重组尿酸氧化酶发酵工艺优化

目的:优化并获得重组尿酸氧化酶(rUOX)基因工程大肠杆菌BL21(DE3)/pET-32a-uox高密度发酵的工艺参数。方法:在三角摇瓶中进行培养条件的优化实验,分别考察了pH值、接种量、无机盐、碳源、诱导强度等对工程菌生长和重组蛋白表达的影响,得到了优化的发酵条件;在此基础上放大至NBS BIOFLO 110 14 L发酵罐,通过对诱导时机的优化,利用分批补料发酵的方式,使rUOX在高密度培养的条件下得到高表达。结果:在优化的发酵条件下,菌体密度(D600nm)最终达到50以上,相当于20 g/L干重;可溶性rUOX占菌体总蛋白量的45%,其含量达到3.45 g/L。结论:为规模化制备重组黄曲霉尿酸氧化酶奠定了基础。     

多拷贝毕赤酵母重组菌表达GCL摇瓶优化和高密度发酵

目的:构建高效表达白地霉脂肪酶的毕赤酵母重组菌株,并对筛选得到的菌株进行摇瓶发酵条件优化和分批补料高密度发酵工艺研究。方法:将诱导型表达载体pPIC9K-gcl电转化至毕赤酵母GS115。通过橄榄油-罗丹明B平板和摇瓶发酵筛选高脂肪酶活力的重组菌株,运用基于TaqMan探针的实时荧光定量PCR 法确定其拷贝数,并对菌株进行摇瓶发酵条件优化。在此基础上,研究重组菌在3L 发酵罐中的高密度发酵工艺。结果:筛选得到一株具有3 个白地霉脂肪酶基因拷贝的菌株GS115/pPIC9K-gcl 78#,初始酶活力为220 U/ml。当摇瓶发酵条件为甲醇诱导96 h,每24 h甲醇添加量1 %,接种量2 %,培养基初始pH 7.0,500 ml摇瓶装液量50 ml,甲醇诱导温度25℃ 时酶活力达735 U/ml。3L 发酵罐高密度发酵176.5 h,酶活力达到3360 U/ml,总蛋白含量达到4.30 g/L,且发酵过程中细胞活性一直保持在96 % 以上。结论:基因拷贝数与重组菌株的产酶水平呈正相关,摇瓶优化可显著提高重组菌株的产酶能力,为白地霉脂肪酶的工业化生产奠定了技术基础。     

提高重组TRAIL表达产率的优化策略

肿瘤坏死因子相关凋亡诱导配体（Apo2L/TRAIL）是一种新型的抗肿瘤蛋白。针对缩短发酵周期,提高生产效率这一目标,首先在摇瓶中利用响应面设计优化发酵表达条件,总TRAIL蛋白的表达量提高到25.7%。在此基础上研究了发酵条件对可溶性TRAIL蛋白表达量的影响。于3.7L发酵罐放大进行补料-分批发酵实验时,单位菌体可溶性TRAIL蛋白的表达量提高了67%,实现了在大肠杆菌高密度培养过程中单位细胞重组TRAIL蛋白的可溶性表达和体积生产率的提高。     

重组巴氏毕赤酵母高密度发酵表达rHSA

对基因工程菌Pichiapastoris的摇瓶发酵条件进行了试验 ,并根据摇瓶发酵的优化结果进行了补料分批高密度发酵。在摇瓶发酵时 ,甲醇诱导基因工程菌P .pastoris表达重组人血清白蛋白的发酵周期为 96h ;甲醇的最佳诱导浓度为 1 0g L ;发酵pH范围为 5 72～ 6 5 9;在摇瓶培养时 ,随着接种量的增加 ,虽然目的蛋白表达量缓慢增加 ,但单位细胞光密度的蛋白产率却明显下降 ,符合y =1 2 941x- 0 50 59方程 (线性相关系数r=0 9789) ,其限制性因子很可能为溶氧。在分批发酵 ,接种量为 1 0 %且种子细胞光密度 (OD60 0 )为 2 0左右时 ,细胞生长的延迟期为 2 1 1h左右 ,细胞生长光密度与培养时间的关系模型为 :y =0 7841e0 .2 3 19t(线性相关系数r=0 .993 6 ) ;在补料发酵时细胞干重浓度可达到 1 1 5g L— 1 6 0g L ,在 1 2 0h重组人血清白蛋白表达量最大达到 3 6g L。     

基因工程菌Pichia pastoris高密度培养条件研究

基因工程菌pichiapastoris最佳种子培养基为添加4mL/LPTMl的BMGY培养基;全合成高密度摇瓶培养基是甘油4%,(NH4)2SO410g/L,CaSO40.93g/L,K2SO418.2g/L,MgSO4@7H2O14.9g/L,0.1mol/L磷酸缓冲液(pH=6.0)配制,培养26h后细胞密度OD600可达到65。经SDS-PAGE电泳图谱分析,甲醇诱导培养72h结果12h有重组人血清白蛋白表达,24h达到最大。此全合成摇瓶培养基与批补料发酵培养基相类似,有利于指导发酵罐上发酵培养。     

毕赤酵母高密度表达重组猪胰岛素前体的研究

对摇瓶和50L罐上的重组菌毕赤酵母(Pichia pastoris)表达猪胰岛素前体(PIP)的发酵过程进行了研究。摇瓶发酵中,最佳诱导周期为60 h左右,诱导期甲醇的最佳加入量为每日2．0%～2．5%。50L发酵过程分为批发酵、补料和诱导表达3个阶段。生长期(批发酵和补料阶段)细胞干重与培养时间的关系可用模型y= 0．6525e~(0．1909t)来描述。在批发酵阶段和补料阶段,流加的氨水和甘油几乎全部用来合成菌体和维持,没有其他副产物产生。诱导表达阶段流加的氨水和甲醇分别约有80%和70%被菌体利用。将摇瓶与发酵罐的实验结果进行了比较,发现摇瓶发酵的限制因子很可能是溶氧,而罐发酵的限制因子为碳源,因此,将摇瓶实验的结果放大到发酵罐时调整了控制策略,加大了甲醇的补料速率,最终PIP浓度达到1．72g/L。     

通过参数相关性分析对发酵控制策略在植酸酶高密度发酵中的作用探讨

为了优化植酸酶高密度发酵条件,有必要获取在发酵过程中由于控制策略引起有关参数的实时变化及其关联性。本研究利用传感器对植酸酶工程菌高密度发酵过程进行数据在线采集,通过改变转速、接种量与补料甘油,探讨三方面控制因素对高密度发酵产酶过程参数具体影响及各参数变化之间的相关性,建立起与转速-细胞密度-溶氧-乳酸相关的发酵罐内外环境氧控制关系,细胞密度-氧气吸收-二氧化碳释放相关的细胞生长氧控制关系,以及细胞密度-二氧化碳释放-pH变化-蛋白表达的细胞诱导表达的关系。基于参数相关性分析并优化发酵控制条件得到:当搅拌转速递增,植酸酶工程菌接种量为10%时,其生长迟滞期最短(20 h)且发酵末期诱导表达植酸酶酶活可达3037.98 U/mL,相较摇瓶优化发酵的酶活提高了176.18%。本文研究结果可为工业植酸酶高效生产提供参考。     

蜡样芽胞杆菌GXBC-3三个普鲁兰酶基因的表达及其酶学特性

探索获得优良的新型普鲁兰酶基因,丰富普鲁兰酶理论,对实现普鲁兰酶国产化具有重要意义。分析GenBank数据库中蜡样芽胞杆菌假定Ⅰ型、Ⅱ型普鲁兰酶基因序列,从实验室保藏的蜡样芽胞杆菌Bacilluscereus GXBC-3中克隆得到3个普鲁兰酶基因pulA、pulB、pulC,并分别导入大肠杆菌进行胞内诱导表达。纯化重组酶酶学性质研究表明重组酶PulA能水解α-l,6-和α-l,4-糖苷键,为Ⅱ型普鲁兰酶,以普鲁兰糖为底物时,最适反应温度及pH分别为40℃和6.5,比活力为32.89 U/mg;以可溶性淀粉为底物时,最适反应温度及pH分别为50℃和7.0,比活力为25.71 U/mg。重组酶PulB和PulC二者均只能水解α-l,6-糖苷键,为I型普鲁兰酶,以普鲁兰糖为底物时,其最适反应温度及pH分别为45℃、7.0和45℃、6.5,比活力分别为228.54 U/mg和229.65 U/mg。     

地衣芽孢杆菌普鲁兰酶编码基因的鉴定

对地衣芽孢杆菌基因组序列分析显示。其中标注为amyX的基因可能编码普鲁兰酶。以PCR方法,从地衣芽孢杆菌染色体DNA中扩增出amyX基因蛋白编码区,插入大肠杆菌表达载体pET28aT7启动予下游。含重组质粒的大肠杆菌BL21（DE3）在IPTG诱导下表达出有活性的普鲁兰酶。酶学性质初步分析表明,重组普鲁兰酶最适反应温度为40℃,最适pH值为6．0。     

南极假丝酵母脂肪酶B基因在大肠杆菌中的表达和发酵优化

旨在利用大肠杆菌实现南极假丝酵母脂肪酶B(CALB)基因的高效可溶性表达,并降低生产成本。构建带有不同信号肽的CALB基因表达质粒,转化至不同大肠杆菌宿主中,在摇瓶中进行基础培养基、诱导条件、培养基组成成分和进程曲线的优化。结果显示,带有PelB信号肽的重组菌pET25b-CALB-1/Rosetta(DE3)在20℃下使用0.5%(W/V)乳糖在TY培养基中诱导表达效果最好,优化后的合成培养基成分为1.75%(W/V)山梨醇、2.25%(W/V)鱼蛋白胨、1%(W/V)安琪酵母提取物、0.75%(W/V)Na2HPO4。在摇瓶中诱导60 h后,CALB酶活力最高达到35.67 U/mL,相比于初始发酵酶活力提高了17.77倍,是目前大肠杆菌生产CALB的最高水平。成功地构建了大肠杆菌表达系统,经过系统优化后,CALB的高水平可溶性表达得以实现。     

High-level production of poly(3-hydroxybutyrate-co-3-hydroxyvalerate) by fed-batch culture of recombinant Escherichia coli.

Fermentation strategies for production of high concentrations of poly(3-hydroxybutyrate-co-3-hydroxyvalerate) [P(3HB-co-3HV)] with different 3-hydroxyvalerate (3HV) fractions by recombinant Escherichia coli harboring the Alcaligenes latus polyhydroxyalkanoate biosynthesis genes were developed. Fed-batch cultures of recombinant E. coli with the pH-stat feeding strategy facilitated production of high concentrations and high contents of P(3HB-co-3HV) in a chemically defined medium. When a feeding solution was added in order to increase the glucose and propionic acid concentrations to 20 g/liter and 20 mM, respectively, after each feeding, a cell dry weight of 120.3 g/liter and a relatively low P(3HB-co-3HV) content, 42.5 wt%, were obtained. Accumulation of a high residual concentration of propionic acid in the medium was the reason for the low P(3HB-co-3HV) content. An acetic acid induction strategy was used to stimulate the uptake and utilization of propionic acid. When a fed-batch culture and this strategy were used, we obtained a cell concentration, a P(3HB-co-3HV) concentration, a P(3HB-co-3HV) content, and a 3HV fraction of 141.9 g/liter, 88.1 g/liter, 62.1 wt%, and 15.3 mol%, respectively. When an improved nutrient feeding strategy, acetic acid induction, and oleic acid supplementation were used, we obtained a cell concentration, a P(3HB-co-3HV) concentration, a P(3HB-co-3HV) content, and a 3HV fraction of 203.1 g/liter, 158.8 g/liter, 78.2 wt%, and 10.6 mol%, respectively; this resulted in a high level of productivity, 2.88 g of P(3HB-co-3HV)/liter-h.     

High-Level Production of Poly(3-Hydroxybutyrate-co-3-Hydroxyvalerate) by Fed-Batch Culture of Recombinant Escherichia coli

Fermentation strategies for production of high concentrations of poly(3-hydroxybutyrate-co-3-hydroxyvalerate) [P(3HB-co-3HV)] with different 3-hydroxyvalerate (3HV) fractions by recombinant Escherichia coli harboring the Alcaligenes latus polyhydroxyalkanoate biosynthesis genes were developed. Fed-batch cultures of recombinant E. coli with the pH-stat feeding strategy facilitated production of high concentrations and high contents of P(3HB-co-3HV) in a chemically defined medium. When a feeding solution was added in order to increase the glucose and propionic acid concentrations to 20 g/liter and 20 mM, respectively, after each feeding, a cell dry weight of 120.3 g/liter and a relatively low P(3HB-co-3HV) content, 42.5 wt%, were obtained. Accumulation of a high residual concentration of propionic acid in the medium was the reason for the low P(3HB-co-3HV) content. An acetic acid induction strategy was used to stimulate the uptake and utilization of propionic acid. When a fed-batch culture and this strategy were used, we obtained a cell concentration, a P(3HB-co-3HV) concentration, a P(3HB-co-3HV) content, and a 3HV fraction of 141.9 g/liter, 88.1 g/liter, 62.1 wt%, and 15.3 mol%, respectively. When an improved nutrient feeding strategy, acetic acid induction, and oleic acid supplementation were used, we obtained a cell concentration, a P(3HB-co-3HV) concentration, a P(3HB-co-3HV) content, and a 3HV fraction of 203.1 g/liter, 158.8 g/liter, 78.2 wt%, and 10.6 mol%, respectively; this resulted in a high level of productivity, 2.88 g of P(3HB-co-3HV)/liter-h.     

Production of poly(3-hydroxybutyrate) by fed-batch culture of filamentation-suppressed recombinant Escherichia coli.

Recombinant Escherichia coli XL1-Blue harboring a high-copy-number plasmid containing the Alcaligenes eutrophus polyhydroxyalkanoate synthesis genes could efficiently synthesize poly(3-hydroxybutyrate) (PHB) in a complex medium containing yeast extract and tryptone but not in a defined medium. One of the reasons for the reduced PHB production in a defined medium was thought to be severe filamentation of cells in this medium. By overexpressing an essential cell division protein, FtsZ, in recombinant E. coli producing PHB, filamentation could be suppressed and PHB could be efficiently produced in a defined medium. A high PHB concentration of 149 g/liter, with high productivity of 3.4 g of PHB/liter/h, could be obtained by the pH-stat fed-batch culture of the filamentation-suppressed recombinant E. coli in a defined medium. It was also found that insufficient oxygen supply at a dissolved oxygen concentration (DOC) of 1 to 3% of air saturation during active PHB synthesis phase did not negatively affect PHB production. By growing cells to the concentration of 110 g/liter and then controlling the DOC in the range of 1 to 3% of air saturation, a PHB concentration of 157 g/liter and PHB productivity of 3.2 g of PHB/liter/h were obtained. For the scale-up studies, fed-batch culture was carried out in a 50-liter stirred tank fermentor, in which the DOC decreased to zero when cell concentration reached 50 g/liter. However, a relatively high PHB concentration of 101 g/liter and PHB productivity of 2.8 g of PHB/liter/h could still be obtained, which demonstrated the possibility of industrial production of PHB in a defined medium by employing the filamentation-suppressed recombinant E. coli.     

High-level expression of a fungal pyranose oxidase in high cell-density fed-batch cultivations of Escherichia coli using lactose as inducer

Expression of a recombinant pyranose oxidase (P2O) from the basidiomycete Trametes ochracea has been increased 10-fold in shaking flask cultures of Escherichia coli BL21(DE3) harboring plasmid pSE33 by optimizing the composition of the culture medium using an experimental design approach. Inexpensive lactose was used as a medium component and inducer of expression of the P2O gene, which is under the control of a trc promoter. The expression system was studied in detail in batch and fed-batch cultivations with the aim to improve the expression level of active recombinant protein and to minimize the formation of inclusion bodies. In batch cultivations, the highest specific P2O activity of 0.9 U (mg of soluble protein)(-1) was measured in oxygen-limited cultures grown at 25 degrees C. The highest overall volumetric productivity of 33 mg of active P2O per liter and hour (corresponding to 345U (L h)(-1)) has been determined in a high-density fed-batch process with a feed-forward exponential feeding strategy. During the fed-batch process, lactose was added intermittently to the culture. A final biomass concentration of 33 g L(-1) (based on cell dry weight) was obtained. Compared to shaking flask cultures in not optimized culture media, the overall volumetric P2O productivity has been improved by a factor of 110 using the fed-batch strategy and the optimized culture medium. Recombinant P2O was expressed in the cytoplasm with 9% of the total soluble protein being active P2O. In terms of physical and enzyme kinetic properties, the purified recombinant P2O was found to be similar to the previously published data of P2O isolated from its original host.     

表达重组葡激酶-水蛭素融合蛋白的大肠杆菌工程菌的高密度培养

采用溶氧反馈的分批培养流加补料的方法高密度培养重组大肠杆菌BL21(DE3)生产重组葡激酶-水蛭素融合蛋白。通过摇瓶培养对菌种和培养条件的初步筛选,采用溶氧反馈的流加补料策略,进行了5L发酵罐的合成培养基和复合培养基的发酵工艺的研究。通过对培养条件的不断优化,重组葡激酶-水蛭素融合蛋白在大肠杆菌BL21(DE3)里得到了高效表达,菌体密度最终达到115g/L(WCW)以上,可溶性重组融合蛋白占菌体总蛋白的30%以上,含量约为1.1~1.2g/L。5L发酵罐的发酵工艺参数在40L发酵罐中进行了放大培养,结果表明该工艺能有效的放大,可适用于工业生产。     

Poly(3-Hydroxybutyrate) Production with High Productivity and High Polymer Content by a Fed-Batch Culture of Alcaligenes latus under Nitrogen Limitation

Alcaligenes latus has been known to produce poly(3-hydroxybutyrate) (PHB) in a growth-associated manner even under nutrient-sufficient conditions. However, the PHB content obtained by fed-batch culture was always low, at ca. 50%, which makes the recovery process inefficient. In this study, the effect of applying nitrogen limitation on the production of PHB by A. latus was examined. In flask and batch cultures, the PHB synthesis rate could be increased considerably by applying nitrogen limitation. The PHB content could be increased to 87% by applying nitrogen limitation in batch culture, which was considerably higher than that typically obtainable (50%) under nitrogen-sufficient conditions. In fed-batch culture, cells were first cultured by the DO-stat feeding strategy without applying nitrogen limitation. Nitrogen limitation was applied at a cell concentration of 76 g (dry cell weight)/liter, and the sucrose concentration was maintained within 5 to 20 g/liter. After 8 h of nitrogen limitation, the cell concentration, PHB concentration, and PHB content reached 111.7 g (dry cell weight)/liter, 98.7 g/liter, and 88%, respectively, resulting in a productivity of 4.94 g of PHB/liter/h. The highest PHB productivity, 5.13 g/liter/h, was obtained after 16 h.     

可溶性TRAIL蛋白的高密度培养及补料策略研究

采用分批补料的方法高密度培养重组大肠杆菌C600/PbvTRAIL制备人可溶性TRAIL蛋白,优化发酵工艺,探索简单高效的分离纯化方法并测定蛋白生物活性。通过比较几种不同的补料策略：间歇流加、Dostat、pHstat,摸索了一种流加策略,即DOstatpHstat组合流加,有效的避免了发酵过程中,尤其是诱导表达阶段乙酸积累的增加,使TRAIL蛋白在高密度培养条件下,得到高效表达。菌体密度最终达到300g/L（WCW）以上,可溶性TRAIL蛋白占菌体总蛋白的4.2%,含量为1.1g/L。在整个发酵过程中,乙酸浓度接近于0,且未使用任何特殊手段,如纯氧、加压等,简化了发酵工艺,降低了发酵成本,为TRAIL的工业化生产创造了条件。     

碱性果胶酶在重组毕赤酵母中高效表达的关键因素研究

为提高重组毕赤酵母生产碱性果胶酶的产量和生产强度, 在摇瓶条件下优化了重组毕赤酵母生产碱性果胶酶的关键因素。结果表明, 以下条件：初始甘油浓度40 g/L、初始甲醇浓度3.1 g甲醇/g DCW、每24 h添加0.51 g甲醇/g DCW、诱导表达周期72 h、250 mL三角瓶诱导培养基装液量30 mL、初始pH 6.0, 最适于菌体生长与产物表达。在此基础上, 7 L罐上通过恒速流加甘油进一步提高细胞密度, 诱导阶段甲醇采取前期恒速流加和后期DO-stat, 发酵结束菌体干重达80 g/L, 酶活为217 U/mL, 比摇瓶结果提高了66.2%。     

碱性果胶酶在重组毕赤酵母中高效表达的关键因素研究

为提高重组毕赤酵母生产碱性果胶酶的产量和生产强度,在摇瓶条件下优化了重组毕赤酵母生产碱性果胶酶的关键因素。结果表明,以下条件：初始甘油浓度40g／L、初始甲醇浓度3.1g甲醇／gDCW、每24h添加0.51g甲醇／gDCW、诱导表达周期72h、250mL三角瓶诱导培养基装液量30mL、初始pH6,0,最适于菌体生长与产物表达。在此基础上,7L罐上通过恒速流加甘油进一步提高细胞密度,诱导阶段甲醇采取前期恒速流加和后期DO-stat,发酵结束菌体干重达80g／L,酶活为217U／mL,比摇瓶结果提高了66.2％。     

溶氧反馈分批补料高密度培养人骨形成蛋白-2工程菌

对表达人骨形成蛋白－2成熟肽的基因工程大肠杆菌E.coli DH5α/pDH-B2m在500mL摇瓶中进行了培养条件的摸索实验,并在此基础上扩大至NBS Bioflo IV20L发酵罐,利用溶氧反馈－分批补料培养技术：在培养过程中保持适当的溶解氧（40％）,以溶氧值在线反馈控制搅拌速度及流加补料培养基,使细菌保持适当的比生长率,成功地进行了工程菌的高密度培养,最终菌体密度达OD600＝57,每升干菌量22.8g,目的蛋白的表达量占细菌总蛋白的30％,人骨形成蛋白－2成熟肽的理论产率达到3.59g/L。