Optimal conditions for hepatitis B core antigen production in shaked flask fermentation

The effects of various environmental factors such as pH (5, 6, 7, 8 and 9), temperature (30, 37 and 40°C) and rotational speed (150, 200 and 250 rpm) on the growth and the hepatitis B core antigen (HBcAg) production ofEscherichia coli W3110IQ were examined in the present study. The highest growth rate is achieved at PH 7, 37°C and at a rotational speed of 250 rpm which is 0.927 h⁻¹. The effect of pH on cell growth is more substantial compared to other parameters; it recorded a 123% different between the highest growth rate (0.927 h⁻¹) at pH 7 and lowest growth at pH 5. The highest protein yield is achieved at pH 9, rotational speed of 250 rpm and 40°C. The yield of protein at pH 7 is 154% higher compared to the lowest yield achieved at pH 5. There is about 28% different of the protein yield for theE. coli cultivated at 250 rpm compared to that at 150 rpm which has the lowest HBcAg yield. The yield of protein at 40°C is 38% higher compared to the lowest yield achieved, at 30°C.     

Does the agitation rate and/or oxygen saturation influence exopolysaccharide production by Aureobasidium pullulans in batch culture?

  When Aureobasidium pullulans was grown at a number of agitation rates under batch conditions, exopolysaccharide yields were dramatically reduced at high rates i.e. at least 750 rpm. Investigations with gas blending, which allowed pO₂ manipulation and control independently of the agitation rate, showed that this yield reduction was due solely to the high pO₂ levels that occurred at these agitation rates. Thus, polysaccharide production at 1000 rpm could be elevated by maintaining the pO₂ at a low level during the initial phase of the fermentation. However, both the timing of the pO₂ decrease and the level at which it was maintained were crucial for obtaining yields at 1000 rpm, similar to those observed at low agitation rates. Received: 29 February 1996 / Received revision: 11 July 1996 / Accepted: 15 July 1996     

A serum-free medium for colony growth and hyaluronic acid production by Streptococcus zooepidemicus NJUST01

A hyaluronic acid (HA)-producing strain, Streptococcus zooepidemicus NJUST01, can grow in a serum-free agar medium, with starch as exclusive carbon source, but not glucose, sucrose, dextrine, xylose, or lactose. In this starch medium, the strain NJUST01 reproduced successively at 37°C for 60 generations, with no obvious variation on morphology and physiology, but colonies of the strain after 60th generation could not produce a clear hemolytic zone on sheep blood agar plates. Hyaluronic acid production by the strain NJUST01 was analyzed relative to the starch medium. Employing a multifactor cross experiment, an optimum medium revealed for hyaluronic acid production was composed of 5% starch, 0.3% glucose, 0.5% peptone, 0.15% MgSO₄, and 2.0% K₂HPO₄. The amount of HA 6.7 g/l was obtained in batch fermentation on a rotary shaker at 37°C, 220 rpm for 36 h.     

One-pot synthesis of 6-aminohexanoic acid from cyclohexane using mixed-species cultures

6-Aminohexanoic acid (6AHA) is a vital polymer building block for Nylon 6 production and an FDA-approved orphan drug. However, its production from cyclohexane is associated with several challenges, including low conversion and yield, and severe environmental issues. We aimed at overcoming these challenges by developing a bioprocess for 6AHA synthesis. A mixed-species approach turned out to be most promising. Thereby, Pseudomonas taiwanensis VLB120 strains harbouring an upstream cascade converting cyclohexane to either є-caprolactone (є-CL) or 6-hydroxyhexanoic acid (6HA) were combined with Escherichia coli JM101 strains containing the corresponding downstream cascade for the further conversion to 6AHA. ε-CL was found to be a better ‘shuttle molecule’ than 6HA enabling higher 6AHA formation rates and yields. Mixed-species reaction performance with 4 g l^-1 biomass, 10 mM cyclohexane, and an air-to-aqueous phase ratio of 23 combined with a repetitive oxygen feeding strategy led to complete substrate conversion with 86% 6AHA yield and an initial specific 6AHA formation rate of 7.7 ± 0.1 U g_CDW^-1. The same cascade enabled 49% 7-aminoheptanoic acid yield from cycloheptane. This combination of rationally engineered strains allowed direct 6AHA production from cyclohexane in one pot with high conversion and yield under environmentally benign conditions.     

Enhanced welan gum production using a two-stage agitation speed control strategy in Alcaligenes sp. CGMCC2428

Batch fermentative production of welan gum by Alcaligenes sp. CGMCC2428 was investigated under various oxygen supply conditions using regulating agitation speed. Based on a three kinetic parameters analysis that includes specific cell growth rate (μ), specific glucose consumption rate (q _s), and specific welan formation rate (q _p), a two-stage agitation speed control strategy was proposed to achieve high concentration, high yield, and high viscosity of welan. During the first 22 h, the agitation speed in 7.5 L fermenter was controlled at 800 rpm to maintain high μ for cell growth. The agitation was then reduced step-wise to 600 rpm to maintain a changing profile with stable dissolved oxygen levels and obtain high qp for high welan accumulation. Finally, the maximum concentration of welan was reached at 26.3 ± 0.89 g L⁻¹ with a yield of 0.53 ± 0.003 g g⁻¹ and the welan gum viscosity of 3.05 ± 0.10 Pa s, which increased by an average of 15.4, 15.2, and 20.1% over the best results controlled by constant agitation speeds.     

High bioreactor production and emulsifying activity of an unusual exopolymer by Chromohalobacter canadensis 28

Unusual composition of an exopolymer (EP) from an obligate halophilic bacterium Chromohalobacter canadensis 28 has triggered an interest in development of an effective bioreactor process for its production. Its synthesis was investigated in 2‐L bioreactor at agitation speeds at interval 600‐1000 rpm, at a constant air flow rate of 0.5 vvm; aeration rates of 0.5, 1.0, and 1.5 vvm were tested at constant agitation rate of 900 rpm. EP production was affected by both, agitation and aeration. As a result twofold increase of EP yield was observed and additionally increased up to 3.08 mg/mL in a presence of surfactants. For effective scale‐up of bioreactors mass transfer parameters were estimated and lowest values of K_La obtained for the highest productivity fermentation was established. Emulsification activity of EP exceeded that of trade hydrocolloids xanthan, guar gum, and cellulose. A good synergism between EP and commercial cellulose proved its potential exploration as an enhancer of emulsifying properties of trade emulsions. A pronounced lipophilic effect of EP was established toward olive oil and liquid paraffin. Cultivation of human keratinocyte cells (HaCaT) with crude EP and purified γ‐polyglutamic acid (PGA) showed higher viability than control group.     

Production of Candida utilis protein from peat extracts

Sphagnum peat extracts or hydrolysates have been obtained and used as a culture medium for the production of Candida utilis biomass as single cell proteins. Acid hydrolysis of ground peat (4–60 mesh) in an autoclave operated under a set of conditions for acid strength (0.3-1.5 (v/v) H₂SO₄), holding time (1–4 hr), temperature (100–165°C), and weight ratio of dry peat to solution (3.3–16.7 g dry peat/100 g solution) yielded carbohydrate-rich extracts of different concentrations (1–34g/liter). The best yield (mg total carbohydrate/g dry peat) was obtained for a holding time of I hr and a temperature of 152°C. Low peat concentratio (4.1 g dry peat/100 g solution)resulted in high yield(280mg total carbohydrate/gdry peat) with a corresponding low carbohydrate content in hydrolysate (13 g/liter), while a lower yield with a higher carbohydrate content (34 g/liter)in hydrolysate were found when increasing peat concentration (16.7 g dry peat/100 g solution). Shake-fladk experiments using peat hydrolysates as the culture medium together with NH₄OH (～4.8 g/liter) and K₂HPO₄(5 g/liter) as nitrogen and phosphate supplement, respectively, gave a maximum biomass concentration of 7.5 g/liter after 60 hr at 30°C and 200rpm. Batch cultivation in a fermentor under controlled conditions for aeration (4.2 liter/min), agitation (500rpm), temperature (30°C), and pH (5.0) produced a maximum biomass of 10 g/liter after 20 hr with a specific growth rate of 0.13 hr^?1. For the continuous cultivation, a maximal biomass productivity of 1.24 g/gliter-he was obtained at a dilution rate of 0.125 hr ^?1. Monod's equation's equation has been used for the estimation of the coefficients μ_Max, K_s, and Y. It was found that the yield coefficient Y is not constant during the progress of batch cultivation.     

STATISTICAL OPTIMIZATION OF GREEN FLUORESCENT PROTEIN PRODUCTION FROM Escherichia coli BL21(DE3)

An optimized cultivation condition is needed to maximize the functional green fluorescent protein (GFP) production. Six process variables (agitation rate, temperature, initial medium pH, concentration of inducer, time of induction, and inoculum density) were screened using the fractional factorial design. Three variables (agitation rate, temperature, and time of induction) exerted significant effects on functional GFP production in E. coli shake flask cultivation and were optimized subsequently using the Box–Behnken design. An agitation rate of 206 rpm at 31°C and induction of the protein expression when the cell density (OD_600nm) reaches 1.04 could enhance the yield of functional GFP production from 0.025 g/L to 0.241 g/L, which is about ninefold higher than the unoptimized conditions. Unoptimized cultivation conditions resulted in protein aggregation and hence reduced the quantity of functional GFP. The model and regression equation based on the shake flask cultivation could be applied to a 2-L bioreactor for maximum functional GFP production.     

Process optimization for the production of diosgenin with Trichoderma reesei

Based on the response surface methodology, an effective microbial system for diosgenin production from enzymatic pretreated Dioscorea zingiberensis tubers with Trichoderma reesei was studied. The fermentation medium was optimized with central composite design (3⁵) depended on Plackett–Burmann design which identified significant impacts of peptone, K₂HPO₄ and Tween 80 on diosgenin yield. The effects of different fermentation conditions on diosgenin production were also studied. Four parameters, i.e. incubation period, temperature, initial pH and substrate concentration were optimized using 4⁵ central composite design. The highest diosgenin yield of 90.57% was achieved with 2.67% (w/v) of peptone, 0.29% (w/v) of K₂HPO₄, 0.73% (w/v) of Tween 80 and 9.77% (w/v) of substrate, under the condition of pH 5.8, temperature 30 °C. The idealized incubation time was 6.5 days. After optimization, the product yield increased by 33.70% as compared to 67.74 ± 1.54% of diosgenin yield in not optimized condition. Scale-up fermentation was carried out in a 5.0 l bioreactor, maximum diosgenin yield of 90.17 ± 3.12% was obtained at an aeration of 0.80 vvm and an agitation rate of 300 rpm. The proposed microbial system is clean and effective for diosgenin production and thus more environmentally acceptable than the traditional acid hydrolysis.     

Effects of hyaluronan treatment on lipopolysaccharide-challenged fibroblast-like synovial cells

Numerous investigations have reported the efficacy of exogenous hyaluronan (HA) in modulating acute and chronic inflammation. The current study was performed to determine the in vitro effects of lower and higher molecular weight HA on lipopolysaccharide (LPS)-challenged fibroblast-like synovial cells. Normal synovial fibroblasts were cultured in triplicate to one of four groups: group 1, unchallenged; group 2, LPS-challenged (20 ng/ml); group 3, LPS-challenged following preteatment and sustained treatment with lower molecular weight HA; and group 4, LPS-challenged following pretreatment and sustained treatment with higher molecular weight HA. The response to LPS challenge and the influence of HA were compared among the four groups using cellular morphology scoring, cell number, cell viability, prostaglandin E₂ (PGE₂) production, IL-6 production, matrix metalloproteinase 3 (MMP3) production, and gene expression microarray analysis. As expected, our results demonstrated that LPS challenge induced a loss of characteristic fibroblast-like synovial cell culture morphology (P < 0.05), decreased the cell number (P < 0.05), increased PGE₂ production 1,000-fold (P < 0.05), increased IL-6 production 15-fold (P < 0.05), increased MMP3 production threefold (P < 0.05), and generated a profile of gene expression changes typical of LPS (P < 0.005). Importantly, LPS exposure at this concentration did not alter the cell viability. Higher molecular weight HA decreased the morphologic change (P < 0.05) associated with LPS exposure. Both lower and higher molecular weight HA significantly altered a similar set of 21 probe sets (P < 0.005), which represented decreased expression of inflammatory genes (PGE₂, IL-6) and catabolic genes (MMP3) and represented increased expression of anti-inflammatory and anabolic genes. The molecular weight of the HA product did not affect the cell number, the cell viability or the PGE₂, IL-6, or MMP3 production. Taken together, the anti-inflammatory and anticatabolic gene expression profiles of fibroblast-like synovial cells treated with HA and subsequently challenged with LPS support the pharmacologic benefits of treatment with HA regardless of molecular weight. The higher molecular weight HA product provided a cellular protective effect not seen with the lower molecular weight HA product.     

Effect of ammonium sulphate concentration and agitation speed on the kinetics of alginate production by Azotobacter vinelandii DSM576 in batch fermentation

Growth and alginate production by Azotobacter vinelandii DSM576 as a function of initial ammonium sulphate concentration (0.45–1.05 g l⁻¹) and agitation speed (300–700 rpm) were studied in batch fermentations at controlled pH. The time course of growth, alginate production and substrate consumption and the effect of nitrogen concentration and agitation speed on kinetic parameters and on maximum alginate molecular weight (MW) was modelled using empirical equations. The kinetics of growth, alginate production and polymerization were deeply affected by agitation speed and, to a lesser extent, by inorganic nitrogen concentration. Average and maximum specific growth rate and maximum alginate MW all increased with agitation speed, and were higher at intermediate ammonium sulphate concentration. Maximum alginate MW (>250,000) was obtained at high agitation speed (600–700 rpm) and alginate depolymerization was limited or did not occur at all when the agitation speed was higher than 500 rpm, while at 400 rpm depolymerization significantly reduced the alginate. However, alginate yield was negatively affected by increasing agitation speed. A good compromise between alginate yield (>2 g l⁻¹) and quality (MW>250,000) was obtained with agitation speed of 500–600 rpm and 0.75–0.90 g l⁻¹ of ammonium sulphate. Journal of Industrial Microbiology & Biotechnology (2000) 25, 242–248. Received 23 February 2000/ Accepted in revised form 04 August 2000     

Optimizing the Conditions of Dextran Synthesis by the Bacterium <Emphasis Type="Italic">Leuconostoc mesenteroides</Emphasis> Grown in a Molasses-Containing Medium

Maximal dextran production (54–55 g/l) by the bacterium Leuconostoc mesenteroides strain V-2317D was observed in molasses-containing media in the presence of 17.5% glucose at pH_init 6.75. The beginning of dextran production depended on the amount of inoculate; maximum yield was observed at a shaker rate of 200 rpm. The dextran produced by L. mesenteroides grown in the molasses-containing medium was representative of three fractions differing in molecular weight and composition: the high-(∼54.5%), medium- (∼ 27.9%), and low-molecular-weight (∼2.85%) fractions.__________Translated from Prikladnaya Biokhimiya i Mikrobiologiya, Vol. 41, No. 4, 2005, pp. 409–413.Original Russian Text Copyright © 2005 by Vedyashkina, Revin, Gogotov.     

Improvement of poly(γ-glutamic acid) biosynthesis and quantitative metabolic flux analysis of a two-stage strategy for agitation speed control in the culture of <Emphasis Type="Italic">Bacillus subtilis</Emphasis> NX-2

In this study, the production of poly(γ-glutamic acid) by Bacillus subtilis NX-2 (PGA) at different agitation speeds was investigated. Based on the analysis of specific cell growth rate (μ) and specific PGA formation rate (q _p ), a two-stage strategy for agitation speed control was proposed. During the first 24 h, an agitation speed of 600 rpm was used to maintain a high μ for better cell growth, which then reduced to 400 rpm after 24 h to maintain a high q _p to enhance PGA production. Using this method, the maximum concentration of PGA reached 40.5 ± 0.91 g/L and the PGA productivity was 0.56 ± 0.012 g/L/h, which was 17.7 and 9.8% higher, respectively, than the best results obtained when a constant agitation speed was used. The flux distributions and the related enzymes of 2-oxoglutarate could be affected by this two-stage strategy for agitation speed. The activity of isocitrate dehydrogenase and glutamate dehydrogenase at the key node of 2-oxoglutarate increased, and more flux distribution was directed to glutamate. The flux distribution from extracellular to intracellular glutamate also increased and improved PGA production as the glutamate uptake rates increased using the agitation-shift control method.     

Hyaluronic acid production is enhanced by the additional co-expression of UDP-glucose pyrophosphorylase in Lactococcus lactis

Hyaluronic acid (HA) production was metabolically engineered in Lactococcus lactis by introducing the HA synthetic machinery from the has operon of the pathogenic bacterium Streptococcus zooepidemicus. This study shows that the insertion of uridine diphosphate (UDP)-glucose pyrophosphorylase (hasC) gene in addition to the HA synthase (hasA) and UDP-glucose dehydrogenase (hasB) genes has a significant impact on increasing HA production. The recombinant L. lactis NZ9000 strain transformed with the plasmid pSJR2 (co-expressing hasA and hasB genes only) produced a maximum of 107 mg/l HA in static flask experiments with varying initial glucose concentrations, while the corresponding experiments with the transformant SJR3 (co-expressing hasA, hasB, and hasC genes) gave a maximum yield of 234 mg/l HA. The plasmid cloned with the insertion of the full has operon comprising of five different genes (hasA, hasB, hasC, hasD, and hasE) exhibited structural instability. The HA yield was further enhanced in batch bioreactor experiments with controlled pH and aeration, and a maximum of 1.8 g/l HA was produced by the SJR3 culture.     

Shake-flask and bench-scale stirred tank bioreactor production optimization of a thermoalkaline protease from Bacillus cereus SIU1 using one-factor-at-a-time and response surface (statistical) methodologies

Abstract

We report the optimization of production of a halotolerant, thermoalkaline protease by Bacillus cereus SIU1, at shake-flask and bench-scale bioreactor level, using conventional and response surface methods. The basal medium supplemented with optimized (w/v) 0.8% glucose, 1.5% peptone, and 0.4% yeast extract produced 224 Uml^{? 1} alkaline protease after 20 h incubation. Enzyme yield was further increased to 491 Uml^{? 1} when the fermentation broth was supplemented with 0.02% (w/v) Ca²⁺. Optimization of physical factors resulted in still higher protease level of 651 Uml^{? 1} within 18 h fermentation at initial pH 9.0, 50°C, and 150 rpm agitation. Statistically designed experiments revealed significant effects of peptone and CaCl₂ on protease production. A maximum of 749 protease Uml^{? 1} was produced at optimum factor levels (w/v) of peptone 1.75%, yeast extract 0.4%, CaCl₂ 0.025%, and pH 9.0 after 18 h incubation. Optimization of agitation and aeration rates in bench-scale bioreactors further enhanced the enzyme yield to 941 protease Uml^{? 1} at 125 rpm and 2.0 vvm aeration. Optimization of protease production by conventional and statistical approaches resulted in a ～10.7-fold increase (941 Uml^{? 1}) compared to un-optimized conditions (88 Uml^{? 1}).     

Hyaluronan-mediated protective effect against cell damage caused by enzymatically produced hydroxyl (OH·) radicals is dependent on hyaluronan molecular mass

Hyaluronan (HA) protected tendon fibroblasts against cell damage mediated by hydroxyl radicals (OH·) as demonstrated by release of ⁵¹Cr from labelled cells. Protection afforded by high molecular mass (M_r) HA (1218 kDa) was much more effective than that provided by lower (176 kDa and 668 kDa) M_r HA. OH· was generated by coupling H₂O₂ produced by glucose oxidase: glucose to [Fe²⁺-EDTA] chelate in a Fenton-type system. The flux of OH· was measured by a spectrofluorimetric assay of salicylate produced by the reaction of benzoate with OH·. Cell damage caused by the OH· generating system was prevented in the presence of catalase, which destroyed H₂O₂. Damage caused in a standard incubation time increased with increased amounts of glucose oxidase. Protection against OH·-mediated cell damage increased with increasing concentration of HA. The presence of HA did not interfere with the enzyme-Fenton system, as monitored by production of gluconate. On the other hand, HA scavenged OH· produced by the enzyme-Fenton system, as shown by competition with benzoate, which produced less salicylate in the spectrofluorimetric assay in the presence of HA. The reaction of OH· with HA was measured directly by a pulse radiolysis technique in which a hydrated electron (e) produced OH· by the reaction with nitrous oxide. Second order rate constants obtained in distilled H₂O or in phosphate buffer showed no dependence on HA M_r. Similarly, fluorimetric assay of the flux of in the enzyme-Fenton system confirmed that HA competed with benzoate, thus lowering salicylate production, and the flux was also independent of the molecular mass of HA. These results demonstrate that part of the HA-mediated protection against enzyme-Fenton produced OH· and other reactive oxygen-derived toxic species was not a consequence of either the primary or secondary structure of HA, but rather depends on higher order HA organization. Some aspects of the formation of the HA meshwork (tertiary structure) are M_r dependent. We therefore propose that cell-anchored HA meshworks excluded relatively large enzyme molecules from the immediate environment of the cell, thus reducing the flux of OH· etc. at the cell surface and diminishing cell damage.     

Influence of culture vessel characteristics and agitation rate on gaseous exchange,hydrodynamic stress,and growth of embryogenic cork oak (<Emphasis Type="BoldItalic">Quercus suber</Emphasis> L.) cultures

Somatic embryogenesis can be induced in the leaves of cork oak (Quercus suber L.) trees. The use of this propagation system in multivarietal forestry requires the mass production of cloned plants at low cost. Investigations were made into the influence of three types of Erlenmeyer flask and three orbiting speeds (60, 110, and 160 rpm) on oxygen transfer rate (K_L a), the shear force index (SFI), biomass production, and the proliferation of embryogenic clumps (EMCs) in cultures during the proliferation phase. K_L a varied between 0.11 and 1.47 h⁻¹ without biomass production being limited by oxygen availability. The EMCs grew even in hypoxic conditions, although the suppression of gaseous exchange strongly reduced biomass production. Cultures with different levels of hydrodynamic stress and SFI values (1.4·10⁻³–8.8·10⁻³ cm min⁻¹) were obtained. Proliferation rates of EMCs increased with agitation rate and the SFI. The largest number of EMCs was obtained in baffled flasks agitated at 160 rpm (K_L a of 1.47 h⁻¹, and SFI of 8.8·10⁻³ cm min⁻¹) with mild hydrodynamic stress enhancing growth. Biomass production increased with agitation and hydrodynamic stress, but only when the SFI value was below 5·10⁻³ cm min⁻¹. The greatest biomass production was obtained in smooth 100 ml flasks agitated at 160 rpm. The differentiation of embryos was favoured by the lowest K_L a (0.11 h⁻¹) and SFI (1.40·10³ cm min⁻¹) values, achieved using these flasks when agitated at 60 rpm.     

Fluid mixing and oxygen transfer in cell suspensions ofTaxus chinensis in a novel stirred bioreactor

In high-density plant cell cultures, mixing and mass transfer are two key issues, which should be emphasized for process optimization. In this work, both mixing and oxygen transfer characteristics of cell suspensions ofTaxus chinensis were studied in a new centrifugal impeller bioreactor with a working volume of 1.2 L. The mixing time (t _M) and the volumetric oxygen transfer coefficient (K _L a) under different operational conditions were determined in both tap water and cell suspensions of 100–400 g fresh weight/L (i.e., 5.65–23.1 g DW/L). At an aeration rate of 0.1 L/min,t _M decreased from 10.6s at 30 rpm to 2.89 s at 200 rpm under 100 g FW/L, and from 9.63 s (120 rpm) to 4.05 s (300 rpm) under 400 g FW/L. Compared with the effect of agitation, aeration was less significant to the suspension mixing. At a relatively high agitation speed (e.g., 200 rpm),t _M remained almost the same even though aeration rate was changed from 0.1 to 0.4 L/min. Thet _M value increased slowly from 3.98 to 5.26 s at 120 rpm when the cell density was raised from 100 to 250 g FW/L. A rapid increase of botht _M and the suspension viscosity was observed at a cell density above 300 g FW/L. As expected, theK _L a value increased with an increase of aeration rate and agitation speed, but decreased with an increase of cell density. The quantitative data obtained here are useful to investigate the effect of mixing stress on the cell physiology and metabolism ofTaxus chinensis in the bioreactor. This paper is dedicated by JJZ to his colleague Prof. Jun-Tang Yu on the occasion of his 70 birthday.     

Improvement in Production and Quality of Gellan Gum by Sphingomonas paucimobilis Under High Dissolved Oxygen Tension Levels

The effect of agitation rate and dissolved oxygen tension (DOT) on growth and gellan production by Sphingomonas paucimobilis was studied. Higher cell growth of 5.4 g l⁻¹ was␣obtained at 700 rpm but maximum gellan (15 g l⁻¹) was produced at 500 rpm. DOT levels above 20% had no effect on cell growth but gellan yield was increased to 23 g l⁻¹ with increase in DOT level to 100%. Higher DOT levels improved the viscosity and molecular weight of the polymer with change in acetate and glycerate content of the polymer.     

Effect of aeration and agitation on the protease production by S<Emphasis Type="Italic">taphylococcus aureus</Emphasis> mutant RC128 in a stirred tank bioreactor

The modified rotating simplex method has been successfully used to determine the best combination of agitation rate and aeration rate for maximum production of extracellular proteases by Staphylococcus aureus mutant RC128, in a stirred tank bioreactor operated in a discontinuous way. This mutant has shown altered exoprotein production, specially enhanced protease production. Maximum production of proteases (15.28 UP/ml), measured using azocasein as a substrate, was obtained at exponential growth phase when the bioreactor was operated at 300 rpm and at 2 vvm with a volumetric oxygen transfer coefficient (K _L a) of 175.75 h⁻¹. These conditions were found to be more suitable for protease production.