重组毕赤酵母高密度发酵表达H5N1禽流感病毒糖蛋白

在10L发酵罐中,对高致病性禽流感病毒H5N1糖蛋白HA1在重组毕赤酵母中的表达发酵工艺进行了研究。通过分批补料培养方法探讨不同培养温度、诱导温度、补料方式、微量元素等因素对菌体的生长以及重组蛋白表达和活性的影响。结果表明,菌种培养和诱导温度均为25oC时,菌体的生长、分泌表达量和与广谱中和抗体的反应活性较好;微量元素是影响重组HA1蛋白生物活性的重要因素;通过优化高密度发酵工艺,H5N1病毒糖蛋白HA1在发酵罐中的表达量比摇瓶培养提高10.5倍,达到约120mg/L,为大规模制备高致病性禽流感病毒的HA1蛋白奠定了基础。     

基因工程菌生产重组人组织因子的发酵研究

根据表达重组人组织因子基因工程菌的自身特点,在30L发酵罐上,通过控制发酵pH、葡萄糖浓度、诱导物磷酸浓度、搅拌速度及采用分批补料等方法,对重组人组织因子基因工程菌高密度发酵和高效表达的条件进行了研究。实验结果表明:诱导物终浓度低于0.1mmol/L,菌体密度OD60014,发酵周期10.5h,基因工程菌批发酵平均产量为37.41g/L,重组人组织因子表达量为6.56 mg/L。关键词:基因工程菌;高密度发酵;组织因子     

毕赤酵母发酵生产颗粒性乙肝表面抗原的条件优化

乙型肝炎病毒的流行对人们的生命健康造成了极大的威胁, 而有效准确的诊断和预防性疫苗是阻止其流行的主要手段, 乙肝表面抗原是诊断试剂和疫苗的主要成分。本试验在构建稳定表达HBsAg的毕赤酵母菌株后, 对其发酵条件进行了研究。采用摇瓶分批培养方法, 探讨了不同培养基、溶解氧、诱导物甲醇的浓度以及pH值等因素对菌体生长与重组蛋白表达的影响。在10 L发酵罐上采用分批补料培养的方法研究了进行扩大培养生产重组HBsAg。结果表明, FBS无机盐合成培养基是理想的工业发酵培养基, 溶解氧对菌体的生长与表达有显著的影响, 甲醇诱导最佳终浓度为1% (V/V), 发酵的最适pH值为5.4~6.0。发酵罐放大培养后, ELISA和 SDS-PAGE分析表明重组HBsAg获得了高效表达, 最终菌体生物量达到310 OD600, 表达量达到27 mg/L。电子显微镜观察表达重组乙肝抗原可以自组装为22 nm类病毒颗粒, 为HBV的新一代早期血清学诊断和疫苗的大规模生产提供了一定的参考。     

50L规模中试发酵重组核苷二磷酸激酶A工程菌

中试规模发酵重组人核苷二磷酸激酶A（rhNDPK-A）工程菌,并对表达产物进行纯化。摇瓶培养一级种子至合适密度,以10%比例接种二级种子培养基,在7L发酵罐中培养至OD600为9.6～10.5,然后转入80L发酵罐中进行补料分批培养,所得菌体裂解后,经离子交换层析和亲和层析两步纯化得重组蛋白制品。结果表明,50L培养液经过10h培养后,湿菌收量为1560 g/批,NDPK-A表达量为23.8%。另外,补料方式对发酵密度有明显影响。与单纯补加碳源相比,同时补加碳源和氮源可以显著提高菌体产量,但对目的蛋白表达量地提高不明显。在较优条件下,菌体产量为(2220.00±169.71) g/批,蛋白表达量为(22.00±0.42) %,纯化后重组蛋白得率为510mg/L。产物可溶、密度适中、工艺简便的中试发酵条件的建立为高得率、大规模制备重组rhNDPK-A奠定了基础。     

乳糖诱导的重组人血管内皮抑素(rhEndostatin)蛋白的表达

研究用乳糖替代IPTG作为诱导剂进行重组蛋白的表达,观察乳糖对乳糖操纵子调控的基因工程菌发酵及重组血管内皮抑素表达的影响,从而选取最佳诱导表达条件。以重组人血管内皮抑素表达工程菌pETrhEN/BL21(DE3)作为研究对象,分别用IPTG和乳糖作为诱导剂,在摇瓶中进行表达实验。并对重组蛋白质表达量进行分析。然后在5 L发酵罐中进行验证。在摇瓶培养条件下,乳糖浓度大于0.5 g/L即可以诱导目的蛋白的表达。乳糖浓度1 g/L时诱导目的蛋白表达量与1 mmol/L的IPTG相当,当乳糖浓度为10 g/L,目的蛋白表达量达到最大。在发酵罐培养条件下,补料4 h后葡萄糖浓度基本耗尽,此时开始加入乳糖。诱导后1 h,即有重组蛋白表达,在诱导后4 h达到高峰(占菌体可溶性蛋白的56%),与此同时,诱导后5 h菌体浓度也达到最高值。在以乳糖操纵子为调控手段的工程菌表达系统中,可以使用乳糖作为诱导剂,诱导应在葡萄糖消耗完后进行。     

大肠杆菌发酵生产重组人源抗-HBs Fab

在KLF2000发酵罐中利用补料分批培养技术培养表达含重组质粒pBAD/HBs Fab的TOP10大肠杆菌,生产人源抗-HBs Fab,为批量生产作准备,在发酵过程中,控制溶氧30%以上,温度37℃,在基础培养基内生长4h后,补加以甘油为碳源的补料,继续生长到9h,加入阿拉伯糖,至终浓度为0.02%,30℃诱导表达5h,收集菌体,纯化制备目的蛋白。利用Western blot方法检测Fab抗原性,Dot blot方法检测生物学活性。14h发酵结束后,菌体密度最终达96g/L,纯化所得蛋白大约占菌体总蛋白的6%,含量为80mg/L,以重组质粒pBAD/HBs Fab,大肠杆菌TOP10表达表达比率与摇瓶相比没有降低,表达量达80mg/L左右,为大批量生产作了准备。     

幽门螺杆菌尿素酶B亚单位基因工程菌发酵工艺的研究

通过不同培养基、不同葡萄糖浓度、不同溶氧条件、补料与非补料对幽门螺杆菌尿素酶B亚单位(UreB)基因工程菌的菌体生长与外源蛋白表达量的影响的比较 ,建立了稳定、适宜的幽门螺杆菌尿素酶B亚单位基因工程菌发酵工艺。多批实验结果证明 ,菌体单产可达 86 g/L ,目的蛋白的表达率为 38.2 %。     

利用重组大肠杆菌生产人生长激素发酵工艺的研究

在摇瓶培养和发酵罐培养条件下,研究了E.coli/BL21(DE3)/pET30a(+)-hGH工程菌的不同发酵工艺条件。确立了该工程菌的最优化工艺参数:M9-2培养基,37℃、pH值为6.8-7.4、诱导起始菌体密度为OD600达3.0-4.0,IPTG浓度为1mmol/L,诱导时溶氧控制为50%以上,补料为10%甘油、5%Yeast extract和5%Tryptone。该工艺条件经过连续三批发酵,证实稳定可行,目的蛋白在胞间质呈可溶性表达,表达量占菌体总蛋白的20%以上。     

生物转化合成苯乳酸工程菌的培养条件优化

本研究旨在优化重组大肠杆菌Escherichia coli BL21 (DE3) harboring pRSF-aad-ldh10-fdh菌株的培养条件,获得高密的供生物转化苯丙氨酸为苯乳酸的细胞。实验考察了摇瓶发酵培养基碳源、氮源种类和浓度,3 L发酵罐中转速和通气量及恒速补料、DO-stat和pH-stat等不同分批补料策略对菌体密度的影响。结果表明,当碳源为4 g/L葡萄糖,氮源为24 g/L安琪酵母浸粉FM802,细胞干重最大可达9.24 g/L;当转速为400 r/min和通气量为1.5 vvm时,细胞干重最大可达10.18 g/L;以4 g/(L·h)恒速流加葡萄糖时,细胞干重最大可达13.71 g/L。本研究还对工程菌酶表达的诱导条件进行了优化,菌体培养2 h后,添加终浓度为0.08 mmol/L IPTG诱导剂,在25℃下诱导培养14 h所得细胞有利于生物转化。底物苯丙氨酸浓度为60 g/L,转化为苯丙酮酸的转化率为50.2%,转化为苯乳酸的转化率为35.2%。     

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。     

Kinetics of inclusion body production in batch and high cell density fed-batch culture of Escherichia coli expressing ovine growth hormone.

A process for maximizing the volumetric productivity of recombinant ovine growth hormone (r-oGH) expressed in Escherichia coli during high cell density fermentation process has been devised. Kinetics of r-oGH expression as inclusion bodies and its effect on specific growth rates of E. coli cells were monitored during batch fermentation process. It was observed that during r-oGH expression in E. coli, the specific growth rate of the culture became an intrinsic property of the cells which reduced in a programmed manner upon induction. Nutrient feeding during protein expression phase of the fed-batch process was designed according to the reduction in specific growth rate of the culture. By feeding yeast extract along with glucose during fed-batch operation, high cell growth with very little accumulation of acetic acid was observed. Use of yeast extract helped in maintaining high specific cellular protein yield which resulted in high volumetric productivity of r-oGH. In 16 h of fed-batch fermentation, 3.2 g l-1 of r-oGH were produced at a cell OD of 124. This is the highest concentration of r-oGH reported to date using E. coli expression system. The volumetric productivity of r-oGH was 0.2 g l-1 h-1, which is also the highest value reported for any therapeutic protein using IPTG inducible expression system in a single stage fed-batch process.     

Proposed mechanism of acetate accumulation in two recombinant Escherichia coli strains during high density fermentation

The productivity of Escherichia coli as a producer of recombinant proteins is affected by its metabolic properties, especially by acetate production. Two commercially used E. coli strains, BL21 (lambdaDE3) and JM109, differ significantly in their acetate production during batch fermentation at high initial glucose concentrations. E. coli BL21 grows to an optical density (OD, 600 nm) of 100 and produces no more than 2 g/L acetate, while E. coli JM109 grows to an OD (600 nm) of 80 and produces up to 14 g/L acetate. Even in fed-batch fermentation, when glucose concentration is maintained between 0.5 and 1.0 g/L, JM109 accumulates 4 times more acetate than BL21. To investigate the difference between the two strains, metabolites and enzymes involved in carbon utilization and acetate production were analyzed (isocitrate, ATP, phosphoenolpyruvate, pyruvate, isocitrate lyase, and isocitrate dehydrogenase). The results showed that during batch fermentation isocitrate lyase activity and isocitrate concentration were higher in BL21 than in JM109, while pyruvate concentration was higher in JM109. The activation of the glyoxylate shunt pathway at high glucose concentrations is suggested as a possible explanation for the lower acetate accumulation in E. coli BL21. Metabolic flux analysis of the batch cultures supports the activity of the glyoxylate shunt in E. coli BL21.     

High-level production of human leptin by fed-batch cultivation of recombinant Escherichia coli and its purification.

Human leptin is a 16-kDa (146-amino-acid) protein that is secreted from adipocytes and influences body weight homeostasis. In order to obtain high-level production of leptin, the human obese gene coding for leptin was expressed in Escherichia coli BL21(DE3) under the strong inducible T7 promoter. The recombinant leptin was produced as inclusion bodies in E. coli, and the recombinant leptin content was as high as 54% of the total protein content. For production of recombinant human leptin in large amounts, pH-stat fed-batch cultures were grown. Expression of leptin was induced at three different cell optical densities at 600 nm (OD600), 30, 90, and 140. When cells were induced at an OD600 of 90, the amount of leptin produced was 9.7 g/liter (37% of the total protein). After simple purification steps consisting of inclusion body isolation, denaturation and refolding, and anion-exchange chromatography, 144.9 mg of leptin that was more than 90% pure was obtained from a 50-ml culture, and the recovery yield was 41.1%.     

HER2胞外段的克隆与原核表达

应用RT-PCR技术从人乳腺癌细胞系SK-BR-3中克隆出人表皮生长因子受体2(human epidermal growth factorreceptor 2,HER2)基因的胞外段,并插入到表达载体pET-30a中,得到重组表达载体pET30-HER2(Ex)。将该载体转化至大肠杆菌BL21(DE3)细胞中,加入IPTG进行诱导表达,成功获得HER2胞外段蛋白。分别提取培养液上清、大肠杆菌周质腔、细胞质可溶性及不可溶性组分蛋白进行SDS-PAGE电泳分析,确定目的蛋白定位于大肠杆菌细胞质包涵体中。通过改变诱导温度、诱导物浓度、诱导起始菌体密度和诱导时间,寻找最佳表达条件,使目的蛋白的表达量达到最高。结果表明,在37℃下,OD600达到1.0时,经终浓度为0.1 mmol/L的IPTG诱导4 h,目的蛋白的表达量最高。将重组表达菌进行超声破碎,分离出包涵体组分,经Ni2+亲和层析纯化后获得了纯度>90%的HER2胞外段蛋白,从而为抗HER2抗体的制备及肿瘤疫苗的研究奠定了基础。     

Direct chemical extraction of a recombinant viral coat protein from Escherichia coli at high cell density.

The release of protein and DNA from nonrecombinant E. coli JM101 and recombinant E. coli HMS174(DE3) expressing L1 (the major viral coat protein of human papillomavirus type 16) as an inclusion body was demonstrated at high cell density (OD(600) = 160). For the nonrecombinant strain, extraction efficiency decreased significantly as cell mass increased, with a high viscosity increase in the postextraction broth. A different dependence on cell concentration was observed for the recombinant strain, with total protein extraction efficiency exceeding 85% for both uninduced and induced cells. Almost complete release of the recombinant L1 protein was achieved at high cell concentration (OD(600) = 80 approximately 160) without the use of reducing agent. This greatly extends the concentration range for chemical extraction.     

Optimization of inclusion body solubilization and renaturation of recombinant human growth hormone from Escherichia coli

Recombinant human growth hormone (r-hGH) was expressed in Escherichia coli as inclusion bodies. In 10 h of fed-batch fermentation, 1.6 g/L of r-hGH was produced at a cell concentration of 25 g dry cell weight/L. Inclusion bodies from the cells were isolated and purified to homogeneity. Various buffers with and without reducing agents were used to solubilize r-hGH from the inclusion bodies and the extent of solubility was compared with that of 8 M urea as well as 6 M Gdn-HCl. Hydrophobic interactions as well as ionic interactions were found to be the dominant forces responsible for the formation of r-hGH inclusion bodies during its high-level expression in E. coli. Complete solubilization of r-hGH inclusion bodies was observed in 100 mM Tris buffer at pH 12.5 containing 2 M urea. Solubilization of r-hGH inclusion bodies in the presence of low concentrations of urea helped in retaining the existing native-like secondary structures of r-hGH, thus improving the yield of bioactive protein during refolding. Solubilized r-hGH in Tris buffer containing 2 M urea was found to be less susceptible to aggregation during buffer exchange and thus was refolded by simple dilution. The r-hGH was purified by use of DEAE-Sepharose ion-exchange chromatography and the pure monomeric r-hGH was finally obtained by using size-exclusion chromatography. The overall yield of the purified monomeric r-hGH was approximately 50% of the initial inclusion body proteins and was found to be biologically active in promoting growth of rat Nb2 lymphoma cell lines.     

High throughput purification of recombinant human growth hormone using radial flow chromatography

Recombinant human growth hormone (r-hGH) was expressed in Escherichia coli as inclusion bodies. Using fed-batch fermentation process, around 670 mg/L of r-hGH was produced at a cell OD600 of 35. Cell lysis followed by detergent washing resulted in semi-purified inclusion bodies with more than 80% purity. Purified inclusion bodies were homogenous in preparation having an average size of 0.6 μm. Inclusion bodies were solubilized at pH 12 in presence of 2 M urea and refolded by pulsatile dilution. Refolded protein was purified with DEAE-anion exchange chromatography using both radial and axial flow column (50 ml bed volume each). Higher buffer flow rate (30 ml/min) in radial flow column helped in reducing the batch processing time for purification of refolded r-hGH. Radial column based purification resulted in high throughput recovery of diluted refolded r-hGH in comparison to axial column. More than 40% of inclusion body protein could be refolded into bioactive form using the above method in a single batch. Purified r-hGH was analyzed by mass spectroscopy and found to be bioactive by Nb2 cell line proliferation assay. Inclusion body enrichment, mild solubilization, pulsatile refolding and radial flow chromatography worked co-operatively to improve the overall recovery of bioactive protein from inclusion bodies.     

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。     

Coexpression of folding accessory proteins for production of active cyclodextrin glycosyltransferase of Bacillus macerans in recombinant Escherichia coli

Coexpression of folding accessory proteins, molecular chaperones, and human peptidyl-prolyl cis-trans isomerase (PPIase) increased production of active cyclodextrin glycosyltransferase (CGTase) of Bacillus macerans, which is otherwise mainly expressed as inclusion body in recombinant Escherichia coli. The best partner for soluble expression of CGTase was found to be human PPIase followed by coexpression of DnaK-DnaJ-GrpE together with GroEL-GroES. Such a significant enhancement by human PPIase coexpression seemed to be due to dual functions of chaperone and peptidyl-prolyl cis-trans isomerization. Coexpression of GroEL-GroES or minichaperone alone did not influence the specific CGTase activity. For production of active CGTase in large amounts, a high cell density culture was achieved using a pH-stat fed-batch strategy. The optimized fed-batch fermentation resulted in dry cell weight of 103.4 g/L and CGTase activity of 1200 U/mL. Combination of human PPIase expression at a gene level and cell culture optimization at a process scale exerted a synergistic effect on the product yield of soluble CGTase expression in recombinant E. coli.