静息细胞转化生产3-羟基丙酸的条件优化

本文研究了静息细胞生物转化生产3-羟基丙酸的反应体系。考察了以甘油为底物,利用静息细胞转化生产3一羟基丙酸的相关因素,确定了最佳的转化条件：细胞浓度20g／L,甘油浓度20g／L,辅酶VB12浓度10mg／L,NAD＋浓度0．15mmol／L,温度35℃,反应体系为0．05mol／LpH7．0Tris—HCl缓冲液。在上述条件下反应6h后,3-羟基丙酸的产量达到为3．17g／L,底物转化率为28．33％。由上述结果可知,采用静息细胞转化法为3-HP的生物合成提供了一种可能的方法。     

球孢白僵菌固定化生物转化合成D-HPPA

[目的]利用球孢白僵菌进行固定化生物转化,将底物R-(+)-2-苯氧基丙酸(D-PPA)转化合成产物R-(+)-2-(4-羟基苯氧基)丙酸(D-HPPA)。[方法]利用海藻酸钠和聚乙烯醇对球孢白僵菌进行包埋处理,并对包埋条件进行累积优化。[结果]4%海藻酸钠和4. 5%聚乙烯醇混合后,再加入2. 5%的氯化钙作为交联剂交联8 h。在此包埋条件下制备的白僵菌凝胶珠,置于30 g/L的D-PPA进行固定化生物转化。反应5 d后,产物浓度最终为29. 9 g/L,平均生产强度为5. 98 g/(L·d),底物转化率为99. 7%。[结论]海藻酸钠和聚乙烯醇可用于白僵菌的固定化,且较游离菌体的生物转化的反应周期缩短28. 6%,平均生产强度增加64. 7%,底物转化率提高17. 7%。     

羰基还原酶不对称还原（R）-6-氰基-5-羟基-3-羰基己酸叔丁酯

选择R-羰基还原酶和葡萄糖脱氢酶双酶,协同催化（R）-6-氰基5-羟基-3-羰基己酸叔丁酯不对称还原制备阿托伐他汀关键手性合成子6-氰基-（3R,5R）-二羟基已酸叔丁酯。转化条件优化结果显示：在不添加外源性辅酶NADP（H）、菌体用量15．0g/L、147．0g/L（R）-6-氰基-5-羟基-3-羰基己酸叔丁酯、128．2g／L葡萄糖,30℃、pH6．5条件下反应6h后,底物转化率达到100％,产物d．e．值大于99．5％。     

β-脱卤酶的基因克隆表达及其酶学性质

根据GenBank中的序列设计引物,克隆芽孢杆菌中的β-脱卤酶基因(命名为bhd)。以pET30a(+)为载体、Escherichia coli BL21(DE3)-CondonPlus为宿主菌,实现了bhd的高效表达。使用HisTrapTMFF亲和层析柱纯化重组β-脱卤酶,分子量约为23.1 kD。酶学性质研究表明,纯化的重组β-脱卤酶水解3-氯丙酸制备3-羟基丙酸的最适反应体系为30°C,100 mmol/L,pH 7.0的磷酸钠缓冲液。在最适反应条件下,重组β-脱卤酶的比活为16.2 U/mg,Km和Vmax分别为3.26μmol/L和17.86 mmol/(min.g protein)。在最适反应条件下,以10 mmol/L 3-氯丙酸为底物,反应36 h的转化率在93%以上。     

双酶偶联转化富马酸制备β-丙氨酸的工艺的建立与优化

酶转化法是生产β-丙氨酸的重要途径,但单一酶法转化存在底物价格较高的问题。通过构建双酶催化体系制备β-丙氨酸,即将来源于大肠杆菌的天冬氨酸酶(AspA)和来源于谷氨酸棒杆菌的L-天冬氨酸α-脱羧酶(PanD)偶联,以富马酸和氨为底物进行酶促反应合成β-丙氨酸。催化反应中AspA与PanD的最适加酶比例为1∶80,其中AspA的浓度为10μg/mL,转化温度为37℃,pH为7.0;浓度为100 mmol/L的富马酸可在8 h内被完全转化,转化率为100%,摩尔产率为90.9%,β-丙氨酸的产量为90 mmol/L,约为7 g/L;浓度为200 mmol/L的富马酸在反应8 h后,体系中β-丙氨酸的产量为126 mmol/L,约合9.8 g/L,继续延长反应时间,转化率并没有明显提高。根据该研究提出的双酶偶联转化工艺可将价格低廉的富马酸一步转化为具有高附加值的β-丙氨酸。     

α-酮戊二酸依赖型双加氧酶催化特性及反应耦联辅因子对其催化羟基化反应的影响

【目的】以重组大肠杆菌表达的枯草芽孢杆菌(Bacillus subtilis)L-异亮氨酸双加氧酶(L-isoleucine dioxygenase,IDO)为研究对象,考察其催化L-异亮氨酸(L-Ile)羟基化反应的影响因素,构建IDO催化合成羟基氨基酸的反应体系。【方法】通过Ni-NTA亲和层析法从重组大肠杆菌(Escherichia coli)BL21/p ET28a-ido中纯化获得重组IDO,以L-Ile为底物,考察重组IDO催化羟基化反应的影响因素,并进一步针对耦联反应优化α-酮戊二酸(α-KG)在重组IDO酶促转化体系中的添加浓度。【结果】基于重组IDO催化L-Ile羟基化的活性测定,计算该酶Km为0.247 mmol/L,kcat为1.260 s-1,kcat/Km为5.101 L/(mmol·s),与其他同源酶动力学参数比较分析表明,重组IDO的底物亲和性及催化效率较高。重组IDO催化反应的最适温度为20°C、最适p H为7.0;在35°C以下较为稳定;反应体系中Fe2+最适浓度为1 mmol/L。重组IDO可催化不同L-氨基酸反应,对L-异亮氨酸、L-正亮氨酸、L-甲硫氨酸的活性较高。通过优化α-KG浓度,反应体系中添加30 mmol/Lα-KG时,可将底物浓度提高至70 mmol/L,产物4-羟基异亮氨酸(4-HIL)的摩尔产率达66.20%,表明α-KG作为反应耦联辅因子,其浓度对重组IDO催化L-Ile羟基化具有显著影响。【结论】重组IDO的底物亲和性、催化效率、最适催化条件、稳定性等基本性质有利于催化L-Ile羟基化反应。在其催化反应体系中,α-KG作为反应耦联辅因子,对酶促转化效果影响显著。研究结果为4-HIL及其他羟基氨基酸的酶促转化提供了研究基础。     

Bacillus megaterium WZ009催化合成(R)-4-氯-3-羟基丁酸乙酯和(S)-3-羟基-γ-丁内酯

以外消旋4-氯-3-羟基丁酸乙酯为唯一C源的富集培养筛选得到一株菌株WZ009,经16S rDNA测序鉴定为巨大芽胞杆菌(Bacillus megaterium)。B.megaterium WZ009静息细胞可以立体选择性催化(S)-4-氯-3-羟基丁酸乙酯水解和脱氯反应得到光学纯的(R)-4-氯-3-羟基丁酸乙酯(e.e.≥99%)和(S)-3-羟基-γ-丁内酯(e.e.≥95%)。笔者对B.megaterium WZ009不对称催化反应影响因素(温度、pH、中和剂、底物浓度、时间进程以及细胞重复利用)进行优化研究,确定了该反应体系最优条件:底物浓度200 mmol/L,中和剂氨水,pH 7.2,40℃反应12 h,转化率达到50.6%,底物对映体过量值为99.6%。该生物催化合成(R)-4-氯-3-羟基丁酸乙酯和(S)-3-羟基-γ-丁内酯过程具有良好的工业化应用前景。     

Gibberella intermedia C2转化4-雄甾烯-3、17-二酮的研究

甾体化合物具有独特的生理活性,已被广泛应用于抗炎、利尿、免疫、避孕及抗癌等领域。近些年,生物催化与转化在甾体药物中间体合成中发挥的作用日益强大。为了能够合成一些具有潜在价值的新型甾体化合物,以实验室菌种库中保藏的一株Gibberella intermedia C2为研究对象,选取了雄甾烷中一种有广泛用途的化合物4-雄甾烯-3、17-二酮(简称雄烯二酮,AD)为底物进行生物转化。转化液经提取分离,最终获得2个转化产物,经结构鉴定分别为15α-OH-AD和11α,15α-diOH-AD。转化机制研究发现,G.intermedia C2先将底物的15位羟基化生成15α-OHAD,再将其11位羟基化形成双羟基产物。赤霉菌能够特异性、有序地完成对AD的两步羟化反应。此外,通过工艺优化,确定了羟化4AD反应的最适工艺参数如下:发酵培养基的初始pH 6.5,装液量30ml/250ml,底物浓度6.0g/L,转化温度28℃,摇床转速220r/min,转化周期为84h。此时,底物AD的摩尔转化率达到81.5%。     

（S）-（-）-β-羟基苯丙酸乙酯的微生物法合成

采用酿酒酵母CGMCC No．2266菌体,不对称还原β-羰基苯丙酸乙酯制备光学纯（S）-（-）-β-羟基苯丙酸乙酯。结果表明：采用初始pH为8．0的液体发酵培养基培养的CGMCCNo．2266菌体经过50℃预热处理30min后用于生物转化获得的（S）-（-）-G-羟基苯丙酸乙酯对映体过剩值可以达到100％ee。确定了合成（S）-（-）-β-羟基苯丙酸乙酯的较佳转化条件为pH7．0,温度30℃,转化时间24h,底物浓度为3．63mmol／L,菌体用量为86g/L（干重／反应体积）。以10％葡萄糖为辅助底物,产率比不加辅助底物时提高了75．4％。在最佳转化条件下反应转化率及（S）-（-）-β-羟基苯丙酸乙酯对映体过剩值可分别达到98．4％和100％ee。     

生物催化法合成6-氰基-（3R，5R）-二羟基己酸叔丁酯

利用E.coli BL21／pCDFDuet-gdh—cr-X共表达全细胞催化6-氰基-（5R）-羟基-3-羰基己酸叔丁酯不对称还原合成6-氰基-（3R,5R）-二羟基已酸叔丁酯。结果表明：在菌体用量4．85g/L、葡萄糖与底物质量浓度比为1：1、温度28℃、pH7．0条件下,80．0g／L6-氰基-（5R）-羟基-3-羰基己酸叔丁酯生物还原2h后,底物转化率可达99．0％,产物d.e．值大于99．5％。在考察范围内,NADP^＋用量对催化效率无显著作用。     

Enhanced acetone-butanol fermentation using repeated fed-batch operation coupled with cell recycle by membrane and simultaneous removal of inhibitory products by adsorption

A novel acetone-butanol production process was developed which integrates a repeated fed-batch fermentation with continuous product removal and cell recycle. The inhibitory product concentrations of the fermentation by Clostridium acetobutylicum were reduced by the simultaneous extraction process using polyvinylpyridine (PVP) as an adsorbent. Because of the reduced inhibition effect, a higher specific cell growth rate and thus a higher product formation rate was achieved. The cell recycle using membrane separation increased the total cell mass density and, therefore, enhanced the reactor productivity. The repeated fed-batchoperation overcame the drawbacks typically associated with a batch operation such as down times, long lag period, and the limitation on the maximum initial substrate concentration allowed due to the substrate inhibition. Unlike a continuous operation, the repeated fed-batch operation could beoperated for a long time at a relatively higher substrate concentration without sacrificing the substrate loss in the effluent. As a result, the integrated process reached 47.2 g/L in the equivalent solvent concentration (including acetone, butanol, and ethanol) and 1.69 g/L . h in the fermentor productivity, on average, over a 239.5-h period. Compared with a controlled traditional batch acetone-butanol fermentation, the equivalent solvent concentration and the tormentor productivity were increased by 140% and 320%, respectively. (c) 1995 John Wiley & Sons Inc.     

Acetate production from whey lactose using co-immobilized cells of homolactic and homoacetic bacteria in a fibrous-bed bioreactor

Acetate was produced from whey lactose in batch and fed-batch fermentations using co-immobilized cells of Clostridium formicoaceticum and Lactococcus lactis. The cells were immobilized in a spirally wound fibrous sheet packed in a 0.45-L column reactor, with liquid circulated through a 5-L stirred-tank fermentor. Industrial-grade nitrogen sources, including corn steep liquor, casein hydrolysate, and yeast hydrolysate, were studied as inexpensive nutrient supplements to whey permeate and acid whey. Supplementation with either 2.5% (v/v) corn steep liquor or 1.5 g/L casein hydrolysate was adequate for the cocultured fermentation. The overall acetic acid yield from lactose was 0.9 g/g, and the productivity was 0.25 g/(L h). Both lactate and acetate at high concentrations inhibited the homoacetic fermentation. To overcome these inhibitions, fed-batch fermentations were used to keep lactate concentration low and to adapt cells to high-concentration acetate. The final acetate concentration obtained in the fed-batch fermentation was 75 g/L, which was the highest acetate concentration ever produced by C. formicoaceticum. Even at this high acetate concentration, the overall productivity was 0.18 g/(L h) based on the total medium volume and 1.23 g/(L h) based on the fibrous-bed reactor volume. The cells isolated from the fibrous-bed bioreactor at the end of this study were more tolerant to acetic acid than the original culture used to seed the bioreactor, indicating that adaptation and natural selection of acetate-tolerant strains occurred. This cocultured fermentation process could be used to produce a low-cost acetate deicer from whey permeate and acid whey.     

一株1,3-丙二醇生产菌的分离鉴定及其发酵特性

从活性污泥中分离筛选得到一株能代谢甘油生产1,3-丙二醇(1,3-PD)的菌株2-1,通过形态学鉴定、生理生化试验、16S rRNA序列分析对菌株分类学地位进行鉴定,用MEGA 4.1软件构建的系统发育树显示菌株2-1与Klebsiella pneumoniae(CP001891)的亲缘关系最近。16S rDNA序列同源性比较发现,菌株2-1与模式菌株同源率为95.4%,疑似为新种。对菌株2-1在5 L发酵罐中进行发酵特性研究,分批补料发酵时得到较高的1,3-PD终浓度,达到63.5 g/L,此时生产强度为2.19 g/(L.h),底物转化率0.64 mol/mol。     

Ethanol production from nonsterilized carob pod extract by free and immobilized Saccharomyces cerevisiae cells using fed-batch culture

The production of ethanol from carob pod extract by free and immobilized Saccharomyces cerevisiae cells in batch and fed-batch culture was investigated. Fed-batch culture proved to be a better fermentation system for the production of ethanol than batch culture. In fed-batch culture, both free and immobilized S. cerevisiae cells gave the same maximum concentration (62 g/L) of final ethanol at an initial sugar concentration of 300 g/L and F = 167 mL/h. The maximum ethanol productivity (4.4 g/L h) was obtained with both free and immobilized cells at a substrate concentration of 300 g/L and F = 334 mL/h. In repeated fed-batch culture, immobilized S. cerevisiae cells gave a higher overall ethanol concentration compared with the free cells. The immobilized S. cerevisiae cells in Ca-alginate beads retained their ability to produce ethanol for 10 days. (c) 1994 John Wiley & Sons, Inc.     

Production of mannitol by Lactobacillus intermedius NRRL B-3693 in fed-batch and continuous cell-recycle fermentations

Improved fermentation processes were developed for the production of mannitol by a heterofermentative lactic acid bacterium (Lactobacillus intermedius NRRL B-3693). A fed-batch fermentation protocol overcame limitations caused by high substrate concentrations. The process was developed using corn steep liquor and glucose as inexpensive industrial nutrient sources, supplemented with a small amount of soy peptone and manganese. The fed-batch process resulted in a concentration of 176 ± 0.5 g mannitol from 184 ± 0 g fructose and 92 ± 0.1 g glucose per L of final fermentation broth in 30 h with a volumetric productivity of 5.9 g/(L h). Further increases in volumetric productivity of mannitol were obtained in a continuous cell-recycle fermentation process that reached more than 40 g/(L h), despite reduced mannitol levels of 78–98 g/L and residual substrate of 10–20 g/L. This is the first report of such a high volumetric productivity of mannitol by a heterofermentative lactic acid bacterium.     

Multi-stage high cell continuous fermentation for high productivity and titer

We carried out the first simulation on multi-stage continuous high cell density culture (MSC-HCDC) to show that the MSC-HCDC can achieve batch/fed-batch product titer with much higher productivity to the fed-batch productivity using published fermentation kinetics of lactic acid, penicillin and ethanol. The system under consideration consists of n-serially connected continuous stirred-tank reactors (CSTRs) with either hollow fiber cell recycling or cell immobilization for high cell-density culture. In each CSTR substrate supply and product removal are possible. Penicillin production is severely limited by glucose metabolite repression that requires multi-CSTR glucose feeding. An 8-stage C-HCDC lactic acid fermentation resulted in 212.9 g/L of titer and 10.6 g/L/h of productivity, corresponding to 101 and 429% of the comparable lactic acid fed-batch, respectively. The penicillin production model predicted 149% (0.085 g/L/h) of productivity in 8-stage C-HCDC with 40 g/L of cell density and 289% of productivity (0.165 g/L/h) in 7-stage C-HCDC with 60 g/L of cell density compared with referring batch cultivations. A 2-stage C-HCDC ethanol experimental run showed 107% titer and 257% productivity of the batch system having 88.8 g/L of titer and 3.7 g/L/h of productivity. MSC-HCDC can give much higher productivity than batch/fed-batch system, and yield a several percentage higher titer as well. The productivity ratio of MSC-HCDC over batch/fed-batch system is given as a multiplication of system dilution rate of MSC-HCDC and cycle time of batch/fed-batch system. We suggest MSC-HCDC as a new production platform for various fermentation products including monoclonal antibody.     

Acetone–butanol–ethanol (ABE) fermentation using Clostridium acetobutylicum XY16 and in situ recovery by PDMS/ceramic composite membrane

PDMS/ceramic composite membrane was directly integrated with acetone-butanol-ethanol (ABE) fermentation using Clostridium acetobutylicum XY16 at 37 °C and in situ removing ABE from fermentation broth. The membrane was integrated with batch fermentation, and approximately 46 % solvent was extracted. The solvent in permeates was 118 g/L, and solvent productivity was 0.303 g/(L/h), which was approximately 33 % higher compared with the batch fermentation without in situ recovery. The fed-batch fermentation with in situ recovery by pervaporation continued for more than 200 h, 61 % solvent was extracted, and the solvent in penetration was 96.2 g/L. The total flux ranged from 0.338 to 0.847 kg/(m(2)/h) and the separation factor of butanol ranged from 5.1 to 27.1 in this process. The membrane was fouled by the active fermentation broth, nevertheless the separation performances were partially recovered by offline membrane cleaning, and the solvent productivity was increased to 0.252 g/(L/h), which was 19 % higher compared with that in situ recovery process without membrane cleaning.     

利用克雷伯肺炎杆菌限制性底物发酵生产1，3-丙二醇

研究了克雷伯肺炎杆菌（Klebsiella pneumoniae）批式流加发酵生产1,3-丙二醇的发酵工艺,根据1,3-丙二醇的生产和菌体生长相关的特点,采用营养基质限制性流加的发酵工艺,通过控制氮源氯化铵以保持细胞稳定生长。结果表明：过低的氮源浓度,细胞生长受到限制,影响产物1,3-PD的合成;过高的氮源浓度,细胞比生长速率增加,但1,3-PD关于消耗甘油的得率降低,用于生长和维持代谢所消耗的甘油量增加。以0.41 g/(L·h)的氮源流加速率,残余氯化铵浓度在0.1 g/L时,转化率和生产强度最高。发酵25 h～28 h后,1,3-丙二醇最终浓度达到52.03 g/L,生产强度为2.04 g/(L·h),相对于甘油的摩尔转化率为0.66,分别比氮源限制前提高了28.0 ％、35.1 ％及29.4 ％。通过限制性流加氯化铵,控制细胞的比生长速率,使底物甘油有效转变为发酵的目标产物1,3-PD,有效实现产物1,3-PD的高生产强度以及对甘油的高转化率。     

Fed-batch sorbose fermentation using pulse and multiple feeding strategies for productivity improvement

Microbial oxidation of D-sorbitol tol-sorbose byAcetobacter suboxydans is of commercial importance since it is the only biochemical process in vitamin C synthesis. The main bottleneck in the batch oxidation of sorbitol to sorbose is that the process is severely inhibited by sorbitol. Suitable fed-batch fermentation designs can eliminate the inherent substrate inhibition and improve sorbose productivity. Fed-batch sorbose fermentations were conducted by using two nutrient feeding strategies. For fed-batch fermentation with pulse feeding highly concentrated sorbitol (600 g/L) along with other nutrients were fed intermittently in four pulses of 0.5 liter in response to the increased DO signal. The fed-batch fermentation was over in 24 h with a sorbose productivity of 13.40 g/L/h and a final sorbose concentration of 320.48 g/L. On the other hand, in fed-batch fermentation with multiple feeds, two pulse feeds of 0.5 liter nutrient medium containing 600 g/L sorbitol was followed by the addition of 1.5 liter nutrient medium containing 600 g/L sorbitol at a constant feed rate of 0.36 L/h till the full working capacity of the reactor. The fermentation was completed in 24 h with an enhanced sorbose productivity of 15.09 g/L/h and a sorbose concentration of 332.60 g/L. The sorbose concentration and productivity obtained by multiple feeding of nutrients was found to be higher than that obtained by pulse feeding and was therefore a better strategy for fed-batch sorbose fermentation.     

High-level production of 1,3-propanediol from crude glycerol by <Emphasis Type="Italic">Clostridium butyricum</Emphasis> AKR102a

The aim of this study was to optimize a biotechnological process for the production of 1,3-propanediol (1,3-PD) based on low-quality crude glycerol derived from biodiesel production. Clostridium butyricum AKR102a was used in fed-batch fermentations in 1-L and 200-L scale. The newly discovered strain is characterized by rapid growth, high product tolerance, and the ability to use crude glycerol at the lowest purity directly gained from a biodiesel plant side stream. Using pure glycerol, the strain AKR102 reached 93.7 g/L 1,3-PD with an overall productivity of 3.3 g/(L*h). With crude glycerol under the same conditions, 76.2 g/L 1,3-PD was produced with a productivity of 2.3 g/(L*h). These are among the best results published so far for natural producers. The scale up to 200 L was possible. Due to the simpler process design, only 61.5 g/L 1,3-PD could be reached with a productivity of 2.1 g/(L*h).