溶氧对L-苏氨酸发酵的影响

探索溶氧对L-苏氨酸发酵过程的影响及其控制方法。通过摇瓶装液量试验、不同溶氧控制方式考察发酵过程中溶氧对L-苏氨酸合成的影响。采用补料分批发酵工艺发酵L-苏氨酸,利用氨基酸分析仪测定发酵液中L-苏氨酸的产量,通过10L罐补料分批发酵36h,产酸可达118.9g/L,糖酸转化率为47.6%。可以得出溶氧对L-苏氨酸生物合成有重要影响,并建立了最佳溶氧控制条件。     

H(2)-CO(2) Recirculation and pH Control for Growth of Methanogens in Mass Culture

We modified a fermentor (10-liter liquid volume) for the growth of anaerobic, H(2)-CO(2)-catabolizing bacteria. Gas in the fermentor (ca. 10% CO(2), 50% H(2), 40% CH(4)) was recirculated by a diaphragm pump. During growth, the gas composition was maintained by the addition of a mixture of 80% H(2) and 20% CO(2), and this addition was controlled by a pH auxostat. During gas addition, gas was discharged from the recirculating gas stream and was collected by the displacement of an acidified salt solution.     

H2-CO2 Recirculation and pH Control for Growth of Methanogens in Mass Culture

We modified a fermentor (10-liter liquid volume) for the growth of anaerobic, H₂-CO₂-catabolizing bacteria. Gas in the fermentor (ca. 10% CO₂, 50% H₂, 40% CH₄) was recirculated by a diaphragm pump. During growth, the gas composition was maintained by the addition of a mixture of 80% H₂ and 20% CO₂, and this addition was controlled by a pH auxostat. During gas addition, gas was discharged from the recirculating gas stream and was collected by the displacement of an acidified salt solution.     

Synthesis of staphylococcal enterotoxin A and nuclease under controlled fermentor conditions.

The production of enterotoxin A and nuclease by Staphylococcus aureus strain 100 was studied in a 1.0-liter fermentor. The effects of the gas flow rate, pH, and dissolved oxygen were evaluated. Toxin and nuclease secretion occurred under all conditions which permitted growth of the organism. Final yields of toxin and nuclease in cultures grown at constant air flow rates, ranging from 50 to 500 cm3 per min, were higher at successively higher flow rates. An optimum flow rate for either toxin or nuclease production was not observed. When the aeration rate alone or aeration rate and pH were held constant, the dissolved oxygen levels in the culture decreased from the initial 100% level to 0 to 5% 3 to 4 h after inoculation. The O2 demand of the culture then maintained this level for an additional 4 to 5 h. This low dissolved oxygen interval was characterized by rapid growth and extracellular protein production. Controlling the dissolved oxygen at a constant level throughout growth did not increase the final levels of toxin and nuclease above those achieved at the respective constant pH values. Growth under the influence of a constant aeration rate of 500 cm3 per min and a constant pH of 6.5 and 7.0 yielded the highest titers of nuclease (1,550 units/ml) and toxin (10.5 mug/ml) obtained in any of the fermentations conducted in this study. Sparging fermentor cultures with pure oxygen at a rate of 100 cm3 per min yielded growth and extracellular protein levels similar to those achieved at the sparge rate of 500 cm3 of air per min. Controlling the dissolved oxygen at 100% of pure oxygen saturation appeared to inhibit the culture, as the final cultural turbidity as well as the levels of toxin and nuclease were reduced. These data indicate that enterotoxin and nuclease secretions are closely associated with the growth of strain 100. Analyses of the production rates of these components indicated that early log phase was the most efficient production interval in the growth cycle and that this efficiency was increased by pH control at 6.7 to 6.8 and dissolved oxygen control at 10% of air saturation.     

Synthesis of staphylococcal enterotoxin A and nuclease under controlled fermentor conditions.

The production of enterotoxin A and nuclease by Staphylococcus aureus strain 100 was studied in a 1.0-liter fermentor. The effects of the gas flow rate, pH, and dissolved oxygen were evaluated. Toxin and nuclease secretion occurred under all conditions which permitted growth of the organism. Final yields of toxin and nuclease in cultures grown at constant air flow rates, ranging from 50 to 500 cm3 per min, were higher at successively higher flow rates. An optimum flow rate for either toxin or nuclease production was not observed. When the aeration rate alone or aeration rate and pH were held constant, the dissolved oxygen levels in the culture decreased from the initial 100% level to 0 to 5% 3 to 4 h after inoculation. The O2 demand of the culture then maintained this level for an additional 4 to 5 h. This low dissolved oxygen interval was characterized by rapid growth and extracellular protein production. Controlling the dissolved oxygen at a constant level throughout growth did not increase the final levels of toxin and nuclease above those achieved at the respective constant pH values. Growth under the influence of a constant aeration rate of 500 cm3 per min and a constant pH of 6.5 and 7.0 yielded the highest titers of nuclease (1,550 units/ml) and toxin (10.5 mug/ml) obtained in any of the fermentations conducted in this study. Sparging fermentor cultures with pure oxygen at a rate of 100 cm3 per min yielded growth and extracellular protein levels similar to those achieved at the sparge rate of 500 cm3 of air per min. Controlling the dissolved oxygen at 100% of pure oxygen saturation appeared to inhibit the culture, as the final cultural turbidity as well as the levels of toxin and nuclease were reduced. These data indicate that enterotoxin and nuclease secretions are closely associated with the growth of strain 100. Analyses of the production rates of these components indicated that early log phase was the most efficient production interval in the growth cycle and that this efficiency was increased by pH control at 6.7 to 6.8 and dissolved oxygen control at 10% of air saturation.     

Automatic control for fed-batch culture of single cell protein

Candida utilis was cultivated in a 5-liter jar fermentor using ethanol as sole carbon source. Control of ethanol in the cultivation broth was performed by using an ethanol vapor monitoring instrument and an oxygen electrode coupled with two control circuits. By setting upper and lower bounds according to the predetermined conditions, a signal from a gas monitoring sensor switched the lower or higher bound relay governing the actuating or switch-off of the motor; this maintained a proper concentration of ethanol in the cultivation of ethanol in the system. The growth of cells was found to be satisfactory. Cell concentration reached 64 g/liter during a 20-hr cultivation. As the results of comparative experiments, the control mode using the gas monitoring instrument was found to be superior to that using dissolved oxygen as a controlling signal, especially at high cell concentration.     

Effect of Oxygen-Supply Rates on Growth of Escherichia coli: II. Comparison of Results in Shake Flasks and 50-Liter Fermentor

Growth of Escherichia coli and chemical changes in the medium were very similar in highly baffled flasks and in a 50-liter fermentor run under the same oxygen-supply conditions, based on sulfite-oxidation rates. Flasks with stainless-steel baffles (Biotech) gave growth patterns and rates of glucose and NH₄-N utilization almost identical to those of the fermentor; results with Bellco 598 flasks (with 6 to 7 mm deep indentations) were quite similar. Unbaffled and Bellco 600 flasks (3 to 4 mm indentations) were similar to the fermentor at very high and very low oxygen-transfer rates, but gave much less growth than the fermentor at intermediate levels. Maximal oxygen-uptake rates occurred in the fermentor at the end of the logarithmic-growth phase when growth was 40 to 75% of maximum. In the fermentor, both sulfite-oxidation rates and rates of oxygen uptake correlated reasonably well with the total amount of growth produced.     

Influence of Dissolved Oxygen Levels on Production of l-Asparaginase and Prodigiosin by Serratia marcescens

The effect of dissolved oxygen concentrations on the behavior of Serratia marcescens and on yields of asparaginase and prodigiosin produced in shaken cultures and in a 55-liter stainless-steel fermentor was studied. A range of oxygen transfer rates was obtained in 500-ml Erlenmeyer flasks by using internal, stainless-steel baffles and by varying the volume of medium per flask, and in the fermentor by high speed agitation (375 rev/min) or low rates of aeration (1.5 volumes of air per volume of broth per min), or both. Dissolved oxygen levels in the fermentation medium were measured with a membrane-type electrode. Peak yields of asparaginase were obtained in unbaffled flasks (3.0 to 3.8 IU/ml) and in the fermentor (2.7 IU/ml) when the level of dissolved oxygen in the culture medium reached zero. A low rate of oxygen transfer was accomplished by limited aeration. Production of prodigiosin required a supply of dissolved oxygen that was obtainable in baffled flasks with a high rate of oxygen transfer and in the fermentor with a combination of high-speed agitation and low-rate aeration. The fermentation proceeded at a more rapid rate and changes in pH and cell populations were accelerated by maintaining high levels of dissolved oxygen in the growth medium.     

High-productivity fermentation process for cultivating industrial microorganisms

Summary High-productivity continuous fermentation processes have been developed for the production of important industrial microorganisms in specially designed fermentors.Saccharomyces cerevisiae, Pichia pastoris, Kluyveromyces fragilis, andCandida utilis yeasts have been grown in bench-scale fermentors at cell densities of over 120 g/l, whileEscherichia coli, Bacillus megaterium, Methylomonas sp. andPseudomonas putida bacteria have been cultivated to cell densities of more than 110 g/l. Productivities (g cells per 1 per h) greater than 25 have been achieved in both bench-scale and 1500-liter fermentors with yeasts, and values as high as 55 have been achieved with bacteria in the bench-scale fermentor. The microorganisms were grown on defined media using ammonia for pH control and as nitrogen source. The fermentor, capable of high oxygen and heat transfer rates, was operated at constant volume with continuous feed and product discharge. The high-productivity process reduces fermentor size, media sterilization requirements, and may under some circumstances eliminate waste and recycle streams. It can also be applied to a variety of biological products.     

Development of a new commercial-scale airlift fermentor for rapid growth of yeast

To grow yeast rapidly, it is necessary to supply sufficient oxygen to the yeast and to effectively remove the heat of the fermentation. We succeeded in developing a commercial-scale fermentor for growing a food yeast (Candida utilis) to produce RNA rapidly. This fermentor is an internal-loop airlift type with vertical heat transfer tubes between inner and the outer columns. The volume of the fermentor is 145 m³ (working volume 75 m³). The oxygen transfer rate (OTR) was 9.9 kg-O₂/m³/h using a superficial gas velocity of 30 cm/s based on the outer column. Much of the heat of fermentation and the energy resulting from aeration could be removed effectively by the heat transfer tubes. This unique airlift fermentor was driven at a dilution rate of 0.43 h⁻¹ for about 70 d, with the yeast concentration being maintained at 22.8 kg-dry cell/m³. The yeast production rate was 9.79 kg-dry cell/m³/h. Compared with a traditional stirred-type fermentor, two Vogelbush-type fermentors and another airlift fermentor, our fermentor was far superior with respect to OTR and yeast productivity.     

Production of Tumor-Inhibitory L-Asparaginase by Submerged Growth of Serratia marcescens

Production of a tumor-inhibitory asparaginase by submerged fermentation with Serratia marcescens ATCC 60 was studied to ascertain optimal nutritional conditions for large-scale production leading to enzyme purification studies. Five strains of S. marcescens were screened in shake-flask studies and were found to produce 0.8 to 3.7 IU/ml 48 hr after inoculation. The requirements for asparaginase production with S. marcescens ATCC 60, the high producing strain, included the following: 4% autolyzed yeast extract medium (initial pH 5.0), an incubation temperature of 26 C, and limited aeration for a zero level of dissolved oxygen during the fermentation. Addition of various carbohydrates to the fermentation medium did not enhance yields. The peak cell population in the fermentation medium and the maximal asparaginase yields occurred simultaneously. Highest enzyme yields were found when the pH of the fermentation cycle rose to approximately 8.5. Yields of 4 IU of asparaginase/ml of cell suspension have been obtained consistently in 40 to 42 hr from 10-liter volumes (500 ml/4-liter bottle) produced on a reciprocating shaker. Scale-up to a 60-liter fermentor yielded 3.1 IU/ml in 35 hr.     

Citric acid production by Candida lipolytica Y 1095 in cell recycle and fed-batch fermentors

The effect of dissolved oxygen on citric acid production and oxygen uptake by Candida lipolytica Y 1095 was evaluated in cell recycle and fed-batch fermentation systems. The maximum observed volumetric productivity, which occurred at a dilution rate of 0.06 h(-1), a dissolved oxygen concentration of 80%, and a biomass concentration of 5% w/v, in the cell recycle system, was 1.32 g citric acid/L . h. At these same conditions, the citric acid yield was 0.65 g/g and the specific citric acid productivity was 24.9 mg citric acid/g cell . h. In the cell recycle system, citric acid yields ranged from 0.45 to 0.72 g/g. Both the volumetric and specific citric acid productivities were dependent on the dilution rate and the concentration of dissolved oxygen in the fermentor. Similar productivities (1.29 g citric acid/L . h) were obtained in the fed-batch system operated at a cycle time of 36 h, a dissolved oxygen concentration of 80%, and 60 g total biomass. Citric acid yields in the fed-batch fermentor were consistently lower than those obtained in the cell recycle system and ranged from 0.40 to 0.59 g/g. Although citric acid yields in the fed-batch fermentor were lower than those obtained in the cell recycle system, higher citric:isocitric acid ratios were obtained in the fed-batch fermentor. As in the cell recycle system, both the volumetric and specific citric acid productivities in the fed-batch fermentor were dependent on the cycle time and dissolved oxygen concentration. (c) 1995 John Wiley & Sons, Inc.     

Dialysis Continuous Process for Ammonium-Lactate Fermentation of Whey: Experimental Tests

Laboratory experiments were conducted to validate theoretical predictions describing a dialysis continuous process for the fermentation of whey lactose to ammonium lactate, in which the fermentor contents are poised at a constant pH by adding ammonia solution and dialyzed through a membrane against water. Dried sweet-cheese whey was rehydrated to contain 230 mg of lactose per ml, supplemented with 8 mg of yeast extract per ml, charged into a 5-liter fermentor without sterilization, adjusted in pH (5.3) and temperature (44°C), and inoculated with Lactobacillus bulgaricus. The fermentor and dialysate circuits were connected, and steady-state conditions were established. A series of such conditions was managed nonaseptically for 94 days to study the process and to demonstrate efficiency and productivity. As time progressed, the fermentation remained homofermentative and increased in conversion efficiency, although membrane fouling necessitated dialyzer cleaning about every 4 weeks. With a retention time of 19 h, 97% of the substrate was converted into products. Relative to nondialysis continuous or batch processes for the fermentation, the dialysis continuous process enabled the use of more concentrated substrate, was more efficient in the rate of substrate conversion, and additionally produced a second effluent of less concentrated but purer ammonium lactate.     

Staphylococcal Enterotoxin B and Nuclease Production Under Controlled Dissolved Oxygen Conditions

Enterotoxin B, nuclease, and total exoprotein production by Staphylococcus aureus strain S-6 was studied in a 0.5-liter fermentor system. While these extracellular products were elaborated over a wide range of aeration rates, maximal production occurred within the very narrow range of 125 to 150 cm(3) of air per min. The levels attained at the optimal aeration rate were not increased by maintaining a constant pH, although yield of enterotoxin:cell mass was highest at a constant pH of 7.0. During the growth cycle of the cultures, when aeration rate alone or aeration rate and pH were held constant, the dissolved oxygen (DO) levels, initially set at 100% of saturation, decreased to 5 to 10% 4 to 5 h after inoculation. The oxygen demand of the culture then maintained this level for an additional 4 to 6 h. This interval of low DO was characterized by maximal growth and exoprotein production. When the DO was controlled at a constant value throughout growth (by increasing or decreasing the airflow rate as appropriate), the culture demonstrated different optima for maximal growth and exoprotein production. A constant DO of 100% stimulated growth to extremely high densities, but the accumulation of toxin and nuclease was not observed. On the other hand, maintaining constant DO levels at 50 or 10% raised exoprotein levels higher than those achieved in a culture grown at the optimal aeration rate. Compared to the optimal aeration rate culture, the 10% DO culture yielded 20% more nuclease, 25% more toxin, and 40 to 50% more total exoprotein. These results indicate that it is the DO and not the aeration rate, per se, that is influential in controlling growth, toxin, nuclease, and total exoprotein production.     

A mechanistic study of oxygen transfer in aqueous systems

Oxygen transfer coefficients were evaluated for a 14-liter stirred tank fermentor equipped with an oxygen probe, employing elemental copper adsorbed on a weakly basic anion-exchange resin as a solid phase oxygen acceptor. The use of a solid phase oxygen acceptor allowed evaluation of mass transfer resistances associated with the solid phase, and the effect of an oxygen adsorbing solid phase on the overall oxygen transport system, portions of the oxygen transfer process that are neglected by the conventional sulfite oxidation method commonly employed. It was concluded from the data obtained that a transport pathway involving transfer of oxygen to particles present near the air-water interface was a significant oxygen transport pathway for the system studied. Oxygen probe measurements performed on the bulk liquid did not recognize this pathway, suggesting that data taken on biological systems by use of techniques involving oxygen concentration measurements in the bulk liquid may not give the true oxygen absorbing capacity of a system.     

Storage of apheresis platelets in ethylene-vinyl acetate copolymer bags: relationship between the bag size and the number of platelets maintaining aerobic metabolism

The present study was designed to determine whether a bag made from ethylene-vinyl acetate copolymer (EV) with superior flexibility at subzero temperature is suitable for a storage container of single-donor apheresis platelets. Apheresis platelets were stored with 100 ml plasma in 1-liter bags made of EV or standard polyvinyl chloride (PVC) plastic at 22 degrees C with constant agitation. The oxygen permeability of the 1-liter EV bag averaged 1447 nmol/min/atm, which was about 1.5 times higher than that of PVC bags. The partial oxygen tension (PO2) of platelet concentrates (PC) has linearly decreased to 16 mm Hg with increasing platelet counts. The level of the partial carbon dioxide was always higher in EV bags than in PVC bags. Oxygen consumption rates of platelets stored in EV and PVC bags with a sufficient oxygen supply averaged 1.25 and 1.20 nmol/min/10(9) platelets, respectively. The rates of glucose consumption and lactate production were not changed in two bags. Ninety percent of the total ATP production of about 8 nmol/min/10(9) platelets were generated through the aerobic metabolism. The platelet counts in the 1-liter EV and PVC bags, at which PO2 is 16 mm Hg, were 2.2 and 1.5 x 10(11) platelets, respectively. The study indicates that apheresis platelets stored in EV bags at 22 degrees C have no different metabolic changes when compared with those of PVC bags. In addition, the number of platelets maintaining the aerobic metabolism is 1.5 times higher than that of PVC bags.     

Dialysis Continuous Process for Ammonium-Lactate Fermentation: Improved Mathematical Model and Use of Deproteinized Whey

Separate terms for substrate limitation and product inhibition were incorporated into an equation describing the rate of cell growth for the steady-state fermentation of lactose to lactic acid with neutralization to a constant pH by ammonia. The equation was incorporated into a generalized mathematical model of a dialysis continuous process for the fermentation, developed previously, in which the substrate is fed into the fermentor and the fermentor contents are dialyzed through a membrane against water. The improved model was used to simulate the fermentation on a digital computer, and the results agreed with previous experimental tests using whole whey as the substrate. Further simulations were then made to guide experimental tests using deproteinized whey as the substrate. Dried cheese-whey ultrafiltrate was rehydrated with tap water to contain 242 mg of lactose per ml, supplemented with 8 mg of yeast extract per ml, charged into a 5-liter fermentor without sterilization, adjusted in pH (5.5) and temperature (44°C), and inoculated with an adapted culture of Lactobacillus bulgaricus. The fermentor and dialysate circuits were connected, and a series of steady-state conditions was managed nonaseptically for 71 days. The fermentation of deproteinized whey relative to whole whey, with both highly concentrated, resulted in similar extents of product accumulation but at a lesser rate.     

Inhibitory effect of carbon dioxide on the fed-batch culture of Ralstonia eutropha: evaluation by CO2 pulse injection and autogenous CO2 methods

In order to see the effect of CO(2) inhibition resulting from the use of pure oxygen, we carried out a comparative fed-batch culture study of polyhydroxybutyric acid (PHB) production by Ralstonia eutropha using air and pure oxygen in 5-L, 30-L, and 300-L fermentors. The final PHB concentrations obtained with pure O(2) were 138.7 g/L in the 5-L fermentor and 131.3 g/L in the 30-L fermentor, which increased 2.9 and 6.2 times, respectively, as compared to those obtained with air. In the 300-L fermentor, the fed-batch culture with air yielded only 8.4 g/L PHB. However, the maximal CO(2) concentrations in the 5-L fermentor increased significantly from 4.1% (air) to 15.0% (pure O(2)), while it was only 1.6% in the 30-L fermentor with air, but reached 14.2% in the case of pure O(2). We used two different experimental methods for evaluating CO(2) inhibition: CO(2) pulse injection and autogenous CO(2) methods. A 10 or 22% (v/v) CO(2) pulse with a duration of 3 or 6 h was introduced in a pure-oxygen culture of R. eutropha to investigate how CO(2) affects the synthesis of biomass and PHB. CO(2) inhibited the cell growth and PHB synthesis significantly. The inhibitory effect became stronger with the increase of the CO(2) concentration and pulse duration. The new proposed autogenous CO(2) method makes it possible to place microbial cells under different CO(2) level environments by varying the gas flow rate. Introduction of O(2) gas at a low flow rate of 0.42 vvm resulted in an increase of CO(2) concentration to 30.2% in the exit gas. The final PHB of 97.2 g/L was obtained, which corresponded to 70% of the PHB production at 1.0 vvm O(2) flow rate. This new method measures the inhibitory effect of CO(2) produced autogenously by cells through the entire fermentation process and can avoid the overestimation of CO(2) inhibition without introducing artificial CO(2) into the fermentor.     

Production of plasmid DNA in a simple, inexpensive and reusable fermentor

Performance data for the production of plasmid DNA in bacterial cultures have been obtained using a new concept of simplified fermentor, the Lofstrand Bactolift. The unique design of this fermentor incorporates a standard 500-ml or 1-liter centrifuge bottle as the bacterial growth vessel, thus eliminating the necessity to transfer the cultures for subsequent processing. Bacterial and plasmid yields have been shown to be equal to or greater than those obtained using conventional shake flasks. Twelve 1-liter Bactolift fermentors can be operated in a standard laboratory water bath that occupies less than two square feet of bench space, as compared to a limit of six 2.8-liter Fernbach flasks containing one liter of culture held in an incubator shaker cabinet that occupies nine square feet of laboratory floor space.     

Production of poly(3-hydroxybutyrate) by fed-batch culture of filamentation-suppressed recombinant Escherichia coli.

Recombinant Escherichia coli XL1-Blue harboring a high-copy-number plasmid containing the Alcaligenes eutrophus polyhydroxyalkanoate synthesis genes could efficiently synthesize poly(3-hydroxybutyrate) (PHB) in a complex medium containing yeast extract and tryptone but not in a defined medium. One of the reasons for the reduced PHB production in a defined medium was thought to be severe filamentation of cells in this medium. By overexpressing an essential cell division protein, FtsZ, in recombinant E. coli producing PHB, filamentation could be suppressed and PHB could be efficiently produced in a defined medium. A high PHB concentration of 149 g/liter, with high productivity of 3.4 g of PHB/liter/h, could be obtained by the pH-stat fed-batch culture of the filamentation-suppressed recombinant E. coli in a defined medium. It was also found that insufficient oxygen supply at a dissolved oxygen concentration (DOC) of 1 to 3% of air saturation during active PHB synthesis phase did not negatively affect PHB production. By growing cells to the concentration of 110 g/liter and then controlling the DOC in the range of 1 to 3% of air saturation, a PHB concentration of 157 g/liter and PHB productivity of 3.2 g of PHB/liter/h were obtained. For the scale-up studies, fed-batch culture was carried out in a 50-liter stirred tank fermentor, in which the DOC decreased to zero when cell concentration reached 50 g/liter. However, a relatively high PHB concentration of 101 g/liter and PHB productivity of 2.8 g of PHB/liter/h could still be obtained, which demonstrated the possibility of industrial production of PHB in a defined medium by employing the filamentation-suppressed recombinant E. coli.