康氏木霉(P2)纤维素酶转化蔗髓纤维素成糖及生产SCP

在30升卧式酶解罐和5升标准发酵罐中,进行了以蔗髓纤维素为基质,用康氏木霉(Trichoderma koningii)P2菌株产生的纤维素酶水解成糖生产单细胞蛋白的试验。10%的底物浓度可以得到较高的转化率。最适搅拌速度为10r/min,用酶量为2.21u/g底物,50℃酶促水解24小时,酶解液中还原糖含量为3—4%,底物得糖率49.5%,全纤维素转化率73.8%。用该酶解糖生产单细胞蛋白,试验了5升标准罐培养酵母的最适条件。     

纤维基质对液体培养灵芝产纤维素酶的影响

本研究通过在培养基中添加滤纸、羧甲基纤维素(CMC)、蔗渣和玉米芯等纤维素类基质,观察纤维素基质对液体培养条件下灵芝产纤维素酶和半纤维素酶的影响.结果表明,这些纤维素基质能促进纤维素酶活力的增加,促进作用效果各异,当滤纸的添加量达到1 g/L时,滤纸酶活(FP酶活)达到空白对照的9.04倍,当蔗渣添加量为1 g/L时,灵芝β-1,4-葡聚糖酶酶活(Cx酶活)、FP酶活、半纤维素酶活分别比空白对照样增加了12%、534%、117.3%.     

玉米秸秆酶水解过程中的酶复配条件优化

降低酶解成本是纤维素乙醇生产的关键。利用酶复配技术优化蒸汽爆破处理后玉米秸秆的酶水解工艺条件,以提高纤维素的转化率。通过单因素实验和正交实验,研究了纤维素酶、木聚糖酶和β-葡萄糖苷酶对酶解效率的影响规律。结果表明,汽爆玉米秸秆,纤维素含量达42.21%,半纤维素仅为3.65%。纤维素酶对酶解过程起决定性作用,添加40 FPU/g时,酶解率为75.45%;木聚糖酶可促使更多的纤维素暴露出来,添加1 500 IU/g时,酶解率最高为78.03%;β-葡萄糖苷酶有助于消除纤维二糖积累造成的反馈抑制,用量40 IU/g时,纤维二糖浓度为0.330 4 g/100 m L,酶解率达76.45%。正交实验确定最佳工艺为:纤维素酶用量30 FPU/g,木聚糖酶用量800 IU/g,β-葡萄糖苷酶用量40 IU/g;该条件下,进行底物质量浓度25%的验证实验,葡萄糖达9.3g/100 m L,若用单一天冠纤维素酶,葡萄糖仅5.9 g/100 m L,提高了57.63%。三种酶的影响顺序为:纤维素酶木聚糖酶β-葡萄糖苷酶。     

玉米秸秆分批补料获得高还原糖浓度酶解液的条件优化

木质纤维素高浓度还原糖水解液的获得是纤维乙醇产业化发展的方向。在发酵工业领域,分批补料法是实现这一目标的重要研究途径。本研究采用分批补料法对获得高浓度玉米秸秆酶解还原糖的条件进行了优化。以稀硫酸预处理的玉米秸秆为原料,考察了液固比、补加量与补加时间对分批补料糖化的影响。结果表明,秸秆高浓度酶解液条件的初始物料为20％ (重量/体积),木聚糖酶220 U/g (底物),纤维素酶6 FPU/g (底物),果胶酶50 U/g (底物),在24 h、48 h后分批补加8％预处理后的物料,同时添加与补料量相应的木聚糖酶20 U/g (底物),纤维素酶2 FPU/g (底物),72 h后,最终糖化结果与非补料法相比,还原糖浓度从48.5 g/L提高到138.5 g/L,原料的酶解率最终达到理论值的62.5％。试验结果表明补料法可以显著提高秸秆水解液还原糖浓度。     

酶水解菊芋糖浆发酵生产琥珀酸的初步研究

用产菊粉酶的一株黑曲霉菌株进行产酶发酵条件和水解条件研究,在30℃,pH 6.0,摇床转速200 r/min,发酵时间为3 d的最适产酶条件下,酶活可以达到45.9 U/mL.以总糖含量为85.2 g/L的菊芋粉为初始底物,最适酶水解条件为温度50℃,加黑曲霉培养液的量为10%(v/v),水解12 h后,水解率达到99.6%.用此酶解液在5 L搅拌发酵罐中进行琥珀酸发酵,初始还原糖浓度53.5 g/L,36 h发酵产琥珀酸43.8 g/L,琥珀酸产率0.83 g/g,糖利用率99.0%,琥珀酸生产强度1.22 g/(L·h).     

桑木层孔菌液体培养过程中几种胞外酶活性的变化

研究了桑木层孔菌Phellinus mori液体培养过程中发酵液中淀粉酶、果胶酶、羧甲基纤维素酶（CMC酶）和漆酶等4种胞外酶的活性变化,同时测定了蛋白质、还原糖和pH的变化。结果表明,桑木层孔菌拥有丰富的胞外酶系,淀粉酶酶活第7天时达到最大值,果胶酶在第9天和第12天的酶活都较高,羧甲基纤维素酶第10天时酶活最高,漆酶酶活第9天时达到最大值,说明桑木层孔菌对淀粉类物质利用最早。蛋白质浓度在第8天和第11天时出现两个峰值,还原糖浓度随培养时间逐渐降低,发酵液pH值在培养初期逐渐变小,后期逐渐变大。     

纤维素酶水解啤酒糟的研究

研究了纤维素酶水解啤酒糟的适宜条件以及底物预处理方法对纤维素转化率和多糖水解率的影响。在适宜条件下,100g干啤酒糟可水解得10．8g还原糖。酶解液用于培养酵母菌提取麦角固醇,残渣是生产含菌体蛋白饲料的原料。     

极端嗜热性微生物纤维素酶的活性

极端嗜热厌氧菌H173羧甲基纤维素酶的最适pH为6.5-7.0.加入二硫苏糖醇(DTT)和CaCl_2.2H_2O能使酶活稳定.80℃酶活非常稳定,放置120分钟仍保留原酶活的77%,90℃9分钟保留50%的活性,120分钟仅保留3%的原始酶活.在缓冲溶液中该酶能将微晶纤维素水解成葡萄糖和纤维二糖.培养基中含有最高至50mm葡萄糖时,对溶解微晶纤维素的活性不敏感.HPLC分析表明葡萄糖是该酶在液体培养基中的主要水解终产物.     

高效低成本纤维素酶诱导物的制备、筛选及应用

本研究利用玉米芯、甘蔗渣、脱木素木糖渣及粗纤维诱导里氏木霉产纤维素酶,对4种材料进行成份测定,然后以逐步添加的方式与微晶纤维素混合诱导里氏木霉产纤维素酶,和使用微晶纤维素诱导产酶对比,玉米芯含有的纤维素代替总纤维素的50%时,酶活力降低2个单位,蛋白减少0.8 g左右,其酶水解能力降低0.4%,对其产纤维素酶的水解能力没产生不利影响。甘蔗渣纤维素替代量可以达到30%,酶活力有1个单位的降低,蛋白分泌降低0.5 g左右,酶的水解能力提高7%左右。脱木素木糖渣纤维素替代量也可达到50%,酶活力和蛋白降低分别达到0.5个单位和0.2 g左右,酶水解能力降低了4.45%。粗纤维的利用可以达到100%替代,对里氏木霉产酶的酶活力影响有0.3个单位之差,水解能力降低1.625%。这说明这几种物质可以部分替代或者完全替代微晶纤维素,诱导里氏木霉发酵产纤维素酶,特别是由玉米芯和甘蔗渣制备的脱木素木糖渣和粗纤维有着较高的应用前景。该研究对降低纤维素酶的生产成本及其工业化应用具有重要意义。     

菊糖芽孢乳杆菌利用麸皮水解液发酵生产D-乳酸

考察菊糖芽孢乳杆菌YBS1-5利用麸皮的水解液发酵生产D-乳酸的性能。首先研究了不同蛋白酶对麸皮中蛋白组分的水解效率,优选酸性蛋白酶并对其进行水解工艺的优化,最终其水解液中的含氮量为4.6 g/L,水解效率为85.8%。对酸性蛋白酶的水解液残渣进行稀酸预处理后,利用纤维素酶对其进行酶解。通过批次补料酶解,水解液中的还原糖质量浓度达141.2 g/L,其中葡萄糖质量浓度为138.1 g/L、木糖质量浓度为1.4 g/L。利用麸皮的蛋白酶水解液和纤维素酶水解液替代葡萄糖和酵母粉发酵制备D-乳酸。在96 h内,D-乳酸产量达99.5 g/L,生产速率达1.04 g/(L·h),转化率89.1%。     

Multicomponent cellulase production by Cellulomonas biazotea NCIM‐2550 and its applications for cellulosic biohydrogen production

Among four cellulolytic microorganisms examined, Cellulomonas biazotea NCIM‐2550 can grow on various cellulosic substrates and produce reducing sugar. The activity of cellulases (endoglucanase, exoglucanase, and cellobiase), xylanase, amylase, and lignin class of enzymes produced by C. biazotea was mainly present extracellularly and the enzyme production was dependent on cellulosic substrates (carboxymethyl cellulose [CMC], sugarcane bagasse [SCB], and xylan) used for growth. Effects of physicochemical conditions on cellulolytic enzyme production were systematically investigated. Using MnCl₂ as a metal additive significantly induces the cellulase enzyme system, resulting in more reducing sugar production. The efficiency of fermentative conversion of the hydrolyzed SCB and xylan into clean H₂ energy was examined with seven H₂‐producing pure bacterial isolates. Only Clostridiumbutyricum CGS5 exhibited efficient H₂ production performance with the hydrolysate of SCB and xylan. The cumulative H₂ production and H₂ yield from using bagasse hydrolysate (initial reducing sugar concentration = 1.545 g/L) were approximately 72.61 mL/L and 2.13 mmol H₂/g reducing sugar (or 1.91 mmol H₂/g cellulose), respectively. Using xylan hydrolysate (initial reducing sugar concentration = 0.345 g/L) as substrate could also attain a cumulative H₂ production and H₂ yield of 87.02 mL/L and 5.03 mmol H₂/g reducing sugar (or 4.01 mmol H₂/g cellulose), respectively. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

利用天然纤维废弃物发酵生产L-乳酸的研究

为了降低L-乳酸的生产成本,更好的实现生物质秸秆的资源化,利用天然纤维素依次接种经离子注入诱变处理的木聚糖酶高产菌黑曲霉P602和米根霉RL6041高产菌进行固、液体二次发酵的方法,将其转化成用于工业生产的L-乳酸。结果表明:本实验条件下,未经过任何化学预处理的秸秆等物质接种黑曲霉P602进行固体发酵,产生的木聚糖酶活力为6 320 IU/g干(培养)基,纤维素酶活力为29 IU/g干基;加入100 mL水浸提后,产生的还原糖浓度为14.07 g/L,纤维物质糖化率为79.45%。取滤液接入米根霉RL6041进行液体发酵后,生成乳酸的量为7 g/L,糖酸转化率为47.6%,以(NH4)2SO4作为氮源时,最佳氮源浓度为3 g/L。     

固定化纤维二糖酶的研究

黑曲霉 (AspergillusnigerLORRE 0 12 )的孢子中富含纤维二糖酶 ,将这些孢子用海藻酸钙凝胶包埋后 ,可以方便有效地固定纤维二糖酶。固定化后的纤维二糖酶性能稳定 ,半衰期为 38d ,耐热性和适宜的pH范围均比固定化前有所增加 ,其Km 和Vmax值分别为 6 .0 1mmol L和 7.0 6mmol (min·L)。利用固定化纤维二糖酶重复分批酶解10g L的纤维二糖 ,连续 10批的酶解得率均可保持在 97%以上 ;采用连续酶解工艺 ,当稀释率为 0 .4h- 1 ,酶解得率可达 98.5 %。玉米芯经稀酸预处理后 ,其纤维残渣用里氏木霉 (Trichodermareesei)纤维素酶降解 ,酶解得率为6 9.5 % ;通过固定化纤维二糖酶的进一步作用 ,上述水解液中因纤维二糖积累所造成的反馈抑制作用得以消除 ,酶解得率提高到 84.2 % ,还原糖中葡萄糖的比例由 5 3 .6 %升至 89.5 % ,该研究结果在纤维原料酶水解工艺中具有良好的应用前景。     

玉米芯稀酸水解及L-乳酸发酵研究

对玉米芯稀硫酸水解条件及糖化液发酵L-乳酸进行了初步研究。结果表明,玉米芯木聚糖最适水解条件为2%H2SO_4、120℃、30 min、固液比1:10,糖化液还原糖含量可达40.8 g/L,主要成分为木塘。细菌A-19可以利用水解液中的葡萄糖和木糖产酸,最适发酵条件为45℃、pH 6.5,从45℃～51℃、pH 5.5～pH 6.5产量均较高。用未浓缩的水解液发酵24 h,L-乳酸产量为30.6g/L,残糖为1.6 g/L,糖酸转化率为82.6%;用浓缩1倍的水解液发酵48 h,L-乳酸产量为41.4 g/L,残糖4.1g/L,糖酸转化率为68.2%,在发酵48 h后继续补料发酵至72 h(补料液为浓缩3倍的水解液),L-乳酸产量为50.9 g/L,残糖6.3 g/L,糖酸转化率为71.8%。该研究为利用木质纤维素生产L-乳酸奠定了一定基础。     

Bioconversion of brewer's spent grains to bioethanol

Spent grains (SG), the residue remaining after extraction of wort, are a major by-product of brewing. This lignocelluose-rich biomass may provide a source of sugars for fuel ethanol fermentations. Dilute acid and enzyme treatments were developed to convert the hemicellulose and cellulose fractions to glucose, xylose and arabinose. Pretreatment of dried, milled grains with 0.16 N HNO(3) at 121 degrees C for 15 min was chosen as the most suitable method for solubilizing grains before enzymatic digestion with cellulase and hemicellulase preparations. Solids loading concentrations (10%, 15% and 20% w/v) were compared and reducing sugar between 40 and 48 g (100 g SG)(-1) was extracted. Hydrolysate, prepared from 20% SG, pretreated with 0.16 N HNO(3), partially neutralized to pH 5-6 and digested with enzymes for 18 h, contained 27 g L(-1) glucose, 16.7 g L(-1) xylose and 11.9 g L(-1) arabinose. Fermentation of this hydrolysate for 48 h by Pichia stipitis and Kluyveromyces marxianus resulted in 8.3 and 5.9 g L(-1) ethanol corresponding to ethanol conversion yields of 0.32 and 0.23 g ethanol (g substrate)(-1), respectively. Substrate utilization efficiency was less when compared with glucose/xylose mixtures in synthetic media, suggesting that yeast inhibitory compounds derived from SG were present in the hydrolysate.     

Engineering cellulase mixtures by varying the mole fraction of Thermomonospora fusca E5 and E3, Trichoderma reesei CBHI, and Caldocellum saccharolyticum beta-glucosidase

In this study, different mole fractions of pure Thermomonospora fusca E(5) and E(3), plus Trichoderma reesei CBHI were studied for reducing sugar production at 2 h, degree of synergism, and cellulose binding. In addition, the effects of introducing the Caldocellum saccharolyticum beta-glucosidase into this cellulase system were investigated. The cellulases used were purified to homogeneity. Avicel PH 102 (4% w/w solution in 0.05 sodium acetate pH 5.5 buffer) was the substrate. Reactions were run at 50 degrees C for 2 h using total cellulase concentrations of 8.3 or 12.2 muM. A bimixture of T. fusca E(3) and T. reesei CBHI was very effective in hydrolyzing microcrystalline cellulose (9.1% conversion). The addition of endoglucanase E(5) to the mixture only increased conversion to 9.8%. However, when both E(5) and beta-glucosidase were added, conversion increased to 14%. It was also observed that increasing total cellulase concentration beyond 8.3 muM did little to increase percent conversion of cellulose into glucose. The results of the binding studies indicate no competition for binding sites between the endo- and exocellulases. (c) 1993 John Wiley & Sons, Inc.     

An integrative process of bioconversion of oil palm empty fruit bunch fiber to ethanol with on-site cellulase production

The aim of this study was to efficiently convert oil palm empty fruit bunch fiber (OPEFB), one of the most commonly generated lingo-wastes in Southeast Asia, into both cellulase and bioethanol. The unprocessed cellulase crude (37.29 %) produced under solid-state fermentation using OPEFB as substrate showed a better reducing sugar yield using filter paper than the commercial enzyme blend (34.61 %). Organosolv pretreatment method could efficiently reduce hemicellulose (24.3–18.6 %) and lignin (35.2–22.1 %) content and increase cellulose content (40.5–59.3 %) from OPEFB. Enzymatic hydrolysis of pretreated OPEFB using the crude cellulase with 20 % solid content, enzyme loading of 15 FPU/g OPEFB at 50 °C, and pH 5.5 resulted in a OPEFB hydrolysate containing 36.01 g/L glucose after 72 h. Fermentation of the hydrolysate medium produced 17.64 g/L ethanol with 0.49 g/g yield from glucose and 0.088 g/g yield from OPEFB at 8 h using Saccharomyces cerevisiae.     

Enzymatic digestion of liquid hot water pretreated hybrid poplar

Liquid hot (LHW) water pretreatment (LHW) of lignocellulosic material enhances enzymatic conversion of cellulose to glucose by solubilizing hemicellulose fraction of the biomass, while leaving the cellulose more reactive and accessible to cellulase enzymes. Within the range of pretreatment conditions tested in this study, the optimized LHW pretreatment conditions for a 15% (wt/vol) slurry of hybrid poplar were found to be 200^oC, 10 min, which resulted in the highest fermentable sugar yield with minimal formation of sugar decomposition products during the pretreatment. The LHW pretreatment solubilized 62% of hemicellulose as soluble oligomers. Hot‐washing of the pretreated poplar slurry increased the efficiency of hydrolysis by doubling the yield of glucose for a given enzyme dose. The 15% (wt/vol) slurry of hybrid poplar, pretreated at the optimal conditions and hot‐washed, resulted in 54% glucose yield by 15 FPU cellulase per gram glucan after 120 h. The hydrolysate contained 56 g/L glucose and 12 g/L xylose. The effect of cellulase loading on the enzymatic digestibility of the pretreated poplar is also reported. Total monomeric sugar yield (glucose and xylose) reached 67% after 72 h of hydrolysis when 40 FPU cellulase per gram glucan were used. An overall mass balance of the poplar‐to‐ethanol process was established based on the experimentally determined composition and hydrolysis efficiencies of the liquid hot water pretreated poplar. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Column cellulose hydrolysis reactor: An efficient cellulose hydrolysis reactor with continuous cellulase recycling

Summary The use of a column cellulose hydrolysis reactor with continuous enzyme recycling was demonstrated by incorporating a continuous ultrafiltration apparatus at the effluent end of the column reactor. Using this setup, over 90% (w/v) cellulose hydrolysis was achieved, resulting in an average sugar concentration of 6.8% (w/v) in the effluent stream. The output of the system was 1.98 g of reducing sugar/l/h with a ratio of 87% (w/v) of the reducing sugars being monomeric sugars. Batch hydrolysis reactors were less effective, resulting in 57% (w/v) of the cellulose being hydrolyzed. The output of the batch reactor was 1.33 g of reducing sugar/l/h with similar product concentrations and percentage of monomeric sugars. The ratio of reducing sugar/filter paper unit of cellulase activity for the column method was 69.1 mg/U as compared to only 21.2 mg/U for the batch reactor.