High-Efficiency Carbohydrate Fermentation to Ethanol at Temperatures above 40 degrees C by Kluyveromyces marxianus var. marxianus Isolated from Sugar Mills

A number of yeast strains, isolated from sugar cane mills and identified as strains of Kluyveromyces marxianus var. marxianus, were examined for their ability to ferment glucose and cane syrup to ethanol at high temperatures. Several strains were capable of rapid fermentation at temperatures up to 47 degrees C. At 43 degrees C, >6% (wt/vol) ethanol was produced after 12 to 14 h of fermentation, concurrent with retention of high cell viability (>80%). Although the type strain (CBS 712) of K. marxianus var. marxianus produced up to 6% (wt/vol) ethanol at 43 degrees C, cell viability was low, 30 to 50%, and the fermentation time was 24 to 30 h. On the basis of currently available strains, we suggest that it may be possible by genetic engineering to construct yeasts capable of fermenting carbohydrates at temperatures close to 50 degrees C to produce 10 to 15% (wt/vol) ethanol in 12 to 18 h with retention of cell viability.     

High-Efficiency Carbohydrate Fermentation to Ethanol at Temperatures above 40°C by Kluyveromyces marxianus var. marxianus Isolated from Sugar Mills

A number of yeast strains, isolated from sugar cane mills and identified as strains of Kluyveromyces marxianus var. marxianus, were examined for their ability to ferment glucose and cane syrup to ethanol at high temperatures. Several strains were capable of rapid fermentation at temperatures up to 47°C. At 43°C, >6% (wt/vol) ethanol was produced after 12 to 14 h of fermentation, concurrent with retention of high cell viability (>80%). Although the type strain (CBS 712) of K. marxianus var. marxianus produced up to 6% (wt/vol) ethanol at 43°C, cell viability was low, 30 to 50%, and the fermentation time was 24 to 30 h. On the basis of currently available strains, we suggest that it may be possible by genetic engineering to construct yeasts capable of fermenting carbohydrates at temperatures close to 50°C to produce 10 to 15% (wt/vol) ethanol in 12 to 18 h with retention of cell viability.     

Simultaneous fermentation and isomerization of xylose

Summary Ethanol was produced from xylose by converting the sugar to xylulose, using commercial xylose isomerases, and simultaneously converting the xylulose to ethanol by anaerobic fermentation using different yeast strains. The process was optimized with the yeast strain Schizosaccharomyces pombe (Y-164). The data show that the simultaneous fermentation and isomerization of 6% xylose can produce final ethanol concentrations of 2.1% w/v within 2 days at temperatures as high as 39°C.Nomenclature SFIX simultaneous fermentation and isomerization of xylose - V _p volumetric production (g ethanol·l^-1 per hour) - Q _p specific rate (g ethanol·g^-1 cells per hour) - Y _s yield from substrate consumed (g ethanol, g^-1 xylose) - ET ethanol concentration (% wt/vol) - XT xylitol concentration (% wt/vol) - Glu glucose - Xyl xylose - --m maximum - --f final     

Production of high concentrations of ethanol from inulin by simultaneous saccharification and fermentation using Aspergillus niger and Saccharomyces cerevisiae.

Pure nonhydrolyzed inulin was directly converted to ethanol in a simultaneous saccharification and fermentation process. An inulinase-hyperproducing mutant, Aspergillus niger 817, was grown in a submerged culture at 30 degrees C for 5 days. The inulin-digestive liquid culture (150 ml) was supplemented with 45 g of inulin, 0.45 g of (NH4)2SO4, and 0.15 g of KH2PO4. The medium (pH 5.0) was inoculated with an ethanol-tolerant strain, Saccharomyces cerevisiae 1200, and fermentation was conducted at 30 degrees C. An additional 20 g of inulin was added to the culture after 15 h of fermentation. S. cerevisiae 1200 utilized 99% of the 65 g of inulin during the fermentation, and produced 20.4 and 21.0% (vol/vol) ethanol from chicory and dahlia inulins, respectively, within 3 days of fermentation. The maximum volumetric productivities of ethanol were 6.2 and 6.0 g/liter/h for chicory and dahlia inulins, respectively. The conversion efficiency of inulin to ethanol was 83 to 84% of the theoretical ethanol yield.     

Effects of particulate materials and osmoprotectants on very-high-gravity ethanolic fermentation by Saccharomyces cerevisiae.

The effects of osmoprotectants (such as glycine betaine and proline) and particulate materials on the fermentation of very high concentrations of glucose by the brewing strain Saccharomyces cerevisiae (uvarum) NCYC 1324 were studied. The yeast growing at 20 degrees C consumed only 15 g of the sugar per 100 ml from a minimal medium which initially contained 35% (wt/vol) glucose. Supplementing the medium with a mixture of glycine betaine, glycine, and proline increased the amount of sugar fermented to 30.5 g/100 ml. With such supplementation, the viability of the yeast cells was maintained above 80% throughout the fermentation, while it dropped to less than 12% in the unsupplemented controls. Among single additives, glycine was more effective than proline or glycine betaine. On incubating the cultures for 10 days, the viability decreased to only 55% with glycine, while it dropped to 36 and 27%, respectively, with glycine betaine and proline. It is suggested that glycine and proline, known to be poor nitrogen sources for growth, may serve directly or indirectly as osmoprotectants. Nutrients such as tryptone, yeast extract, and a mixture of purine and pyrimidine bases increased the sugar uptake and ethanol production but did not allow the population to maintain the high level of cell viability. While only 43% of the sugar was fermented in unsupplemented medium, the presence of particulate materials such as wheat bran, wheat mash insolubles, alumina, and soy flour increased sugar utilization to 68, 75, 81, and 82%, respectively.     

溶氧对Candida glycerinogenes产甘油发酵过程的影响

研究了溶氧浓度对产甘油假丝酵母分批发酵生产甘油过程的影响。实验结果表明：当溶氧浓度控制在30%时,C. glycerinogenes的甘油产量、得率和产率达到最高,分别为120.7 g/L、0.575 g/g和1.69 g/(L•h),而糖酵解代谢副产物形成最少。当溶氧浓度为10%时,发酵过程呈现出“巴斯德效应”的特征,生成的酵解代谢副产物维持在较高水平。在快速生长阶段,随着溶氧从10%增加到60%,细胞呼吸类型表现为从厌氧呼吸向好氧呼吸转变,酵解代谢副产物依次减少。在生长稳定期,控制的溶氧浓度越高,酵解代谢副产物乙醇、乙酸等的生成减少。分别选用Logistic方程、Luedeking-Piret方程和Luedeking-Piret-like方程,能较好地模拟细胞生长、甘油合成和葡萄糖消耗的动力学过程。     

Continuous ethanol production by immobilized yeast reactor coupled with membrane pervaporation unit

A system comprised of an immobilized yeast reactor producing ethanol, with a membrane pervaporation module for continuously removing and concentrating the produced ethanol, was developed. The combined system consisted of two integrated circulation loops: In one the sugar-containing medium is circulated through the membrane pervaporation module. The two loops were interconnected in a way allowing for separate parameter optimization (e.g., flow rate, temperature, pH) for each loop.The fermentation unit was 2.0 L bioreactor with five equal segments, packed with 5-mm beads of immobilized yeasts. The bead matrix was a crosslinked polyacrylamide hydrazide gel coated with calcium alginate. The fast circulation loop of the bioreactor allowed for efficient liberation of CO(2) at the top of the immobilized yeast reactor. Continuous operation of the uncoupled reactor for over 50 days with inflowing defined medium or dilute molasses at a residence time of 1.25 h yielded ethanol at a rate of about 10 g/L h.The pervaporation unit was constructed from four 60-cm-long tubular membranes of silicone composite on a polysulfone support. The output from the fermentor was circulated through the inside of the tubes of a unit with a total surface area of 800 cm(2), having an average flux of 150 mL/h, and selectivities to ethanol vs. water up to 7. A vacuum of 30 mb was applied to the outside of the tubes, removing 20-30 g of ethanol per hour, which was collected in condensors. The continuous removal of ethanol, avoiding inhibition of the fermentation process, resulted in an improved productivity and allowed the use of high sugar concentrations (40% wt/vol) offering the potential of a compact system with reduced stillage.The combined system of ethanol production and removal enabled an operative steady state at which the liquid volume of the system, and the concentrations of ethanol within the reactor ( 4% wt/vol), as well as within the flux crossing the pervaporation membrane (17%-20% wt/vol) were kept constant. At the steady state, a 40% wt/vol sugar solution could be continuously added to the fermentor when 12%-20% wt/vol clear ethanol solution was continuously removed by the pervaporation unit. Membrane fouling was reversed by short washing steps, and continuous step operation was maintained by working with two different modules that were interchanged. In this manner, long term continuous operation (over 40 days) was achieved with a productivity of 20-30 g/L h, representing over a twofold increase relative to the continuously operated reactor uncoupled from the membrane and a fivefold increase in comparison with the value obtained fro a corresponding batch fermentation.     

Influence of Dissolved Oxygen Levels on Production of l-Asparaginase and Prodigiosin by Serratia marcescens

The effect of dissolved oxygen concentrations on the behavior of Serratia marcescens and on yields of asparaginase and prodigiosin produced in shaken cultures and in a 55-liter stainless-steel fermentor was studied. A range of oxygen transfer rates was obtained in 500-ml Erlenmeyer flasks by using internal, stainless-steel baffles and by varying the volume of medium per flask, and in the fermentor by high speed agitation (375 rev/min) or low rates of aeration (1.5 volumes of air per volume of broth per min), or both. Dissolved oxygen levels in the fermentation medium were measured with a membrane-type electrode. Peak yields of asparaginase were obtained in unbaffled flasks (3.0 to 3.8 IU/ml) and in the fermentor (2.7 IU/ml) when the level of dissolved oxygen in the culture medium reached zero. A low rate of oxygen transfer was accomplished by limited aeration. Production of prodigiosin required a supply of dissolved oxygen that was obtainable in baffled flasks with a high rate of oxygen transfer and in the fermentor with a combination of high-speed agitation and low-rate aeration. The fermentation proceeded at a more rapid rate and changes in pH and cell populations were accelerated by maintaining high levels of dissolved oxygen in the growth medium.     

Indonesian tapé ketan fermentation

Indonesian tapé ketan is a fermentation in which a mold, Amylomyces rouxii Calmette (Chlamydomucor oryzae Went and Prinsen Geerligs), in combination with one or more yeasts such as Endomycopsis burtonii converts steamed rice to a sweet-sour, slightly alcoholic paste. A study was made to determine the biochemical changes that occur in the substrate during fermentation. It was found that the product was ready for consumption after fermentation at 30 degrees C for 36 to 48 h. A. rouxii used about 30% of the total rice solids, resulting in a crude protein of 12% in 96 h, whereas the combination of the mold with E. burtonii reduced total solids by 50% in 192 h, causing crude protein to increase to 16.5%. Soluble solids increased from 5 to about 67% in 36 h and decreased to 12% at 192 h with A. rouxii alone, whereas soluble solids fell to about 8% at 192 h in the fermentation with both the mold and the yeast. The mold, by itself, reduced the starch content of the rice from 78 to 10% in 48 h and to less than 2% in 144 h. The mold plus yeast reduced the starch content to about 18% in 48 h; however the "starch" content did not fall below 6% even at 192 h, presumably because the yeast was producing glycogen, which was determined along with the residual starch. With both the mold and the mold plus yeast fermentations, reducing sugars increased from less than 1% to approximately 5% in 24 h and reached maximum concentration, 16 to 17%, between 36 and 48 h. A. rouxii by itself produced a maximum of about 5.6% (vol/vol) ethanol at 96 h. The highest concentration of ethanol (8%, vol/vol) was produced by the mold plus E. burtonii at 144 h. The mold by itself reduced the starting pH from 6.3 to about 4.0 in 48 h. The combination of the mold and yeast reduced the pH to 4.1 in 144 h. The mold increased total acidity to approximately 6.2 meq of H per 100 ml, and the combination of the mold and yeast increased the total acidity to 7.8 meq of H per 100 ml in 192 h. At 48 h there was practically no difference in the volatile acidity (0.20) for the combined fermentation compared with 0.26 meq of H per 100 ml for the mold fermentation. The mold and at least one species of yeast were required to develop the rich aroma and flavor of typical Indonesian tapé.     

Ethanol from Sugar Cane: Flask Experiments Using the EX-FERM Technique

Alcohol production at the laboratory scale from sugar cane pieces by the EX-FERM technique was studied with 37 strains of Saccharomyces spp. The EX-FERM process is novel in that it employs the simultaneous extraction and fermentation of the sucrose in a cane-water suspension. Two types of cane treatments were used: chips and shredded pith, either fresh or dried. A mother culture of the yeast was prepared in enriched cane juice and then added to the cane-water mixture. After static fermentation for 40 h at 30°C, the cane was removed, and fresh cane was added to the yeast-alcohol broth. After an additional 24 h, the cane was again removed and the liquor was analyzed. After the first 40-h cycle, sugar consumption was above 99% with 10 of the 37 yeast strains tested, and ethanol reached levels of 1.29 to 4.00 g per 100 ml, depending on the yeast strain. The final ethanol concentration reached 4.27 to 5.37 g per 100 ml, and sugar consumption was above 98% in three cases during a second EX-FERM cycle employing previously air-dried chips and pith. Product yields were within accepted values. Cane treatment did not appear to affect the results at this level.     

Production of ethanol from guava pulp by yeast strains

Guava pulp used for ethanol production by three yeast strains contained 10% (w/v) total sugars and was pH 4.1. Ethanol production at the optimum sugar concentration of 10%, at pH 4.1 and 30°C was 1.5%, 3.6% and 3.9% (w/v) by Saccharomyces cerevisiae MTCC 1972, Isolate-1 and Isolate-2, respectively, at 60 h fermentation. Higher sugar concentrations at 15 and 20% were inhibitory for ethanol production by all test cultures. The maximum production of ethanol at optimum natural sugar concentration (10%) of guava pulp, was 5.8% (w/v) at pH 5.0 by Isolate-2 over 36 h fermentation, which was only slightly more than the quantity of ethanol produced by Saccharomyces cerevisiae (5.0%) and Isolate-1 (5.3%) over 36 and 60h fermentation, respectively.     

Growth, death, and oxygen uptake kinetics of Pichia stipitis on xylose

Pichia stipitis NRRL Y-7124 has potential application in the fermentation of xylose-rich waste streams, produced by wood hydrolysis. Kinetic models of cell growth, death, and oxygen uptake were investigated in batch and oxygen-limited continuous cultures fed a rich synthetic medium. Variables included rates of dilution (D) and oxygen transfer (K(1)a) and concentrations of xylose (X), ethanol (E), and dissolved oxygen (C(ox)). Sustained cell growth required the presence of oxygen. Given excess xylose, specific growth rate (micro) was a Monod function of C(ox). Specific oxygen uptake rate was proportional to mu by a yield coefficient relating biomass production to oxygen consumption; but oxygen uptake for maintenance was negligible. Thus steady-state C(OX) depended only on D, while steady-state biomass concentration was controlled by both D and K(1)a. Given excess oxygen, cells grew subject to Monod limitation by xylose, which became inhibitory above 40 g/L. Ethanol inhibition was consistent with Luong's model, and 64. 3 g/L was the maximum ethanol concentration allowing growth. Actively growing cells died at a rate that was 20% of micro. The dying portion increased with E and X.     

Influence of the membrane on T-2 toxin toxicity in Saccharomyces spp

In growing cells of Saccharomyces cerevisiae and Saccharomyces carlsbergensis, T-2 toxin inhibits cell growth. We have examined the role of the yeast membranes in the uptake mechanism(s) of T-2 toxin. The effects of membrane-modulating agents, ethanol, cetyltrimethylammonium bromide, Triton X-100, and heat were studied; these agents were found to increase the sensitivity of the yeasts toward T-2 toxin. In the presence of 5% (vol/vol) ethanol, 2 micrograms of T-2 toxin per ml caused complete inhibition of growth. In the presence of 1 microgram of cetyltrimethylammonium bromide per ml, yeast cells became sensitive to T-2 toxin, starting with a concentration of 0.5 micrograms/ml. Triton X-100 at concentrations below 1% (vol/vol) sensitized the cells toward T-2 toxin, but at higher concentrations it protected the cells from T-2 toxin. Temperatures of incubation between 7 and 30 degrees C influenced the growth reduction caused by T-2 toxin. The greatest observed reduction of growth in T-2 toxin-treated cultures occurred at 30 degrees C. To further prove that the membrane influences the interaction of T-2 toxin with yeasts, we have studied a yeast mutant with a reduced plasma membrane permeability (G. H. Rank et al., Mol. Gen. Genet. 152:13-18, 1977). This yeast mutant proved to be resistant to T-2 toxin concentrations of up to 50 micrograms/ml. These results show that the membrane plays a significant role in the interaction of T-2 toxin with yeast cells.     

Influence of the membrane on T-2 toxin toxicity in Saccharomyces spp.

In growing cells of Saccharomyces cerevisiae and Saccharomyces carlsbergensis, T-2 toxin inhibits cell growth. We have examined the role of the yeast membranes in the uptake mechanism(s) of T-2 toxin. The effects of membrane-modulating agents, ethanol, cetyltrimethylammonium bromide, Triton X-100, and heat were studied; these agents were found to increase the sensitivity of the yeasts toward T-2 toxin. In the presence of 5% (vol/vol) ethanol, 2 micrograms of T-2 toxin per ml caused complete inhibition of growth. In the presence of 1 microgram of cetyltrimethylammonium bromide per ml, yeast cells became sensitive to T-2 toxin, starting with a concentration of 0.5 micrograms/ml. Triton X-100 at concentrations below 1% (vol/vol) sensitized the cells toward T-2 toxin, but at higher concentrations it protected the cells from T-2 toxin. Temperatures of incubation between 7 and 30 degrees C influenced the growth reduction caused by T-2 toxin. The greatest observed reduction of growth in T-2 toxin-treated cultures occurred at 30 degrees C. To further prove that the membrane influences the interaction of T-2 toxin with yeasts, we have studied a yeast mutant with a reduced plasma membrane permeability (G. H. Rank et al., Mol. Gen. Genet. 152:13-18, 1977). This yeast mutant proved to be resistant to T-2 toxin concentrations of up to 50 micrograms/ml. These results show that the membrane plays a significant role in the interaction of T-2 toxin with yeast cells.     

Alcoholic fermentation by immobilized yeast at high sugar concentrations

Summary Glucose fermentation bySaccharomyces cerevisiae immobilized by entrapment in agar, carrageenan, alginate and polyacrylamide gels, was compared to that of freely suspended cells at concentrations of 10–50% (w.w.) sugar. The rate of ethanol production by the entrapped cells was 20–25% higher than that of the free cells. Concentrations of up to 14,5% w/w ethanol (30% glucose initial concentration) could be obtained. A number of hypotheses for the improved alcoholic fermentation are discussed.     

自絮凝酵母SPSC01在组合反应器系统中酒精连续发酵的研究

建立了一套由四级磁力搅拌发酵罐串联组成、总有效容积4000mL的小型组合生物反应器系统 ,其中一级罐作为种子培养罐。以脱胚脱皮玉米粉双酶法制备的糖化液为种子培养基和发酵底物 ,进行了自絮凝颗粒酵母酒精连续发酵的研究。种子罐培养基还原糖浓度为100g L ,添加 (NH₄)₂HPO₄ 和KH₂PO₄ 各 20g L ,以0.017h^-1 的恒定稀释速率流加 ,并溢流至后续酒精发酵系统。发酵底物初始还原糖浓度 220g/L ,添加 (NH₄)₂HPO₄ 15g/L和KH₂PO₄2 5g/L ,流加至第一级发酵罐 ,稀释速率分别为 0.017、0.025、0.033、0.040和0.05 0h^-1。实验数据表明 ,自絮凝颗粒酵母在各发酵罐中呈部分固定化状态 ,在稀释速率0.040h^-1 条件下 ,发酵系统呈一定的振荡行为 ,其他四个稀释速率实验组均能够达拟稳态。当稀释速率不超过 0 0 33h^-1 ,流出末级发酵罐的发酵液中酒精浓度可以达到 12 % (V/V)以上 ,残还原糖和残总糖分别在 0 11%和 0 35 % h^-1,流出末级发酵罐的发酵液中酒精浓度可以达到12%（V/V）以上,残还原糖和残总糖分别在0.11%和0.35%（W/V）以下。在稀释速率为0.033h^-1时,计算发酵系统酒精的设备生产强度指标为3.32（g·L^-1·h^-1）,与游离酵母细胞传统酒精发酵工艺相比,增加约1倍。     

Ethanol production from eucalyptus wood hemicellulose hydrolysate by Pichia stipitis

Ethanol production was evaluated from eucalyptus wood hemicellulose acid hydrolysate using Pichia stipitis NRRL Y-7124. An initial lag phase characterized by flocculation and viability loss of the yeast inoculated was observed. Subsequently, cell regrowth occurred with sequential consumption of sugars and production of ethanol. Polyol formation was detected. Acetic acid present in the hydrolysate was an important inhibitor of the fermentation, reducing the rate and the yield. Its toxic effect was due essentially to its undissociated form. The fermentation was more effective at an oxygen transfer rate between 1.2 and 2.4 mmol/L h and an initial pH of 6.5. The hydrolysate used in the experiences had the following composition (expressed in grams per liter): xylose 30, arabinose 2.8, glucose 1.5, galactose 3.7, mannose 1.0, cellobiose 0.5, acetic acid 10, glucuronic acid 1.5, and galacturonic acid 1.0. The best values obtained were maximum ethanol concentration 12.6 g/L, fermentation time 75 h, fermentable sugar consumption 99% ethanol yield 0.35 g/g sugars consumed, and volumetric ethanol productivity 4 g/L day. (c) 1992 John Wiley & Sons, Inc.     

Rapid ethanol fermentations using vacuum and cell recycle

Cell recycle and vacuum fermentation systems were developed for continuous ethanol production. Cell recycle was employed in both atmospheric pressure and vacuum fermentations to achieve high cell densities and rapid ethanol fermentation rates. Studies were conducted with Saccharomyces cerevisiae (ATCC No. 4126) at a fermentation temperature of 35°C. Employing a 10% glucose feed, a cell density of 50 g dry wt/liter was obtained in atmospheric-cell recycle fermentations which produced a fermentor ethanol productivity of 29.0 g/liter-hr. The vacuum fermentor eliminated ethanol inhibition by boiling away ethanol from the fermenting beer as it was formed. This permitted the rapid and complete fermentation of concentrated sugar solutions. At a total pressure of 50 mmHg and using a 33.4% glucose feed, ethanol productivities of 82 and 40 g/liter-hr were achieved with the vacuum system with and without cell recycle, respectively. Fermentor ethanol productivities were thus increased as much as twelvefold over conventional continuous fermentations. In order to maintain a viable yeast culture in the vacuum fermentor, a bleed of fermented broth had to be continuously withdrawn to remove nonvolatile compounds. It was also necessary to sparge the vacuum fermentor with pure oxygen to satisfy the trace oxygen requirement of the fermenting yeast.     

Studies on Oxygen Transfer in Submerged Fermentations

In conventional shaken culture system, control of oxygen supply is performed by changing liquid volume in flasks and it necessarily introduces variation in the effectiveness of agitation and in the partial pressure of carbon dioxide. In jar or tank culture system, also, the changes in mechanical agitation and in the flow rate of air for control of aeration induce similar problems. It is impossible, therefore, to isolate the effects of oxygen on microbial metabolism from these accompanying ones. Hence, there is a basic requirement of making clear distinction among them, and in this paper the effects of agitation and carbon dioxide on product formation are presented in glutamic acid fermentation using the apparatus of controlling the level of dissolved oxygen throughout the fermentation.

To obtain fundamental knowledge required for attaining adequate aeration, the rate of oxygen demand in glutamic acid fermentation was discussed in connection with its fermentation rates. On the basis of specific rates, rates of change per unit mass of cells, glutamic acid fermentation was found to fall in the process pattern of Gaden’s type II, in which a constant rate of oxygen demand was sustained for a considerable time. On the basis of volumetric rates, rates of change per unit volume of broths, oxygen demand was recognized to be correlated with growth, sugar utilization and product formation, and it was pointed out particularly that the oxygen demand was closedly related with sugar utilization. In the particular cases where rapid utilization of sugar occurred, therefore, oxygen deficiency was liable to be evoked being unable to fill the growing oxygen demand. This finding might be useful for scale-up studies or process design.