Formulation of a protein-free medium based on IPL-41 for the sustained growth of Drosophila melanogaster S2 cells

An animal protein-free medium was developed for Drosophila melanogaster S2 (S2AcGPV2) cells genetically modified to produce the rabies virus G glycoprotein (GPV). IPL-41, used as a basal medium, was supplemented with yeastolate, carbohydrates, amino acids and lipids aiming initially to reduce and further to eliminate the need of fetal bovine serum. The S2AcGPV2 cells were fully capable of growing in serum-free supplemented IPL-41 medium containing 6 g L⁻¹ yeastolate ultrafiltrate, 10 g L⁻¹ glucose, 3.5 g L⁻¹ glutamine, 0.5 g L⁻¹ fructose, 2 g L⁻¹ lactose, 0.6 g L⁻¹ tyrosine, 1.48 g L⁻¹ methionine and 1% (v/v) lipid emulsion, reaching 19 × 10⁶ cells mL⁻¹. Maximum specific growth rate and cell productivity were 0.025 h⁻¹ and 0.57 × 10⁵ cells mL⁻¹ h⁻¹, respectively. Glucose and lactose were consumed during cell culture, but not fructose. Lactate concentration generally decreased during cell culture, while ammonium concentration reached 167 mg L⁻¹, however, without noticeable deleterious effects on cell growth. GPV concentration values achieved were, however, modest in the proposed medium formulation.     

Recombinant protein production in insect cell cultures infected with a temperature-sensitive baculovirus

Spodoptera frugiperda (IPLB-SF-21) insect cells were grown in shake-flasks and infected with a temperature-sensitive baculovirus to express the gene of chloramphenicol acetyl transferase (CAT) in serum-free medium (SF-900) and two serum-supplemented media (IPL-41 and Grace's). In temperature-shift experiments (cell growth at 33°C followed by virus replication at 27°C 3–4 days later), virus and CAT production were much poorer in the serum-free medium than in serum-supplemented media, though cell growth was virtually the same in the different media tested. In all the three media, highest virus and CAT titers were obtained at the lowest MOI (multiplicity of infection 0.02). This result is contrary to that obtained in constant-temperature culture (27°C for both cell growth and virus replication). Virus and CAT production was greatly improved when the entire culture was run at constant temperature. It appeared that infected cells were severely damaged at 33°C (6°C above the optimal 27°C), resulting in little or no virus and protein production. As a result of these temperature-shift experiments, a larger-scale (141 air-lift bioreactor) serum-free culture of Sf-9 insect cells was conducted at constant temperature (27°C) to produce recombinant protein (β-galactosidase). A cell density as high as 1×10⁷ cells.ml⁻¹, and a β-gal concentration of up to 104,000 unit.ml⁻¹ were achieved.     

Obtaining and selection of hexokinases-less strains of <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis> for production of ethanol and fructose from sucrose

Saccharomyces cerevisiae hexokinase-less strains were produced to study the production of ethanol and fructose from sucrose. These strains do not have the hexokinases A and B. Twenty-three double-mutant strains were produced, and then, three were selected for presenting a smaller growth in yeast extract–peptone–fructose. In fermentations with a medium containing sucrose (180.3 g L⁻¹) and with cell recycles, simulating industrial conditions, the capacity of these mutant yeasts in inverting sucrose and fermenting only glucose was well characterized. Besides that, we could also see their great tolerance to the stresses of fermentative recycles, where fructose production (until 90 g L⁻¹) and ethanol production (until 42.3 g L⁻¹) occurred in cycles of 12 h, in which hexokinase-less yeasts performed high growth (51.2% of wet biomass) and viability rates (77% of viable cells) after nine consecutive cycles.     

Characterisation of a novel thermotolerant yeast, Kluyveromyces marxianus var marxianus: development of an ethanol fermentation process

The fermentation characteristics of the novel, thermotolerant, isolate Kluyveromyces marxianus var marxianus were determined to evaluate its aptitude for use in an ethanol production process. Sustainable growth was not observed under anaerobic conditions, even in the presence of unsaturated fatty acid and sterol. A maximum ethanol concentration of 40 g L⁻¹ was produced at 45°C, with an initial specific ethanol production rate of 1.7 g g⁻¹ h⁻¹. This was observed at ethanol concentrations below 8 g L⁻¹ and under oxygen-limited conditions. The low ethanol tolerance and low growth under oxygen-limited conditions required for ethanol production implied that a simple continuous process was not feasible with this yeast strain. Improved productivity was achieved through recycling biomass into the fermenter, indicating that utilising an effective cell retention method such as cell recycle or immobilisation, could lead to the development of a viable industrial process using this novel yeast strain. Received 14 February 1998/ Accepted in revised form 19 May 1998     

Analysis and optimization of a two-substrate fermentation for xylitol production using Candida tropicalis

Xylitol, a functional sweetener, was produced from xylose using Candida tropicalisATCC 13803. A two-substrate fermentation was designed in order to increase xylitol yield and volumetric productivity. Glucose was used initially for cell growth followed by conversion of xylose to xylitol without cell growth and by-product formation after complete depletion of glucose. High glucose concentrations increased volumetric productivity by reducing conversion time due to high cell mass, but also led to production of ethanol, which, in turn, inhibited cell growth and xylitol production. Computer simulation was undertaken to optimize an initial glucose concentration using kinetic equations describing rates of cell growth and xylose bioconversion as a function of ethanol concentration. Kinetic constants involved in the equations were estimated from the experimental results. Glucose at 32 g L⁻¹ was estimated to be an optimum initial glucose concentration with a final xylose concentration of 86 g L⁻¹ and a volumetric productivity of 5.15 g-xylitol L⁻¹ h⁻¹. The two-substrate fermentation was performed under optimum conditions to verify the computer simulation results. The experimental results were in good agreement with the predicted values of simulation with a xylitol yield of 0.81 g-xylitol g-xylose⁻¹ and a volumetric productivity of 5.06 g-xylitol L⁻¹ h⁻¹. Received 16 June 1998/ Accepted in revised form 28 February 1999     

Very high ethanol productivity in an innovative continuous two-stage bioreactor with cell recycle

The performance of an innovative two-stage continuous bioreactor with cell recycle—potentially capable of giving very high ethanol productivity—was investigated. The first stage was dedicated to cell growth, whereas the second stage was dedicated to ethanol production. A high cell density was obtained by an ultrafiltration module coupled to the outlet of the second reactor. A recycle loop from the second stage to the first one was tested to improve cell viability and activity. Cultivations of Saccharomyces cerevisiae in mineral medium on glucose were performed at 30°C and pH 4. At steady state, total biomass concentrations of 59 and 157 gDCW l⁻¹ and ethanol concentrations of 31 and 65 g l⁻¹ were obtained in the first and second stage, respectively. The residual glucose concentration was 73 g l⁻¹ in the first stage and close to zero in the second stage. The present study shows that a very high ethanol productivity (up to 41 g l⁻¹ h⁻¹) can indeed be obtained with complete conversion of the glucose and with a high ethanol titre (8.3°GL) in the two-stage system.     

Use of sugarcane molasses “B” as an alternative for ethanol production with wild-type yeast <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis> ITV-01 at high sugar concentrations

Molasses “B” is a rich co-product of the sugarcane process. It is obtained from the second step of crystallization and is richer in fermentable sugars (50–65%) than the final molasses, with a lower non-sugar solid content (18–33%); this co-product also contains good vitamin and mineral levels. The use of molasses “B” for ethanol production could be a good option for the sugarcane industry when cane sugar prices diminish in the market. In a complex medium like molasses, osmotolerance is a desirable characteristic for ethanol producing strains. The aim of this work was to evaluate the use of molasses “B” for ethanol production using Saccharomyces cerevisiae ITV-01 (a wild-type yeast isolated from sugarcane molasses) using different initial sugar concentrations (70–291 g L⁻¹), two inoculum sizes and the addition of nutrients such as yeast extract, urea, and ammonium sulphate to the culture medium. The results obtained showed that the strain was able to grow at 291 g L⁻¹ total sugars in molasses “B” medium; the addition of nutrients to the culture medium did not produce a statistically significant difference. This yeast exhibits high osmotolerance in this medium, producing high ethanol yields (0.41 g g⁻¹). The best conditions for ethanol production were 220 g L⁻¹ initial total sugars in molasses “B” medium, pH 5.5, using an inoculum size of 6 × 10⁶ cell mL⁻¹; ethanol production was 85 g L⁻¹, productivity 3.8 g L⁻¹ h⁻¹ with 90% preserved cell viability.     

Increase of ethanol productivity by cell-recycle fermentation of flocculating yeast

Using the recombinant flocculating Angel yeast F6, long-term repeated batch fermentation for ethanol production was performed and a high volumetric productivity resulted from half cells not washed and the optimum opportunity of residual glucose 20 g l⁻¹ of last medium. The obtained highest productivity was 2.07 g l⁻¹ h⁻¹, which was improved by 75.4% compared with that of 1.18 g l⁻¹ h⁻¹ in the first batch fermentation. The ethanol concentration reached 8.4% corresponding to the yield of 0.46 g g⁻¹. These results will contribute greatly to the industrial production of fuel ethanol using the commercial method with the flocculating yeast.     

Butanol production from wheat straw hydrolysate using <Emphasis Type="Italic">Clostridium beijerinckii</Emphasis>

In these studies, butanol (acetone butanol ethanol or ABE) was produced from wheat straw hydrolysate (WSH) in batch cultures using Clostridium beijerinckii P260. In control fermentation 48.9 g L⁻¹ glucose (initial sugar 62.0 g L⁻¹) was used to produce 20.1 g L⁻¹ ABE with a productivity and yield of 0.28 g L⁻¹ h⁻¹ and 0.41, respectively. In a similar experiment where WSH (60.2 g L⁻¹ total sugars obtained from hydrolysis of 86 g L⁻¹ wheat straw) was used, the culture produced 25.0 g L⁻¹ ABE with a productivity and yield of 0.60 g L⁻¹ h⁻¹ and 0.42, respectively. These results are superior to the control experiment and productivity was improved by 214%. When WSH was supplemented with 35 g L⁻¹ glucose, a reactor productivity was improved to 0.63 g L⁻¹ h⁻¹ with a yield of 0.42. In this case, ABE concentration in the broth was 28.2 g L⁻¹. When WSH was supplemented with 60 g L⁻¹ glucose, the resultant medium containing 128.3 g L⁻¹ sugars was successfully fermented (due to product removal) to produce 47.6 g L⁻¹ ABE, and the culture utilized all the sugars (glucose, xylose, arabinose, galactose, and mannose). These results demonstrate that C. beijerinckii P260 has excellent capacity to convert biomass derived sugars to solvents and can produce over 28 g L⁻¹ (in one case 41.7 g L⁻¹ from glucose) ABE from WSH. Medium containing 250 g L⁻¹ glucose resulted in no growth and no ABE production. Mixtures containing WSH + 140 g L⁻¹ glucose (total sugar approximately 200 g L⁻¹) showed poor growth and poor ABE production. Mention of trade names or commercial products in this article is solely for the purpose of providing scientific information and does not imply recommendation or endorsement by the United States Department of Agriculture.     

Production and characterisation of a biosurfactant isolated from Pseudomonas aeruginosa UW-1

Pseudomonas aeruginosa UW-1 produced 17–24 g L⁻¹ rhamnolipid in vegetable oil-containing media in shake flask cultures in 13 days. In time course studies of growth and rhamnolipid production in a salts medium containing 6% canola oil, total bacterial count reached 2.6 × 10¹⁰ CFU ml⁻¹ after 48 h and a maximum rhamnolipid yield of 24.3 g L⁻¹ was obtained after 9 days. Rhamnolipid components were purified and separated by chloroform-methanol extraction and TLC chromatography. The major rhamnolipid components were characterised as L-rhamnosyl-β-hydroxydecanoyl-β-hydroxydecanoate and L-rhamnosyl-L-rhamnosyl-β-hydroxydecanoyl-β-hydroxydecanoate by nuclear magnetic resonance and mass spectrometry. The components were separated preparatively by silica gel column chromatography. The recovered monorhamnosyl fraction contained no dirhamnosyl moiety while the recovered dirhamnosyl fraction contained 5% of the monorhamnosyl moiety when analyzed by HPLC. The ratio of mono- to dirhamnosyl components produced by P. aeruginosa UW-1 was determined by HPLC to be 4 : 1 by weight. Purified mono- and dirhamnosyl components had the same CMC value of 40 μg ml⁻¹ and decreased the surface tension of water to 27.7 and 30.4 dynes cm⁻¹, respectively. Received 04 April 1997/ Accepted in revised form 15 July 1997     

Efficient and rapid plant regeneration of oil palm zygotic embryos cv. ‘Tenera’ through somatic embryogenesis

An efficient and rapid plant regeneration system through somatic embryogenesis was developed using 13-week-old zygotic embryos of oil palm (Elaeis guineensis Jacq.) cv. ‘Tenera’. Zygotic embryos were cultured on MS and N6 media supplemented with 2.0 mg L⁻¹ picloram, 2,4-D and dicamba. The highest embryogenic callus formation (32%) was observed on N6 medium with 2,4-D after 3 month culture on callus induction medium. Somatic embryos were continuously formed from nodular calli on embryo maturation medium [N6 + 0.1 mg L⁻¹ 2,4-D, 0.16 g L⁻¹ putrescine, 0.5 g L⁻¹ casein amino acids and 2.0 g L⁻¹ activated charcoal(AC)] for 3–5 months. Histological analysis confirmed that embryo development occurred via somatic embryogenesis. For plant regeneration, modified N6 medium (MN6) with AC (0.5 g L⁻¹) without growth regulators, induced both shoot and root formation simultaneously with the highest regeneration rate of 56%. This combined shoot and root induction protocol shortened the culture time to 9–12 months. Furthermore, after acclimatization, more than 85% of transferred plants from our protocol developed successfully in the soil.     

Effects of salinity on cell growth and docosahexaenoic acid content of the heterotrophic marine microalga Crypthecodinium cohnii

The effects of salinity on cell growth and docosahexaenoic acid (DHA) content of three marine microalgal strains, Crythecodinium cohnii ATCC 30556, C. cohnii ATCC 50051 and C. cohnii RJH were investigated. The lag phases of the three strains increased with increasing salinity in Porphyridium medium. The specific growth rate of C. cohnii ATCC 30556 was the highest at 9 g L⁻¹ NaCl while the other two strains had their highest specific growth rates at 5 g L⁻¹ NaCl. The highest cell dry weight concentrations of 2.51 g L⁻¹ and 1.56 g L⁻¹ were achieved at 9 g L⁻¹ NaCl for C. cohnii ATCC 30556 and ATCC 50051, respectively, while the highest dry weight concentration of 2.49 g L⁻¹ was achieved at 5 g L⁻¹ NaCl for C. cohnii RJH. The highest cell growth yield coefficient on glucose was 0.5 g g⁻¹ for both C. cohnii ATCC 30556 and C. cohnii RJH and 0.45 g g⁻¹ for C. cohnii ATCC 50051. All three strains responded to the change of salinity by modifying their cellular fatty acid compositions. At 9 g L⁻¹ NaCl, C. cohnii ATCC 30556 had the highest total fatty acid content and DHA (C22:6) proportion. In contrast, C. cohnii ATCC 50051 and C. cohnii RJH had the highest DHA content at 5 g L⁻¹ NaCl. C. cohnii ATCC 30556 and ATCC 50051 had the highest DHA yield (131.55 and 68.24 mg L⁻¹ respectively) at 9 g L⁻¹ NaCl while C. cohnii RJH had the highest DHA yield (128.83 mg L⁻¹) at 5 g L⁻¹ NaCl. Received 27 May 1999/ Accepted in revised form 27 August 1999     

Ethanol adaptation in a thermotolerant yeast strain Kluyveromyces marxianus IMB3

The maximum ethanol concentration produced from glucose in defined media at 45°C by the thermotolerant yeast Kluyveromyces marxianus IMB3 was 44 g L⁻¹. Acclimatisation of the strain through continuous culture at ethanol concentrations up to 80 g L⁻¹, shifted the maximum ethanol concentration at which growth was observed from 40 g L⁻¹ to 70 g L⁻¹. Four isolates were selected from the continuous culture, only one of which produced a significant increase in final ethanol concentration (50 ± 0.4 g L⁻¹), however in subsequent fermentations, following storage on nutrient agar plates, the maximum ethanol concentration was comparable with the original isolate. The maximum specific ethanol production rates (approximately 1.5 g (gh)⁻¹) were also comparable with the original strain except for one isolate (0.7 g (gh)⁻¹). The specific ethanol productivity decreased with ethanol concentration; this decrease correlated linearly (rval 0.92) with cell viability. Due to the transience of induced ethanol tolerance in the strain it was concluded that this was not a valid method for improving final ethanol concentrations or production rates. Received 18 July 1997/ Accepted in revised form 19 February 1998     

Construction of the industrial ethanol-producing strain of Saccharomyces cerevisiae able to ferment cellobiose and melibiose

The gene mel1, encoding α-galactosidase in Schizosaccharomyces pombe, and the gene bgl2, encoding and α-glucosidase in Trichoderma reesei, were isolated and co-expressed in the industrial ethanolproducing strain of Saccharomyces cerevisiae. The resulting strains were able to grow on cellobiose and melibiose through simultaneous production of sufficient extracellular α-galactosidase and β-glucosidase activity. Under aerobic conditions, the growth rate of the recombinant strain GC1 co-expressing 2 genes could achieve 0.29 OD600 h⁻¹ and a biomass yield up to 7.8 g l⁻¹ dry cell weight on medium containing 10.0 g l⁻¹ cellobiose and 10.0 g l⁻¹ melibiose as sole carbohydrate source. Meanwhile, the new strain of S. cerevisiae CG1 demonstrated the ability to directly produce ethanol from microcrystalline cellulose during simultaneous saccharification and fermentation process. Approximately 36.5 g l⁻¹ ethanol was produced from 100 g of cellulose supplied with 5 g l⁻¹ melibose within 60 h. The yield (g of ethanol produced/g of carbohydrate consumed) was 0.44 g/g, which corresponds to 88.0% of the theoretical yield.     

Development of a cost-effective glucose-corn steep medium for production of butanol by Clostridium beijerinckii

Corn steep water (CSW) medium (1.6% solids plus 6% glucose) was evaluated for growth and butanol production by Clostridium beijerinckii NCIMB 8052 wild-type and hyper-amylolytic, hyper-butanol-producing mutant strain BA101. CSW alone was not a suitable substrate, whereas addition of glucose supported growth and butanol production by both strains. In a batch-scale fermentation using an optimized 6% glucose-1.6% solids CSW medium, C. beijerinckii NCIMB 8052 and strain BA101 produced 10.7 g L⁻¹ and 14.5 g L⁻¹ of butanol, respectively. The total solvents (acetone, butanol, and ethanol) produced by C. beijerinckii NCIMB 8052 and strain BA101 were 14 g L⁻¹ and 20 g L⁻¹, respectively. Initial fermentation in small-scale flasks containing 6% maltodextrin-1.6% solids concentration CSW medium resulted in 6 g L⁻¹ and 12.6 g L⁻¹ of butanol production by C. beijerinckii NCIMB 8052 and strain BA101, respectively. CSW can serve as an economic source of nitrogen, vitamins, amino acids, minerals, and other nutrients. Thus, it is feasible to use 6% glucose-1.6% solids CSW medium in place of semi-defined P2 medium. Received 9 February 1998/ Accepted in revised form 1 September 1998     

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     

Characterization of growth and Oryctes rhinoceros nudivirus production in attached cultures of the DSIR-HA-1179 coleopteran insect cell line

The DSIR-HA-1179 coleopteran cell line is a susceptible and permissive host to the Oryctesrhinoceros nudivirus (OrNV), which has been used as a biocontrol agent against the coconut rhinoceros beetle (Oryctes rhinoceros); a pest of palms in the Asia-Pacific region. However, little is known about growth and metabolism of this cell line, knowledge of which is necessary to develop an in vitro large-scale OrNV production process. The strong anchorage-dependent characteristics of the cell line, its particular fragility and its tendency to form dense clumps when manipulated, are the most likely reasons that have precluded further development of the cell line. In order to characterize DSIR-HA-1179 cells, there was first a need for a reliable technique to count the cells. A homogenous cell suspension suitable for enumeration could be produced by treatment with TrypLE Express™ with optimum mean time for cell release calculated as 30 min. The cell line was adapted to grow in four serum-supplemented culture media namely TC-100, IPL-41, Sf-900 II and Sf-900 III and cell growth, glucose consumption, lactate and ammonia production were assessed from static-batch cultures. The maximum viable cell density was reached in Sf-900 II (17.9 × 10⁵ cells/ml), with the maximum specific growth rate observed in this culture medium as well (0.0074 h⁻¹). Higher production of OrNV was observed in IPL-41 and TC-100 (4.1 × 10⁷ TCID₅₀/ml) than in cultures infected in Sf-900 III (2.0 × 10⁷ TCID₅₀/ml) and Sf-900 II (1.4 × 10⁷ TCID₅₀/ml). At the end of the growth period, glucose was completely consumed in cultures grown in TC-100, while remained in excess in the other three culture media. The cell line produced lactate and ammonia to very low levels in the TC-100 culture medium which is a promising aspect for its cultivation at large-scale.     

Production of recombinant herpes simplex virus protease in 10-L stirred vessels using a baculovirus–insect cell expression system

A gene expression system using recombinant Autographa californica nuclear polyhedrosis virus (baculovirus) and Sf-9 cells has been scaled up to the 10-L tank level and shown to be capable of producing herpes simplex virus (HSV) protease in serum-free media. High densities of Spodoptera frugiperda (Sf-9) cells were achieved by modifying two 10-L Biolafitte fermenters specifically for insect cell growth. The existing Rushton impellers were replaced by marine impellers to reduce shear and the aeration system was modified to allow external addition of air/O₂ mixtures at low flow rates through either the sparge line or into the head space of the fermenter. To inoculate the tanks, Sf-9 cells were adapted to grow to high cell densities (6–10 × 10⁶ cells ml⁻¹) in shake flasks in serum-free media. With these procedures, cell densities of 5 × 10⁶ cells ml⁻¹ were routinely achieved in the 10-L tanks. These cells were readily infected with recombinant baculovirus expressing the 247-amino acid catalytic domain of the HSV-1 strain 17 protease UL26 gene as a glutathione-S-transferase (GST) fusion protein (GST-247). Three days after infection at a multiplicity of infection (MOI) of 3 pfu cell⁻¹, the GST-247 fusion protein was purified from a cytoplasmic lysate by Glutathione Sepharose 4-B affinity chromatography with reproducible yields of 11–38 mg L⁻¹ of recombinant protein and ≥ 90% purity. Maximum production of this protein was observed at a cell density of 5.0 × 10⁶ cells ml⁻¹. Received 09 December 1996/ Accepted in revised form 13 April 1997     

Alcoholic fermentation of xylose and mixed sugars using recombinant <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis> engineered for xylose utilization

Previously, a Saccharomyces cerevisiae strain was engineered for xylose assimilation by the constitutive overexpression of the Orpinomyces xylose isomerase, the S. cerevisiae xylulokinase, and the Pichia stipitis SUT1 sugar transporter genes. The recombinant strain exhibited growth on xylose, under aerobic conditions, with a specific growth rate of 0.025 h⁻¹, while ethanol production from xylose was achieved anaerobically. In the present study, the developed recombinant yeast was adapted for enhanced growth on xylose by serial transfer in xylose-containing minimal medium under aerobic conditions. After repeated batch cultivations, a strain was isolated which grew with a specific growth rate of 0.133 h⁻¹. The adapted strain could ferment 20 g l⁻¹ of xylose to ethanol with a yield of 0.37 g g⁻¹ and production rate of 0.026 g l⁻¹ h⁻¹. Raising the fermentation temperature from 30°C to 35°C resulted in a substantial increase in the ethanol yield (0.43 g g⁻¹) and production rate (0.07 g l⁻¹ h⁻¹) as well as a significant reduction in the xylitol yield. By the addition of a sugar complexing agent, such as sodium tetraborate, significant improvement in ethanol production and reduction in xylitol accumulation was achieved. Furthermore, ethanol production from xylose and a mixture of glucose and xylose was also demonstrated in complex medium containing yeast extract, peptone, and borate with a considerably high yield of 0.48 g g⁻¹.     

Ethanol production by Saccharomyces cerevisiae in biofilm reactors

Biofilms are natural forms of cell immobilization in which microorganisms attach to solid supports. At ISU, we have developed plastic composite-supports (PCS) (agricultural material (soybean hulls or oat hulls), complex nutrients, and polypropylene) which stimulate biofilm formation and which supply nutrients to the attached microorganisms. Various PCS blends were initially evaluated in repeated-batch culture-tube fermentation with Saccharomyces cerevisiae (ATCC 24859) in low organic nitrogen medium. The selected PCS (40% soybean hull, 5% soybean flour, 5% yeast extract-salt and 50% polypropylene) was then used in continuous and repeated-batch fermentation in various media containing lowered nitrogen content with selected PCS. During continuous fermentation, S. cerevisiae demonstrated two to 10 times higher ethanol production in PCS bioreactors than polypropylene-alone support (PPS) control. S. cerevisiae produced 30 g L⁻¹ ethanol on PCS with ammonium sulfate medium in repeated batch fermentation, whereas PPS-control produced 5 g L⁻¹ ethanol. Overall, increased productivity in low cost medium can be achieved beyond conventional fermentations using this novel bioreactor design. Received 20 May 1997/ Accepted in revised form 29 August 1997