Scalable biocatalytic synthesis of optically pure ethyl (R)-2-hydroxy-4-phenylbutyrate using a recombinant E. coli with high catalyst yield

Ethyl (R)-2-hydroxy-4-phenylbutanoate [(R)-HPBE] is a versatile and important chiral intermediate for the synthesis of angiotensin-converting enzyme (ACE) inhibitors. Recombinant E. coli strain coexpressing a novel NADPH-dependent carbonyl reductase gene iolS and glucose dehydrogenase gene gdh from Bacillus subtilis showed excellent catalytic activity in (R)-HPBE production by asymmetric reduction. IolS exhibited high stereoselectivity (>98.5% ee) toward α-ketoesters substrates, whereas fluctuant ee values (53.2–99.5%) for β-ketoesters with different halogen substitution groups. Strategies including aqueous/organic biphasic system and substrate fed-batch were adopted to improve the biocatalytic process. In a 1-L aqueous/octanol biphasic reaction system, (R)-HPBE was produced in 99.5% ee with an exceptional catalyst yield (gproduct/gcatalyst) of 31.7 via bioreduction of ethyl 2-oxo-4-phenylbutyrate (OPBE) at 330 g/L.     

A two-step enzymatic resolution of glycidyl butyrate

A two-step enzymatic resolution process for production of (R)- and (S)-glycidyl butyrate was investigated and the lipases were screened. The first step involved a hydrolysis of (R,S)-glycidyl butyrate catalyzed by porcine pancreatic lipase (S-favored) with an E of 21 for production of (R)-glycidyl butyrate (13.2 mmol, 98% ee, 36% yield) under the optimal conditions (pH 7.4, 30 °C, 30 mg/ml CTAB). Then, the recovered (R)-enriched glycidol (19.8 mmol, 65% ee, 56% yield) was used for transesterification catalyzed by Novozym 435 (R-favored) with an E of 69 to obtain (S)-glycidyl butyrate (15.1 mmol, 98% ee, 42% yield) under the optimum conditions (a_W = 0.24, n-heptane, 80 min).     

Harnessing the respiration machinery for high-yield production of chemicals in metabolically engineered Lactococcus lactis

When modifying the metabolism of living organisms with the aim of achieving biosynthesis of useful compounds, it is essential to ensure that it is possible to achieve overall redox balance. We propose a generalized strategy for this, based on fine-tuning of respiration. The strategy was applied on metabolically engineered Lactococcus lactis strains to optimize the production of acetoin and (R,R)-2,3-butanediol (R-BDO). In the absence of an external electron acceptor, a surplus of two NADH per acetoin molecule is produced. We found that a fully activated respiration was able to efficiently regenerate NAD⁺, and a high titer of 371 mM (32 g/L) of acetoin was obtained with a yield of 82% of the theoretical maximum. Subsequently, we extended the metabolic pathway from acetoin to R-BDO by introducing the butanediol dehydrogenase gene from Bacillus subtilis. Since one mole of NADH is consumed when acetoin is converted into R-BDO per mole, only the excess of NADH needs to be oxidized via respiration. Either by fine-tuning the respiration capacity or by using a dual-phase fermentation approach involving a switch from fully respiratory to non-respiratory conditions, we obtained 361 mM (32 g/L) R-BDO with a yield of 81% or 365 mM (33 g/L) with a yield of 82%, respectively. These results demonstrate the great potential in using finely-tuned respiration machineries for bio-production.     

Kinetic modeling and implementation of superior process strategies for β-galactosidase production during submerged fermentation in a stirred tank bioreactor

This paper reports development and implementation of superior fermentation strategies for β-galactosidase production by Lactobacillus acidophilus in a stirred-tank bioreactor. Process parameters (aeration and agitation) were optimized for the process by application of Central Composite Design. Aeration rate of 0.5 vvm and agitation speed of 250 rpm were most suitable for β-galactosidase production (2001.2 U/L). Further improvement of the operation in pH controlled environment resulted in 2135 U/L of β-galactosidase with productivity of 142.39 U/L h. Kinetic modeling for biomass and enzyme production and substrate utilization were carried out at the aforementioned pH controlled conditions. The logistic regression model (X₀ = 0.01 g/L; X_max = 2.948 g/L; μ_max = 0.59/h; R² = 0.97) was used for mathematical interpretation of biomass production. Mercier's model proved to be better than Luedeking–Piret model in describing β-galactosidase production (P₀ = 0.7942 U/L; P_max = 2169.3 U/L; P_r = 0.696/h; R² = 0.99) whereas the latter was more efficient in mathematical illustration of lactose utilization (m = 0.187 g/g h; Y_x/s = 0.301 g/L; R² = 0.98) among the two used in this study. Strategies like fed-batch fermentation (3694.6 U/L) and semi-continuous fermentation (5551.9 U/L) further enhanced β-galactosidase production by 1.8 and 2.8 fold respectively.     

Metabolic engineering of Clostridium tyrobutyricum for enhanced butyric acid production from glucose and xylose

Clostridium tyrobutyricum is a promising microorganism for butyric acid production. However, its ability to utilize xylose, the second most abundant sugar found in lignocellulosic biomass, is severely impaired by glucose-mediated carbon catabolite repression (CCR). In this study, CCR in C. tyrobutyricum was eliminated by overexpressing three heterologous xylose catabolism genes (xylT, xylA and xlyB) cloned from C. acetobutylicum. Compared to the parental strain, the engineered strain Ct-pTBA produced more butyric acid (37.8 g/L vs. 19.4 g/L) from glucose and xylose simultaneously, at a higher xylose utilization rate (1.28 g/L·h vs. 0.16 g/L·h) and efficiency (94.3% vs. 13.8%), resulting in a higher butyrate productivity (0.53 g/L·h vs. 0.26 g/L·h) and yield (0.32 g/g vs. 0.28 g/g). When the initial total sugar concentration was ~120 g/L, both glucose and xylose utilization rates increased with increasing their respective concentration or ratio in the co-substrates but the total sugar utilization rate remained almost unchanged in the fermentation at pH 6.0. Decreasing the pH to 5.0 significantly decreased sugar utilization rates and butyrate productivity, but the effect was more pronounced for xylose than glucose. The addition of benzyl viologen (BV) as an artificial electron carrier facilitated the re-assimilation of acetate and increased butyrate production to a final titer of 46.4 g/L, yield of 0.43 g/g sugar consumed, productivity of 0.87 g/L·h, and acid purity of 98.3% in free-cell batch fermentation, which were the highest ever reported for butyric acid fermentation. The engineered strain with BV addition thus can provide an economical process for butyric acid production from lignocellulosic biomass.     

Efficient production of glycyrrhetic acid 3-O-mono-β-d-glucuronide by whole-cell biocatalysis in an ionic liquid/buffer biphasic system

Hydrolysis of glycyrrhizin (GL) to glycyrrhetic acid 3-O-mono-β-d-glucuronide (GAMG) by whole-cell biocatalysts in a system containing non-conventional solvents was performed. Three whole-cell biocatalysts were used, including wild-type Penicillium purpurogenum Li-3 (w-PGUS) and recombinant strains Escherichia coli BL21 and Pichia pastoris GS115. The biotransformation of GL to GAMG by w-PGUS in a 1-butyl-3-methylimidazolium hexafluorophosphate ([Bmim]PF₆)/buffer biphasic system was the main focus of this study because w-PGUS showed a higher GAMG yield and a higher relative activity in this system than the other two whole-cell biocatalysts. Using the optimized reaction conditions determined as a pH 5.2 buffer, a 6.0 mM substrate concentration, a reaction temperature of 30 °C, and a 60 g/L (1.23 U/g) cell concentration, a GAMG yield of 87.63% was achieved after 60 h. After eight reaction cycles, [Bmim]PF₆ retained a high recovery percentage (85.48%)_[0], indicating the reusability of this IL. The biotransformation activity of w-PGUS was not significantly affected, even after two batch reaction cycles. Furthermore, the product GAMG and the byproduct glycyrrhetinic acid were spontaneously separated in the biphasic system. In conclusion, the combination of whole cells and ionic liquid is a promising approach for economical and industrial-scale production of GAMG.     

Mixed culture of Saccharomyces cerevisiae and Acetobacter pasteurianus for acetic acid production

Mixed culture of Saccharomyces cerevisiae and Acetobacter pasteurianus was carried out for high yield of acetic acid. Acetic acid production process was divided into three stages. The first stage was the growth of S. cerevisiae and ethanol production, fermentation temperature and aeration rate were controlled at 32 °C and 0.2 vvm, respectively. The second stage was the co-culture of S. cerevisiae and A. pasteurianus, fermentation temperature and aeration rate were maintained at 34 °C and 0.4 vvm, respectively. The third stage was the growth of A. pasteurianus and production of acetic acid, fermentation temperature and aeration rate were controlled at 32 °C and 0.2 vvm, respectively. Inoculation volume of A. pasteurianus and S. cerevisiae was 16% and 0.06%, respectively. The average acetic acid concentration was 52.51 g/L under these optimum conditions. To enhance acetic acid production, a glucose feeding strategy was subsequently employed. When initial glucose concentration was 90 g/L and 120 g/L glucose was fed twice during fermentation, acetic acid concentration reached 66.0 g/L.     

Production of microbial lipid by Cryptococcus curvatus on rice straw hydrolysates

Microbial biolipids/biodiesels derived from volatile fatty acids (VFAs) can be a valuable alternative to plant oils if optimum fermentation conditions are determined. VFAs were used for cell mass and microbial lipid production by Cryptococcus curvatus. The lipid content in the cells increased up to 48% and 28% in batch cultures with the use of 20 g/L glucose and 6 g/L of VFAs as the carbon source, respectively. In this study, C. curvatus used VFAs as a carbon source via anaerobic digestion of rice straw hydrolysates. VFAs produced from rice straw resulted in yield of 0.43 g VFAs/g substrate and 40% higher specific growth rate(0.305 h⁻¹) than synthetic VFAs. The highest fatty acid composition observed was C18:1, was obtained using glucose and VFAs as the carbon source to yield a cetane number of 56–59, which is suitable for biodiesel production. The cost of microbial lipids was estimated to be 0.30–1.15 USD/L given 0–150 USD/ton of VFAs cost for a yield of 0.17 g/g of lipids. Thus, VFAs can be a suitable carbon source for economical biodiesel production.     

Production of 1,3-propanediol, 2,3-butanediol and ethanol by a newly isolated Klebsiella oxytoca strain growing on biodiesel-derived glycerol based media

The production of 1,3-propanediol, 2,3-butanediol and ethanol was studied, during cultivations of strain Klebsiella oxytoca FMCC-197 on biodiesel-derived glycerol based media. Different kinds of glycerol feedstocks and experimental conditions had an important impact upon the distribution of metabolic products; production of 1,3-propanediol was positively influenced by stable pH conditions and by the absence of N₂ gas infusions throughout the fermentation. Thus, during batch bioreactor fermentations conducted at increasing glycerol concentrations, 1,3-propanediol at 41.3 g/L and yield ～47% (w/w) was achieved at initial glycerol concentration ～120 g/L. At even higher initial glycerol media (150 and 170 g/L), growth was not ceased, but 1,3-propanediol production declined. During fed-batch fermentation under optimal experimental conditions, 126 g/L of glycerol were converted into 50.1 g/L of 1,3-propanediol. In this experiment, also 25.2 g/L of ethanol (conversion yield ～20%, w/w) were formed. A batch-bioreactor culture was performed under non-sterilized conditions and the 1,3-propanediol production was almost equivalent to the sterilized process. Concerning 2,3-butanediol formation, the most detrimental parameter was the absence of N₂ sparging and as a result, no 2,3-butanediol was produced. The presence of glucose as co-substrate seriously enhanced 2,3-butanediol production; when commercial glucose was employed as sole substrate, 32.1 g/L of 2,3-butanediol were formed.     

A laboratory study of producing docosahexaenoic acid from biodiesel-waste glycerol by microalgal fermentation

Crude glycerol is the primary by-product in the biodiesel industry, which is too costly to be purified into to higher quality products used in the health and cosmetics industries. This work investigated the potential of using the crude glycerol to produce docosahexaenoic acid (DHA, 22:6 n-3) through fermentation of the microalga Schizochytrium limacinum. The results showed that crude glycerol supported alga growth and DHA production, with 75–100 g/L concentration being the optimal range. Among other medium and environmental factors influencing DHA production, temperature, trace metal (PI) solution concentration, ammonium acetate, and NH₄Cl had significant effects (P < 0.1). Their optimal values were determined 30 mL/L of PI, 0.04 g/L of NH₄Cl, 1.0 g/L of ammonium acetate, and 19.2 °C. A highest DHA yield of 4.91 g/L with 22.1 g/L cell dry weight was obtained. The results suggested that biodiesel-derived crude glycerol is a promising feedstock for production of DHA from heterotrophic algal culture.     

Use of Saccharum spontaneum (wild sugarcane) as biomaterial for cell immobilization and modulated ethanol production by thermotolerant Saccharomyces cerevisiae VS3

Saccharum spontaneum is a wasteland weed consists of 45.10 ± 0.35% cellulose and 22.75 ± 0.28% of hemicellulose on dry solid (DS) basis. Aqueous ammonia delignified S. spontaneum yielded total reducing sugars, 53.91 ± 0.44 g/L (539.10 ± 0.55 mg/g of substrate) with a hydrolytic efficiency of 77.85 ± 0.45%. The enzymes required for hydrolysis were prepared from culture supernatants of Aspergillus oryzae MTCC 1846. A maximum of 0.85 ± 0.07 IU/mL of filter paperase (FPase), 1.25 ± 0.04 IU/mL of carboxy methyl cellulase (CMCase) and 55.56 ± 0.52 IU/mL of xylanase activity was obtained after 7 days of incubation at 28 ± 0.5 °C using delignified S. spontaneum as carbon source under submerged fermentation conditions. Enzymatic hydrolysate of S. spontaneum was then tested for ethanol production under batch and repeated batch production system using “in-situ” entrapped Saccharomyces cerevisiae VS₃ cells in S. spontaneum stalks (1 cm × 1 cm) size. Immobilization was confirmed by the scanning electron microscopy (SEM). Batch fermentation of VS₃ free cells and immobilized cells showed ethanol production, 19.45 ± 0.55 g/L (yield, 0.410 ± 0.010 g/g) and 21.66 ± 0.62 g/L (yield, 0.434 ± 0.021 g/g), respectively. Immobilized VS₃ cells showed maximum ethanol production (22.85 ± 0.44 g/L, yield, 0.45 ± 0.04 g/g) up to 8th cycle during repeated batch fermentation followed by a gradual reduction in subsequent cycles of fermentation.     

l-Lactic acid production from liquefied cassava starch by thermotolerant Rhizopus microsporus: Characterization and optimization

The thermotolerant Rhizopus microsporus DMKU 33 capable of producing l-lactic acid from liquefied cassava starch was isolated and characterized for its phylogenetic relationship and growth temperature and pH ranges. The concentrations of (NH₄)₂SO_4, KH₂PO₄, MgSO₄ and ZnSO₄·7H₂O in the fermentation medium was optimized for lactic acid production from liquefied cassava starch by Rhizopus microsporus DMKU 33 in shake-flasks at 40 °C. The fermentation was then studied in a stirred-tank bioreactor with aeration at 0.75 vvm and agitation at 200 rpm, achieving the highest lactic acid production of 84 g/L with a yield of 0.84 g/g at pH 5.5 in 3 days. Lactic acid production was further increased to 105–118 g/L with a yield of 0.93 g/g and productivity of 1.25 g/L/h in fed-batch fermentation. R. microsporus DMKU 33 is thus advantageous to use in simultaneous saccharification and fermentation for l-lactic acid production from low-cost starchy substrates.     

Continuous 2-keto-gluconic acid (2KGA) production from corn starch hydrolysate by Pseudomonas fluorescens AR4

A continuous fermentation process for 2-keto-gluconic acid (2KGA) production from cheap raw material corn starch hydrolysate was developed using the strain Pseudomonas fluorescens AR4. The dilution rate and feeding glucose concentration had a significant effect on the cell concentrations, glucose utilization and 2KGA production performance. The optimal operating factors were obtained as: 0.065 h⁻¹ of dilution rate, 180 g/L of feeding glucose concentration, and 16 h of batch fermentation time as the starting point. Under these conditions, the steady state had the 135.92 g/L of produced 2KGA concentration, 8.83 g/L.h of average volumetric productivity, and 0.9510 g/g of yield. In conclusion, the proposed efficient and stable continuous fermentation process for 2KGA production by the strain P. fluorescens AR4 is potentially competitive for industrial production from corn starch hydrolysate in terms of 2KGA productivity and yield.     

A bioprocess for the production of high concentrations of R-(+)-α-terpineol from R-(+)-limonene

A bioprocess with a high conversion rate of limonene to α-terpineol was described. The enzyme hydratase involved in this process was found as being cofactor independent, non-inducible and able to perform the transformation of both R-(+) and S-(−)-limonene. The system used consisted of a biphasic medium in which the aqueous phase contained a concentrated resting cells of Sphingobium sp. and the organic phase was sunflower oil. After 30 h at 30 °C ca. 25 g of R-(+)-α-terpineol per liter of organic phase were obtained from R-(+)-limonene in Erlenmeyer flasks. Performance of the bioconversion in a bioreactor increased the production rate with no changes in yield and maximal R-(+)-α-terpineol concentration, which demonstrated that experiments in flasks were limited by liquid–liquid transport phenomena. A mathematical model able to explain the fact that the reaction always stopped before the precursor became exhausted has also been proposed and validated. Finally, the process reported was the most promising alternative for the biotechnological production of natural R-(+)-α-terpineol published so far and up to ca. 130 g L⁻¹ metabolite could finally be obtained.     

Production of butyric acid by a cellulolytic actinobacterium Thermobifida fusca on cellulose

Thermobifida fusca not only produces cellulases, hemicellulases and xylanases, but also excretes butyric acid. In order to achieve a high yield of butyric acid, the effect of different carbon sources: mannose, xylose, lactose, cellobiose, glucose, sucrose and acetates, on butyric acid production was studied. The highest yield of butyric acid was 0.67 g/g C (g-butyric acid/g-carbon input) on cellobiose. The best stir speed and aeration rate for butyric acid production were found to be 400 rpm and 2 vvm in a 5-L fermentor. The maximum titer of 2.1 g/L butyric acid was achieved on 9.66 g/L cellulose. In order to test the production of butyric acid on lignocellulosic biomass, corn stover was used as the substrate, on which there was 2.37 g/L butyric acid produced under the optimized conditions. In addition, butyric acid synthesis pathway was identified involving five genes that catalyzed reactions from acetyl-CoA to butanoyl-CoA in T. fusca.     

Enhancing production of prodigiosin from Serratia marcescens C3 by statistical experimental design and porous carrier addition strategy

Serratia marcescens C3 produces a natural red-pigment, prodigiosin, which exhibits immunosuppressive properties, in vitro apoptotic effects, and in vivo anti-tumor activities. This work seeks to improve the production of prodigiosin by S. marcescens C3 using various strategies. Starch and peptone were identified as the optimized carbon and nitrogen sources for the production of prodigiosin, yielding a prodigiosin concentration of 2.3 g/L. This value was significantly increased to 6.7 g/L using a carbon/nitrogen ratio of 6/4 (starch/peptone = 16 g/L/10.67 g/L). To enhance prodigiosin production even further, a statistical experimental design methodology was utilized to optimize the composition of the culture medium that is utilized in the production of prodigiosin. Prodigiosin production of 7.07 g/L was achieved when the concentrations of two trace compounds, FeSO₄·4H₂O and MnSO₄·4H₂O, were optimized using the statistical experimental design methodology. Their optimal concentrations were 0.56 mM and 3.25 mM, respectively. Ultimately, the production of prodigiosin was increased from 2.3 g/L to 15.6 g/L, or by a factor of nearly seven by immobilizing microorganisms in 3% calcium alginate beads.     

Metabolic engineering of Thermoanaerobacterium saccharolyticum for n-butanol production

The thermophilic anaerobe Thermoanaerobacterium saccharolyticum JW/SL-YS485 was investigated as a host for n-butanol production. A systematic approach was taken to demonstrate functionality of heterologous components of the clostridial n-butanol pathway via gene expression and enzymatic activity assays in this organism. Subsequently, integration of the entire pathway in the wild-type strain resulted in n-butanol production of 0.85 g/L from 10 g/L xylose, corresponding to 21% of the theoretical maximum yield. We were unable to integrate the n-butanol pathway in strains lacking the ability to produce acetate, despite the theoretical overall redox neutrality of n-butanol formation. However, integration of the n-butanol pathway in lactate deficient strains resulted in n-butanol production of 1.05 g/L from 10 g/L xylose, corresponding to 26% of the theoretical maximum.     

Enantioselective synthesis of (S)-phenylephrine by whole cells of recombinant Escherichia coli expressing the amino alcohol dehydrogenase gene from Rhodococcus erythropolis BCRC 10909

(R)-phenylephrine [(R)-PE] is an α₁-adrenergic receptor agonist that is widely used in over-the-counter drugs to treat the common cold. We found that Rhodococcus erythropolis BCRC 10909 can convert detectable level of 1-(3-hydroxyphenyl)-2-(methylamino) ethanone (HPMAE) to (S)-PE by high performance liquid chromatography tandem mass spectrometry analysis. An amino alcohol dehydrogenase gene (RE_AADH) which possesses the ability to convert HPMAE to (S)-PE was then isolated from R. erythropolis BCRC 10909 and expressed in Escherichia coli NovaBlue. The purified RE_AADH, tagged with 6×His, had a molecular mass of approximately 30 kDa and exhibited a specific activity of 0.19 μU/mg to HPMAE in the presence of NADPH, indicating this enzyme could be categorized as NADP⁺-dependent short-chain dehydrogenase reductase. E. coli NovaBlue cell expressing the RE_AADH gene was able to convert HPMAE to (S)-PE with more than 99% enantiomeric excess (ee), 78% yield and a productivity of 3.9 mmol (S)-PE/L h in 12 h at 30 °C and pH 7. The (S)-PE, recovered from reaction mixture by precipitation at pH 11.3, could be converted to (R)-PE (ee > 99%) by Walden inversion reaction. This is the first reported biocatalytic process for the production of (S)-PE from HPMAE.     

Production of fructooligosaccharides by mycelium-bound transfructosylation activity present in Cladosporium cladosporioides and Penicilium sizovae

Different filamentous fungi isolated from molasses and jams (kiwi and fig) were screened for fructooligosaccharides (FOS) producing activity. Two strains, identified as Penicilium sizovae (CK1) and Cladosporium cladosporioides (CF₂15), were selected on the basis of the FOS yield and kestose/nystose ratio. In both strains the activity was mostly mycelium-bound. Starting from 600 g/L of sucrose, maximum FOS yield was 184 and 339 g/L for P. sizovae and C. cladosporioides, respectively. Interestingly, the highest FOS concentration with C. cladosporioides was reached at 93% sucrose conversion, which indicated a notable transglycosylation to hydrolysis ratio. The main FOS in the reaction mixtures were identified by HPAEC–PAD chromatography. C. cladosporioides synthesized mainly 1-kestose (158 g/L), nystose (97 g/L), ¹F-fructosylnystose (19 g/L), 6-kestose (12 g/L), neokestose (10 g/L) and a disaccharide (34 g/L) that after its purification and NMR analysis was identified as blastose [Fru-β(2 → 6)-Glc]. P. sizovae was very selective for the formation of ¹F-FOS (in particular 1-kestose) with minor contribution of neoFOS and negligible of levan-type FOS.     

Efficient production of α-arbutin by whole-cell biocatalysis using immobilized hydroquinone as a glucosyl acceptor

The aim of the present study is to develop an efficient and cost-effective method for α-arbutin production by using whole-cell of Xanthomonas maltophilia BT-112 as a biocatalyst. Hydroquinone (HQ), substrate for the bioconversion as glucosyl acceptor, was immobilized on H107 macroporous resin to reduce its toxic effect on the cells, and the optimal reaction conditions for α-arbutin synthesis were investigated. When 350 g/L H107 resin (254.5 mM HQ) and 20 g/L (4.2 U/g) of cells were shaken in 10 mL Na₂HPO₄–KH₂PO₄ buffer (50 mM, pH 6.5) containing 509 mM sucrose at 35 °C with 150 rpm for 48 h, the final yield of α-arbutin reached 65.9 g/L with a conversion yield of 95.2% based on the amount of HQ supplied. The α-arbutin production was 202% higher than that of the control (free HQ) and the cells maintained its full activity for almost six consecutive batch reactions, indicating a potential for reducing production costs. Additionally, the product was one-step isolated and identified as α-arbutin by ¹³C NMR and ¹H NMR analysis. In conclusion, the combination of whole cells and immobilized hydroquinone (IMHQ) is a promising approach for economical and industrial-scale production of α-arbutin.