Effects of glucose and glycerol on gamma-poly(glutamic acid) formation by Bacillus licheniformis ATCC 9945a

Bacillus licheniformis ATCC 9945a is one of the bacterial strains that produce gamma-poly(glutamic acid) (gamma-PGA). The use of carbohydrate medium components for gamma-PGA production was explored. Cells were grown in shake flasks or in controlled pH fermentors using medium formulations that contain different carbon sources. During the cultivations, aliquots were removed to monitor cell growth, carbon utilization, polymer production, and polymer molecular weight. Glucose was a better carbon source than glycerol for cell growth. Furthermore, glucose was utilized at a faster rate than glycerol, citrate, or glutamate. However, by using mixtures of glucose and glycerol in medium formulations, the efficiency of gamma-PGA production increased. For example, by increasing the glycerol in medium formulations from 0 to 40 g/L, the gamma-PGA broth concentration after 96 h increased from 5.7 to 20.5 g/L. Considering that glycerol utilization was low for the glucose/glycerol mixtures studied, it was unclear as to the mechanism by which glycerol leads to enhanced product formation. Cell growth and concomitant gamma-PGA production (12 g/L) at pH 6.5 was possible using glucose as a carbon source if trace amounts (0.5 g/L each) of citrate and glutamate were present in the medium. We suggested that citrate and glutamate were useful in preventing salt precipitation from the medium. In addition, glutamate may be preferred relative to ammonium chloride as a nitrogen source. The conversion of glucose to gamma-PGA by the strain ATCC 9945a was believed to occur by glycolysis of glucose to acetyl-CoA and tricarboxylic acid (TCA) cycle intermediates that were then metabolized via the TCA cycle to form alpha-ketoglutarate, which is a direct glutamate precursor.     

Production of glucose 6-phosphate dehydrogenase from genetically modified Saccharomyces cerevisiae grown by batch fermentation process

In a 5-L fermentor (NBS-MF 105), Saccharomyces cerevisiae W303-181 (1.0 g dry matter/L) was inoculated into 3.0 L of liquid medium containing glucose (10 or 20 g/L), yeast nitrogen base (YNB, 3.7 or 7.4 g/L), l-histidine (0.02 g/L), l-tryptophan (0.02 g/L), uracil (0.02 g/L), and adenine (0.02 g/L). The culture was carried out batchwise for 12 or 24 h at 30 degrees C, pH 4.6 or 5.7, aeration of 0, 0.8, 1.7 or 2.2 vvm, and agitation of 400 rpm. The highest G6PDH productivity (10.5 U/L.h) and specific activity (320 U/mg of protein) occurred at aeration of 2.2 vvm, pH 5.7, 10 g/L of glucose, and 3.7 g/L of YNB. The G6PDH specific activity attained was comparable with those of commercial preparations, which are between 50 and 600 U/mg of protein.     

Effect of aeration and agitation on synthesis of poly (γ-glutamic acid) in batch cultures of <Emphasis Type="Italic">Bacillus licheniformis</Emphasis> NCIM 2324

The effects of aeration and agitation on the production and molecular weight of poly (γ-glutamic acid) (PGA) were systematically investigated in batch fermentor cultures of Bacillus licheniformis NCIM 2324. A high aeration rate and agitation speed enhanced the growth of B. licheniformis NCIM 2324, but did not always lead to high PGA production. Additionally, PGA production actually decreased at very high aeration rates and agitation speeds. The maximum PGA concentration was obtained at 750 rpm and 1 vvm. Rheological studies revealed that fermentation broth during production of PGA exhibited pseudoplastic behavior. The effects of aeration and agitation on the molecular weight of PGA were also studied, and the rate and extent of the decrease in the molecular weight of PGA as a function of time were found to be much greater at high aeration than low aeration. The PGA production of 46.34 g/L with a specific productivity of 0.17 g-PGA/g-biomass/ h and a PGA yield of 0.48 with respect to total substrate observed in the present study are much higher than the values reported in previously conducted studies.     

Production of chum salmon cystatin from the recombinant <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis> optimized using response surface methodology

Chum salmon cystatin was overexpressed on Saccharomyces cerevisiae YPH 499. At first, the culture condition for the production of recombinant chum salmon cystatin (RC) by S. cerevisiae YPH 499 was optimized in a shake flask using response surface methodology. Three independent variables; medium pH, inducing time, and the amount of inducing assistant, were analyzed to get the optimal condition for the production of RC. The results were fitted to a second-order polynomial equation, in which the determination coefficient (R ²) was 0.904. The highest RC production in a shake flask, 0.57 U/mL was obtained at 5.7 of medium pH, 6.7 h of inducing time, and 5.6 g/L of inducing assistant. Based on the results of shake flask, the effects of agitation and aeration rates on the production of RC by S. cerevisiae YPH 499 were determined for scaleup in a fermentor. The highest production of RC in a fermentor, 0.56 U/mL was obtained at 350 rpm of agitation rate and 1.0 vvm of aeration rate. RC at 100 μg/g showed the highest inhibitory activity against the autolysis of Alaska pollock surimi based on the analysis of TCA-soluble peptides.     

Increase of xylitol production rate by controlling redox potential in Candida parapsilosis

The effect of redox potential on xylitol production by Candida parapsilosis was investigated. The redox potential was found to be useful for monitoring the dissolved oxygen (DO) level in culture media, especially when the DO level was low. An increase in the agitation speed in a 5 L fermentor resulted in an increased culture redox potential as well as enhanced cell growth. Production of xylitol was maximized at a redox potential of 100 mV. As the initial cell concentration increased from 8 g/L to 30 g/L, the volumetric productivity of xylitol increased from 1.38 g/L. h to 4.62 g/L. h. A two-stage xylitol production strategy was devised, with stage 1 involving rapid production of cells under well-aerated conditions, and stage 2 involving cultivation with reduced aeration such that the culture redox potential was 100 mV. Using this technique, a final xylitol concentration of 180 g/L was obtained from a culture medium totally containing 254.5 g/L xylose in a 3,000 L pilot scale fermentor after 77 h fermentation. The volumetric productivity of xylitol during the fermentation was 2.34 g/L. h.     

重组毕赤酵母发酵牛肉风味肽的中试研究

研究分泌表达16拷贝牛肉风味肽（beefy meaty peptide, BMP）毕赤酵母工程菌株(Pichia pastoris GS115-16B2)的500L发酵罐中试发酵工艺。在500L发酵罐中采用三步发酵法进行了3批次中试发酵实验,设定菌体培养阶段温度为30℃,pH5.0,诱导表达阶段温度为28℃,pH3.0。在发酵程中通过调节搅拌速度、通气量和罐压等措施来使DO维持在20%~35%左右,总共发酵126h（诱导时间为96h）,当诱导88h后（发酵118h）,600nm波长下的光密度值(OD600)达到184.5,菌体湿重达到318.7g/L,目的产物BMP的表达量达到最高为172 mg/L,实现了BMP的高效表达。通过中试发酵初步建立了工程菌P. pastoris GS115-16B2的中试发酵工艺,为BMP的进一步研究开发奠定了良好基础。     

Effect of flow rate pattern on glucose-6-phosphate dehydrogenase synthesis in fed-batch culture of recombinant Saccharomyces cerevisiae

A strain of genetically modified Saccharomyces cerevisiae (S. cerevisiae) W303 181 was used to improve glucose-6-phosphate dehydrogenase (G6PDH) production in aerobic culture. Fed-batch cultures were carried out in a 5 L fermentor at variable values of the parameter K, namely, 0.2, 0.3, 0.5, 0.7, and 0.8 h(-)(1). The highest G6PDH production (1164 U/L) and specific activity (517 U/g(cell)) were obtained using the following conditions: glucose, 5.0 g/L; adenine, 8 microg/mL; histidine, 8 microg/mL; tryptophan, 8 microg/mL; temperature, 30 degrees C; inoculum, 1.28 g/L; pH, 5.7; agitation, 400 rpm; aeration, 2.2 vvm; and K, 0.2 h(-)(1). The exponential feeding pattern increased cell density (2.14 g/L), enzyme productivity (149.27), and biomass yield (0.18 g(glu)/g(cell)( )(mass)). The level of G6PDH in the genetically modified S. cerevisiae was approximately 4.1-fold higher than that found in a commercial strain.     

Rhamnolipid production in batch and fed-batch fermentation using<Emphasis Type="Italic">Pseudomonas aeruginosa</Emphasis> BYK-2 KCTC 18012P

The optimization of culture conditions for the bacteriumPseudomonas aeruginosa BYK-2 KCTC 18012P, was performed to increase its rhamnolipid production. The optimum level for carbon, nitrogen sources, temperature and pH, for rhamnolipid production in a flask, were identified as 25 g/L fish oil, 0.01% (w/v) urea, 25 and pH 7.0, respectively. Optimum conditions for batch culture, using a 7-L jar fermentor, were 200 rpm of agitation speed and a 2.0 L/min aeration rate. Under the optimum conditions, on fish oil for 216 h, the final cell and rhamnolipid concentrations were 5.3 g/L and 17.0 g/L respectively. Fed-batch fermentation, with different feeding conditions, was carried out in order to increase, cell growth and rhamnolipid production by thePseudomonas aeruginosa, BYK-2 KCTC 18012P. When 2.5 g of fish oil and 100 mL basal salts medium, containing 0.01% (w/v) urea, were fed intermittently during the fermentation, the final cell and rhamnolipid concentrations at 264 h, were 6.1 and 22.7 g/L respectively. The fed-batch culture resulted in a 1.2-fold increase in the dry cell mass and a 1.3-fold increase in rhamnolipid production, compared to the production of the batch culture. The rhamnolipid production-substrate conversion factor (0.75 g/g) was higher than that of the batch culture (0.68 g/g).     

Optimization of process parameters for the production of carbonyl reductase by <Emphasis Type="Italic">Candida viswanathii</Emphasis> in a laboratory-scale fermentor

The effect of pH, aeration and mixing on the growth and production of carbonyl reductase by Candida viswanathii was investigated in a 6.6-l fermentor. Controlling the pH at 8.0 had a very significant effect on the enzyme production. Aeration and agitation influenced the dissolved oxygen concentration which in turn affected growth as well as enzyme production. A maximum carbonyl reductase activity (53 Umg⁻¹) was attained in 24 h under the optimal cultivation conditions of controlled pH at 8.0, aeration rate 1 vvm and an agitation speed of 250 rpm at 25°C. The enzyme activity was twice as high (56 Umg⁻¹) in the fermentor as compared to a shake flask. Further, the duration of growth and enzyme production in the fermentor was shortened. Cells cultivated under the optimized conditions were used for the preparative scale reduction of N, N-dimethyl-(3-keto)-2-thienyl-propanamine to (S)-N, N-dimethyl-(3-hydroxy)-2-thienyl-propanamine, a key intermediate in the production of the important antidepressant drug (S)-duloxetine.     

Optimization of ectoine synthesis through fed-batch fermentation of Brevibacterium epidermis

A production process for ectoine has been developed, using Brevibacterium epidermis DSM20659 as the producer strain. First, the optimal conditions for intracellular synthesis of ectoine were determined. The size of the intracellular ectoine pool is shown to be dependent on the external salt concentration, type of carbon source, and yeast extract concentration. Under the optimized conditions of 1 M NaCl, 50 g/L monosodium glutamate, and 2.5 g/L yeast extract, a maximum concentration of intracellular ectoine of 0.9 g/L was obtained in shake flask cultures. After optimizing the batch fermentation parameters of temperature, pH, agitation, and aeration, the yield could be further increased by applying the fed-batch fermentation principle in 1.5- to 2-L fermentors. Glutamate and yeast extract were fed to the bacterial cells such that the total glutamate concentration in the broth remained constant. A total yield of 8 g ectoine/L fermentation broth was obtained with a productivity of 2 g ectoine/L/day. After the bacterial cells were harvested from the culture broth, the ectoine was recovered from them by a two-step extraction with water and ethanol. Crystallization of the product was obtained after concentration of the extract via evaporation under reduced pressure. After this downstream process, 55% of the ectoine produced in the fermentor could be crystallized in four fractions. The first fractions were of very high purity (98%). This production process can compete with other described production processes for ectoine in productivity and simplicity. Further advantages are the relatively low amounts of NaCl needed and the absence of hydroxyectoine, often a byproduct, in the final product.     

Production of carbonyl reductase by Geotrichum candidum in a laboratory scale bioreactor

Fungal fermentation is very complex in nature due to its nonlinear relationship with the time, especially in batch culture. Growth and production of carbonyl reductase by Geotrichum candidum NCIM 980 have been studied in a laboratory scale stirred tank bioreactor at different pH (uncontrolled and controlled), agitation, aeration and dissolved oxygen concentration. The yield of the process has been calculated in terms of glucose consumed. Initial studies showed that fermenter grown cells have more than 15 times higher activity than that of the shake flask grown cells. The medium pH was found to have unspecific but significant influence on the enzyme productivity. However, at controlled pH 5.5 the specific enzyme activity was highest (306U/mg). Higher agitation had detrimental effect on the cell mass production. Dissolved oxygen concentration was maintained by automatic control of the agitation speed at an aeration rate of 0.6 volume per volume per minute (vvm). Optimization of glucose concentration yielded 21g/l cell mass with and 9.77x10(3)U carbonyl reductase activity/g glucose. Adaptation of different strategies for glucose feeding in the fermenter broth was helpful in increasing the process yield. Feeding of glucose at a continuous rate after 3h of cultivation yielded 0.97g cell mass/g glucose corresponding to 29.1g/l cell mass. Volumetric oxygen transfer coefficient (K(L)a) increased with the increasing of agitation rate.     

Production of L(+)-lactic acid from glucose and starch by immobilized cells of Rhizopus oryzae in a rotating fibrous bed bioreactor

A rotating fibrous-bed bioreactor (RFB) was developed for fermentation to produce L(+)-lactic acid from glucose and cornstarch by Rhizopus oryzae. Fungal mycelia were immobilized on cotton cloth in the RFB for a prolonged period to study the fermentation kinetics and process stability. The pH and dissolved oxygen concentration (DO) were found to have significant effects on lactic acid productivity and yield, with pH 6 and 90% DO being the optimal conditions. A high lactic acid yield of 90% (w/w) and productivity of 2.5 g/L.h (467 g/h.m(2)) was obtained from glucose in fed-batch fermentation. When cornstarch was used as the substrate, the lactic acid yield was close to 100% (w/w) and the productivity was 1.65 g/L.h (300 g/h.m(2)). The highest concentration of lactic acid achieved in these fed-batch fermentations was 127 g/L. The immobilized-cells fermentation in the RFB gave a virtually cell-free fermentation broth and provided many advantages over conventional fermentation processes, especially those with freely suspended fungal cells. Without immobilization with the cotton cloth, mycelia grew everywhere in the fermentor and caused serious problems in reactor control and operation and consequently the fermentation was poor in lactic acid production. Oxygen transfer in the RFB was also studied and the volumetric oxygen transfer coefficients under various aeration and agitation conditions were determined and then used to estimate the oxygen transfer rate and uptake rate during the fermentation. The results showed that the oxygen uptake rate increased with increasing DO, indicating that oxygen transfer was limited by the diffusion inside the mycelial layer.     

Cytochrome c production in jar fermentor by a mutant,methlomonas sp.

The growth and cytochrome c production of Methylomonas sp. YK 56 were optimized by the control of pH, aeration and agitation in a jar fermentor. Under the optimal conditions, 5.8 g of dry cell weight (DCW) and 64 mg of cytochrome c per l of culture broth were obtained. These values were increased to 6.6 g and 76 mg, respectively, by additions of peptone and L-histidine.When methanol and the feed medium were fed during the cultivation, about 160 mg of cytochrome c per l of culture broth was obtained after 34 h of cultivation. In continuous culture, the production rate of the cytochrome c reached a maximum value of 11.6 mg per h at a dilution rate of 0.13 per h.     

Adsorption of toxic mercury(II) by an extracellular biopolymer poly(gamma-glutamic acid)

Adsorption of mercury(II) by an extracellular biopolymer, poly(gamma-glutamic acid) (gamma-PGA), was studied as a function of pH, temperature, agitation time, ionic strength, light and heavy metal ions. An appreciable adsorption occurred at pH>3 and reached a maximum at pH 6. Isotherms were well predicted by Redlich-Peterson model with a dominating Freundlich behavior, implying the heterogeneous nature of mercury(II) adsorption. The adsorption followed an exothermic and spontaneous process with increased orderliness at solid/solution interface. The adsorption was rapid with 90% being attained within 5 min for a 80 mg/L mercury(II) solution, and the kinetic data were precisely described by pseudo second order model. Ionic strength due to added sodium salts reduced the mercury(II) binding with the coordinating ligands following the order: Cl(-) >SO(4)(2-) >NO(3)(-). Both light and heavy metal ions decreased mercury(II) binding by gamma-PGA, with calcium(II) ions showing a more pronounced effect than monovalent sodium and potassium ions, while the interfering heavy metal ions followed the order: Cu(2+) > Cd(2+) > Zn(2+). Distilled water adjusted to pH 2 using hydrochloric acid recovered 98.8% of mercury(II), and gamma-PGA reuse for five cycles of operation showed a loss of only 6.5%. IR spectra of gamma-PGA and Hg(II)-gamma-PGA revealed binding of mercury(II) with carboxylate and amide groups on gamma-PGA.     

Enhancement of ribitol production during fermentation of <Emphasis Type="Italic">Trichosporonoides oedocephalis</Emphasis> ATCC 16958 by optimizing the medium and altering agitation strategies

To maximize the productivity of ribitol, which is an important starting material for the production of one expensive rare sugar, L-ribose, the effects of culture medium and agitation speed on cell growth as well as on the productivity of ribitol were thoroughly investigated in a 7 L fermentor. The maximum volumetric productivity, 0.322 g/L/h of ribitol, were obtained at an initial glucose concentration of 200 g/L in a batch culture. Based on the optimum glucose concentration, the ribitol yield conversed from glucose was up to 0.193 g/g when 1% yeast extract was used as a nitrogen source. When the agitation speed was maintained at 200 rpm, the ribitol concentration of 38.60 g/L was collected after 120 h of cultivation time. Additionally, the scheme of two-phase agitation and glucose infusion was employed. To begin, in the first 24 h of fermentation, a high agitation rate at 350 rpm and the initial glucose concentration of 50 g/L were applied, and the biomass concentration of 25.50 g/L was achieved at 36 h of incubation; whereas this value was observed until 60 h in the former batch fermentation methods. Then, in the second phase, with the agitation speed reduced to 150 rpm and the infusion amount of glucose controlled at 150 g/L, the yield of ribitol reached to 65.00 g/L in two-phase agitation fermentation and was 1.68 fold of that obtained in one-stage batch fermentation. To our knowledge, this study first demonstrates its significant effectiveness in improving ribitol production with the application of Trichosporonoides oedocephalis ATCC 16958.     

Batch and fed batch production of pectin lyase and pectate lyase by novel strain Debaryomyces nepalensis in bioreactor

The effect of various parameters such as pH, agitation and aeration was studied for maximum production of pectin lyase (PL) and pectate lyase (PGL) by a novel yeast strain Debaryomyces nepalensis in bioreactor. The optimal levels of pH, aeration and agitation rate was found to be 7.0, 300rpm and 1vvm, respectively. Under these conditions, D. nepalensis produced 14,200U/L of PL and 12,000U/L of PGL corresponding to a productivity of 600U/Lh and 500U/Lh of PL and PGL, respectively. Fed-batch production was studied by feeding inducer (lemon peel), carbon source (galactose) individually and in combination at 12h of growth for enhanced production of PL and PGL. Combined feeding of inducer and carbon source at 12h was found to be the best strategy for enhanced production of PL and PGL. Under these conditions, production of PL and PGL increased to 23,300U/L and 22,400U/L, respectively which corresponded to a productivity of 728U/Lh of PL and 700U/Lh of PGL, respectively. The production was increased by 1.6- and 1.8-fold and productivity by 1.2- and 1.4-fold for PL and PGL, respectively when compared to batch culture.     

Effects of cultivation conditions on the production of natamycin with Streptomyces gilvosporeus LK-196

Natamycin is a very attractive antifungal agent with wide applications in medical and food industries. In order to improve the productivity of natamycin, the effects of cultivation conditions were investigated with Streptomyces gilvosporeus LK-196 in the shake flasks and 30-L fermentors. The results showed that dissolved oxygen and shear force would affluence the biosynthesis of natamycin significantly. The high concentration of natamycin (2.03g/L) was achieved under the suitable culture conditions in the shake flask scale. Further investigations in 30-L fermentors showed that the optimal pH was controlled at 6.0 during the whole bioprocess, and the dissolved oxygen level should be more than 30% by adjusting the aeration and agitation rates for high production of natamycin. Under these optimal conditions the high concentration of natamycin (3.94g/L) was achieved with Str. gilvosporeus LK-196 in the 30-L fermentor. Finally, the high-level fermentation process was successfully scaled up to 1000-L fermentors and 18,000-L fermentors in the pilot plant.     

High yield and cost‐effective production of poly(γ‐glutamic acid) with Bacillus subtilis

Poly(γ‐glutamic acid) (γ‐PGA) is a promising biopolymer with many potential industrial and pharmaceutical applications. To reduce the production costs, the effects of yeast extract and L ‐glutamate in the substrate for γ‐PGA production were investigated systematically at shake flask scale. The results showed that lower concentrations of yeast extract (40 g/L) and L ‐glutamate (30 g/L) were beneficial for the cost‐effective production of γ‐PGA in the formulated medium. By maintaining the glucose concentration in the range of 3–10 g/L via a fed‐batch strategy in a 10‐L fermentor, the production of γ‐PGA was greatly improved with the highest γ‐PGA concentration of 101.1 g/L, a productivity of 2.19 g/L·h and a yield of 0.57 g/g total substrate, which is about 1.4‐ to 3.2‐fold higher than those in the batch fermentation. Finally, this high‐density fermentation process was successfully scaled up in a 100‐L fermentor. The present work provides a powerful approach to produce this biopolymer as a bulk chemical in large scale.     

溶氧对Blakeslea trispora分批发酵生产β-胡萝卜素的影响

在摇瓶和5 L发酵罐中研究了溶氧 (DO) 对Blakeslea trispora分批发酵生产β-胡萝卜素的影响,总结了5 L发酵罐中β-胡萝卜素发酵过程中溶氧的变化规律.结果表明,当500 mL摇瓶装液量为50 mL,转速为240 r/min条件下发酵生产β-胡萝卜素产量最大,达到3.416 g/L; 5 L发酵罐中,在搅拌转速为1 000 r/min,通气量为1.5 vvm的条件下,β-胡萝卜素的产量可达到3.712 g/L,略高于摇瓶,这可能是由于5 L发酵罐中的气液传递和混合状况好于摇瓶,促进了产物的合成.