离子交换层析纯化透明质酸

考察6种离子交换树脂的静态吸附解析效果,选出201＊7阴离子交换树脂填柱,确定洗脱流速为0.6mL/min,40mL0.3mol/LNaCl和50mL0.5mol/L NaCl双浓度洗脱,实现透明质酸和杂蛋白的分离。制得透明质酸产品蛋白含量为0.057%,葡萄糖醛酸含量为43%,平均相对分子质量大于1.1×10^6,收率为54%,符合医用级透明质酸行业标准的要求。     

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     

The impact of protein exclusion on the purity performance of ion exchange resins

Dynamic binding capacity (DBC) decreases with increasing conductivity in the equilibrium regime for ion exchange chromatography. An exclusion regime has been demonstrated in ion exchange resins where DBC increases with increasing conductivity and decreasing protein charge. The purpose of this work was to examine the impact of the exclusion regime on impurity removal. Resin performance was evaluated based on dynamic binding capacities and purity within the exclusion and equilibrium regimes. The results revealed that Chinese hamster ovary proteins (CHOP), a major impurity, exhibit similar exclusion trends as the MAb proteins. The results further the understanding of the exclusion regime and its impact on product purity, a critical area for IEX development and optimization.     

Fluidized bed ion exchange for improving purification of lactic acid from fermentation

A strong anionic exchange resin was used to recover lactic acid directly from fermentation in an upflow fluidized bed column, resulting in 0.18 g lactic acid/g resin bound with a subsequent elution of 94%. When the culture broth was heated and adjusted pH to 8.0, 0.4 g lactic acid was bound per g resin, with a subsequent elution of 90%. L(+) and D(–) lactic acid isomers distribution was analyzed in the elution product resulting in an increase of L(+) isomer concentration. The resin did not alter its binding capacity after 23 cycles.     

335弱碱性阴离子交换树脂对甘草酸的吸附过程

研究了335弱碱性阴离子交换树脂对甘草酸的吸附过程。拟合得到的吸附等温线方程为:c1/[q×(329-c1)]=0.035 8 1.872(c1/329),符合BET方程,计算得出335树脂的饱和吸附量是524.2 mg.g-1。通过吸附动力学曲线的研究,表明该树脂属于慢型吸附类型,得到树脂对甘草酸的吸附穿透曲线,穿透容量为42.00 mg.g-1,饱和容量近似为203.0 mg.g-1,交换柱的利用率小于0.206 9。用碱性洗脱液不易将树脂上吸附的甘草酸洗脱下来,利于甘草浸膏溶液中甘草酸和其它组分的分离。     

Understanding the interaction of proteins to ion exchange chromatographic supports: A surface energetics approach

Ion exchange chromatography is one of the most widely used chromatographic technique for the separation and purification of important biological molecules. Due to its wide applicability in separation processes, a targeted approach is required to suggest the effective binding conditions during ion exchange chromatography. A surface energetics approach was used to study the interaction of proteins to different types of ion exchange chromatographic beads. The basic parameters used in this approach are derived from the contact angle, streaming potential, and zeta potential values. The interaction of few model proteins to different anionic and cationic exchanger, with different backbone chemistry, that is, agarose and methacrylate, was performed. Generally, under binding conditions, it was observed that proteins having negative surface charges showed strong to lose interaction (20 kT for Hannilase to 0.5 kT for IgG) with different anionic exchangers (having different positive surface charges). On the contrary, anionic exchangers showed almost no interaction (0–0.1 kT) with the positively charged proteins. An inverse behavior was observed for the interaction of proteins to cationic exchangers. The outcome from these theoretical calculations can predict the binding behavior of different proteins under real ion exchange chromatographic conditions. This will ultimately propose a better bioprocess design for protein separation.     

Antibody purification from CHO cell supernatant using new multimodal membranes

This contribution describes strategies to purify monoclonal antibodies from Chinese hamster ovary (CHO) cell culture supernatant using newly designed multimodal membranes (MMMs). The MMMs were used for the capture step purification of human IgG₁ following a size‐exclusion desalting column to remove chaotropic salts that interfere with IgG binding. The MMM column attained higher dynamic binding capacity than a Protein A resin column at an equivalent residence time of 1 min. The two‐step MMM chromatography process achieved high selectivity for capturing hIgG₁ from the CHO cell culture supernatant, though the desalting step resulted in product dilution. Product purity and host cell protein (HCP) level in the elution pool were analyzed and compared to results from a commercial Protein A column. The product purity was >98% and HCP levels were <20 ppm for both purification methods. In addition, hIgG₁ could be eluted from the MMM chromatography column at neutral pH, which is important for limiting the formation of aggregates; although slow elution dilutes the product. Overall, this paper shows that MMMs are highly effective for capture step purification of proteins and should be considered when Protein A cannot be used, e.g., for pH sensitive mAbs or proteins lacking an Fc binding domain. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:658–665, 2017     

An exclusion mechanism in ion exchange chromatography

Protein dynamic binding capacities on ion exchange resins are typically expected to decrease with increasing conductivity and decreasing protein charge. There are, however, conditions where capacity increases with increasing conductivity and decreasing protein charge. Capacity measurements on two different commercial ion exchange resins with three different monoclonal antibodies at various pH and conductivities exhibited two domains. In the first domain, the capacity unexpectedly increased with increasing conductivity and decreasing protein charge. The second domain exhibited traditional behavior. A mechanism to explain the first domain is postulated; proteins initially bind to the outer pore regions and electrostatically hinder subsequent protein transport. Such a mechanism is supported by protein capacity and confocal microscopy studies whose results suggest how knowledge of the two types of IEX behavior can be leveraged in optimizing resins and processes.     

High‐throughput ion exchange purification of positively charged recombinant protein in the presence of negatively charged dextran sulfate

Product quality analyses are critical for developing cell line and bioprocess producing therapeutic proteins with desired critical product quality attributes. To facilitate these analyses, a high‐throughput small‐scale protein purification (SSP) is required to quickly purify many samples in parallel. Here we develop an SSP using ion exchange resins to purify a positively charged recombinant growth factor P1 in the presence of negatively charged dextran sulfate supplemented to improve the cell culture performance. The major challenge in this work is that the strong ionic interaction between P1 and dextran sulfate disrupts interaction between P1 and chromatography resins. To solve this problem, we develop a two‐step SSP using Q Sepharose Fast Flow (QFF) and SP Sepharose XL (SPXL) resins to purify P1. The overall yield of this two‐step SSP is 78%. Moreover, the SSP does not affect the critical product quality attributes. The SSP was critical for developing the cell line and process producing P1. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:516–520, 2014     

Pilot scale recovery of monoclonal antibodies by expanded bed ion exchange adsorption

The aim of the investigations was to estimate the scale up properties of an efficient chromatographic first capture step for the recovery of murine IgG₁ from undiluted and unclarified hybridoma cell culture broth using an ion exchange matrix in expanded bed mode. The tested new sulfopropyl-based ion exchange matrix (Streamline^TM SP XL, Amersham Pharmacia Biotech) stands out due to its enhanced capacity compared to its precursor (Streamline^TM SP). Defining the working pH in preliminary electrophoretic analyses (titration curve, SDS-PAGE) and small-scaled chromatographic binding studies showed, that the optimal value for the IgG purification was pH 4.6, where a co-chromatography of the medium supplement albumin (500 mg l^-1, pI = 4.8) could not be avoided. Further scouting experiments dealt with the dynamic capacity of the matrix, which was evaluated by frontal adsorption analysis. In packed bed mode no break-through of the target protein was achieved even after 6.5 mg IgG per ml matrix were applied. These results could not be reproduced in expanded bed mode with cell-free supernatant, where the dynamic capacity was found to be only 1.5 mg IgG/ml SP XL. Processing cell-containing broth resulted in an additional decrease of the value down to 0.5 mg ml^-1, presumably caused by the remarkable biomass adsorption to the matrix. The search for the reasons led to the examination of the hydrodynamic conditions. Buffer experiments with a tracer substance (acetone) pointed out, that the flow in expanded bed was significantly more influenced by back-mixing effects and channel formations than in packed bed. These effects could be compensated with an enhanced viscosity of the liquid phase, which was achieved by the addition of glucose. As a result of the improved hydrodynamic conditions in the expanded bed, the dynamic capacity could be increased from 0.5 to more than 4.5 mg IgG/ml matrix for the processing of cell culture broth with 400 mM glucose. Finally, the scale up from a Streamline^TM 25 to a Streamline^TM 200 column was performed under conditions, which proved to be optimal: 100 L of unclarified hybridoma broth were concentrated with a binding rate of 95% in less than 3.5 hours. Loading the column no break-through of the target protein was achieved. However, the eluate still contained debris and cells, which points out the major disadvantage of the method: the biomass attachment to the matrix.     

Increasing parvovirus filter throughput of monoclonal antibodies using ion exchange membrane adsorptive pre‐filtration

Pre‐filtration using ion exchange membrane adsorbers can improve parvovirus filter throughput of monoclonal antibodies (mAbs). The membranes work by binding trace foulants, and although some antibody product also binds, yields ≥99% are easily achieved by overloading. Results show that foulant adsorption is dependent on pH and conductivity, but independent of scale and adsorber brand. The ability to use ion exchange membranes as pre‐filters is significant because it provides a clean, well defined, chemically stable option for enhancing throughput. Additionally, ion exchange membranes facilitate characterization of parvovirus filter foulants. Examination of adsorber elution samples using sedimentation velocity analysis and SEC‐MALS/QELS revealed the presence of high molecular weight species ranging from 8 to 13 nm in hydrodynamic radius, which are similar in size to parvoviruses and thus would be expected to plug the pores of a parvovirus filter. A study of two identical membranes in‐series supports the hypothesis that the foulants are soluble, trace level aggregates in the feed. This study's significance lies in a previously undiscovered application of membrane chromatography, leading to a more cost effective and robust approach to parvovirus filtration for the production of monoclonal antibodies. Biotechnol. Bioeng. 2010;106: 627–637. © 2010 Wiley Periodicals, Inc.     

Characterization of superporous cellulose matrix for high‐throughput adsorptive purification of lysozyme

Protein purification essentially requires macroporous adsorbents matrices, which can provide high efficiency in packed bed and expanded bed (EB) even at high flow rates on account of reduced pore diffusion resistance resulting from finite intraparticle flow in the superpores. Rigid spherical superporous adsorbent beads with high carboxyl group density were prepared by crosslinking of cellulose. The matrix (diameter: 100–300 μm, mean pore size: 1–3 μm, pore volume: 57–59%, and bulk density: ～1,438 kg/m³) could be used in packed bed as well as EB for purification of various biomolecules. Attempts were made to use indigenously developed rigid, superporous crosslinked cellulose adsorbent for high‐throughput purification of lysozyme from chicken egg white's extract. A typical adsorption isotherm for lysozyme in crude was well correlated with the Langmuir isotherm model. Two maxima of binding capacity on celbeads bearing carboxymethyl (celbeads‐CM) group for lysozyme were observed at pH 4.5 and 7.5. Uptake kinetics showed that the diffusivity of lysozyme was 100 times higher than conventional matrices. Such superporous matrix can be used for high‐throughput purification of proteins from crude feedstocks and is reflected in leveling off of height equivalent to theoretical plate vs. flow curve after threshold velocity. Optimization of binding and elution conditions resulted in overall purification of lysozyme in a high yield and purity of 98.22 and 98.8%, respectively, with purification factor of 51.54 in a single step. The overall productivity (14.21 kg/m³ h) and specific activity (2.2 × 10⁵ U/mg) were higher than that obtained with traditional particulate resins. © 2011 American Institute of Chemical Engineers Biotechnol. Prog., 2011     

Prospective field study of transovarial dengue‐virus transmission by two different forms of Aedes aegypti in an urban area of Bangkok,Thailand

A prospective field study was conducted to determine transovarial dengue‐virus transmission in two forms of Aedes aegypti mosquitoes in an urban district of Bangkok, Thailand. Immature Aedes mosquitoes were collected monthly for one year and reared continuously until adulthood in the laboratory. Mosquitoes assayed for dengue virus were processed in pools and their dengue virus infection status was determined by one‐step RT‐PCR and nested‐PCR methods. Of a total 15,457 newly emerged adult Ae. aegypti, 98.2% were dark and 1.8% of the pale form. The results showed that the minimum infection rate (MIR) by transovarial transmission (TOT) of dengue virus during the one‐year study ranged between 0 to 24.4/1,000 mosquitoes. Dengue virus TOT increased gradually during the hot summer months, reaching a peak in April‐June, while dengue cases peaked in September, a rainy month near the end of the rainy season. Therefore, mosquito infections due to TOT were prevalent four months before a high incidence of human infections. TOT dengue virus infections occurred in both forms of Ae. aegypti. All four dengue serotypes were detected, with DEN‐4 predominant, followed by DEN‐3, DEN‐1, and DEN‐2, respectively.     

High-throughput protein purification under denaturating conditions by the use of cation exchange chromatography

A high-throughput protein purification strategy using the polycationic Z(basic) tag has been developed. In order for the strategy to be useful both for soluble and less soluble proteins, a denaturating agent, urea, was used in all purification steps. First, four target proteins were genetically fused to the purification tag, Z(basic). These protein constructs were purified by cation exchange chromatography and eluted using a salt gradient. From the data achieved, a purification strategy was planned including stepwise elution to enable parallel protein purification using a laboratory robot. A protocol that includes all steps, equilibration of the chromatography resin, load of sample, wash, and elution, all without any manual handling steps, was handled by the laboratory robot. The program allows automated purification giving milligram amounts of pure recombinant protein of up to 60 cell lysates. In this study 22 different protein constructs, with different characteristics regarding pI and solubility, were successfully purified by the laboratory robot. The data show that Z(basic) can be used as a general purification tag also under denaturating conditions. Moreover, the strategy enables purification of proteins with different pI and solubility using ion exchange chromatography (IEXC). The procedure is highly reproducible and allows for high protein yield and purity and is therefore a good complement to the commonly used His(6)-tag.     

Countercurrent tangential chromatography for large-scale protein purification

Recent advances in cell culture technology have created significant pressure on the downstream purification process, leading to a "downstream bottleneck" in the production of recombinant therapeutic proteins for the treatment of cancer, genetic disorders, and cardiovascular disease. Countercurrent tangential chromatography overcomes many of the limitations of conventional column chromatography by having the resin (in the form of a slurry) flow through a series of static mixers and hollow fiber membrane modules. The buffers used in the binding, washing, and elution steps flow countercurrent to the resin, enabling high-resolution separations while reducing the amount of buffer needed for protein purification. The results obtained in this study provide the first experimental demonstration of the feasibility of using countercurrent tangential chromatography for the separation of a model protein mixture containing bovine serum albumin and myoglobin using a commercially available anion exchange resin. Batch uptake/desorption experiments were used in combination with critical flux data for the hollow fiber filters to design the countercurrent tangential chromatography system. A two-stage batch separation yielded the purified target protein at >99% purity with 94% recovery. The results clearly demonstrate the potential of using countercurrent tangential chromatography for the large-scale purification of therapeutic proteins.     

离子交换法分离发酵液中鸟苷和肌苷

乌苷发酵液中乌苷与副产物肌苷的分离对乌苷工业有重要的意义。对乌苷和肌苷的分离条件进行研究,得到了最佳分离条件：采用Hd-8树脂,树脂床高度为4cm,前120mL采用0．05mol／L盐酸洗脱收集肌苷,120mL至240mL采用0．74mol／L pH5．0醋酸钠缓冲液洗脱收集乌苷,可以获得很好的效果。     

Viral clearance by flow‐through mode ion exchange columns and membrane adsorbers

Anion exchange (AEX) is a common downstream purification operation for biotechnology products manufactured in cell culture such as therapeutic monoclonal antibodies (mAbs) and Fc‐fusion proteins. We present a head‐to‐head comparison of the viral clearance efficiency of AEX adsorbers and column chromatography using the same process fluids and comparable run conditions. We also present overall trends from the CDER viral clearance database. In our comparison of multiple brands of resins and adsorbers, clearance of three model viruses (PPV, X‐MuLV, and PR772) was largely comparable, with some exceptions which may reflect run conditions that had not been optimized on a resin/membrane specific basis. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 30:124–131, 2014     

Combination of size-exclusion chromatography and ion exchange adsorption for improving the proteomic analysis of plasma-derived extracellular vesicles

Extracellular vesicles (EVs) are lipid membrane vesicles released by live cells that carry a variety of biomolecules, including nucleic acids, lipids, and proteins. Recently, proteins in plasma-derived EVs have emerged as novel biomarkers with essential functions in the diagnosis and prognosis of human diseases. However, the current methods of isolating EVs from plasma often lead to coisolated impurities in biological fluids. Therefore, before performing any research protocol, the process of extracting EVs from plasma for proteomic analysis must be optimized. In this study, two EV isolation strategies, size exclusion chromatography (SEC) and SEC combined with ion exchange adsorption (SEC + IEA), were compared in terms of the purity and quantity of protein in EVs. Our results demonstrated that, compared to single-step SEC, SEC combined with IEA could produce plasma-derived EVs with a higher purity by decreasing the abundance of lipoprotein. Additionally, with MS analysis, we demonstrated that the combination approach maintained the stability and improved the purity of EVs in many plasma samples. Furthermore, by combining SEC with IEA, more cancer-associated proteins were detected in the plasma of various cancer samples.     

Isolation and purification of lactoferrin and immunoglobulin G from bovine colostrum with serial cation-anion exchange chromatography

High-value dairy proteins such as lactoferrin (LF) and immunoglobulin (IgG) were separated from bovine colostrum. The whey was initially adjusted to pH 6.8 with 1 mol/L NaOH and then went through centrifugation, precipitation, and filtration to eliminate the fat and caseins in bovine colostrum. The treated whey was further ultra-filtrated to partially remove both other proteins and carbohydrates under 50 kD molecular weight. Then the ultra-filtrated whey was passed through cation and anion exchange columns in series. The LF and IgG were adsorbed on cation and anion exchanger, respectively, due to their different pI. Both the cation and anion exchange columns were washed with de-ionized water followed by successive elution with sodium chloride solutions of increasing molarities (0.27 and 0.85 mol/L; 17 and 51 mmol/L) in a stepwise manner, respectively. After desalted, the elution was freeze-dried. Finally, the LF and IgG with respective purities of 95.0% and 96.6% were obtained.     

Capturing of cell culture‐derived modified Vaccinia Ankara virus by ion exchange and pseudo‐affinity membrane adsorbers

Smallpox is an acute, highly infectious viral disease unique to humans, and responsible for an estimated 300–500 million deaths in the 20th century. Following successful vaccination campaigns through the 19th and 20th centuries, smallpox was declared eradicated by the World Health Organization in 1980. However, the threat of using smallpox as a biological weapon prompted efforts of some governments to produce smallpox vaccines for emergency preparedness. An additional aspect for the interest in smallpox virus is its potential use as a platform technology for vector vaccines. In particular, the latter requires a high safety level for routine applications. IMVAMUNE®, a third generation smallpox vaccine based on the attenuated Modified Vaccinia Ankara (MVA) virus, demonstrates superior safety compared to earlier generations and represents therefore an interesting choice as viral vector. Current downstream production processes of Vaccinia virus and MVA are mainly based on labor‐intensive centrifugation and filtration methods, requiring expensive nuclease treatment in order to achieve sufficient low host‐cell DNA levels for human vaccines. This study compares different ion exchange and pseudo‐affinity membrane adsorbers (MA) to capture chicken embryo fibroblast cell‐derived MVA‐BN® after cell homogenization and clarification. In parallel, the overall performance of classical bead‐based resin chromatography (Cellufine® sulfate and Toyopearl® AF‐Heparin) was investigated. The two tested pseudo‐affinity MA (i.e., sulfated cellulose and heparin) were superior over the applied ion exchange MA in terms of virus yield and contaminant depletion. Furthermore, studies confirmed an expected increase in productivity resulting from the increased volume throughput of MA compared to classical bead‐based column chromatography methods. Overall virus recovery was ～60% for both pseudo‐affinity MA and the Cellufine® sulfate resin. Depletion of total protein ranged between 86% and 102% for all tested matrices. Remaining dsDNA in the product fraction varied between 24% and 7% for the pseudo‐affinity chromatography materials. Cellufine® sulfate and the reinforced sulfated cellulose MA achieved the lowest dsDNA product contamination. Finally, by a combination of pseudo‐affinity with anion exchange MA a further reduction of host‐cell DNA was achieved. Biotechnol. Bioeng. 2010. 105: 761–769. © 2009 Wiley Periodicals, Inc.