Studies on quantitative physiology of Trichoderma reesei with two-stage continuous culture for cellulose production

By employing a two-stage continuous-culture system, some of the more important physiological parameters involved in cellulose biosynthesis have been evaluated with an ultimate objective of designing an optimally controlled cellulose process. The two-stage continuous-culture system was run for a period of 1350 hr with Trichoderma reesei strain MCG-77. The temperature and pH were controlled at 32°C and pH 4.5 for the first stage (growth) and 28°C and pH 3.5 for the second stage (enzyme production). Lactose was the only carbon source for the both stages. The ratio of specific uptake rate of carbon to that of nitrogen, Q(C)/Q(N), that supported good cell growth ranged from 11 to 15, and the ratio for maximum specific enzyme productivity ranged from 5 to 13. The maintenance coefficients determined for oxygen, M_O, and for carbon source, M_C, are 0.85 mmol O₂/g biomass/hr and 0.14 mmol hexose/g biomass/hr, respectively. The yield constants determined are: Y_X/O = 32.3 g biomass/mol O₂, Y_X/C = 1.1 g biomass/g C or Y_X/C = 0.44 g biomass/g hexose, Y_X/N = 12.5 g biomass/g nitrogen for the cell growth stage, and Y_X/N = 16.6 g biomass/g nitrogen for the enzyme production stage. Enzyme was produced only in the second stage. Volumetric and specific enzyme productivities obtained were 90 IU/liter/hr and 8 IU/g biomass/hr, respectively. The maximum specific enzyme productivity observed was 14.8 IU/g biomass/hr. The optimal dilution rate in the second stage that corresponded to the maximum enzyme productivity was 0.026 ～ 0.028 hr^?1, and the specific growth rate in the second stage that supported maximum specific enzyme productivity was equal to or slightly less than zero.     

Xylitol formation by Candida boidinii in oxygen limited chemostat culture

Summary Production of xylitol by Candida boidinii NRRL Y-17213 occurs under conditions of an oxygen limitation. The extent to which substrate is converted to xylitol and its coproducts (ethanol, other polyols, acetic acid), and the relative flow rates of substrate to energetic and biosynthetic pathways is controlled by the degree of oxygen limitation.With decrease in oxygen concentration in the inlet gas, for a constant dilution rate of 0.05 1/h. the specific oxygen uptake rate decreased from 1.30 to 0.36 mmol/gh Xylitol was not produced at specific oxygen uptake rates above 0.91 mmol/gh. Upon shift to lower oxygen rates, specific xylitol production rate increased more rapidly than specific ethanol production rate:Nomenclature D dilution rate (1/h) - DOT dissolved oxygen tension (%) - m_o2 maintenance coefficient (mmol O₂/g cell mass h) - q_o2 specific oxygen uptake rate (mmol O₂/g cell mass h) - q_s specific xylose uptake rate (g xylose/g cell mass h) or (mmol xylose/g cell mass h) - q_x specific xylitol production rate (g xylitol/ g cell mass h) or (mmol xylitol/ g cell mass h) - q_e specific ethanol production rate (g ethanol/ g cell mass h) or (mmol ethanol/ g cell mass h) - q_CO2 specific carbon dioxide production rate (mmol CO₂/g cell mass h) - S xylose concentration (g/1) - Y_cm/s cell mass yield coefficient, (g cell mass/mmol xylose) or (g cell mass/ g xylose consumed) - Y_cm/O2 cell mass yield coefficient, (g cell mass/mmol O₂) - Y_X/S xylitol yield coefficient (g xylitol/g xylose consumed) - Y_x/O2 xylitol yield coefficient (g xylitol/mmol O₂) - Y_e/s ethanol yield coefficient (g ethanol/g xylose consumed) - OUR oxygen uptake rate (mmol O₂/1h) - specific growth rate (1/h)     

Biomethanation: Anaerobic fermentation of CO2, H2 and CO to methane

Studies to examine the microbial fermentation of coal gasification products (CO₂, H₂ and CO) to methane have been done with a mixed culture of anaerobic bacteria selected from an anaerobic sewage digestor. The specific rate of methane production at 37°C reached 25 mmol/g cell hr. The stoichiometry for methane production was 4 mmol H₂/mol CO₂. Cell recycle was used to increase the cell concentration from 2.5 to 8.3 g/liter; the volumetric rate of methane production ran from 1.3 to 4 liter/liter hr. The biogasification was also examined at elevated pressure (450 psi) and temperature to facilitate interfacing with a coal gasifier. At 60°C, the specific rate of methane production reached 50 mmol/g cell hr. Carbon monoxide utilization by the mixed culture of anaerobes and by a Rhodopseudomonas species was examined. Both cultures are able to carry out the shift conversion of CO and water to CO₂ and hydrogen.     

An adaptive on-line control feed rate system in a laboratory scale bakers yeast process

Summary A new control policy for the on-line optimization of the nutrient supply in bakers yeast process is proposed. A feed rate corresponding to minimal substrate uptake time was shown to be optimal for cell yield and specific growth rate. Cultivation results of baker's yeast are presented.Nomenclature c glucose concentration in wort (mol.l^–1) - C total glucose used (mol) - c_e ethanol concentration in wort (mg.l^–1) - c_p glucose concentration in fresh medium (mol.l^–1) - dt/dc glucose consumption time (sec.mol^–1) - F substrate feed rate (litre.hr^–1) - q_c glucose uptake rate (mol.hr^–1) - Q_c specific glucose uptake rate (moll.g^–1.hr^–1) - qO₂ oxygen uptake rate (mol.hr^–1) - QO₂ specific oxygen uptake rate (mol.g^–1.hr^–1) - r_x productivity (g.l^–1.hr^–1) - t time (hr) - x biomass concentration (g.l^–1) - X total biomass (g) - Y_x/c cell yield (g.g^–1): (g.mol^–1) - Y_o/c consumed oxygen to glucose ratio (mol.mol^–1)     

The influence of mechanical forces on the morphology and penicillin production of Penicillium chrysogenum

The influence of mechanical forces resulting from the rotation of (multiple) turbine impellers on the morphology and penicillin production of Penicillium chrysogenum Panlabs P-1 was investigated in batch fermentations using semi-defined media. Experiments were carried out at three different scales of fermentation, 5 dm³,100 dm³ and 1000 dm³ working volume, with the impeller tip speed ranging from 2.5 to 6.3 m/s. Throughout all fermentations, the dissolved oxygen concentration never fell below the critical value for maximum penicillin production. Morphological measurements using image analysis showed that the mean main hyphal length and mean hyphal growth unit increased during the rapid growth period and then decreased to a relatively constant value dependent on the agitation intensity. The specific rate of penicillin production (q _pen)and the average main hyphal length during the linear penicillin production phase were lower at high agitation speed, which promoted more rapid mycelial fragmentation and a higher branching frequency. Comparison of the results from the three scales showed that impeller tip speed is a poor scale up parameter whereas a term based on mycelial circulation through the zone of high energy dissipation fitted the data well.List of Symbols C.E.R. mmol/(dm³h) Carbon dioxide evolution rate - D m Impeller diameter - D.O.T. % air saturation Dissolved oxygen tension - L _e m Mean effective length or main hyphal length - O.U.R. mmol/(dm³h) Oxygen uptake rate - P W Total power dissipation - q _pen units/(mg dry cell weight h) rate Specific penicillin production - R.Q. Respiratory quotient - 1/t _cs^–1 Circulation frequency     

The effects of copper,cadmium and zinc on particle filtration and uptake of glycine in the pacific oyster Crassostrea gigas

1. The filtration rate (volume of water completely cleared of collodial carbon per unit time) by control oysters is 36.60 ml/g hr ± 7.68 (sd).2. Filtration rates decrease with increasing concentrations of Cd²⁺ and Zn²⁺.3. In 8–16 mg/l Cu²⁺, filtration rates are significantly higher than the control, but in Cu²⁺ concentrations above 32 mg/l, filtration rates are lower than controls.4. Influx of ¹⁴C-glycine is characterized by Michaelis-Menten kinetics with J_max and K_t values of 1.85 ± 0.097 μmol/g hr and 33.7 ± 4.6 μM respectively.5. The uptake rate of glycine from 1 μM solution is 37.79 μmol/g hr.6. In order of degree of inhibition of glycine uptake, Cu²⁺ > Cd²⁺ > Zn²⁺.7. In 128 mg/l Cu²⁺, glycine uptake rate is reduced to 3.96 nmol/g hr or 10.5% of control.8. The rate of glycine uptake by filter feeding bivalves is dependent on rate of water pumping rate.9. The volume specific glycine transport (amount of glycine transported/unit volume of seawater completely cleared of colloidal carbon) by control oysters in 1 μM glycine concentrations is 1.03 μmol/l.10. The volume specific glycine transport remains constant in increasing Zn²⁺ concentrations, and declines in increasing Cu²⁺ concentrations, suggesting differential effects of the metals on particle filtration and the epithelial amino acid carriers.11. The apparent volume specific glycine transport increases to 2.14 μmol/l in 128 mg/l Cd²⁺. This volume specific transport greater than the glycine concentration in the medium suggests that there may be uptake of cadmium complexed glycine by the oysters.     

Production of Bacterial Cells from Methane

A mixed methane-oxidizing bacterial culture capable of stable and predictable growth in continuous culture was isolated. The culture consisted of two types of gram-negative nonsporulating rods resembling pseudomonads. The culture grew well at 45 C on an inorganic medium without asepsis. Specific metal requirements for Ca²⁺, Cu²⁺, MoO₄²⁻, Zn²⁺, Mn²⁺, Mg²⁺, and Fe³⁺ (or Fe²⁺) were shown. The cells grown in continuous culture contained 11.7 to 12.1% total nitrogen. From an animal nutrition standpoint, the distribution of amino acids was satisfactory. The continuous fermentation was operated over a range of steady-state dilution rates from 0.085 to 0.301 hr⁻¹. The maximum specific growth rate for the culture, μ_max, was 0.303 hr⁻¹ (doubling time 2.29 hr). The average yield for all fermentations analyzed was 0.616 g (dry weight of cells per g of methane used and 0.215 g (dry weight) of cells per g of oxygen used. The yields on both methane and oxygen were higher for the oxygen-limited than for the methane-limited fermentations. The maximum productivity attained in the fermentor was 2.39 g (dry weight) of cells per hr per liter at a dilution rate of 0.187 hr⁻¹ and a cell concentration of 12.8 g (dry weight) of cells per liter. The limit on maximum cell productivity was determined only by the mass transfer rate of oxygen in the fermentor. The simultaneous volumetric mass-transfer coefficients (k_La in hr⁻¹) for oxygen and methane were determined. The results appear to indicate an oxygen to methane mass-transfer coefficient ratio of approximately 1.4.     

Microcalorimetric investigations of the metabolism of yeasts. Growth in chemostat cultures on glucose

Summary As part of a project on the production of penicillin, the penicillin production of two strains of Penicillium chrysogenum which have a different penicillin productivity was investigated in bubble column bioreactors and for comparison in stirred fermenters. The main interest of this study were the complicated interrelations between the stirrer speed, the stirrer type, the shear stress, the morphology of the mycelium and broth viscosity as well as the effect of the oxygen transfer behavior on antibiotic productivity.Stirred tank reactors with different turbine stirrers as well as with a draught tube and propeller were employed.The main variable investigated was the stirrer speed. At low stirrer speeds, gas dispersion is inadequate and the insufficient oxygen transfer rate is a limiting factor. At higher stirrer speeds, the oxygen supply of pulpy mycelia is improved and more cell mass is formed. This result is the same for both strains in all three reactors.If the oxygen partial pressure is near the lower cirtical value, a high percentage of the carbon source is converted into penicillin but the penicillin productivity is low due to a low percentage of penicillin producing cells. At oxygen partial pressures just above 8% saturation, the absolute penicillin productivity is maximal. At higher stirrer speeds and dissolved oxygen concentrations the penicillin production phase is shorter, cell growth is higher and a higher percentage of the carbon source is converted into CO₂.In reactors with a draught tube and propeller, a lower productivity is attained than in those with turbine stirrers.The behavior of the two strains is fairly similar. The higher producing strain, however, has a more distinct separation between its periods of growth and production than does the low producing one. At high stirrer speeds the increase in the cell growth rate is less significant and the substrate yield coefficients are higher for the high producing strain than for the low producing one.Symbols C Dissolved oxygen concentration (mg l^–1) - C^* C at saturation (mg l^–1) - k_La Volumetric mass transfer coefficient (h^–1) - OTR Oxygen transfer rate (mg l^–1 h^–1) - OUR Oxygen uptake rate (mg l^–1 h^–1) - rpm Impeller speed (min^–1) - X (Dry) biomass concentration (g kg^–1) - V_g Volumetric gas flow rate (Nl min^–1) - CMC Carboxymethyl cellulose     

Pantothenate limitation does not induce uncoupled growth of Zymomonas in chemostat culture

Summary Growth coefficients ofZymomonas mobilis were compared in glucose-limited chemostat culture using a complex medium and a defined minimal growth medium at non inhibitory concentrations of ethanol. Under carbon and energy limited conditions in the complex medium containing yeast extract, the max. molar growth yield (Y_G ^max) and maintenance energy coefficient (m_e) were 10.8 g cell/mol glucose and 8.3 mmol glu/g cell/hr, respectively. Glucose-limited growth in the minimal medium with NH₄Cl as nitrogen source promoted slight energetic uncoupling, as reflected in the decrease in the maximum growth yield. The growth yield with respect to calcium pantothenate was calculated to be 1.4×10⁴ g cell/g Ca-pantothenate. However, pantothenate-limited growth did not result in a decrease in growth yield nor an increase in the specific rate of glucose catabolism. Steady-state growth measurements failed to confirm the previously held view of Belaïchet al. (1972) that pantothenate deficiency induces energetic uncoupling inZymomonas.     

Respiration and glycolysis in the human diploid cell strain WI-38

Assessment of the respiratory and glycolytic capacity of non-growing WI-38 cells shows that, in the absence and presence of added glucose, the mean rates of oxygen consumption were 247 (QO₂ = 5.61) and 208 (QO₂ = 4.73) mμmoles/mg dry wt/hr., respectively. Mean glucose consumption was 225 mμmoles/mg dry wt/ hr. With uniformly labeled ¹⁴C glucose as substrate, 36 mμg atoms of carbon dioxide were produced, corresponding to 15–20% of the total cellular respiration. Mean values for lactate production in the presence and absence of glucose were 345 (Q_L^O2 = 7.85) and 196 (Q_L^O2 = 4.45) mμmoles/mg dry wt/hr., respectively. Human diploid cells in culture age, in the sense that their ability to proliferate decreases with time during serial subcultivation. Studies of their respiratory and glycolytic capacity as a function of the aging process showed that total respiration, glucose respiration and glycolytic capacity were relatively constant for cells in the middle and late passages and indicate that aging in this sense is not directly related to the respiratory and glycolytic capacity of the cell.     

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.     

PHOSPHATE METABOLISM IN BLUE-GREEN ALGAE. II. CHANGES IN PHOSPHATE DISTRIBUTION DURING STARVATION AND THE “POLYPHOSPHATE OVERPLUS” PHENOMENON IN PLECTONEMA BORYANUM

Physiological aspects of phosphate utilization by the blue-green alga Plectonema boryanum were studied. It was found that the external phosphate concentration influenced the distribution of phosphorus-containing compounds in the cell. Culturing the alga in concentrations of 10, 100, and 1000 mg PO₄/l resulted in increases in the level of acid-soluble and acid-insoluble polyphosphates. The values reported for 100 and 1000 mg PO₄/l were the same, indicating that the cells were able to assimilate and utilize only fixed amounts of phosphates. The total phosphorus value for these cells was calculated to be 6.5 μg P per 10⁶ cells. Culturing the alga in 1 mg PO₄/l led to a decrease in phosphate concentration of all cell fractions. Cells grown in the absence of phosphate for 5 days had total cell phosphorus levels of 0.76 μg P per 10⁶ cells. Cells in culture for two months or longer were found to have total cell phosphorus levels of 0.73 μg P per 10⁶ cells. This was determined to be the minimum cell phosphorus level limiting growth. Transfer of cells from either culture condition to a medium containing phosphate led to an “overplus” phenomenon. This overplus phenomenon was characterized by increases in all cellular phosphorus fractions. The most dramatic increase was found in both the acid-soluble and acid-insoluble polyphosphates. These fractions often increased by more than an order of magnitude. The greatest phosphate uptake occurred within 1 hr of transfer of phosphate-starved cells into a medium containing a known amount of phosphate and is essentially complete at 4 hr. The total cell phosphorus levels for uptake never increased beyond 18.9 μg per 10⁶ cells.     

A modified unstructured mathemathical model for the penicillin G fed-batch fermentation

Summary In this paper, an updated unstructured mathematical model for the penicillin G fed-batch fermentation is proposed, in order to correct some physical and biochemical shortcomings in the model of Heijnen et al. (1979,Biotechnol. Bioeng.,21, 2175–2201) and the model of Bajpai and Reuß (1980,J. Chem. Tech. Biotechnol.,30, 332–344). Its main features are the consistency for all values of the variables, and the ability to adequately describe different metabolic conditions of the mould. The model presented here can be considered as the translation of the latest advances in the biochemical knowledge of the penicillin biosynthesis.Nomenclature t time (h) - S amount of substrate in broth (g) - X amount of cell mass in broth (g) - P amount of product in broth (g) - V fermentor volume (L) - F input substrate feed rate (L/hr) - C _s S/V substrate concentration in broth (g/L) - C _x X/V cell mass concentration in broth (g/L) - C _P P/V product concentration in broth (g/L) - s _F substrate concentration in feed stream (g/L) - E _m parameter related to the endogenous fraction of maintenance (g/L) - E _p parameter related to the endogenous fraction of production (g/L) - K _x Contois saturation constant for substrate limitation of biomass production (g/g DM) - K _s Monod saturation constant for substrate limitation of biomss production (g/L) - K _p saturation constant for substrate limitation of product formation (g/L) - K _i substrate inhibition constant for product formation (g/L) - m _s maintenance constant (g/g DM hr) - k _h penicillin hydrolysis or degradation constant (hr^–1) - Y _x/s cell mass on substrate yield (g DM/g) - Y _p/s product on substrate yield (g/g) - specific substrate consumption rate (g/g DM hr) - specific growth rate (hr^–1) - _substr specific substrate to biomass conversion rate (hr^–1) - _x maximum specific substrate to biomass conversion rate (hr^–1) - specific production rate (g/g DM hr) - _p specific production constant (g/g DM hr)     

Model-based control of feed rate and illuminance in a photosynthetic fed-batch reactor for H2S removal

Traditional application of computer to fermentation processes has focused on the measurement and control of parameters such as temperature, pH, vessel pressure, sparge rate, dissolved oxygen, substrate concentration, and product concentration. In a fed-batch reactor with the photosynthetic green sulfur bacterium Chlorobium thiosulfatophilum which converts hydrogen sulfide to elementary sulfur or sulfate, separate measurement of cell mass concentration and sulfur particle concentration turbidimetrically was difficult due to their combined contributions to the total turbidity. Instead of on-line measurement of many process variables, a model-based control of feed rate and illuminance was designed. Optimal operation condition relating feed rate vs. light intensity was obtained to suppress the accumulation of sulfate and sulfide, and to save light energy in a 4-1 photosynthetic fed-batch reactor. This relation was correlated with the inreasing cell mass concentration. A model which describes the cell growth by considering the light attenuation effects due to scattering and absorption, and to crowding effect of the cells, was established beforehand with the results from the experiments. Based on these optimal operating conditions and the cell growth model, automatic controls of feed rate and illuminance were carried out alternatively to the traditional application of computer to fermentation with on-line measurement, realtime response and adjustment of process variables.List of Symbols F ml/min Flow rate of gas mixture - hV lux Average illuminance - Q mmol/(l h) Removal rate of hydrogen sulfide - X mg protein/l Cell mass concentration as protein - X ₀ mg protein/l Initial cell mass concentration - X _m mg protein/l Maximum cell mass concentration - _a h^–1 Apparent specific growth rate     

Oxygen supply to bacterial suspensions of high cell densities by hydrogen peroxide

The supply of heterotrophically growing suspensions of Alcaligenes eutrophus PHB^?4 with oxygen formed by the continuous addition of H₂O₂ in the presence of bovine liver catalase was found to be restricted to well-defined conditions. The catalase-H₂O₂ system proved to be suitable during the growth at low cell densities equivalent to 2 g dry weight/liter. When under these conditions the oxygen concentration was held constant at 1.8 mg O₂/liter, the cells grew for 6–8 hr at a rate almost identical to that observed with conventional aeration. However, aeration with H₂O₂ for longer durations (10–20 hr) and at higher cell densities (5?20 g dry weight/liter) led invariably to cell damage and retardation of growth. The impairment of growth observed during the oxygen supply by the catalase?H₂O₂ system was traced back to the formation of gradually increasing steady-state concentrations of H₂O₂ in the medium. Possible sites of cell damage by H₂O₂ such as membrane function, excretion and function of siderophores, and synthesis of cell polymers have been studied, and the cytotoxic mechanism of low concentrations of H₂O₂ was discussed.     

An investigation of cell density effects on hybridoma metabolism in a homogeneous perfusion reactor

In this work, metabolite and antibody production kinetics of hybridoma cultures were investigated as a function of cell density and growth rate in a homogeneous perfusion reactor. Hydrophilized hollow fiber polypropylene membranes with a pore size of 0.2 m were used for medium perfusion. Oxygen was supplied to the cells through thin walled silicone tubing. The mouse-mouse hybridoma cells were grown in three identical bioreactors at perfusion rates of 1.1, 2.0, and 3.2/day for a period of eight days during which the viable cell concentrations reached stable values of 2.6×10⁶, 3.5×10⁶, and 5.2×10⁶ cells/ml, respectively. Total cell densities reached values ranging from 8×10⁶ to 1×10⁶ cells/ml. Specific substrate consumption and product formation rates responded differently to changes in cell density and apparent specific growth rate, which were not varied independently. Using multiple regression analysis, the specific glucose consumption rate was found to vary with viable cell density while the specific glutamine uptake and lactate production rates varied with both viable cell density and apparent specific growth rate. These results suggest that cell density dictates the rate of glucose consumption while the cell growth rate influences how glucose is metabolized, i.e., through glycolysis or the TCA cycle. The specific antibody production rate was found to be a strong function of cell density, increasing as cell density increased, but was essentially independent of the specific growth rate for the cell line under study.List of Symbols MAb monoclonal antibody - X _v viable cell density (cells/ml) - X _d nonviable cell density (cells/ml) - specific growth rate (1/day) - k _d specific death rate (1/day) - D dilution rate (1/day) - S _f substrate concentration in feed (g/l or mM) - S substrate concentration (g/l or mM) - P _f product concentration in feed (g/l or g/ml) - P product concentration (g/l or ug/ml) - q _s specific consumption rate of substrate (g/hr/cell or mmol/hr/cell) - q _p specific production rate of product (g/hr/cell) - q _MAb specific production rate of monoclonal antibody (g/hr/cell) This work was supported in part by a grant for the National Science Foundation (BCS-9157851) and by matching funds from Merck and Monsanto. We sincerely thank Mr. Roland Buchele of Akzo Inc. (Germany) for donation of the polypropylene membranes, Dr. Michael Fanger (Dartmouth Medical School) for the hybridoma cell line, Dr. Sadettin Ozturk (Verax Corp., Lebanon, NH) for technical discussions regarding reactor design, and Dr. Derrick Rollins (Iowa State University) for advice on statistical methods.     

Enhancement of erythritol production by Trichosporonoides oedocephalis ATCC 16958 through regulating key enzyme activity and the NADPH/NADP ratio with metal ion supplementation

Erythritol, a well-known natural sweetener, is mainly produced by microbial fermentation. Various metal ions (Al³⁺, Cu²⁺, Mn²⁺, and Ni²⁺) were added to the culture medium of Trichosporonoides oedocephalis ATCC 16958 at 30?mg/L in shake flask cultures. Compared with controls, Cu²⁺ increased the erythritol content by 86% and decreased the glycerol by-product by 31%. After 48 hr of shake flask culture, sodium dodecyl sulfate polyacrylamide gel electrophoresis showed that expression levels of erythrose reductase (ER) in the presence of 30?mg/L CuSO₄?·?5H₂O were higher than those obtained after treatment with other examined metal ions. Furthermore, after 108 hr of batch culture in a 5-L bioreactor, supplementation with 30?mg/L of CuSO₄?·?5H₂O increased the specific erythritol content by 27%. Further studies demonstrated that ER activity under 30?mg/L CuSO₄?·?5H₂O supplementation in a fermentor was overtly increased compared with the control after 60 hr, while glycerol-3-phosphate dehydrogenase activity was clearly reduced in most of the fermentation process. Furthermore, the NADPH/NADP ratio was slightly lower in T. oedocephalis cells treated with Cu²⁺ compared with control cells. These results provide further insights into Cu²⁺ effects on erythritol biosynthesis in T. oedocephalis and should improve the industrial production of erythritol by biological processes.     

The effect of dissolved oxygen tension and the utility of oxygen uptake rate in insect cell culture

Dissolved oxygen tension and oxygen uptake rate are critical parameters in animal cell culture. However, only scarce information of such variables is available for insect cell culture. In this work, the effect of dissolved oxygen tension (DOT) and the utility of on-line oxygen uptake rate (OUR) measurements in monitoring Spodoptera frugiperda (Sf9) cultures were determined. Sf9 cells were grown at constant dissolved oxygen tensions in the range of 0 to 30%. Sf9 metabolism was affected only at DOT below 10%, as no significant differences on specific growth rate, cell concentration, amino acid consumption/production nor carbohydrates consumption rates were found at DOT between 10 and 30%. The specific growth rate and specific oxygen uptake rate followed typical Monod kinetics with respect to DOT. The calculated _max and max were 0.033 h^-1 and 3.82×10^-10 mole cell^-1h^-1, respectively, and the corresponding saturation constants were 1.91 and 1.57%, respectively. In all aerated cultures, lactate was consumed only after glucose and fructose had been exhausted. The yield of lactate increased with decreasing DOT. It is proposed, that an apparent DOT in non-instrumented cultures can be inferred from the lactate yield of bioreactors as a function of DOT. Such a concept, can be a useful and important tool for determining the average dissolved oxygen tension in non-instrumented cultures. It was shown that the dynamic behavior of OUR can be correlated with monosaccharide (fructose and glucose) depletion and viable cell concentration. Accordingly, OUR can have two important applications in insect cell culture: for on-line estimation of viable cells, and as a possible feed-back control variable in automatic strategies of nutrient addition.Abbreviations DOT Dissolved oxygen tension - OUR Oxygen uptake rate - specific oxygen uptake rate - specific growth rate - X_v viable cell concentration - C_L, C^*, and oxygen concentrations in liquid phase, in equilibrium with gas phase, and medium molar concentration, respectively - H Henry's constant - K_La volumetric oxygen transfer coefficient - P_T total pressure - oxygen partial pressure - oxygen molar fraction - i discrete element     

Effects of oxygen supply on yeast growth and metabolism in continuous fermentation

The yield changes in cell mass and metabolites with changes in the oxygen supply rate were investigated in continuous ethanol fermentation. With increases in oxygen concentration in the purging gas from 5.3 to 39.3 %, the specific oxygen uptake rate (qO₂) increased from 0.158 to 1.24 mmol/g/h. With this change, cell mass increased from 13.2 to 14.9 g/l and glycerol decreased from 4.8 to 0.99 g/l, although little change in ethanol yield was observed. At a higher oxygen concentration and/or at a lower respiratory quotient (RQ), glycerol disappeared, acetaldehyde, acetoin and 2,3-butanediol increased, and ethanol started to decrease. The yields of iso-butylalcohol and iso-amylalcohol also increased with increases in the oxygen supply rate when RQ was lower than approximately 10. Reduction in the redox balance (NADH/NAD) in the cells by qO₂, appeared to reduce initially the rate of glycerol-3-phosphate formation and next the rate of ethanol formation, resulting in the accumulation of acetaldehyde and formation of 2,3-butanediol through acetoin. Fatty acid composition changed with changes in the oxygen supply rate. The value for unsaturation, Δ mol⁻¹, increased from 0.745 to 0.836 with the increase in qO₂ from 0.158 to 1.79 mmol/g/h. Increases in oleic acid (C18:1) and decreases in palmitic acid (C16:0) were the major changes with the increases in Δ mol⁻¹.     

Prodigiosin formation by Serratia marcescens in a chemostat

In a study of the control of metabolite formation, prodigiosin production by Serratia marcescens was used as a model. Specific production rates of prodigiosin formation were determined using batch culture technique. Sucrose as carbon source and NH₄NO₃ as nitrogen source resulted in a specific production rate of 0.476 mg prodigiosin (g cell dry weight)⁻¹ h⁻¹. Prodigiosin formation and productivity was inversely correlated to growth rate when the bacterium was grown under carbon limitation on a defined medium in a chemostat culture. The maximum specific growth rate (μ_max) was 0.54 h⁻¹ and prodigiosin was formed in amounts over 1 mg l⁻¹ up to a growth rate (μ) of 0.3 h⁻¹ at steady state conditions. At a dilution rate of 0.1 h⁻¹ growth at steady state with carbon and phosphate limitation supported prodigiosin formation giving a similar specific yield [1.17 mg prodigiosin (g cell dry weight)⁻¹ and 0.94 mg g⁻¹, respectively], however, cells grown with nitrogen limitation [(NH₄)₂SO₄] did not form prodigiosin. Productivity in batch culture was 1.33 mg l⁻¹ h⁻¹ as compared to 0.57 mg l⁻¹ h⁻¹ in the chemostat.