疏水层析结合冷乙醇沉淀纯化人血清白蛋白

将层析技术与冷乙醇工艺相结合用于人血清白蛋白的纯化 ,对各过程所采用的层析介质及层析条件进行了探索 ,得到了一条从人血浆中制备血清白蛋白的新路线 :将一步冷乙醇沉淀后的血浆上清进行脱盐除乙醇 ,用阳离子交换介质CMSepharoseFF以透过式层析的模式吸附非白蛋白组分 ,最后选用ButylSepharoseFF一步疏水层析后所得样品经SDS-PAGE银染显示一条单带 ,分析其纯度大于 99% ,计算工艺收率为 81.2%。与传统冷乙醇工艺相比较 ,该工艺最终样品纯度更高 ,且层析可以在常温下操作 ,易实现自动化控制.     

A novel Method for the selective recovery and purification of γ‐polyglutamic acid from Bacillus licheniformis fermentation broth

Microbially produced gamma‐polyglutamic acid (γ‐PGA) is a commercially important biopolymer with many applications in biopharmaceutical, food, cosmetic and waste‐water treatment industries. Owing to its increasing demand in various industries, production of γ‐PGA is well documented in the literature, however very few methods have been reported for its recovery. In this paper, we report a novel method for the selective recovery and purification of γ‐PGA from cell‐free fermentation broth of Bacillus licheniformis. The cell‐free fermentation broth was treated with divalent copper ions, resulting in the precipitation of γ‐PGA, which was collected as a pellet by centrifugation. The pellet was resolubilized and dialyzed against de‐ionized water to obtain the purified γ‐PGA biopolymer. The efficiency and selectivity of γ‐PGA recovery was compared with ethanol precipitation method. We found that 85% of the original γ‐PGA content in the broth was recovered by copper sulfate‐induced precipitation, compared to 82% recovery by ethanol precipitation method. Since ethanol is a commonly used solvent for protein precipitation, the purity of γ‐PGA precipitate was analyzed by measuring proteins that co‐precipitated with γ‐PGA. Of the total proteins present in the broth, 48% proteins were found to be co‐precipitated with γ‐PGA by ethanol precipitation, whereas in copper sulfate‐induced precipitation, only 3% of proteins were detected in the final purified γ‐PGA, suggesting that copper sulfate‐induced precipitation offers better selectivity than ethanol precipitation method. Total metal content analysis of the purified γ‐PGA revealed the undetectable amount of copper ions, whereas other metal ions detected were in low concentration range. The purified γ‐PGA was characterized using infrared spectroscopy. © 2010 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

Cationic polymer precipitation for enhanced impurity removal in downstream processing

Precipitation can be used for the removal of impurities early in the downstream purification process of biologics, with the soluble product remaining in the filtrate through microfiltration. The objective of this study was to examine the use of polyallylamine (PAA) precipitation to increase the purity of product via higher host cell protein removal to enhance polysorbate excipient stability to enable a longer shelf life. Experiments were performed using three monoclonal antibodies (mAbs) with different properties of isoelectric point and IgG subclass. High throughput workflows were established to quickly screen precipitation conditions as a function of pH, conductivity and PAA concentrations. Process analytical tools (PATs) were used to evaluate the size distribution of particles and inform the optimal precipitation condition. Minimal pressure increase was observed during depth filtration of the precipitates. The precipitation was scaled up to 20L size and the extensive characterization of precipitated samples after protein A chromatography showed >75% reduction of host cell protein (HCP) concentrations (by ELISA), >90% reduction of number of HCP species (by mass spectrometry), and >99.8% reduction of DNA. The stability of polysorbate containing formulation buffers for all three mAbs in the protein A purified intermediates was improved at least 25% after PAA precipitation. Mass spectrometry was used to obtain additional understanding of the interaction between PAA and HCPs with different properties. Minimal impact on product quality and <5% yield loss after precipitation were observed while the residual PAA was <9 ppm. These results expand the toolbox in downstream purification to solve HCP clearance issues for programs with purification challenges, while also providing important insights into the integration of precipitation–depth filtration and the current platform process for the purification of biologics.     

Continuous fractionation of human plasma.

Continuous processing has been applied to human plasma fractionation by the cold ethanol process. On-line pH control of +/- 0.05 pH units, flow control of +/- 1%, and temperature control of +/- 0.5 degree C have been achieved. Optimization of precipitation pHs has been carried out for purifying plasma protein fractions and albumin. During precipitation, the irreversible nature of the pH overshoots has been demonstrated. Compared to the batch processing mode, the continuous scheme produces an increased yield between 6 to 11%.     

人血清白蛋白纯化技术研究进展

本文综述了国内外关于血浆人血清白蛋白（pHSA）和基因重组人血清白蛋白（rHSA）分离纯化的进展和发展趋势。以冷乙醇沉淀为主的pHSA分离方法仍是目前多数工业采用的工艺,但近年来发展的离子交换色谱、凝胶过滤色谱、亲和色谱等多种色谱分离技术具有自动化程度高、生产周期短、更符合GMP等特点,正在逐步取代传统的冷乙醇沉淀法。当前用基因工程技术表达的人血清白蛋白对分离纯化提出了新的挑战。为获得高纯度、安全、稳定的产品,各种色谱分离技术得到更多的应用,其中扩张床离子交换色谱可以省去离心、过滤等传统固液分离操作。尽管rHSA的纯化技术已有一定的发展,但纯化过程仍需进一步优化以提高产品纯度及收率。     

Purification of a High Molecular Weight Kininogen from Rat Plasma

A high molecular weight kininogen has been isolated from rat plasma and purified. At each preparative step the kininogen concentration and purity were monitored by assay on the perfused isolated rat uterus in terms of bradykinin equivalents formed per mg protein following incubation of the plasma fractions with rodent acid protease for 24 hours at 37 and pH 4.0. Kinin formation by crystalline trypsin and human pancreatic kallikrein also was compared. Citrated rat plasma first was precipitated with 43% ammonium sulfate. The kininogen fractions then were subjected to a series of gel filtration ion exchange chromatographic columns that included G-200 Sephadex, G-200: G-100 Sephadex interconnected columns, DEAE-A50 Sephadex, and hydroxylapatite. The kininogen fractions finally were subjected to preparative polyacrylamide gel electrophoresis, resulting in a final purification of 92.9-fold compared to the initial rat plasma. A single major kininogen protein band and a minor band of protein impurity were obtained on disc gel electrophoresis. Only the pancreatic kallikrein did not form kinin from this purified kininogen. The apparent molecular weight was estimated by SDS polyacrylamide gel technique to be 110,000.     

Evaluation of the effect of crude extract purity and pure paclitaxel content on the increased surface area fractional precipitation process for the purification of paclitaxel

This study evaluated the effect of crude extract purity and pure paclitaxel content on the behavior in terms of purity, yield, fractional precipitation time, and precipitate shape and size of fractional precipitation in the increased surface area fractional precipitation process for the purification of paclitaxel. With increased pure paclitaxel content and crude extract purity, the purity and yield of paclitaxel were improved and the fractional precipitation time was reduced. Regardless of changes in crude extract purity and pure paclitaxel content, it was possible to obtain a small paclitaxel precipitate size by hindering the growth of precipitate particles using an ion exchange resin to increase the surface area. In addition, according to the type of surface-area increasing substance used, precipitate size and shape differed because of a differing affinity for the paclitaxel particles. The lower the crude extract purity and pure paclitaxel content, the higher the yield and the improvement in purity in the process of increased surface area fractional precipitation, with a greater effect on the decrease in paclitaxel particle size.     

Purification of heparin,dermatan sulfate and chondroitin sulfate from mixtures by sequential precipitation with various organic solvents

Heparin, dermatan sulfate and chondroitin sulfate in mixtures were fractionated by sequential precipitation with methanol, ethanol and propanol. The recovered fractions from 0.1 to 2.0 volumes of various solvents were analyzed by agarose-gel electrophoresis and densitometric analysis. Heparins with different relative percentages of slow-moving and fast-moving components were precipitated from 0.5 to 0.7 volumes of methanol, and in this range of volumes, the amount of slow-moving component of heparin decreases and that of the fast-moving species increases. From 0.8 to 1.6 volumes of methanol, mixtures with different percentages of the fast-moving component, dermatan sulfate and chondroitin sulfate are precipitated. Heparin was precipitated from mixtures in the range of 0.1 to 0.4 volumes of ethanol, and from 0.5 to 0.8 volumes mixtures with different relative percentages of dermatan sulfate and chondroitin sulfate were precipitated. From 1.0 to 2.0 volumes of ethanol, high purity (about 100%) chondroitin sulfate can be precipitated. Propanol induces the precipitation of heparin from 0.3 to 0.4 volumes, whilst dermatan sulfate with a purity greater than 85% is precipitated at 0.5 and 0.6 volumes of propanol. 100% chondroitin sulfate is obtained with volumes greater than 0.8. Heparin and chondroitin sulfate from a bovine lung extract of glycosaminoglycans were purified by sequential precipitation with ethanol. The fraction precipitated with 0.4 volumes of ethanol shows greater than 90% heparin and that recovered from 0.9 to 2.0 volumes is composed of 100% chondroitin sulfate.     

The kinetics of protein precipitation by different reagents

The kinetics of precipitation of soya protein has been examined in a tubular flow reactor with the precipitants, ammonium sulfate, ethanol, divalent calcium, and sulfuric acid. The precipitate growth profiles obtained in all cases showed the rapid formation of a precipitate phase and the attainment of a final size within 16 s. The final mean particle diameter d(m) varied with precipitating agent used in the order: sulfuric acid (12.5 mum) > ethanol (7.5 mum) approximately calcium ion (7.2 mum) > ammonium sulfate (3.1 mum). In the case of ethanol precipitation, changes in the design of the contacting section of the reactor led to differences in the precipitate growth curve. Protein solubility curves are also presented, and with the reactor data, they provide a convenient method for assessing the effect of precipitating agent on the design of protein precipitation reactors.     

Development of an improved procedure for isolation and purification of exopolysaccharides produced by Lactobacillus delbrueckii subsp. bulgaricus NCFB 2483

A method was developed for the isolation and purification of exopolysaccharide (EPS) produced by Lactobacillus delbrueckii subsp. bulgaricus NCFB 2483 that can be adapted for industrial-scale operation. Hydrolyzed milk medium, which was ultrafiltered to remove molecular species larger than 2.5×10⁵ Da, was found to be a suitable growth medium for the bacteria, which produced approximately 400 mg EPS/l . Optimal isolation of EPS was achieved using centrifugation, filtration and ethanol precipitation methods. Insoluble and soluble EPS fractions were obtained. The soluble fraction was purified using a series of ethanol precipitations to achieve approximately 98% (w/w) purity. This fraction consisted of galactose, glucose, rhamnose and mannose in the ratio of approximately 5:1:0.6:0.5, with traces of glucosamine.     

Chromatography in plasma fractionation: benefits and future trends

Industrial-scale chromatographic fractionation and purification methods have been used increasingly in the last few years for plasma fractionation. This has resulted in the development of a new generation of therapeutic plasma derivatives, especially coagulation factors, protease inhibitors and anticoagulants. Implementation and combination of ion-exchange, affinity and size-exclusion chromatography have allowed the development of new therapeutic products with improved purity and safety for treating congenital or acquired plasma protein deficiencies in patients. More recently, the benefit of chromatographic purification of plasma proteins in the removal of plasma-borne viruses has been revealed. Development of packing materials with improved characteristics for industrial applications, including higher capacity and rigidity, should further promote the use of chromatography as an essential plasma fractionation tool and confine more and more the traditional ethanol precipitation methods to the final processing stages used to recover albumin.     

Purification Process for the Preparation and Characterizations of Hen Egg White Ovalbumin,Lysozyme, Ovotransferrin,and Ovomucoid

Abstract

In this study, four major egg white proteins were purified by two step ion exchange chromatography followed by precipitation. Lysozyme and ovalbumin were separated with Q Sepharose Fast Flow anion exchange chromatography in the first step, resulting in two peaks of lysozyme and three peaks of ovalbumin with 87% and 70% purity by HPLC, respectively. Ovotransferrin was separated with CM-Toyopearl 650 M cation exchange chromatography in the second step, giving 80% purity. Ovomucoid was precipitated from the partial purified protein fraction from the first two steps, and concentrated in the final step to yield 90% purity. Protein recoveries were estimated to be 55, 21, 54, and 21% for lysozyme, ovotransferrin, ovalbumin, and ovomuciod, respectively. Lysozyme was identified from the purified peaks using zymogram refolding gel, whereas ovalbumin was identified by western blotting. Purified ovotransferrin and ovomucoid was identified by mass spectrometry. The results indicate that this purification process is adequate for preparation of lysozyme, ovalbumin, ovotransferrin, and ovomucoid, at least on a laboratory scale.     

Isolation and partial characterization of human kidney gangliosides.

1. Eight gangliosides were purified from chloroform/methanol extracts of human kidneys by using modified Folch partition, dialysis, ethanol precipitation, silicic acid column chromatography and preparative thin-layer chromatography. 2. By thin-layer chromatographic behaviour and gas-liquid chromatographic determinations the main gangliosides in human kidney are N-acetylneuraminyllactosylceramide (74% of total) and di-N-acetylneuraminyllactosylceramide (19% of total). 3. Five hexosamine-containing fractions were isolated. Four of them were homogeneous on thin-layer chromatography, and one contained two gangliosides. By gas-liquid chromatography-mass spectrometry it was shown that two gangliosides (together 5% of total) contain glucosamine, and one (1% of total) contains galactosamine. The other of the glucosamine gangliosides contains fucose in addition to the usual sugars found in gangliosides. Of the two remaining hexosamine positive fractions (together 1% of total) one was homogeneous on thin-layer chromatography, the other contained two gangliosides. These two fractions contained both glucosamine and galactosamine. 4. The main long-chain base in all fractions was sphingosine.     

羊抗人IgG的纯化及其在抗—HCV检测中的应用

单独或联合应用辛酸沉淀、饱和硫酸铵沉淀、阴离子交换等方法对羊抗人IgG进行纯化,对纯化前后抗体的纯度和免疫学活性进行比较,并与辣根过氧化物酶连接,作为二抗用于抗－HCV的ELISA检测。结果表明,不同方法纯化的抗体其纯度和免疫学活性具有一定程度的差别,其中经辛酸＋饱和硫酸铵沉淀纯化的抗体为最佳,凝胶扫描纯度为98．05％,比活性近1800,为纯化前的6．8倍。用痞根过氧化物酶标记后,作为酶标二抗检测HCV阴性和阳性标准血清各40份,阴性符合率为97．5％,阳性符合率为95％,可用于抗－HCV的ELISA检测。     

Isolation and Purification of Chondroitin 6-Sulfate Protein From Umbilical Cord

Intact chondroitin 6-sulfate protein can be extracted from umbilical cord with dilute saline. Hyaluronic acid which is also extracted, is removed by precipitation with cetylpyridinium chloride followed by washing of the precipitate with aqueous sodium chloride. Subsequent purification is effected by passage through cation and anion exchange resins. Elution from the latter with salt solutions of increasing concentration yields chondroitin 6-sulfate proteoglycan in two fractions. The product is isolated from each of the fractions as the calcium salt by fractional precipitation with ethanol. The protein moiety can be cleaved from the mucopolysaccharide either by proteolytic digestion or treatment with alkali. The results obtaired on reaction with alkali and with sodium borohydride indicate that the polysaccharide is covalently linked to the protein through a serine unit.     

Purification of recombinant aprotinin from transgenic corn germ fraction using ion exchange and hydrophobic interaction chromatography

Plants have attracted interest as hosts for protein expression because of the promise of a large production capacity and a low production cost. However, recovery costs remain a challenge as illustrated for recovery of recombinant aprotinin, a trypsin inhibitor, with removal of native corn trypsin inhibitor from transgenic corn (Azzoni et al. in Biotechnol Bioeng 80:268–276, 2002). When expression is targeted to corn grain fractions, dry milling can separate germ and endosperm fractions. Hence, only the product-containing fraction needs to be extracted, reducing the cost of extraction and the impurity level of the extract. Selective extraction conditions can reduce impurity levels to the point that low-cost adsorbents can result in relatively high purity levels. In this work, we attempted to achieve comparable purity with these lower cost methods. We replaced whole grain extraction and purification of recombinant aprotinin with sequential trypsin affinity and IMAC steps with an alternative of germ fraction extraction and purification with ion exchange and hydrophobic interaction chromatography (HIC). Using germ extraction at acidic pH supplemented with heat precipitation to remove additional host proteins resulted in a higher specific activity feed to the chromatographic steps. The cation exchange step provided 7.6× purification with 76.4% yield and no sodium dodecyl sulfate–polyacrylamide gel electrophoresis detectable native corn trypsin inhibitor. After the HIC step (2.7× step purification with 44.0% yield), the final product had a specific activity that was 75.3% of that of the affinity-purified aprotinin.     

The antigenic structure ofFrancisella tularensis

The ether antigen ofFrancisella tularensis was submitted to fractionation using ammonium sulphate, ethanol and trichloracetic acid (TCA). A simple antigenic mixture was obtained by this fractionation from the original complex ether antigen. However, no separation of antigenically and chemically homogenous substances was achieved, by this procedure. The precipitation with TCA permitted the separation of an antigenic component that was found to be identical with the phenol antigen or its component migrating faster towards cathode in electrophoresis. The sediment obtained possessed common properties with the precipitate obtained by ethanol precipitation. The fraction having the highest anodic mobility could be obtained by salting out the original antigen with ammonium sulphate to 50% saturation. By increasing the concentration of ammonium sulphate to 60% saturation, all components of the ether antigen could be precipitated. The number of precipitation lines in the original antigen and its fractions depends both on the concentration of antigen and the quality of antisera.     

A novel purification strategy for retrovirus gene therapy vectors using heparin affinity chromatography

Membrane separation and chromatographic technologies are regarded as an attractive alternative to conventional academic small-scale ultracentrifugation procedures used for retrovirus purification. However, despite the increasing demands for purified retroviral vector preparations, new chromatography adsorbents with high specificity for the virus have not been reported. Heparin affinity chromatography is presented here as a novel convenient tool for retrovirus purification. The ability of bioactive retroviral particles to specifically bind to heparin ligands immobilized on a chromatographic gel is shown. A purification factor of 63 with a recovery of 61% of functional retroparticles was achieved using this single step. Tentacle heparin affinity supports captured retroviral particles more efficiently than conventional heparin affinity chromatography supports with which a lower recovery was obtained (18%). Intact, infective retroviral particles were recovered by elution with low salt concentrations (350 mM NaCl). Mild conditions for retrovirus elution from chromatographic columns are required to preserve virus infectivity. VSV-G pseudotyped retroviruses have shown to be very sensitive to high ionic strength, losing 50% of their activity and showing membrane damage after a short exposure to 1M NaCl. We also report a complete scaleable downstream processing scheme for the purification of MoMLV-derived vectors that involves sequential microfiltration and ultra/diafiltration steps for virus clarification and concentration respectively, followed by fractionation by heparin affinity chromatography and final polishing by size-exclusion chromatography. Overall, by using this strategy, a 38% yield of infective particles can be achieved with a final purification factor of 2,000.     

Purification of porcine plasma factor VIII using chromatographic methods

Factor VIII was purified from porcine plasma using adsorption on aluminium hydroxide with CM-cellulose as a filtration aid, cold ethanol precipitation, and two anion-exchange (Q-Sepharose fast flow) chromatographies. The final product was purified 264-fold and had a specific activity of 10 U mg^–1. The method is suitable to produce purified porcine FVIII by an easy process where all steps can be scaled up. The final product is free of von Willebrand factor that is responsible for the main side effects in patients. Finally, this method can be used to obtain purified porcine plasma FVIII for use in haemophilic patients with inhibitors.     

Continuous integrated antibody precipitation with two-stage tangential flow microfiltration enables constant mass flow

Continuous precipitation is a new unit operation for the continuous capture of antibodies. The capture step is based on continuous precipitation with PEG6000 and Zn⁺⁺ in a tubular reactor integrated with a two-stage continuous tangential flow filtration unit. The precipitate cannot be separated with centrifugation, because a highly compressed sediment results in poor resolubilization. We developed a new two-stage tangential flow microfiltration method, where part of the concentrated retentate of the first stage was directly fed to the second stage, together with the wash buffer. Thus, the precipitate was concentrated and washed in a continuous process. We obtained 97% antibody purity, a 95% process yield during continuous operation, and a fivefold reduction in pre-existing high-molecular-weight impurities. For other unit operations, surge tanks are often required, due to interruptions in the product mass flow out of the unit operation (e.g., the bind/elute mode in periodic counter-current chromatography). Our setup required no surge tanks; thus, it provided a truly continuous antibody capture operation with uninterrupted product mass flow. Continuous virus inactivation and other flow-through unit operations can be readily integrated downstream of the capture step to create truly continuous, integrated, downstream antibody processing without the need for hold tanks.