Optimal dissolved oxygen concentration for the production of chitinases by Serratia marcescens

Chitinase production by Serratia marcescens 990E was maximal (34 U/ml) for a dissolved oxygen concentration ranging from 20 to 50% saturation. Chitin addition (6 g/l) at the end of fermentation reactivated the growth but did not bring about further chitinase accumulation. Four chitinases with different isoelectric points were separated.     

Lipolytic enzyme production by Thermus thermophilus HB27 in a stirred tank bioreactor

In this study, lipolytic enzyme production by Thermus thermophilus HB27 at bioreactor scale has been investigated. Cultivation was performed in a 5-L stirred tank bioreactor in discontinuous mode, at an agitation speed of 200 rpm. Different variables affecting intra- and extra-cellular lipolytic enzyme production such as culture temperature and aeration rate have been analysed. The bacterium was able to grow within the temperature range tested (from 60 to 70 °C) with an optimum value of 70 °C for intra- and extra-cellular lipolytic enzyme production.On the other hand, various aeration levels (from 0 to 2.5 L/min) were employed. A continuous supply of air was necessary, but no significant improvement in biomass or enzyme production was detected when air flow rates were increased above 1 L/min. Total lipolytic enzyme production reached a maximum of 167 U/L after 3 days, and a relatively high concentration of extra-cellular activity was detected (40% of the total amount). Enzyme yield was around 158 U/g cells. Moreover, it is noteworthy that the lipolytic activity obtained operating at optimal conditions (70 °C and air flow of 1 L/min) was about five-fold higher than that attained in shake flask cultures     

Extracellular chitinase production by wild-type B-10 and mutant M-1 strains of Serratia marcescens

Molecular weights of extracellular chitinases from wild-type B-10 (62, 54, 43, 38, and 21 kDa) and mutant M-1 strains of Serratia marcescens (62, 52, 43, 38, and 21 kDa) were estimated by sodium dodecyl sulfate-polyacrylamide gel electrophoresis. In the absence of chitin inductors, chitinolytic enzymes were not found in the culture liquid of B-10, while M-10 cells produced the chitinase complex (to 470 pU/cell). Crystalline chitin insignificantly stimulated the synthesis of chitinases with molecular weights of 62, 54, and 21 kDa by B-10 (up to 20 pU/cell), but caused overproduction of all chitinases by the mutant strain (up to 2600 pU/cell). Colloidal chitin induced the production of chitinases by cells of both strains. Two peaks of chitinolytic activity were observed during cultivation of strains B-10 (350 and 450 pU/cell) and M-1 (2200 and 2400 pU/cell). The first peak of cell productivity was associated with biosynthesis of the chitinase complex. The second peak was related to the production of enzymes with molecular weights of 54, 43, 38, and 21 kDa (B-10) or 43, 38, and 21 kDa (M-1).     

Maximizing mouse embryonic stem cell production in a stirred tank reactor by controlling dissolved oxygen concentration and continuous perfusion operation

One of the key challenges in stem cell bioprocessing is the large-scale cultivation of stem cells in order to meet the demanding meaningful cell numbers needed for biomedical applications, especially for clinical settings. Mouse embryonic stem cells [1], used as a model system herein, were cultivated on microcarriers in a fully controlled stirred tank reactor (STR) [2]. The impact of varying the concentration of dissolved oxygen (at 5%, 10%, 20% and 30% DO) and operating under a continuous perfusion mode on cell growth and pluripotency maintenance was investigated. In addition, in order to further optimize the feeding strategy of the STR operating under continuous perfusion toward maximal cell production, the influence of different medium residences times (12 h, 24 h, 32 h, 48 h and 96 h) was evaluated. Overall, the maximal cell concentration of 7.9–9.2 × 10⁶ cells/mL were attained after 11 days, with no passaging required, under a DO of 10–20% in the continuous perfused bioreactor with cell retention and medium residences times of 32–48 h. Importantly, mESC expanded under these conditions, retained the expression of pluripotency markers (Oct4, Nanog and Ssea-1), as well as their differentiation potential into cells of the three embryonic germ layers.The STR-based cultivation platform optimized herein represents a major contribution toward the development of large-volume production systems of differentiated cell derivatives for a wide range of biomedical applications.     

Effects of different organic acids on 2,3-butanediol production by Serratia marcescens

考察了不同的短链有机酸对粘质沙雷氏菌合成2,3-丁二醇的影响,结果表明乙酸、乳酸、丙酮酸、琥珀酸、延胡索酸和柠檬酸均能在一定程度上提高2,3-丁二醇的产量,其中乙酸的效果最为明显,在基础培养基中添加6 g/L乙酸,与对照相比,2,3-丁二醇的产量提高了91.06％,此外菌体干重也提高了58.28％.为了揭示其中的调控机制,构建了启动子:lacZ融合报告载体,lacZ活性测定显示六种有机酸均可提高报告基因β-半乳糖苷酶的表达,其中乙酸提高β-半乳糖苷酶活性近4倍,暗示六种有机酸促进2,3-丁二醇的合成可能与诱导该合成途径相关基因的表达有关.     

不同有机酸对粘质沙雷氏菌合成2,3-丁二醇的影响

考察了不同的短链有机酸对粘质沙雷氏菌合成2,3－丁二醇的影响,结果表明乙酸、乳酸、丙酮酸、琥珀酸、延胡索酸和柠檬酸均能在一定程度上提高2,3－丁二醇的产量,其中乙酸的效果最为明显,在基础培养基中添加6g／L乙酸,与对照相比,2,3．丁二醇的产量提高了91．06％,此外菌体干重也提高了58．28％。为了揭示其中的调控机制,构建了启动子：lacZ融合报告载体,fncz活性测定显示六种有机酸均可提高报告基因B．半乳糖苷酶的表达,其中乙酸可提高B．半乳糖苷酶活性近4倍,暗示六种有机酸促进2,3－丁二醇的合成可能与诱导该合成途径相关基因的表达有关。     

Enhanced production of valienamine by Stenotrophomonas maltrophilia with fed-batch culture in a stirred tank bioreactor

Valienamine is an important medicinal intermediate with broad use in the synthesis of some stronger α-glucosidase inhibitors. In order to improve valienamine concentration in the fermentation broth and make the downstream treatment easy, a fed-batch process for the enhanced production of valienamine by Stenotrophomonas maltrophilia in a stirred tank bioreactor was developed. Results showed that supplementation of validamycin A in the process of cultivation could increase the valienamine concentration. One-pulse feeding was observed to be the best strategy. The maximum valienamine concentration of 2.35 g L⁻¹ was obtained at 156 h when 86.4 g of validamycin A was added to a 15-L bioreactor containing 8 L fermentation medium with one-pulse feeding. The maximum valienamine concentration had a great improvement and was increased above 100% compared to batch fermentation in the stirred tank bioreactor. The pH-controlled experiments showed that controlling the pH in the process of one-pulse feeding fermentation had not obvious effect on the production of valienamine.     

Production of hepatitis B core antigen in a stirred tank bioreactor: The influence of temperature and agitation

The influence of temperature and agitation on the growth ofEscherichia coli expressing hepatitis B core antigen (HBcAg) in stirred tank bioreactor were investigated. The highest specific growth rate forE. coli (0.844 h⁻¹) was achieved at a temperature of 37°C and an agitation speed of 250 rpm. The activation energy for the growth of theE. coli strain W3110IQ in the stirred tank bioreactor was estimated to be 11 kcal/mol. The highest protein yield was achieved at a temperature of 44°C and an agitation speed of 250 rpm. The relative protein concentration at 44°C is 30 and 6% higher compared to that at 30 and 37°C, respectively.     

Studies on the production of enantioselective nitrilase in a stirred tank bioreactor by Pseudomonas putida MTCC 5110

Nitrilases constitute an important class of hydrolases, having numerous industrial applications. The present work aims to address the production of nitrile hydrolyzing enzymes from Pseudomonas putida MTCC 5110 in a 6l bioreactor. Effect of various physico-chemical conditions and process parameters like pH, temperature, aeration and agitation rates and inducer concentration was studied. Further, the enzyme activity was enhanced by adopting the inducer feeding strategy. Various biochemical engineering parameters pertaining to the cultivation of P. putida in different physico-chemical conditions were reported. Finally, segregation of growth phase from the enzyme production phase allowed significant reduction in total fermentation time.     

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

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

Kinetic modeling and scale up of lipoic acid (LA) production from Saccharomyces cerevisiae in a stirred tank bioreactor

Scale up studies for production of lipoic acid (LA) from Saccharomyces cerevisiae have been reported in this paper for the first time. LA production in batch mode was carried out in a stirred tank bioreactor at varying agitation and aeration with maximum LA production of 512 mg/L obtained at 350 rpm and 25 % dissolved oxygen in batch culture conditions. Thus, LA production increased from 352 mg/L in shake flask to 512 mg/L in batch mode in a 5 L stirred tank bioreactor. Biomass production under these conditions was mathematically explained using logistic equation and data obtained for LA production and substrate utilization were successfully fitted using Luedeking–Piret and Mercier’s models. The kinetic studies showed LA production to be growth associated. Further enhancement of LA production was carried out using fed-batch (variable volume) and semi-continuous modes of fermentation. Semi-continuous fermentation with three feeding cycles of sucrose effectively increased the production of LA from 512 to 725 mg/L.     

Influence of dissolved oxygen concentration on intracellular pH for regulation of Aspergillus niger growth rate during citric acid fermentation in a stirred tank bioreactor

In this paper we report the regulation of Aspergillus niger growth rate during citric acid fermentation in a stirred tank bioreactor. For this, the influence of dissolved oxygen concentration in a medium on intracellular pH values and consequently on overall microbial metabolism was emphasized. Intracellular pH of mycelium grown under different concentrations of dissolved oxygen in the medium was determined. Sensitivity of proteins toward proton concentration is well recognized, therefore pH influences on the activities of key regulatory enzymes of Aspergillus niger were determined at pH values similar to those detected in the cells grown under lower dissolved oxygen concentrations. The results have shown significantly reduced specific activities of hexokinase, 6-phosphofructokinase and glucose-6-phosphate dehydrogenase in more acidic environment, while pyruvate kinase was found to be relatively insensitive towards higher proton concentration. As expected, due to the reduced specific activities of regulatory enzymes under more acidic conditions, overall metabolism should be hindered in the medium with lower dissolved oxygen concentration which was confirmed by detecting the reduced specific growth rates. From the studies, we conclude that dissolved oxygen concentration affects the intracellular pH and thus growth rate of Aspergillus niger during the fermentation process.     

Enhanced acetoin production by Serratia marcescens H32 using statistical optimization and a two-stage agitation speed control strategy

Enhanced acetoin production was carried out by Serratia marcescens H32. First, medium compositions were optimized statistically for shake flask fermentations to produce acetoin. Sucrose and corn steep liquor powder (CSLP) were identified as the most significant factors by Plackett-Burman design. The path of steepest ascent and response surface methodology were then employed to determine the optimal concentrations of the two factors. Acetoin yield was up to 41.5 g/L in flask fermentations using the optimized medium. Furthermore, the optimal medium was used to conduct fermentation experiments in a 3.7-L bioreactor. The influences of different agitation speeds on acetoin production were investigated. Based on a process analysis, a two-stage agitation speed control strategy was proposed, in which the agitation speed was controlled at 700 rpm during the first 8 h and then switched to 600 rpm. A relatively high acetoin concentration (44.9 g/L) and high acetoin productivity (1.73 g/L/h) were achieved by applying this strategy. Fed-batch fermentation based on the two-stage agitation speed control strategy was performed, and a maximum acetoin concentration of 60.5 g/L with productivity of 1.44 g/L/h was achieved.     

Optimization of agitation for production of swainsonine from Metarhizium anisopliae in stirred tank and airlift reactors

The optimal agitation rate for production of swainsonine from Metarhizium anisopliae grown in batch stirred tank reactors (2 to 20 l) was 400 rpm with a mixed hyphal and pelleted morphology where the specific swainsonine production rate was 9×10^–2 mg g^–1 cell dry wt h from 87 to 142 h. Culture of the fungus in a 6-l airlift reactor produced loose pellets and the production of swainsonine started at least 24 h earlier than in the stirred tank reactor. The final yield (5.9 mg swainsonine g^–1 cell dry wt) after 168 h in the airlift reactor was 18% less than those obtained in the stirred tank reactor with an agitation rate of 400 rpm.     

High production of prodigiosin by Serratia marcescens grown on ethanol

Serratia marcescens S389, isolated as an ethanol-utilizing bacterium, produced prodigiosin at up to 3 mg ml^–1 when grown on ethanol and with the omission of inorganic phosphate and NaCl from the medium. This yield was some 200-fold greater than that previously reported.     

Effect of agitation and aeration on the production of nitrile hydratase by Rhodococcus erythropolis MTCC 1526 in a stirred tank reactor

Aims: To evaluate the effect of different physicochemical parameters such as agitation, aeration and pH on the growth and nitrile hydratase production by Rhodococcus erythropolis MTCC 1526 in a stirred tank reactor. Methods and Results: Rhodococcus erythropolis MTCC 1526 was grown in 7‐l reactor at different agitation, aeration and controlled pH. The optimum conditions for batch cultivation in the reactor were an agitation rate of 200 rev min^?1, aeration 0·5 v/v/m at controlled pH 8. In this condition, the increase in nitrile hydratase activity was almost threefold compared to that in the shake flask. Conclusion: Agitation and aeration rate affected the dissolved‐oxygen concentration in the reactor which in turn affected the growth and enzyme production. Significance and Impact of the Study: Cultivation of R. erythropolis MTCC 1526 in the reactor was found to have significant effect on the growth and nitrile hydratase production when compared to the shake flask.     

Ethanol production by immobilized whole cells ofZymomonas mobilis in a continuous flow expanded bed bioreactor and a continuous flow stirred tank bioreactor

Continuous ethanol fermentation by immobilized whole cells ofZymomonas mobilis was investigated in an expanded bed bioreactor and in a continuous stirred tank reactor at glucose concentrations of 100, 150 and 200 g L^–1. The effect of different dilution rates on ethanol production by immobilized whole cells ofZymomonas mobilis was studied in both reactors. The maximum ethanol productivity attained was 21 g L^–1 h^–1 at a dilution rate of 0.36 h^–1 with 150 g glucose L^–1 in the continuous expanded bed bioreactor. The conversion of glucose to ethanol was independent of the glucose concentration in both reactors.