Improvement of welan gum production and redistribution of metabolic flux under pH control process in Alcaligenes sp. CGMCC2428

Batch fermentations of welan gum from Alcaligenes sp. CGMCC2428 at pH values of 5.5 ～ 7.0 were studied. Based on the kinetic analysis, a pH control process for improving welan production was developed. By maintaining the culture pH at 7.0, the process significantly improved the maximal welan concentration and productivity to reach 25.1 ± 0.65 g/L and 0.42 ± 0.003 g/L/h, respectively, compared with those in native pH processes where pH value would decrease from 7.0 to 5.1 (18.5 ± 0.72 g/L and 0.28 ± 0.002 g/L/h). This improvement may be due to the increased metabolic flux of glucose-1-phosphate to welan induced by pH control process. Furthermore, scale-up fermentation under controlled pH was implemented using 300-L fermentor. The highest welan concentration of 27.5 ± 0.97 g/L was obtained. This simplified process proved effective in industry fermentation for high welan production.     

Fed-batch fermentation of Tuber melanosporum for the hyperproduction of mycelia and bioactive Tuber polysaccharides

For the first time, a fed-batch fermentation process of Tuber melanosporum was developed for the efficient production of bioactive mycelia and Tuber polysaccharides. Each 1.67 g/L of peptone and 8.33 g/L of yeast extract were added on day 3, 6, and 9, respectively, and sucrose was fed to maintain its concentration around 35–5 g/L when its residual level decreased to 10–5 g/L. Then, the maximal biomass, the production of extracellular polysaccharides (EPS) and intracellular polysaccharides (IPS) reached 53.72 ± 2.57 g DW/L, 7.09 ± 0.62 and 4.43 ± 0.21 g/L, respectively. Compared with the batch culture conducted in the enriched medium, the biomass, the production of EPS and IPS were enhanced by 55.8%, 222.3% and 103.2%, respectively. Not only the cell density but also the production of EPS and IPS were the highest ever reported in truffle fermentation, and the biomass was also the highest as ever reported in mushroom fermentation.     

Optimisation of exopolysaccharide production by Gomphidius rutilus and its antioxidant activities in vitro

The production conditions of the Gomphidius rutilus exopolysaccharides (GREP) in submerged culture were optimised, and the antioxidant activities of GREP in vitro were evaluated. The optimal culture medium constituents were determined as follows: 30 g/L sucrose, 3.0 g/L soybean meal, 0.25 g/L MgSO₄, 1.5 g/L K₂HPO₄, 0.5 g/L KH₂PO₄, 0.03 g/L ZnSO₄, and 0.01 g/L FeSO₄. The optimum parameters for the liquid fermentation were as follows: temperature, 25 °C; cultivation time, 6 d; initial pH, 8.0; volume of medium, 150 mL; and rotary speed, 180 rpm. GREP content and dry cell weight in optimised conditions were 540.1 ± 15.9 mg/L and 8.2 ± 0.3 g/L, respectively. GREP content under the optimised conditions was 2.5 times than that under the basic culture medium and initial conditions. GREP demonstrated positive antioxidant potential on superoxide anion radical, 1,1-diphenyl-2-picrylhydrazyl, and hydroxyl radical scavenging, and reducing power.     

Use of glycerol for producing 1,3-dihydroxyacetone by Gluconobacter oxydans in an airlift bioreactor

1,3-Dihydroxyacetone can be produced by biotransformation of glycerol with glycerol dehydrogenase from Gluconobacter oxydans cells. Firstly, improvement the activity of glycerol dehydrogenase was carried out by medium optimization. The optimal medium for cell cultivation was composed of 5.6 g/l yeast extract, 4.7 g/l glycerol, 42.1 g/l mannitol, 0.5 g/l K₂HPO₄, 0.5 g/l KH₂PO₄, 0.1 g/l MgSO₄·7H₂O, and 2.0 g/l CaCO₃ with the initial pH of 4.9. Secondly, an internal loop airlift bioreactor was applied for DHA production from glycerol by resting cells of G. oxydans ZJB09113. Furthermore, the effects of pH, aeration rate and cell content on DHA production and glycerol feeding strategy were investigated. 156.3 ± 7.8 g/l of maximal DHA concentration with 89.8 ± 2.4% of conversion rate of glycerol to DHA was achieved after 72 h of biotransformation using 10 g/l resting cells at 30 °C, pH 5.0 and 1.5 vvm of aeration rate.     

Hydrogen production by the newly isolated Clostridium beijerinckii RZF-1108

A fermentative hydrogen-producing strain, RZF-1108, was isolated from a biohydrogen reactor, and identified as Clostridium beijerinckii on the basis of the 16S rRNA gene analysis and physiobiochemical characteristics. The effects of culture conditions on hydrogen production by C. beijerinckii RZF-1108 were investigated in batch cultures. The hydrogen production and growth of strain RZF-1108 were highly dependent on temperature, initial pH and substrate concentration. Yeast extract was a favorable nitrogen source for hydrogen production and growth of RZF-1108. Hydrogen production corresponded to cell biomass yield in different culture conditions. The maximum hydrogen evolution, yield and production rate of 2209 ml H₂/l medium, 1.97 mol H₂/mol glucose and 104.20 ml H₂/g CDW h⁻¹ were obtained at 9 g/l of glucose, initial pH of 7.0, inoculum volume of 8% and temperature of 35 °C, respectively. These results demonstrate that C. beijerinckii can efficiently produce H₂, and is another model microorganism for biohydrogen investigations.     

Optimization of medium composition for butyric acid production by Clostridium thermobutyricum using response surface methodology

The optimal medium for butyric acid production by Clostridium thermobutyricum in a shake flask culture was studied using statistical experimental design and analysis. The optimal composition of the fermentation medium for maximum butyric acid yield, as determined on the basis of a three-level four-factor Box-Behnken design (BBD), was obtained by response surface methodology (RSM). The high correlation between the predicted and observed values indicated the validity of the model. A maximum butyric acid yield of 12.05 g/l was obtained at K₂HPO₄ 7.2 g/l, 34.9 g/l glucose, 20 g/l yeast extract, and 15 g/l acetate, which compared well to the predicated production of 12.13 g/l.     

Optimization of production conditions for mushroom polysaccharides with high yield and antitumor activity

Single factor experiment and response surface methodology were conducted to optimize the production conditions for polysaccharide with higher antitumor activity from mushroom fermentation broth. Based on the results of single factor experiments, a central composite design was applied to the following optimization and second-order polynomial regression models were established. As the yield and antitumor activity of the polysaccharides were considered with equal weight, the optimal conditions were that ethanol concentration and pH of the broth was adjusted to 85.00% and 7.70 respectively, then precipitated at 12 °C for 1 h and dried the precipitates at 40 °C. The verification experiments completed under the optimal conditions gave the polysaccharides yield of 9.843 ± 0.217 g/l, and the cancer cell growth inhibitory rate of 83.69 ± 0.167% by the polysaccharides, which were in close agreement with values predicted by the models (RSD < 5%).     

Maximization of bioconversion of castor oil into ricinoleic acid by response surface methodology

In this study, response surface methodology was applied to optimize process variables like temperature, pH, enzyme concentration (mg/g oil), and buffer concentration (g/g oil) for hydrolysis of castor oil using Candida rugosa lipase. A 2⁴ full factorial central composite design was used to develop the quadratic model that was subsequently optimized and the optimal conditions were as follows: temperature 40 °C, pH 7.72, enzyme concentration 5.28 mg/g oil, buffer concentration 1 g/g oil and there was 65.5% conversion in 6 h. These predicted optimal conditions agreed well with the experimental results. This is the first report on the application of response surface methodology in castor oil hydrolysis using C. rugosa lipase with higher percentage conversion in 6 h.     

Biohydrogen production in a three-phase fluidized bed bioreactor using sewage sludge immobilized by ethylene–vinyl acetate copolymer

Ethylene–vinyl acetate (EVA) copolymer was used to immobilize H₂-producing sewage sludge for H₂ production in a three-phase fluidized bed reactor (FBR). The FBR with an immobilized cell packing ratio of 10% (v/v) and a liquid recycle rate of 5 l/min (23% bed expansion) was optimal for dark H₂ fermentation. The performance of the FBR reactor fed with sucrose-based synthetic medium was examined under various sucrose concentration (C_so) and hydraulic retention time (HRT). The best volumetric H₂ production rate of 1.80 ± 0.02 H₂ l/h/l occurred at C_so = 40 g COD/l and 2 h HRT, while the optimal H₂ yield (4.26 ± 0.04 mol H₂/mol sucrose) was obtained at C_so = 20 g COD/l and 6 h HRT. The H₂ content in the biogas was stably maintained at 40% or above. The primary soluble metabolites were butyric acid and acetic acid, as both products together accounted for 74–83% of total soluble microbial products formed during dark H₂ fermentation.     

Hydrogen production by immobilized R. faecalis RLD-53 using soluble metabolites from ethanol fermentation bacteria E. harbinense B49

In order to increase the hydrogen yield from glucose, hydrogen production by immobilized Rhodopseudomonas faecalis RLD-53 using soluble metabolites from ethanol fermentation bacteria Ethanoligenens harbinense B49 was investigated. The soluble metabolites from dark-fermentation mainly were ethanol and acetate, which could be further utilized for photo-hydrogen production. Hydrogen production by B49 was noticeably affected by the glucose and phosphate buffer concentration. The maximum hydrogen yield (1.83 mol H₂/mol glucose) was obtained at 9 g/l glucose. In addition, we found that the ratio of acetate/ethanol (A/E) increased with increasing phosphate buffer concentration, which is favorable to further photo-hydrogen production. The total hydrogen yield during dark- and photo-fermentation reached its maximum value (6.32 mol H₂/mol glucose) using 9 g/l glucose, 30 mmol/l phosphate buffers and immobilized R. faecalis RLD-53. Results demonstrated that the combination of dark- and photo- fermentation was an effective and efficient process to improve hydrogen yield from a single substrate.     

Production of α-ketoisocaproate via free-whole-cell biotransformation by Rhodococcus opacus DSM 43250 with L-leucine as the substrate

This work aims to produce α-ketoisocaproate (KIC) from l-leucine via the free-whole-cell biotransformation of Rhodococcus opacus DSM 43250. The effects of temperature, pH, substrate concentration, cell concentration, and rotating speed on KIC production were examined. Furthermore, the biotransformation conditions were optimized with response surface methodology (RSM). The optimal biotransformation conditions were as follows: temperature 43.7 °C, pH 8.4, l-leucine concentration 5.1 g/L, cell concentration 30.4 g/L, and rotating speed 170 rpm. The maximal KIC production predicted by RSM model reached 1275 mg/L at the optimal conditions, and in the validated experiments, the maximal KIC production reached 1264 mg/L, which was very close to the predicted KIC production. The current work provides an alternative for the production of KIC and the results obtained here are useful for the biotransformatic KIC production on a large scale.     

Nutritional characterization of Mucuna pruiriens: 2. In vitro ruminal fluid fermentability of Mucuna pruriens,Mucunal-dopa and soybean meal incubated with or without l-dopa

Three in vitro experiments were conducted to determine the rumen fermentability of Mucuna (M) pruriens (24 g 3,4-dihydroxy-l-phenylalanine (l-dopa)/kg dry matter (DM) and soybean meal treated with (SBD) or without (SB) 138 g l-dopa/kg DM). Additional objectives were to determine if l-dopa inhibits rumen fermentation, and if ruminal microbes can adapt to l-dopa or M. In Experiment 1, ground (1 mm) substrates were incubated in triplicate at 38 °C in 9 ml nutrient media and 1 ml rumen fluid in a series of six, 48 h, consecutive batch cultures. The first culture was inoculated with rumen fluid from two donor cows. Subsequent cultures were inoculated with fluid (1 ml) from the previous culture. The DM digestibility (DMD, 616 g/kg vs. 540 g/kg; P<0.01) and gas production (51.7 ml/g vs. 44.2 ml/g DM; P<0.05) were higher from fermentation of M versus SB but similar for SB and SBD (540 g/kg vs. 554 g/kg and 44.2 ml/g DM vs. 43.5 ml/g DM, respectively). The slopes of the relationships between DMD (g/kg) or gas production (ml/g DM) and fermentation period were not reduced by fermenting M (−0.014 DMD slope; 2.28 gas production slope) or SBD (−0.014 DMD slope; 0.459 gas production slope), instead of SB (−0.002 DMD slope; 1.039 gas production slope), indicating microbial adaptation to M and SBD. Total volatile fatty acid concentration (VFA; 53.7, 54.9 and 54.9 mmol/l) and molar proportions of VFA were similar among substrates. Gas production kinetics of M versus SB (Experiment 2), and SB versus SBD (Experiment 3) were also measured after substrates were incubated in triplicate in buffered rumen fluid for 24 h using a non-linear exponential model to fit the data. Residual l-dopa was measured after separate fermentation of substrates in triplicate for 0, 4, 8, 16 and 24 h. Fermentation of M versus SB produced more (P<0.05) gas (250 ml/g vs. 100 ml/g DM) and total VFA (203 mmol/l vs. 180 mmol/l) and a lower (P<0.05) acetate:propionate ratio (1.35 vs. 1.87; P<0.05). Adding l-dopa to SB increased (P<0.01) gas production (92 ml/g DM vs. 200 ml/g DM), and total VFA concentration (132 mmol/l vs. 188 mmol/l), but reduced (P<0.05) gas production rate (0.08 ml/h vs. 0.05 ml/h). The concentration of l-dopa in fermented M and SBD decreased by 53 and 47%, respectively during fermentation. In conclusion, M was more fermented than SB and degradation of l-dopa during ruminal fermentation and microbial adaptation to l-dopa were confirmed. Adding l-dopa to SB did not impair ruminal fermentation.     

Biodiesel-derived crude glycerol bioconversion to animal feed: a sustainable option for a biodiesel refinery

This study examined the potential of producing an edible fungus, Rhizopus microsporus var. oligosporus, on biodiesel-derived crude glycerol. Prolific fungal growth was observed with a fungal biomass yield of 0.83 ± 0.02 (g biomass increase/g initial biomass) under optimal cultivation conditions (e.g. nonsterile crude glycerol at a concentration of 75% (w/v) with nutrient supplementation and without pH control). The potential of utilizing front-end processed banagrass (Pennisetum purpureum) juice as a source of nutrients for crude glycerol fermentation was evaluated with a 2.3-fold improvement in the fungal biomass yield. The glycerol-derived fungal biomass showed high amounts of threonine, one of the main limiting amino acids in non-ruminant feeds. An inexpensive fungal protein has the potential to reduce meat product prices by lowering the production costs of animal feeds. The application of fungal technology thus provides a unique sustainable option for biodiesel refineries by providing an additional source of revenue from fungal products.     

Lipid production by Lipomyces starkeyi cells in glucose solution without auxiliary nutrients

Two-stage fermentation process was used for lipid production by Lipomyces starkeyi AS 2.1560 in glucose solution without auxiliary nutrients. In the first stage, cells were cultivated in a nutrient-rich medium for propagation. In the second stage, cells were resuspended in glucose solution to achieve high cellular lipid contents. The effects of the inocula age, cell density and initial glucose concentration on lipid production were briefly studied. When high cell density fermentation was performed in a 7-L stirred-tank bioreactor for 40 h using non-sterile glucose solution as carbon source, the biomass, lipid and lipid content reached 104.6 g/L, 67.9 g/L and 64.9%, respectively. More significantly, lipid productivity reached 2.0 g/L h during the initial 16 h-period and 1.6 g/L h for the entire culture. Our results demonstrated that cell propagation and lipid accumulation processes can be spatially separated, allowing further optimization to improve both processes. The two-stage fermentation method should have a great potential to develop more efficient processes to convert renewable materials into biofuel and related products.     

Continuous hydrogen and butyric acid fermentation by immobilized Clostridium tyrobutyricum ATCC 25755: Effects of the glucose concentration and hydraulic retention time

The effects of the hydraulic retention time (HRT = 8, 10, 12 or 16.7 h) and glucose concentration (30, 40 or 50 g/L) on the production of hydrogen and butyrate by an immobilized Clostridium tyrobutyricum culture, grown under continuous culturing conditions, were evaluated. With 30 g/L glucose, the higher HRTs tested led to greater butyrate concentrations in the culture, i.e., 9.3 g/L versus 12.9 g/L with HRTs of 8 h and 16.7 h, respectively. In contrast, higher biogas and hydrogen production rates were generally seen when the HRT was lower. Experiments with different glucose concentrations saw a significant amount of glucose washed out when 50 g/L was used, the highest being 22.7 g/L when the HRT was 16.7 h. This study found the best conditions for the continuous production of hydrogen and butyric acid by C. tyrobutyricum to be with an HRT of 12 h and a glucose concentration of 50 g/L, respectively.     

Isolation of a solventogenic Clostridium sp. strain: Fermentation of glycerol to n-butanol,analysis of the bcs operon region and its potential regulatory elements

A new solventogenic bacterium, strain GT6, was isolated from standing water sediment. 16S-rRNA gene analysis revealed that GT6 belongs to the heterogeneous Clostridium tetanomorphum group of bacteria exhibiting 99% sequence identity with C. tetanomorphum 4474^T. GT6 can utilize a wide range of carbohydrate substrates including glucose, fructose, maltose, xylose and glycerol to produce mainly n-butanol without any acetone. Additional products of GT6 metabolism were ethanol, butyric acid, acetic acid, and trace amounts of 1,3-propanediol. Medium and substrate composition, and culture conditions such as pH and temperature influenced product formation. The major fermentation product from glycerol was n-butanol with a final concentration of up to 11.5 g/L. 3% (v/v) glycerol lead to a total solvent concentration of 14 g/L within 72 h. Growth was not inhibited by glycerol concentrations as high as 15% (v/v).     

Butyric acid fermentation in a fibrous bed bioreactor with immobilized Clostridium tyrobutyricum from cane molasses

Butyrate fermentation by immobilized Clostridium tyrobutyricum was successfully carried out in a fibrous bed bioreactor using cane molasses. Batch fermentations were conducted to investigate the influence of pH on the metabolism of the strain, and the results showed that the fermentation gave a highest butyrate production of 26.2 g l⁻¹ with yield of 0.47 g g⁻¹ and reactor productivity up to 4.13 g l⁻¹ h⁻¹ at pH 6.0. When repeated-batch fermentation was carried out, long-term operation with high butyrate yield, volumetric productivity was achieved. Several cane molasses pretreatment techniques were investigated, and it was found that sulfuric acid treatment gave better results regarding butyrate concentration (34.6 ± 0.8 g l⁻¹), yield (0.58 ± 0.01 g g⁻¹), and sugar utilization (90.8 ± 0.9%). Also, fed-batch fermentation from cane molasses pretreated with sulfuric acid was performed to further increase the concentration of butyrate up to 55.2 g l⁻¹.     

High production of cold-tolerant chitinases on shrimp wastes in bench-top bioreactor by the Antarctic fungus Lecanicillium muscarium CCFEE 5003: Bioprocess optimization and characterization of two main enzymes

The Antarctic fungus Lecanicillium muscarium CCFEE-5003 was preliminary cultivated in shaken flasks to check its chitinase production on rough shrimp and crab wastes. Production on shrimp shells was much higher than that on crab shells (104.6 ± 9.3 and 48.6 ± 3.1 U/L, respectively). For possible industrial applications, bioprocess optimization was studied on shrimp shells in bioreactor using RSM to state best conditions of pH and substrate concentration. Optimization improved the production by 137% (243.6 ± 17.3). Two chitinolytic enzymes (CHI1 and CHI2) were purified and characterized. CHI1 (MW ca. 61 kDa) showed optima at pH 5.5 and 45 °C while CHI2 (MW ca. 25 kDa) optima were at pH 4.5 and 40 °C. Both enzymes maintained high activity levels at 5 °C and were inhibited by Fe⁺⁺, Hg⁺⁺ and Cu⁺⁺. CHI2 was strongly allosamidin-sensitive. Both proteins were N-acetyl-hexosaminidases (E.C. 3.2.1.52) but showed different roles in chitin hydrolysis: CHI1 could be defined as “chitobiase” while CHI2 revealed a main “eso-chitinase” activity.     

Efficient mosquitocidal toxin production by Bacillus sphaericus using cheese whey permeate under both submerged and solid state fermentations

Whey permeate (WP) was used efficiently for production of mosquitocidal toxin by Bacillus sphaericus 2362 (B. sphaericus 2362) and the Egyptian isolate, B. sphaericus 14N1 (B. sphaericus 14N1) under both submerged and solid state fermentation conditions. Under submerged fermentation, high mosquitocidal activity was produced by B. sphaericus 2362 and B. sphaericus 14N1 at 50-100% and 25-70% WP, respectively. Initial pH of WP was a critical factor for toxin production by both tested organisms. The highest toxicity was obtained at initial pH 7. Egyptian isolate, B. sphaericus 14N1 was tested for growth and toxin production under solid state fermentation conditions (SSF) by using WP as moistening agent instead of distilled water. The optimum conditions for production of B. sphaericus 14N1 on wheat bran-WP medium were 10 g wheat bran/250 ml flask moistened with 10-70% WP at 50% moisture content, inoculum size ranged between 17.2 × 10⁷ and 34.4 × 10⁷ and 6 days incubation under static conditions at 30 °C. Preliminary pilot-scale production of B. sphaericus 14N1 under SSF conditions in trays proved that wheat bran-WP medium was efficient and economic for industrial production of mosquitocidal toxin by B. sphaericus.     

Green and economical production of propionic acid by Propionibacterium freudenreichii CCTCC M207015 in plant fibrous-bed bioreactor

Propionic acid production by Propionibacterium freudenreichii from molasses and waste propionibacterium cells was studied in plant fibrous-bed bioreactor (PFB). With non-treated molasses as carbon source, 12.69 ± 0.40 g l^-1 of propionic acid was attained at 120 h in free-cell fermentation, whereas the PFB fermentation yielded 41.22 ± 2.06 g l^-1 at 120 h and faster cells growth was observed. In order to optimize the fermentation outcomes, fed-batch fermentation was performed with hydrolyzed molasses in PFB, giving 91.89 ± 4.59 g l^-1 of propionic acid at 254 h. Further studies were carried out using hydrolyzed waste propionibacterium cells as substitute nitrogen source, resulting in a propionic acid concentration of 79.81 ± 3.99 g l^-1 at 302 h. The present study suggests that the low-cost molasses and waste propionibacterium cells can be utilized for the green and economical production of propionic acid by P. freudenreichii.