Effect of matrices on affinity purification of protein C

One of the critical problems in scale-up of affinity chromatography is the mechanical strength of the support matrix against pressure. Because the costs of both the gel matrix and the ligand for the affinity chromatography are very high, the reusability of gel matrices is directly related to the total production cost. In certain cases, where the source material is viscous (e.g., blood plasma), irreversible deformation of gel matrices can readily occur, necessitating severe constraints in the flow rate. Consequently, productivity is low.We have characterized the system parameters and investigated the performance of various matrices that are commercially available. The experimental system used for this study was the immunoaffinity purification of protein C (an anticoagulant protein) from human blood plasma. The support matrices studied were cross-linked agarose, polymethyl acrylic, cellulose, and polyvinyl alcohol polymers. The major system parameters studied were pressure tolerance, coupling efficiency, adsorption efficiency, and batch adsorption/desorption kinetics of protein C to/from the monoclonal antibody (MAb)-Matrix complex. In addition, the apparent equilibrium constant and bandwidth of the product concentration profile in the eluate were characterized by performing pulse tests.A methodology was developed for evaluating the immunoaffinity colum performance for the separation of protein C. By utilizing the experimentally measured parameters, the flow rate limitation for each purification step was computed. Then, the purification performance of the matrices were evaluated in terms of productivity per unit time. Among the matrices tested, cellulose was superior in overall performance for the immunoaffinity purification of protein C using a 10 cm x 10 cm column.     

Evaluation of the electroosmotic medium pump system for preparative disk gel electrophoresis

This paper describes an improved electroosmotic elution system for preparative sodium dodecyl sulfate-polyacrylamide gel electrophoresis (SDS-PAGE) based on the epochal idea of H. V. Tan et al. (Nucleic Acids Res. 1988, 16, 1921-1930). In this elution system, a semipermeable membrane, mounted under the gel terminal end, works as the elution pump as well as the partition of the elution chamber. We refer to this system as the "electroosmotic medium pump system." Operation of the constructed apparatus (3.6 cm i.d. disk gel column) and resolution of the protein bands were examined by separation of the model protein mixture (bovine serum albumin (BSA), ovalbumin, bovine carbonic anhydrase, soybean trypsin inhibitor) and purification of the membrane protein, dipeptidyl peptidase IV (DPP IV). The Spectra/Por 7 dialysis membrane provided a better flow profile for the elution buffer. The four model proteins of the protein mixture were able to be completely separated from each other and recovered without dilution. The maximum protein concentration of eluate achieved was 93 mg/ml, when applying a single component, BSA fraction V, as a sample. Furthermore, the multifunctional ectoenzyme, DPP IV, was purified in a single step.     

Artifact-inducing enrichment of ethylenediaminetetraacetic acid and ethyleneglycoltetraacetic acid on anion exchange resins

Multivalent metal chelators, ethylenediaminetetraacetic acid (EDTA) and ethyleneglycoltetraacetic acid (EGTA), are used extensively during protein purification. Both strong (Q) and weak (DEAE) anion exchange resins were found to adsorb surprisingly large quantities of EDTA and EGTA that elute from the resin at NaCl concentrations of approximately 240 mM (EDTA) and 140 mM (EGTA). The EDTA/EGTA elution and saturation parameters were determined for five commonly used anion exchange resins. The resulting concentration of eluted EDTA was 10- to 200-fold higher than that originally present in the sample or in the mobile phase. Samples from fractions containing such a high concentration of EDTA were found to inhibit Mg²⁺-dependent polymerase chain reaction (PCR). EDTA binding to the anion exchange resins could saturate the resin, decrease its binding capacity, and displace weakly bound proteins such as green fluorescent protein (GFP). Several steps are suggested to minimize on-column EDTA concentration, including column equilibration in the absence of any EDTA, lower concentrations (0.1–0.5 mM) of EDTA, monitoring eluate absorbance at 280 nm as well as at 215 nm, adding EDTA back into fractions eluting before the EDTA peak, and performing blank column runs to control for the effect of changes in EDTA concentration in downstream assays.     

Purification of histidine-tagged nucleocapsid protein of Nipah virus using immobilized metal affinity chromatography

Nucleocapsid (N) protein of Nipah virus (NiV) is a potential serological marker used in the diagnosis of NiV infections. In this study, a rapid and efficient purification system, HisTrap? 6 Fast Flow packed bed column was applied to purify recombinant histidine-tagged N protein of NiV from clarified feedstock. The optimizations of binding and elution conditions of N protein of NiV onto and from Nickel Sepharose? 6 Fast Flow were investigated. The optimal binding was achieved at pH 7.5, superficial velocity of 1.25 cm/min. The bound N protein was successfully recovered by a stepwise elution with different concentration of imidazole (50, 150, 300 and 500 mM). The N protein of NiV was captured and eluted from an inlet N protein concentration of 0.4 mg/ml in a scale-up immobilized metal affinity chromatography (IMAC) packed bed column of Nickel Sepharose? 6 Fast Flow with the optimized condition obtained from the method scouting. The purification of histidine-tagged N protein using IMAC packed bed column has resulted a 68.3% yield and a purification factor of 7.94.     

Purification of glucoamylase by acarbose (BAY g-5421) affinity chromatography

Aspergillus niger and Rhizopus sp. glucoamylases were purified on an affinity chromatography column from commercially available, impure enzyme preparations. Up to 2 mg of glucoamylase protein was bound without leakage to a 1-ml affinity gel column (0.7 X 2.5 cm) possessing a covalently linked acarbose ligand (1 mg acarbose/g wet gel), and the bound enzyme was specifically released by irrigation of the column with a solution of maltose. A complete cycle of purification was accomplished in about 8 h. Glucoamylases were recovered, in more than 80% yield, free of alpha-amylase activity and possessing specific activities comparable to those of preparations obtained by time-consuming, multistep procedures involving several ion-exchange and hydrophobic column fractionations. Thus, acarbose affinity chromatography provides a general method for the rapid and efficient purification of the glucoamylases, and seems to be ideally suited for scale-up for the commercial purification of these enzymes.     

Steroid-affinity purification of the rat liver glucocorticoid hormone receptor complex

The molybdate-stabilized GHRC was isolated from rat liver cytosol with a 9000-fold purification and 46% yield. The major purification step was achieved using an affinity matrix consisting of an agarose support coupled to a dexamethasone ligand via an aliphatic spacer arm. Spacer arms containing disulfide bridges were found to be unsuitable due to their instability in cytosol. To reduce the non-specific binding properties of the affinity matrix, underivatized amino groups were acetylated, since the receptor was found to bind avidly to such groups thus evading elution by the ligand. Sodium molybdate present during biospecific elution from the gel stabilized the steroid-binding activity of the receptor. The use of denaturing and sulfhydryl modifying reagents (NaSCN, DMSO, Mersalyl) during elution led to partial or complete irreversible loss of steroid-binding activity of the unoccupied receptor. Efficient biospecific elution occurred at competing concentration of high affinity steroid in the presence of sodium molybdate. The ligand specific eluate was further purified by DEAE-Sephacel chromatography resulting in additional purification of 3.2-fold. The GHRC eluted from the DEAE-Sephacel column at a salt concentration characteristic of the untransformed GHRC. Molybdate was removed from the purified untransformed GHRC in the ligand eluate by DEAE-Sephacel chromatography in the absence of molybdate, for subsequent heat transformation.     

两步串联层析法纯化鼠抗人CD80单克隆抗体4E5

采用阴离子交换与凝胶过滤两步串联层析法,纯化了小鼠腹水来源的CD80阻断型单克隆抗体4E5。腹水样品经离心、过滤预处理后,在Tris-HCl缓冲溶液(pH8.0, 50mmol/L)条件下上阴离子交换柱对目的单抗进行捕集,采用0-0.5 mol/L NaCl浓度分步洗脱;含目的单抗的洗脱馏分再上凝胶过滤柱纯化,用PB缓冲溶液（pH7.2, 20mmol/L）洗脱,获得目的单抗4E5,其生物学活性高、纯度大于95%,抗体总回收率达61%。     

Isolation of a recombinant formate dehydrogenase by pseudo-affinity expanded bed adsorption.

Formate dehydrogenase (FDH) is an enzyme of industrial interest, which is recombinantly expressed as an intracellular protein in Escherichia coli. In order to establish an efficient and reliable purification protocol, an expanded bed adsorption (EBA) process was developed, starting from the crude bacterial homogenate. EBA process design was performed with the goal of finding operating conditions which, on one hand, allow efficient adsorption of the target protein and which, on the other hand, support the formation of a perfectly classified fluidised bed (expanded bed) in the crude feed solution. A pseudo-affinity ligand (Procion Red HE3B) was used to bind the FDH with high selectivity and reasonable capacity (maximum equilibrium capacity of 30 U/ml). Additionally, a simplified modelling approach, involving small packed beds for generation of process parameters, was employed for defining the operating conditions during sample application. In combination with extended elution studies, a process was set up, which could be scaled up to 7.5 l of adsorbent volume yielding a total amount of 100,000 U of 94% pure FDH per run. On this scale, 19 l of a benzonase-treated E. coli homogenate of 15% wet-weight (pH 7.5, 9 mS/cm conductivity) were loaded to the pseudo-affinity adsorbent (0.25 m sed. bed height, 5 x 10(-4) m/s fluid velocity). After a series of two wash steps, a particle-free eluate pool was obtained with 85% yield of FDH. This excellently demonstrates the suitability of expanded bed adsorption for efficient isolation of proteins by combining solid-liquid separation with adsorptive purification in a single unit operation.     

Partial preparative separation and properties of the isoinhibitors of human alpha 1-antitrypsin (alpha 1-protease inhibitor).

Human lapha 1-antitrypsin (alpha 1-protease inhibitor) was chromatographed on a DEAE-cellulose column at pH 6.4. After elution with a linearly increasing concentration of NaCl, five pools (pools I-V) were formed from the eluate, pool I corresponding to the lowest and pool V to the highest concentration of salt. As demonstrated by analytical isoelectric focusing, with increasing concentrations of NaCl the concentration of the cathodal isoinhibitors gradually decreased and the concentration of the anodal ones increased in the pools. Pool I contained only three cathodal and pool V only three anodal isoinhibitors with a limited overlap between the pools. In contrast with the isoinhibitor composition, the sialic acid contents of the pools did not vary with the elution conditions. In line with the chemical evidence, desialylation of the fractions did not affect their electrofocusing positions relative to one another and did not abolish the microheterogeneity of the protein.     

Preparative isoelectric focusing in immobilized pH gradients. II. A case report

The preparative aspects of isoelectric focusing (IEF) in immobilized pH gradients (IPG) have been investigated as a function of the following parameters: environmental ionic strength (I), gel geometry and shape of pH gradient. As model proteins, hemoglobin (Hb) A and a minor, glycosylated component (HbA1c), with a delta pI = 0.04 pH units, have been selected. The load capacity increases almost linearly, as a function of progressively higher I values, from 0.5 X up to 2 X molarity of buffering Immobiline (pK 7.0) to abruptly reach a plateau at 3 X concentration of buffering ion. The load capacity also increases almost linearly as a function of gel thickness from 1 to 5 mm, without apparently levelling off. When decreasing the pH interval from 1 pH unit (pH 6.8-7.8) to 1/2 pH unit (pH 7.05-7.55) the amount of protein loaded in the HbA zone could be increased by 40%. In 5 mm thick gels, at 2 X pK 7.0 Immobiline concentration, over a 1/2 pH unit span, up to 350 mg HbA (in a 12.5 X 11 cm gel) could be loaded in a single zone, the load limit of the system being around 45 mg protein/ml gel volume.     

Optimization and scale up of the adsorption fractionation of cod pyloric caeca deoxyribonuclease using axial and radial flow columns.

The key step in the purification of a deoxyribonuclease (DNase) from extracts of cod (Gadus morhua L.) pyloric caeca, is the selective retention of the enzyme by anion exchange chromatography. The cod DNase purification on Q-Sepharose Fast Flow (Pharmacia) was optimized, using a 60 ml fixed-bed column. In combination with titration curve analysis, we have screened the effect of buffer pHs, feed conductivity and protein loading, on the product recovery and purity. We have developed elution conditions which allow effective separation of the cod DNase from bounded impurities, such as proteinases and nucleic acids. Low levels of these impurities were regarded as essential for the desired product quality. The optimum resolution and maximum purification (ca. 20-fold increase in specific activity) of DNase, was, however, achieved at low protein loading (2.6 mg ml-1 gel), corresponding to less than 4% of the dynamic bed capacity. Scale-up to a 2.5 l pilot scale column (axial flow) and a 0.25 l radial flow column showed that the separation and yield obtained at laboratory scale was retained, and was independent of column geometry and bed height. The implications for a production scale scenario of 100 g of fractionated protein, are also discussed, as well as process hygiene. The optimization described herein adds further knowledge to the treatment of fish waste and the downstream processing of valuable biochemicals from marine raw material.     

Simple protein complex purification and identification method for high-throughput mapping of protein interaction networks

Most current methods for purification and identification of protein complexes use endogenous expression of affinity-tagged bait, tandem affinity tag purification of protein complexes followed by specific elution of complexes from beads, and gel separation and in-gel digestion prior to mass spectrometric analysis of protein interactors. We propose a single affinity tag in vitro pull-down assay with denaturing elution, trypsin digestion in organic solvent, and LC-ESI MS/MS protein identification using SEQUEST analysis. Our method is simple and easy to scale-up and automate, making it suitable for high-throughput mapping of protein interaction networks and functional proteomics.     

Caprylic acid‐induced impurity precipitation from protein A capture column elution pool to enable a two‐chromatography‐step process for monoclonal antibody purification

This article presents the use of caprylic acid (CA) to precipitate impurities from the protein A capture column elution pool for the purification of monoclonal antibodies (mAbs) with the objective of developing a two chromatography step antibody purification process. A CA‐induced impurity precipitation in the protein A column elution pool was evaluated as an alternative method to polishing chromatography techniques for use in the purification of mAbs. Parameters including pH, CA concentrations, mixing time, mAb concentrations, buffer systems, and incubation temperatures were evaluated on their impacts on the impurity removal, high‐molecular weight (HMW) formation and precipitation step yield. Both pH and CA concentration, but not mAb concentrations and buffer systems, are key parameters that can affect host–cell proteins (HCPs) clearance, HMW species, and yield. CA precipitation removes HCPs and some HMW species to the acceptable levels under the optimal conditions. The CA precipitation process is robust at 15–25°C. For all five mAbs tested in this study, the optimal CA concentration range is 0.5–1.0%, while the pH range is from 5.0 to 6.0. A purification process using two chromatography steps (protein A capture column and ion exchange polishing column) in combination with CA‐based impurity precipitation step can be used as a robust downstream process for mAb molecules with a broad range of isoelectric points. Residual CA can be effectively removed by the subsequent polishing cation exchange chromatography. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:1515–1525, 2015     

铜藻岩藻黄素提取及纯化工艺研究

为了对岩藻黄素的提取、纯化进行系统研究,进而为高纯度岩藻黄素的工业化生产提供研究基础,筛选了适用于提取铜藻（Sargassum horneri）鲜藻中岩藻黄素的有机溶剂,并通过单因素实验和正交实验确定了最佳的提取溶剂浓度、提取温度、提取时间、料液比等工艺参数。随后采用硅胶柱层析法进行纯化,并通过单因素实验确定了最佳的硅胶柱床高度、上样量和洗脱流速。最后采用制备液相法对经层析纯化的岩藻黄素进一步纯化。结果表明,有机溶剂萃取的最佳工艺条件为：甲醇浓度90%,提取温度50 ℃,提取时间1 h,料液比1∶10,此条件下岩藻黄素提取率达到(0.258 9±0.003 6) mg·g-1鲜重（FW）［(1.078 8±0.015 0) mg·g-1干重（DW）］。硅胶柱层析的最佳工艺条件为：硅胶柱床高度10 cm,上样量6 g,洗脱流速10 mL·min-1,此条件下岩藻黄素得率为0.176 5 mg·g-1FW（0.735 3 mg·g-1 DW）,纯度为87.01%±0.88%。经制备液相进一步纯化后,岩藻黄素得率为0.127 1 mg·g-1 FW（0.529 4 mg·g-1 DW）,纯度为99.27%±0.22%。研究所用工艺简单,岩藻黄素得率高,为高纯度岩藻黄素的制备提供了实验基础。     

Ultra scale‐down approach to correct dispersive and retentive effects in small‐scale columns when predicting larger scale elution profiles

Ultra scale‐down approaches represent valuable methods for chromatography development work in the biopharmaceutical sector, but for them to be of value, scale‐down mimics must predict large‐scale process performance accurately. For example, one application of a scale‐down model involves using it to predict large‐scale elution profiles correctly with respect to the size of a product peak and its position in a chromatogram relative to contaminants. Predicting large‐scale profiles from data generated by small laboratory columns is complicated, however, by differences in dispersion and retention volumes between the two scales of operation. Correcting for these effects would improve the accuracy of the scale‐down models when predicting outputs such as eluate volumes at larger scale and thus enable the efficient design and operation of subsequent steps. This paper describes a novel ultra scale‐down approach which uses empirical correlations derived from conductivity changes during operation of laboratory and pilot columns to correct chromatographic profiles for the differences in dispersion and retention. The methodology was tested by using 1 mL column data to predict elution profiles of a chimeric monoclonal antibody obtained from Protein A chromatography columns at 3 mL laboratory‐ and 18.3 L pilot‐scale. The predictions were then verified experimentally. Results showed that the empirical corrections enabled accurate estimations of the characteristics of larger‐scale elution profiles. These data then provide the justification to adjust small‐scale conditions to achieve an eluate volume and product concentration which is consistent with that obtained at large‐scale and which can then be used for subsequent ultra scale‐down operations. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Purification of monoclonal antibodies from whole hybridoma fermentation broth by fluidized bed adsorption

To achive the coarse purification of a monoclonal antibody from whole hybridoma fermentation broth a fluidized bed cation exchange process was used. The procedure consisted of application of the crude sample and washing of the bed in a fluidized mode and elution in a fixed bed mode. A completely clarified eluate was obtained with purification factors between 4 and 8 and a concentration of the desired product (monoclonal antibody) by a factor of more than 3 was achived. Thus, a combination of the three early steps of the downstream process clarification, concentration and coarse purification was possible. Two different materials were tested: a commercially available agarose-based matrix (Stream-line-SP), and a self-derivatized material based on controlled-pore glass (Bioran). Initial experiments were performed to describe the fluidization of the glass material. Comparison with the agarose material showed several differences, the agarose matrix allowing liquid flow closer to plug flow than the glass material. Increased backmixing in the liquid phase was detected when fluidizing the glass adsorbent compared with the agarose-based matrix. Despite this fact, comparison of the two materials with respect to antibody binding and elution demonstrated a similar performance. (c) 1995 John Wiley & Sons, Inc.     

The Synthesis of Gibberethiones,Gibberellin-related Diterpenoids

The factors affecting desalting by gel chromatography were investigated both experimentally and theoretically. In most cases, the desalting of bovine serum albumin dissolved in an ammonium sulfate solution on a Sephadex G-25 Coarse column was chosen as a model experiment, and the effects of sample volume and concentration on the desalting were examined. The elution curves observed were in fairly good agreement with those calculated on the basis of a mass balance model, when the concentration of ammonium sulfate was lower than 0.4 m. Otherwise, the concentrations of solutes in the eluate were considerably diluted in comparison with the calculated results. Finally, useful charts were illustrated, from which appropriate operational conditions for desalting could be predicted.     

Clarification and capture of high‐concentration refold pools for E. coli‐based therapeutics using expanded bed adsorption chromatography

Expanded bed adsorption (EBA) chromatography was investigated for clarification and capture of high‐concentration refold pools of Escherichia coli‐based therapeutics. Refolding of denatured inclusion bodies (IBs) at high protein concentration significantly improved product throughput; however, direct filtration of the refold materials became very challenging because of high content of protein precipitates formed during refolding. In addition, irreversible protein precipitation caused by high local concentration was encountered in packed bed capture during cation exchange chromatography elution, which limited column loading capacity and capture step productivity. In this study, the two issues are addressed in one unit operation by using EBA. Specifically, EBA can handle feed streams with significant amount of particles and precipitates, which eliminated the need for refold pool clarification through filtration. The relatively broad EBA elution profile is particularly suitable for proteins of low solubility and can effectively avoid product loss previously associated with on‐column precipitation during capture. As the EBA resin (RHOBUST^® FastLine SP IEX) used here has unique properties, it can be operated at high linear velocity (800–1,600 cm/h), while achieving a selectivity and impurity clearance largely comparable to the packed bed resin of the same ligand chemistry (SP Sepharose FF). Furthermore, the filtration of the EBA elution pool is easily manageable within facility capability. Overall, this study demonstrates that the EBA process helps debottleneck the purification of high‐turbidity refold pools by removing precipitates and concurrently capturing the product, which can be applied to other E. coli‐based therapeutics that also requires refolding of IBs. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 30:113–123, 2014     

宁夏枸杞叶总黄酮提取和纯化方法的优化

采用L9(3⁴)正交设计,以黄酮含量为指标,确定的宁夏枸杞叶总黄酮的最佳超声提取方法为: 30倍70%乙醇超声提取50 min,超声功率为250 W;纯化方法条件为: 5倍柱体积70%乙醇洗脱,浓度为4 mg/mL、pH值5.0的上样液,上样速度和洗脱流速均为1 mL/min。并以吸附率、解吸率、回收率等作为考察参数,对提取和纯化方法进行了验证。实验结果表明,该方法简便节时、易操作且毒害小,各项变异系数低。     

Immunoaffinity purification and reconstitution of sodium-coupled branched-chain amino acid carrier of Pseudomonas aeruginosa.

The gene product of braB encoding the Na+(Li+)-coupled carrier protein for L-leucine, L-isoleucine, and L-valine (LIV-II carrier) of Pseudomonas aeruginosa PML strain was identified and overexpressed using a T7 RNA polymerase/promoter plasmid system. The gene product was pulse-labeled with [35S]methionine as a protein of an apparent Mr of 34,000 on a sodium dodecyl sulfate-polyacrylamide gel. Cell membranes overproducing the LIV-II carrier were solubilized with n-dodecyl beta-D-maltopyranoside. The carrier protein was purified from the detergent extract by two purification steps: (i) immunoaffinity column chromatography using purified polyclonal antibody directed against synthetic 13-mer peptide corresponding to the carboxyl terminus region of the carrier and (ii) subsequent DEAE-cellulose column chromatography. The detergent was replaced by n-octyl beta-D-glucopyranoside prior to the first elution and phospholipid was present during purification. Proteoliposomes reconstituted with the purified LIV-II carrier exhibited Na+ or Li+ concentration gradient-driven transport of leucine, isoleucine, and valine. These results show that the LIV-II carrier was purified to be in a functional form.