疏水相互作用层析分离重组人干扰素α2b

目的采用疏水相互作用层析分离重组人干扰素α2b,去除干扰素样品中的二聚体,得到高纯度的干扰素用于进一步的研究。方法首先采用阳离子交换层析纯化复性重组人干扰素α2b,去除了大部分的杂蛋白,然后采用疏水相互作用层析纯化重组人干扰素α2b,去除复性过程中产生的错误折叠体和二聚体,并考察盐浓度、pH值、流速和洗脱液中尿素对疏水相互作用层析纯化效果的影响。结果硫酸铵初始浓度1.2 mol/L、缓冲液pH值6.0、流速2.5 mL/min、洗脱液中添加尿素浓度为2 mol/L时疏水相互作用层析纯化效果最佳。最终得到的重组人干扰素α2b非还原型SDS-PAGE电泳均呈单一条带。结论确定了疏水层析纯化重组人干扰素α2b的最优条件,成功提取到具有高活性、高纯度的重组人干扰素α2b纯品。     

Modeling of protein monomer/aggregate purification and separation using hydrophobic interaction chromatography

Hydrophobic interaction chromatography (HIC) is commonly used to separate protein monomer and aggregate species in the purification of protein therapeutics. Despite being used frequently, the HIC separation mechanism is quite complex and not well understood. In this paper, we examined the separation of a monomer and aggregate protein mixture using Phenyl Sepharose FF. The mechanisms of protein adsorption, desorption, and diffusion of the two species were evaluated using several experimental approaches to determine which processes controlled the separation. A chromatography model, which used homogeneous diffusion (to describe mass transfer) and a competitive Langmuir binary isotherm (to describe protein adsorption and desorption), was formulated and used to predict the separation of the monomer and aggregate species. The experimental studies showed a fraction of the aggregate species bound irreversibly to the adsorbent, which was a major factor governing the separation of the species. The model predictions showed inclusion of irreversible binding in the adsorption mechanism greatly improved the model predictions over a range of operating conditions. The model successfully predicted the separation performance of the adsorbent with the examined feed.     

离子交换色谱法对大肠杆菌表达的人重组骨形态发生蛋白-7的纯化

重组大肠杆菌高量表达重组人骨形态发生蛋白-7(rhBMP-7),每升培养液约得到湿菌体3g,其中目的蛋白约占菌体总蛋白量的40％。裂解离心,用低浓度变性剂洗涤初步纯化包涵体,上清中无目的蛋白损失;将包涵体溶解于高浓度变性剂溶液中,目的蛋白纯度提高到60％;然后在不同条件下用离子交换色谱法对变性状态下的蛋白质进行纯化,绝大部分杂蛋白被除去,目的蛋白纯度达95％以上;改变条件,可以减少rhBMP-7损失;用Western blot对目的蛋白进行特异性鉴定。     

In situ PEGylation of recombinant hirudin on an anion exchange chromatography column

In this study, an integrated process was developed for successive solid-phase PEGylation of recombinant hirudin variant-2 (HV2) and separation of PEGylated HV2 species on an anion exchange chromatography column (so-called in situ PEGylation). The effects of different PEG sizes, ion exchange resins and reaction conditions on in situ PEGylation were investigated. The results showed that in situ PEGylation efficiently integrates the reaction, separation and purification into a single-unit operation using the same column. In situ PEGylation could improve the selectivity of PEGylation reactions by significantly reducing the formation of multi-PEG-HV2. The pore sizes and internal surface structures of different resins had a significant impact on the yield of mono-PEG-HV2. In contrast to liquid-phase PEGylation, the yield of mono-PEG-HV2 decreased as PEG size increased during the in situ PEGylation process, indicating that in situ PEGylation is a pore diffusion-controlled process. The in vitro and in vivo anticoagulant activities of mono-PEG-HV2 derived from in situ PEGylation were higher than those from liquid-phase PEGylation, indicating that in situ PEGylation could enhance the bioactivity retention of mono-PEG-HV2. The results of this study demonstrated that in situ PEGylation can be used as an effective approach for the development of PEGylated protein drugs.     

Refolding and purification of recombinant human (Pro)renin receptor from Escherichia coli by ion exchange chromatography

Purification of the recombinant human renin receptor (rhRnR) is a major aspect of its biological or biophysical analysis, as well as structural research. A simple and efficient method for the refolding and purification of rhRnR expressed in Escherichia coli with weak anion‐exchange chromatography (WAX) was presented in this work. The solution containing denatured rhRnR in 8.0 mol/L urea extracted from the inclusion bodies was directly injected into the WAX column. The aggregation was prevented and the soluble form of renatured rhRnR in aqueous solution was obtained after desorption from the column. Effects of the extracting solutions, the pH values and urea concentrations in the mobile phase, as well as the sample size on the refolding and purification of rhRnR were investigated, indicating that the above mentioned factors had remarkable influences on the efficiency of refolding, purification and mass recovery of rhRnR. Under the optimal conditions, rhRnR was successfully refolded and purified simultaneously by WAX in one step within only 30 min. The result was satisfactory with mass recovery of 71.8% and purity of 94.8%, which was further tested by western blotting. The specific binding of the purified rhRnR to recombinant human renin was also determined using surface plasmon resonance (SPR). The association constant of rhRnR to recombinant human renin was calculated to be 3.25 × 10⁸ L/mol, which demonstrated that rhRnR was already renatured and simultaneously purified in one step using WAX. All of the above demonstrate that protein folding liquid chromatography (PFLC) should be a powerful tool for the purification and renaturation of rhRnR. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:864–871, 2014     

On the use of mild hydrophobic interaction chromatography for "method scouting" protein purification strategies in aqueous two-phase systems: a study using model proteins

The behavior of a series of pure proteins partitioned in aqueous two-phase systems is compared with their behavior during mild hydrophobic interaction chromatography (HIC). A simple theoretical rationale for this comparison is presented based upon solvophobic theory. Similarities were found in the behavior of the model proteins in the two forms of partition chromatography. This indicates that HIC may be employed as a rapid instrumental technique for the broad characterization of protein behavior, which may be of benefit in the development of liquid-liquid partitioning strategies. However, it has proved difficult to completely account for this behavior on the basis of the known physical and structural properties of the proteins used. The variety in the detailed partitioning behavior of this small sample of protein types suggests that partition in aqueous two-phase systems is uniquely sensitive to subtle differences in surface properties of complex macromolecules. (c) 1994 John Wiley & Sons, Inc.     

Purification and characterization of a transgenic corn grain‐derived recombinant collagen type I alpha 1

Corn offers advantages as a transgenic host for producing recombinant proteins required at large volumes (1,000's of tons per year) and low cost (less than US$50/kg) by generating them as co‐products of biorefining. We describe the purification and characterization of a corn grain‐derived mammalian structural protein having such market characteristics: a full length recombinant collagen type I alpha 1 (rCIα1) chain. Material properties of interest are gelation behavior, which would depend on as yet unverified ability of corn to carry out post‐translational prolyl hydroxylation and formation of triple helical conformation. The starting material was grain where the expression of rCIα1 had been directed by an embryo‐specific promoter. Purification consisted of extraction at low pH followed by membrane and chromatographic steps to isolate rCIα1 for characterization. The amino acid composition and immunoreactivity of CIα1 was similar to that of an analogous native human CIα1 and to rCIα1 produced by the yeast Pichia pastoris. Tandem mass spectrometry confirmed the primary sequence of the corn‐derived rCIα1 with 46% coverage. Fragments of the rCIα1chains were also observed, possibly caused by endogenous plant proteases. The corn‐derived rCIα1 had a low level of prolyl hydroxylation (～1% versus 11%) relative to animal‐derived CIα1 and folded into its characteristic triple‐helical structure as indicated by its resistance to pepsin digestion below its melting temperature of 26^oC. The 29 amino acid foldon fused to the C‐terminus to initiate triple helix formation was not cleaved from the rCIα1chains, but could be removed by pepsin treatment. © 2009 American Institute of Chemical Engineers Biotechnol. Prog. 2009     

Interfacial thermodynamics of protein adsorption, ion co-adsorption and ion binding in solution. II. Model interpretation of ion exchange in lysozyme chromatography

In this paper we present a model for the ion exchange effects in protein adsorption. The model is applied to chromatography of lysozyme on strong cation exchanger ‘mono S’. The experimental and general thermodynamic aspects have been discussed in Part 1, the preceding paper. The main modelling assumptions are (i) the charge regulation is confined to the small layer of contact between adsorbed protein and exchanger surface, (ii) the contact layer as a whole is electroneutral and (iii) the number of protein acid/base groups and exchanger surface acid groups which participate in the ion exchange is proportional to the area of the contact layer. The model is fitted to the experimental data by adjustment of only two or three parameters. The experimental co-adsorption numbers are very well reproduced. A few conspicuous features emerge: (i) the number of protein acid/base groups and exchanger surface acid groups in the contact layer varies with the medium conditions, such that the number is higher when the interaction between protein and exchanger surface is stronger. (ii) There is indirect evidence for structural alterations in the upper layers of the exchanger surface: the adsorbed protein is probably partly ‘buried’ in the surface.     

Purification of long helical capsid of newcastle disease virus from Escherichia coli using anion exchange chromatography

NP_Δc375 is a truncated version of the nucleocapsid protein of Newcastle disease virus (NDV) which self‐assembles into a long helical structure. A packed bed anion exchange chromatography (PB‐AEC), SepFastTM Supor Q pre‐packed column, was used to purify NP_Δc375 from clarified feedstock. This PB‐AEC column adsorbed 76.2% of NP_Δc375 from the clarified feedstock. About 67.5% of the adsorbed NP_Δc375 was successfully eluted from the column by applying 50 mM Tris‐HCl elution buffer supplemented with 0.5 M NaCl at pH 7. Thus, a recovery yield of 51.4% with a purity of 76.7% which corresponds to a purification factor of 6.5 was achieved in this PB‐AEC operation. Electron microscopic analysis revealed that the helical structure of the NP_Δc375 purified by SepFast^TM Supor Q pre‐packed column was as long as 490 nm and 22–24 nm in diameter. The antigenicity of the purified NP_Δc375 was confirmed by enzyme‐linked immunosorbent assay. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 29: 564–567, 2013     

Influence of tryptophan tags on the purification of cutinase, secreted by a recombinant Saccharomyces cerevisiae, using cationic expanded bed adsorption and hydrophobic interaction chromatography

During cationic bed adsorption (EBA), with cutinase with varying length tryptophan tags (WP)(2)and (WP)(4), 33% and 10% of adsorption capacity and 80% and 32% eluted specific activity were observed in relation to wild type (wt)-cutinase in the conventional process. Therefore, as the hydrophobicity of the protein increases, it is important to integrate the EBA step with a hydrophobic interaction chromatography (HIC) process. As the length of the hydrophobic tag-(WP) increases from n = 2 to n = 4, the purification factor obtained by HIC was 1.8 and 2.2-fold higher than wt-cutinase. However, the recovery yield obtained in HIC decreases substantially as the length of hydrophobic tag increases (97%, 84% and 70% for wt-cutinase, cutinase-(WP)(2) and cutinase-(WP)(4)). The integration of two purification steps, EBA followed by HIC, resulted in the highest overall purity level for cutinase-(WP)(2), and the highest overall recovery yield for wt-cutinase. When optimizing the design of a hydrophobic tag fused to a protein secreted by Saccharomyces cerevisiae it must be considered that the cultivation parameters could impair the downstream process, and consequently the optimum tag is not necessarily the one that presents the highest purification factor in HIC.     

Interfacial thermodynamics of protein adsorption, ion co-adsorption and ion binding in solution. I. Phenomenological linkage relations for ion exchange in lysozyme chromatography and titration in solution

In this paper we discuss the thermodynamics of ion binding in solution, protein adsorption and ion co-adsorption. The emphasis is on charge regulation effects. To this end, we introduce phenomenological linkage relations from which the ion binding can be calculated from the electrolyte dependency of proton titration curves and the co-adsorption from the electrolyte dependency of protein adsorption isotherms. The linkage relations are derived from classical interfacial thermodynamics, and thus offer an alternative approach as compared to the mass balance equations which are currently used in biotechnology, and Record et al.'s 1978 analysis of Wyman's Binding Polynomial for protein interactions. The co-adsorption theory is an extension of our previous analysis of ion binding in solution, which we include here for comparison of the ion co-adsorption with the ion binding in solution. The theory is applied to the chromatography of lysozyme on the strong cation exchanger ‘mono S’ and to the proton titration of lysozyme in solution. In the accompanying Part 2 of this paper the results are interpreted with a simple model.     

Purification and characterization of recombinant human antithrombin containing the prelatent form in Chinese hamster ovary cells

Antithrombin (AT) is a serine proteinase inhibitor and a major regulator of the blood coagulation cascade. AT in human plasma has two isoforms, a predominant alpha-isoform and a minor beta-isoform; the latter lacks N-glycosylation at Asn 135 and has a higher heparin affinity. From the difference in its folding states, the AT molecule can be separated into three forms: a native form, a denatured and inactive form known as the latent form, and a partially denatured form called the prelatent form. In this study, we purified and characterized recombinant human AT (rAT) containing the prelatent form produced by Chinese hamster ovary (CHO) cells. When rAT was purified at physiological pH, its specific activity was lower than that of plasma-derived human AT (pAT). The latent and prelatent forms were detected in rAT by using hydrophobic interaction chromatography analysis. However, when rAT was purified at alkaline pH, the prelatent form was reversibly folded to the native form and the inhibitory activity of rAT increased to a value similar to that of pAT. Highly purified rAT was analyzed and compared with pAT by using sodium dodecyl sulfate-polyacrylamide gel electrophoresis, circular dichroism spectroscopy, amino acid composition, N-terminal sequence, monosaccharide composition, peptide mapping, and heparin-binding affinity. From these analyses, rAT was found to be structurally identical to pAT, except for carbohydrate side-chains. rAT in CHO cells had a high beta-isoform content and it caused a higher heparin affinity than by pAT and also pH-dependent reversible inhibitory activity.     

Separation of D- and L-amino acids by ion exchange column chromatography in the form of alanyl dipeptides

Summary A method of ion exchange column chromatography was developed for the determination of D- and L-amino acids in the form of diastereomeric dipeptide. First the protein containing samples were hydrolyzed with 6 molar hydrochloric acid, then the single amino acids were separated in an LKB automated amino acid analyzer with the LKB fraction collector. Following lyophilization, the single amino acids were transformed into alanyl dipeptides with tertiary-butyloxycarbonil-L-alanine-N-hydroxy-succinimide (t-BOC-L-Ala-ONSu) active ester. The alanyl dipeptides were easily separated from one another and the initial amino acids. Determination of the D- and L-amino acids in this form is relatively accurate and reproducible but takes some time (33–38 min). Accuracy of the determination is satisfactory. The coefficient of variation amounts to 3–5%. The use of the method is suggested to laboratories having an amino acid analyzer and wish to determine D-and L-amino acids in synthetic-amino acids complements, peptides or natural materials.     

Efficient and easily scalable protein folding strong anion exchange chromatography for renaturation and simultaneous purification of recombinant human asparaginase from E. coli

Recombinant proteins are revolutionizing present day therapeutics. They are generally expressed as insoluble inclusion bodies in the E. coli and mis‐folding, loss of protein, and high cost of down streaming are the hurdles in their recovery. For the first time, we are reporting the refolding with simultaneous purification of rhASP in E. coli using a single step utilizing protein folding‐strong anion exchange chromatography (PF‐SAX). The purification method is also standardized for optimal concentration of solution additives, pH, and mobile phase composition. The results showed purification of rhASP with anion exchange chromatography was effective. Phosphate buffer and slightly alkaline pH produced significant recovery yields and purity profiles. The effect of solution additives such as arginine, glycerol, TMAO, sorbitol, dextran, glutamate, and fructose on rhASP renaturation is also investigated. Significant results were achieved using arginine‐TMAO combination in terms of purity, recovery yield and specific activity of 99%, 78%, and 210 IU/mg, respectively. The work concludes that PF‐SAX refolding method is superior to other conventional methods and it can be applied to large scale purification of rhASP produced in E. coli. © 2018 American Institute of Chemical Engineers Biotechnol. Prog., 34:1036–1044, 2018     

牛脑中神经特异性S-100蛋白的纯化及鉴定

牛脑充分匀浆后经三次硫酸铵分级沉淀,再通过一次DEAE-Sepharose CL-6B层析柱,线性梯度洗脱后共收集4个峰洗脱液。PAGE分析(7.5％凝胶)显示第3峰为单一区带;免疫双扩散证实该洗脱液中蛋白为S-100蛋白。SDS-PAG E分析显示S-100蛋白分子量约为10kD;非还原条件下,凝胶过滤(Sephadex G-75)显示S-100蛋白位于MW为20kD区域。认为该纯化方法简便、快速,可获得较高纯度的S-100蛋白,活性高达1∶128以上,完全能满足进一步研究之用。     

Purification of cell culture‐derived modified vaccinia ankara virus by pseudo‐affinity membrane adsorbers and hydrophobic interaction chromatography

A purification scheme for cell culture‐derived smallpox vaccines based on an orthogonal downstream process of pseudo‐affinity membrane adsorbers (MA) and hydrophobic interaction chromatography (HIC) was investigated. The applied pseudo‐affinity chromatography, based on reinforced sulfated cellulose and heparin‐MA, was optimized in terms of dynamic binding capacities, virus yield and process productivity. HIC was introduced as a subsequent method to further reduce the DNA content. Therefore, two screens were undertaken. First, several HIC ligands were screened for different adsorption behavior between virus particles and DNA. Second, elution from pseudo‐affinity MA and adsorption of virus particles onto the hydrophobic interaction matrix was explored by a series of buffers using different ammonium sulfate concentrations. Eventually, variations between different cultivation batches and buffer conditions were investigated.The most promising combination, a sulfated cellulose membrane adsorber with subsequent phenyl HIC resulted in overall virus particle recoveries ranging from 76% to 55% depending on the product batch and applied conditions. On average, 61% of the recovered virus particles were infective within all tested purification schemes and conditions. Final DNA content varied from 0.01% to 2.5% of the starting material and the level of contaminating protein was below 0.1%. Biotechnol. Bioeng. 2010;107: 312–320. © 2010 Wiley Periodicals, Inc.     

Purification and scale-up of a recombinant heavy chain fragment C of botulinum neurotoxin serotype E in Pichia pastoris GS115

A recombinant C-terminus heavy chain fragment from botulinum neurotoxin serotype E (BoNT/E) is proposed as a vaccine against the serotype E neurotoxin. This fragment, rBoNTE(Hc), was produced intracellular in Pichia pastoris GS115 by a three-step fermentation process, i.e., glycerol batch phase and a glycerol fed-batch phase to achieve high cell densities, followed by a methanol fed-batch induction phase. The rBoNTE(Hc) protein was purified from the soluble fraction of cell lysates using three ion-exchange chromatography steps (SP Sepharose Fast Flow, Q Sepharose Fast Flow, Sp Sepharose High Performance) and polished with a hydrophobic charge induction chromatography step (MEP HyperCel). Method development at the bench scale was achieved using 7-380 mL columns and the process was performed at the pilot scale using 0.5-3.1 L columns in preparation for technology transfer to cGMP manufacturing. The purification process resulted in greater than 98% pure rBoNTE(Hc) based on HPLC and yielded up to 1.01g of rBoNTE(Hc)/kg cells at the bench scale and 580mg vaccine/kg cells at the pilot scale. N-terminal sequencing showed that the purified rBoNTE(Hc) N-terminus is intact and was found to protect mice against a challenge of 1000 mouse intraperitoneal LD50's of BoNT/E.     

Separation of phycocyanin from <Emphasis Type="Italic">Spirulina platensis</Emphasis> using ion exchange chromatography

This paper presents the evaluation of some important parameters for the purification of phycocyanin using ion exchange chromatography. The influences of pH and temperature on the equilibrium partition coefficient were investigated to establish the best conditions for phycocyanin adsorption. The equilibrium isotherm for the phycocyanin-resin system was also determined. The separation of phycocyanin using the Q-Sepharose ion exchange resin was evaluated in terms of the pH and elution volume that improved the increase in purity and recovery. The highest partition coefficients were obtained in the pH range from 7.5 to 8.0 at 25 degrees C. Under these conditions the equilibrium isotherm for phycocyanin adsorption was well described by the Langmuir model, attaining a Q (m) of 22.7 mg/mL and K (d) of 3.1 x 10(-2) mg/mL. The best conditions for phycocyanin purification using the ion exchange column were at pH 7.5 with an elution volume of 36 mL, obtaining 77.3% recovery and a 3.4-fold increase in purity.