Lipase production of Aspergillus oryzae

Aspergillus oryzae produced a small amount of lipase (0.05–0.8 U/wet-g of solid medium) in solid cultures, in contrast to the larger amount (0.46 U/ml) in a shake-flask culture in a modified GYP medium containing 2% glucose, 1% yeast extract and 2% Polypepton. Optimum conditions of lipase production in the submerged culture of A. oryzae were determined in terms of pH, composition of medium, and temperature. In a shake-flask culture at 28°C, the maximum amount of lipase increased to 0.78 U/ml upon the addition of 3% soybean oil to the modified GYP medium. In a jar fermentor culture, 30 U/ml lipase activity was obtained after 72 h at 28°C under appropriate conditions. Lipase production was greatly influenced by the culture temperature, and the optimum temperature for lipase production was about 24°C with a narrow temperature range, which was 10 degrees lower than that for the growth. In the submerged cultures, two kinds of lipase at least exhibiting different substrate specificities were also suggested.     

Effects of agitation and aeration on the production of extracellular glucose oxidase from a recombinant Saccharomycescerevisiae

A recombinant strain of Saccharomyces cerevisiae, GAL-GO2, was developed to facilitate the production of extracellular glucose oxidase (GOD). The recombinant strain secreted 85% (8.7?U/ml) of the total GOD (10.3?U/ml) produced in shake flask culture. For further enhancement of GOD production, optimization of the speed of agitation and the rate of aeration in a stirred tank fermentor was carried out. Response surface methodology with appropriate statistical experimental design was employed for this purpose. The maximal level of extracellular GOD was achieved when the speed of agitation and the rate of aeration were 420?rpm and 0.25?vvm, respectively. The enzyme production was increased by 74% compared to the level obtained under unoptimized conditions.     

Production of the antifungal peptide antibiotic,iturin by Bacillus subtilis NB22 in solid state fermentation

Production of iturin, an antifungal peptide effective at suppressing phytopathogens, by Bacillus subtilis NB22 was investigated in solid state fermentation (SSF) using soy bean curd residue (okara). In scale-up from 15 g to 3 kg, aeration, temperature, and moisture content were controlling factors for the efficient production of iturin. It was found that solid state fermentation was 6–8 times more efficient with respect to iturin productivity than submerged fermentation on the basis of unit wet weight. Higher productivity in selective production of specific components of iturin which are stronger inhibitors of plant pathogens was also confirmed in SSF.     

Characteristics of CHO-K1 cell culture producing two types of recombinant soluble thrombomodulin

Recombinant CHO-K1 cells, expressing human soluble thrombomodulin, were cultured in a serum-free medium and characteristics of the culture associated with glucose and lactate were investigated. In 3 L fermentor (3LFM) cultures, the cell density was found to have a proportional relationship with the volumetric glucose consumption rate, and the specific glucose consumption rates were constant at about 0.2 mg/(10⁶ cells·d) despite many differences in the culture conditions. Thus, it was concluded that the glucose consumption rate is little influenced by the condition of the cells or the culture conditions, and that the cell density can be estimated by the glucose consumption rate calculated from glucose measurement. Two types of thrombomodulin (rsTMα and rsTMβ) were produced, in which rsTMβ possesses chondroitin-4-sulfate and has greater anticoagulant activities than rsTMα. Therefore, it is important to investigate the rsTMα and rsTMβ production properties, and to determine the optimal culture conditions for high rsTMβ production. The most important factor to increase the production of rsTMβ relative to rsTMα (the β/α ratio) was effective aeration. Moreover, a lower ratio of lactate production/glucose consumption (the L/G ratio) with sufficient oxygen, high glucose concentration, and a longer medium exchange interval contributed to a higher specific rsTMβ production rate. Since there was a linear relationship between the production rate of each type of rsTM and the overall rsTM production rate per liter, it is expected that the rsTMα and rsTMβ production rates may be able to be estimated from the overall rate and the rsTMβ production increased by increasing the overall rsTM production with a lower L/G ratio.     

Effect of inoculum size on the aeration pattern of batch cultures of a fungal microorganism

Trichoderma reesei QM 9123 has been grown in batch culture in a 10 liter stirred fermentor, at a temperature of 30°C and pH 4.0. The fermentor was operated at a single stirrer speed of 400 rpm and air rate of 1 v/v/m. The effect of four inoculum sizes (0.5, 1.0, 3.0 and 5.0%) on the growth pattern and the aeration profiles was examined. Logarithmic growth of the fungus was observed. The aeration profile changed with inoculum size and at 5.0%, it was found that the oxygen uptake rate was controlled by the oxygen supply rate, during which the oxygen tension was zero.     

Continuous cultivation of the yeastSaccharomyces cerevisiae at different dilution rates and glucose concentrations in nutrient media

The influence of glucose concentration in nutrient media on the specific growth rate and biomass yield in the course of continuous fermentation ofSaccharomyces cerevisiae was investigated. An increase of glucose content in media decreased the specific growth rate and the biomass yield. Glucose concentration had significant effects on protein and phosphate contents of cells. However, an increased glucose concentration increased the fermentative power ofS. cerevisiae (SJA-method). An increase of the dilution rate decreased the cell concentration in the fermentor. Specific growth rate approached the values of the dilution rate. The best agreement has been obtained at a dilution rate of 0.20/h. This dilution rate proved to be most convenient for the investigated microorganism and cultivation conditions (media composition, pH, aeration intensity and temperature). Biomass yield proved to be decreased by an increase of the dilution rate.     

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.     

Medium Promoting Sporulation of Bacillus larvae and Metabolism of Medium Components

A new medium, designated TMYGP broth, was developed that allowed the honeybee pathogen Bacillus larvae NRRL B-3650 to produce up to 5 × 10⁸ spores per ml of culture (microscopic count). This species normally sporulates poorly, if at all, in artificial broth media. An aeration rate lower than that normally used to cultivate other Bacillus species was required for sporulation. During the exponential growth phase, acids were produced by catabolism of yeast extract components, causing a decrease in pH of the medium. Thereafter, the pH began to increase, probably because of derepression of the citric acid cycle and consumption of the acids. Only after this time did usage of glucose from the medium occur. Thus, glucose usage seems to be regulated by catabolite repression. The presence of glucose was needed for one or more of the later events of sporulation. Of many substances tested, only gluconic acid and glucosamine partially substituted for glucose as a requirement for sporulation. Pyruvate was also required for good sporulation. It was metabolized during the late-exponential phase of growth.     

Rhamnolipids as affinity foaming agent for selective collection of β-glucosidase from cellulase enzyme mixture

Selective and effective separation can potentially be achieved with affinity foam fractionation using simple foaming setup and operation. In this study the use of affinity foam fractionation for selective collection and enrichment of β-glucosidase from a cellulase enzyme mixture was evaluated. Rhamnolipids, a group of glycolipids produced most commonly by Pseudomonas aeruginosa, were used as the affinity foaming agent, because of their foaming property and the presence of dirhamnose moiety (a potential substrate analog for β-glucosidase) in some rhamnolipids. The effects of aeration rate, medium pH, cellulase concentration and rhamnolipid concentration on the foam fractionation performance were examined. Among the pH studied (3.1, 5.0, 7.0 and 9.0), pH 5 was clearly the optimal for selective enrichment of β-glucosidase, presumably corresponding to the high binding affinity between the enzyme and the substrate analog (dirhamnose). With adequate rhamnolipid concentrations (≥0.1 g/L), the aeration rate of 0.1L/min (i.e., 2VVM) for 50 ml test samples was found to give the highest enrichment; higher aeration rates produced wetter foam and, thus, lower (diluted) enzyme activity in the foamate. The enrichment increased with the increasing rhamnolipids-to-cellulase ratio, in the range of 0-2 (w/w) investigated in this study. The finding indicated that rhamnolipids were the limiting compounds in these systems so that the amount of surfactant-enzyme complexes formed and removed into the foam phase would increase when more rhamnolipids were added. At the rhamnolipids-to-cellulase ratio of 2, the β-glucosidase activity in the foamate was about 9 times as high as the activity in the original sample of cellulase mixture and about 17 times the activity in the remaining solution (after foaming). The overall FPU (filter paper unit, a measurement of total cellulase activity) and the activities of endo- and exo-glucanases were only enriched 70-150%. The feasibility of affinity foam fractionation was demonstrated.     

Magnetic forced sedimentation of flocs in activated sludge supplemented with ferromagnetic powder of iron oxide

Aiming to increase the sedimentation rate of flocs prepared by the activated sludge process, the effect of the application of ferromagnetic powder of iron oxide (magnetic powder) and a gradient magnetic field on the sedimentation process was examined. The volumetric loading rate of Polypepton was kept to 200–1,000 mgl⁻¹ d⁻¹ during 7 d in the activated sludge supplemented with 2,000 mg l⁻¹ of magnetic powder. When a gradient magnetic field was applied, the initial zone settling velocity in the case of the Polypepton loading rate of 1,000 mg l⁻¹ d⁻¹ was found to be 36 times faster than that in the case of the control.     

Production of peroxidase with horseradish hairy root cells in a two step culture system

Horseradish hairy root cells transformed by a soil bacterium Agrobacterium rhizogenes had peroxidase (POD) activity comparable to that of the original plant root tubers. To enhance POD production by the hairy root culture, various additives to the medium were tested including casein hydrolysates and plant extracts. Polypepton addition had a significant effect on the growth and POD production; at low concentrations (below 1 g/l) the growth was stimulated, while at high concentrations (3–10 g/l), POD activity in the cells was enhanced in spite of a low growth rate. Therefore, the hairy roots were at first cultured in the medium with 1 g/l Polypepton, and then 5 g/l Polypepton was added to enhance intracellular POD activity. POD activity in this two step culture system was 5.4 times higher than that in conventional culture in Polypepton-free medium.     

The effect of dissolved oxygen and aeration rate on antibiotic production of Streptomyces fradiae

Different dissolved oxygen concentrations and aeration rates were imposed on a stable mutant of Streptomyces fradiae during the antibiotic-producing phase. At high aeration rate (1 vvm), the tylosin yield in the fermentor broth with dissolved oxygen (DO) concentrations controlled close to 100% saturation (6-8 ppm) increased 10% as against uncontrolled. The rates of cellular growth, oil consumption, and tylosin production were severely reduced when DO concentration fell below 25% saturation, but all resumed to their initial rates when DO was raised to saturation level again. The DO concentration in combination with air flow rate affected the pattern of the antibiotics produced. At high DO levels, an additional macrolide antibiotic, macrocin, was synthesized to more than one-third the amount of tylosin at high aeration rate (1 vvm). On the other hand, tylosin production rate remained constant and no significant amount of macrocin was produced at low aeration rate (0.2 vvm).     

The influence of process parameters in production of lipopeptide iturin A using aerated packed bed bioreactors in solid-state fermentation

The strain Bacillus iso 1 co-produces the lipopeptide iturin A and biopolymer poly-γ-glutamic acid (γ-PGA) in solid-state fermentation of substrate consisting of soybean meal, wheat bran with rice husks as an inert support. The effects of pressure drop, oxygen consumption, medium permeability and temperature profile were studied in an aerated packed bed bioreactor to produce iturin A, diameter of which was 50 mm and bed height 300 mm. The highest concentrations of iturin A and γ-PGA were 5.58 and 3.58 g/kg-dry substrate, respectively, at 0.4 L/min after 96 h of fermentation. The low oxygen uptake rates, being 23.34 and 22.56 mg O₂/kg-dry solid substrate for each air flow rate tested generated 5.75 W/kg-dry substrate that increased the fermentation temperature at 3.7 °C. The highest pressure drop was 561 Pa/m at 0.8 L/min in 24 h. This is the highest concentration of iturin A produced to date in an aerated packed bed bioreactor in solid-state fermentation. The results can be useful to design strategies to scale-up process of iturin A in aerated packed bed bioreactors. Low concentration of γ-PGA affected seriously pressure drop, decreasing the viability of the process due to generation of huge pressure gradients with volumetric air flow rates. Also, the low oxygenation favored the iturin A production due to the reduction of free void by γ-PGA production, and finally, the low oxygen consumption generated low metabolic heat. The results show that it must control the pressure gradients to scale-up the process of iturin A production.     

Kojic acid production byAspergillus flavus using gelatinized and hydrolyzed sago starch as carbon sources

Direct conversion of gelatinized sago starch into kojic acid byAspergillus flavus strain having amylolytic enzymes was carried out at two different scales of submerged batch fermentation in a 250-mL shake flask and in a 50-L stirred-tank fermentor. For comparison, fermentations were also carried out using glucose and glucose hydrolyzate from enzymic hydrolysis of sago starch as carbon sources. During kojic acid fermentation of starch, starch was first hydrolyzed to glucose by the action of α-amylase and glucoamylase during active growth phase. The glucose remaining during the production phase (non-growing phase) was then converted to kojic acid. Kojic acid production (23.5g/L) using 100 g/L sago starch in a shake flask was comparable to fermentation of glucose (31.5 g/L) and glucose hydrolyzate (27.9 g/L) but in the 50-L fermentor was greatly reduced due to non-optimal aeration conditions. Kojic acid production using glucose was higher in the 50-L fermentor than in the shake flask.     

Fed-batch production of thermomonospora fusca endoglucanase by recombinant streptomyces lividans

The factors affecting the production of a Thermomonospora fusca endoglucanase by a recombinant Streptomyces lividans strain were studied in a fermentor with glucose addition controlled by a pH-stat. The recombinant plasmid was stable for 35 generations with constant endoglucanase productivity. Glucose and peptone were used as the carbon and nitrogen sources. Addition of Tween-80 increased endoglucanase production twofold. A significant decrease in endoglucanase production was observed at low aeration. During fed-batch cultivation, pulse feeding (6 g/L) of a glucose-ammonium sulfate solution was optimal for endoglucanase production. With higher concentrations of glucose (15 g/L), a significant amount of organic acid, including acetic acid, was produced, which inhibited cell growth and endoglucanase production. Under optimum conditions, 1.7 U/mL of endoglucanase were produced. Copyright 1998 John Wiley & Sons, Inc.     

Optimization of antifungal lipopeptide production from Bacillus sp. BH072 by response surface methodology

Antifungal lipopeptide produced by Bacillus sp. BH072 was extracted from fermentation liquor and determined as iturin A by liquid chromatography-mass spectrometry (LC-MS). For industrial-scale production, the yield of iturin A was improved by optimizing medium components and fermentation conditions. A one-factor test was conducted; fermentation conditions were then optimized by response surface methodology (RSM) to obtain the following: temperature, 29.5°C; pH 6.45; inoculation quantity, 6.7%; loading volume, 100 ml (in 500 ml flasks); and rotary speed, 150 rpm. Under these conditions, the mass concentration of iturin A was increased from 45.30 mg/ml to 47.87 mg/ml. The following components of the medium were determined: carbon sources (glucose, fructose, sucrose, xylose, rhamnose, and soluble starch); nitrogen sources (peptone, soybean meal, NH₄Cl, urea, and ammonium citrate); and metal ions (Zn²⁺, Fe³⁺, Mg²⁺, Mn²⁺, Ca²⁺, and K⁺). The effects of these components on iturin A production were observed in LB medium. We selected sucrose, soybean meal, and Mg²⁺ for RSM to optimize the conditions because of several advantages, including maximum iturin A production, high antifungal activity, and low cost. The optimum concentrations of these components were 0.98% sucrose, 0.94% soybean meal, and 0.93% Mg²⁺. After iturin A production was optimized by RSM, the mass concentration reached 52.21 mg/ml. The antifungal specific activity was enhanced from 350.11 AU/mg to 513.92 AU/mg, which was 46.8% higher than the previous result. The present study provides an important experimental basis for the industrial-scale production of iturin A and the agricultural applications of Bacillus sp. BH072.     

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.     

Effect of simple and complex carbon sources,low temperature culture and complex carbon feeding policies on poly-3-hydroxybutyric acid (PHB) content and molecular weight (Mw) from Azotobacter chroococcum 6B

The molecular weight (M _w) of poly-3-hydroxybutyrate (PHB), produced by shake-flask culture of Azotobacter chroococcum showed little variation with increasing glucose concentration as carbon source (being in the range of 400–500 kDa), while M _w increased from 300–400 to 640 kDa when grown with increasing concentration of sugar cane molasses. Molecular weight increased nearly 30% from 48 to 72 h culture time when 5% molasses as carbon source was used, while with glucose the highest M _w was reached at 48 h. Under fermentor cultivation A. chroococcum produced PHB with a relatively high M _w of 1590 kDa at 53 h culture time when grown in modified Burk's medium with glucose as carbon source at an initial C/N ratio (molar basis) of 69 under fermentor cultivation. A batch glucose-grown ammonium-limited fermentor culture was repeatedly fed with sugar cane molasses (initial C/N ratio 69) and it was observed that PHB content curve decreased at a slower rate than in the fed-batch culture in which glucose and sucrose were not consumed in the culture medium after the feed.     

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.     

Control of carbon dioxide in exhaust air as a method for equal biomass yields at different bed heights in a column fermentor

Summary The rate of aeration of the medium in a solid state fermentation system for biomass production by Schwanniomyces castellii in a large column fermentor was found to influence the gradient of biomass yield at different bed heights. The variations were lower with a higher rate of aeration. These trends were used to formulate a successful strategy to ensure equal biomass yield at all the bed heights by controlling the level of CO₂ at about 2% in exhaust air from the fermentor. Correspondence to: B. K. Lonsane