Isolation of l-phenylalanine dehydrogenase from Rhodococcus sp. M4 and its application for the production of l-phenylalanine

Summary l-Phenylalanine dehydrogenase [l-phenylalanine: NAD⁺-oxidoreductase (deaminating)] of Rhodococcus sp. strain M4 was studied emphasizing its application for the production of l-phenylalanine. A high enzyme level (30,000 U·l^-1, 25–30 U·mg^-1 in the crude extract) could be reached during aerob degradation of l-phenylalanine (10 g·l^-1) under optimized growth coditions. A partial purification of the intracellular enzyme by liquid-liquid extraction, and DEAE-cellulose led to a specific activity of more than 1300 U·mg^-1. The continuous production of l-phenylalanine in an enzyme-membrane-reactor for 350h resulted in a space-time yield of 456 g·l^-1·d^-1 with a mean substrate conversion of 95%. Consumption of phenylalanine dehydrogenase was 1,500 U·kg Phe^-1.Abbreviations BSA bovine serum albumine - pheDH l-phenylalanine dehydrogenase - phepyr phenylpyruvate - OD optical density - FDH formate dehydrogenase     

Synthesis of l-dopa by escherichia intermedia cells immobilized in a polyacrylamide gel

Summary Escherichia intermedia cells were immobilized by entrapment in a polyacrylamide gel and used for l-dopa synthesis from pyrocatechol, pyruvate and ammonia. An immobilized cell preparation containing 75 mg cells/g gel retained 45%–50% of the activity of free cells. The effect of temperature, pH and substrate concentration of the initial rate of l-dopa synthesis was very similar for free and immobilized cells. Substrate inhibition was observed for pyrocatechol, pyruvate and ammonia. In a batch reactor, 5.4 g·l^-1 l-dopa was obtained, with 100% conversion yield of pyrocatechol and l-dopa productivity of 0.18 g·l^-1·h^-1. The use of a pyrocatechol-borate complex decreased by-product formation and catalyst inactivation.     

Comparative study of the enzymatic synthesis of l-valine by purified enzymes,crude extract,intact or permeabilized cells from Bacillus megaterium

Summary A detailed study on the reductive amination of -ketoisovalerate to l-valine by l-valine dehydrogenase using glucose dehydrogenase as an NADH regeneration enzyme was performed. The presence of both enzyme activities in Bacillus megaterium ATCC 39 118 permitted a direct and systematic comparison of the performances (initial l-valine production rate, productivity, molar conversion yield) of different types of conversion systems: purified enzymes or crude extract and whole cells, intact or permeabilized. A maximal l-valine productivity of 8 mmol·l^–1 · h^–1 was obtained using purified enzymes which constituted the most efficient system with a maximal rate of 0.87 mol · ml^–1 · min^–1 and a molar conversion yield of 0.91. Permeabilized cells were also an attractive system because of their easy preparation and of the good performances attained.Offprint requests to: F. Monot     

Fermentation of glycerol to 1,3-propanediol in continuous cultures of Citrobacter freundii

The conversion of glycerol to 1,3-propanediol by Citrobacter freundii DSM 30040 was optimized in single- and two-stage continuous cultures. The productivity of 1,3-propanediol formation was highest under glycerol limitation and increased with the dilution rate (D) to a maximum of 3.7 g·l^–1·h^–1. Glycerol dehydratase seemed to be the rate-limiting step in 1,3-propanediol formation. Conditions for the two-stage fermentation process were as follows: first stage, glycerol limitation (250mM), pH 7.2, D=0.1 h^–, 31° C; second stage, additional glycerol, pH 6.6, D=0.05 h^–1, 28° C. Under these conditions 875mM glycerol were consumed, the final 1,3-propanediol concentration was 545mM, and the overall productivity 1.38 g·1^–1·h^–1. Correspondence to: G. Gottschalk     

Direct alcoholic fermentation of starchy biomass using amylolytic yeast strains in batch and immobilized cell systems

Summary Direct alcoholic fermentation of dextrin or soluble starch with selected amylolytic yeasts was studied in both batch and immobilized cell systems. In batch fermentations, Saccharomyces diastaticus was capable of fermenting high dextrin concentrations much more efficiently than Schwanniomyces castellii. From 200 g·l^–1 of dextrin S. diastaticus produced 77 g·l^–1 of ethanol (75% conversion efficiency). The conversion efficiency decreased to 59% but a higher final ethanol concentration of 120 g·l^–1 was obtained with a medium containing 400 g·l^–1 of dextrin. With a mixed culture of S. diastaticus and Schw. castellii 136 g·l^–1 of ethanol was produced from 400 g·l^–1 of dextrin (67% conversion efficiency). S. diastaticus cells attached well to polyurethane foam cubes and a S. diastaticus immobilized cell reactor produced 69 g·l^–1 of ethanol from 200 g·l^–1 of dextrin, corresponding to an ethanol productivity of 7.6g·l^–1·h^–1. The effluent from a two-stage immobilized cell reactor with S. diastaticus and Endomycopsis fibuligera contained 70 g·l^–1 and 80 g·l^–1 of ethanol using initial dextrin concentrations of 200 and 250 g·l^–1 respectively. The corresponding values for ethanol productivity were 12.7 and 9.6 g·l^–1·h^–1. The productivity of the immobilized cell systems was higher than for the batch systems, but much lower than for glucose fermentation.     

Physiological aspects of l-lysine production: effect of nutritional limitations on a producing strain of Corynebacterium glutamicum

The effect of nutritional limitations, such as phosphorus and carbon, on the production of l-lysine by Corynebacterium glutamicum was studied in continuous culture. We observed that phosphate-limited cultures at low growth rates were favourable to l-lysine production. l-Lysine was produced when a culture at low dilution rate (0.03 h^–1) was established. A dilution rate of about 0.04 h^–1 should be maintained in order to assure good productivity and an l-lysine yield of 0.53 g/g. Under carbon-limiting conditions the maintenance energy and growth yield of 0.03 g/g·g^–1·h^–1 and 0.41 g/g, respectively, have been obtained. Under these limiting conditions the l-lysine production was not favoured even at lower dilution rates.Correspondence to: N. Coello     

Studies on the variables and kinetics of SCP production from nopal fruit juice

Summary Submerged batch cultivation under controlled environmental conditions of pH 3.8, temperature 30°C, and K_La200 h^–1 (above 180 mMO₂ l ^–1 h^–1 oxygen supply rate) produced a maximum (12.0 g·l ^–1) SCP (Candida utilis) yield on the deseeded nopal fruit juice medium containing C/N ratio of 7.0 (initial sugar concentration 25 g·l ^–1) with a yield coefficient of 0.52 g cells/g sugar. In continuous cultivation, 19.9 g·l ^–1 cell mass could be obtained at a dilution rate (D) of 0.36 h^–1 under identical environmental conditions, showing a productivity of 7.2 g·l ^–1·h^–1. This corresponded to a gain of 9.0 in productivity in continuous culture over batch culture. Starting with steady state values of state variables, cell mass (C_X–19.9 g·l ^–1), limiting nutrient concentration (C_ln–2.5 g·l ^–1) and sugar concentration (C_S–1.5 g·l ^–1) at control variable conditions of pH 3.8, 30°C, and K_La 200 h^–1 keeping D=0.36 h^–1 as reference, transient response studies by step changes of these control variables also showed that this pH, temperature and K_La conditions are most suitable for SCP cultivation on nopal fruit juice. Kinetic equations obtained from experimental data were analysed and kinetic parameters determined graphically. Results of SCP production from nopal fruit juice are described.Nomenclature C_ln concentration of ammonium sulfate (g·l ^–1) - C_S concentration of total sugar (g·l ^–1) - C_X cell concentration (g·l ^–1) - D dilution rate (h^–1) - K_ln Monod's constant (g·l ^–1) - m maintenance coefficient (g ammonium sulfate cell^–1 h^–1) - m_(S) maintenance coefficient (g sugar g cell^–1 h^–1) - t time, h - Y yield coefficient (g cells/g ammonium sulfate) - Y_m maximum of Y - Y_S yield coefficient based on sugar consumed (g cells · g sugar^–1) - Y_S(m) maximum value of Y_S - ^µm maximum specific growth rate constant (h^–1)     

Production of l-phenylalanine from phenylpyruvate by Paracoccus denitrificans containing aminotransferase activity

Summary To establish an efficient production method for l-phenylalanine, the production of l-phenylalanine from phenylpyruvate by Paracoccus denitrificans pFPr-1 containing aminotransferase activity was investigated. By using intact cells, 0.74M l-phenylalanine was produced from 0.8M phenylpyruvate (conversion yield, 92.5%). Moreover, by using immobilized cells with -carrageenan, when the space velocity was 0.1 h^-1 at 30°C, 0.135 M l-phenylalanine was produced from 0.15 M phenylpyruvate (conversion yield, 90%). The half-life of the l-phenylalanine-forming activity of the column was estimated to be about 30 days at 30°C.     

Production of <Emphasis Type="SmallCaps">l</Emphasis>-phenylalanine from glycerol by a recombinant <Emphasis Type="Italic">Escherichia coli</Emphasis>

The production of l-phenylalanine is conventionally carried out by fermentations that use glucose or sucrose as the carbon source. This work reports on the use of glycerol as an inexpensive and abundant sole carbon source for producing l-phenylalanine using the genetically modified bacterium Escherichia coli BL21(DE3). Fermentations were carried out at 37°C, pH 7.4, using a defined medium in a stirred tank bioreactor at various intensities of impeller agitation speeds (300–500 rpm corresponding to 0.97–1.62 m s⁻¹ impeller tip speed) and aeration rates (2–8 L min⁻¹, or 1–4 vvm). This highly aerobic fermentation required a good supply of oxygen, but intense agitation (impeller tip speed ~1.62 m s⁻¹) reduced the biomass and l-phenylalanine productivity, possibly because of shear sensitivity of the recombinant bacterium. Production of l-phenylalanine was apparently strongly associated with growth. Under the best operating conditions (1.30 m s⁻¹ impeller tip speed, 4 vvm aeration rate), the yield of l-phenylalanine on glycerol was 0.58 g g⁻¹, or more than twice the best yield attainable on sucrose (0.25 g g⁻¹). In the best case, the peak concentration of l-phenylalanine was 5.6 g L⁻¹, or comparable to values attained in batch fermentations that use glucose or sucrose. The use of glycerol for the commercial production of l-phenylalanine with E. coli BL21(DE3) has the potential to substantially reduce the cost of production compared to sucrose- and glucose-based fermentations.     

Enhancement of biomass and fermentation activity of surplus brewers' yeast in a fed-batch process

The growth of surplus brewers' yeast in a fed-batch process was studied with the aim of increasing the fermentation activity of the yeast cells and of optimizing the growth conditions: 20 h cultivation at 30° C and pH 5.0–5.5 using beet molasses as substrate, with a regulated feeding rate, showed satisfactory results. Under the chosen conditions, the final amount of biomass increased more than fivefold, achieving a specific growth rate of 0.1 h^–1 and substrate yield coefficient of 0.54 g·g^–1. The increase in fermentation activity of yeast cells during cultivation correlated very well with the concentration of reduced glutathione, which increased from 1.2 to 2.7 mg·g^–1 (dry matter). At the same time the fermentation activity increased fivefold, which related to the nitrogen content of the yeast cells. Ethanol formation throughout the cultivation did not exceed 0.5 g·l^–1. Correspondence to: B. Strel     

Fermentative production of 1,3-propanediol from glycerol by Clostridium butyricum up to a scale of 2m3

Summary The conversion of glycerol to 1,3-propanediol (PD) by Clostridium butyricum DSM 5431 was studied in anaerobic culture. Growth and product formation were optimal at pH = 7.0 and T = 35° C, while aeration rate and stirrer speed were found to have no significant influence. As increasing amounts of initial glycerol led to inhibition of growth, cultivations were done in fed-batch operation. Comparative cultivations were carried out in an air-lift (ALR) and a stirred-tank reactor (STR) having equal working volumes (V _L = 30 l) and no difference in product formation was found. The process was scaled up to reactor sizes of 1.2 m³ (ALR) and 2.0 m³ (STR). The same results were obtained irrespective of reactor volume as well as reactor type (STR/ALR). PD concentrations of approximately 50–58 g·l^–1 and overall productivities of 2.3–2.9 g·l^–1 ·h^–1 could be reached. Offprint requests to: W.-D. Deckwer     

Factors affecting the production of <Emphasis Type="SmallCaps">l</Emphasis>-xylulose by resting cells of recombinant <Emphasis Type="Italic">Escherichia coli</Emphasis>

Factors affecting the production of the rare sugar l-xylulose from xylitol using resting cells were investigated. An E. coli BPT228 strain that recombinantly expresses a gene for xylitol dehydrogenase was used in the experiments. The ratio of xylitol to l-xylulose was three times lower in the cytoplasm than in the medium. The effects of pH, temperature, shaking speed, and initial xylitol concentration on l-xylulose production were investigated in shaking flasks using statistical experimental design methods. The highest production rates were found at high shaking speed and at high temperature (over 44°C). The optimal pH for both productivity and conversion was between 7.5 and 8.0, and the optimal xylitol concentration was in the range 250–350 g l⁻¹. A specific productivity of 1.09 ± 0.10 g g⁻¹ h⁻¹ was achieved in a bioreactor. The response surface model based on the data from the shake flask experiments predicted the operation of the process in a bioreactor with reasonable accuracy.     

2,3-Butanediol production from Jerusalem artichoke,Helianthus tuberosus,by Bacillus polymyxa ATCC 12 321. Optimization of k L a profile

Summary Optimization of d-(-)-2,3-butanediol production from the Jerusalem artichoke, Helianthus tuberosus, by Bacillus polymyxa ATCC 12 321 is described. The effects of initial sugar concentration and oxygen transfer rate were examined. The latter appears to be the most important parameter affecting the kinetics of the process. The best results (44 g·l^-1 2,3-butanediol, productivity of 0.79 g·l^-1·h^-1) were obtained by setting an optimal k _L a profile during batch culture.     

l-Ribulose production by an Escherichia coli harboring l-arabinose isomerase from Bacillus licheniformis

Recombinant Escherichia coli harboring the l-arabinose isomerase (BLAI) from Bacillus licheniformis was used as a biocatalyst to produce l-ribulose in the presence of borate. Effects of substrate concentration, the borate to l-arabinose ratio, pH, and temperature on the conversion of l-arabinose to l-ribulose were investigated. l-Ribulose production was efficient when pH was higher than 9 and temperature was higher than 50 °C. Borate addition to the reaction mixture was essential for high conversion of l-arabinose to l-ribulose as it resulted in an equilibrium shift in favor of the product. Under the optimal conditions determined by response surface methodology, the E. coli harboring BLAI produced 375 g l⁻¹ L-ribulose from 500 g l⁻¹ l-arabinose at a reaction time of 60 min, corresponding to a conversion yield of 75% and productivity of 375 g l⁻¹ h⁻¹. When the resting recombinant E. coli cells were recycled, 85% of the yield was obtained even after seven cycles of reuse. The productivity and final concentration of l-ribulose obtained in the present study were the highest yet reported.     

Factors which influence the sedimentation characteristics of Torulopsis glabrata after growth in a recirculation system

Summary Some environmental affects on cell aggregation described in the literature are briefly summarized. By means of a biomass recirculation culture (Contact system), using the yeast Torulopsis glabrata, the aggregation behavior of cells in static and in dynamic test systems is described. Sedimentation times required to obtain 50 g · l^–1 yeast dry matter in static systems were always higher than in dynamic ones.In addition to, influencing the biomass yield, the specific growth rate of the yeast also affected cell aggregation. The specific growth rate and therefore the aggregation could be regulated by the biomass recirculation rate as well as by the sedimenter volume.Abbreviations f_o Overflow flow rate (l·h^–1) - f_R Recycle flow rate (l·h^–1) - f_t0t Total flow rate through the fermenter (l·h^–1) - g Gram - h Hour - D_R Fermenter dilution rate due to recycle (h^–1) - D_S Fermeter dilution rate due to substrate (h^–1) - D_tot Total fermenter dilution rate (h^–1) - l Liter - Specific growth rate (h^–1) - P_F Fermenter productivity (g·l^–1·h^–1) - P_FS Overall productivity (g·l^–1·h^–1) - R_pM Rates per minute - RS Residual sugar content in the effluent with respect to the substrate concentration (%) - Y Yield of biomass with respect to sugar concentration (%) - Sed 50 Sedimentation time to reach a YDM of 50 g·l^–1 (min) - V Volume (l) - V_F Fermenter volume (l) - V_Sed Sedimenter volume (l) - VVM Volumes per volume and minute - X_F YDM in the fermenter (g·l^–1) - X_F YDM in the recycle (g·l^–1) - X_S Yeast dry matter due to substrate concentration (g·l^–1) - YDM Yeast dry matter (g·l^–1)     

Production of lipid from starch by a nitrogen-controlled mixed culture of Saccharomycopsis fibuliger and Rhodosporidium toruloides

Summary Production of lipid from starch in a two-component mixed culture in a fed batch process was studied. Saccharomycopsis fibuliger was used as the amylolytic microorganism and Rhodosporidium toruloides, which does not grow on starch, as the lipid producer. The concentration of nitrogen can be used as an external regulator of growth and competition in this process. The total biomass concentration decreased and the relative amount of Rh. toruloides increased with decreasing initial concentration of nitrogen in the medium. The highest lipid concentration (9.7 g·l^-1), highest overall lipid production rate (0.15 g·l^-1·h^-1) and highest concentration of lipid in biomass (36.5%) were obtained in cultures with an initial nitrogen concentration of 0.5 g·l^-1. Compared to monocultures of Lipomyces starkeyi and Aspergillus oryzae on starch, the mixed culture showed slightly lower conversion of starch to lipid but was superior in the final lipid concentration and the overall lipid production rate.     

The production of 2,3-butanediol by fermentation of high test molasses

Summary Klebsiella oxytoca fermented 199 g·l^–1 high test or invert molasses using batch fermentation with substrate shift to produce 95.2–98.6 g 2,3-butanediol·l^–1 and 2,4–4.3 g acetoin·l^–1 with a diol yield of 96–100% of the theoretical value and a diol productivity of 1.0–1.1 g·l^–1·h^–1. Fermentation was performed numerous times with molasses in repeated batch culture with cell recovery. Such repeated batch fermentation, in addition to a high product yield, also showed a very high product concentration. For example, 118 g 2,3-butanediol·l^–1 and 2.3 g acetoin·l^–1 were produced from 280 g·l^–1 of high test molasses. The diol productivity in this fermentation amounted to 2.4 g·l^–1·h^–1 and can undoubtedly be further increased by increasing the cell concentration. Because the Klebsiella cultures ferment 2,3-butanediol at an extremely high rate once the sugar has been consumed, the culture was inhibited completely by the addition of 15 g ethanol·l^–1 and switching off aeration. Offprint requests to: A. S. Afschar     

Fermentative production of l-lactic acid by Lactobacillus casei DSM 20011 and product recovery using ion exchange resins

In order to produce l(+)-lactic acid to be employed in poly-l-lactic acid polymer production, for biomedical applications, the strain Lactobacillus casei subsp. casei DSM 20011 was studied in a conventional batch mode using different initial concentrations of glucose. The results obtained showed that the initial glucose concentration exerts an influence on the fermentation pattern, modifying the different fermentation parameters. Nevertheless, the product yield remained at a constant value of 0.86 g·g^–1. The proposed novel system of product recovery, based on the use of ion-exchange resins, gave high yields of pure lactic acid. Correspondence to: D. Matteuzzi     

Cell recovery by continuous flotation

Summary Cell recovery by means of continuous flotation of the Hansenula polymorpha cultivation medium without additives was investigated as a function of the cultivation conditions as well as of the flotation equipment construction and flotation operational parameters. The cell enrichment and separation is improved at high liquid residence times, high aeration rates, small bubble sizes, increasing height of the aerated column, and diameter of the foam column. Increasing cell age and cultivation with nitrogen limitation reduce the cell separation.Symbols C_P cell mass concentration in medium g·l^–1 - C_R cell mass concentration in residue g·l^–1 - C_S cell mass concentration in foam liquid g·l^–1 - V equilibrium foam volume cm³ - V gas flow rate through the aerated liquid column cm³·s^–1 - V_F feed rate to the flotation column ml/min - ¹ V _S/V foaminess s - mean liquid residence time in the column s     

Formic acid production from H2 and bicarbonate by a formateutilizing methanogen

Summary Resting cells of a formate-utilizing methanogen (strain HU) were used as a biocatalyser for formic acid production from H₂ and bicarbonate. In the presence of methyl viologen, a potent inhibitor of methanogenesis, the cells could accumulate formic acid in the reaction mixture, whereas methane was produced in the absence of the inhibitor. Under optimal conditions (pH 8.0, 32°C, 100% H₂ gas phase), 674 mmol·l^-1 of formic acid (31 g·l^-1 yield; 33% conversion of bicarbonate) was obtained at about 0.7 atm of gas pressure. When the reaction was carried out in an ultrafiltration vessel with a hydrogen pressure of 3 atm, a final product concentration of 1.02 mol·l^-1 (47 g·l^-1 yield, 51% conversion) could be obtained, indicating that the hydrogen lyase system of this methanogen has a high tolerance to formic acid, bicarbonate and hydrogen. The results obtained in this work open a new perspective for the utilization of methanogens for processes other than methane production.