P.L. Rogers, H.S. Shin and B. Wang- Biotransformation for L-Ephedrine Production

 

 

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Biotransformation for L-Ephedrine Production P.L. Rogers, H.S. Shin and B. Wang. Department of Biotechnology, University of New South Wales, Sydney 2052, Australia 1 2 2.1 2.2 2.3 2.4 3 3.1 3.2 4 5 5.1 5.2 5.3 6 6.1 6.2 6.3 7 8

Introduction Factors Affecting L-phenylaœtylcarbinol L-phenylaœtylcarbinol (L-PAC) Production Pyruvate Decarboxylase (PDC) Activity Metabolic Status of Yeast Benzaldehyde Concentration End-product Inhibition Biotransformation Using Yeasts - Free Cells Fed-Batch Process Continuous Process Biotransformation Using Yeasts - Immobilized Cells Biotransformation Using Purified PDC - Free Enzyme Characteristics of Purified PDC Factors Influencing Biotransformation Kinetics Kinetic Analysis Biotransformation Using Purified PDC-Immobilised Enzyme PDC Immobilisation Factors Influencing Biotransformation Kinetics Continuous Biotransformation Discussion and Conclusions References

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L-ephedrine is widely used in pharmaœutical preparations as a decongestant and anti-asthmatic compound. One of the key intermediates in its production is L-phenylacetylcarbino L-phenylacetylcarbinoll (L-PAC) which can be obtained either from plants ( Ephedra  Ephedra sp.), sp.), chemical synthesis involving isolation of a racemic mixture, or by biotransformation of benzaldehyde using various yeasts. In the present review, recent significant improvements in the microbial biotransformation are assessed for both fed-batch and continuous processes using free and immobilized yeasts. From previous fed-batch culture data, maximal levels of L-PAC of 10-12 g L-1were reported with yields of 55-60% theoretical based on benzaldehyde. However, recently concentrations of more than 22 g L-1 have been obtained using a wild-type stain of Candida utilis. utilis. This has been achieved through optimal control of yeast metabolism (via microprocessor control of the respiratory quotient, RQ) in order to enhance substrate pyruvate production and induce pyruvate decarboxylase (PDC) activity. Processes involving purified PDC have also been evaluated and it has been demonstrated that L-PAC levels up to 28 g L-1 can be obtained with yields of 90-95% theoretical based on the benzaldehyde added. In the review the advantages and disadvantages of the various strategies for the microbial and enzymatic production of the L-PAC are compared. In view of the increasing interest in microbial biotransformations, L-PAC production  provides an interesting interesting example of enhancement through through on-line control of a process process involving  both toxic substrate substrate (benzaldehyde) and end-product end-product (L-PAC, benzyl alcohol) in inhibition. hibition.

 

 

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1 Introduction The transformation of organic compounds using biocatalysts - enzymes, cell organelles or whole cells are important processes in organic synthesis, and have been widely used in the production of steroids, antibiotics, vitamins and other highvalue products (1). The advantages advantage s of such biotransformations are that they are reaction-specific processes (e.g. condensation, hydrogenation, esterification, decarboxylation, etc.), and can involve high degrees of regio- and stereo specificity. In addition, in most cases relatively mild reaction conditions are used (2). As well as these advantages some problem areas have been identified. These include low substrate and  product solubilities in the aqueous phase, substrate and product toxicities, together with low yields and low productivities particularly with whole cell biotransformation. As a result there has been considerable recent research on the enhancement of  biotransformation kinetics by the use of two phase systems (3,4,5), (3,4,5), biotransformation in a ‘micro-aqueous’ environment in the presence of an organic solvent (6,7,8), the use of reverse micelles (9,10) and the application of supercritical fluid extraction for product removal (11,12). Microbial biotransformation for the production of biologically active chiral compounds (L-form), which are important building blocks in the pharmaceutical industry, is a field which has grown significantly in recent recen t times. This has been largely due to the toxicological problems which have been encountered with the pharmaceutical use of racemic mixtures (13). In the present review, various strategies are assessed for a biotransformation process which involves the conversion of benzaldehyde to L-phenylacetylcarbinol (L-PAC), an intermediate in the production of L-ephedrine and related psuedoephedrines. This can be considered as an interesting biotransformation process for evaluation, as it includes both b oth toxic substrate and end-product inhibition. L-ephedrine is a natural plant alkaloid isolated originally from the dried young  branches of Ephedra, a plant with interesting pharmacological activities. Extracts of Ephedra sp., particularly Ephedra sinica, E.equisetina and E.distachya commonly called ‘Ma Huang’ in China, have been used for several thousand years as folk remedies for inducing sweat, soothing breath andisolated easing excretion The active ingredient these extract, L-ephedrine, was first in 1855, and aof ndurine. international interest in thisof drug was stimulated by the classical investigations of Chem Che m & Schmidt in 1930, who reported on its cardiovascular effects and its similarity to epinephrine (14) Ephedrine, known chemically as 1-methylamino-ethyl-benzyl alcohol or 2-methylamino-l-phenyl-l-propanol, contains two asymmetric carbon atoms, so that there are four optically active forms (Fig. 1), of which the (L-) isomers are used clinically. These four isomers occur naturally in Ephedra plants, and can be extracted with alcohol and benzene. Purified ephedrine is obtained as odourless, colourless crystals or as a white crystalline powder with bitter taste.

 

 

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L-norephedrine

D-norpsuedoephedrine

L-ephedrine

D-psuedoephedrine

Fig. 1. The Structural formulae for ephedrine and its analogs (15)

Ephedrine and pseudoephedrine are very stable. A solution of ephedrine hydrochloride sealed for six years showed neither oxidation nor loss of activity (15, 16). Its main use pharmacologically is as a decongestant or anti-asthmatic compound, although recent reports have indicated its potential in obesity control (17). Three production methods have been used for L-ephedrine: traditional extraction from  plant species of Ephedra, of Ephedra, a  a synthetic chemical process involving resolution of the racemic mixture, and a process which involves the biotransformation of benzaldehyde to L-PAC by various species of yeasts followed by reductive animation (18, 19). The biotransformation process which involves the condensation of an ‘active  benzaldehyde' (from pyruvic pyruvic acid) and benzaldehyde is sh shown own in Fig. 2. The production production of the LPAC is catalysed by the enzyme pyruvate decarboxylase (PDC), and can be associated with  benzyl alcohol by-product by-product formation, due to the acti activity vity of alcohol dehydrogenase(s) dehydrogenase(s) (ADH) and/or other non-specific oxidoreductases. Some traces of benzoic acid as a by-product have also  been reported. Previous studies have reported concentrations if 10-12 g L -1 L-PAC in batch culture with free cells (20, 21) and with immobilized yeast (22, 23). The addition of cyclodextrins (particularly β-cyclodextrin) was shown to enhance L-PAC production with immobilized Saccharomyces cerevisiae (24) cerevisiae (24) although again maximal concentrations of 12 g L-1  L-PAC were reported. Evaluation of a large number of yeast strains by Netrval and Vojtisek (19) identified strains of Saccharomyces Saccharomyces,, Candida Candida and  and Hansenula  Hansenula sp.  sp. which were capable of significant L-PAC  production in shake-bask shake-bask cultures (up to a maximum of 6.3 g L-1). Strain improvement studies to develop acetaldehyde and L-ephedrine resistant mutants have been reported by Seely et al. (25) with mutants capable of increased L-PAC levels compared to wild-type strains. However, maximal L-PAC levels did not exceed 10 g L-1.

 

 

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Benzaldehyde

Pyruvate

L-phenylacetylcarbinol L-phenylacetylcarbin ol

L-ephedrine (R, S)

Fig.2. Mechanism of L-PAC and ephedrine production

In further fundamental investigations into the biotransformation biotransformation of aromatic substrates by yeasts, other authors have indicated that oxidoreductases other than alcohol dehydrogenates may be involved in benzyl alcohol by-product formation (26-31). Current commercial practice involves a fed-batch process with fermentative yeast growth on sugars to produce biomass, pyruvic acid and induce PDC activity. The growth phase is followed by biotransformation, with the further addition of sugars and the programmed feeding of  benzaldehyde to maximise maximise L-PAC production. Cessation Cessation of L-PAC formation occurs as a result result of the following factors acting either together or independently: (a) reduction of PDC activity due to benzaldehyde inhibition; (b) pyruvic acid limitation at end of biotransformation phase; (c) cell viability loss due to extended exposure to benzaldehyde and/or increasing concentrations of benzyl alcohol and L-PAC.

2 Factors Affecting L-phenylacetylcarbi L-phenylacetylcarbinol nol (L-PAC) Production

2.1 Pyruvate Decarboxylase (PDC) Activity Although L-PAC production depends on PDC activity, little research has been published on the induction and deactivation of this enzyme during the biotransformation process. In our research. studies have been carried out or a strain of Candida utilis selected utilis selected for its ability to tolerate  benzaldehyde and produce produce relatively high levels of L-PAC. The yeast has been grown in batch batch culture under partial fermentation conditions to produce biomass and also induce PDC activity.

 

 

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As shown in Fig. 3, after 18-20 h the PDC activity reached a level of 0.9 U mg protein -1, while the ADH activity was 1.4 U mg protein -1. The fermentative nature of the metabolism was illustrated by ethanol accumulation of 35 g L -1. As indicated earlier, the enhanced PDC activity should be conducive to rapid L-PAC production, while the higher ADH activity may result in more  benzyl alcohol.

 

2.2 Metabolic Status of Yeast In a study to develop strategies for on-line control of the L-PAC process, the eff effect ect of the respiratory quotient (RQ) on the production of L-PAC has been investigated by our group. An RQ value of 1.0 for growth on glucose corresponds to full respiratory growth while RQ values greater than 1.0 indicate fermentative metabolism. Increasing fermentation results in increasing RQ vales. Data using cells of C .utilis utilis grown  grown in continuous culture at controlled RQ values of 1.0, 1.9 and 4.4 are shown in Fig. 4. The biotransformations were carried out in shake flasks at 300C, pH = 6.0 at various initial concentrations of benzaldehyde (0.5-4.0 g L-1). Initial specific rates L-PAC (qPAC) and benzyl alcohol production ( qBA) were estimated from the kinetic data. From Fig. 4 it is evident that full respiratory growth (RQ = 1.0) resulted in a low specific rate of L-PAC and a high specific rate of benzyl alcohol production. Increasing RQ had a significant effect in improving LPAC production rates and yields (65-70% theoretical at higher RQ values). For the  biotransformation process process an RQ value of 4-5 was optimal optimal for the yeast growth ph phase ase as this corresponded to an RQ which produced sufficient yeast biomass for rapid biotransformation, while enhancing L-PAC production rates and yields. Through the use of on-line gas analysers for O2 (paramagnetic) and CO2 (infrared) measurements, interfaced to a microprocessor for calculation of RQ and subsequent stirrer speed adjustment, an effective feedback control strategy for RQ has been developed.

2.3 Benzaldehyde Concentrati Concentration on The effect of benzaldehyde on L-PAC production by S.cerevisiae S.cerevisiae has  has been investigated by Gupta et al. (32) and Agarwal et al. (33). The latter authors reported that once the benzaldehyde concentration increased above 16 mM (1.7 g L-1), the species rate of L-PAC production decreased, and beyond 20 mM (2.1 g L -1) it was inhibited completely. When the residual  benzaldehyde declined below below 4 mM (0.4 g L-1), the formation of benzyl alcohol was predominant over4-16 L-PAC. estimated the optimum benzaldehyde concentration range was mM.They Further studiesthat (34) cited the optimum concentration for L-PAC -1  production as 10 mM (1.1 g L ).

 

 

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  utilis. a Cell growth: ( ) biomass, Fig. 3. Kinetics of growth and enzyme profiles of Candida utilis. (O) ethanol, ( () glucose. b Enzyme profiles: () PDC, (O) ADH

 

 

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Fig 4a-c. Effect of RQ and benzaldehyde concentrations on a initial specific rate of L-PAC

(qPAC) production, b specific rate of benzyl alcohol (qBA) productions, and c final L-PAC 

Benzaldehyde concentrations: (o) 0.5, () 1.0, ( -1 (conversion ) 4.0 g Lefficiency.

) 1.5, () 2.0, () 3.0,

 

 

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Fig. 5. Effect of benzaldehyde concentration on the specific rate of L-PAC production by C.utilis. Cells grown in continuous culture at T = 300C, pH = 5.2, D = 0.15 h -1 and RQ values (o) 1.0, () 1.9, () 4.4

 

 

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  In recent studies by our group it has been found with C.utilis C.utilis that  that cessation of growth occurred for -1  benzaldehyde concentrations concentrations above 1.0 g L . A growth inhibition constant for benzaldehyde was estimated at 0.30 g L-1 (unpublished data). Using initial rate analysis, the effect of benzaldehyde on L-PAC production has been investigated. An analysis of the data for a range of initial  benzaldehyde concentrations concentrations (0.5--4.0 g L-1) is shown in Fig. 5. From the analysis. the maximum specific rate of L-PAC production ( qPAC) was estimated as 0 10 gg -1 h -1 for RQ = 4.4, the Ks value (saturation constant) was 1.0 g L -1 benzaldehyde and concentrations of benzaldehyde in excess of 3.0 g L -1 caused a significant decrease in qPAC. In studies of Tripathi ct al. (34) with a strain of S.cerevisiae S.cerevisiae,, a maximum qPAC value of 0.07 gg-1  h-1 was reported.

2.4 End Product Inhibition The main products which are likely to influence yeast growth and metabolism as well as L-PAC  production are: ethanol ethanol produced by fermentativ fermentativee metabolism, benzyl alcohol by-product by-product and the L-PAC product itself. It is possible also that acetaldehyde or benzoic acid accumulation might influence L-PAC production, although only very low levels were detected during  biotransformation with with free cells of C.utilis. C.utilis.   In this context, Seely et at. (25) have mutagenized strains of S.cerevisiae S.cerevisiae and  and C.flareri C.flareri   using classical methods, eg. N-methyl-N'-nitro-N-nitrosoguani N-methyl-N'-nitro-N-nitrosoguanidine dine (NTG), ultra-violet light (UV) and gamma rays and have selected mutants with increased resistance to acetaldehyde and Lephedrine. Strains were isolated capable of producing L-PAC to higher levels than parent cultures, and final concentrations to a maximum of L-PAC of 9,9 g L-1 were reported. Studies in our laboratory on a strain of C.utilis C.utilis have  have indicated the potential for significant end-product and by-product inhibition inhibition of growth. Product inhibit inhibition ion constants for growth (Kp) -1 -1 have been estimated as 4.1 g L  L-PAC, 5.0 g L  benzyl alcohol and 39 g L -1 ethanol (unpublished data). The effect of these products on the specific rate of L-PAC production (qPAC) for the free cells are yet to be determined.

3 Biotransformation Using Yeasts- Free Cells 3.1 Fed-Batch Process A fed-batch process for L-PAC production can be subdivided into three basic phrases: (1) growth of the yeast under partial fermentation conditions to produce sufficient biomass for the biotransformation process, and also to facilitate the accumulation of pyruvate for subsequent L-PAC production;

 

 

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  (2) optimal induction of PDC for biotransformation - however PDC induction in an increasingly fermentative environment results in conversion of pyruvate to ethanol via acetaldehyde, and an increase in alcohol dehydrogenases which may enhance benzyl alcohol formation; (3) programmed feeding of benzaldehyde to maintain concentrations of 1-2 g L-1 and the subsequent production of L-PAC. As discussed earlier, L-PAC concentrations of 10-12 g L-1 have been reported in the literature using various species of yeasts. However, it is only recently that higher levels have been found. Presumably pyruvate depletion occurred in many of the earlier studies and insufficient attention was paid to initial pyruvate accumulation, PDC activity and the metabolic status of the yeast. Some studies (20,28) evaluated the addition of pyruvate and acetaldehyde to achieve higher L-PAC levels; however the effects were variable and in many cases no enhancement was found. In a recent study by our group, L-PAC levels up to 22 g L -1 have been achieved through the optimal control of metabolism of a strain of C.utilis C.utilis (viz.  (viz. RQ = 4-5) and the sustained feeding of benzaldehyde while maintaining a concentration of 1-2 g L-1 in the bioreactor (35). The results of a typical experiment in a controlled bioreactor (T = 200C, pH = 6.0) using a fully-defined medium are shown in Fig. 6. Prior to PDC activation, pyruvic acid levels were typically 10-15 g L-1 with PDC activity low (0.2 U mg protein-1). After cell growth and pyruvate accumulation (total 22 h) with glucose addition to maintain active metabolism, PDC activity was enhanced (to -1

greater than 1.0 U mg ). Benzaldehyde feedingofwas initiated andoccurred resulted to in 4subsequent L-PAC production. Asprotein shown in Fig. 6, accumulation benzyl alcohol g L-1 and LPAC reached 22 g L -1. Biotransformation finally ceased due to pyruvate depletion accompanied  by declining PDC activity. activity. Cell viability studies studies after 14 h biotransformation biotransformation indicated 100% viability loss. The productivity for the biotransformation phase was 1.6 g L -1 h-1 with a yield of 65% theoretical based on the benzaldehyde utilized. No benzoic acid was detected.

3.2 Continuous Process Continuous promises are often cited as having the advantages of higher productivities, easier  process control and compatible compatible operation with ssubsequent ubsequent downstr downstream eam product recovery. However, there are relatively few reports on the application of free cells in continuous culture to  biotransformation processes, processes, although Rohner Rohner et al. (36, 37) have reported on the successful successful application of chemostat cultures of S.cerevisiae S.cerevisiae for  for the stereospecific reduction of acetoacetic acid esters to the 3-(5)-hydroxy-butanoic acid esters. A continuous single-stage steady-state  production system system was found to be superior to the the pulse-batch and fed-bat fed-batch ch systems in terms of  product optical purity, purity, biomass concentration and and production rates. It was es established tablished also in this this  process that the reduced product product

 

 

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Fig. 6a, b. Fed-batch biotransformation of benzaldehyde to L-PAC by C.utilis. a Enzyme

 profiles: () PDC, (O) ADH, b Biotransformation kinetics: (O) benaldehyde, () benzyl alcohol, () pyruvate, () L-PAC

 

 

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  (3-(5)-hydroxybutanoic (3-(5)-hydroxybutan oic acid ester) did not inhibit the cells (36) although the starting material (acetoacetic acid ester) influenced both the respiration and cell physiology of S.cerevisiae S.cerevisiae.. With L-PAC production, both the substrate (benzaldehyde) and the product (L-PAC) have significant inhibitory effects on yeast metabolism and PDC activity. These factors necessitate the design of a more complex continuous culture process, and suggest one involving multistage operation and later stage benzaldehyde feeding in order to sustain steady-state conditions. Other workers have reported on the use of a single-stage continuous culture for the  production of active active yeast cells for L-PAC production production (34), however the biotransformation biotransformation of benzaldehyde was carried out in batch culture. In recent studies in our laboratories a detailed evaluation of various continuous culture systems has been carried out, and the results of this research can be summarised as follows: (1) A single-stage continuous culture operating as a glucose-limited chemostat with continuous feeding of benzaldehyde was not suitable for the biotransformation process due to the strongly inhibitory inhibitory effects of benzaldehyde on cell growth. (2) For a two-stage system, partially fermentative conditions can be established in the first stage to provide for pyruvic acid accumulation and PDC induction, while benzaldehyde can be added to the second stage to facilitate the biotransformation. However, it was found that the  biomass yield under the the partially fermentative con conditions ditions in the first stage stage was too low to produ produce ce sufficient yeast cells for rapid L-PAC production in the second stage. (3) To overcome the disadvantages of the single- and two-stage processes, a three-stage system was designed as follows: Stage 1. A 1. A fully aerobic stage (RQ = 1) designed to give yields to C.utilis C.utilis of  of Yx/s = 0.450.50 gg-1  glucose, close to the theoretical maximum biomass yield. Stage 2. A 2. A partially fermentative stage (RQ = 4-5) designed to increase PDC activity as well as  providing for some some accumulation of pyruvic acid acid.. A supplementary feed of glucose was was supplied to this second stage. Stage 3. A 3. A continuous biotransformation biotransformation stage was established with benzaldehyde addition at various feed rates. Low level glucose feeding was also supplied to this stage to provide substrate for continuing yeast metabolic activity. A diagram of the three-stage process together with a typical set of operating conditions is shown in Fig. 7. This system was evaluated with a range of benzaldehyde and supplementary glucose feed rates using defined medium containing 60 g L -1 glucose to the first stage. Under fully aerobic conditions (DO > 20% air saturation), it was established that close to 30 g L -1  biomass was  produced in the first stage stage (RQ = 1). PDC induction up to 0.50 0.50 U mg protein -1  and pyruvate accumulation to 2-3

 

 

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TYPICAL ENZYME ACTIVITIES IN EACH STAGE

Operating characteristics for 3-stage continuous process for PAC production biotransformation n process, showing Fig. 7. Operating conditions for a three-stage continuous biotransformatio typical enzyme activities for each stage

g L-1 occurred during Stage 2, as well as the formation of 45-50 g L-1 ethanol. The ethanol has  been shown to be beneficial beneficial for enhancing the solubility solubility of benzaldehyde benzaldehyde during Stage 3; however it is represented a significant consumption consumption of glucose. As shown in Fig. 8, when the  benzaldehyde feeding rate rate was increased

 

 

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Fig. 8a, b. Effect of increased benzaldehyde feeding on L-PAC production in a three-stage

 process, a Benzaldehyde feed rate; b concentrations: (o) benzaldehyde, () benzyl alcohol, () L-PAC Incrementally during 300 h, the L-PAC concentration increased to 10.6 g L-1 to a controlled fermentor of 4 L working volume during Stage 3 resulted in a decline in L-PAC levels and the accumulation of benzaldehyde. Under these conditions, the PDC activity declined to less than 0.05 U mg protein -1.

 

 

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  At the maximal steady-state L-PAC concentration of 10.6 g L-1, the productivity, based on the total volume of the three fermentors, was 0.44 g L-1 h-1  with a yield of 0.80 gg-1 (56% theoretical) based on the benzaldehyde used.

4 Biotransformations Using Yeasts - Immobilized Cells It has been reported that cell immobilization of yeasts is able to reduce the toxic effects of  benzaldehyde by virtue virtue of divisional limitations limitations and the toxic substrate substrate gradients that are established within the immobilizing matrix (22, 23, 38). Recent studies by our group using cells of C.utilis immobilized within calcium alginate  beads of 2-3 mm diameter have confirmed this this enhanced resistance to b benzaldehyde enzaldehyde (39), with the immobilized cells producing higher L-PAC levels than free cells in shake bask experiments. In experiments with the programmed feeding of benzaldehyde in a controlled bioreactor (T = 20 DC, pH = 5.0), under similar conditions to those described previously with free cells, the final LPAC concentration was 15 g L-1 (39). The PDC activity of the cells in the beads which was initially at 0.65 U mg protein -1 declined to 0.2 U mg protein-1, with cessation of L-PAC  production resulting resulting from pyruvate depletion. depletion. Electron microscope pictures pictures taken at the end of the  biotransformation (Fig. (Fig. 9) indicated that major cell wal walll damage had occurred within th thee calcium -1 alginate beads. The reason that the final L-PAC level of 15 g L  with immobilized cells was significantly less than the 22 g L -1 achieved with the free-cell fed-batch system is that better control of yeast metabolism (via RQ) in the latter case provided for greater pyruvate accumulation. Levels of 10-15 g L -1 were achieved with the free cells, while for the immobilized cell system the maximum concentration was only 5 g L-1. When this evaluation with immobilized C.utilis was extended to a continuous bioreactor, the steady-state L-PAC levels were low (no more than 4 g L-1 in sustained operation). These results were similar to those of Mahmoud et at.(22, 38) who reported on a semicontinuous immobilized cell process. These authors found with immobilized S.cerevisiae S.cerevisiae that  that L-PAC  production in the first first and second cycles (with an iintervening ntervening reactivation reactivation period of 24 h) could -1 reach 4.5 g L . Attempts to extend the process to three or more cycles resulted in rupturing of the cells/beads in the continuing presence of benzaldehyde.

5 Biotransformation with Purified PDC - Free Enzyme One of the problems of using yeast whole cells for the biotransformation process is that considerable amounts of benzaldehyde are converted to the unwanted

 

 

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Fig. 9a-d. Comparision of electron microscope pictures of immobilised cells of C.Utilis in

calcium alginate beads. a,b Before exposure to benzaldehyde, c,d following prolonged exposure to 1-2 g L-1 benzaldehyde. The scales are given on the four photographs.

 

 

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   by-product, benzyl alcohol. alcohol. The use of purified PDC offers the the possibility of ov overcoming ercoming this  problem. However, in the latter latter case, pyruvate will have to be su supplied pplied as a substrate and tthere here is the further likelihood that the pyruvate added will be removed via decarboxylation to acetaldehyde and condensation to acetoin. Bringer-Meyer and Sahm (40) have investigated the use of purified PDC from  Zymomonas mobilia mobilia and S.carlsbergensis S.carlsbergensis for  for L-PAC production, and demonstrated that the PDC from Z.mobilis from  Z.mobilis is  is unsuitable for the biotransformation biotransformation due to its low affinity for benzaldehyde and  because of significant substrate substrate inhibiti inhibition on effects. However, the substrate substrate levels and consequent L-PAC concentrations achieved with S.carlsbergensis S.carlsbergensis were  were relatively low in this investigation investigation.. To provide an effective comparison between the yeast biotransformation process and one which involves the purified enzyme, it is necessary to evaluate similar operating conditions and substrate concentrations. Details of our recent study (41) are as follows.

5.1 Characteristics of Purified PDC

Purified PDC was prepared from cells of C.utilis C.utilis growing  growing under partially fermentative conditions in a 100-1 fermented at a constant temperature of 250C and a pH of 6.0. When the PDC activity had reached 0.9 U mg protein-1, the cells were harvested, disrupted in a high pressure homogenizer and the PDC was purified by means of (NH4)2SO4. precipitation and gel chromatography. Previous studies with PDC have demonstrated that the enzyme has a dimeric tetramer structure (α (α2β2) which dissociates in vitro into dimer and monomer subunits with the concomitant release of the cofactors thiamine pyrophosphate (TPP) and magnesium ions (42). This dissociation, predominantly predominantly a function of pH, is affected also by the buyer species. The dissociation was found to be greater in Tris-Cl compared with phosphate and citrate buffers. As a result, in the reported study (41), the reaction mixtures contained various PDC activities and  pyruvate : benzaldehyde benzaldehyde ratios with 30 mM TPP, 0.5 mM MgSO4.7H2O in 40mM phosphate  buffer (pH 6.0) in order to achieve achieve maximal enzyme stability. As shown in Fig. 10, the Km value of PDC for pyruvate was determined to be 2.2 mM at 250C and pH 6.0, with saturation at concentrations in excess of 10mM pyruvate. The Km value is in good agreement with other reported values for PDC from yeasts (43-45).

5.2 Factors Influencing Biotransformat Biotransformation ion Kinetics The effects of various factors on L-PAC formation with purified PDC have been reported in detail (41) and can be summarised as follows (a) Higher yields of L-PAC were achieved at lower temperatures due to reduced acetaldehyde production. For this reason, a temperature of 40C was selected for the enzyme  biotransformations..  biotransformations

 

 

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C.utilis at  at T = 25 0C, pH = 6.0 Fig. 10. Estimation of the Km value for pyruvate for PDC from C.utilis

(b) The optimum pH for L-PAC formation was 7.0 while that for acetaldehyde  production was 6.0. (c) As acetaldehyde is an inhibiting by-product, its role in L-PAC formation was investigated. Initial rate studies established that the inhibition constant (Kp ) for acetaldehyde was of the order of 20 mM (0.9 g L-1) indicating that it could play a significant role in reducing the LPAC formation rate. (d) The influence of an organic solvent such as ethanol in enhancing the benzaldehyde solubility and increasing the L-PAC production rate was evaluated. The selection of ethanol as a water miscible organic solvent was based on the following information: PDC has significant resistance to denaturation by ethanol up to a concentration of 3M (46), PDC has been reported to have highly hydrophobic substrate binding sites and the presence of ethanol may assist enzyme/substrate interactions (47). Furthermore, benzaldehyde is reported to have infinite solubility in ethanol (48) compared to its very limited solubility in water (0.3 g 100 mL -1). Initial rate studies showed that an increase of 30-40% in the rate could be achieved by addition of 2.03.0M ethanol. Based on the above optimal conditions, the substrate saturation constant (Km) for benzaldehyde was determined (Fig. 11), and it is interesting to note that substrate inhibition (benzaldehyde toxicity) only compareswas withevident data for the above concentrations of 180 my (19.1 g 1- 1) for the free enzyme. This

 

 

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C.utilis at  at T = 4 0C, pH = 7.0 Fig. 11. Estimation of Km value for benzaldehyde for PDC from C.utilis

influence of benzaldehyde on the growth of C.utilis C.utilis where  where concentrations above 10 mM were found to inhibit growth completely. The Km value for benzaldehyde substrate limitation limitation for the free enzyme was determined to be 42 mM which compares well with values for Km of 50 mM for PDC from S.carlsbergen S.carlsbergensis sis in the literature (40).. As well as pyruvate and benzaldehyde concentrations, concentrations, it has been established that initial L-PAC formation rates are influenced significantly by PDC activity. As evident from Fig. 12, higher PDC activities resulted in higher initial rates over a wide range of benzaldehyde concentrations (up to 200 mM). Benzaldehyde toxicity was greater for the lower PDC activities. However, although the initial rates were strongly affected by PDC activity, the final L-PAC concentrations were not influenced to the same extent. There was a trend also towards increased acetaldehyde production at the higher PDC activity levels (Table 1). The influence of the molar ratio of pyruvate:benzaldehyde is shown in Table 2. From the data, while the highest molar biotransformation yield of 97.8% (based on initial benzaldehyde) was achieved using 150 mM benzaldehyde and a 1.5 molar ratio, the highest concentration of 191 mM (28.6 g L -1) L-PAC was obtained using 200 mM benzaldehyde and a 2.0 molar ratio after an 8 h biotransformation. Molar conversion yields close to 90% (based on initial pyruvate) were achieved only in the range of 150-200 mM benzaldehyde when molar ratios of 1.0 or 0.5 were used. In other situations, a higher proportion of pyruvate was converted to by-products (free acetaldehyde and acetoin) or

 

 

20

 

Fig. 12. Effect of PDC activity on initial rate of L-PAC formation in the present of various concentrations of benzaldehyde and equimolar concentrations of sodium pyruvate in 40 mM  phosphate buffer (pH = 7.0) containing containing 30 µM TPP, 0.5 mM MgSO4.7H2O and 2.0 M ethanol. The initial rates were determined within 30 min at 40C. The symbols refer to PDC activities of () 4.0, () 5.0, () 6,0, (O) 7.0, () 8.2 and () 10.0 unit.ml-1 

remained in excess concentrations in the reaction mixture. It is interesting to note also that increases in initial benzaldehyde (200-300 mM) and PDC activity (7.0-20 U mL-1) did not further raise the final L-PAC concentrations, presumably because of substrate toxicity effects.

5.3 Kinetic Analysis Detailed kinetics of a typical time course for the biotransformation of 150 mM benzaldehyde with  purified PDC are shown in Fig. 13; 13; they demonstrate the time d dependence ependence of simultaneous L L-PAC, acetaldehyde and acetoin formation together with biotransformation of pyruvate and  benzaldehyde. In the first 2-3 h, h, L-PAC formation increased rapid rapidly, ly, while further L-PAC formation occurred more slowly and was influenced by substrate depletion and probable probable product inhibition. After a 6 h incubation period, giving a maximum L-PAC concentration of 147 mM (22 gL-1), a mass balance based on pyruvate indicated that of the original 225 mM pyruvate, 147 mM had contributed to L-PAC formation, 25 mM pyruvate had been converted to acetous and 22 mM had been converted to free acetaldehyde. The residual pyruvate was 30 mM, indicating

 

 

21

  Table 1. Final L-PAC and acetaldehyde concentrations (mM) with various PDC activities in the  presence of equimolar benzaldehyde benzaldehyde and sodium pyruvate pyruvate at 40C and pH 7.0 PDC L-PAC (mM) activity Benzaldehyde (mM) -1 (Unit mL ) 30 50 100 150 a 

 a 

4.0 5.0

19.0 20.1

34.8 34.8

48.2 64.5

3.4  a  30.0

6.0 7.0 8.2 10.0

17.9 17.3 16.2 15.1

34.2 33.5 32.1 30.5

76.8 78.3 71.3 62.9

94.0 135.6 129.3 125.7 

PDC activity

Acetaldehyde (mM) Benzaldehyde (mM)

(Unit mL-1)

30

50

100

150 

4.0

6.1

9.5

2.3

5.0

6.5

10.2

7.5

 a

 a

 ND  a ND  

6.0 7.1 10.8 10.5 8.3 7.0 7.5 11.0 11.4 8.4 8.2 8.2 12.0 16.0 9.2 10.0 9.1 13.5 17.8 10.1 a  Reaction did not proceed fully due to toxicity of benzaldehyde at low PDC activity

0

Fig. 13. Typical biotransformation kinetics with purified PDC from C.utilis. C.utilis. T  T = 4 C, pH

= 7.0. Concentrations () benzaldehyde, (O) pyruvic acid, () acetaldehyde, () acetoin, () L-PAC

 

 

22

Table 2. L-PAC formation with various molar ratios of pyruvate to benzaldehyde at 40C. The reaction mixture consisted of 40mM phosphate buffer (pH 7.0) containing 7 U mL-1 PDC, 2.0 M ethanol and various concentrations of sodium pyruvate and benzaldehyde.

Final concentration of L-PAC (g L -1) and molar conversion yeilds (%) Molar ratio of pyruvate to benzaldehyde BZ (mM)

0.5

1.0

1.2

1.5

2.0

100

5.8

11.7

14.2

14.5

14.5  

77.0

78.2

78.3

64.5

48.4  

38.3 7.0 77.2 38.6 10.9 97.0 48.6 12.1 89.5 44.4 13.3 88.5 44.2

78.2 14.6 81.1 81.8 20.5 90.6 90.6 24.2 90.0 90.0 22.7 75.6 75.6

94.6 16.8 7.6 93.2 21.5 79.6 95.3 25.1 77.5 93.0 24.9 69.1 82.9

96.7 17.6 65.2 97.5 22.0 64.9 97.8 25.5 63.0 94.4 27.9 62.0 93.0

96.7   17.6 48.9 97.5 22.0 48.9 97.8 25.5 47.2 94.4 28.6 47.6 95.3

120

150

180

200

a

 b c

a

L-PAC (g L-1); expressed as g L-1 for comparison with literature values.

 b   Y p/s (mole L-PAC,mole added pyruvate-1) x 100 (%). c   Y p/s (mole L-PAC,mole added benzaldehyde-1) x 100 (%).

a closing mass balance based on pyruvate. With the complete utilization of 150 mM  benzaldehyde, the mass balance balance based on benzaldehyde conversion conversion to L-PAC closed to wi within thin 2%. The small mass balance discrepancy was probably due to evaporative losses of benzaldehyde and/or minor experimental errors. In addition, after 6 h incubation, 20-30% of initial PDC activity still remained, indicating the potential for further biotransformation if more benzaldehyde were available.

6 Biotransformation using Periled PDC - Immobilized Enzyme Previous studies have reported that cell and enzyme immobilization in suitable gels and matrices could minimise substrate inhibition effects by means of dimensional limitation and the substrate gradients which exist within the immobilizing material (22, 23, 38). Furthermore, the development of an immobilised system provides the technology for long-term continuous operation, provided that enzyme stability can be maintained.

 

 

23

6.1 PDC Immobilization

In our recent work, various immobilizing methods have been evaluated for PDC, including adsorption on cationic exchange resins and entrapment in gel matrices (49). It was found that entrapment in calcium polyacrylamide gel provided a higher activity than adsorption on either Amberlite IR-200 or CM-sephadex (activities expressed as U mL -1 immobilizing material), and that the addition of 0.2-0.3% glyceraldehyde to the polyacrylamide gel enhanced the PDC  binding capacity and and increased PDC activity by 40%. 40%. The 'apparent' Km for PDC immobil immobilized ized 0 with respect to pyruvate was determined at 25 C from initial-rate data, and a value of 3.2 mM estimated from Lineweaver-Burk analysis. This compares with with 2.2 mM for the free enzyme - the higher Km for the immobilized enzyme being consistent with mass transfer limitations within the gel.

6.2 Factors Influencing Biotransformat Biotransformation ion Kinetics In a similar evaluation to that with free PDC, the optimal conditions for the immobilized PDC were determined. Although higher temperatures gave rise to an initial increase in the L-PAC 0

 production rate, the relatively relatively high acetaldehyde and acetoin acetoin concentrations at 25 C resulted in reduced final L-PAC formation. As for the free enzyme, a temperature of 4 0C was selected to maximise the L-PAC yield. The optimum pH for L-PAC with immobilized PDC was shifted slightly to more acidic conditions (pH = 6.5) compared to the free enzyme (pH = 7.0). Ethanol was again found to enhance initial rates (due to improved benzaldehyde solubility) and a concentration of 3-4 M gave a 40% increase in initial rates compared to the control. For a batch biotransformation process, the immobilized PDC process did not provide any real advantages compared to the free PDC system. The results were much as expected with the immobilized enzyme able to function better at higher benzaldehyde concentrations (up to 300 mM). The maximum final L-PAC concentrations were similar, viz. 27.1 gL-1 with 300 mM  benzaldehyde and 1.5 molar ratio ratio of pyruvate:benzaldehyde. pyruvate:benzaldehyde.

6.3 Continuous Biotransformation Biotransformation The operating parameters for a continuous process are shown in Fig. 14 with increasing molar ratios and residence times (viz. decreasing dilution rates) resulting in the increased formation of L-PAC and by-products, acetaldehyde and acetoin. While the highest concentration of 5.3 g L-1 L-PAC was achieved with a 2.0 molar ratio at D = 0.05 h -1 higher LPAC productivities could be achieved at higher dilution rates. In an evaluation of the long-term operation of the process it was found that a gradual decline in PDC activity occurred, with the enzyme half-life estimated to be 32 days.

 

 

24

 

Fig. 14. Effect of dilution rate and molar ratios of pyruvate: benzaldehyde on L-PAC production using immobilised PDC in a packed-bed bioreactor. T = 40c, pH = 7.0. L-PAC concentrations for molar ratios: () 1.0, () 1.5, () 2.0; productivities for molar ratios: (O) 1.0, () 1.5, () 2.0

7 Discussion and Conclusions

A comparison of the various biotransformation processes for the conversion of benzaldehyde to L-PAC is given in Table 3. From the data it is evident that for both free and immobilized yeast, the biotransformation is a relatively low efficiency process in which there is significant diversion of benzaldehyde to benzyl alcohol and a loss of up to 30-40% due to the formation of by products. This diversion diversion has been attributed attributed to the activity of alcohol alcohol dehydrogenates in yeast. However, studies by Nikolova and Ward (29) using mutant strains of S.cervisiae S.cervisiae that  that lack ADH-I, -11 and -111 demonstrated that these strains were still able to produce ethanol and benzyl alcohol and suggested that other oxidoreductases were catalyzing these reductive biotransformations. Other authors (50, 51) have demonstrated the presence of ADH-IV, activated by Zn, in low amounts in S.cerevisiae S.cerevisiae and  and it is possible that this enzyme may play some part in ethanol and  benzyl alcohol production. production. Using yeast strain selection, immobilized cell technology and cyclodextrin addition,  previous studies have have reported maximal L-PAC concentrat concentrations ions of 10-12 g L-1. Recent studies by our group, however, have demonstrated with the control of yeast activity and metabolism (via control of the respiratory quotient,

 

 

25

  Table 3. Comparison of kinetic evaluations for various methods of L-PAC production Process

L-PAC (g L-1)

Biotrans. time (h)

Productivity (g L-1h-1)

Yield theorectical  based on  benzaldehyde

Ref.

(1) Batch and fed-batch processes Free cells 12.4 22.4 Free cells 12 (cyclodextrins) Immobilised cells 9.9 10 15 Free PDC 28.6 Immobilised PDC 27.1

17 14

0.73 1.6

57 65

(21) (35) (24)

3 24 22 8 12

3.3 0.42 0.7 3.6 2.3

60 59 58 95 93

(23) (22) (39) (41) (49)

(2) Continuous processes Immobilised cells 4

-

0.6

45

(39)

4.5

-

0.4-0.8

57

(22)

10.6

-

0.44

56

(53)

Immobilised cells (semi-continuous) Three-stage system (free cells)

RQ), that L-PAC concentrations up to 22 g L-1 can be achieved in defined media in the normal  biotransformation time. time. This has resulted from accumulation accumulation of pyruvic acid, indu induction ction of PDC and controlled feeding of benzaldehyde. It is interesting to note that other authors (52) using defined media and a Candida Candida strain  strain have also achieved relatively high levels of pyruvic acid by manipulation of PDC activity. Furthermore, the use use of defined media also offers the advantages advantages of easier solvent-extraction of L-PAC and, fewer pollution problems compared to the use of industrial substrates such as molasses. From Table 3 it is evident that continuous biotransformation processes do not offer any advantages when compared to a fed-batch process under optimal control. This results from the highly toxic nature of the substrate benzaldehyde which considerably reduces cell viability and PDC activity in a continuous process. Rohner et al (36, 37) demonstrated that a chemostat culture was the most suitable for a biotransformation which involved involved the stereo-specific reduction of acetoacetic acid esters; however, in this case the inhibition effects of substrate/products on S. cerevisiae were cerevisiae  were much lower. The use of purified PDC for the biotransformation demonstrated that the PDC could maintain its activity at benzaldehyde concentrations greater than 2?0 mM (21 g L-1) and give LPAC concentrations up to 28 g L-1. Very high conversion efficiencies were achieved (greater than 95% theoretical based on benzaldehyde added) as no significant aromatic by-products were  produced. However, with the the purified PDC process it was n necessary ecessary to add pyruvic acid wi with th a mole ratio of pyruvate : acetaldehyde greater than 1.0, due to formation of the by-products acetaldehyde and acetoin. Mass balances on both the

 

 

26

 benzaldehyde and the pyruvate pyruvate closed to within 2 2% % indicating the accuracy of of the analytical  procedures and the identification identification of all major products products in the biotransformation biotransformation process. In an overall assessment of the L-PAC process, it is clear that significant enhancements can be achieved by either improved process control of the yeast biotransformation or by the development of an enzymatic process based on purified PDC. The choice will ultimately be based on economic criteria; however, it may also be influenced by the development of genetically engineered strains of yeasts with enhanced PDC and reduced oxidoreductase activities, resulting in higher L-PAC yields and productivities.

8 References

1. Creuger W. Creuger C reuger A (1988) In: Biotechnology: A Textbook of Industrial Microbiology, 2nd Edn. Science Tech. Publ., Madison, p.286 2. Fear K (1993) Biotransformations in Organic Chemistry, Springer New York Berlin Heidel berg 3. Klibanov AM ( 1986) Chemtech 16: 354 4. Haling PJ (1987) In: Moody GW. Baker PB (eds) Bioreactors and Biotransformations. Elsevier  New York, p. 189 5. Yamane Aldercreutz P, Mattiasson B (1987) 1(2): 99 6. T (1988) B iocatalysis Biocatalysis 2(1):Biocatalysis 1 7. Fukui S, Ahmed SA, Omata T, Tanaka A (1980) Eur J Appl Microbial Biotechnol 10: 289 8. Zaks A, Klibanov AM (1988) J Biol Chem 263: 8017 9. Margolin AL, Klibanov AM (1987) J Am Chem Soc 109: 3802 10. Hedström G, Slotte JP, Bachlund M, Molander O, Rosenholm JB (1992) Biocatalysis 6: 282 11. Nakamura K, Chi YM, Yamada Y, Yano T (1986) Chem Eng Comm 45: 207 12. Kamat S, Barrera J. Beckman EJ, Russell A (1992) Biotech Bioeng 40: 158 13. Stinson SC (1993) Chcm & Eng News, Sept. 27, 38. 14. Hu S-Y (1969) Econ Botany 23: 346 15. Sorensen GG. Spenser ID (1988) J Am Chem Soc 110: 3714 16. Sorensen GG, Spenser ID (1989) Can J Chem 67: 998 17. Astrup A. Breum L, Toubro S, Hein P, Quaade F (1992) Int J Obesity 16(4): 269 18. Voets JP, Vandamme EJ, Vlerick C (1973) Z Allg Mikrobiol 13: 355 19. Vojtisek Netrval J,V, Vojtisek Eur J Microbiol Appl Microbiol Biotechnol 16: 35 20. NetrvalVJ (1982) (1982) Folia 27: 173 21. Culic J. Ulbrecht S, Vojtisek V, Vodansky M (1984) Method of cost re reduction duction in the  production of D-(-)-phenyl-l-hydrox -(-)-phenyl-l-hydroxy-2-propane y-2-propane for the production of L-(-) ephedrine. Czech Patent No. 22941 22. Mahmoud WM. El-Sayed AH, Coughlin RW (1990) Biotech Bioeng 36: 55 23 Seely RJ, Heefner DL, Hageman RW, Yarus MJ, Sullivan SA (1989) Process for producing L-PAC. An immobilized cell mass for use in the process and method for preparing cell mass. US Patent No. PCT/US89/64421 24. Mahmoud WM, El-Sayed AH, Coughlin RW (1990) Biotech Bioeng 36: 256 25. Seely RJ. Hageman RV, Yarus MJ. Sullivan SA (1989) Process for making L-PAC. Microorganisms for use in the process and method for preparing the microorganism. US Patent  No. PCT US 89/04423 26. Long A, Ward OP (1989) J Ind Microbiol 4: 49 27. Long A, James P, Ward OP (1989) Biotech Bioeng 33: 657 28. Long A, Ward OP (1989) Biotech Bioeng 34: 933

 

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living through Engineering. Press, Singapore, p.249 36. Rohner M,Innovative Locher G, Biochemical Sonnleitner B, Fiechter A Continental (1988) (1988) J Biotechnol 9: 11 37. Rohner M, Locher G, Sonnleitner B, Fiecht Fiechter er A (1990) Biocatalysis 3: 37 38. Mahmoud WM, El-Sayed AH, Coughl Coughlin in RW (1990) Biotech Bioeng 36 36:: 47 39. Shin HS, Rogers PL (1995) Appl Microbiol Biotechnol 44: 44: 7 40. Bringer-Meyer S, Sahm H (1 (1988) 988) Biocatalysis 1: 321 41. Shin HS, Rogers PL (1996) Biotech Bi Bioeng oeng 49: 52 42. Ullrich J, Donner I (1970) Ho Hoppe-Seyler’s ppe-Seyler’s Z Physiol Chem 3 351: 51: 1030 43. Bioteux A, Hess B (1970) FEBS Letters 9(5) : 293 44. Lehmann H, Fisher G, Hubner G, Kohn Kohnert ert KD, Schellenberger A (1973) E Eur ur J Biochem 32: 83 45. Urk H, Schipper D, Breedveld GJ, Paul RM, Scheffers WA WA,, van Dijken JP (1989) Biochim Biochim Biophys Acta 992: 78 46. Scopes RK (1989) In: van Un Unden den N (ed), Alcohol tox toxicity icity in yeast and bacteria, CRC Press Inc, p. 89 47. Jencks Wp (1975) In: Mei Meister ster A (ed), Advances in Enymol Enymology ogy and Related Areas of Molecular Biology, Wiley, New York, Vol. 43, p. 219 48. Perry RH (1984) Chemical Engineering Handbook, Handbook, 6th Edn, McGraw-Hill International Edition, 3-27 49. Shin HS, Rogers PL (1996) Biotech Bi Bioeng oeng 49: 429 50. Buisson D, El-Baba S, Azered R (1986) Tetrahed Tetrahedron ron Lett 27: 4453 51. Drewke C, Ciriacy M (19 (1988) 88) Biochim Biophys Biophys Acta 950: 54 52. Besnainou B, Giani D, Sahut C (1990) Method for producing pyruvic acid by fermentation. US Patent No. 4,918,013 53. Wang B (1993) Kinetic study of fed-batch and continuous bi bioconversion oconversion process for L phenylacetylcarbinoll (L-PAC) production by the  phenylacetylcarbino the yeast Candida utilis. utilis. PhD Thesis, University of  New South Wales, Sydney, Australia Australia