Factors affecting l-arginine production in the continuous culture of an l-arginine producer of Corynebacterium acetoacidophilum

The effects of culture conditions on l-arginine production by continuous culture were studied using a stable l-arginine hyperproducing strain of Corynebacterium aceto-acidophilum, SC-190. Strain SC-190 demonstrated a volumetric productivity of 35 g l⁻¹·h⁻¹ at a dilution rate of 0.083h⁻¹ and feeding sugar concentration of 8%, and a product yield of 29.2% at a dilution rate 0.021h⁻¹ and feeding sugar concentration of 15%. The corresponding values for fed-batch culture are 0.85 g·l⁻¹·h⁻¹ and 26%. However, the product yield decreased with an increase in the volumetric productivity. To achieve stable l-arginine production, aeration and agitation conditions sufficient to maintain an optimal level of redox potential (>−100 mV) were necessary. The addition of phosphate to the feeding medium led to a decrease in l-arginine production. It was confirmed in the steady state that growth and l-arginine formation were inhibited by a high concentration of l-arginine.     

Production of l-Methionine-enriched cells of a mutant derived from a methylotrophic yeast,Candida boidinii

l-Methionine-enriched cells production of an ethionine-resistant mutant of Candida boidinii no. 2201 was greatly improved by the control of pH and by feeding of methanol and other medium components during cultivation in a jar fermentor. Under the optimal conditions, 38.5 g (as dry weight)_of cells abd 282 mg of pool methionine (intracellular pool of free l-methionine) per l of culture broth were obtained after 11 d of cultivation.The culture conditions for production of l-methionine-enriched cells in continuous culture were investigated. With limited methanol in continuous cultivation, pool methionine productivity reached a maximum value of 1.14 mg·l⁻¹·h⁻¹ at a dilution rate of 0.05·h⁻¹. During methanol-limited growth in continuous cultivation, the pool methionine content of the mutant was about 20–35% higher than that in batch cultivation.     

Effect of dilution rates on the amount of wasted substrate during alcohol fermentation

Continuous ethanol production in a one-stage continuous stirred tank fermentor without recycle was carried out using a yeast strain Saccharomyces cerevisiae. Different dilution rates were used. Cell and ethanol concentrations in the culture medium decreased with increasing dilution rates, and the maximum value of 3.0 g l⁻¹h⁻¹was found at a dilution rate of 0.340 h⁻¹. Specific ethanol productivities increased as dilution rates were increased, and the highest value appeared at about the same dilution rate as that for the maximum fermentor productivity. A material balance equation, which relates total amount of spent medium to cell synsthesis, ethanol production, and overall maintenance, was introduced. The cellular yield and overall maintenance coefficients increased with increasing dilution rates. The fraction of limiting substrate utilized for overall maintenance, which includes the limiting substrate spent for purposes other than cell synthesis and ethanol production, decreased with increasing dilution rates. The non-product associated substrate utilization can be minimized if correct dilution rate is chosen.     

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.     

Effect of oxygen supply and dilution rate on the production of 2,3-butanediol in continuous bioreactor by Klebsiella pneumoniae

Kinetics of 2,3-butanediol production by Klebsiella pneumoniae (NRRL B199) from glucose have been studied in a continuous bioreactor. The effect of oxygen supply rate and dilution rate on the product output rate and yield of 2,3-butanediol were investigated. For a feed glucose concentration of 100 g l⁻¹, the optimum oxygen transfer rate is between 25.0–35.0 mmol l⁻¹ h⁻¹. Under these conditions, maximum product concentration obtained was 35 g l⁻¹ at a dilution rate of 0.1 h⁻¹ and the maximum product output rate obtained was 4.25 g l⁻¹ h⁻¹. The product yield based on the substrate utilized approached the theoretical value (50%) at low values of oxygen transfer rate but decreased with increasing oxygen transfer rate.     

Continuous high-ethanol fermentation from cane molasses by a flocculating yeast

Repeated-batch fermentation by a flocculating fusant, Saccharomyces cerevisiae HA 2, was done in a molasses medium that contained 20% (w/v) total sugar, at 30°C in an automatically controlled fermentor, and the effects of ethanol concentration on the specific growth rate and the specific production rate of ethanol were studied. Both the specific growth rate and the specific production rate of ethanol fell with increase of ethanol concentration, and there was a linear correlation between each rate and the concentration of thanol. The maximum specific growth rate (μ_max) and the maximum specific production rate of ethanol (q_max) were 0.12 h⁻¹ and 0.1 g ethanol/10⁹ cells·h, respectively. The specific growth rate and the specific production rate of ethanol fell to zero at ethanol concentration of 89 g/l and 95 g/l, respectively. The number of viable cells, calculated from the linear inhibition equation, was 1.3 × 10⁹ cells/ml for production of 85 g/l ethanol at a dilution rate (D₁) of 0.2 h⁻¹. Based on this estimation, a laboratory-scale continuous fermentation, using two fermentors in series, was done. In the second fermentor, 85 g/l ethanol was produced at a dilution rate (D₁) of 0.2 h⁻¹ by the active feedig of the fermented mash from the first fermentor into the second fermentor by pumping (hereafter called active feeding). To maintain the number of viable cells above 10⁹ cells/ml in the second fermentor, a active feeding ratio of more than 23% was required. Under these conditions, 81 g/l ethanol was produced in the second fermentor at a dilution rate (D_t) of 0.25 h⁻¹, and the high ethanol productivity of 20.3 g/l·h could be achieved. A bench-scale continuous fermentation, using two fermentors in series, with a active feeding ratio of 25% was done. An ethanol concentration of 84 g/l in the second fermentor at a dilution rate (D_t) of 0.25 h⁻¹ was achieved, just as it was in the laboratory-scale fermentation test.     

Use of chemostat data for modelling extracellular-inulinase production by Kluyveromyces marxianus in a high-cell-density fed-batch process

Production of extracellular inulinase by low-cell-density (2 kg dry weight·m⁻³) sucrose-limited chemostat cultures of Kluyveromyces marxianus obeyed saturated kinetics at dilution rates ranging from 0.02 to 0.5 h⁻¹. A non-structured Monod-type equation, describing the relation between specific growth rate and specific extracellular-inulinase production rate, was used to fit experimental data. THis equation was subsequently incorporated in a model for the production of biomass and extracellular inulinase in a high-cell-density (> 100 kg dry weight·m⁻³) fed-batchculture of K. marxianus grown on sucrose. The model adequately described biomass production in the fed-batch culture. However, the production of extracellular inulinase in the fed-batch process was slightly higher than predicted by the model. This observation may be related to differences in growth conditions between in the chemostat and fed-batch cultures.     

Continuous production of an antibiotic polypeptide (nisin) by Lactococcus lactis using a bioreactor coupled to a microfiltration module

The continuous production of nisin, an antibiotic polypeptide, by Lactococcus lactis in a bioreactor system coupled to a microfiltration module is described. Nisin productivity with respect to both cultivation time (ND) and the quantity of glucose consumed (ND/S_f) in continuous production was enhanced by maintaining a low concentration of lactic acid in the broth. A maximum ND of 7.80 × 10⁴ U·l⁻¹·h⁻¹ and ND/S_f of 5.20 × 10³ U·g⁻¹·h⁻¹ were obtained when the glucose concentration in the feed medium was 15 g/l. These values represent about 4.1- and 4.5-fold increases, respectively, over those obtained in batch culture.     

Influence of the concentrations of d-xylose and yeast extract on ethanol production by Pachysolen tannophilus

To determine the most favorable conditions for the production of ethanol by Pachysolen tannophilus, this yeast was grown in batch cultures with various initial concentrations of two of the constituents of the culture medium: d-xylose (s_o), ranging from 1 g·l⁻¹ to 200 g·l⁻¹, and yeast extract (l_o), ranging from 0 g·l⁻¹ to 8 g·l⁻¹. The most favorable conditions proved to be initial concentrations of S_o=25 g·l⁻¹ and l_o=4 g·l⁻¹, which gave a maximum specific growth rate of 0.26 h⁻¹, biomass productivity of 0.023 g·l⁻¹·h⁻¹, overall biomass yield of 0.094 g·g⁻¹, specific xylose-uptake rate (q_s) of 0.3 g·g⁻¹·h⁻¹ (for t=50 h), specific ethanol-production rate (q_E) of 0.065 g·g⁻¹·h⁻¹ and overall ethanol yield of 0.34 g·g⁻¹; q_s values decreased after the exponential growth phase while q_E remained practically constant.     

Continuous solvent production from whey permeate using cells of Clostridium acetobutylicum immobilized by adsorption onto bonechar

Cells of Clostridium acetobutylicum were immobilized by adsorption onto bonechar and used in a packed bed reactor for the continuous production of solvents from whey permeate. A maximum solvent productivity of 4.1 g l⁻¹ h⁻¹, representing a yield of 0.23 g solvent/g lactose utilized, was observed at a dilution rate of 1.0 h⁻¹. The reactor was operated under stable conditions for 61 days. High concentrations of lactose in the whey permeate favored solventogenesis, while low concentrations favored acidogenesis.     

The simultaneous utilization of kinetic analysis and flow cytometry in the assessment of Lactobacillus rhamnosus ATCC 7469 physiological states produced by increasing oxygen limitation levels and lactic acid accumulation

Carbon limited continuous cultures of Lactobacillus rhamnosus ATCC 7469 were grown at dilution rates between 0.1 h⁻¹ and 0.6 h⁻¹. At 0.45 h⁻¹, oxygen uptake decreases producing a deficiency in the production of cell energy, lowering the concentration of biomass and finally accumulating glucose in the broth. Under the lack of energy pressure, L. rhamnosus ATCC 7469 triggers the production of lactic acid from pyruvate freeing NAD⁺ and stimulates glycolysis to continue, producing extra ATP from substrate-level phosphorylation. The 12-fold growing concentration of lactic acid and the 2-fold increase of succinic acid are in parallel with the steep 4-fold decrease of acetic acid production and small concentration changes of formic and propionic acids.The way the cells balance the available energy between the growing dilution rate and detoxification produces a stress within the culture, detected and described by flow cytometry. As the dilution rate increased, the proportion of L. rhamnosus ATCC 7469 cells with depolarized membrane steadily increased (1% at D = 0.20 h⁻¹, 8% at D = 0.30 h⁻¹, 14% at D = 0.45 h⁻¹ and 26% for D = 0.62 h⁻¹, respectively). Only a low level of 3.7% of the population did not recover from the demanding growth rates in the acidic environment.     

The activity of beta-galactosidase and lactose metabolism in Kluyveromyces lactis cultured in cheese whey as a function of growth rate

Aims: Kluyveromyces lactis was cultured in cheese whey permeate on both batch and continuous mode to investigate the effect of time course and growth rate on β‐galactosidase activity, lactose consumption, ethanol production and protein profiles of the cells. Methods and Results: Cheese whey was the substrate to grow K. lactis as a batch or continuous culture. In order to precise the specific growth rate for maximum β‐galactosidase activity a continuous culture was performed at five dilution (growth) rates ranging from 0·06, 0·09, 0·12, 0·18 to 0·24 h^?1. The kinetics of lactose consumption and ethanol production were also evaluated. On both batch and continuous culture a respirofermentative metabolism was detected. The growth stage for maximum β‐gal activity was found to be at the transition between late exponential and entrance of stationary growth phase of batch cultures. Fractionating that transition stage in several growth rates at continuous culture a maximum β‐galactosidase activity at 0·24 h^?1 was observed. Following that stage β‐gal activity undergoes a decline which does not correlate to the density of its corresponding protein band on the gel prepared from the same samples. Conclusion: The maximum β‐galactosidase activity per unit of cell mass was found to be 341·18 mmol ONP min^?1 g^?1 at a dilution rate of 0·24 h^?1. Significance and Impact of the Study: The physiology of K. lactis growing in cheese whey permeate can proven useful to optimize the conversion of that substrate in biomass rich in β‐gal or in ethanol fuel. In addition to increasing the native enzyme the conditions established here can be set to increase yields of recombinant protein production based on the LAC4 promoter in K. lactis host.     

Factors affecting conjugative transfer rates of plasmids in batch and continuous cultures

Factors affecting the rates of plasmid transfer were investigated using Escherichia coli LC102 bearing a conjugative plasmid R100-1 and E. coli DH1. The rate constant of transconjugant increase, k_ti, was used for presenting the degree of plasmid transmissibility instead of the plasmid transfer efficiency (pte). The rate constant was defined as the specific rate of transconjugant increase (srti, the number of transconjugants per donor per h) divided by the recipient cell concentration. The k_ti values ranged between 10⁻¹⁰ and 10⁻¹⁵ ml cells⁻¹ h⁻¹, when estimated under various conditions. Moderate liquid agitation had a favorable effect on k_tf but agitation rates higher than 33 s⁻¹ (intergrated shear force) greatly decreased the value of k_ti. The transconjugant-forming activity of the cells growing in continuous culture did not significantly change with the dilution rate, except those growing at dilution rates less than 0.1 h⁻¹. The rate constant k_ti at temperatures of 10–15°C was as low as the detection limit (10⁻¹⁵ ml cells⁻¹ h⁻¹).     

Effect of temperature on the ATP pool and adenylate energy charge in Escherichia coli

The effect of cultivation temperature on the ATP pool and adenylate energy charge (EC) in Escherichia coli has been studied in both batch and continuous cultures. In batch culture, μ_max and the ATP pool increased with increasing growth temperatures between 27–42°C (from 0.26 to 0.62 h⁻¹, and from 5.1 to 8.2 nmol/mg dry wt., respectively). In continuous culture at a constant dilution rate (D = 0.2 h⁻¹), with increasing growth temperatures between 28–43°C, the ATP pool increased about 2-fold (from 4.2 to 8.1 nmol/mg dry wt) and the EC from 0.80 to 0.99.     

Cell mass production of Acinetobacter calcoaceticus in palm oil-limited chemostat culture

Chemostat culture of Acinetobacter calcoaceticus KB-2 was done under palm oil-limiting conditions for cell production, and variation of cell compositions and yield coefficients were investigated in connection with the specific growth rates. At the concentration of 0.6% palm oil, the productivity of cells and yield coefficient were 4.76 g cells/l/h and 1.18 g cells/g palm oil, respectively, at a practical dilution rate of 0.85 h⁻¹. About 80% of the palm oil was assimilated by the strain, and the maintenance coefficient was 0.035 g palm oil/g cells/h. Although the carbohydrate content remained essentially constant when the growth rate was varied, the lipid, protein, and nucleic acid contents were increased slightly at higher growth rates. Although the protein content increased only 3%, the protein yield coefficient (Y_p) increased about 1.5 times over the range of specific growth rates between 0.1 and 0.7 h⁻¹. The increase in Y_p was due to the higher protein content of the biomass and to higher values of the cell yield coefficient.     

Continuous ethanol production from raw starch using a reversibly soluble-autoprecipitating amylase and flocculating yeast cells

Direct ethanol production from raw starch was performed continuously using a combination of a reversibly soluble-autoprecipitating amylase (D-AS) in which Dabiase K-27 was immobilized covalently on an enteric coating polymer (hydroxypropyl methylcellulose acetate succinate, AS) as a carrier, and a flocculating yeast. Continuous production was carried out using a reactor equipped with a mixing vessel and a separation vessel. D-AS and the yeast were separated continuously from the product solution by self-sedimentation in the separation vessel and they were utilized repeatedly. In the continuous saccharification of raw starch by D-AS alone, the glucose productivity was about 3.6 g/l/h at a dilution rate (D) of 0.1 h⁻¹. In the continuous ethanol production from raw starch by a combination of D-AS and flocculating yeast cells, high ethanol productivity up to 2.0 g/l/h was achieved at D=0.1 h⁻¹. Although the enzymatic activity of D-AS is inactivated due to insolubilization of the enzyme by the accumulation of NaCl produced in controlling the pH in the reactor, it is possible to recover the D-AS enzymatic activity by removing the NaCl. This continuous fermentation system suggests a potential for effective ethanol production from raw starch, and it may be widely applicable in heterogeneous culture systems using solid substrates other than raw starch.     

Continuous ethanol production by yeast immobilized on to channeled alumina beads

Vertical and near-horizontal (15° angle) packed-bed columns were compared for continuous ethanol fermentation using an alcohol- and glucose-tolerant Saccharomyces cerevisiae strain immobilized on to channeled alumina beads (5·0 × 10⁹ cells g⁻¹ beads). Spaces between beads (1·0–6·5 mm) and angle (15°) of near-horizontal reactor columns (with six ports in each) efficiently removed CO₂ and increased ethanol productivity. Malt-glucose-yeast-extract broth containing 16·7% glucose at 35°C fed at a dilution rate of 3· h⁻¹ to thw two horizontal columns (in series) yielded maximum ethanol productivity of 40·0 g liter⁻¹ h⁻¹. Feedstock flow rate and other factors (temperature, pH, nutrients, and glucose levels) affected productivities. The immobilized-cell system showed operational stability for >3 months without plugging, and could be stored for at least one year with no loss of bioreactor performance. Scanning electron micrographs of the beads revealed large numbers of yeast-cells attached on to internal and external surfaces of beads.     

Lactic acid from acid whey permeate in a membrane recycle bioreactor

Whey permeate was obtained by ultrafiltration of cottage cheese whey and supplemented with yeast extract. The lactose in the permeate was converted into lactic acid by Lactobacillus bulgaricus in a high-performance membrane bioreactor configured in the cell recycle mode. At a cell concentration of 10 g l⁻¹, optimum productivity of lactic acid was 35 g l⁻¹ h⁻¹. Increasing the cell concentration to 30 g l⁻¹ enabled the use of a dilution rate of 1 h⁻¹ with complete substrate utilization. At 60 g l⁻¹, productivity was over 80 g l⁻¹ h⁻¹ with complete substrte utilization; this is vastly superior to conventional batch fermentations.     

Selection of sulfur source for methane production by Methanobacterium thermoautotrophicum

Sulfur sources capable of replacing sulfide were surveyed for biomethanation from H₂ and CO₂ by thermoautotrophic methanogen, Methanobacterium thermoautotrophicum. Among sulfur containing compounds tested, l-cysteine, thiosulfate and coenzyme M gave poor growth when added as sulfur sources, whereas simultaneous addition of two sulfur sources, l-cysteine+thiosulfate, l-cysteine+l-methionine or l-cysteine+coenzyme M stimulated the growth.In a pressure-controlled fermentor system developed to obtain stoichiometry between input and output gases, the ratio of H₂ and CO₂ consumption to CH₄ production was almost stoichiometric, and when l-cysteine and thiosulfate or l-methionine were used in place of sulfide (control) similar growth patterns were observed. In a culture with continuous supply of substrates gases (1.3 vvm) and sulfur sources of 1 mM l-cysteine+2 mM thiosulfate, specific growth rate and specific methane production rate were 0.35 h⁻ and 3.24 l g⁻¹h⁻¹, respectively, compared to 0.22 h⁻¹ and 5.76 l g⁻h⁻¹ with Na₂ S.     

Dilution rates influence ammonia-assimilating enzyme activities and cell parameters of Selenomonas ruminantium strain D in continuous (glucose-limited) culture

Aims: The objective of this study was to examine the effect of dilution rates (Ds, varying from 0·05 to 0·42 h^?1) in glucose‐limited continuous culture on cell yield, cell composition, fermentation pattern and ammonia assimilation enzymes of Selenomonas ruminantium strain D. Methods and Results: All glucose‐limited continuous culture experiments were conducted under anaerobic conditions. Except for protein, all cell constituents including carbohydrates, RNA and DNA yielded significant cubic responses to Ds with the highest values at Ds of either 0·10 or 0·20 h^?1. At Ds higher than 0·2 h^?1, fermentation acid pattern shifted primarily from propionate and acetate to lactate production. Succinate also accumulated at the higher Ds (0·30 and 0·42 h^?1). Glucose was most efficiently utilized by S. ruminantium D at 0·20 h^?1 after which decreases in glucose and ATP yields were observed. Under energy limiting conditions, glutamine synthetase (GS) and glutamate dehydrogenase (GDH) appeared to be the major enzymes involved in nitrogen assimilation suggesting that other potential ammonia incorporating enzymes were of little importance in ammonia assimilation in S. ruminantium D. GS exhibited lower activities than GDH at all Ds, which indicates that the bacterial growth rate is not a primary regulator of their activities. Conclusions: Studied dilution rates influenced cell composition, fermentation pattern and nitrogen assimilation of S. ruminantium strain D grown in glucose‐limited continuous culture. Significance and Impact of the Study: Selenomonas ruminantium D is an ecologically and evolutionary important bacterium in ruminants and is present under most rumen dietary conditions. Characterizing the growth physiology and ammonia assimilation enzymes of S. ruminantium D during glucose limitation at Ds, which simulate the liquid turnover rates in rumen, will provide a better understanding of how this micro‐organism responds to differing growth conditions.