The distinctive separation attributes of mixed-mode resins and their application in monoclonal antibody downstream purification process

Increased upstream productivity and the continuous pressure to deliver high quality drug product have resulted in the development of new separation technologies and platform strategies for downstream purification processes of monoclonal antibodies (mAb). In this study, the separation attributes of three mixed-mode resins, Mercapto-Ethyl-Pyridine (MEP) hydrophobic charge induction resin, Capto adhere multi-modal anion exchange resin, and ceramic hydroxyapatite/fluoroapatite (CHT/CFT) resins, were investigated to define their roles in monoclonal antibody purification processes. We demonstrated that the multi-modal nature of ligands on mixed-mode resins allows the separation resolution to be honed, either through a single dominant mechanism or through mix-modal balanced purification strategies. In addition, the three mixed-mode resins present different purification powers for different types of impurities. We also demonstrated that besides enhancing chromatography separation and improve product quality, especially for high molecular weight (HMW) aggregate reduction, mixed-mode resins can also help to improve process efficiency in industrial-scale mAb drug manufacturing. Our results underscore the importance of selecting appropriate chromatography resins during DSP design to obtain the best overall process outcome.     

Oligonucleotide trapping method for purification of transcription factors

Initial purification of two serotypic variants of recombinant botulinum neurotoxin toxin heavy chain fragment [rBoNT(Hc)], produced intracellularly in the yeast Pichia pastoris, using hydrophobic charge induction chromatography (HCIC) is reported. HCIC employs a matrix containing a weakly ionizable ligand that binds proteins through hydrophobic interactions at neutral pH and elutes the proteins by charge repulsion at acidic pH. HCIC optimization led to different purification conditions for each of the proteins even though they have 58% sequence similarity. The HCIC resin has a higher affinity for the fragment of serotype A than that of serotype B. The 10% dynamic breakthrough capacity for the serotype A fragment is >12.5 mg per ml of resin and is approximately 3.5 mg or the serotype B fragment per ml of resin. Stable elution conditions are also different for the two serotypes. The serotype A fragment is unstable when citrate is used to elute the product. However the serotype B fragment is stable when eluted with citrate buffer, and it is further purified by a overnight precipitation caused by the citrate buffer. This paper reports the development strategy, dynamic capacity breakthrough curves, resin and separation reproducibility, and preliminary scale-up data. The summation of the data demonstrates that HCIC is a scaleable process step for biopharmaceutical production of rBoNT(Hc) proteins.     

Protein A chromatography: Challenges and progress in the purification of monoclonal antibodies

Antibodies for therapeutic use are being continuously approved and their demand has been steadily growing. As known, the golden standard for monoclonal antibody (mAb) purification is Protein A affinity chromatography, a technology that has gained high interest because of its great performance and capabilities. The main concerns are the elevated resins costs and their limited lifetime compared to other resins (e.g. ion exchange chromatography). Great efforts have been carried out to improve purification conditions, such as resin characterization and designing alkali/acid stable resins with a longer lifetime. Modification of Protein A ligands and alternative formats such as monoliths membranes and microshperes have been tested to increase the purification performance. New technology has been proposed to improve the large‐scale separation; in addition, alternative ligands have been suggested to capture mAbs instead of Protein A ligand; however, most of the information is locked by pharmaceutical companies. This mini review summarizes and describes the advances, results, and impact on the Protein A chromatography purification processing.     

Evaluation and comparison of alternatives to Protein A chromatography Mimetic and hydrophobic charge induction chromatographic stationary phases

In this paper Protein A mimetic and hydrophobic charge induction chromatographic (HCIC) stationary phases are characterized in terms of their protein adsorption characteristics and their selectivity is compared with Protein A chromatography using a set of Chinese hamster ovary-derived monoclonal antibodies and Fc-fusion proteins. Linear retention experiments were employed to compare the selectivities of these resins for both non-IgG model proteins as well as antibodies and the fusion proteins. While none of the non-IgG model proteins were observed to bind to the Protein A resin, most of them did in fact bind to the alternative resins. In addition, while the elution pH was similar for the model proteins and antibodies on the HCIC resin, the mimetic resins did exhibit higher binding for the antibodies under these linear pH gradient conditions. A mixed mode preparative isotherm model previously developed for HCIC was shown to accurately describe the adsorption behavior of the mimetic materials as well. Host cell protein clearance profiles were also investigated under preparative conditions using complex biological feeds and the results indicated that while some selectivity was observed for both the HCIC and the mimetic materials, the purification factors were in general significantly less than those obtained with Protein A. It is important to note, however, that the selectivity of the mimetic and HCIC materials was also observed to be antibody specific indicating that further optimization may well result in increased selectivities for these materials.     

Protein adsorption isotherm behavior in hydrophobic interaction chromatography

The adsorption behavior of proteins in hydrophobic interaction chromatography (HIC) was evaluated by determining the isotherms of a wide range of proteins on various HIC resin systems. Parallel batch experiments were carried out with eleven proteins on three hydrophobic resins with different ligand chemistries and densities. The effects of salt concentration, resin chemistry and protein properties on the isotherms were also examined. The resulting isotherms exhibited unique patterns of adsorption behaviors. For certain protein-resin combinations, a "critical salt behavior" was observed where the amount of protein bound to the resin increased significantly above this salt concentration. Proteins that exhibited this behavior tended to be relatively large with more solvent accessible hydrophobic surface area. Further, calculations indicated that under these conditions the occupied surface area of the adsorbed protein layer could exceed the accessible surface area. The establishment of unique classes of adsorption behavior may shed light on our understanding of the behavior of proteins in HIC systems.     

Factorial screening of antibody purification processes using three chromatography steps without protein A

Protein A affinity chromatography is often employed as a capture step to meet the purity, yield, and throughput requirements for pharmaceutical antibody purification. However, a trade-off exists between step performance and price. Protein A resin removes 99.9% of feed stream impurities; however, its price is significantly greater than those of non-affinity media. With many therapeutic indications for antibodies requiring high doses and/or chronic administration, the consideration of process economics is critical. We have systematically evaluated the purification performance of cation-exchange, anion-exchange, hydroxyapatite, hydrophobic interaction, hydrophobic charge induction, and small-molecule ligand resins in each step of a three-step chromatographic purification process for a CHO-derived monoclonal antibody. Host cell proteins were removed to less-than-detectable for three processes (cation-exchange-anion-exchange-hydrophobic interaction chromatography, cation-exchange-anion-exchange-mixed cation-exchange chromatography, and cation-exchange-mixed cation-exchange-anion-exchange chromatography). The order of the process steps affected purification performance significantly.     

Preparation of hydrophobic interaction chromatographic packings based on monodisperse poly(glycidylmethacrylate-co-ethylenedimethacrylate) beads and their application

The monodisperse, poly(glycidylmethacrylate-co-ethylenedimethacrylate) beads with macroporous in the range of 8.0-12.0 microm were prepared by a single-step swelling and polymerization method. The seed particles prepared by dispersion polymerization exhibited good absorption of the monomer phase. The pore size distribution of the beads was evaluated by gel permeation chromatography and mercury instrusion method. Based on this media, a hydrophobic interaction chromatographic (HIC) stationary phase for HPLC was synthesized by a new chemically modified method. The prepared resin has advantages for biopolymer separation, high column efficiency, low column backpressure, high protein mass recovery and good resolution for proteins. The dynamic protein loading capacity of the synthesized HIC packings was 40.0 mg/ml. Six proteins were fast separated in less than 8.0 min using the synthesized HIC stationary phase. The HIC resin was firstly used for the purification and simultaneous renaturation of recombinant human interferon-gamma (rhIFN-gamma) in the extract solution containing 7.0 mol/l guanidine hydrochloride with only one step. The purity and specific bioactivity of the purified of rhIFN-gamma was found more than 95% and 1.3 x 10(8) IU/mg, respectively.     

Purification of an Fc-fusion biologic: clearance of multiple product related impurities by hydrophobic interaction chromatography

An hydrophobic interaction chromatography step was developed for the large-scale production of an Fc-fusion biologic. Two abundant product-related impurities were separated from the active monomer using a Butyl resin and a simple step-wash and step-elution strategy. Capacity and resolution of the HIC step was optimal when sodium sulfate was employed as the lyotropic salt and pore size of the Butyl resin was 750A. Factorial analysis identified critical parameters for the Butyl chromatography and an operating window capable of delivering high product quality and yield over a broad column loading range.     

Hydrophobic interaction chromatography at low salt concentration for the capture of monoclonal antibodies

We evaluated hydrophobic interaction chromatography (HIC) at low salt concentration for the capture of proteins from feed stocks by using monoclonal antibodies as model samples. It was indicated that the HIC at low salt concentration on critical hydrophobicity supports has a potential for capturing hydrophobic monoclonal antibodies directly from large volumes of feed stocks and recovering bound monoclonal antibodies in high yield. On the other hand, the HIC at low salt concentration did not seem so useful for the capture of weakly hydrophobic monoclonal antibodies. The recovery of weakly hydrophobic monoclonal antibodies from columns packed with critical hydrophobicity supports was not quantitative and significantly decreased as the residence time of the monoclonal antibodies in the columns became longer.     

转Bt基因植物表达产物Cry1Ab蛋白的制备纯化方法研究

以转Bt基因水稻为试材,研究其表达产物Cry1Ab蛋白的提取、分离及纯化的方法。实验结果表明,DEAE-纤维素填料对Bt蛋白有较好捕获效果。根据生物信息学方法预测了目标蛋白和主要共存蛋白的等电点和疏水性差异。合理地选择了阴离子交换色谱与疏水作用色谱组合方法。提取液经DEAE-Sephadex A-50柱层析及Phenyl-Sepharose Fast Flow疏水层析分离后,目标蛋白得到了显著的纯化。考察了疏水层析中用不同洗脱液洗脱Cry1Ab蛋白对活性回收率和纯度的影响,结果表明：以0．25mol／L KSCN作洗脱液对活性影响最小,HIC一步纯化倍数可达8倍,总纯化倍数达100倍。     

Purification of antibody heteropolymers using hydrophobic interaction chromatography

A heteropolymer (HP) is a unique dual antibody conjugate composed of specific, chemically cross-linked monoclonal antibodies (mAbs). In this study we have demonstrated that HPs can be purified using hydrophobic interaction chromatography (HIC). Two propyl HIC resins; [PolyPropyl A and EMD Fractogel Propyl (S)] were evaluated in this study. Phosphate buffers, pH 6.5 containing ammonium sulfate or sodium sulfate were used to bind the HP to the column. A descending sulfate gradient or step gradient was used to elute the bound HP species from the column. The HP reaction mixture typically contains multiple conjugated HP species, as well as unreacted monomer mAbs. Conjugated HP product was successfully separated from unreacted antibody monomers with both propyl resins using buffers with ammonium sulfate. There was no monomer separation from HP using buffers with sodium sulfate. The purification processes, presented in this study allows the non-cross-linked antibodies to pass through the column without being bound to the resin, while the cross-linked antibodies (the HP product) bound to the column were subsequently eluted by decreasing the ammonium sulfate concentration in the running buffer. HP product was efficiently separated from free mAbs using Propyl HIC resins at both analytical and preparative scales.     

Loading, stationary phase, and salt effects during hydrophobic interaction chromatography: alpha-lactalbumin is stabilized at high loadings

Amide hydrogen-deuterium exchange labeling has been used to study the effects of salt and protein loading on alpha-lactalbumin (BLA) stability during hydrophobic interaction chromatography (HIC). Stability in the adsorbed phase increased dramatically with increasing loading, and unfolding was nearly undetectable close to the resin saturation capacity. We also found that a butyl surface destabilized BLA more than a phenyl surface, despite the fact that BLA was bound more strongly on the phenyl surface. These observations have important implications for HIC process design and indicate that in some cases column capacity does not have to be sacrificed to preserve protein stability.     

Retention Behavior of Polyethylene Glycol and Its Influence on Protein Elution on Hydrophobic Interaction Chromatography Media

The retention behavior of polyethylene glycol (PEG) on different types of hydrophobic interaction chromatography (HIC) resins containing butyl, octyl, and phenyl ligands was analyzed. An incomplete elution or splitting of the polymer peak into two parts was observed, where the first one was eluted at the dead time of the column, whereas the second one was strongly retained. The phenomenon was attributed to conformation changes of the polymer upon its adsorption on hydrophobic surface. The effect enhanced with increasing molecular weight of the polymer and hydrophobicity of the HIC media. Addition of PEG to the mobile phase reduced binding of proteins to HIC resins, which was demonstrated with two model systems: lysozyme (LYZ) and immunoglobulin G (IgG), and their mixtures. In case of LYZ, the presence of PEG caused reduction in the protein retention, whereas for IgG—a decrease in efficiency of the protein capture. The effect depended on the adsorption pattern of PEG; it was pronounced in the systems in which conformational changes of the polymer were suggested to occur.     

High-throughput protein precipitation and hydrophobic interaction chromatography: salt effects and thermodynamic interrelation

Salt-induced protein precipitation and hydrophobic interaction chromatography (HIC) are two widely used methods for protein purification. In this study, salt effects in protein precipitation and HIC were investigated for a broad combination of proteins, salts and HIC resins. Interrelation between the critical thermodynamic salting out parameters in both techniques was equally investigated. Protein precipitation data were obtained by a high-throughput technique employing 96-well microtitre plates and robotic liquid handling technology. For the same protein-salt combinations, isocratic HIC experiments were performed using two or three different commercially available stationary phases-Phenyl Sepharose low sub, Butyl Sepharose and Resource Phenyl. In general, similar salt effects and deviations from the lyotropic series were observed in both separation methods, for example, the reverse Hofmeister effect reported for lysozyme below its isoelectric point and at low salt concentrations. The salting out constant could be expressed in terms of the preferential interaction parameter in protein precipitation, showing that the former is, in effect, the net result of preferential interaction of a protein with water molecules and salt ions in its vicinity. However, no general quantitative interrelation was found between salting out parameters or the number of released water molecules in protein precipitation and HIC. In other words, protein solubility and HIC retention factor could not be quantitatively interrelated, although for some proteins, regular trends were observed across the different resins and salt types.     

Effect of surface hydrophobicity distribution on retention of ribonucleases in hydrophobic interaction chromatography

The effect of surface hydrophobicity distribution of proteins on retention in hydrophobic interaction chromatography (HIC) was investigated. Average surface hydrophobicity as well as hydrophobic contact area between protein and matrix were estimated using a classical thermodynamic model. The applicability of the model to predict protein retention in HIC was investigated on ribonucleases with similar average surface hydrophobicity but different surface hydrophobicity distribution. It was shown experimentally that surface hydrophobicity distribution could have an important effect on protein retention in HIC. The parameter "hydrophobic contact area," which comes from the thermodynamic model, was able to represent well the protein retention in HIC with salt gradient elution. Location and size of the hydrophobic patches can therefore have an important effect on protein retention in HIC, and the hydrophobic contact area adequately describes this.     

Investigation of salt properties with electro-acoustic measurements and their effect on dynamic binding capacity in hydrophobic interaction chromatography

The pH dependence in hydrophobic interaction chromatography (HIC) is usually discussed exclusively in terms of protein dependence and there are no clear defined trends. Many of the deviations from an ideal solution are caused solely by the high salt concentration, as protein concentration is usually negligible. So pH dependency in hydrophobic interaction chromatography could also be the result of pH dependent changes of ion properties from the salt solution. The possibility that pH dependent ion hydration or ion association in highly concentrated salt solutions may influence the dynamic protein binding capacity onto HIC resins was investigated. In buffer solutions commonly used in HIC e.g. sodium chloride, ammonium sulphate and sodium citrate pH dependent maxima in the electro-acoustic signals were found. These maxima are related to an increase of the ion sizes by hydration or ion association. At low ionic strength the maxima are in the range between 4.5 and 6 and they increased in concentrated electrolyte solutions to values between 6 and 8. The range of these maxima is in the same region as dynamic protein binding capacity maxima often observed in HIC. For a qualitative interpretation of this phenomenon of increased protein stabilization by volume exclusion effect extended scaling theory can be used. This theory predicts a maximum of protein stabilization if the ratio of salt ion diameter to water is 1.8. According to the hypothesis raised here, if the pH dependent ratio of salt ion diameter to water approaches this value the transport of the protein in the pore system is less restricted and an increase in binding capacity can be produced.     

Analytical tools for monitoring changes in physical and chemical properties of chromatography resin upon reuse

Protein A resins are often reused for multiple cycles to improve process economy during mAb purification. Significant reduction in binding capacity and product recovery are typically observed due to the presence of unwanted materials (foulants) deposited on the resin upon reuse. In this paper, we have used a wide spectrum of qualitative and quantitative analytical tools (particle size analysis, HPLC, fluorescence, SEM, MS, and FTIR) to compare the strengths and shortcomings of different analytical tools in terms of their capability to detect the fouling of the resin and relate it to chromatographic cycle performance. While each tool offers an insight into this complex phenomena, fluorescence is the only one that can be used for real‐time monitoring of resin fouling. A correlation could be established between fluorescence intensity and the process performance attributes (like yield or binding capacity) impacted upon resin reuse. This demonstration of the application of fluorescence for real‐time monitoring correlated empirically with process performance attributes and the results support its use as a PAT tool as part of a process control strategy. While the focus of this paper is on fouling of protein A chromatography resin, the approach and strategy are pertinent to other modes of chromatography as well.     

Purification of monoclonal antibody from tobacco extract using membrane-based bioseparation techniques

Transgenic plants offer a promising system for large-scale production of therapeutic proteins such as monoclonal antibodies (mAbs). This paper describes a membrane-based process suitable for purification of a humanized mAb expressed in tobacco. Most monoclonal antibody purification schemes rely on the use of Protein A as the affinity ligand for antibody capture. The main objective of our work was to develop non-Protein A-based purification methods to avoid some of the problems and limitations associated with this ligand, e.g. cost, immunotoxicity, and antibody aggregation during elution. Ion exchange membrane chromatography (IEMC) was used for primary capture and preliminary purification of the mAb from tobacco juice. Hydrophobic interaction membrane chromatography (HIMC) was then used for high-resolution purification, followed by ultrafiltration for polishing, desalting and buffer exchange. Using this scheme, both high mAb purity (single peak in size exclusion chromatogram, i.e., ca. 100% purity) and high recovery (77% of mAb spiked into the tobacco extract) were achieved. Membrane chromatography is generally considered unsuitable for resolving bound proteins by gradient elution and is therefore commonly used in the bind and elute mode with a single-step change of mobile phase. We show that the gradient elution process in the HIMC step can be optimized to increase the resolution and thereby obtain product of high purity.     

Displacement chromatography of proteins on hydrophobic charge induction adsorbent column

Displacement chromatography of protein mixtures is proposed on hydrophobic charge induction chromatography (HCIC). We have used an HCIC medium, MEP-Hypercel as the stationary phase and a quaternary ammonium salt, benzethonium chloride, as the displacer. It was found that the multiple interactions between proteins/displacer and the HCIC sorbent, i.e. hydrophobic interaction and charge repulsion, enabled a greater flexibility for the design of displacement processes and ease of column regeneration by adjustment of pH. The capacity factors of proteins and displacers were used to predict their performances in column displacement, and the experimental results agreed well with the prediction. An isotachic displacement train of lysozyme and alpha-chymotrypsinogen A was formed with benzethonium chloride as the displacer at pH 5.0 with good yields and purities of the two proteins. Column regeneration was efficiently achieved by charge repulsion between the displacer and the adsorbent at lower pH values (pH 3 and 4). The results indicate that the displacement chromatography on HCIC is a good alternative to traditional hydrophobic displacement chromatography.     

Evaluation of recombinant green fluorescent protein, under various culture conditions and purification with HiTrap hydrophobic interaction chromatography resins

To determine the influence of various culture conditions, transformed cells of Escherichia coli expressing recombinant green fluorescent protein (GFPuv) were grown in nine cultures with four variable conditions (storage of inoculated broth at 4°C prior to incubation, agitation speed, isopropyl-β-d-thiogalactopyranoside [IPTG] concentration, and induction time). The pelleted cells were resuspended in extraction buffer and subjected to the three-phase partitioning (TPP) extraction method. To determine the most appropriate purification resin, protein extracts were eluted through one of four types of HiTrap hydrophobic interaction chromatography (HIC) columns prepacked with methyl, butyl, octyl, or phenyl resins and analyzed further on a 12% sodium dodecylsulfatepolyacrylamidegel. With Coomassie staining, a single band between 27 (standard GFPuv) and 29 kDa (molecular weight standard) was visualized for every HIC column sample. TPP extraction with HIC elution provided about 90% of the GFPuv recovered and eight-fold GFPuv enrichment related to the specific mass. Rotary speed and IPTG concentration showed, respectively, greater negative and positive influences on GFPuv expression at the beginning of the logarithmic phase for the set culture conditions (37°C, 24-h incubation).