) and due to low water concentration in the system ( approximately 0.000% v/v) the second phase was not created.     

Enzymes in lyotropic liquid crystal — A new method of bioconversion in non-aqueous media

Summary A new method has been developed for the use of enzymes as catalysts in organic solvents. The enzyme and cofactor are entrapped in a lyotropic liquid crystal which is insoluble in an organic solvent. The biocatalyst is significantly stabilized in this biphasic reaction system and product recovery is facilitated.