Production of acetone and butanol by Clostridium acetobutylicum in continuous culture with cell recycle

Summary To increase the solvent productivity of the acetone-butanol fermentation, a continuous culture of Clostridium acetobytylicum with cell recycling was used. At a dry cell mass concentration of 8 g l^-1 and a dilution rate of D=0.64 h^-1, a solvent productivity of 5.4 g l^-1 h^-1 was attained. To prevent degeneration of the culture, which occurs with high concentrations of solvents (acetone, butanol and ethanol), different reactor cascades were used. A two-stage cascade with cell recycling and turbidostatic cell concentration control turned out to be the best solution, the first stage of which was kept at relatively low cell and product concentrations. A solvent productivity of 3 and 2.3 g l^-1 h^-1, respectively, was achieved at solvent concentrations of 12 and 15 g l^-1.Symbols D Dilution rate (h^-1) - r _p solvent productivity (g l^-1 h^-1) - s residual glucose concentration (g l^-1) - V _R reactor volume (l) - V _O overall volume (l) - x (dry) cell mass concentration (g l^-1) - Y _P/S solvent yield (g g^-1)     

Bubble free gaseous transfer in bioreactors using perfluorocarbons

In this work the concept of bubble-free oxygenation that was able to ensure oxygen supply and carbon dioxide extraction for a chemostat culture of Escherichia coli was experimentally demonstrated. It was operated at the dilution rate of 0.275 h^–1 under atmospheric pressure and at 35.5 °C. Foralkyl, a commercial perfluorocarbon, added in the influent medium under emulsified form and at 50% volumic fraction, was able to provide 0.17 g O₂/l/h and extract 0.23 g CO₂/l/h for a culture at 0.74 g/l of biomass. This oxygen supply was close to the maximum oxygenation Foralkyl was theoretically able to provide at this pressure when imposing a minimum oxygen concentration of 1 mg/l in the water phase. The quantification of transfer was not done from a direct measurement of oxygen transfer rates because conventional oxygen concentration measurement by membrane polarographic probe in an emulsion was not judged reliable. This evaluation was done by referring to conventional aerated culture whose measurable parameters (biomass and product concentrations) were found unaffected when shifting to the novel oxygenation device.List of Symbols C _LV ^* , C _LV g/l dissolved oxygen concentration in the vector phase at equilibrium and in the reactor - C _LW ^* , C _LW g/l dissolved oxygen concentration in the water phase at equilibrium and in the reactor - C _LWinput , C _LWoutput g/l dissolved oxygen concentrations in aqueous medium in the reactor input and output flow - D h^–1 dilution rate - ^DMM_{o 2}, MM_{co 2} g/mol oxygen and carbon dioxide molar masses - %O_2input, %O_2output oxygen percentages in the reactor input and output flow - %CO_2input, %CO_2output carbon dioxide percentages in the reactor input and output flow - %N _2input %N _2output nitrogen percentages in the reactor input and output flow - Q _G.i ⁿ Q _G.o ⁿ l/h gas flow rates at the reactor input and output at normal conditions (273 K, 1 atm) - Q _L l/h liquid flow rate - Q _LW , Q _LV l/h water and vector flow rates - r_{O 2} g/l/h oxygen consumption rate - r _x g/l/h biomass production rate - r _{CO 2} g/l/h carbon dioxide production rate - V _L l fermentor aqueous volume - V _LW , V _LV l water phase and vector phase volume - V _{O 2}, V _{CO 2}, l/mol oxygen and carbon dioxide molar volume under gaseous form at normal conditions (273 K, 1 atm) - Y _{O 2 x} gO₂/g cell oxygen consumption yield for biomass growth - Y _sx g glucose/g cell glucose consumption yield for biomass growth - vector volumic fraction - h^–1 growth rate This work was totally financed by the European Space Agency.     

Influence of operational parameters in the flocculation and production ofLactobacillus plantarum

Summary The influence of different operational parameters, such as the dilution rate (D) and the bleeding rate (B), in the production of a flocculent strain ofLactobacillus plantarum was studied. The effect of the dilution rate was demonstrated to be related to the lactic acid concentration inside the reactor. The effect of the bleeding rate was shown to be critical in the stabilization of the operation (due to a better pH control). It also allowed a continuous recovery of cells outside the reactor. Viability testing of the lactic starter cultures showed that operation with cell purge increased the viability of the starter cultures obtained.Nomenclature B Bleeding rate, h^–1 - D Dilution rate, h^–1 - F Feed flow rate, L h^–1 - I Feed velocity, m h^–1 - Specific growth rate, h^–1 - v Lactic acid specific productivity, g g^–1 h^–1 - P Product concentration (lactic acid), g L^–1 - P _out Product concentration leaving the system, g L^–1 - Q _b Bleeding flow rate, L h^–1 - R Recirculation velocity, m h^–1 - S Substract concentration, g L^–1 - t Time, h - T _p Time of ascensional flow (length of the column/total ascensional velocity), h - T _r Residence time (1/D), h - V Volume of the reactor, L - X Cell concentration, g L^–1 - X _out Cell concentration leaving the system, g L^–1     

Factors which influence the sedimentation characteristics of Torulopsis glabrata after growth in a recirculation system

Summary Some environmental affects on cell aggregation described in the literature are briefly summarized. By means of a biomass recirculation culture (Contact system), using the yeast Torulopsis glabrata, the aggregation behavior of cells in static and in dynamic test systems is described. Sedimentation times required to obtain 50 g · l^–1 yeast dry matter in static systems were always higher than in dynamic ones.In addition to, influencing the biomass yield, the specific growth rate of the yeast also affected cell aggregation. The specific growth rate and therefore the aggregation could be regulated by the biomass recirculation rate as well as by the sedimenter volume.Abbreviations f_o Overflow flow rate (l·h^–1) - f_R Recycle flow rate (l·h^–1) - f_t0t Total flow rate through the fermenter (l·h^–1) - g Gram - h Hour - D_R Fermenter dilution rate due to recycle (h^–1) - D_S Fermeter dilution rate due to substrate (h^–1) - D_tot Total fermenter dilution rate (h^–1) - l Liter - Specific growth rate (h^–1) - P_F Fermenter productivity (g·l^–1·h^–1) - P_FS Overall productivity (g·l^–1·h^–1) - R_pM Rates per minute - RS Residual sugar content in the effluent with respect to the substrate concentration (%) - Y Yield of biomass with respect to sugar concentration (%) - Sed 50 Sedimentation time to reach a YDM of 50 g·l^–1 (min) - V Volume (l) - V_F Fermenter volume (l) - V_Sed Sedimenter volume (l) - VVM Volumes per volume and minute - X_F YDM in the fermenter (g·l^–1) - X_F YDM in the recycle (g·l^–1) - X_S Yeast dry matter due to substrate concentration (g·l^–1) - YDM Yeast dry matter (g·l^–1)     

Optimization of lipid production in the oleaginous yeastApiotrichum curvatum in wheypermeate

Summary Lipid production of the oleaginous yeastApiotrichum curvatum was studied in wheypermeate to determine optimum operation conditions in this medium. Studies on the influence of the carbon to nitrogen ratio (C/N-ratio) of the growth medium on lipid production in continuous cultures demonstrated that cellular lipid content in wheypermeate remained constant at 22% of the cell dry weight up to a C/N-ratio of about 25. The maximal dilution rate at which all lactose is consumed in wheypermeate with excess nitrogen was found to be 0.073 h^-1. At C/N-ratios higher than 25–30 lipid content gradually increased to nearly 50% at C/N=70 and the maximal obtainable dilution rate decreased to 0.02 h^-1 at C/N=70. From these studies it could be derived that maximal lipid production rates can be obtained at C/N-ratios of 30–35 in wheypermeate. Since the C/N-ratio of wheypermeate normally has a value between 70 and 101, some additional nitrogen is required to optimize the lipid production rate. Lipid production rates ofA. curvatum in wheypermeate were compared in four different culture modes: batch, fed-batch, continuous and partial recycling cultures. Highest lipid production rates were achieved in culture modes with high cell densities. A lipid production rate of nearly 1 g/l/h was reached in a partial recycling culture. It was calculated that by using this cultivation technique lipid production rates of even 2.9 g/l/h may be reached when the supply of oxygen can be optimized.Nomenclature C/N-ratio carbon to nitrogen ratio of the growth medium (g/g) - C/N_crit C/N-ratio at which there is just enough nitrogen to allow all carbon source to be converted to biomass - D dilution rate=volume of incoming medium per unit time/volume of medium in the culture vessel (h^-1) - D_max maximum dilution rate (h^-1) - DW cell dry weight - L lipid yield (g storage lipid/g carbon source) - specific growth rate (h^-1) - _max maximum specific growth rate (h^-1) - Q_L lipid production rate (g/l/h) - Y_i molecular fraction of carbon substrate that is converted to storage carbohydrate (C-mol/C-mol) - Y_ls maximal amount of storage lipid that can be produced per mol carbon source (C-mol/C-mol)     

Adaptation of hybridoma cells to higher ammonia concentration

Using two mouse-mouse hybridoma cell lines, the response to ammonia step and serial changes was investigated in batch and continuous cultures with serum-free medium. The inhibitory effect of ammonia on cell growth depended on the cultivation mode, and differed markedly between cell lines. The cell line, 4C10B6 producing IgG monoclonal antibody against Pseudomonas, showed a high adaptation ability to ammonia. The 4C10B6 cells could grow under ammonia concentration as high as 21 mmol/l NH₄Cl with a viability of 80% in the continuous culture with serial increase in ammonia concentration. Whereas, in the batch culture with ammonia step change the cell growth completely ceased at 12 mmol/l NH₄Cl. The other cell line, TO-405 producing IgG monoclonal antibody against hepatitis B surface antigen, could not adapt to ammonia, and the cell growth did not occur at 9 mmol/l NH₄Cl even under the ammonia serial change.List of symbols D_Feed d^-1 Dilution rate of fresh feed medium (=F_o/V) - D_Out d^-1 Dilution rate of cell suspension (=F₁/V) - F₁ ml·d^-1 Volumetric discharge rate of cell suspension - F₀ ml·d^-1 Volumetric flow rate of fresh feed medium - k_D h^-1 Specific death rate - P mmol·l^-1 Product concentration - S mmol·l^-1 Substrate concentration in culture broth - S₀ mmol·l^-1 Substrate concentration in feed medium - t d Cultivation time - V ml Working volume of reactor - X₀ cells·ml^-1 Total cell density - X_V cells·ml^-1 Viable cell density - Y_P/S mmol·mmol^-1 Yield of product from substrate - Y_X/S cells·mmol^-1 Yield of cells from substrate - mmol·cell^-1·h^-1 Specific production rate - h^-1 Specific growth rate - mmol·cell^-1·h^-1 Specific consumption rate of substrate     

Effect of cell recycle on continuous butanol-acetone fermentation with Clostridium acetobutylicum under phosphate limitation

Summary An overflow filtration unit for cell recycle with Clostridium acetobutylicum was developed. A cellulose-triacetate ultrafiltration membrane with a cut-off volume of 20 000 MW was found to work best. C. acetobutylicum was grown in continuous culture under phosphate limitation (0.74 mM) at a pH value of 4.4 with cell recycle, the cell dry weight in the culture vessel reached 13.1 g/l at a dilution rate of D=0.10 h^-1 and 37°C. 377 mM of glucose were fermented to 190 mM butanol, 116.2 mM acetone and 25.8 mM ethanol. Total acids were 47.6 mM. The butanol productivity was 1.41 g/l/h. At a dilution rate of 0.40 h^-1 the butanol productivity was increased to 4.1 g/l/h but glucose consumption was decreased to 285 mM and butanol, acetone and ethanol production to 138.2, 97.5, 16.5 mM, respectively.     

Malate degradation by Schizosaccharomyces yeasts included in alginate beads

Schizosaccharomyces yeasts can be used for deacidification of grape musts. To this aim, we studied malic acid degradation by yeasts included in double layer alginate beads in a bubble column reactor. Use of immobilized micro-organisms allowed a continuous process with high dilution rates giving a deacidification capacity of 0.032 g of malate/hour/dm³/g of beads. The pneumatic agitation was very convenient in this case.List of Symbols D h^–1 Dilution rate for continuous culture - h Residence time for continuous culture - dM/dt kg/(m³ · h) Rate of degradation of malic acid - dS/dt kg/(m³ · h) Rate of consumption of glucose - _max h^–1 Maximal specific rate of growth     

Production of glutamine by micro-gel bead-immobilized Corynebacterium glutamicum 9703-T cells in a stirred tank reactor

The effectiveness of using micro-gel bead-immobilized cells for aerobic processes was investigated. Glutamine production by Corynebacterium glutamicum, 9703-T, cells was used as an example. The cells were immobilized in Sr-alginate micro-gel beads 500 m in diameter and used for fermentation processes in a stirred tank reactor with a modified impeller at 400 min^–1. Continuous production of glutamine was carried out for more than 220 h in this reactor and no gel breakage was observed. As a result of the high oxygen transfer capacity of this system, the glutamine yield from glucose was more than three times higher, while the organic acid accumulation was more than 24 times lower than those obtained with 3.0 mm-gel bead-immobilized cells in an airlift fermentor under similar experimental conditions. During the continuous fermentations there was evolution and proliferation of non-glutamine producing strains which led to a gradual decrease in the productivity of the systems. Although a modified production medium which suppresses cell growth during the production phase was effective in maintaining the productivity, the stability of the whole system was shortened due to high cell deactivation rate in such a medium.List of Symbols C kg/m³ glutamine concentration - C _A mol/m ³ local oxygen concentration inside the gel beads - C _AS mol/m ³ oxygen concentration at the surface of the gel beads - De m²/h effective diffusion coefficient of oxygen in the gel bead - DO mol/m³ dissolved oxygen concentration - F dm³/h medium flow rate - K h^–1 glutamine decomposition rate constant - Km mol/m³ Michaelis Menten constant - QO _2max mol/(kg · h) maximum specific respiration rate - R m radius of the gel beads - r m radial distance - t h time - V _C dm ³ volume of the gel beads - V _L dm ³ liquid volume in the reactor - Vm mol/(m³ · h) maximum respiration rate - X kg/m³ cell concentration - x r/R - y C _A /C_AS - h^–1 cell deactivation rate constant - Thiele modulus defined by R(Vm/De Km) ^1/2 - C _AS /Km - _C kg/(m³-gel · h) specific glutamine formation rate - _c dm³-gel/dm³ V _C /V _L      

Butanol production by Clostridium acetobutylicum in a continuous packed bed reactor

In this study, we report on a butanol production process by immobilized Clostridium acetobutylicum in a continuous packed bed reactor (PBR) using Tygon^® rings as a carrier. The medium was a solution of lactose (15–30 g/L) and yeast extract (3 g/L) to emulate the cheese whey, an abundant lactose-rich wastewater. The reactor was operated under controlled conditions with respect to the pH and to the dilution rate. The pH and the dilution rate ranged between 4 and 5, the dilution rate between 0.54 and 2.4 h^?1 (2.5 times the maximum specific growth rate assessed for suspended cells). The optimal performance of the reactor was recorded at a dilution rate of 0.97 h^?1: the butanol productivity was 4.4 g/Lh and the selectivity of solvent in butanol was 88%_w.     

The DNA,RNA and protein composition of the cyanobacterium Anacystis nidulans grown in light- and carbon dioxide-limited chemostats

The DNA, RNA and protein content of the cyanobacterium Anacystis nidulans was determined in light-limited and carbon dioxide-limited chemostat cultures over the dilution rate range, D=0.02 h^-1 to 0.19 h^-1. The macromolecular contents as a percentage of the dry weight and on a per cell basis varied significantly as a function of organism growth rate and the nature of the growth conditions. For both limitations the RNA content per cell increased [20–55 fg RNA (cell)^-1] with increasing dilution rate and also showed an increase as a percentage of the dry weight. The DNA content as a percentage of the dry weight showed a 2-fold decrease with increasing dilution rate over the range examined. On a per cell basis DNA reached a peak at D=0.1 h^-1 [4.5 fg DNA (cell)^-1] for light-limited organisms and at D=0.08 h^-1 [8.0 fg DNA (cell)^-1] for carbon dioxide-limited organisms. The q _RNA increased with increasing dilution rates over the complete growth rate range examined whilst q _DNA reached a maximum at D=0.09 to 0.10 h^-1. The protein content as a percentage of the dry weight was greater in CO₂-limited organisms than light-limited organisms but in both cultures declined as the dilution rate was increased above D=0.10 h^-1.     

Product inhibition during the feeding phasein fed-batch ethanol fermentation of sugar-cane blackstrap molasses

Summary The following equations represent the influence of the ethanol concentration (E) on the specific growth rate of the yeast cells () and on the specific production rate of ethanol () during the reactor filling phase in fed-batch fermentation of sugar-cane blackstrap molasses: = ₀ - k · E and v = v ₀ · K/(K +E) Nomenclature E ethanol concentration in the aqueous phase of the fermenting medium (g.L^–1) - E_m value of E when = 0 or = 0 (g.L^–1) - F medium feeding rate (L.h^–1) - k empirical constant (L.g^–1.h^–1) - K empirical constant (g.L^–1) - M_as mass of TRS added to the, reactor (g) - M_cs mass of consumed TRS (g) - M_e mass of ethanol in the aqueous phase of the fermenting medium (g) - M_s mass of TRS in the aqueous phase of the fermenting medium (g) - M_x mass of yeast cells (dry matter) in the fermenting medium (g) - r correlation coefficient - S TRS concentration in the aqueous phase of the fermenting medium (g.L^–1) - S_m TRS concentration of the feeding medium (g.L^–1) - t time (h) - T temperature (° C) - TRS total reducing sugars calculated as glucose - V volume of the fermenting medium (L) - V₀ volume of the inoculum (L) - X yeast cells concentration (dry matter) in the fermenting medium (g.L^–1) - filling-up time (h) - specific growth rate of the yeast cells (h^–1) - ₀ value of when E=0 - specific production rate of ethanol (h^–1) - ₀ value of when E=0 - density of the yeast cells (g.L^–1) - dry matter content of the yeast cells     

Growth characteristics of a thermotolerant strain of lodderomyces elongisporus grown on sucrose

A thermotolerant yeast species of Lodderomyces elongisporus EH 60 was isolated and physiologically characterized. This yeast possesses a high specific growth rate with μ_max = 0.61 h^?1. The dependence of the specific growth rate and cell yield on temperature, dilution rate, sucrose concentration and pH-value is investigated. Sucrose concentrations greater than 10 g/l inhibit the growth velocity. The specific growth rate μ can be calculated by a simple combination equation in the form: . The total optimum values for a sucrose-based continuous growth process with regard to the optimum cell yeild are: Y_S = 0.50 g DM/g S. T_opt. = 38,6 °C and D_opt. = 0,35 h^?1. The function Y_S = f(D, T) is represented by a total model.     

Long term shear effects on a hybridoma cell line by dynamic perfusion devices

The long term shear effects on a hybridoma cell line were studied by the simulation of a hollow fiber perfusion system. Various mechanical/environmental stress conditions were applied and steady state concentrations of live, dead and lysed cells were measured or calculated in a continuous culture. From mathematical modeling, it is shown that inclusion of a lysed cell index (LCI) renders a better fit to the material balance equation at steady state. The specific cell death rate increased with increasing shear force as expected only when the LCI was included. Without the inclusion of the LCI, the calculated specific cell growth rates are about 25–60% of the value when included. The results reported may lend some insight to design improvements since most perfusion devices add shear stresses to the cells in the reactor.List of Symbols b ml/hr continuous culture flow rate - D hr^–1 dilution rate (b/V) - m g glucose/10⁹ cells/hr specific maintenance coefficient - S ₀ g/l feed substrate concentration - S g/l reactor substrate concentration - t hr time - V ml reactor volume - X ⁺ cells/ml live cell concentration - X ^– cells/ml dead cell concentration - X ⁰ cells/ml lysed cell concentration - Y _x/s 10⁹ cells/g glucose cell/substrate yield coefficient - hr^–1 specific growth rate - hr^–1 specific death rate - hr^–1 specific lysis rate - hr^–1 specific lysis rate for simultaneous death and lysis     

Dialysis cultures with immobilized hybridoma cells for effective production of monoclonal antibodies

An industrial scale reactor concept for continuous cultivation of immobilized animal cells (e.g. hybridoma cells) in a radial-flow fixed bed is presented, where low molecular weight metabolites are removed via dialysis membrane and high molecular products (e.g. monoclonal antibodies) are enriched. In a new nutrient-split feeding strategy concentrated medium is fed directly to the fixed bed unit, whereas a buffer solution is used as dialysis fluid. This feeding strategy was investigated in a laboratory scale reactor with hybridoma cells for production of monoclonal antibodies. A steady state monoclonal antibody concentration of 478 mg l^-1 was reached, appr. 15 times more compared to the concentration reached in chemostat cultures with suspended cells. Glucose and glutamine were used up to 98%. The experiments were described successfully with a kinetic model for immobilized growing cells. Conclusions were drawn for scale-up and design of the large scale system.Abbreviations: c_Glc – glucose concentration, mmol l^-1; c_Gln – glutamine concentration, mmol l^-1; c_Amm – ammonia concentration, mmol l^-1; c_Lac – lactate concentration, mmol l^-1; c_MAb – MAb concentration, mg l^-1; D – dilution rate, d^-1; D_i – dilution rate in the inner chamber of the membrane dialysis reactor, d^-1; D₀ – dilution rate in the outer chamber of the membrane dialysis reactor, d^-1; q*_FB,Glc – volume specific glucose uptake rate related to the fixed bed volume, mmol l_FB ^-1 h^-1; q*_FB,Gln – volume specific glutamine uptake rate related to the fixed bed volume, mmol l_FB ^-1 h^-1.     

Reactor comparison and scale-up for the microaerobic production of 2,3-butanediol by Enterobacter aerogenes at constant oxygen transfer rate

Stirred tank (STR), bubble column (BCR) and airlift (ALR) bioreactors of 0.05 and 1.5 m³ total volume were compared for the production of 2,3-butanediol using Enterobacter aerogenes under microaerobic conditions. Batch fermentations were carried out at constant oxygen transfer rate (OTR=35 mmol/lh). At 0.05 m³ scale, the STR reactor achieved much higher biomass and product concentrations than the BCR and ALR reactors. At 1.5 m³ scale, however, exactly the same biomass and product concentrations could be obtained in both STR and ALR reactors. The 1.5 m³ ALR reactor performed also much better than its counterpart at small scale, achieving a productivity 2.4-fold as high as that of the 0.05 m³ BCL and ALR reactors. No differences in performances were observed between BCR and ALR. As compared to STR the tower reactors have a 12 time higher energetic efficiency (referred to product formation) and thus should be the choice for large scale production of 2,3-butanediol.The criterion of constant OTR or constant k _L a is not applicable for the scale-up of this oxygen-sensitive culture due to strong influence of reactor hydrodynamics under microaerobic conditions. The effects of mixing and circulation time on growth and metabolism of E. aerogenes were quantitatively studied in scaled-down experiments with continuous culture. For a successful scale-up of this microaerobic culture it is necessary to have an homogeneous oxygen supply over the entire reactor volume. Under conditions of inhomogeneous oxygen supply an optimum liquid circulation time exists which gives a maximum production of 2,3-butanediol.List of Symbols BD 2,3-butanediol - [mmol/l] saturation value of dissolved oxygen - D [h^–1] dilution rate - D [mm] reactor diameter - D _K [mm] top section diameter - D _R [mm] stirrer diameter - D _S [mm] draft tube diameter - EtOH ethanol - E _P [kg/kWh] energy efficiency refered to product formation - H [mm] height of reactor - HAc acetate - H _L [mm] height of liquid - k _L a [h^–1] volumetric oxygen transfer coefficient - N [rpm=min^–1] stirrer speed - OTR [mmol/lh] oxygen transfer rate - OUR [mmol/lh] oxygen uptake rate - p [Pa] pressure - P [kW] power input - P/V _L [kW/m³] specific power input - [mmHg] oxygen partial pressure (mmHg) or - [mmol/l] dissolved oxygen (mmol/l) - [mmol/gh] specific oxygen uptake rate - q _P [mmol/gh] specific productivity - R [Nm/kgK] gas constant, R = 287.06 - RQ respiration quotient - t _c [s] liquid circulation time - T [°C or K] temperature - TCA tricarboxylic acid - u _G [cm/s] mean superficial gas velocity - v _G [m/s] gas velocity at nozzels of gas distributor - V_G [l/h] aeration rate at inlet - V [m³ or l] total volume - V _L [m³ or l] liquid volume - V _N [l/mol] gas mole volume under normal conditions, V _N = 24.4116 - X [g/l] biomass concentration - CO₂ mole fraction in the effluent gas - O₂ mole fraction in the effluent gas - inlet (above the gas distributor) - ratio of oxygen consumed through TCA cycle to the total oxygen uptake rate - [g/l or kg/m³] density - [%] degree homogeneity - outlet of fermenter or top of the dispersion phase Dedicated to the 65th birthday of Professor Fritz Wagner.We thank Dr. C. Posten and T. Gabel for support with the computer control system UBICON. T.-G. Byun gratefully acknowledges financial support by DAAD.     

Influence of culture conditions on the cell yield and amylases biosynthesis in continuous culture by Schwanniomyces castellii

Schwanniomyces castellii excreted -amylase and amyloglucosidase into the medium in the presence of starch. The biosynthesis and the rate of excretion were influenced by dissolved oxygen (specially for -amylase), pH of the culture and dilution rate. The cell yield observed (0.59) remained constant up to D=0.35h^-1 with starch as substrate. But in the case of growth on glucose, the yield observed was equal to 0.62 up to a dilution rate of D=0.18 h^-1. Beyond this value Y x/s decreased and ethanol was produced. The onset of fermentation dependend partly on the nature of the substrate and not only on the environment in particular on the quantity of dissolved oxygen present.     

Phosphate-limited growth of Chromatium vinosum in continuous culture

Chromatium vinosum DSM 185 was grown in continuous culture at a constant dilution rate of 0.071 h^-1 with sulfide as the only electron donor. The organism was subjected to conditions ranging from phosphate limitation (S _R-phosphate=2.7 M and S _R-sulfide=1.8 mM) to sulfide limitation (S _R-phosphate=86 M and S _R-sulfide=1.8 mM). At values of S _R-phosphate below 7.5 M the culture was washed out, whereas S _R-phosphate above this value resulted in steady states. The saturation constant (K ) for growth on phosphate was estimated to be between 2.6 and 4.1 M. The specific phosphorus content of the cells increased from 0.30 to 0.85 mol P mg^-1 protein with increasing S _R-phosphate. The specific rate of phosphate uptake increased with increasing S _R-phosphate, and displayed a non-hyperbolic saturation relationship with respect to the concentration of phosphate in the inflowing medium. Approximation of a hyperbolic saturation function yielded a maximum uptake rate (V _max) of 85 nmol P mg^-1 protein h^-1, and a saturation constant for uptake (K _t) of 0.7 M. When phosphate was supplied in excess 8.5% of the phosphate taken up by the cells was excreted as organic phosphorus at a specific rate of 8 nmol P mg^-1 protein h^-1.Non-standard abbreviations BChla bacteriochlorophyll a - D dilution rate; _max, maximum specific growth rate - maximum specific growth rate if the substrate were not inhibitory - K saturation constant for growth on phosphate - V _max maximum rate of phosphate uptake - K _i saturation constant for phosphate uptake - K _i inhibition constant for growth in the presence of sulfide - S _R concentration of substrate in the inflowing medium     

Mixed substrate growth of methylotrophic yeasts in chemostat culture: Influence of the dilution rate on the utilisation of a mixture of glucose and methanol

The growth of Hansenula polymorpha and Kloeckera sp. 2201 with a mixture of glucose and methanol (38.8%/61.2%, w/w) and the regulation of the methanol dissimilating enzymes alcohol oxidase, catalase, formaldehyde dehydrogenase and formate dehydrogenase were studied in chemostat culture, as a function of the dilution rate. Both organisms utilized and assimilated glucose and methanol simultaneously up to dilution rates of 0.30 h^-1 (H. polymorpha) and 0.26h^-1, respectively (Kloeckera sp. 2201) which significantly exceeded _max found for the two yeasts with methanol as the only source of carbon. At higher dilution rates methanol utilisation ceased and only glucose was assimilated. Over the whole range of mixed-substrate growth both carbon sources were assimilated with the same efficiency as during growth with glucose or methanol alone.In cultures of H. polymorpha, however, the growth yield for glucose was lowered by the unmetabolized methanol at high dilution rates. During growth on both carbon sources the repression of the synthesis of all catabolic methanol enzymes which is normally caused by glucose was overcome by the inductive effect of the simultaneously fed methanol. In both organisms the synthesis of alcohol oxidase was found to be regulated differently as compared to catalase, formaldehyde and formate dehydrogenase. Whereas increasing repression of the synthesis of alcohol oxidase was found with increasing dilution rates as indicated by gradually decreasing specific activities of this enzyme in cell-free extracts, the specific activities of this enzyme in cell-free extracts, the specific activities of catalase and the dehydrogenases increased with increasing growth rates until repression started. The results indicate similar patterns of the regulation of the synthesis of methanol dissimilating enzymes in different methylotrophic yeasts.Abbreviations and Terms C₁ Methanol - C₆ glucose; D dilution rate (h^-1) - D _c critical dilution rate (h^-1) - q _s specific, rate of substrate consumption (g substrate [g cell dry weight]^-1 h^-1) - q _CO2 and q _O2 are the specific rates of carbon dioxide release and oxygen consumption (mmol [g cell dry weight]^-1 h^-1) - RQ respiration quotient (q _CO2 q _O2 ¹ ) - s ₀(C₁) and s ₀(C₆) are the concentrations of methanol and glucose in the inflowing medium (g l^-1) - s residual substrate concentration in the culture liquid (g l^-1) - Sp. A. enzyme specific activity - x cell dry weight concentration (gl^-1) - Y _X/C6 growth yield on glucose (g cell dry weight [g substrate]^-1     

Improvement of the culture stability of non-anchorage-dependent animal cells grown in serum-free media through immobilization

A murine hybridoma cell line producing a monoclonal antibody against penicillin-G-amidase and a murine transfectoma cell line secreting a monovalent chimeric human/mouse Fab-antibody fragment were cultivated in three different media (serum-containing, low protein serum-free, and iron-rich protein-free) in flask cultures, stirred reactors and a fixed bed reactor. In static batch cultures in flasks both cell lines showed similar good growth in all three media.In suspension in a stirred reactor, the hybridoma cell line could be cultivated satisfactory only in serum-containing medium. In low protein serum-free medium, Pluronic F68 had to be added to protect the hybridoma cells against shear stress. But even with this supplement only batch, not chemostat mode was possible. In iron-rich protein-free medium the hybridoma cells grew also in continuous chemostat mode, but the stability of the culture was low. The transfectoma cell line did not grow in stirred reactors in any of the three media.Good results with both cell lines were obtained in fixed bed experiments, where the cells were immobilized in macroporous Siran^®-carriers. The media, which were optimized in flask cultures, could be used without any further adaptation in the fixed bed reactor. Immobilization improved the stability and reliability of cultures of non-adherent animal cells in serum-free media tremendously compared to suspension cultures in stirred reactors. The volume-specific glucose uptake rate, an, indicator of the activity of the immobilized cells, was similar in all three media. Deviations in the metabolism of immobilized and suspended cells seem to be mainly due to low oxygen concentrations within the macroporous carriers, where the cells are supplied with oxygen only by diffusion.List of symbols c substrate or product concentration mmol l^–1 - c₀ substrate or product concentration in the feed mmol l^–1 - c_Glc glucose concentration mmol l^–1 - c_Gln glutamine concentration mmol l^–1 - c_Amm ammonia concentration mmol l^–1 - c_Lac lactate concentration mmol l^–1 - c_FAB concentration of Fab# 10 antibody fragment g l^–1 - c_MAb monoclonal antibody concentration mg l^–1 - D dilution rate d^–1 - q cell-specific substrate uptake or metabolite production rate mmol cell^–1 h^–1 - q_Glc cell-specific glucose uptake rate mmol cell^–1 h^–1 - q_Gln cell-specific glutamine uptake rate mmol cell^–1 h^–1 - q_MAb cell-specific MAb production rate mg cell^–1 h^–1 - q^* volume-specific substrate uptake or metabolite production rate mmol l^–1 h^–1 - q^*FB volume-specific substrate uptake or metabolite production rate related to the fixed bed volume mmol l_FB ^–1 h^–1 - q^*FB,Glc volume-specific glucose uptake rate related to the fixed bed volume mmol l_FB ^–1 h^–1 - q^*FB,Gln volume-specific glutamine uptake rate related to the fixed volume mmol l_FB ^–1 h^–1 - q^*FB,MAb volume-specific MAb production rate related to the fixed volume mg l_FB ^–1 h^–1 - q^*FB,02 volume-specific oxygen uptake rate related to the fixed bed volume mmol l_FB ^–1 h^–1 - t time h - U superficial flow velocity mm s^–1 - V medium volume in the conditioning vessel of the fixed bed reactor l - V_FB volume of the fixed bed l - x_v viable cell concentration cells ml^–1 - y_Amm,Gln yield of Ammonia from glutamine - y_Lac,Glc yield of lactate from glucose - specific growth rate h^–1 - _d specific death rate h^–1