Enantioselective oxidation of racemic lactic acid to d-lactic acid and pyruvic acid by Pseudomonas stutzeri SDM

d-Lactic acid and pyruvic acid are two important building block intermediates. Production of d-lactic acid and pyruvic acid from racemic lactic acid by biotransformation is economically interesting. Biocatalyst prepared from 9 g dry cell wt l^?1 of Pseudomonas stutzeri SDM could catalyze 45.00 g l^?1 dl-lactic acid into 25.23 g l^?1 d-lactic acid and 19.70 g l^?1 pyruvic acid in 10 h. Using a simple ion exchange process, d-lactic acid and pyruvic acid were effectively separated from the biotransformation system. Co-production of d-lactic acid and pyruvic acid by enantioselective oxidation of racemic lactic acid is technically feasible.     

Integrated bioprocess for the oxidation of limonene to perillic acid with Pseudomonas putida DSM 12264

An efficient integrated bioprocess for the oxidation of limonene to perillic acid with Pseudomonas putida DSM 12264 was developed. Perillic acid is a promising candidate for natural preservation and pharmaceutical application. At elevated concentrations the monoterpenoic acid inhibits growth and biotransformation activity of P. putida DSM 12264. The maximum growth rate showed a linear decrease from μ = 1.43 h^?1 in the absence of perillic acid to complete inhibition at 165 ± 7 mM perillic acid. The maximum specific activity of limonene-transforming resting cells revealed an exponential decrease from almost 8 U/g cdw without perillic acid to <0.5 U/g cdw at >25 mM perillic acid. A method for in situ product recovery (ISPR) based on anion exchange resin was established to overcome product inhibition. A column containing a fluidized bed of Amberlite IRA 410 Cl was coupled to the bioreactor and enabled product removal by continuously recirculating the unfiltered broth through the ISPR unit. This led to a cumulative perillic acid concentration of 187 mM (31 g/L) after 7 days, which represents the highest product concentration achieved in a microbial monoterpene oxyfunctionalization so far. The ISPR approach reduced the further downstream processing steps needed which yielded a 93% pure product with a loss of 2%.     

Novel biotransformation process of podophyllotoxin to produce podophyllic acid and picropodophyllotoxin by Pseudomonas aeruginosa CCTCC AB93066, Part II: Process optimization

This work optimized the novel biotransformation process of podophyllotoxin to produce podophyllic acid by Pseudomonas aeruginosa CCTCC AB93066. Firstly, the biotransformation process was significantly affected by medium composition. 5 g/l of yeast extract and 5 g/l of peptone were favorable for podophyllic acid production (i.e. 25.3 ± 3.7 mg/l), while not beneficial for the cell growth of P. aeruginosa. This indicated that the accumulation of podophyllic acid was not corresponded well to the cell growth of P. aeruginosa. 0 g/l of sucrose was beneficial for podophyllic acid production (i.e. 34.3 ± 3.9 mg/l), which led to high podophyllotoxin conversion (i.e. 98.2 ± 0.1%). 1 g/l of NaCl was the best for podophyllic acid production (i.e. 47.6 ± 4.0 mg/l). Secondly, the production of podophyllic acid was significantly enhanced by fed-batch biotransformation. When each 100 mg/l of podophyllotoxin was added to the biotransformation system after 4, 10 and 25 h of culture, respectively, podophyllic acid concentration reached 99.9 ± 12.3 mg/l, enhanced by 284% comparing to one-time addition (i.e. 26.0 ± 2.1 mg/l). The fundamental information obtained in this study provides a simple and efficient way to produce podophyllic acid.     

Development of a recombinant Escherichia coli-based biocatalyst to enable high styrene epoxidation activity with high product yield on energy source

A highly active recombinant whole-cell biocatalyst, Escherichia coli pETAB2/pG-KJE1, was developed for the efficient production of (S)-styrene oxide from styrene. The recombinant E. coli overexpressed styAB the genes of styrene monooxygenase of Pseudomonas putida SN1 and coexpressed the genes encoding chaperones (i.e., GroEL–GroES and DnaK–DnaJ–GrpE). The styrene monooxygenases were produced to ca. 40% of the total soluble proteins, enabling the whole-cell activity of the recombinant of 180 U/g CDW. The high StyAB activity in turn appeared to direct cofactors and molecular oxygen to styrene epoxidation. The product yield on energy source (i.e., glucose) reached ca. 40%. In addition, biotransformation in an organic/aqueous two-liquid phase system allowed the product to accumulate to 400 mM in the organic phase within 6 h, resulting in an average specific and volumetric productivity of 6.4 mmol/g dry cells/h (106 U/g dry cells) and 67 mM/h (1110 U/L_aq), respectively, under mild reaction conditions. These results indicated that the high productivity and the high product yield on energy source were driven by the high enzyme activity. Therefore, it was concluded that oxygenase activity of whole-cell biocatalysts is one of the critical factors to determine their catalytic performance.     

Production of ω-hydroxyundec-9-enoic acid and n-heptanoic acid from ricinoleic acid by recombinant Escherichia coli-based biocatalyst

ω-Hydroxyundec-9-enoic acid and n-heptanoic acid are valuable building blocks for the production of flavors and antifungal agents as well as bioplastics such as polyamides and polyesters. However, a biosynthetic process to allow high productivity and product yield has not been reported. In the present study, we engineered an Escherichia coli-based biocatalytic process to efficiently produce ω-hydroxyundec-9-enoic acid and n-heptanoic acid from a renewable fatty acid (i.e., ricinoleic acid). Expression systems for catalytic enzymes (i.e., an alcohol dehydrogenase of Micrococcus luteus, a Baeyer–Villiger monooxygenase of Pseudomonas putida KT2440, an esterase of Pseudomonas fluorescens SIK WI) and biotransformation conditions were investigated. Biotransformation during stationary growth phase of recombinant E. coli in a bioreactor allowed to produce ω-hydroxyundec-9-enoic acid and n-heptanoic acid at a rate of 3.2 mM/h resulting in a final product concentration of ca. 20 mM. The total amount of ω-hydroxyundec-9-enoic acid and n-heptanoic acid produced reached 6.5 g/L (4.0 g/L of ω-hydroxyundec-9-enoic acid and 2.5 g/L of n-heptanoic acid). These results indicate that the high value carboxylic acids ω-hydroxyundec-9-enoic acid and n-heptanoic acid can be produced from a renewable fatty acid via whole-cell biotransformation.     

Enhanced selective oxidation of trimethylolpropane to 2,2-bis(hydroxymethyl)butyric acid using Corynebacterium sp. ATCC 21245

2,2-Bis(hydroxymethyl)butyric acid (BHMB) is an important multifunctional chemical for the emerging bio-based polymer industry. It can be produced from trimethylolpropane (TMP) by selective oxidation using growing cells of Corynebacterium sp. ATCC 21245. However, this process is limited by the low volumetric productivity and low concentration of the final product. In the present study, we performed sequential batch operation with cell recycling in media containing glycerol, acetic acid, and increasing concentrations of yeast extract. This approach enhanced the conversion of 10 and 15 g/L TMP to 11.0 and 16.3 g/L BHMB at rates of 0.50 and 0.20 g/L^.h, respectively. Applying a cell bleeding strategy resulted in an overall 10-fold improvement in productivity. The consequently prolonged biocatalyst viability resulted in a quantitative conversion of 20 g/L TMP to 22.3 g/L BHMB and a yield of 1.10 g_BHMB/g_TMP (100% molar yield). This work facilitates further studies of the selective oxidation on other industrially important polyols.     

Development of Halomonas TD01 as a host for open production of chemicals

Genetic engineering of Halomonas spp. was seldom reported due to the difficulty of genetic manipulation and lack of molecular biology tools. Halomonas TD01 can grow in a continuous and unsterile process without other microbial contaminations. It can be therefore exploited for economic production of chemicals. Here, Halomonas TD01 was metabolically engineered using the gene knockout procedure based on markerless gene replacement stimulated by double-strand breaks in the chromosome. When gene encoding 2-methylcitrate synthase in Halomonas TD01 was deleted, the conversion efficiency of propionic acid to 3-hydroxyvalerate (3HV) monomer fraction in random PHBV copolymers of 3-hydroxybutyrate (3HB) and 3HV was increased from around 10% to almost 100%, as a result, cells were grown to accumulate 70% PHBV in dry weight (CDW) consisting of 12 mol% 3HV from 0.5 g/L propionic acid in glucose mineral medium. Furthermore, successful deletions on three PHA depolymerases eliminate the possible influence of PHA depolymerases on PHA degradation in the complicated industrial fermentation process even though significant enhanced PHA content was not observed. In two 500 L pilot-scale fermentor studies lasting 70 h, the above engineered Halomonas TD01 grew to 112 g/L CDW containing 70 wt% P3HB, and to 80 g/L CDW with 70 wt% P(3HB-co-8 mol% 3HV) in the presence of propionic acid. The cells grown in shake flasks even accumulated close to 92% PHB in CDW with a significant increase of glucose to PHB conversion efficiency from around 30% to 42% after 48 h cultivation when pyridine nucleotide transhydrogenase was overexpressed. Halomonas TD01 was also engineered for producing a PHA regulatory protein PhaR which is a robust biosurfactant.     

Proximate,mineral, fibre,phytate–phosphate,vitamin E,amino acid and fatty acid composition of Terminalia sericea

Terminalia sericea is widely distributed in the African Savannah bushveld. It is one of the indigenous fruit bearing trees put to multiple uses. Research has focused on the phytochemical composition of its root, bark, and leaf extracts that are used in ethnomedicine neglecting the potential of its seed. This study purposed to determine, by chemical analyses, the nutritive value of T. sericea seed. 78.8% of the seed was found to be crude protein (46.2%) and lipid (32.6%). Ash made up 6.90% of the seed mass. Linoleic and oleic acids constituted 68.63% and 14.05%, respectively, of the seed oil. Phosphorus (1121.75 ± 10.39 mg 100 g^− 1 DM) and glutamic acid (8.07 ± 0.13 g 100^− 1 DM) constituted the most concentrated mineral and amino acid, respectively. T. sericea seed could be utilized as a protein source in feeds and foods and could also be exploited as a non-conventional plant oil source of oleic acid and linoleic acid.     

Characterization of a recombinant Escherichia coli TOP10 [pQR239] whole-cell biocatalyst for stereoselective Baeyer–Villiger oxidations

This paper describes the kinetic characterization of a recombinant whole-cell biocatalyst for the stereoselective Baeyer–Villiger type oxidation of bicyclo[3.2.0]hept-2-en-6-one to its corresponding regio-isomeric lactones (−)-(1S,5R)-2-oxabicyclo[3.3.0]oct-6-en-3-one and (−)-(1R,5S)-3-oxabicyclo[3.3.0]oct-6-en-2-one. Escherichia coli TOP10 [pQR239], expressing cyclohexanone monooxygenase (CHMO) from Acinetobacter calcoaceticus (NCIMB 9871), was shown to be suitable for this biotransformation since it expressed CHMO at a high level, was simple to produce, contained no contaminating lactone hydrolase activity and allowed the intracellular recycle of NAD(P)H necessary for the biotransformation. A small-scale biotransformation reactor (20 ml) was developed to allow rapid collection of intrinsic kinetic data. In this system, the optimized whole-cell biocatalyst exhibited a significantly lower specific lactone production activity (55–60 μmol min⁻¹ g⁻¹ dry weight) than that of sonicated cells (500 μmol min⁻¹ g⁻¹ dry weight). It was shown that this shortfall was comprised of a difference in the pH optima of the two biocatalyst forms and mass transfer limitations of the reactant and/or product across the cell barrier. Both reactant and product inhibition were evident. The optimum ketone concentration was between 0.2 and 0.4 g l⁻¹ and at product concentrations above 4.5–5 g l⁻¹ the specific activity of the whole cells was zero. These results suggest that a reactant feeding strategy and in situ product removal should be considered in subsequent process design.     

Synthesis,characterization and swelling behaviors of sodium alginate-g-poly(acrylic acid)/sodium humate superabsorbent

A novel sodium alginate-g-poly(acrylic acid)/sodium humate superabsorbent was prepared by graft copolymerization with sodium alginate, acrylic acid and sodium humate in aqueous solution, using N,N’-methylenebisacrylamide as a crosslinker and ammonium persulfate as an initiator. The effects of crosslinker, sodium alginate and sodium humate content on water absorbency of the superabsorbent were studied. The swelling behavior in solutions of various pH and the swelling kinetics in saline solutions (5 mmol/L NaCl and CaCl₂) were also investigated. The results from IR analysis showed that both sodium alginate and sodium humate react with the acrylic acid monomer during the polymerization process. The introduction of sodium humate into the sodium alginate-g-poly(acrylic acid) system could enhance the water absorbency and the superabsorbent containing 10 wt% sodium humate acquired the highest water absorbency (1380 g/g in distilled water and 83 g/g in 0.9 wt% NaCl solution).     

Production enhancement of Rhizopus arrhizus lipase by feeding oleic acid

A strategy for Rhizopus arrhizus lipase production enhancement by feeding oleic acid was developed. The oleic acid was proved to have strong inducing effect on lipase production, but high concentration oleic acid could repress lipase production. The decrease rate of oleic acid concentration using peanut oil as initial carbon source was figured out according to the change of oleic acid concentration in the fermentation broth. Our feeding strategy designed based on the decrease rate of oleic acid could avoid the repression of lipase production that is caused by high concentration of oleic acid in the fermenting liquor, and this strategy worked as a new feeding method showing excellent performance. The maximum lipase activity was gained by feeding dilute oleic acid every 12 h starting at 60 h, which maintained the oleic acid concentration around 18 mg/L, and the lipase activity was 31% higher than that of no feeding.     

HPLC-DAD analysis of arbutin produced from hydroquinone in a biotransformation process in Origanum majorana L. shoot culture

The hydroquinone glucoside arbutin is a plant derived compound medically applied due to its uroantiseptic activity. It also has skin whitening properties and thus is widely used in dermatology and cosmetology. Origanum majorana L. (Lamiaceae) is known to produce arbutin, however the content of the compound in cultivated plants is very variable and low. Since plant cell and tissue cultures are capable to perform specific biotransformation reactions including glucosylation, this investigation targeted the formation of arbutin from hydroquinone in agitated O. majorana shoot cultures. For this purpose different doses of hydroquinone (96, 144, 192, 288 and 384 mg/L of medium) were added to the culture flasks in one, two or three portions. Arbutin was qualitatively and quantitatively determined in methanol extracts from dry biomass and lyophilized media using HPLC-DAD. Cells of O. majorana shoot cultures efficiently converted hydroquinone into arbutin. The product was accumulated in the biomass and was not observed (or in trace amounts) in the medium samples. Different doses as well as portioning of the precursor had a significant impact on the biotransformation process. Arbutin accumulation increased from 0.23 ± 0.03 mg/g DW up to 52.6 ± 4.8 mg/g DW in the biomass. The highest product content was observed after the addition of 192 mg/L hydroquinone in three portions. The highest efficiency of the biotransformation process, i.e. 67.5 ± 5.2% was calculated for a dose of 96 mg/L precursor divided into three portions. After further optimization of the biotransformation process, O. majorana shoot cultures could serve as a rich source of arbutin.     

d- and l-lactic acid production from fresh sweet potato through simultaneous saccharification and fermentation

The aim of this study was to develop a bioprocess for l- and d-lactic acid production from raw sweet potato through simultaneous saccharification and fermentation by Lactobacillus paracasei and Lactobacillus coryniformis, respectively. The effects of enzyme and nitrogen source concentrations as well as of the ratio of raw material to medium were investigated. At dried material concentrations of 136.36–219.51 g L⁻¹, yields of 90.13–91.17% (w/w) and productivities of 3.41–3.83 g L⁻¹ h⁻¹ were obtained with lactic acid concentrations as high as 198.32 g L⁻¹ for l-lactic acid production. In addition, d-lactic acid was produced with yields of 90.11–84.92% (w/w) and productivities of 2.55–3.11 g L⁻¹ h⁻¹ with a maximum concentration of 186.40 g L⁻¹ at the same concentrations of dried material. The simple and efficient process described in this study will benefit the tuber and root-based lactic acid industries without requiring alterations in plant equipment.     

Biotransformation of 2-phenylethanol to phenylacetaldehyde in a two-phase fed-batch system

Phenylacetaldehyde (PA) can be produced by the oxidation of 2-phenylethanol (PE) through biotransformation. In order to prevent substrate and product inhibitions and the transformation of the PA to phenylacetic acid (PAA), utilization of a two-phase system is very attractive. Gluconobacter oxydans B-72 was used as the microorganism and iso-octane as the solvent. The effect of initial substrate concentration on the PA production was investigated in single- and two-phase systems. In the single-phase system, substrate inhibition occurred above 5 g/l, and in the two-phase system, above 7.5 g/l. Substrate inhibition kinetics were also studied in the two-phase system and kinetic constants were determined as r_max=0.64 g/l min, K_M=8.15 g/l, K_PA=2.5 g/l. Because it was observed that two-phase system is insufficient to remove the substrate inhibition effect, fed-batch operation was utilised in this study. For 7.5 g/l of PE, 1.65, 3.85, and 7.35 g/l of PA were obtained in the single-phase, two-phase, and two-phase three fed-batch systems, respectively. Effect of biotransformation time, initial substrate concentration, agitation speed, and fed-batch number on the PA production was investigated in a two-phase fed-batch system by the response surface methodology (RSM). The optimum values were found as 3 fed-batch number, 2.75 g/l initial substrate concentration, 150 rpm agitation speed, and 65 min of one batch biotransformation time. In order to verify these results, an experiment was performed at these optimum conditions and 7.10 g/l of PA concentration was obtained.     

Enhanced biotransformation of l-phenylalanine to 2-phenylethanol using an in situ product adsorption technique

An in situ product adsorption technique was used to enhance the biotransformation of l-phenylalanine to 2-phenylethanol by Saccharomyces cerevisiae BD. As a suitable adsorbent, the non-polar macroporous resin D101, selected from several resins tested, showed high adsorption capacity for 2-phenylethanol but not l-phenylalanine. Product inhibition was effectively alleviated by the addition of macroporous resin D101 to the biotransformation medium. When 2 g of hydrated resin D101 was added to 30 mL of the biotransformation medium, the total 2-phenylethanol concentration achieved was 6.17 g/L, of which 3.15 g/L remained in the aqueous phase and 3.02 g/L was adsorbed onto the resin. The molar yield of 2-phenylethanol reached 0.70 after 24 h cultivation. Addition of the macroporous resin greatly increased the volumetric productivity of 2-phenylethanol, and made the downstream processing more feasible and easier to perform in an industrial application.     

Modelling and simulation of continuous L (+) lactic acid production from sugarcane juice in membrane integrated hybrid-reactor system

Modelling and simulation was done for a two-stage membrane-integrated hybrid reactor system for continuous production of L (+) lactic acid under non-neutralizing conditions. The model captures microbial conversion of sugar cane juice to lactic acid under substrate–product inhibitions with downstream purification by nanofiltration. All the major phenomena and the governing parameters like fluid flow, feed dilution, substrate–product inhibitions, Donnan and steric effects during micro and nanofiltration for cell recycle, product separation and purification have been reflected in the modelling. The model describes a green, integrated continuous process of direct lactic acid production starting with a cheap, renewable carbon source. The highest lactic acid concentration achieved after the final stage of nanofiltration was 66.97 g/L at 13 kg/cm² operating pressure when the overall productivity reached 12.40 g/(L h). The developed model could successfully predict production, purification and transport of lactic acid through two stage membrane modules. Performance of the model was very good as indicated in the high overall correlation coefficient (R² > 0.980) and the low relative error (RE < 0.1).     

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.     

Fermentative production of succinic acid from straw hydrolysate by Actinobacillus succinogenes

In this work, straw hydrolysates were used to produce succinic acid by Actinobacillus succinogenes CGMCC1593 for the first time. Results indicated that both glucose and xylose in the straw hydrolysates were utilized in succinic acid production, and the hydrolysates of corn straw was better than that of rice or wheat straw in anaerobic fermentation of succinic acid. However, cell growth and succinic acid production were inhibited when the initial concentration of sugar, which was from corn straw hydrolysate (CSH), was higher than 60 g l^?1. In batch fermentation, 45.5 g l^?1 succinic acid concentration and 80.7% yield were attained after 48 h incubation with 58 g l^?1 of initial sugar from corn straw hydrolysate in a 5-l stirred bioreactor. While in fed-batch fermentation, concentration of succinic acid achieved 53.2 g l^?1 at a rate of 1.21 g l^?1 h^?1 after 44 h of fermentation. Our work suggested that corn straw could be utilized for the economical production of succinic acid by A. succinogenes.     

Improving the lactic acid production of Actinobacillus succinogenes by using a novel fermentation and separation integration system

This work describes the development of a novel integrated system for lactic acid production by Actinobacillus succinogenes. Fermentation and separation were integrated with the use of a microfiltration (MF) membrane, and lactic acid was recovered by resin adsorption following MF. The fermentation broth containing residual sugar and nutrients was then recycled back into the fermenter after lactic acid adsorption. This novel approach overcame the problem of product inhibition and extended the cell growth period from 41 h to 120 h. Production of lactic acid was improved by 23% to 183.4 g L⁻¹. The overall yield and productivity for glucose were 0.97 g g⁻¹ and 1.53 g L⁻¹ h⁻¹, respectively. These experimental results indicate that the integrated system could benefit continuous production of lactic acid at high levels.     

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.