Maximizing the functional lifetime of Protein A resins

Protein A chromatography is currently the industry gold‐standard for monoclonal antibody and Fc‐fusion protein purification. The high cost of Protein A, however, makes resin lifetime and resin reuse an important factor for process economics. Typical resin lifetime studies performed in the industry usually examine the effect of resin re‐use on binding capacity, yield, and product quality without answering the fundamental question of what is causing the decrease in performance. A two part mechanistic study was conducted in an attempt to decouple the effect of the two possible factors (resin hydrolysis and/or degradation vs. resin fouling) on column performance over lifetime of the most commonly used alkali‐stable Protein A resins (MabSelect SuRe and MabSelect SuRe LX). The change in binding capacity as a function of sodium hydroxide concentration (rate of hydrolysis), temperature, and stabilizing additives was examined. Additionally, resin extraction studies and product cycling studies were conducted to determine cleaning effectiveness (resin fouling) of various cleaning strategies. Sodium hydroxide‐based cleaning solutions were shown to be more effective at preventing resin fouling. Conversely, cold temperature and the use of stabilizing additives in conjunction with sodium hydroxide were found to be beneficial in minimizing the rate of Protein A ligand hydrolysis. An effective and robust cleaning strategy is presented here to maximize resin lifetime and thereby the number of column cycles for future manufacturing processes. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:708–715, 2017     

Improved process analytical technology for protein a chromatography using predictive principal component analysis tools

Protein A chromatography is widely employed for the capture and purification of antibodies and Fc‐fusion proteins. Due to the high cost of protein A resins, there is a significant economic driving force for using these chromatographic materials for a large number of cycles. The maintenance of column performance over the resin lifetime is also a significant concern in large‐scale manufacturing. In this work, several statistical methods are employed to develop a novel principal component analysis (PCA)‐based tool for predicting protein A chromatographic column performance over time. A method is developed to carry out detection of column integrity failures before their occurrence without the need for a separate integrity test. In addition, analysis of various transitions in the chromatograms was also employed to develop PCA‐based models to predict both subtle and general trends in real‐time protein A column yield decay. The developed approach has significant potential for facilitating timely and improved decisions in large‐scale chromatographic operations in line with the process analytical technology (PAT) guidance from the Food and Drug Administration (FDA). Biotechnol. Bioeng. 2011; 108:59–68. © 2010 Wiley Periodicals, Inc.     

Protein a resin lifetime study: Evaluation of protein a resin performance with a model-based approach in continuous capture

A modified shrinking core model (MSCM) has been used to describe the mechanism for the degradation of Protein A resin particles taking place under continuous chromatographic operation. The model is based on the hypothetical shrinkage of the boundary layer of the resin particles, which house the active Protein A ligands within their pores. The caustic during the sanitization phase of chromatography has been determined to cause the Protein A ligand degradation. Protein A resins provided by manufacturers possess unique caustic stability, which has been used in MSCM to appraise the ligand degradation. The kinetic model utilized semiempirical parameters including diffusion constant, rate constant, stoichiometric factor, and reaction order. The parameters were estimated from column breakthrough experiments to simulate continuous Protein A chromatography for three distinct resins. The reaction order has been identified as the key parameter for predicting the degradation kinetics. The recorded reaction orders vary for three different resins with the resin B showing the highest reaction order of 4 and lowest being 1.65 for the resin C. The model can predict the effects of caustic on resin performance and displayed that minimal degradation of the resins A and B occurred, when exposed to 0.1?N and 0.2N NaOH, retaining up to 96% binding capacity after 240?cycles. The adsorption study conducted for the resin B demonstrated the dynamic physical and chemical changes transpiring through the life cycle of the resin, further supported the degradation model. The performance data demonstrate that the resin B exhibits the desirable performance, with higher reaction order indicating slower resin degradation, higher binding capacities, and increased sustenance of this binding capacity for extended duration. The degradation model can be extended to build effective cleaning strategies for continuous downstream processing.     

Viral clearance studies on new and used chromatography resins: critical review of a large dataset.

Viral clearance studies for na?ve and maximally cycled chromatographic resins used for cGMP recombinant protein production are reviewed for three products, comprising 10 different chromatographic steps, including affinity, ion exchange, immobilized metal ion affinity, and hydrophobic interaction modes. Thirty-two separate studies were conducted (over 90 runs in total). No consistent reductions in model virus clearance were observed with used resins. The results address the reproducibility of virus clearance studies conducted by different scientists over several years at multiple contract labs. The log reduction values (LRVs) are typically within 0.5 LRVs for new and used resin, but varied as much as 2 LRVs for resins showing no functional deterioration. This relatively large difference is not believed to reflect resin changes, but highlights the challenges encountered in modeling column clearance. Production column performance and cleaning efficacy are demonstrated for these steps by trending mock runs, impurity removal and product recovery. No deterioration in cGMP column performance is seen over the established resin lifetimes, confirming that the resin regeneration and sanitization procedures restore the resins to a suitable initial state without damage. It is proposed that for some chromatography steps, the combination of lab-scale cycling studies confirming consistent performance throughout the resin lifetime and monitoring of cGMP manufacturing preclude the need for virus clearance studies on maximally cycled resin.     

Demonstrating β-glucan and yeast peptide clearance in biopharmaceutical downstream processes

The use of yeast- and plant-derived hydrolysates in cell culture production processes has sparked concerns over the potential immunogenicity risk posed by β-glucans and yeast peptides contained in these raw materials. This article utilizes a combination of in-process testing from large-scale manufacturing and scale-down spiking studies to demonstrate the clearance of β-glucans and yeast peptides through chromatographic steps in the downstream purification process for a monoclonal antibody. β-Glucans were found to flow through most all three modes of chromatography (Protein A, cation and anion exchange) without binding to the resins or the product. Protein A affinity chromatography was found to provide the best clearance factor. The efficacy of the resin sanitization and storage procedures to prevent carryover from one run to the next was also demonstrated. Yeast peptides were found to be metabolized during the cell culture process and were undetectable after the Protein A purification step. The data presented here serve to allay concerns about the use of hydrolysates in cell culture production. The methodology presented here provides a template to demonstrate clearance of β-glucans and yeast peptides through chromatographic steps in downstream processing.     

Protein A chromatography resin lifetime—impact of feed composition

Adsorbent lifetime during protein A chromatography is not readily predicted or understood, representing a key challenge to be addressed for biopharmaceutical manufacturers. This article focuses on the impact of feed composition on the performance of a typical agarose‐based protein A resin across a lifetime of 50 cycles. Cycling studies were performed using three different feed materials with varying levels of feed components including proteases, histones, DNA, and nonhistone proteins. Changes in the process and quality attributes were measured. The DBCs were not seen to vary between conditions although there was a reduction in particle porosity in all cases. Fluorescence spectroscopy and LC‐MS/MS were used to identify the contribution and extent of fouling to the observed capacity loss. Residual protein A ligand density and deposition of foulants (HCP, residual mAb, and DNA) varied between the three feed materials. Resins cycled in feed materials containing high concentrations of HCP and histones were seen to have greater extents of capacity loss. The mode of performance loss, capacity loss, or impact on product quality was seen to vary depending on the feed material. The results indicate that feed material composition may be correlated to the rate and mode of resin aging as a basis for improved process understanding. © 2018 American Institute of Chemical Engineers Biotechnol. Prog., 34:412–419, 2018     

Evaluation of a novel methacrylate‐based protein a resin for the purification of immunoglobulins and Fc‐fusion proteins

Protein A affinity chromatography is a central part of most commercial monoclonal antibody and Fc‐fusion protein purification processes. In the last couple years an increasing number of new Protein A technologies have emerged. One of these new Protein A technologies consists of a novel, alkaline‐tolerant, Protein A ligand coupled to a macroporous polymethacrylate base matrix that has been optimized for immunoglobulin (Ig) G capture. The resin is interesting from a technology perspective because the particle size and pore distribution of the base beads are reported to have been optimized for high IgG binding and fast mass transfer, while the Protein A ligand has been engineered for enhanced alkaline tolerance. This resin was subjected to a number of technical studies including evaluating dynamic and static binding capacities, alkaline stability, Protein A leachate propensity, impurity clearance, and pressure–flow behavior. The results demonstrated similar static binding capacities as those achieved with industry standard agarose Protein A resins, but marginally lower dynamic binding capacities. Removal of impurities from the process stream, particularly host cell proteins, was molecule dependent, but in most instances matched the performance of the agarose resins. This resin was stable in 0.1 M NaOH for at least 100 h with little loss in binding capacity, with Protein A ligand leakage levels comparable to values for the agarose resins. Pressure–flow experiments in lab‐scale chromatography columns demonstrated minimal resin compression at typical manufacturing flow rates. Prediction of resin compression in manufacturing scale columns did not suggest any pressure limitations upon scale up. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:1125–1136, 2014     

High-throughput screening of chromatographic separations: IV. Ion-exchange

Ion-exchange (IEX) chromatography steps are widely applied in protein purification processes because of their high capacity, selectivity, robust operation, and well-understood principles. Optimization of IEX steps typically involves resin screening and selection of the pH and counterion concentrations of the load, wash, and elution steps. Time and material constraints associated with operating laboratory columns often preclude evaluating more than 20-50 conditions during early stages of process development. To overcome this limitation, a high-throughput screening (HTS) system employing a robotic liquid handling system and 96-well filterplates was used to evaluate various operating conditions for IEX steps for monoclonal antibody (mAb) purification. A screening study for an adsorptive cation-exchange step evaluated eight different resins. Sodium chloride concentrations defining the operating boundaries of product binding and elution were established at four different pH levels for each resin. Adsorption isotherms were measured for 24 different pH and salt combinations for a single resin. An anion-exchange flowthrough step was then examined, generating data on mAb adsorption for 48 different combinations of pH and counterion concentration for three different resins. The mAb partition coefficients were calculated and used to estimate the characteristic charge of the resin-protein interaction. Host cell protein and residual Protein A impurity levels were also measured, providing information on selectivity within this operating window. The HTS system shows promise for accelerating process development of IEX steps, enabling rapid acquisition of large datasets addressing the performance of the chromatography step under many different operating conditions.     

The role of more than 40 years of improvement in protein A chromatography in the growth of the therapeutic antibody industry

Protein A chromatography has been used as the mAb capture step in the majority of FDA submissions. In this study, the performance of protein A chromatography, as indicated by capacity, operational flow rate, and productivity (rate of mAb production per liter of resin) was examined over its full history to gain insights into the reasons for its consistent use. Protein A productivity and capacity have increased 4.3 and 5.5% a year, respectively, since 1978. In contrast, protein A operational flow rate increased between 1978 and 2001 and then remained constant or declined as further improvements provided only marginal benefits. The productivity of protein A resin and also the mAb bioreactor titer (14% growth) rapidly improved starting in about 1990 to economically provide material for clinical trials. Technology improvement is typically driven by product sales. The sales of protein A resin, as indicated by sales of protein A ligand (21% growth), have closely paralleled the sales of mAbs (20% growth). Both increased rapidly in 2000 after the first major mAb therapeutics were approved and the markets were developed. It is likely that alternatives to protein A chromatography have not been implemented because of the order of magnitude improvement in protein A performance. Protein A membrane adsorbers and monoliths have higher productivity than packed columns due to their short bed heights and high operational flow rates. These devices are not currently practical for large‐scale manufacturing but may represent a format for future improvements in protein A productivity. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:1193–1202, 2016     

Structural and performance characteristics of representative anion exchange resins used for weak partitioning chromatography

Weak partitioning chromatography (WPC) has been proposed for the purification of monoclonal antibodies using an anion exchange (AEX) resin to simultaneously remove both acidic and basic protein impurities. Despite potential advantages, the relationship between resin structure and WPC performance has not been evaluated systematically. In this work, we determine the structure of representative AEX resins (Fractogel® EMD TMAE HiCap, Q Sepharose FF, and POROS 50 HQ) using transmission electron microscopy and inverse size exclusion chromatography and characterize protein interactions while operating these resins under WPC conditions using two mAb monomers, a mAb dimer, mAb multimers, and BSA as model products and impurities. We determine the isocratic elution behavior of the weakly bound monomer and dimer species and the adsorptive and mass transfer properties of the strongly bound multimers and BSA by confocal laser scanning microscopy. The results show that for each resin, using the product K_p value as guidance, salt, and pH conditions can be found where mAb multimers and BSA are simultaneously removed. Isocratic elution and adsorption mechanisms are, however, different for each resin and for the different components. Under WPC conditions, the Fractogel resin exhibited very slow diffusion of both mAb monomer and dimer species but fast adsorption for both mAb multimers and BSA with high capacity for BSA, while the Sepharose resin, because of its small pore size, was unable to effectively remove mAb multimers. The POROS resin was instead able to bind both multimers and BSA effectively, while exhibiting a greater resolution of mAb monomer and dimer species. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:425–434, 2017     

Cleaning characterization of protein drug products using UV-vis spectroscopy

This study uses on-line absorbance monitoring to evaluate cleanability of protein drug products. Characterization and validation of equipment cleanliness is a key requirement for a biopharmaceutical facility. A manufacturing-scale cleaning cycle has to be developed and validated for its ability to clean all of the equipment parts for a given soil. Cleaning validation in a multiproduct fill-finish facility could benefit from using a worst-case-based approach that involves validating the cleaning process for the most difficult to clean product. Such an approach minimizes the number of required validation runs. Scaled-down cleaning evaluations can provide helpful information for evaluating multiple products and determine the worst case. This study presents a simple and rapid technique for bench-scale characterization of cleanability of protein drug products. On-line A280 (UV absorbance at 280 nm) measurements are performed using a fiber optic probe, and the data are used to establish the dynamics of protein dissolution in cleaning solution. The model not only helps to estimate cleaning time of different formulated proteins (and peptides) but also provides insights into the kinetics of cleaning under different thermal and chemical conditions. Protein product degradation during cleaning is also evaluated through gel electrophoresis. Such information is useful in designing new cleaning cycles. While the study is performed using drug products, the model as well as the findings are also applicable for characterization of final purified bulk soils relevant to bulk drug manufacturing.     

Observations on different resin strategies for affinity purification mass spectrometry of a tagged protein

Co-affinity purification mass spectrometry (CoAP-MS) is a highly effective method for identifying protein complexes from a biological sample and inferring important interactions, but the impact of the solid support is usually not considered in design of such experiments. Affinity purification (AP) experiments typically utilize a bait protein expressing a peptide tag such as FLAG, c-Myc, HA or V5 and high affinity antibodies to these peptide sequences to facilitate isolation of a bait protein to co-purify interacting proteins. We observed significant variability for isolation of tagged bait proteins between Protein A/G Agarose, Protein G Dynabeads, and AminoLink resins. While previous research identified the importance of tag sequence and their location, crosslinking procedures, reagents, dilution, and detergent concentrations, the effect of the resin itself has not been considered. Our data suggest the type of solid support is important and, under the conditions of our experiments, AminoLink resin provided a more robust solid-support platform for AP-MS.     

Evaluation of new affinity chromatography resins for polyclonal,oligoclonal and monoclonal antibody pharmaceuticals

The performance of MabSelect SuRe and IgSelect affinity chromatography resins designed for process-scale purification of antibodies was investigated. Various antibodies (4 human monoclonal, 1 human polyclonal and 1 bovine polyclonal antibody and 1 Fc-fusion protein) were used to evaluate the elution pH and dynamic binding capacity of the resins. The elution pH for each human antibody was similar on MabSelect SuRe and IgSelect (pH 3.5–3.8). No significant differences in dynamic binding capacity were observed among human antibodies on MabSelect SuRe (∼20–40 mg/mL resin) and IgSelect (∼10–30 mg/mL resin). The binding capacity order for the human antibodies was the same on MabSelect SuRe and IgSelect. Using a linear pH gradient, both resins were able to partially separate monomeric and aggregated forms of the antibodies. The results indicate that these new affinity resins are powerful tools for the purification of human polyclonal antibodies from transgenic animals and oligoclonal antibodies from CHO cell cultures.     

Model-based rational strategy for chromatographic resin selection

A model-based rational strategy for the selection of chromatographic resins is presented. The main question being addressed is that of selecting the most optimal chromatographic resin from a few promising alternatives. The methodology starts with chromatographic modeling,parameters acquisition, and model validation, followed by model-based optimization of the chromatographic separation for the resins of interest. Finally, the resins are rationally evaluated based on their optimized operating conditions and performance metrics such as product purity, yield, concentration, throughput, productivity, and cost. Resin evaluation proceeds by two main approaches. In the first approach, Pareto frontiers from multi-objective optimization of conflicting objectives are overlaid for different resins, enabling direct visualization and comparison of resin performances based on the feasible solution space. The second approach involves the transformation of the resin performances into weighted resin scores, enabling the simultaneous consideration of multiple performance metrics and the setting of priorities. The proposed model-based resin selection strategy was illustrated by evaluating three mixed mode adsorbents (ADH, PPA, and HEA) for the separation of a ternary mixture of bovine serum albumin, ovalbumin, and amyloglucosidase. In order of decreasing weighted resin score or performance, the top three resins for this separation were ADH [PPA[HEA. The proposed model-based approach could be a suitable alternative to column scouting during process development, the main strengths being that minimal experimentation is required and resins are evaluated under their ideal working conditions, enabling a fair comparison. This work also demonstrates the application of column modeling and optimization to mixed mode chromatography.     

Antibody capture from corn endosperm extracts by packed bed and expanded bed adsorption

Topical treatments of chronic infections with monoclonal antibodies will require large quantities of antibodies. Because plants have been proven capable of producing multisubunit antibodies and provide for large-scale production, they are likely hosts to enable such applications. Recovery costs must also be low because of the relatively high dosages required. Hence, we have examined the purification of a human secretory antibody from corn endosperm extracts by processing alternatives of packed bed and expanded bed adsorption (EBA). Because of the limited availability of the transgenic corn host, the system was modeled by adding the antibody to extracts of nontransgenic corn endosperm. Complete clarification of a crude extract followed by packed bed adsorption provided antibody product in 75% yield with 2.3-fold purification (with antibody accounting for 24% of total protein). The small size of the packed bed, cation-exchange resin SP-Sepharose FF and the absence of a dense core (present in EBA resins) allowed for more favorable breakthrough performance compared to EBA resins evaluated. Four adsorbents specifically designed for EBA operation, with different physical properties (size and density), chemical properties (ligand), and base matrices were tested: SP-steel core resin (UpFront Chromatography), Streamline SP and Streamline DEAE (Amersham Biosciences), and CM Hyper-Z (BioSepra/Ciphergen Biosystems). Of these, the small hyperdiffuse-style resin from BioSepra had the most favorable adsorption characteristics. However, it could not be utilized with crude feeds due to severe interactions with corn endosperm solids that led to bed collapse. UpFront SP-steel core resin, because of its relatively smaller size and hence lower internal mass transfer resistance, was superior to the Streamline resins and operated successfully with application of a crude corn extract filtered to remove all solids of >44 microm. However, the EBA performance with this adsorbent provided a yield of only 61% and purification factor of 2.1 (with antibody being 22% of total protein). Process simulation showed that capital costs were roughly equal between packed and expanded bed processes, but the EBA design required four times greater operating expenditures. The use of corn endosperm as the starting tissue proved advantageous as the amount of contaminating protein was reduced approximately 80 times compared to corn germ and approximately 600 times compared to canola. Finally, three different inlet designs (mesh, glass beads, and mechanical mixing) were evaluated on the basis of their ability to produce efficient flow distribution as measured by residence time distribution analysis. All three provided adequate distribution (axial mixing was not as limiting as mass transfer to the adsorption process), while resins with different physical properties did not influence flow distribution efficiency values (i.e., Peclet number and HETP) when operated with the same inlet design.     

Polymer‐mediated flocculation of transient CHO cultures as a simple,high throughput method to facilitate antibody discovery

Most biopharmaceutical drugs, especially monoclonal antibodies (mAbs), bispecific antibodies (BsAbs) and Fc‐fusion proteins, are expressed using Chinese Hamster Ovary (CHO) cell lines. CHO cells typically yield high product titers and high product quality. Unfortunately, CHO cell lines also generate high molecular weight (HMW) aggregates of the desired product during cell culture along with CHO host cell protein (HCP) and CHO DNA. These immunogenic species, co‐purified during Protein A purification, must be removed in a multi‐step purification process. Our colleagues have reported the use of a novel polymer‐mediated flocculation step to simultaneously reduce HMW, HCP and DNA from stable CHO cell cultures prior to Protein A purification. The objective of this study was to evaluate this novel “smart polymer” (SmP) in a high throughput antibody discovery workflow using transiently transfected CHO cultures. SmP treatment of 19 different molecules from four distinct molecular categories (human mAbs, murine mAbs, BsAbs and Fabs) with 0.1% SmP and 25 mM stimulus resulted in minimal loss of monomeric protein. Treatment with SmP also demonstrated a variable, concentration‐dependent removal of HMW aggregates after Protein A purification. SmP treatment also effectively reduced HCP levels at each step of mAb purification with final HCP levels being several fold lower than the untreated control. Interestingly, SmP treatment was able to significantly reduce high concentrations of artificially spiked levels of endotoxin in the cultures. In summary, adding a simple flocculation step to our existing transient CHO process reduced the downstream purification burden to remove impurities and improved final product quality. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:1393–1400, 2017     

Selective removal of closely related clipped protein impurities using poly(ethylenimine)- grafted anion-exchange chromatography resin

Abstract

Proteolytic degradation is a serious problem that complicates downstream processing during production of recombinant therapeutic proteins. It can lead to decreased product yield, diminished biological activity, and suboptimal product quality. Proteolytic degradation or protein truncation is observed in various expression hosts and is mostly attributed to the activity of proteases released by host cells. Since these clipped proteins can impact pharmacokinetics and immunogenicity in addition to potency, they need to be appropriately controlled to ensure consistency of product quality and patient safety. A chromatography step for the selective removal of clipped proteins from an intact protein was developed in this study. Poly(ethylenimine)-grafted anion- exchange resins (PolyQUAT and PolyPEI) were evaluated and compared to traditional macroporous anion-exchange and tentacled anion-exchange resins. Isocratic retention experiments were conducted to determine the retention factors (k′) and charge factors (Z) were determined through the classical stoichiometric displacement model. High selectivity in separation of closely related clipped proteins was obtained with the PolyQUAT resin. A robust design space was established for the PolyQUAT chromatography through Design-Of-Experiments (DoE) based process optimization. Results showed a product recovery of up to 63% with purity levels >99.0%. Approximately, one-log clearance of host cell protein and two-logs clearance of host cell DNA were also obtained. The newly developed PolyQUAT process was compared with an existing process and shown to be superior with respect to the number of process steps, process time, process yield, and product quality.     

The effect of protein a cycle number on the performance and lifetime of an anion exchange polishing step

Most mAb platform purification processes consist of an affinity capture step followed by one or two polishing steps. An understanding of the performance linkages between the unit operations can lead to robust manufacturing processes. In this study, a weak‐partitioning anion‐exchange chromatography polishing step used in a mAb purification process was characterized through high‐throughput screening (HTS) experiments, small‐scale experiments including a cycling study performed on qualified scale‐down models, and large‐scale manufacturing runs. When material from a Protein A column that had been cycled <10× was loaded on the AEX resin, early breakthrough of impurities and premature loss of capacity was observed. As the cycle number on the Protein A resin increased, the capacity of the subsequent AEX step increased. Different control strategies were considered for preventing impurity breakthrough and improving AEX resin lifetimes. Depth filtration of the Protein A peak pool significantly improved the AEX resin capacity, robustness, and lifetime. Further, the turbidity of the Protein A pool has the potential for use as an in‐process control parameter for monitoring the performance of the AEX step. Biotechnol. Bioeng. 2013; 110: 1142–1152. © 2012 Wiley Periodicals, Inc.     

Advective hydrogel membrane chromatography for monoclonal antibody purification in bioprocessing

Protein A chromatography is widely employed for the capture and purification of monoclonal antibodies (mAbs). Because of the high cost of protein A resins, there is a significant economic driving force to seek new downstream processing strategies. Membrane chromatography has emerged as a promising alternative to conventional resin based column chromatography. However, to date, the application has been limited to mostly ion exchange flow through (FT) mode. Recently, significant advances in Natrix hydrogel membrane has resulted in increased dynamic binding capacities for proteins, which makes membrane chromatography much more attractive for bind/elute operations. The dominantly advective mass transport property of the hydrogel membrane has also enabled Natrix membrane to be run at faster volumetric flow rates with high dynamic binding capacities. In this work, the potential of using Natrix weak cation exchange membrane as a mAb capture step is assessed. A series of cycle studies was also performed in the pilot scale device (> 30 cycles) with good reproducibility in terms of yield and product purities, suggesting potential for improved manufacturing flexibility and productivity. In addition, anion exchange (AEX) hydrogel membranes were also evaluated with multiple mAb programs in FT mode. Significantly higher binding capacity for impurities (support mAb loads up to 10Kg/L) and 40X faster processing speed were observed compared with traditional AEX column chromatography. A proposed protein A free mAb purification process platform could meet the demand of a downstream purification process with high purity, yield, and throughput. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:974–982, 2015     

Weak partitioning chromatography for anion exchange purification of monoclonal antibodies

Weak partitioning chromatography (WPC) is an isocratic chromatographic protein separation method performed under mobile phase conditions where a significant amount of the product protein binds to the resin, well in excess of typical flowthrough operations. The more stringent load and wash conditions lead to improved removal of more tightly binding impurities, although at the cost of a reduction in step yield. The step yield can be restored by extending the column load and incorporating a short wash at the end of the load stage. The use of WPC with anion exchange resins enables a two-column cGMP purification platform to be used for many different mAbs. The operating window for WPC can be easily established using high throughput batch-binding screens. Under conditions that favor very strong product binding, competitive effects from product binding can give rise to a reduction in column loading capacity. Robust performance of WPC anion exchange chromatography has been demonstrated in multiple cGMP mAb purification processes. Excellent clearance of host cell proteins, leached Protein A, DNA, high molecular weight species, and model virus has been achieved.