Improved enzymatic two-phase biotransformation for (R)-phenylacetylcarbinol: Effect of dipropylene glycol and modes of pH control

An octanol/aqueous two-phase process for the enzymatic production of (R)-phenylacetylcarbinol (PAC) has been investigated further with regard to optimal pH control and replacement of 2.5 M MOPS buffer by a low cost solute. The specific rate of PAC production in the 2.5 M MOPS system controlled at pH 7 was 0.60 mg U^-1 h^-1 (reaction completed at 34 h), a 1.6 times improvement over the same 2.5 M MOPS system without pH control (0.39 mg U^-1 h^-1 at 49 h). An improved stability of PDC was evident at the end of biotransformation for the pH-controlled system with 84% residual carboligase activity, while 23% of enzyme activity remained in the absence of pH control. Lowering the MOPS concentration to 20 mM resulted in a lower benzaldehyde concentration in the aqueous phase with a major increase in the formation of by-product acetoin and three times decreased PAC production (0.21 mg U^-1 h^-1). Biotransformation with 20 mM MOPS and 2.5 M DPG as inexpensive replacement of high MOPS concentrations provided similar aqueous phase benzaldehyde concentrations compared to 2.5 M MOPS and resulted in a comparable PAC concentration (92.1 g L^-1 in the total reaction volume in 47 h) with modest formation of acetoin.     

Improved enzymatic two-phase biotransformation for (R)-phenylacetylcarbinol: Effect of dipropylene glycol and modes of pH control

An octanol/aqueous two-phase process for the enzymatic production of (R)-phenylacetylcarbinol (PAC) has been investigated further with regard to optimal pH control and replacement of 2.5?M MOPS buffer by a low cost solute. The specific rate of PAC production in the 2.5?M MOPS system controlled at pH?7 was 0.60?mg?U^?1?h^?1 (reaction completed at 34?h), a 1.6 times improvement over the same 2.5?M MOPS system without pH control (0.39?mg?U^?1?h^?1 at 49?h). An improved stability of PDC was evident at the end of biotransformation for the pH-controlled system with 84% residual carboligase activity, while 23% of enzyme activity remained in the absence of pH control. Lowering the MOPS concentration to 20?mM resulted in a lower benzaldehyde concentration in the aqueous phase with a major increase in the formation of by-product acetoin and three times decreased PAC production (0.21?mg?U^?1?h^?1). Biotransformation with 20?mM MOPS and 2.5?M DPG as inexpensive replacement of high MOPS concentrations provided similar aqueous phase benzaldehyde concentrations compared to 2.5?M MOPS and resulted in a comparable PAC concentration (92.1?g?L^?1 in the total reaction volume in 47?h) with modest formation of acetoin.     

Increased pyruvate efficiency in enzymatic production of (R)-phenylacetylcarbinol

Loss of substrate, pyruvate, a limitation for enzymatic batch production of (R)-phenylacetylcarbinol (PAC), resulted from two phenomena: temperature dependent non-enzymatic concentration decrease due to the cofactor Mg²⁺ and formation of by-products, acetaldehyde and acetoin, by pyruvate decarboxylase (PDC). In the absence of enzyme, pyruvate stabilization was achieved by lowering the Mg²⁺ concentration from 20 to 0.5 mM. With 0.5 mM Mg²⁺ Rhizopus javanicus and Candida utilis PDC produced similar levels of PAC (49 and 51 g l^–1, respectively) in 21 h at 6 °C; however C. utilis PDC formed less by-product from pyruvate and was more stable during biotransformation. The process enhancements regarding Mg²⁺ concentration and source of PDC resulted in an increase of molar yield (PAC/consumed pyruvate) from 59% (R. javanicus PDC, 20 mM Mg²⁺) to 74% (R. javanicus PDC, 0.5 mM Mg²⁺) to 89% (C. utilis PDC, 0.5 mM Mg²⁺).     

Comparative studies on enzyme preparations and role of cell components for (R)-phenylacetylcarbinol production in a two-phase biotransformation

Whole cell pyruvate decarboxylase (PDC) from Candida utilis enhanced the enzymatic production of (R)-phenylacetylcarbinol (PAC) in an aqueous/octanol biotransformation compared to the partially purified PDC especially for a lower range of initial activities (0.3-2.5 U/mL). With an initial activity of 1.1 U/mL and at a 1:1 phase volume ratio, whole cell PDC achieved a maximum specific PAC production of 42 mg/U (2.8 g/L/h) in comparison to 13 mg/U (0.9 g/L/h) for partially purified PDC. The enhanced performance of whole cell PDC was associated with high stability towards the substrate benzaldehyde. The strong PDC inactivation by benzaldehyde was minimal even when whole cells were broken as long as cell debris was not removed from the broken cells. Biotransformations with various cellular components added to partially purified PDC revealed that membrane components especially 2 mg/mL phosphatidylcholine enhanced PAC concentrations. The role of surfactants was further confirmed from the results with synthetic surfactant sodium bis(2-ethyl-1-hexyl)sulfosuccinate (AOT). It was apparent that the membrane components in whole cells were sufficient for optimal PAC production and no further surfactant addition is required for optimal performance.     

Enzymatic (R)-phenylacetylcarbinol production in benzaldehyde emulsions

(R)-Phenylacetylcarbinol [(R)-PAC)] is the chiral precursor for the production of the pharmaceuticals ephedrine and pseudoephedrine. Reaction conditions were improved to achieve increased (R)-PAC levels in a simple batch biotransformation of benzaldehyde emulsions and pyruvate, using partially purified pyruvate decarboxylase (PDC) from the filamentous fungus Rhizopus javanicus NRRL 13161 as the catalyst. Lowering the temperature from 23 degrees C to 6 degrees C decreased initial rates but increased final (R)-PAC concentrations. Addition of ethanol, which increases benzaldehyde solubility, was not beneficial for (R)-PAC production. It was established that proton uptake during biotransformation increases the pH above 7 thereby limiting (R)-PAC production. For small-scale studies, biotransformations were buffered with 2-2.5 M MOPS (initial pH 6.5). High concentrations of MOPS as well as some alcohols and KCl stabilised PDC. A balance between PDC and substrate concentrations was determined with regards to ( R)-PAC production and yields on enzyme and substrates. R. javanicus PDC (7.4 U/ml) produced 50.6 g/l (337 mM) ( R)-PAC in 29 h at 6 degrees C with initial 400 mM benzaldehyde and 600 mM pyruvate. Molar yields on consumed benzaldehyde and pyruvate were 97% and 59%, respectively, with 17% pyruvate degraded and 24% converted into acetaldehyde and acetoin; 43% PDC activity remained, indicating reasonable enzyme stability at high substrate and product concentrations.     

Screening of yeasts for cell-free production of (R)-phenylacetylcarbinol

105 yeast strains from 10 genera and 40 species were evaluated for cell-free production of (R)-phenylacetylcarbinol (PAC), the chiral precursor in the manufacture of the pharmaceuticals ephedrine and pseudoephedrine. Carboligase activity of pyruvate decarboxylase (PDC), forming PAC from benzaldehyde and pyruvate, was found in extracts of 98 strains. PAC was not formed from benzaldehyde and acetaldehyde, an activity of bacterial PDCs from Zymomonas mobilis and Zymobacter palmae. Two interesting groups of candidates were identified in the yeast screening: carboligase activities of Schizosaccharomyces pombe PDCs were very low but showed best resistance to pre-incubation with acetaldehyde and benzaldehyde; and highest carboligase activities combined with medium resistance were found in strains of Candida utilis, C. tropicalis and C. albicans.     

Biotransformation of benzaldehyde into (R)-phenylacetylcarbinol by filamentous fungi or their extracts

Extracts of 14 filamentous fungi were examined regarding their potential for production of (R)-phenylacetylcarbinol [(R)-PAC], which is the chiral precursor in the manufacture of the pharmaceuticals ephedrine and pseudoephedrine. Benzaldehyde and pyruvate were transformed at a scale of 1.2 ml into PAC by cell-free extracts of all selected strains, covering the broad taxonomic spectrum of Ascomycota, Zygomycota and Basidiomycota. Highest final PAC concentrations were obtained with the extracts of Rhizopus javanicus and Fusarium sp. [78-84 mM (11.7-12.6 g/l) PAC within 20 h from initial substrate concentrations of 100 mM benzaldehyde and 150 mM pyruvate]. (R)-PAC was in about 90-93% enantiomeric excess. Rhizopus javanicus had the advantage of faster growth than Fusarium sp. Rhizopus javanicus mycelia were used as an example in a biotransformation process based on whole cells and benzaldehyde and glucose as substrates. The substrate pyruvate was generated through the fungal fermentation of glucose. Only 19 mM PAC (2.9 g/l) were produced within 8 h from 80 mM benzaldehyde. with evidence of significant benzyl alcohol production.     

Comparison of a batch, fed-batch and continuously operated stirred-tank reactor for the enzymatic synthesis of (R)-mandelonitrile by using a process model

The suitability of a batch, fed-batch and continuously operated stirred-tank reactor for the enzymatic production of (R)-mandelonitrile in an aqueous-organic biphasic system was investigated by using a process model. The considered biphasic system is 10-50% (v/v) 100 mM sodium citrate buffer of pH 5.5 dispersed in methyl tert-butyl ether. The constraints were that 750 moles of benzaldehyde per cubic meter should react towards (R)-mandelonitrile with an enantiomeric excess of 99% and a conversion of 98%. A continuously operated stirred-tank reactor could not meet the constraints, but the production in a batch or fed-batch reactor was feasible. The choice for a batch or fed-batch reactor is dependent on the influence of the costs for reactor operation and for the enzyme on the product costs. The choice for operating at a small or large aqueous-phase volume fraction is dependent on the costs and reusability of the enzyme. The volumetric productivity is maximal when operating as batch. The enzymatic productivity and turnover are maximal when operating as fed batch. In the fed-batch mode, the enzymatic productivity increased by 24-37%, the turnover increased by 50-60% and the volumetric productivity decreased by 33-71% as compared to a batch reactor. By enhancement of mass transfer both the volumetric and enzymatic productivity can be increased considerably, while the turnover is only slightly decreased.     

Yeast pyruvate decarboxylases: variation in biocatalytic characteristics for (R)-phenylacetylcarbinol production

Based on previous studies, Candida utilis pyruvate decarboxylase (PDC) proved to be a stable and high productivity enzyme for the production (R)-phenylacetylcarbinol (PAC), a pharmaceutical precursor. However, a portion of the substrate pyruvate was lost to by-product formation. To identify a source of PDC which might overcome this problem, strains of four yeasts -- C. utilis, Candida tropicalis, Saccharomyces cerevisiae and Kluyveromyces marxianus -- were investigated for their PDC biocatalytic properties. Biotransformations were conducted with benzaldehyde and pyruvate as substrates and three experimental systems were employed (in the order of increasing benzaldehyde concentrations): (I) aqueous (soluble benzaldehyde), (II) aqueous/benzaldehyde emulsion, and (III) aqueous/octanol-benzaldehyde emulsion. Although C. utilis PDC resulted in the highest concentrations of PAC and was the most stable enzyme, C. tropicalis PDC was associated with the lowest acetoin formation. For example, in system (III) the ratio of PAC over acetoin was 35 g g(-1) for C. tropicalis PDC and 9.2 g g(-1) for C. utilis PDC. The study thereby opens up the potential to design a PDC with both high productivity and high yield characteristics.     

Kinetic analysis and modelling of streptokinase fermentation

The kinetics based on the MONOD conception of anaerobic, discontinuous, isothermal, isobaric fermentation producing a special protein in secondary metabolism is studied. The kinetic analysis results in a growth limitation by the primary product which shows a sigmoidal behaviour, a lineary correlation between the specific substrate degradation and the specific rate of formation lactic acid and a lineary correlation in a good approximation between the formation of proteins and substrate degradation. In this study a process model with coupled differential equations is provided. Kinetic and stoichiometric coefficients are determined.     

Enzymatic (R)-phenylacetylcarbinol production in a benzaldehyde emulsion system with Candida utilis cells

Recent progress in enzymatic (R)-phenylacetylcarbinol (PAC) production has established the need for low cost and efficient biocatalyst preparation. Pyruvate decarboxylase (PDC) added in the form of Candida utilis cells showed higher stability towards benzaldehyde and temperature in comparison with partially purified preparations. In the presence of 50 mM benzaldehyde and at 4°C, a half-life of 228 h was estimated for PDC added as C. utilis cells, in comparison with 24 h for the partially purified preparation. Increasing the temperature from 4 to 21°C for PAC production with C. utilis cells resulted in similar final PAC levels of 39 and 43 g l⁻¹ (258 and 289 mM), respectively, from initial 300 mM benzaldehyde and 364 mM pyruvate. The overall volumetric productivity was enhanced 2.8-fold, which reflected the 60% shorter reaction time at the higher temperature. Enantiomeric excess values of 98 and 94% for R-PAC were obtained at 4 and 21°C, respectively, and benzyl alcohol (a potential by-product from benzaldehyde) was not formed.     

A two-step enzymatic resolution process for large-scale production of (S)- and (R)-ethyl-3-hydroxybutyrate

An efficient two-step enzymatic process for production of (R)- and (S)-ethyl-3-hydroxybutyrate (HEB), two important chiral intermediates for the pharmaceutical market, was developed and scaled-up to a multikilogram scale. Both enantiomers were obtained at 99% chemical purity and over 96% enantiomeric excess, with a total process yield of 73%. The first reaction involved a solvent-free acetylation of racemic HEB with vinylacetate for the production of (S)-HEB. In the second reaction, (R)-enriched ethyl-3-acetoxybutyrate (AEB) was subjected to alcoholysis with ethanol to derive optically pure (R)-HEB. Immobilized Candida antarctica lipase B (CALB) was employed in both stages, with high productivity and selectivity. The type of butyric acid ester influenced the enantioselectivity of the enzyme. Thus, extending the ester alkyl chain from ethyl to octyl resulted in a decrease in enantiomeric excess, whereas using bulky groups such as benzyl or t-butyl, improved the enantioselectivity of the enzyme. A stirred reactor was found unsuitable for large-scale production due to attrition of the enzyme particles and, therefore, a batchwise loop reactor system was used for bench-scale production. The immobilized enzyme was confined to a column and the reactants were circulated through the enzyme bed until the targeted conversion was reached. The desired products were separated from the reaction mixture in each of the two stages by fractional distillation. The main features of the process are the exclusion of solvent (thus ensuring high process throughput), and the use of the same enzyme for both the acetylation and the alcoholysis steps. Kilogram quantities of (S)-HEB and (R)-HEB were effectively prepared using this unit, which can be easily scaled-up to produce industrial quantities.     

Kinetic analysis of the influence of inverse effectors (inhibitors and activators) on enzymatic (transport) activity of proteins

The method is proposed for calculation of the most important parameters of the two-stage enzymatic or transport process--modification factors alpha and beta (which characterize the effector action mechanism) as well as the inhibition constant K(i) or activation constant K(a) (characterize the effector affinity for protein). The method was derived as based on the analysis of kinetic regularities of the action of reversible effectors (inhibitors and activators) on the catalytic (transport) activity of proteins. The method is based on the titration of enzymatic (transport) protein by the substrate with the absence and with presence of the effector taken in one of concentrations as well as determination (under the fixed substrate concentration) of the inhibition coefficient i(0.5) (in case of the inhibitor action) or the activation coefficient a(0.5) (in case of the activator action). Practical use of the method has been demonstrated on the example of reversible inhibition to eosine Y (2', 4', 5', 7' - tetrabromofluorescein) ofthe reaction of enzymatic hydrolysis of ATP catalyzed by highly purified transport Ca2+, Mg(2+)-ATPase isolated from the smooth-muscle sarcolemma. In this case the inhibitory effect is characterized by the following parameters: alpha = 6-8 > 1; beta = 0.50-0.53 < 1; inhibition constant K(i) = 10(-9) - 10(-8) M. Consequently, judging from the values of alpha and beta, the eosine Y effect on the analyzed Ca2+, Mg(2+)-dependent ATP-hydrolase enzymatic reaction is based on the mechanism of the mixed inhibition (one can observe the inhibition of the both stages of enzymatic transformation--the substrate binding with the enzyme and decomposition of "Michaelis complex" in the direction of formation of the reaction products). The inhibitor itself, in correspondence with K(ij) values is characterized by rather high affinity for Ca2+, Mg(2+)-ATPase. It is supposed that the proposed approach can be useful when identifying the type of the reversible effector action on the enzymatic (transport) activity of proteins, estimation of real affinity of the inhibitors and activators for the latter.     

Kinetic modeling of batch hydrogen production process by mixed anaerobic cultures

The kinetics of batch anaerobic hydrogen production by mixed anaerobic cultures was systemically investigated in this study. Unstructured models were used to describe the substrate utilization, biomass growth and product formation in the hydrogen production process. The relationship between the substrate, biomass and products were also evaluated. Experimental results show that the Michaelis-Menten equation, Logistic model and modified Gompertz equation all could be adopted to respectively describe the kinetics of substrate utilization, biomass growth and product formation. Furthermore, the relationship between the acidogenic products and biomass was simulated by Luedeking-Piret model very well. The experimental results suggest that the formation of hydrogen and the main aqueous products, i.e., butyrate and acetate, was all growth-associated.     

Simultaneous ANAMMOX and denitrification (SAD) process in batch tests

The occurrence of simultaneous anaerobic ammonia oxidation and nitrate reduction (SAD) processes by enrichment culture in the presence of glucose were clarified in batch tests. Nitrate conversion and the formation of interim by-products were investigated under autotrophic and mixotrophic conditions. Eventually, the nitrite was fully consumed and co-occurred with ammonia oxidation. The effect of penicillin G and methanol on the SAD process was also investigated. Methanol addition led to complete loss of ANAMMOX activity at concentrations as low as 1?mM. Penicillin G has little effect on the SAD process. Scanning electron microscopy (SEM) observation and denaturing gradient gel electrophoresis (DGGE) analysis revealed that ANAMMOX bacteria and co-existing bacteria are responsible for the SAD process. In conclusion, this study indicates that the ratio of nitrogen to organic carbon, and the cooperation and competition between microbes can affect the dynamics of this process. It has a potential application to remove ammonia and nitrate in the presence of organic matter by the SAD process.     

(R)-phenylacetylcarbinol production in aqueous/organic two-phase systems using partially purified pyruvate decarboxylase from Candida utilis

Aqueous/organic two-phase systems have been evaluated for enhanced production of (R)-phenylacetylcarbinol (PAC) from pyruvate and benzaldehyde using partially purified pyruvate decarboxylase (PDC) from Candida utilis. In a solvent screen, octanol was identified as the most suitable solvent for PAC production in the two-phase system in comparison to butanol, pentanol, nonanol, hexane, heptane, octane, nonane, dodecane, methylcyclohexane, methyl tert butyl ether, and toluene. The high partitioning coefficient of the toxic substrate benzaldehyde in octanol allowed delivery of large amounts of benzaldehyde into the aqueous phase at a concentration less than 50 mM. PDC catalyzed the biotransformation of benzaldehyde and pyruvate to PAC in the aqueous phase, and continuous extraction of PAC and byproducts acetoin and acetaldehyde into the octanol phase further minimized enzyme inactivation, and inhibition due to acetaldehyde. For the rapidly stirred two-phase system with a 1:1 phase ratio and 8.5 U/mL carboligase activity, 937 mM (141 g/L) PAC was produced in the octanol phase in 49 h with an additional 127 mM (19 g/L) in the aqueous phase. Similar concentrations of PAC could be produced in the slowly stirred phase separated system at this enzyme level, although at a much slower rate. However at lower enzyme concentration very high specific PAC production (128 mg PAC/U carboligase at 0.9 U/mL) was achieved in the phase separated system, while still reaching final PAC levels of 102 g/L in octanol and 13 g/L in the aqueous phase. By comparison with previously published data by our group for a benzaldehyde emulsion system without octanol (50 g/L PAC, 6 mg PAC/U carboligase), significantly higher PAC concentrations and specific PAC production can be achieved in an octanol/aqueous two-phase system.     

Continuous production of (R)-phenylacetylcarbinol in an enzyme-membrane reactor using a potent mutant of pyruvate decarboxylase from Zymomonas mobilis.

The optimization of a continuous enzymatic reaction yielding (R)-phenylacetylcarbinol (PAC), an intermediate of the L-ephedrine synthesis, is presented. We compare the suitability of three pyruvate decarboxylases (PDC), PDC from Saccharomyces cerevisiae, PDC from Zymomonas mobilis, and a potent mutant of the latter, PDCW392M, with respect to their application in the biotransformation using acetaldehyde and benzaldehyde as substrates. Among these, the mutant enzyme was the most active and most stable one. The reaction conditions of the carboligation reaction were investigated by determining initial rate velocities with varying substrate concentrations of both aldehydes. From the resulting data a kinetic model was inferred which fits the experimental data with sufficient reliability to deduce the optimal concentrations of both substrates for the enzymatic process. The results demonstrate that the carboligation is most efficiently performed using a continuous reaction system and feeding both aldehydes in equimolar concentration. Initial studies using a continuously operated enzyme-membrane reactor gave (R)-PAC with a space-time yield of 81 g L(-1). d(-1) using a substrate concentration of 50 mM of both aldehydes. The yield was easily increased by cascadation of enzyme-membrane reactors. The new strategy allows the synthesis of (R)-PAC from cheap substrates in an aqueous reaction system. It thereby overcomes the limitation of by-product formation that severely limits the current fermentative process.     

Kinetic modelling of Amadori N-(1-deoxy-D-fructos-1-yl)-glycine degradation pathways. Part II--kinetic analysis

A kinetic model for N-(1-deoxy-D-fructos-1-yl)-glycine (DFG) thermal decomposition was proposed. Two temperatures (100 and 120 degrees C) and two pHs (5.5 and 6.8) were studied. The measured responses were DFG, 3-deoxyosone, 1-deoxyosone, methylglyoxal, acetic acid, formic acid, glucose, fructose, mannose and melanoidins. For each system the model parameters, the rate constants, were estimated by non-linear regression, via multiresponse modelling. The determinant criterion was used as the statistical fit criterion. Model discrimination was performed by both chemical insight and statistical tests (Posterior Probability and Akaike criterion). Kinetic analysis showed that at lower pH DFG 1,2-enolization is favoured whereas with increasing pH 2,3-enolization becomes a more relevant degradation pathway. The lower amount observed of 1-DG is related with its high reactivity. It was shown that acetic acid, a main degradation product from DFG, was mainly formed through 1-DG degradation. Also from the estimated parameters 3-DG was found to be the main precursor in carbohydrate fragments formation, responsible for colour formation. Some indication was given that as the reaction proceeded other compounds besides DFG become reactants themselves with the formation among others of methylglyoxal. The multiresponse kinetic analysis was shown to be both helpful in deriving relevant kinetic parameters as well as in obtaining insight into the reaction mechanism.     

Kinetic analysis of enzymatic chiral resolution by progress curve evaluation

The present study deals with kinetic modeling of enzyme-catalyzed reactions by integral progress curve analysis, and shows how to apply this technique to kinetic resolution of enantiomers. It is shown that kinetic parameters for both enantiomers and the enantioselectivity of the enzyme may be obtained from the progress curve measurement of a racemate only.A parameter estimation procedure has been established and it is shown that the covariance matrix of the obtained parameters is a useful statistical tool in the selection and verification of the model structure. Standard deviations calculated from this matrix have shown that progress curve analysis yields parameter values with high accuracies.Potential sources of systematic errors in (multiple) progress curve analysis are addressed in this article. Amongst these, the following needed to be dealt with: (1) the true initial substrate concentrations were obtained from the final amount of product experimentally measured (mass balancing); (2) systematic errors in the initial enzyme concentration were corrected by incorporating this variable in the fitting procedure as an extra parameter per curve; and (3) enzyme inactivation is included in the model and a first-order inactivation constant is determined.Experimental verification was carried out by continuous monitoring of the hydrolysis of ethyl 2-chloropropionate by carboxylesterase NP and the alpha-chymotrypsin-catalyzed hydrolysis of benzoylalanine mathyl ester in a pH-stat system. Kinetic parameter values were obtained with high accuracies and model predictions were in good agreement with independent measurements of enantiomeric excess values or literature data. (c) 1994 John Wiley & Sons, Inc.