Ethanol fermentation of mixed-sugars using a two-phase, fed-batch process: method to minimize D-glucose repression of Candida shehatae D-xylose fermentations

Candida shehatae cells pre-grown on D-xylose simultaneously consumed mixtures of D-xylose and D-glucose, under both non-growing (anoxic) and actively growing conditions (aerobic), to produce ethanol. The rate of D-glucose consumption was independent of the D-xylose concentration for cells induced on D-xylose. However, the D-xylose consumption rate was approximately three times lower than the D-glucose consumption rate at a 50% D-glucose: 50% D-xylose mixture. Repression was not observed (substrate utilization rates were approximately equal) when the percentage of D-glucose and D-xylose was changed to 22% and 78%, respectively. In fermentations with actively growing cells (50% glucose and D-xylose), ethanol yields from D-xylose increased, the % D-xylose utilized increased, and the xylitol yield was significantly reduced in the presence of D-glucose, compared to anoxic fermentations (Y_ETOH,xylose = 0.2–0.40 g g⁻¹, 75–100%, and Y_xylitol = 0–0.2 g g⁻¹ compared to Y_ETOH,xylose = 0.15 g g⁻¹, 56%, Y_xylitol = 0.51 g g⁻¹, respectively). To increase ethanol levels and reduce process time, fed-batch fermentations were performed in a single stage reactor employing two phases: (1) rapid aerobic growth on D-xylose (μ = 0.32 h⁻¹) to high cell densities; (2) D-glucose addition and anaerobic conditions to produce ethanol (Y_ETOH,xylose = 0.23 g g⁻¹). The process generated high cell densities, 2 × 10⁹ cells ml⁻¹, and produced 45–50 g L⁻¹ ethanol within 50 h from a mixture of D-glucose and D-xylose (compared to 30 g L⁻¹ in 80 h in the best batch process). The two-phase process minimized loss of cell viability, increased D-xylose utilization, reduced process time, and increased final ethanol levels compared to the batch process. Received 23 February 1998/ Accepted in revised form 15 July 1998     

Enhanced l-lysine production in threonine-limited continuous culture of Corynebacterium glutamicum by using gluconate as a secondary carbon source with glucose

In order to improve the production rate of l-lysine, a mutant of Corynebacterium glutamicum ATCC 21513 was cultivated in complex medium with gluconate and glucose as mixed carbon sources. In a batch culture, this strain was found to consume gluconate and glucose simultaneously. In continuous culture at dilution rates ranging from 0.2 h⁻¹ to 0.25 h⁻¹, the specific l-lysine production rate increased to 0.12 g g⁻¹ h⁻¹ from 0.1 g g⁻¹ h⁻¹, the rate obtained with glucose as the sole carbon source [Lee et al. (1995) Appl Microbiol Biotechnol 43:1019–1027]. It is notable that l-lysine production was observed at higher dilution rates than 0.4 h⁻¹, which was not observed when glucose was the sole carbon source. The positive effect of gluconate was confirmed in the shift of the carbon source from glucose to gluconate. The metabolic transition, which has been characterized by decreased l-lysine production at the higher glucose uptake rates, was not observed when gluconate was added. These results demonstrate that the utilization of gluconate as a secondary carbon source improves the maximum l-lysine production rate in the threonine-limited continuous culture, probably by relieving the limiting factors in the lysine synthesis rate such as NADPH supply and/or phosphoenolpyruvate availability. Received: 16 May 1997 / Received revision: 28 August 1997 / Accepted: 29 August 1997     

Transport of hemicellulose monomers in the xylose-fermenting yeastCandida shehatae

Summary Cells ofCandida shehatae repressed by growth in glucose- or D-xylose-medium produced a facilitated diffusion system that transported glucose (K _s±2 mM,V _max±2.3 mmoles g⁻¹ h⁻¹),d-xylose (K _s±125 mM,V _max±22.5 mmoles g⁻¹ h⁻¹) and D-mannose, but neither D-galactose norl-arabinose. Cells derepressed by starvation formed several sugar-proton symports. One proton symport accumulated 3-0-methylglucose about 400-fold and transported glucose (K _s±0.12 mM,V _max ± 3.2 mmoles g⁻¹ h⁻¹) andd-mannose, a second proton symport transportedd-xylose (K _s± 1.0 mM,V _max 1.4 mmoles g⁻¹ h⁻¹) andd-galactose, whilel-arabinose apparently used a third proton symport. The stoicheiometry was one proton for each molecule of glucose or D-xylose transported. Substrates of one sugar proton symport inhibited non-competitively the transport of substrates of the other symports. Starvation, while inducing the sugar-proton symports, silenced the facilitated diffusion system with respect to glucose transport but not with respect to the transport of D-xylose, facilitated diffusion functioning simultaneously with thed-xylose-proton symport.     

Continuous production of l(+)-lactic acid by Lactobacillus casei in two-stage systems

A two-stage two-stream chemostat system and a two-stage two-stream immobilized upflow packed-bed reactor system were used for the study of lactic acid production by Lactobacillus casei subsp casei. A mixing ratio of D ₁₂/D ₂= 0.5 (D = dilution rate) resulted in optimum production, making it possible to generate continuously a broth with high lactic acid concentration (48 g l⁻¹) and with a lowered overall content of initial yeast extract (5  g l⁻¹), half the concentration supplied in the one-step process. In the two-stage chemostat system, with the first stage at pH 5.5 and 37 °C and a second stage at pH 6.0, a temperature change from 40 °C to 45 °C in the second stage resulted in a 100% substrate consumption at an overall dilution rate of 0.05 h⁻¹. To increase the cell mass in the system, an adhesive strain of L. casei was used to inoculate two packed-bed reactors, which operated with two mixed feedstock streams at the optimal conditions found above. Lactic acid fermentation started after a lag period of cell growth over foam glass particles. No significant amount of free cells, compared with those adhering to the glass foam, was observed during continuous lactic acid production. The extreme values, 57.5 g l⁻¹ for lactic acid concentration and 9.72 g l⁻¹ h⁻¹ for the volumetric productivity, in upflow packed-bed reactors were higher than those obtained for free cells (48 g l⁻¹  and 2.42 g l⁻¹ h⁻¹) respectively and the highest overall l(+)-lactic acid purity (96.8%) was obtained in the two-chemostat system as compared with the immobilized-cell reactors (93%). Received: 4 December 1997 / Received revision: 23 February 1998 / Accepted: 14 March 1998     

Bioreactor for continuous synthesis of compactin by Penicillium cyclopium

Compactin was synthesized by Penicillium cyclopium in submerged as well as in bioreactor systems and assayed spectrophotometrically with a detection limit of 0.5 μg ml⁻¹ solvent. Synthesis in submerged culture was affected by aeration, glucose level, pH, and type and molarity of buffer. Citrate or succinate (pH 4.0, 0.10 M) in malt glucose peptone broth (MGPB) stimulated cell specialization, sporulation, enhanced compactin permeation from mycelia and its production (60.05 μg ml⁻¹ after 12 days). Fungal spores, immobilized onto-into loofah sponge, in a bioreactor, using MGPB-citrate as feed stock, resulted in productivity of 23.04 mg compactin (L⁻¹ h⁻¹) during 50 days operation at 0.45 h⁻¹ dilution rate. Compactin synthesis in the bioreactor was also affected by culture age, substrate, incubation and dilution rates. Scanning electron micrographs of the loofah sponge, prior to, during and post-spores immobilization showed that loofah channels served well for fungal support in the bioreactor. Received 6 October 1997/ Accepted in revised form 2 September 1998     

Physiology and kinetics of trimethylamine conversion by two methylotrophic strains in continuous cultivation systems

The change of dilution rate (D) on both Methylophilus methylotrophus NCIMB11348 and Methylobacterium sp. RXM CCMI908 growing in trimethylamine (TMA) chemostat cultures was studied in order to assess their ability to remove odours in fish processing plants. M. methylotrophus NCIMB11348 was grown at dilution rates of 0.012–0.084 h⁻¹ and the biomass level slightly increased up to values of D around 0.07 h⁻¹. The maximum cell production rate was obtained at 0.07 h⁻¹ corresponding to a maximum conversion of carbon into cell mass (35%). The highest rate of TMA consumption was 3.04 mM h⁻¹ occurring at D=0.076 h⁻¹. Methylobacterium sp. RXM CCMI908 was grown under similar conditions. The biomass increased in a more steep manner up to values of D around 0.06 h⁻¹. The maximum cell production rate (0.058 g l⁻¹h⁻¹) was obtained in the region close to 0.06 h⁻¹ where a maximum conversion of the carbon into cell mass (40%) was observed. The maximum TMA consumption was 2.33 mM h⁻¹ at D=0.075 h⁻¹. The flux of carbon from TMA towards cell synthesis and carbon dioxide in both strains indicates that the cell is not excreting products but directing most of the carbon source to growth. Carbon recovery levels of approximately 100% show that the cultures are carbon-limited. Values for theoretical maximum yields and maintenance coefficients are presented along with a kinetic assessment based on the determination of the substrate saturation constant and maximum growth rate for each organism. Received: 25 February 1999 / Received revision: 14 May 1999 / Accepted: 17 May 1999     

Pyranose 2-oxidase from Phanerochaete chrysosporium– further biochemical characterisation

Pyranose 2-oxidase (P2O) was purified 43-fold to apparent homogeneity from the basidiomycete Phanerochaete chrysosporium using liquid chromatography on phenyl Sepharose, Mono Q (twice) and phenyl Superose. The native enzyme has a molecular mass of about 250 kDa (based on native PAGE) and is composed of four identical subunits of 65 kDa. It contains three isoforms of isoelectric point (pI) 5.0, 5.05 and 5.15 and does not appear to be a glycoprotein. P2O is optimally stable at pH 8.0 and up to 60 °C. It is active over a broad pH range (5.0–9.0) with maximum activity at pH 8.0–8.5 and at 55 °C, and a broad substrate specificity. d-Glucose is the preferred substrate, but 1-β-aurothioglucose, 6-deoxy-d-glucose, l-sorbose, d-xylose, 5-thioglucose, d-glucono-1,5-lactone, maltose and 2-deoxy-d-glucose are also oxidised at relatively high rates. A Ping Pong Bi Bi mechanism was demonstrated for the P2O reaction at pH 8.0, with a catalytic constant (k _cat) of 111.0 s⁻¹ and an affinity constant (K _m) of 1.43 mM for d-glucose and 83.2 μM for oxygen. Whereas the steady-state kinetics for glucose oxidation were unaffected by the medium at pH ≥ 7.0, at low pH both pH and buffer composition affected the P2O kinetics with the k _cat/K _m value decreasing with decreasing pH. The greatest effect was observed in acetate buffer (0.1 M, pH 4.5), where the k _cat decreased to 60.9 s⁻¹ and the K _m increased to 240 mM. The activity of P2O was completely inhibited by 10 mM HgCl₂, AgNO₃ and ZnCl₂, and 50% by lead acetate, CuCl₂ and MnCl₂. Received: 28 August 1996 / Received revision: 25 November 1996 / Accepted: 29 November 1996     

Biotechnological production of <Emphasis Type="SmallCaps">l</Emphasis>-ribose from <Emphasis Type="SmallCaps">l</Emphasis>-arabinose

l-Ribose is a rare and expensive sugar that can be used as a precursor for the production of l-nucleoside analogues, which are used as antiviral drugs. In this work, we describe a novel way of producing l-ribose from the readily available raw material l-arabinose. This was achieved by introducing l-ribose isomerase activity into l-ribulokinase-deficient Escherichia coli UP1110 and Lactobacillus plantarum BPT197 strains. The process for l-ribose production by resting cells was investigated. The initial l-ribose production rates at 39°C and pH 8 were 0.46 ± 0.01 g g⁻¹ h⁻¹ (1.84 ± 0.03 g l⁻¹ h⁻¹) and 0.27 ± 0.01 g g⁻¹ h⁻¹ (1.91 ± 0.1 g l⁻¹ h⁻¹) for E. coli and for L. plantarum, respectively. Conversions were around 20% at their highest in the experiments. Also partially purified protein precipitates having both l-arabinose isomerase and l-ribose isomerase activity were successfully used for converting l-arabinose to l-ribose.     

Actual and potential rates of hydrogen photoproduction by continuous culture of the purple non-sulphur bacterium Rhodobacter capsulatus

The influence of (NH₄)₂SO₄ concentration and dilution rate (D) on actual and potential H₂ photoproduction has been studied in ammonium-limited chemostat cultures of Rhodobacter capsulatus B10. The actual H₂ production in a photobioreactor was maximal (approx. 80 ml h⁻¹l⁻¹) at D = 0.06 h⁻¹ and 4 mM (NH₄)₂SO₄. However, it was lower than the potential H₂ evolution (calculated from hydrogen evolution rates in incubation vials), which amounted to 100–120 ml h⁻¹ l⁻¹ at D = 0.03–0.08 h⁻¹. Taking into account the fact that H₂ production in the photobioreactor under these conditions was not limited by light or lactate, another limiting (inhibiting) factor should be sought. One possibility is an inhibition of H₂ production by the H₂ accumulated in the gas phase. This is apparent from the non-linear kinetics of H₂ evolution in the vials or from its inhibition by the addition of H₂; initial rates were restored in both cases after the vials had been refilled with argon. The actual H₂ production in the photobioreactor at D = 0.06 h⁻¹ was shown to increase from approximately 80 ml h⁻¹ l⁻¹ to approximately 100 ml h⁻¹ l⁻¹ under an argon flow at 100 ml min⁻¹. Under maximal H₂ production rates in the photobioreactor, up to 30% of the lactate feedstock was utilised for H₂ production and 50% for biomass synthesis. Received: 22 April 1997 / Received revision: 14 July 1997 / Accepted: 27 July 1997     

Quasi steady state growth of <Emphasis Type="Italic">Lactococcus lactis</Emphasis> in glucose-limited acceleration stat (A-stat) cultures

Quasi steady state growth of Lactococcus lactis IL 1403 was studied in glucose-limited A-stat cultivation experiments with acceleration rates (a) from 0.003 to 0.06 h⁻² after initial stabilization of the cultures in chemostat at D = 0.2–0.3 h⁻¹. It was shown that the high limit of quasi steady state growth rate depended on the acceleration rate used—at an acceleration rate 0.003 h⁻² the quasi steady state growth was observed until μ _crit = 0.59 h⁻¹, which is also the μ _max value for the culture. Lower values of μ _crit were observed at higher acceleration rates. The steady state growth of bacteria stabilized at dilution rate 0.2 h⁻¹ was immediately disrupted after initiating acceleration at the highest acceleration rate studied—0.06 h⁻². Observation was made that differences [Δ(μ − D)] of the specific growth rates from pre-programmed dilution rates were the lowest using an acceleration rate of 0.003 h⁻² (< 4% of preset changing growth rate). The adaptability of cells to follow preprogrammed growth rate was found to decrease with increasing dilution rate—it was shown that lower acceleration rates should be applied at higher growth rates to maintain the culture in the quasi steady state. The critical specific growth rate and the biomass yields based on glucose consumption were higher if the medium contained S ₀ = 5 g L⁻¹ glucose instead of S ₀ = 10 g L⁻¹. It was assumed that this was due to the inhibitory effect of lactate accumulating at higher concentrations in the latter cultures. Parallel A-stat experiments at the same acceleration and dilution rates showed good reproducibility—Δ(μ − D) was less than 5%, standard deviations of biomass yields per ATP produced (Y _ATP), and biomass yields per glucose consumed (Y _XS) were less than 15%.     

The Impact of Oxygen Tension on Cell Density and Metabolic Diversity of Microbial Communities in Alkane Degrading Continuous-Flow Cultures

Abstract The impact of the dissolved O₂ tension (DOT) and the dilution rate on the metabolic diversity of an autochthonous hexadecane-degrading community in continuous-flow cultures containing hexadecane-coated intertidal sediment was determined in a set of experiments. The DOT was kept constant within each culture at values of 80% (168 μmol O₂L⁻¹) or 0.4% (0.84 μmol O₂ L⁻¹). The dilution rate was increased from D= 0.012 h⁻¹ to D= 0.06 h⁻¹. To determine the culture activity, we analyzed the hexadecane degradation rate, the protein production rate, and the oxygen consumption rate. The cell concentration of different metabolic groups was determined by colony forming units (CFU), and by most probable number (MPN). The metabolic diversity was determined by the substrate utilization spectrum in Biolog GN microtiter plates. The substrate utilization pattern of the cultures decreased considerably as D increased. This effect was more pronounced at 0.4% of DOT than at 80% of DOT. The MPN and CFU revealed that as D increased, only minor changes occurred in the community structure. The hexadecane degradation rate, the protein production rate, and the oxygen consumption rate increased parallel to D independently of the DOT. This means that the biocenosis at 0.4% of DOT was different from the biocenosis at 80% of DOT, although the metabolic activity of the cultures was unaffected by a 200-factor difference in the oxygen tension and revealed a considerable buffer capacity with respect to changes in DOT. Received: 23 May 1998; Accepted: 24 August 1998     

Continuous bio-catalytic conversion of sugar mixture to acetone–butanol–ethanol by immobilized <Emphasis Type="Italic">Clostridium acetobutylicum</Emphasis> DSM 792

Continuous production of acetone, n-butanol, and ethanol (ABE) was carried out using immobilized cells of Clostridium acetobutylicum DSM 792 using glucose and sugar mixture as a substrate. Among various lignocellulosic materials screened as a support matrix, coconut fibers and wood pulp fibers were found to be promising in batch experiments. With a motive of promoting wood-based bio-refinery concept, wood pulp was used as a cell holding material. Glucose and sugar mixture (glucose, mannose, galactose, arabinose, and xylose) comparable to lignocellulose hydrolysate was used as a substrate for continuous production of ABE. We report the best solvent productivity among wild-type strains using column reactor. The maximum total solvent concentration of 14.32 g L⁻¹ was obtained at a dilution rate of 0.22 h⁻¹ with glucose as a substrate compared to 12.64 g L⁻¹ at 0.5 h⁻¹ dilution rate with sugar mixture. The maximum solvent productivity (13.66 g L⁻¹ h⁻¹) was obtained at a dilution rate of 1.9 h⁻¹ with glucose as a substrate whereas solvent productivity (12.14 g L⁻¹ h⁻¹) was obtained at a dilution rate of 1.5 h⁻¹ with sugar mixture. The immobilized column reactor with wood pulp can become an efficient technology to be integrated with existing pulp mills to convert them into wood-based bio-refineries.     

Xylose utilisation by recombinant strains of Saccharomyces cerevisiae on different carbon sources

Autoselective xylose-utilising strains of Saccharomyces cerevisiae expressing the xylose reductase (XYL1) and xylitol dehydrogenase (XYL2) genes of Pichia stipitis were constructed by replacing the chromosomal FUR1 gene with a disrupted fur1::LEU2 allele. Anaerobic fermentations with 80 g l⁻¹ d-xylose as substrate showed a twofold higher consumption of xylose in complex medium compared to defined medium. The xylose consumption rate increased a further threefold when 20 g l⁻¹ d-glucose or raffinose was used as co-substrate together with 50 g l⁻¹ d-xylose. Xylose consumption was higher with raffinose as co-substrate than with glucose (85% versus 71%, respectively) after 82 h fermentations. A high initial ethanol concentration and moderate levels of glycerol and acetic acid accompanied glucose as co-substrate, whereas the ethanol concentration gradually increased with raffinose as co-substrate with no glycerol and much less acetic acid formation. Received: 12 March 1999 / Received revision: 31 June 1999 / Accepted: 5 July 1999     

Hydrogen production with high yield and high evolution rate by self-flocculated cells of Enterobacter aerogenes in a packed-bed reactor

Continuous hydrogen gas evolution by self-flocculated cells of Enterobacter aerogenes, a natural isolate HU-101 and its mutant AY-2, was performed in a packed-bed reactor under glucose-limiting conditions in a minimal medium. The flocs that formed during the continuous culture were retained even when the dilution rate was increased to 0.9 h⁻¹. The H₂ production rate increased linearly with increases in the dilution rate up to 0.67 h⁻¹, giving maximum H₂ production rates of 31 and 58 mmol l⁻¹ h⁻¹ in HU-101 and AY-2 respectively, at a dilution rate of more than 0.67 h⁻¹. The molar H₂ yield from glucose in AY-2 was maintained at about 1.1 at dilution rates between 0.08 h⁻¹ and 0.67 h⁻¹, but it decreased rapidly at dilution rates more than 0.8 h⁻¹. Received: 27 August 1997 / Received revision: 11 November 1997 / Accepted: 14 December 1997     

Anomalies in the growth kinetics of Saccharomyces cerevisiae strains in aerobic chemostat cultures

Aerobic glucose-limited chemostat cultivations were conducted with Saccharomyces cerevisiae strains NRRL Y132, ATCC 4126 and CBS 8066, using a complex medium. At low dilution rates all three strains utilised glucose oxidatively with high biomass yield coefficients, no ethanol production and very low steady-state residual glucose concentrations in the culture. Above a threshold dilution rate, respiro-fermentative (oxido-reductive) metabolism commenced, with simultaneous respiration and fermentation occurring, which is typical of Crabtree-positive yeasts. However, at high dilution rates the three strains responded differently. At high dilution rates S. cerevisiae CBS 8066 produced 7–8 g ethanol L⁻¹ from 20 g glucose L⁻¹ with concomitant low levels of residual glucose, which increased markedly only close to the wash-out dilution rate. By contrast, in the respiro-fermentative region both S. cerevisiae ATCC 4126 and NRRL Y132 produced much lower levels of ethanol (3–4 g L⁻¹) than S. cerevisiae CBS 8066, concomitant with very high residual sugar concentrations, which was a significant deviation from Monod kinetics and appeared to be associated either with high growth rates or with a fermentative (or respiro-fermentative) metabolism. Supplementation of the cultures with inorganic or organic nutrients failed to improve ethanol production or glucose assimilation. Journal of Industrial Microbiology & Biotechnology (2000) 24, 231–236. Received 09 August 1999/ Accepted in revised form 18 December 1999     

Growth and bacteriocin production by Enterococcus faecium DPC1146 in batch and continuous culture

Production of the bacteriocin enterocin 1146 (E1146) by Enterococcus faecium DPC1146 was studied in batch and continuous fermentation. Growth was strongly inhibited by lactic acid. In batch fermentations maximum E1146 activity (2.8 MBU L⁻¹) was obtained in 9 h with 20 g L⁻¹ glucose. Increase in initial glucose concentration did not lead to a proportional increase in E1146 activity. A simple linear model was found to be adequate to explain the relationship between specific bacteriocin production rate and specific growth rate in batch fermentations with initial glucose concentration higher than 20 g L⁻¹. Maximum bacteriocin activity (2.9–3.2 MBU L⁻¹) was obtained in continuous fermentations at dilution rates between 0.12 and 0.17 h⁻¹ and specific bacteriocin production rate increased linearly with dilution rate. Received 31 July 1996/ Accepted in revised form 01 November 1996     

Oxygen starvation induces cell death in Candida shehatae fermentations of d-xylose, but not d-glucose

Candida shehatae cells, cultivated on d-glucose and d-xylose, were subjected to a shift from fully aerobic to anaerobic fermentative conditions. After anaerobic conditions were imposed, growth was limited to approximately one doubling or less as C. shehatae rapidly entered a stationary phase of growth. Following the shift to anoxia, cell viability rapidly declined and the total cell volume declined in the d-xylose fermentations. Moreover, the cell volume distribution shifted to smaller volumes. Cell viability, measured by plate counts, declined nine times faster for d-xylose fermentations than for d-glucose fermentations. Anaerobic growth did not occur on either d-glucose or d-xylose. Selected vitamins and amino acids did not stimulate anaerobic growth in C. shehatae, but did enhance anaerobic growth on d-glucose in S. cerevisiae. The decline in cell viability and lack of anaerobic growth by C. shehatae were attributed to oxygen deficiency and not to ethanol inhibition. The results shed light on why C. shehatae anaerobic fermentations are not currently practical and suggest that research directed towards a biochemical understanding of why C. shehatae can not grow anaerobically will yield significant improvements in ethanol fermentations from d-xylose. Received 26 October 1998 / Received revision: 26 January 1999 / Accepted: 12 February 1999     

Enhanced iturin A production by <Emphasis Type="Italic">Bacillus subtilis</Emphasis> and its effect on suppression of the plant pathogen <Emphasis Type="Italic">Rhizoctonia solani</Emphasis>

The behavior of Streptomyces peucetius var. caesius N47 was studied in a glucose limited chemostat with a complex cultivation medium. The steady-state study yielded the characteristic constants μ _max over 0.10 h⁻¹, Y _XS 0.536 g g⁻¹, and m_S 0.54 mg g⁻¹ h⁻¹. The product of secondary metabolism, ɛ-rhodomycinone, was produced with characteristics Y _PX 12.99 mg g⁻¹ and m _P 1.20 mg g⁻¹ h⁻¹. Significant correlations were found for phosphate and glucose consumption with biomass and ɛ-rhodomycinone production. Metabolic flux analysis was conducted to estimate intracellular fluxes at different dilution rates. TCA, PPP, and shikimate pathway fluxes exhibited bigger values with production than with growth. Environmental perturbation experiments with temperature, airflow, and pH changes on a steady-state chemostat implied that an elevation of pH could be the most effective way to shift the cells from growing to producing, as the pH change induced the biggest transient increase to the calculated ɛ-rhodomycinone flux.     

Production of L-arabitol from L-arabinose by Candida entomaea and Pichia guilliermondii

 Lignocellulosic biomass, particularly corn fiber, represents a renewable resource that is available in sufficient quantities from the corn wet milling industry to serve as a low cost feedstock for production of fuel alcohol and valuable coproducts. Several enzymatic and chemical processes have potential for the conversion of cellulose and hemicellulose to fermentable sugars. The hydrolyzates are generally rich in pentoses (D-xylose and L-arabinose) and D-glucose. Yeasts produce a variety of polyalcohols from pentose and hexose sugars. Many of these sugar alcohols have food applications as low-calorie bulking agents. During the screening of 49 yeast strains capable of growing on L-arabinose, we observed that two strains were superior secretors of L-arabitol as a major extracellular product of L-arabinose. Candida entomaea NRRL Y-7785 and Pichia guilliermondii NRRL Y-2075 produced L-arabitol (0.70 g/g) from L-arabinose (50 g/l) at 34°C and pH 5.0 and 4.0, respectively. Both yeasts produced ethanol (0.32–0.33 g/g) from D-glucose (50 g/l) and only xylitol (0.43–0.51 g/g) from D-xylose (50 g/l). Both strains preferentially utilized D-glucose>D-xylose>L-arabinose from mixed substrate (D-glucose, D-xylose and L-arabinose, 1:1:1, 50 g/l, total) and produced ethanol (0.36–0.38 g/g D-glucose), xylitol (0.02–0.08 g/g D-xylose) and L-arabitol (0.70–0.81 g/g L-arabinose). The yeasts co-utilized D-xylose (6.2–6.5 g/l) and L-arabinose (4.9–5.0 g/l) from corn fiber acid hydrolyzate simultaneously and produced xylitol (0.10 g/g D-xylose) and L-arabitol (0.53–0.54 g/g L-arabinose). Received: 24 April 1995/Received revision: 9 August 1995/Accepted: 7 September 1995     

Enhancement of xylitol productivity and yield using a xylitol dehydrogenase gene-disrupted mutant of Candida tropicalis under fully aerobic conditions

The effects of glycerol and the oxygen transfer rate on the xylitol production rate by a xylitol dehydrogenase gene (XYL2)-disrupted mutant of Candida tropicalis were investigated. The mutant produced xylitol near the almost yield of 100% from d-xylose using glycerol as a co-substrate for cell growth and NADPH regeneration: 50 g d-xylose l⁻¹ was completely converted into xylitol when at least 20 g glycerol l⁻¹ was used as a co-substrate. The xylitol production rate increased with the O₂ transfer rate until saturation and it was not necessary to control the dissolved O₂ tension precisely. Under the optimum conditions, the volumetric productivity and xylitol yield were 3.2 g l⁻¹ h⁻¹ and 97% (w/w), respectively.