Gas holdup and overall volumetric oxygen transfer coefficient in airlift contactors

The two major types of airlift contactors, concentric-tube and external-loop, were investigated for their gas holdup (riser and downcomer) and overall mass transfer characteristics. Results obtained in batch charges of tap water and 0.15 kmol/m(3) NaCl solution are reported for external-loop airlift contactors having downcomer-to-riser cross-sectional area ratios, A(d)/A(r), ranging from 0.11 相似文献   

Mass transfer phenomena in an airlift reactor: effects of solids loading and temperature

Gas holdups and volumetric mass transfer coefficients were measured in a concentric tube airlift reactor designed for the microbial desulfurization of coal. The solutions studied were comprised of an acidified basal salts solution containing thirteen different weight percentages (0 to 40) of coal (74 mum Ohio #1) at three different temperatures (30, 50, and 72 degrees C). Gas holdup epsilon(G) decreased with solids loading for the entire range studied. An enhancement in the volumetric mass transfer coefficient K(L)a with respect to that in pure solution was observed from zero to approximately 5 wt % (solids volume fraction epsilon(s) = 0.035), the maximum enhancement occurring at approximately 2 wt % (epsilon(s) = 0.014). At higher solids fractions, the mass transfer coefficient decreased with further solids additions. Gas holdups and the mass transfer coefficients increased with temperature over the studied range. The K(L)a and epsilon(G) were correlated to three process variables separately and the separate correlations combined to yield generalized correlations for the mass transfer coefficient and gas holdup for this system. The correlations may be used for design, operation, and ost estimation of such systems.     

Optimization of culture variables for improving glucoamylase production by alginate-entrapped Thermomucor indicae-seudaticae using statistical methods

Alginate-entrapped sporangiospores of Thermomucor indicae-seudaticae were used for the production of glucoamylase. The critical variables that affected glucoamylase production were identified by Plackett-Burman design (sucrose, yeast-extract, K(2)HPO(4) and asparagine) and further optimized by using a four factor central composite design (CCD) of response surface methodology (RSM). Immobilized sporangiospores secreted 41% and 60% higher glucoamylase titers in shake flasks and airlift fermenter, respectively, when the variables were used at their optimum levels (sucrose 3.0%, yeast-extract 0.2%, K(2)HPO(4) 0.1% and asparagine 0.35%). Glucoamylase production (26.3 U ml(-1)) in the optimized medium was in good agreement with the values predicted by the quadratic model (26.7 U ml(-1)), thereby confirming its validity. The enzyme production was sustainable in flasks of higher volume and also airlift fermenter, and attained a peak within 32 h in the fermenter as compared to that of 48 h in shake flasks.     

Poly(L-lactide)-degrading enzyme production by Actinomadura keratinilytica T16-1 in 3 L airlift bioreactor and its degradation ability for biological recycle

The optimal physical factors affecting enzyme production in an airlift fermenter have not been studied so far. Therefore, the physical parameters such as aeration rate, pH, and temperature affecting PLA-degrading enzyme production by Actinomadura keratinilytica strain T16-1 in a 3 l airlift fermenter were investigated. The response surface methodology (RSM) was used to optimize PLA-degrading enzyme production by implementing the central composite design. The optimal conditions for higher production of PLA-degrading enzyme were aeration rate of 0.43 vvm, pH of 6.85, and temperature at 46° C. Under these conditions, the model predicted a PLA-degrading activity of 254 U/ml. Verification of the optimization showed that PLA-degrading enzyme production of 257 U/ml was observed after 3 days cultivation under the optimal conditions in a 3 l airlift fermenter. The production under the optimized condition in the airlift fermenter was higher than un-optimized condition by 1.7 folds and 12 folds with un-optimized medium or condition in shake flasks. This is the first report on the optimization of environmental conditions for improvement of PLA-degrading enzyme production in a 3 l airlift fermenter by using a statistical analysis method. Moreover, the crude PLA-degrading enzyme could be adsorbed to the substrate and degraded PLA powder to produce lactic acid as degradation products. Therefore, this incident indicates that PLA-degrading enzyme produced by Actinomadura keratinilytica NBRC 104111 strain T16-1 has a potential to degrade PLA to lactic acid as a monomer and can be used for the recycle of PLA polymer.     

微生物发酵生产十三碳二元酸的研究

分类号ＴＱ９２０．１文献标识码Ｂ文章编号０００１６２０９（１９９９）０３０２７９８１十三碳二元酸（ＤＣ１３）是化学合成麝香Ｔ香料和尼龙１３１３工程塑料的重要原料。ＤＣ１３在自然界中不单独存在,用化学方法难以合成,只能从菜籽油中提出甘油芥酸酯再经…     

Influence of ambient air temperature on the cooling/heating load of a single cell protein jacketed fermenter operating on cheese whey under continuous conditions

The heat generated by mixing and lactose metabolism, during the continuous production of single cell protein from cheese whey lactose using a jacketed fermenter with running cooling water, was calculated using a heat balance equation. The technique quantified the heat produced in and lost from the fermentation unit. Most of the heat generated by mixing in the cell-free system (97.47%) was lost with exhaust gas, while a very small amount (2.53%) was lost through the fermenter lid, wall, and bottom. The heat generated by mixing was significant (26.31% of the total heat generated in the fermentation system with an active yeast population present) and, therefore, cannot be ignored in heat balance calculations. About 19.71% of the total heat generated in the reactor was lost through the coolant at an ambient temperature of 22 +/- 0.5 degrees C, showing the need for a cooling system. A yeast population size of 986 million cells/mL and a lactose removal efficiency of 95.6% were observed. About 72.5% and 27.5% of the lactose consumed were used for growth and respiration, respectively. A yield of 0.66 g of cells/g of lactose was achieved. The heat released by unit biomass was 7.05 kJ/g of cells. The results showed the significant impact of ambient air temperature on the cooling load. The heat to be removed from the medium by the cooling system varied from 3.46 to 281.56 kJ/h when the temperature increased from 16 to 30 degrees C. A heating system is needed to maintain the medium temperature at 34 degrees C when the ambient air temperature is below 16 degrees C.     

Hydrodynamics and mass transfer in Aspergillus niger fermentations in bubble column and loop bioreactors

The influence of Aspergillus niger broth rheology, bioreactor geometry, and superficial gas velocity on the volumetric liquid phase oxygen transfer coefficient (k(L)a(L)), riser gas holdup (epsilon(GR)), and circulating liquid velocity (u(LR)) was studied in a bubble column (BC) and two external-circulation-loop airlift (ECLAL) bioreactors. The results are compared to those of previous studies on homogeneous fluids and in particular with a recent study on non-Newtonian carboxymethylcellulose (CMC) solutions conducted in the same contactors used for the A. niger fermentations. As expected from the CMC-based studies, in the heterogeneous broths of A. niger epsilon(GR), k(L)a(L), and u(LR) decreased with increasing broth apparent viscosity; epsilon(GR) and k(L)a(L) decreased with increasing downcomer-to-riser cross-sectional area ratio, A(d)/A(r), whereas u(LR) increased with increasing A(d)/A(r). Gas holdup data in the airlift fermentations of A. niger were well predicted by the CMC-based correlation. However, the CMC-based correlations produced conservative estimations of k(L)a(L) and overestimates of u(LR) compared to the observed values in the A. niger broths.     

Microbial growth and production kinetics of Streptomyces antibioticus Tü 6040

Streptomyces antibioticus Tü 6040 is the producer of simocyclinones, which belong to a novel family of angucyclinone antibiotics some of which show antitumor activities. Growth and antibiotic production is dependent on the medium composition, especially on the carbon and nitrogen source, and on the fermentation conditions. The best results with respect to antibiotic productivity were achieved using a chemically defined medium with glycerol and L-lysine as carbon and nitrogen source, respectively, in an airlift fermenter with minimised shear stress at low gas flow rates withour oxygen limitation. These conditions led to a homogeneous formation of pellets of 1–2 mm in diameter and guaranteed reproducible product yields of the main compound, simocyclinone D8, in the range of 300 mg/l.     

Medium optimization for the production of cyclic adenosine 3',5'-monophosphate by Microbacterium sp. no. 205 using response surface methodology

Response surface methodology was employed to optimize medium composition for the production of cyclic adenosine 3',5'-monophosphate (cAMP) with Microbacterium sp. no. 205. A fractional factorial design (2(11-7)) was applied to evaluate the effects of different components in the medium. K(2)HPO(4), MgSO(4) and NaF were found to significantly influence on the cAMP production. The steepest ascent method was used to access the optimal region of the medium composition. The concentrations of the three factors were optimized subsequently using central composite design and response surface methodology. The optimal medium composition to achieve the optimal cAMP production was determined (g/L): K(2)HPO(4), 12.78; MgSO(4), 3.53 and NaF, 0.18. The corresponding cAMP concentration was 8.50 g/L, which was about 1.8-fold increase compared with that using the original medium. Validation experiments were also carried out to prove the adequacy and the accuracy of the model obtained. The cAMP fermentation in 5L fermenter reached 9.87 g/L.     

Growth kinetics of Lactobacillus acidophilus under ohmic heating

Lactobacillus acidophilus OSU133 was inoculated into MRS broth in a fermenter vessel and incubated at 30, 35, or 45 degrees C with agitation. Incubation temperatures were attained by conventional or ohmic heating. An electrical current at low (15 V) or high (40 V) voltage was used to heat the culture directly during fermentations under ohmic heating. The growth parameters (lag period, minimum generation time, and maximum growth) and changes in pH were determined during fermentation. Metabolic activities (consumption of glucose and production of lactic acid and bacteriocin) were determined during fermentation at 35 degrees C under both heating methods. Lag period for L. acidophilus was affected appreciably by the method of heating, but the magnitude of these changes depended on the fermentation temperature. When fermentation was done at 30 degrees C, lag period decreased by 94% under low-voltage ohmic, compared with conventional, heating methods. Ohmic heating did not change the generation time significantly and caused slight, but significant (p < 0.01) decrease in maximum growth. Therefore, the electric current enhances the early stages, but it inhibits the late stages of growth. Ohmic, compared with conventional, heating resulted in higher final pH and lower bacteriocin activity in the fermented medium. However, ohmic heating at 35 degrees C had minimal effect on glucose utilization and lactic acid production by L. acidophilus. Results show that measurement of the electric current when ohmic heating is done at a constant voltage may be used in monitoring such fermentations. In conclusion, ohmic heating is potentially useful in certain applications related to fermented foods. (c) 1996 John Wiley & Sons, Inc.     

On-line estimation of lactic acid concentration by conductivity measurement in fermentation broth

On-line estimation of lactic acid concentration in fermentation broth is very feasible with conductivity probe directly in fermenter. This paper shows that lactic acid is the most influent parameter of medium on the conductivity measurements. The precision and longevity of conductivity probe are excellent in normal conditions of lactic acid production by fermentation process.     

Optimization of fermentation medium and conditions for mycelial growth and water-soluble exo-polysaccharides production by Isaria farinosa B05

The optimal fermentation medium and conditions for mycelial growth and water-soluble exo-polysaccharides production by Isaria farinosa B05 were investigated. The medium components and fermentation conditions were optimized according to the one at a time method, while the concentration of medium components was determined by the orthogonal matrix method. The results showed that the optimal fermentation medium was as follows: sucrose 3.5% (w/v), peptone 0.5%, yeast extract 0.2%, K(2)HPO(4) 0.1%, and MgSO(4) 0.05%. The suitable fermentation conditions were as follows: initial pH 7.0, temperature 25 degrees C, medium volume 75 mL/250 mL, inoculum volume 5% (v/v), time 5d. In such optimal nutrition and environmental conditions, the maximal mycelial yield was 2.124 g/100 mL after 4 day's fermentation, while maximal water-soluble exo-polysaccharides production reached 2.144 g/L after 5 day's fermentation.     

Medium optimization for the production of recombinant nattokinase by Bacillus subtilis using response surface methodology

Nattokinase is a potent fibrinolytic enzyme with the potential for fighting cardiovascular diseases. Most recently, a new Bacillus subtilis/Escherichia coli (B. subtilis/E. coli) shuttle vector has been developed to achieve stable production of recombinant nattokinase in B. subtilis (Chen; et al. 2007, 23, 808-813). With this developed B. subtilis strain, the design of an optimum but cost-effective medium for high-level production of recombinant nattokinase was attempted by using response surface methodology. On the basis of the Plackett-Burman design, three critical medium components were selected. Subsequently, the optimum combination of selected factors was investigated by the Box-Behnken design. As a result, it gave the predicted maximum production of recombinant nattokinase with 71 500 CU/mL for shake-flask cultures when the concentrations of soybean hydrolysate, potassium phosphate, and calcium chloride in medium were at 6.100, 0.415, and 0.015%, respectively. This was further verified by a duplicated experiment. Moreover, the production scheme based on the optimum medium was scaled up in a fermenter. The batch fermentation of 3 L was carried out by controlling the condition at 37 degrees C and dissolved oxygen reaching 20% of air saturation level while the fermentation pH was initially set at 8.5. Without the need for controlling the broth pH, recombinant nattokinase production with a yield of 77 400 CU/mL (corresponding to 560 mg/L) could be obtained in the culture broth within 24 h. In particular, the recombinant B. subtilis strain was found fully stable at the end of fermentation when grown on the optimum medium. Overall, it indicates the success of this experimental design approach in formulating a simple and cost-effective medium, which provides the developed strain with sufficient nutrient supplements for stable and high-level production of recombinant nattokinase in a fermenter.     

Enhanced doxorubicin production by Streptomyces peucetius using a combination of classical strain mutation and medium optimization

Abstract

Doxorubicin (DXR), which is produced by Streptomyces peucetius, is an important anthracycline-type antibiotic used for the treatment of various cancers. However, due to the low DXR productivity of wild-type S. peucetius, it is difficult to produce DXR by one-step fermentation. In this study, a DXR-resistance screening method was developed to screen for DXR high-producing mutants. Then, S. peucetius SIPI-11 was treated several times with UV and ARTP (atmospheric and room temperature plasma) to induce mutations. Treated strains were screened by spreading on a DXR-containing plate, isolating a mutant (S. peucetius 33-24) with enhanced DXR yield (570?mg/L vs. 119?mg/L for the original strain). The components of the fermentation medium, including the carbon and nitrogen sources, were optimized to further enhance DXR yield (to 850?mg/L). The pH of the fermentation medium and culture temperature were also optimized for effective DXR production. Finally, DXR production by S. peucetius 33-24 was investigated in flask culture and a fermenter. The yield of DXR was as high as 1100?mg/L in a 5-L fermenter, which is the highest DXR productivity reported thus far, suggesting that S. peucetius 33-24 has the potential to produce DXR by direct fermentation.     

代谢甘油高产乳酸的菌种选育及培养基优化

分离出一株可高效利用甘油生产乳酸的菌株, 经过生理生化和16S rDNA分子鉴定, 确定其属于大肠埃希氏菌, 命名为Escherichia coli AC-521。通过五因素四水平正交试验, 优化了其最佳发酵培养基成分为初始甘油70 g/L, 酵母粉4 g/L, 蛋白胨7 g/L, (NH4)2SO4 10 g/L, K2HPO4 2.5 g/L。利用该最佳条件的5 L发酵罐批式补料发酵实验表明: 该菌株发酵80 h后, 乳酸产量可达到74.5 g/L, 得率为0.87 mol/mol甘油。     

Steroid transformation in a laboratory-scale glass air-lift fermenter

A glass airlift fermenter, 1550 ml working volume, was used for microbiological transformation of phytosterols. A gas hold-up of 1.6% was observed with the lowest superficial gas velocity (1.89 cm/s). The volumetric liquid circulation rate remained relatively constant (0.21 l/s to 0.23 l/s) for superficial gas velocity values up to 11.37 cm/s. A 72% conversion of sitosterol to 1,4-androstadiene-3,17-dione was obtained.     

重组大肠杆菌产尿素酶B高密度发酵条件的优化

探究重组大肠杆菌产尿素酶B（urease B subunit, UreB）的高密度发酵条件。通过实验室摇瓶和30 L发酵罐对UreB基因工程菌的发酵条件进行优化。结果表明：30 L发酵罐中以TB培养基为发酵培养基,接种量为5%,发酵温度为37 ℃,pH为6.8,溶氧量为30%左右,培养至2 h开始恒速流加50%甘油,4 h流加50%酵母提取物和50%胰蛋白胨,并加入终浓度为0.5 mmol/L的异丙基β-D-硫代半乳糖苷（isopropyl β-D-thiogalactoside,IPTG),诱导表达4 h,结束发酵,所得菌体干物质约为25.7 g/L,UreB表达量为31.4%。此工艺可以提高UreB的产量。     

固定化根霉发酵生产脂肪酶

以聚氨酯为少根根霉固定化载体,对固定化后的细胞连续重复批次发酵进行了研究。优化了重复批次发酵培养基组成。在取代发酵液40mL,取代培养基组成为全脂豆粉3%,花生油0.5％条件下,固定化菌体摇瓶实验可连续使用140h,重复9批次。酶的时空产率提高6倍。5L发酵罐小试固定化菌体可连续发酵6批次。固定化细胞连续发酵,大大缩短了发酵的时间,酶的时空产率获得大幅提高。     

Growth and nicotinate biotransformation in batch cultured and airlift fermenter grown soybean cell suspension cultures

Summary Fermentation of a heterotrophic cell suspension culture of soybean (Glycine max) in a 15 l airlift fermenter for 10 to 12 days yielded appr. 4.67 kg fr. wt. (233.5 g dr. wt.) of biomass starting with an inoculum of 300 g fr. wt. Growth limiting factors were the conditions of preculturing the cells and the available amounts of phosphate and oxygen in the fermenter culture medium. Comparison of the metabolic activity of cells grown in 200 ml Erlenmeyer flasks and in the fermenter was performed by measuring the enzyme activities of nicotinamide-amidohydrolase and SAM: nicotinic acid-N-methyltransferase both in the presence and the absence of exogenous nicotinic acid during the biotransformation of nicotinate to trigonelline. The applied nicotinic acid was quantitatively taken up by the cells and an enhanced production of trigonelline could be observed. The activities of the aforementioned soybean enzymes were the same both in the batch cultured and in the airlift fermenter grown cells indicating good physiological conditions of the cells from the fermenter process.Abbreviations SAM S-adenosyl methionine - SCV sedimented cell volume - fr. wt. fresh weight - dr. wt. dry weight     

Scale-up of biotransformation process in stirred tank reactor using dual impeller bioreactor

The gas-liquid mass transfer coefficient K(L)a in the fermenter is a strong function of mode of energy dissipation and physico-chemical properties of the liquid media. A combination of disc turbine (DT) and pitched blade turbine down flow (PTD) impellers has been tested in laboratory bioreactor for gas hold-up and gas-liquid mass transfer performance for the growth and biotransformation medium for an yeast isolate VS1 capable of biotransforming benzaldehyde to L-phenyl acetyl carbinol (L-PAC) and compared with those in water.Correlations have been developed for the prediction of the fractional gas hold-up and gas-liquid mass transfer coefficient for the above media. The mass transfer coefficient and respiration rate have been determined in the shake flask for the growth as well as for biotransformation medium. These results, then have been used to optimize the operating parameters (impeller speed and aeration) for growth and biotransformation in a laboratory bioreactor. The comparison of cell mass production and L-PAC production in the bioreactor has been done with that obtained in shake flask studies.