芽孢杆菌(Bacillus sp.)脂肽抗生素发酵工艺及分离纯化

微生物脂肽具有抗菌谱广、热稳定性高、低毒、低抗药性等优点,近年来受到国内外广泛关注。综述了芽孢杆菌脂肽抗生素的发酵和分离纯化工艺的最新研究进展。在发酵工艺中,培养基营养组成、发酵温度、搅拌转速和通气量等参数对脂肽的产量至关重要,碳源、氮源和金属离子的组成与配比都会影响芽孢杆菌的生长与产物的合成,适当控制搅拌转速和通气量可提高脂肽产量。此外,近年来一些新型发酵工艺,如泡沫回流、固定化细胞、无泡发酵、固态发酵等被用于脂肽生产,通过改进发酵方式,在降低成本的同时提高了脂肽抗生素产量。抗菌脂肽分离纯化的主要方法包括超滤、吸附、泡沫分离及色谱法等,这些方法相对于传统的酸沉和萃取,具有可连续生产、脂肽提取量高及成本低等优点。同时,多种纯化方法的组合应用大幅度提高了抗菌脂肽的提取效果,有效降低了成本,是脂肽抗生素分离提取的发展方向。     

脂肽的分离纯化与结构研究*

采用酸沉淀分离、有机溶剂提取、分级沉淀、脱色吸附及制备薄板的方法,从枯草芽孢杆菌HSO121的培养液中分离得到一种脂肽类化合物。茚三酮试验、红外光谱分析表明该脂肽具有环状结构,电喷雾离子化质谱结果显示,该脂肽是分子量为1022D和1036D的两个同系物,氨基酸分析及串联质谱分析表明,脂肽的肽链结构为Leu-Leu-AspValLeu-Leu-Glu,说明它是Surfactin的结构类似物。     

脂肽的分离纯化与结构研究

采用酸沉淀分离、有机溶剂提取、分级沉淀、脱色吸附及制备薄板的方法,从枯草芽孢杆菌HSO121的培养液中分离得到一种脂肽类化合物。茚三酮试验、红外光谱分析表明该脂肽具有环状结构,电喷雾离子化质谱结果显示,该脂肽是分子量为1,022D和1,036D的两个同系物,氨基酸分析及串联质谱分析表明,脂肽的肽链结构为Leu-Leu-Asp-Val-Leu-Leu-Glu,说明它是Surfactin的结构类似物。     

枯草芽孢杆菌HS-A38产抗菌脂肽Bacillomycin D的组分分析及鉴定

对一株枯草芽孢杆菌HS-A38产生的脂肽类物质进行分离鉴定及抑菌活性研究。通过酸沉淀分离和有机溶剂抽提的方法,从枯草芽孢杆菌HS-A38发酵液中得到脂肽粗提物LP,产率为1.956 g/L。利用薄层色谱和茚三酮染色法确定该脂肽粗提物中存在四个组分,分别为LP1、LP2、LP3和LP4;抑菌活性检测显示,组分LP3对两株海洋致病菌副溶血性弧菌和铜绿假单胞杆菌的活性较高。组分LP3经硅胶柱层析纯化分离后,应用反相高效液相色谱(RP-HPLC)和基质辅助激光解析电离飞行时间质谱(MALDI-TOF-MS)对该组分做进一步纯化和鉴定。分析表明,LP3样品在保留时间20 min~28 min产生单峰团LP3-1,其纯度为85.24%;经MALDI-TOF-MS分析和数据比对,组分LP3-1中的主要成分为杆菌霉素Bacillomycin D。     

海洋微生物抗菌脂肽及新生物农药研发

近年来,微生物脂肽作为生物农药的研究与应用,在国内外得到了广泛重视,成为今后生物农药发展的一个重要方向。从不同生境分离获得多批海洋微生物,通过筛选抗植物病原真菌活性强的菌株,发酵、分离、纯化及鉴定其代谢产物,从3种芽胞杆菌中发现了6个新的抗菌脂肽,属于iturins和fengycin类化合物。芽胞杆菌的芽胞及脂肽可研发防治植物真菌病害新生物农药。     

解淀粉芽孢杆菌TF28抗菌脂肽芬芥素的分离鉴定及抑菌作用

对一株解淀粉芽孢杆菌TF28产生的抗菌脂肽进行分离鉴定及抑菌活性研究,采用酸沉淀、乙酸乙酯和甲醇萃取技术制备了抗菌脂肽粗提物,经过2次HPLC分离纯化,在保留时间32～42min内获得8个抗菌脂肽纯品,经MALDI-TOF-MS鉴定为芬芥素(fengycins),对尖孢镰刀菌和禾谷镰刀菌显示出较强的抑菌活性,该研究为提高菌株TF28抗菌脂肽产量的定向遗传改造奠定基础。     

枯草芽孢杆菌JA脂肽类及挥发性物质抑菌效应的研究

枯草芽孢杆菌JA产生的脂肽类抗生素对植物病原真菌有广谱抗性.将发酵液经过酸沉淀、甲醇抽提以及反相高效液相色谱等步骤,分离得到脂肽类抗生素的纯品.经IC50实验和抗菌谱测定,考察了脂肽类抗生素对多种植物病原菌的作用,确定了脂肽类抗生素的抗菌谱.深入研究表明,枯草芽孢杆菌JA还产生未知成分的挥发性抑菌物质,能够抑制灰霉病菌孢子的萌发和菌丝的生长.脂肽类抗生素和挥发性抑菌物质的协同作用,有助于提高枯草芽孢杆菌的生物防治效果.     

混菌发酵芝麻粕制备芝麻多肽及其体外抗氧化活性研究

活性氧自由基(ROS)是细胞有氧代谢过程中产生的一类活性物,利用食源蛋白制备具有抗氧化能力的天然活性肽是当前的研究热点。本研究以机械冷榨芝麻粕为原料,比较了解淀粉芽孢杆菌、植物乳杆菌单菌及其混菌发酵芝麻粕制备芝麻多肽的过程,以DPPH·与·OH清除能力为评价指标,研究其体外抗氧化活性。数据表明,解淀粉芽孢杆菌、植物乳杆菌单菌及其混菌发酵芝麻粕36 h,芝麻多肽提取液中芝麻多肽的浓度分别达到9.841 mg/m L、11.620 mg/m L、14.412 mg/m L,DPPH·清除率分别是71.378%、77.013%、87.622%,·OH清除率分别是68.427%、82.507%、92.460%。因此,芝麻多肽具有较强的抗氧化活性,芝麻粕是制备抗氧化活性肽的良好原料;微生物发酵制备芝麻多肽时,解淀粉芽孢杆菌与植物乳杆菌混菌发酵显著优于单菌发酵,其多肽产量及DPPH·与·OH清除能力均优于相应单菌发酵。     

枯草芽孢杆菌JA脂肽类及挥发性物质抑菌效应的研究

枯草芽孢杆菌JA产生的脂肽类抗生素对植物病原真菌有广谱抗性。将发酵液经过酸沉淀、甲醇抽提以及反相高效液相色谱等步骤, 分离得到脂肽类抗生素的纯品。经IC50实验和抗菌谱测定, 考察了脂肽类抗生素对多种植物病原菌的作用, 确定了脂肽类抗生素的抗菌谱。深入研究表明, 枯草芽孢杆菌JA还产生未知成分的挥发性抑菌物质, 能够抑制灰霉病菌孢子的萌发和菌丝的生长。脂肽类抗生素和挥发性抑菌物质的协同作用, 有助于提高枯草芽孢杆菌的生物防治效果。     

聚合物纳米微球分离纯化放线菌素D的研究（英文）

本实验考察从链霉菌发酵产生的放线菌素D粗提物中分离制备高纯度放线菌素D的工艺,以聚合物纳米微球为固相载体,对聚合物纳米微球型号、洗脱条件进行优化。最终确立放线菌素D的分离纯化工艺为:采用PS40-300(以聚苯乙烯/二乙烯基苯聚合物为基质,粒径40μm,孔径300)纳米微球作为层析填料;以链霉菌发酵产生的放线菌素D粗提物为上样样品,用适量95%乙醇(V/V)充分溶解,上样量为0.5 g/100 m L,控制洗脱速度为5.0 m L/min,以65%乙醇水(V/V)洗脱,收集纯度95%以上的洗脱液,真空浓缩得到高纯度的放线菌素D。结果表明该分离纯化工艺,纯度与收率都较高,流程简单、可行,为该产品产业化开发奠定基础。     

产胶原酶的蜡样芽胞杆菌发酵条件优化及酶的分离纯化

【目的】优化蜡样芽胞杆菌R75E菌株产胶原酶的条件,并通过蛋白分离纯化技术获得高纯度胶原酶。【方法】利用单因素及正交试验优化蜡样芽胞杆菌R75E产胶原酶的发酵条件及发酵培养基,将发酵液离心除菌后得到粗酶液,对其依次通过硫酸铵分级沉淀、Butyl FF疏水层析及SuperdexTM 200凝胶过滤层析等方法对目标胶原酶进行分离纯化,利用SDS-PAGE电泳检测其纯度。【结果】优化后发酵条件为培养温度41°C、接种量6%、培养时间36 h,优化后发酵培养基为葡萄糖10 g/L、蛋白胨5 g/L、起始p H 7.0,粗酶液酶活力较优化前提高了2.9倍;将该粗酶液经过一系列纯化后得到纯度超过90%的胶原酶产物,其纯化倍数和回收率分别为18.4和1.1%。【结论】获得蜡样芽胞杆菌R75E的最佳产酶条件,并对胶原酶分离纯化的方法进行了探索,为微生物胶原酶的开发应用奠定基础。     

Bacillus amyloliquefaciens ES-2发酵产抗菌脂肽消泡剂的筛选及脂肽的提取和纯化

将大豆油、有机硅消泡剂和聚醚类消泡剂3种消泡剂分别用于Bacillus amyloliquefaciens ES-2抗菌脂肽发酵,研究表明大豆油既可以实现消泡,又有利于抗菌脂肽的发酵,使其产量达到了2497.67mg/L。经过提取得到纯度为55.68%的产品,提取率达到88.72%。此外还比较了不同大孔树脂对抗菌脂肽吸附和解吸附效果,发现大孔树脂X-5最适合抗菌脂肽的纯化。纯化的工艺参数为:上样浓度14.4mg/ml、上样速率1ml/min,洗脱速率2ml/min、洗脱剂用量2.5BV,产品的回收率达90.01%,纯度达74.4%。     

Purification and some properties of an extracellular ribonuclease with antiviral activity against tobacco mosaic virus from <Emphasis Type="Italic">Bacillus cereus</Emphasis>

A new ribonuclease (RNase) with tobacco mosaic virus inhibition was isolated and purified from Bacillus cereus ZH14 through ammonium sulfate precipitation, ultrafiltration, ion-exchange chromatography of DEAE-Sephadex A-50 column, and gel chromatography of Sephacryl S-200HR column. The enzyme was purified approximately 134-fold with a recovery of 9.2%. The RNase had an MW of 75.6 kDa in SDS-PAGE, which differed from RNases reported previously. The inhibitory activity of the RNase in the purification process against tobacco mosaic virus was tested, and the percentage inhibition of the purified RNase (48 U/ml) reached 90%. The protein could tolerate 90°C and pH 4.0.     

Development of a process for large-scale purification of C-phycocyanin from Synechocystis aquatilis using expanded bed adsorption chromatography

In this paper a large and scaleable method for purification of C-phycocyanin (C-PC) from the cyanobacteria Synechocystis aquatilis has been developed. Phycobiliproteins are extracted from the cells by osmotic shock and separated by passing the centrifuged cell suspension through an expanded bed adsorption chromatography (EBAC) column using Streamline-DEAE as adsorbent. The eluted C-PC rich solution is finally purified by packed-bed chromatography using DEAE-cellulose. Optimal extraction is achieved using phosphate 0.05 M buffer pH 7.0 twice. The operation of EBAC is optimized on a small scale using a column of 15 mm internal diameter (I.D.). The optimal conditions are a sample load of 4.9 mg C-PC/mL adsorbent, an expanded bed volume twice the settled bed volume and a sample viscosity of 1.020 mP. The EBAC process is then scaled up by increasing the column I.D. (15, 25, 40, 60 and 90 mm) and the success of the scale-up process is verified by determining the protein breakthrough capacity and product recovery. The yield of the EBAC step is in the range of 90-93% for every column diameter. To obtain pure C-PC, conventional ion-exchange chromatography with DEAE-cellulose is utilized and a yield of 74% is obtained. The overall yield of the process, comprising all steps, is 69%. The purification steps are monitored using SDS-PAGE and the purity of recovered C-PC is confirmed by absorption and emission spectroscopy and RP-HPLC. Results show that EBAC method is a scalable technology that allows large quantities of C-PC to be obtained without product loss, maintaining a high protein recovery while reducing both processing cost and time.     

Large-scale purification of recombinant human angiostatin

A process for the purification of recombinant human angiostatin (rhAngiostatin), produced by Pichia pastoris fermentation operated at the 2000-L scale, is reported. rhAngiostatin was recovered and purified directly from crude fermentation broth by cation exchange expanded bed adsorption chromatography. Anion exchange chromatography, hydroxyapatite chromatography, and hydrophobic interaction chromatography were used for further purification. Full-length rhAngiostatin was separated from rhAngiostatin molecules fragmented by endoproteolysis. On average, 140 g of rhAngiostatin was produced per batch, with an overall yield of 59% (n = 9). The purification process was completed in approximately 48 h and used only inexpensive and nontoxic raw materials. Methods development, process synthesis, and process scale-up data are presented and discussed.     

正辛酸沉淀在单克隆抗体纯化中的工艺优化与应用

为应对治疗性抗体快速增长的市场需求,抗体上游细胞培养规模和表达量水平已显著提高,而下游纯化工艺的生产效率则相对落后,下游处理能力已成为限制抗体产能的瓶颈。本研究以单克隆抗体mab-X为实验材料,优化了细胞培养液、低pH病毒灭活收集液2种模式的正辛酸(caprylic acid,CA)沉淀工艺条件,并研究了CA处理去除聚体、CA处理灭活病毒等2种应用,在小试的基础上,采用低pH病毒灭活收集液CA沉淀的模式进行了500 L细胞培养规模生产放大研究,对沉淀前后的产品质量和收率进行了检测和对比。结果显示,两种模式的CA沉淀均可显著降低宿主细胞蛋白(host cell protein,HCP)残留和聚体含量,在聚体去除实验中CA沉淀可去除约15%的聚体,病毒灭活研究显示CA对逆转录模型病毒具有完全的病毒灭活能力。在放大生产规模中,下游依次进行了深层过滤收获、亲和层析、低pH病毒灭活、CA沉淀及深层过滤、阳离子交换层析,CA沉淀过程中混合时间和搅拌速度显著影响CA沉淀效果,CA沉淀处理后低pH病毒灭活液中的HCP残留量降低了895倍,沉淀后产品纯度和HCP残留均已控制在单克隆抗体质量要求范围内,CA沉淀可以减少传统纯化工艺中的一个精纯步骤。总之,下游工艺中采用CA沉淀,能够精简传统纯化工艺,并完全满足mab-X的纯化质量要求,而且能提高生产效率、降低生产成本。本研究结果将推动CA沉淀在单克隆抗体下游纯化生产中的应用,为解决目前传统纯化工艺的问题提供参考。     

Isolation and structural analysis of bamylocin A, novel lipopeptide from Bacillus amyloliquefaciens LP03 having antagonistic and crude oil-emulsifying activity

Bacillus amyloliquefaciens strain LP03 isolated from soil, produced an antagonistic compound that strongly inhibited the growth of plant-pathogenic fungi and a lipopeptide biosurfactant. Also, isolated strain LP03 had a marked crude oil-emulsifying activity as it developed a clear zone around the colony after incubation for 24 h at 37°C. LP03 was identified as Bacillus amyloliquefaciens by analysis of partial 16 S rRNA gene and partial gyrA gene sequence. The lipopeptide was purified by acid precipitation of cell-free culture broth, extraction of the precipitates with methanol, silica gel column chromatography, and reverse-phase, high-pressure liquid chromatography. The purified biosurfactant was analyzed biochemical structure by matrix-assisted laser desorption/ionization time-of-flight mass spectrometry (MALDI-TOF) and electrospray ionization mass spectrometry/mass spectrometry (ESI-MS/MS). The masses of the two peaks were observed by HPLC chromatography. Their masses were determined to be 1,044 and 1,058 m/z with MALDI-TOF mass spectrometry. As constituents of the peptide and lipophilic part of the m/z 1,022.6, seven amino acids (Glu-Leu-Met-Leu-Pro-Leu-Leu) and β-hydroxy-C13 fatty acid were determined by ESI-MS/MS. The lipopeptide of 1,022.6 Da differed from surfactins in the substitution of leucine, valine and aspartic acid in positions 3, 4, and 5 by methionine, leucine, and proline, respectively. Novel lipopeptide was designated as bamylocin A.     

Purification of an acidic recombinant protein from transgenic tobacco

Tobacco has proven to be a promising alternative for the production of recombinant therapeutic proteins and offers numerous advantages over other plants as a host system. However, the recovery and purification steps needed to obtain a protein at high recovery and purity have not been well investigated. In this study, a process was developed to purify a model acidic protein, recombinant beta-glucuronidase (rGUS) from transgenic tobacco leaf tissue, in three main steps after extraction: polyelectrolyte precipitation, hydrophobic interaction chromatography (HIC), and hydroxyapatite chromatography (HAC). Using this three-step process, up to 40% of the initial rGUS activity could be recovered to near homogeneity as judged by SDS-PAGE. This work demonstrates that acidic recombinant proteins expressed in tobacco may be purified to high yield with high purity in a minimal amount of steps that are suitable for scale-up. Furthermore, the general steps used in this process may suggest that a wide variety of acidic recombinant proteins may be purified in a similar manner from transgenic tobacco or other leafy crops.     

Evaluation of different primary recovery methods for E. coli-derived recombinant human growth hormone and compatibility with further down-stream purification

Due to advances in fermentation technology, it is now possible to obtain fermentation broth with over 30% solids. The high solid content makes the clarification step difficult, especially at large scale. The primary protein recovery step is challenging due to the heterogeneous solution of soluble and insoluble material. In this study, we compare different primary recovery routes and the compatibility with the initial capture chromatography step. The primary recovery routes studied are standard clarification by centrifugation and extraction in aqueous two-phase systems. The compatibility of the feed streams from the different primary recovery steps with the first chromatography step is addressed. An anion-exchange column was used as the first capture column in the purification process. The aqueous two-phase system was composed of a random copolymer of ethylene oxide and propylene oxide (EOPO) in combination with a waxy starch. The target protein in this study was human growth hormone (hGH) produced in recombinant Escherichia coli. The purity of hGH in the top phase after aqueous two-phase extraction was found to be significantly higher than in clarified homogenate supernatant and increased as the EOPO polymer concentration in the aqueous two-phase system increased. Stability of the supernatant and EOPO top phases and hGH were determined by turbidity measurements and LC-MS assay. All of the feed-streams from the primary recovery steps were compatible with the anion-exchange chromatography step; however, the capacity of the resin was strongly dependent on the purity of the load. Different process aspects, e.g., resin capacity, viscosity, purification, and yield of hGH and scalability are compared.