Continuous ethanol production from Jerusalem artichoke tubers. I. Use of free cells of Kluyveromyces marxianus

The Continuous fermentation of Jerusalem artichoke juice to ethanol by free cells of Kluyveromyces marxianus UCD (FST) 55-82 has been studied in a continuous-stirred-tank bioreactor at 35 degrees C and pH 4.6. A maximum yield of 90% of the theoretical was obtained at a dilution rate of 0.05 h(-1). About 95% of the sugars were utilized at dilution rates lower than 0.15 h(-1). Volumetric ethanol productivity and volumetric biomass productivity reached maximum values of 7 g ETOH/L/h and 0.6 g dry wt/L/h, respectively, at a dilution rate of 0.2 h(-1). The maintenance energy coefficient for K. marxianus culture was found to be 0.46 g sugar/g biomass/h/ Oscillatory behavior was following a change in dilution rate from a previous steady state and from batch to continuous culture. Values of specific ethanol production rate and specific sugar uptake were found to increase almost linearly with the increase of the dilution rate. The maximum specific ethanol production rate and maximum specific sugar uptake rate were found to be 2.6 g ethanol/g/ cell/h and 7.9 sugars/g cell/h, respectively. Washout occurred at a dilution rate of 0.41 h(-1).     

Improved production of live cells of Lactobacillus rhamnosus by continuous cultivation using glucose-yeast extract medium

In this study, the growth kinetics of Lactobacillus rhamnosus and lactic acid production in continuous culture were assessed at a range of dilution rates (0.05 h(-1) to 0.40 h(-1)) using a 2 L stirred tank fermenter with a working volume of 600 ml. Unstructured models, predicated on the Monod and Luedeking-Piret equations, were employed to simulate the growth of the bacterium, glucose consumption, and lactic acid production at different dilution rates in continuous cultures. The maximum specific growth rate of L. rhamnosus, mu-max, was estimated at 0.40 h(-1), and the Monod cell growth saturation constant, Ks, at approximately 0.25 g/L. Maximum cell viability (1.3 x 10(10) CFU/ml) was achieved in the dilution rate range of D = 0.28 h(-1) to 0.35 h(-1). Both maximum viable cell yield and productivity were achieved at D = 0.35 h(-1). The continuous cultivation of L. rhamnosus at D = 0.35 h(-1) resulted in substantial improvements in cell productivity, of 267% (viable cell count) that achieved via batch cultivation.     

Continuous ethanol production from pineapple cannery waste using immobilized yeast cells

The cells of Saccharomyces cerevisiae ATCC 24553, were immobilized in k-carrageenan and packed in a tapered glass column reactor for ethanol production from pineapple cannery waste at temperature 30 degrees C and pH 4.5. The maximum productivity was 42.8 g ethanol 1(-1) h(-1) at a dilution rate of 1.5 h(-1). The volumetric ethanol productivity of the immobilized cells was ca. 11.5 times higher than the free cells. The immobilized cell reactor was operated over a period of 87 days at a dilution rate of 1.0 h(-1), without any loss in the immobilized cell activity. The maximum specific ethanol productivity and specific sugar uptake rate of the immobilized cells were 1.2 g ethanol g(-1) dry wt. cell h(-1) and 2.6 g sugar g(-1) dry wt. cell h(-1), respectively, at a dilution rate of 1.5 h(-1).     

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)     

Ethanol fermentation in a magnetically fluidized bed reactor with immobilized Saccharomyces cerevisiae in magnetic particles

Ethanol fermentation by immobilized Saccharomyces cerevisiae cells in magnetic particles was successfully carried out in a magnetically stabilized fluidized bed reactor (MSFBR). These immobilized magnetic particles solidified in a 2 % CaCl(2) solution were stable and had high ethanol fermentation activity. The performance of ethanol fermentation of glucose in the MSFBR was affected by initial particle loading rate, feed sugar concentration and dilution rate. The ethanol theoretical yield, productivity and concentration reached 95.3%, 26.7 g/L h and 66 g/L, respectively, at a particle loading rate of 41% and a feed dilution rate of 0.4 h(-1) with a glucose concentration of 150 g/L when the magnetic field intensity was kept in the range of 85-120 Oe. In order to use this developed MSFBR system for ethanol production from cheap raw materials, cane molasses was used as the main fermentation substrate for continuous ethanol fermentation with the immobilized S. cerevisiae cells in the reactor system. Molasses gave comparative ethanol productivity in comparison with glucose in the MSFBR, and the higher ethanol production was observed in the MSFBR than in a fluidized bed reactor (FBR) without a magnetic field.     

Relationships between cellobiose catabolism, enzyme levels, and metabolic intermediates in Clostridium cellulolyticum grown in a synthetic medium

Continuous cultures, under cellobiose sufficient concentrations (14. 62 mM) using a chemically defined medium, were examined to determine the carbon regulation selected by Clostridium cellulolyticum. Using a synthetic medium, a q(cellobiose) of 2.57 mmol g cells(-1) h(-1) was attained whereas the highest value obtained on complex media was 0.68 mmol g cells(-1) h(-1) (Payot et al. 1998. Microbiology 144:375-384). On a synthetic medium at D = 0.035 h(-1) under cellobiose excess, lactate and ethanol biosynthesis were able to use the reducing equivalents supplied by acetic acid formation and the H(2)/CO(2) ratio was found equal to 1. At a higher dilution rate (D = 0.115 h(-1)), there was no lactate production and the pathways toward ethanol and NADH-ferredoxin-hydrogenase contributed to balance the reducing equivalents; in this case a H(2)/CO(2) ratio of 1.54 was found. With increasing D, there was a progressive increase (i) in the steady-state concentration of NADH and NAD(+) pools from 11.8 to 22.1 micromol (g cells) (-1), (ii) in the intracellular NADH/NAD(+) ratios from 0.43 to 1.51. On synthetic media, under cellobiose excess the carbon flow was also equilibrated by three overflows: exopolysaccharide, extracellular protein, and amino acid excretions. At D = 0.115 h(-1), 34% of the cellobiose consumed was converted into exopolysaccharides; this deviation of the carbon flow and the increase of the phosphoroclastic activity decreased dramatically the pyruvate excretion and explained the break in lactate production. Whatever the dilution rate, C. cellulolyticum, using ammonium and cellobiose excess, always spilled usual amino acids accompanied by other amino compounds. In vitro, GAPDH, phosphoroclastic reaction, alcohol dehydrogenase, and acetate kinase activities were high under conditions giving high in vivo specific production rates. There were also correlations between the in vitro lactate dehydrogenase activity and in vivo lactate production, but in contrast with the preceding activities, these two parameters decreased with D. All the results demonstrate that C. cellulolyticum was able to optimize carbon catabolism from cellulosic substrates in a synthetic medium.     

Production of ethanol by Clostridium thermosaccharolyticum: I. Effect of cell recycle and environmental parameters

The direct microbial conversion (DMC) process for the production of ethanol from lignocellulosic biomass is limited by low volumetric ethanol production rates due to the low cell densities of Clostridium thermosaccharolyticum which is a key organism for ethanol production in this process. Hence, this study focuses on the use of a continuous- culture cell recycle system to improve the volumetric ethanol productivity and yield of the fermentation of xylose by C. thermosaccharolyticum. Early experiments with the continuous-culture cell recycle system showed a two-fold improvement in volumetric ethanol productivity. However, the ethanol yield at the higher dilution rates suffered because of the large amount of lactate produced. The manipulation of two environmental parameters-iron concentration in the nutrient medium and the N(2) purge rate of the fermentor headspace-allowed a dramatic reduction in the lactate production and a simultaneous improvement in the ethanol titer and yield. Under the improved conditions of increased iron concentration (12.5 mg/L FeSO(4) . 7H(2)O) and decreased N(2) purge rate (0.1 L/min), a continuous culture of C. thermosaccharolyticum operating at a dilution rate of 0.24 h(-1) and 50% cell recycle produced 8.6 g/L ethanol and less than 1 g/L each of acetate and lactate. The volumetric ethanol productivity was 2.2 g/L/h, which is 8 times larger than obtained for a continuous culture operated with no cell recycle and the same specific growth rate.     

Kinetics of hydrogen production with continuous anaerobic cultures utilizing sucrose as the limiting substrate

In this study, local sewage sludge was acclimated to establish H2-producing enrichment cultures, which were used to convert sucrose to H2 with continuously stirred anaerobic bioreactors. The steady-state behaviors of cell growth, substrate utilization, and product formation were closely monitored. Kinetic models were developed to describe and predict the experimental results from the H2-producing cultures. Operation at dilution rates (D) of 0.075-0.167 h(-1) was preferable for H2 production, resulting in a H2 concentration of nearly 0.02 mol/l. The optimal hydrogen production rate was 0.105 mol/h occurring at D=0.125 h(-1). The major volatile fatty acid produced was butyric acid (HBu), while acetic acid and propionic acid were also produced in lesser quantities. The major solvent product was ethanol, whose concentration was only 15% of that of HBu, indicating that the metabolic flow favors H2 production. The proposed model was able to interpret the trends of the experimental data. The maximum specific growth rate (mu(max)), Monod constant (Ks), and yield coefficient for cell growth (Y(x/s)) were estimated as 0.172 h(-1), 68 mg COD/l, and 0.1 g/g, respectively. The model study also suggests that product formation in the continuous hydrogen-producing cultures was essentially a linear function of biomass concentration.     

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)     

Performance assessment of two patent strains ofZymomonas mobilis in batch and continuous fermentations

Summary The performance ofZymomonas mobilis strains ATCC 31821 and ATCC 31823 was assessed in batch and continuous culture. In batch culture using a medium containing 250 g/l glucose, identical maximum specific growth rates of 0.16/h were found, though final biomass concentration and growth yield were significantly lower for ATCC 31 823 than for ATCC 31 821. Final ethanol concentrations in this medium were about 110 g/l vor both organisms. In continuous culture at increasing dilution rates using a medium containing 100 g/l glucose, no significant differences were seen between the two strains with respect to the fermentation parameters studied. For ATCC 31 821, maximum rates of glucose uptake (Q_s) and ethanol produktion (Q_p) of 8.7 g glu/g/h and 4.4 g eth/g/h, respectively, were found. Both strains showed a similar performance at a fixed dilution rate of 0.1/h, where maximum ethanol concentrations of about 68 g/l were reached at a feed glucose concentration of about 139 g/l. At this dilution rate the maximum values of Q_s and Q_p were about 5.8 g glu/g/h and 2.8 g eth/g/h, respectively. Test tube experiments showed that growth, measured as optical density, decreased with increasing concentrations of exogenous ethanol with complete inhibition of growth at ethanol concentrations >8% (v/v). As evidenced by the results presented here, we have been unable to practice the invention as described in U.S. Patent 4,403,034 (Rogers and Tribe 1983).Nomenclature D Dilution rate, 1/h - _max maximum specific growth rate, 1/h - S_R Initial substrate concentration, g glucose/1 - S Residual substrate concentration, g glucose/1 - S₀ Effluent substrate concentration, g glucose/1 - X Blomass concentration; g cells/l - OD₆₂₀ Optical density at 620 nm, dimensionless - [P] Product concentration, g ethanol/1 - Y_x/s Growth yield, g cells/g glucose used - Y_p/s Product yield, g ethanol/g glucose used - %, Yield Percentage yield, Y_p/sx100/Y _p ^s/max =Y_p/sx100/0.51 - Q_s Specific rate of glucose uptake, g glucose/g cells/h - Q_p Specific rate of ethanol formation, g ethanol/g cells/h - m_e Maintenance energy coefficient, g glucose/g cells/h - VP Volumetric productivity, g ethanol/l/h - t Fermentation time, h     

In situ detoxification and continuous cultivation of dilute-acid hydrolyzate to ethanol by encapsulated S. cerevisiae

Dilute-acid lignocellulosic hydrolyzate was successfully fermented to ethanol by encapsulated Saccharomyces cerevisiae at dilution rates up to 0.5h(-1). The hydrolyzate was so toxic that freely suspended yeast cells could ferment it continuously just up to dilution rate 0.1h(-1), where the cells lost 75% of their viability measured by colony forming unit (CFU). However, encapsulation increased their capacity for in situ detoxification of the hydrolyzate and protected the cells against the inhibitors present in the hydrolyzate. While the cells were encapsulated, they could successfully ferment the hydrolyzate at tested dilution rates 0.1-0.5h(-1), and keep more than 75% cell viability in the worst conditions. They produced ethanol with yield 0.44+/-0.01 g/g and specific productivity 0.14-0.17 g/(gh) at all dilution rates. Glycerol was the main by-product of the cultivations, which yielded 0.039-0.052 g/g. HMF present in the hydrolyzate was converted 48-71% by the encapsulated yeast, while furfural was totally converted at dilution rates 0.1 and 0.2h(-1) and partly at the higher rates. Continuous cultivation of encapsulated yeast was also investigated on glucose in synthetic medium up to dilution rate 1.0 h(-1). At this highest rate, ethanol and glycerol were also the major products with yields 0.43 and 0.076 g/g, respectively. The experiments lasted for 18-21 days, and no damage in the capsules was detected.     

Continuous fermentation of undetoxified dilute acid lignocellulose hydrolysate by Saccharomyces cerevisiae ATCC 96581 using cell recirculation

Saccharomyces cerevisiae ATCC 96581 was cultivated in a chemostat reactor with undetoxified dilute acid softwood hydrolysate as the only carbon and energy source. The effects of nutrient addition, dilution rate, cell recirculation, and microaerobicity were investigated. Fermentation of unsupplemented dilute acid lignocellulose hydrolysate at D = 0.10 h(-1) in an anaerobic continuous reactor led to washout. Addition of ammonium sulfate or yeast extract was insufficient for obtaining steady state. In contrast, dilute acid lignocellulose hydrolysate supplemented with complete mineral medium, except for the carbon and energy source, was fermentable under anaerobic steady-state conditions at dilution rates up to 0.14 h(-1). Under these conditions, washout occurred at D = 0.15 h(-1). This was preceded by a drop in fermentative capacity and a very high specific ethanol production rate. Growth at all different dilution rates tested resulted in residual sugar in the chemostat. Cell recirculation (90%), achieved by cross-flow filtration, increased the sugar conversion rate from 92% to 99% at D = 0.10 h(-1). Nutrient addition clearly improved the long-term ethanol productivity in the recirculation cultures. Application of microaerobic conditions on the nutrient-supplemented recirculation cultures resulted in a higher production of biomass, a higher cellular protein content, and improved fermentative capacity, which further improves the robustness of fermentation of undetoxified lignocellulose hydrolysate.     

Kinetic parameters of continuous cultures of Bacillus thermoleovorans sp. A2 degrading phenol at 65 degrees C

In this paper, we report on the kinetics of phenol degradation and cell growth in continuous cultures of suspended cells of Bacillus thermoleovorans sp. A2 at 65 degrees C. A high yield coefficient of Y(x/s)=0.84 g cell dry weight g(-1) phenol was measured at a dilution rate of 0.5 h(-1). At the same dilution rate the coefficient for maintenance metabolism (m(s)) was determined to be 0.045 g phenol g(-1) cell dry weight h(-1). The maximal growth rate (wash-out) determined at a phenol inlet concentration of 188 mg l(-1) was 0.9 h(-1). Up to 7 g phenol l(-1) per day were degraded in a continuously operated 2-l stirred tank reactor with suspended cells (feed concentration 660 mg l(-1)). Additionally, yield coefficients for oxygen and ammonium are reported.     

High productivity continuous ethanol fermentation with a flocculating mutant strain of Zymomonas mobilis

High fermenter (volumetric) ethanol productivities (80 g/lh^–1) were attained in a simple single-stage continuous-stirred-tank-reactor (CSTR) employing a flocculent mutant of Zymomonas mobilis with a feed containing 100g/l glucose. Under these conditions a final ethanol concentration of 47.6 g/l was obtained, representing a maximum conversion efficiency of 97% of theoretical.Nomenclature SR = Medium glucose concentration (g/l)X Biomass concentration (g/l) - P Ethanol concentration (g/l) - VP Volumetric productivity (g ethanol/l/h) - Yp/s Product yield coefficient (g ethanol/g glucose consumed) - Qp Specific rate of ethanol formation (g ethanol/g cells/h) - D Dilution rate (h^–1) - Dmax Maximum dilution rate: ie., highest dilution rate at which the effluent glucose concentration 4g/l (h^–1)     

Experimental investigations of multiple steady states in aerobic continuous cultivations of Saccharomyces cerevisiae

The steady-state behavior of a glucose-limited, aerobic, continuous cultivation of Saccharomyces cerevisiae CEN.PK113-7D was investigated around the critical dilution rate. Oxido-reductive steady states were obtained at dilution rates up to 0.09 h(-1) lower than the critical dilution rate by operating the bioreactor as a productostat, where the dilution rate was controlled on the basis of an ethanol measurement. Thus, the experimental investigations revealed that multiple steady states exist in a region of dilution rates below the critical dilution rate. The existence of multiple steady states was attributed to two distinct physiological effects occurring when growth changed from oxidative to oxido-reductive: (i) a decrease in the efficiency of ATP production and utilization (at ethanol concentrations below 3 g/L) and (ii) repression of the oxidative metabolism (at higher ethanol concentrations). The first effect was best observed at low ethanol concentrations, where multiple steady states were observed even when no repression of the oxidative metabolism was evident, i.e., the oxidative capacity was constant. However, at higher ethanol concentrations repression of the oxidative metabolism was observed (the oxidative capacity decreased), and this resulted in a broader range of dilution rates where multiple steady states could be found.     

Vancomycin production is enhanced in chemostat culture with biomass-recycle

Production of the glycopeptide antibiotic vancomycin by Amycolatopsis orientalis ATCC 19795 was examined in phosphate-limited chemostat cultures with biomass-recycle, employing an oscillating membrane separator, at a constant dilution rate (D= 0. 14 h-1). Experiments made under low agitation conditions (600 rpm) showed that the biomass concentration could be increased 3.9-fold with vancomycin production kinetics very similar to that of chemostat culture without biomass-recycle. The specific production rate (qvancomycin) was maximal when the biomass-recycle ratio (R) was 0.13 (D= 0.087 h-1). When the dissolved oxygen tension dropped below 20% (air saturation), the biomass and vancomycin concentrations decreased and an unidentified red metabolite was released into the culture medium. Using increased agitation (850 rpm), used to maintain the dissolved oxygen tension above 20% air saturation, maximum increases in biomass concentration (7.9-fold) and vancomcyin production 1.6-fold (0.6 mg/g dry weight/h) were obtained when R was 0.44 (D= 0.056 h -1) compared to chemostat culture without biomass-recycle. Moreover, at this latter recycle ratio the volumetric vancomycin production rate was 14.7 mg/L/h (a 7-fold increase compared to chemostat culture without biomass-recycle). These observations encourage further research on biomass-recycling as a means of optimising the production of antibiotics.     

Coupling two sizes of CSTR-type bioreactors for sequential lactic acid and xylitol production from hemicellulosic hydrolysates of vineshoot trimmings

This study develops a system for the efficient valorisation of hemicellulosic hydrolysates of vineshoot trimmings. By connecting two reactors of 2L and 10L, operational conditions were set up for the sequential production of lactic acid and xylitol in continuous fermentation, considering the dependence of the main metabolites and fermentation parameters on the dilution rate. In the first bioreactor, Lactobacillus rhamnosus consumed all the glucose to produce lactic acid at 31.5°C, with 150rpm and 1L of working volume as the optimal conditions. The residual sugars were employed for the xylose to xylitol bioconversion by Debaryomyces hansenii in the second bioreactor at 30°C, 250rpm and an air-flow rate of 2Lmin(-1). Several steady states were reached at flow rates (F) in the range of 0.54-5.33mLmin(-1), leading to dilution rates (D) ranging from 0.032 to 0.320h(-1) in Bioreactor 1 and from 0.006 to 0.064h(-1) in Bioreactor 2. The maximum volumetric lactic acid productivity (Q(P LA)=2.908gL(-1)h(-1)) was achieved under D=0.266h(-1) (F=4.44mLmin(-1)); meanwhile, the maximum production of xylitol (5.1gL(-1)), volumetric xylitol productivity (Q(P xylitol)=0.218gL(-1)h(-1)), volumetric rate of xylose consumption (Q(S xylose)=0.398gL(-1)h(-1)) and product yield (0.55gg(-1)) were achieved at an intermediate dilution rate of 0.043h(-1) (F=3.55mLmin(-1)). Under these conditions, ethanol, which was the main by-product of the fermentation, was produced in higher amounts (1.9gL(-1)). Finally, lactic acid and xylitol were effectively recovered by conventional procedures.     

Effect of nutrient limitation on product formation during continuous fermentation of xylose with <Emphasis Type="Italic">Thermoanaerobacter ethanolicus</Emphasis> JW200 Fe(7)

Thermoanaerobacter ethanolicus JW200 Fe(7) was grown in continuous culture, using xylose as the primary carbon source, with progressively lower concentrations of supplementary yeast extract. This enabled the comparison of metabolic flux to fermentation end-products under carbon-limited and carbon-sufficient (yeast extract-limited) conditions and the determination of process data under fully mass-balanced conditions. Under carbon-limitation, the specific ethanol-formation rate was described by q (p)=40.34 micro +3.74, the specific rate of substrate utilisation for maintenance was 0.31+/-0.02 g x g(-1) x h(-1) and the maximum cell yield on xylose, corrected for maintenance requirements, was 0.15+/-0.04 g x g(-1). Based on the product profiles, these corresponded to a maintenance coefficient of m(ATP)=4.1+/-0.5 mmol x g(-1) x h(-1) and a maximum cell yield of = 14.7+/-0.8 x g x mol(-1). Limitation by a component in yeast extract resulted in incomplete xylose utilisation, increased catabolic flux rates (primarily resulting in increased lactate production, due to limitations in the flux through the phosphoroclastic reaction), a reduction in cell yield = 10.0+/-1.0 g x mol(-1) and an increase in maintenance energy requirements of m(ATP)=7.95+/-0.7 mmol x g(-1). The latter was also reflected in a shift from ethanol to acetate production at lower growth rates. An analysis of ethanol and acetate tolerance indicated that any high-intensity process employing this strain would require a bioreactor design which incorporated continuous ethanol stripping.     

Changes in metabolism of the rumen bacterium Streptococcus bovis H13/1 resulting from alteration in dilution rate and glucose supply per unit time

Streptococcus bovis H13/1 was grown in a glucose-limited chemostat. A concomitant increase in dilution rate and glucose supply per unit time caused both an increase in lactate production per mole of glucose fermented and a linear increase in growth yield over the dilution rate range 0.052 to 0.141/h. When the dilution rate was increased with no change in glucose supply per unit time there was a reduction in lactate production and an increase in that of acetate and ethanol coinciding with a non-linear increase in growth yield. YMaxglu = 38.6 and a maintenance coefficient, ms = 0.290 mmol/l glucose/g cells/h were calculated. The results also suggested an interaction between the formate and CO2 pools.     

Effect of operating parameters on specific production rate of a cloned-gene product and performance of recombinant fermentation process

A two-stage continuous system in combination with a temperature-sensitive expression system were used as model systems to maximize the productivity of a cloned gene and minimize the problem associated with the plasmid instability for a high-expression recombinant. In order to optimize the two-stage fermentation process, the effects of such operational variables as temperature and dilution rate on productivity of cloned gene were studied using the model systems and a recombinant, Escherichia coli K12 DeltaH1 Deltatrp/pPLc23trp A1. When the expression of cloned gene is induced by raising the operating temperature above 38 degrees C, a significant decrease in the colony-forming-units (CFU) of the plasmid-harboring cell was observed, and the decrease was related to the product concentration. In order to describe this phenomenon, a new kinetic parameter related to the metabolic stress (metabolic stress factor) was introduced. It is defined as the ratio of the rate of change of pheno-type from colony-forming to non-colony-forming cells to the product accumulation per unit cell mass. At a fixed temperature of 40 degrees C, the varying dilution rate D in the range of 0.35-0.90 h(-1) did not affect the metabolic stress factor significantly. At a fixed dilution rate of D = 0.35 h(-1), this factor remained practically constant up to 41 degrees C but increased rapidly beyond 41 degrees C. The effects of temperature and dilution rate in the second stage on the specific production rate were also studied while maintaining the apparent specific growth rate (mu(2) (app)) of the second stage constant at or near mu(2) (app) = 0.26 h(-1). Under a constant dilution rate, D(2) = 0.35 h(-1), the maximum specific production rate obtained was about q(p, max) = 38 units TrpA/mg cell/h at 41 degrees C. At a constant temperature, T(2) = 40 degrees C, specific production rate increased with decreasing dilution rate with in the dilution rate range of D(2) = 0.35-0.90 h(-1). Based on the results of our study, the optimal operating conditions found were dilution rate D(2) = 0.35 h(-1) and operating temperature T(2) = 41 degrees C at the apparent specific growth rate of 0.26 h(-1). Under the optimal operating conditions, about threefold increase in productivity was achieved compared to the best batch culture result. In addition, the fermentation period could be extended for more than 100 h.