Evaluation of eco-friendly zwitterionic detergents for enveloped virus inactivation.

Inclusion of a detergent in protein biotherapeutic purification processes is a simple and very robust method for inactivating enveloped viruses. The detergent Triton X-100 has been used for many years and is part of the production process of several commercial therapeutic proteins. However, recent ecological studies have suggested that Triton X-100 and its break-down products can potentially behave as endocrine disrupters in aquatic organisms, raising concerns from an environmental impact perspective. As such, discharge of Triton X-100 into the waste water treatment plants is regulated in some jurisdictions, and alternative detergents for viral inactivation are required. In this work, we report on the identification and evaluation of more eco-friendly detergents as viable replacements for Triton X-100. Five detergent candidates with low to moderate environmental impact were initially identified and evaluated with respect to protein stability, followed by proof-of-concept virus inactivation studies using a model enveloped virus. From the set of candidates lauryldimethylamine N-oxide (LDAO) was identified as the most promising detergent due to its low ecotoxicity, robust anti-viral activity (LRV >4 at validation set-point conditions with X-MuLX), and absence of any negative impact on protein function. This detergent exhibited effective and robust virus inactivation in a broad range of protein concentrations, solution conductivities, pHs, and in several different cell culture fluid matrices. The only process parameter which correlated with reduced virus inactivation potency was LDAO concentration, and then only when the concentration was reduced to below the detergent's critical micelle concentration (CMC). Additionally, this work also demonstrated that LDAO was cleared to below detectable levels after Protein A affinity chromatography, making it suitable for use in a platform process that utilizes this chromatographic mode for protein capture. All these findings suggest that LDAO may be a practical alternative to Triton X-100 for use in protein therapeutic production processes for inactivating enveloped viruses. Biotechnol. Bioeng. 2017;114: 813-820. © 2016 Wiley Periodicals, Inc.

Evaluation of high-capacity cation exchange chromatography for direct capture of monoclonal antibodies from high-titer cell culture processes.

Advances in molecular biology and cell culture technology have led to monoclonal antibody titers in excess of 10 g/L. Such an increase can pose concern to traditional antibody purification processes due to limitations in column hardware and binding capacity of Protein A resins. Recent development of high capacity cation exchangers can make cation exchange chromatography (CEX) a promising and economic alternative to Protein A capture. This work investigates the feasibility of using CEX for direct capture of monoclonal antibodies from high titer cell culture fluids. Two resin candidates were selected from seven newer generation cation exchangers for their higher binding capacity and selectivity. Two monoclonal antibodies with widely differing pI values were used to evaluate the capability of CEX as a platform capture step. Screening of loading pH and conductivity showed both resins to be capable of directly capturing both antibodies from undiluted cell culture fluid. At appropriate acidic pH range, product loading of over 65 g/L resin was achieved for both antibodies. A systematic design of experiment (DOE) approach was used to optimize the elution conditions for the CEX step. Elution pH showed the most significant impact on clearance of host cell proteins (HCPs). Under optimal conditions, HCP reduction factors in the range of 9-44 were achieved on the CEX step based on the pI of the antibody. Apart from comparing CEX directly to Protein A as the capture method, material from either modality was also processed through the subsequent polishing steps to compare product quality at the drug substance level. Process performance and product quality was found to be acceptable using the non-affinity based process scheme. The results shown here present a cheaper and higher capacity generic capture method for high-titer antibody processes.

Using partition designs to enhance purification process understanding.

Characterization of purification processes by identifying significant input parameters and establishing predictive models is vital to developing robust processes. Current experimental design approaches restrict analysis to one process step at a time, which can severely limit the ability to identify interactions between process steps. This can be overcome by the use of partition designs which can model multiple, sequential process steps simultaneously. This paper presents the application of partition designs to a monoclonal antibody purification process. Three sequential purification steps were modeled using both traditional experimental designs and partition designs and the results compared as a proof of concept study. The partition and traditional design approaches identified the same input parameters within each process step that significantly affected the product quality output examined. The partition design also identified significant interactions between input parameters across process steps that could not be uncovered by the traditional approach.

Modeling on-column reduction of trisulfide bonds in monoclonal antibodies during protein A chromatography.

Trisulfides can be a common post-translational modification in many recombinant monoclonal antibodies. These are a source of product heterogeneity that add to the complexity of product characterization and hence, need to be reduced for consistent product quality. Trisulfide bonds can be converted to the regular disulfide bonds by incorporating a novel cysteine wash step during Protein A affinity chromatography. An empirical model is developed for this on-column reduction reaction to compare the reaction rates as a function of typical operating parameters such as temperature, cysteine concentration, reaction time and starting level of trisulfides. The model presented here is anticipated to assist in the development of optimal wash conditions for the Protein A step to effectively reduce trisulfides to desired levels.

Pool-less processing to streamline downstream purification of monoclonal antibodies.

With cell culture titers and productivity increasing in the last few years, pressure has been placed on downstream purification to look at alternative strategies to meet the demand of biotech products with high dose requirements. Even when the upstream process is not continuous (perfusion based), adopting a more productive and/or continuous downstream process can be of significant advantage. Due to the recent trend in exploring continuous processing options for biomolecules, several enabling technologies have been assessed at Biogen. In this paper, we evaluate the capability of one of these technologies to streamline and improve our downstream mAb purification platform. Current conventional downstream polishing steps at Biogen are operated in flow-through mode to achieve higher loadings while maintaining good selectivity. As titers increase, this would result in larger columns and larger intermediate product pool holding tanks. A semicontinuous downstream process linking the second and third chromatography steps in tandem can reduce/eliminate intermediate holding tanks, reduce overall processing time, and combine unit operations to reduce validation burdens. A pool-less processing technology utilizing inline adjustment functionality was evaluated to address facility fit challenges for three high titer mAbs. Two different configurations of polishing steps were examined: (i) anion exchange and hydrophobic interaction and (ii) anion exchange and mixed mode chromatography. Initial laboratory scale proof of concept studies showed comparable performance between the batch purification process and the pool-less process configuration.

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.

Maximizing binding capacity for protein A chromatography.

Advances in cell culture expression levels in the last two decades have resulted in monoclonal antibody titers of ≥10 g/L to be purified downstream. A high capacity capture step is crucial to prevent purification from being the bottleneck in the manufacturing process. Despite its high cost and other disadvantages, Protein A chromatography still remains the optimal choice for antibody capture due to the excellent selectivity provided by this step. A dual flow loading strategy was used in conjunction with a new generation high capacity Protein A resin to maximize binding capacity without significantly increasing processing time. Optimum conditions were established using a simple empirical Design of Experiment (DOE) based model and verified with a wide panel of antibodies. Dynamic binding capacities of >65 g/L could be achieved under these new conditions, significantly higher by more than one and half times the values that have been typically achieved with Protein A in the past. Furthermore, comparable process performance and product quality was demonstrated for the Protein A step at the increased loading.

Purification of monoclonal antibodies by hydrophobic interaction chromatography under no-salt conditions.

Hydrophobic interaction chromatography (HIC) is commonly used as a polishing step in monoclonal antibody purification processes. HIC offers an orthogonal selectivity to ion exchange chromatography and can be an effective step for aggregate clearance and host cell protein reduction. HIC, however, suffers from the limitation of use of high concentrations of kosmotropic salts to achieve the desired separation. These salts often pose a disposal concern in manufacturing facilities and at times can cause precipitation of the product. Here, we report an unconventional way of operating HIC in the flowthrough (FT) mode with no kosmotropic salt in the mobile phase. A very hydrophobic resin is selected as the stationary phase and the pH of the mobile phase is modulated to achieve the required selectivity. Under the pH conditions tested (pH 6.0 and below), antibodies typically become positively charged, which has an effect on its polarity and overall surface hydrophobicity. Optimum pH conditions were chosen under which the antibody product of interest flowed through while impurities such as aggregates and host cell proteins bound to the column. This strategy was tested with a panel of antibodies with varying pI and surface hydrophobicity. Performance was comparable to that observed using conventional HIC conditions with high salt.

Downstream antibody purification using aqueous two-phase extraction.

The extraction of antibodies using a polyethylene glycol (PEG)-citrate aqueous two-phase system (ATPS) was investigated. Studies using purified monoclonal antibody (mAb) identified operating ranges for successful phase formation and factors that significantly affected antibody partitioning. The separation of antibody and host cell protein (HCP) from clarified cell culture media was examined using statistical design of experiments (DOE). The partitioning of antibody was nearly complete over the entire range of the operating space examined. A model of the HCP partitioning was generated in which both NaCl and citrate concentrations were identified as significant factors. To achieve the highest purity, the partitioning of HCP from cell culture fluid into the product containing phase was minimized using a Steepest Descent algorithm. An optimal ATPS consisting of 14.0% (w/w) PEG, 8.4% (w/w) citrate, and 7.2% (w/w) NaCl at pH 7.2 resulted in a product yield of 89%, an approximate 7.6-fold reduction in HCP levels relative to the clarified cell culture fluid before extraction and an overall purity of 70%. A system consisting of 15% (w/w) PEG, 8% (w/w) citrate, and 15% (w/w) NaCl at pH 5.5 reduced product-related impurities (aggregates and low molecular product fragments) from ∼40% to less than 0.5% while achieving 95% product recovery. At the experimental conditions that were optimized in the batch mode, a scale-up model for the use of counter-current extraction technology was developed to identify potential improvements in purity and recovery that could be realized in the continuous operational mode.