Pete Gagnon

Technology trends in antibody purification

This article reviews technology trends in antibody purification. Section 1 discusses non-chromatography methods, including precipitation, liquid-liquid extraction, and high performance tangential flow filtration. The second addresses chromatography methods. It begins with discussion of fluidized and fixed bed formats. It continues with stationary phase architecture: diffusive particles, perfusive particles, membranes and monoliths. The remainder of the section reviews recent innovations in size exclusion, anion exchange, cation exchange, hydrophobic interaction, immobilized metal affinity, mixed-mode, and bioaffinity chromatography. Section 3 addresses an emerging trend of formulating process buffers to prevent or correct anomalies in the antibodies being purified. Methods are discussed for preventing aggregate formation, dissociating antibody-contaminant complexes, restoring native antibody from aggregates, and conserving or restoring native disulfide pairing.

Method for obtaining unique selectivities in ion-exchange chromatography by addition of organic polymers to the mobile phase

We have observed that the addition of poly(ethylene glycol) (PEG) to the mobile phase systematically and significantly alters the retention behaviour of proteins in ion-exchange chromatography. The magnitude of the effect is proportional to the molecular mass and concentration of the added PEG. Retention of most proteins is increased, with fair correlation between protein size and degree of enhancement, but with significant influence by variations in protein surface chemistry. The charge on the exchanger and the native (nonenhanced) retention characteristics of the proteins appear to have no effect. Because of its independence from the native selectivity of the ion-exchanger, mobile phase polymer addition creates unique compound selectivites. Addition of PEG also increases viscosity, with the attendant affects of reducing flow-rate and dynamic binding capacity, while increasing eluted peak width.

Nonspecific interactions of chromatin with immunoglobulin G and protein A, and their impact on purification performance

Chromatin released from dead host cells during in vitro production of IgG monoclonal antibodies exists mostly in complex hetero-aggregates consisting of nucleosomal arrays (DNA+histone proteins), non-histone proteins, and aberrant forms of IgG. They bind immobilized protein A more aggressively than IgG, through their nucleosomal histone components, and hinder access of IgG to Fc-specific binding sites, thereby reducing dynamic binding capacity. The majority of host cell contaminants in eluted IgG are leachates from chromatin hetero-aggregates that remain bound to protein A. Formation of turbidity in eluted IgG during pH titration is caused by neutral-pH insolubility of chromatin hetero-aggregates. NaOH is required at 500 mM to remove accumulated chromatin. A chromatin-directed clarification method removed 99% of histones, 90% of non-histone proteins, achieved a 6 log reduction of DNA, 4 log reduction of lipid-enveloped virus, and 5 log reduction of non-enveloped retrovirus, while conserving 98% of the native IgG. This suspended most of performance compromises imposed on protein A. IgG binding capacity increased ~20%. Host protein contamination was reduced about 100-fold compared to protein A loaded with harvest clarified by centrifugation and microfiltration. Aggregates were reduced to less than 0.05%. Turbidity of eluted IgG upon pH neutralization was nearly eliminated. Column cleaning was facilitated by minimizing the accumulation of chromatin.

Characterization and removal of aggregates formed by nonspecific interaction of IgM monoclonal antibodies with chromatin catabolites during cell culture production

We observed that IgM monoclonal antibodies and aggregates in mammalian cell culture supernatants were associated nonspecifically with nucleosomes, DNA, and histone proteins derived from nuclei of host cells that died during antibody production. A series of multimodal sample treatments were evaluated for their ability to selectively remove these contaminants without significant antibody loss. The first consisted of adding 2,5-dioxo-4-imidazolidinyl urea (allantoin) and the DNA intercalating agent 7-ethoxyacridine-3,9-diamine (ethacridine), then flowing the supernatant through a column of mixed porous particles bearing metal affinity, anion exchange, and cation exchange functionalities. A one-step variant of the method was to mix chromatography particles with the allantoin-ethacridine-treated supernatant. An alternative one-step treatment consisted of passing untreated cell supernatant through a chelating monolith in tandem with an anion exchange monolith. All methods eliminated high molecular weight aggregates, and reduced smaller aggregates to 2-4%. They also achieved 98% DNA reduction, 99% reduction of nucleosomes and histones, 30-70% reduction of general host proteins, and 98% IgM recovery. Size exclusion chromatography analysis indicated that IgG monoclonal antibodies benefit similarly from treatment. Subsequent IgM purification reduced DNA levels beneath the level of detectability by fluorescent dye intercalation, histones to less than 10 parts per million by ELISA, and aggregates to less than 0.05% by size exclusion chromatography. The results point to chromatin catabolites as promoters of antibody aggregate formation.

Chromatographic behavior of IgM:DNA complexes.

This study documents the presence of stable complexes between monoclonal IgM and genomic DNA in freshly harvested mammalian cell culture supernatants. 75% of the complex population elutes from size exclusion chromatography with the same retention volume as IgM. DNA comprises 24% of the complex mass, corresponding to an average of 347 base pairs per IgM molecule, distributed among fragments smaller than about 115 base pairs. Electrostatic interactions appear to provide most of the binding energy, with secondary stabilization by hydrogen bonding and metal affinity. DNA-dominant complexes are unretained by bioaffinity chromatography, while IgM-dominant complexes are retained and coelute with IgM. DNA-dominant complexes are repelled from cation exchangers, while IgM-dominant complexes are retained and partially dissociated. Partially dissociated forms elute in order of decreasing DNA content. The same pattern is observed with hydrophobic interaction chromatography. All complex compositions bind to anion exchangers and elute in order of increasing DNA content. A porous particle anion exchanger was unable to dissociate DNA from IgM. Monolithic anion exchangers, offering up to 15-fold higher charge density, achieved nearly complete complex dissociation. The charge-dense monolith surface appears to outcompete IgM for the DNA. Monoliths also exhibit more than double the IgM dynamic binding capacity of the porous particle anion exchanger, apparently due to better surface accessibility and more efficient mass transfer.

Cleavage efficient 2A peptides for high level monoclonal antibody expression in CHO cells

Linking the heavy chain (HC) and light chain (LC) genes required for monoclonal antibodies (mAb) production on a single cassette using 2A peptides allows control of LC and HC ratio and reduces non-expressing cells. Four 2A peptides derived from the foot-and-mouth disease virus (F2A), equine rhinitis A virus (E2A), porcine teschovirus-1 (P2A) and Thosea asigna virus (T2A), respectively, were compared for expression of 3 biosimilar IgG1 mAbs in Chinese hamster ovary (CHO) cell lines. HC and LC were linked by different 2A peptides both in the absence and presence of GSG linkers. Insertion of a furin recognition site upstream of 2A allowed removal of 2A residues that would otherwise be attached to the HC. Different 2A peptides exhibited different cleavage efficiencies that correlated to the mAb expression level. The relative cleavage efficiency of each 2A peptide remains similar for expression of different IgG1 mAbs in different CHO cells. While complete cleavage was not observed for any of the 2A peptides, GSG linkers did enhance the cleavage efficiency and thus the mAb expression level. T2A with the GSG linker (GT2A) exhibited the highest cleavage efficiency and mAb expression level. Stably amplified CHO DG44 pools generated using GT2A had titers 357, 416 and 600 mg/L for the 3 mAbs in shake flask batch cultures. Incomplete cleavage likely resulted in incorrectly processed mAb species and aggregates, which were removed with a chromatin-directed clarification method and protein A purification. The vector and methods presented provide an easy process beneficial for both mAb development and manufacturing.

Principles and applications of steric exclusion chromatography.

We introduce a chromatography method for purification of large proteins and viruses that works by capturing them at a non-reactive hydrophilic surface by their mutual steric exclusion of polyethylene glycol (PEG). No direct chemical interaction between the surface and the target species is required. We refer to the technique as steric exclusion chromatography. Hydroxyl-substituted polymethacrylate monoliths provide a hydrophilic surface and support convective mass transport that is unaffected by the viscosity of the PEG. Elution is achieved by reducing PEG concentration. Selectivity correlates with molecular size, with larger species retained more strongly than smaller species. Retention increases with PEG size and concentration. Salts weaken retention in proportion to their concentration and Hofmeister ranking. Retention is enhanced near the isoelectric point of the target species. Virus binding capacity was measured at 9.9×10(12) plaque forming units per mL of monolith. 99.8% of host cell proteins and 93% of DNA were eliminated. Mass recovery exceeded 90%. IgM capacity was greater than 60 mg/mL. 95% of host cell proteins were eliminated from IgM produced in protein-free media, and mass recovery was up to 90%. Bioactivity was fully conserved by both viruses and antibodies. Process time ranged from less than 30 min to 2 h depending on the product concentration in the feed stream.

Transient conformational modification of immunoglobulin G during purification by protein A affinity chromatography

Exposure of three native IgG1 monoclonal antibodies to 100mM acetate, pH 3.5 had no significant effect on their hydrodynamic size (11.5±0.5nm), while elution from protein A with the same buffer created a conformation of 5.5±1.0nm. Formation of the reduced-size conformation was preceded by the known destabilization of the second constant domain of the heavy chain (Cγ2) by contact with protein A, then compounded by exposure to low pH, creating extended flexibility in the hinge-Cγ2 region and allowing the Fab region to fold over the Fc region. The reduced-size conformation was necessary for complete elution. It persisted unchanged for at least 7 days under elution conditions. Physiological conditions restored native size, and it was maintained on re-exposure to 100mM acetate, pH 3.5. Protein A-mediated destabilization and subsequent restoration of native size did not create aggregates, but the reduced-size conformation was more susceptible to aggregation by secondary stress than native antibody. Protein A-mediated formation of the reduced-size conformation is probably universal during purification of human IgG1 antibodies, and may occur with other subclasses and IgG from other species, as well as Fc-fusion proteins.

Advance chromatin extraction improves capture performance of protein A affinity chromatography

Practical effects of advance chromatin removal on performance of protein A affinity chromatography were evaluated using a caprylic acid-allantoin-based extraction method. Lacking this treatment, the practice of increasing loading residence time to increase capacity was shown to increase host protein contamination of the eluted IgG. Advance chromatin extraction suspended that compromise. Protein A ligand leakage from columns loaded with chromatin-extracted harvest was half the level observed on protein A columns loaded with non-extracted harvest. Columns loaded with chromatin-extracted harvest were cleaned more effectively by 50-100mM NaOH than columns loaded with non-extracted harvest that were cleaned with 250-500mM NaOH. Two protein A media with IgG capacities in excess of 50g/L were loaded with chromatin-extracted harvest, washed with 2.0M NaCl before elution, and the eluted IgG fraction titrated to pH 5.5 before microfiltration. Host protein contamination in the filtrate was reduced to <1ppm, DNA to <1ppb, protein A leakage to 0.5ppm, and aggregates to 1.0%. Caprylic acid and allantoin were both reduced below 5ppm. Step recovery of IgG was 99.4%. Addition of a single polishing step reduced residual protein A beneath the level of detection and aggregates to <0.1%. Overall process recovery including chromatin extraction was 90%.

High productivity purification of immunoglobulin G monoclonal antibodies on starch-coated magnetic nanoparticles by steric exclusion of polyethylene glycol.

We achieved exceptionally high capacity capture of monoclonal IgG by adding 200 nm starch-coated magnetic particles as nucleation centers, adding polyethylene glycol (PEG), then collecting the particle-associated antibody in a magnetic field. Experimental data suggest that accretion of IgG begins on particle surfaces then continues with fusion of particle-centric accretions up to about 1mm in a process that closely parallels PEG precipitation. An embedded nanoparticle mass of 1.3% of the IgG mass is adequate to enable efficient magnetic collection of the associated IgG. Recovery of purified IgG averaged 98% up to loads of 78 mg of IgG per mg of particles. Converted to an equivalent volume of settled particles, this represents about 58 g IgG per mL of nanoparticles, which is roughly 1000 times higher than the average capacity of commercial protein A porous particles packed in columns. When applied to cell culture harvest clarified by centrifugation and microfiltration, performing the nanoparticle technique under physiological conditions permitted only a 10-fold reduction of host cell protein (HCP) contamination and IgG recovery less than 50%. Application of a more capable clarification method and operating the nanoparticle method at 0.5-1.0M NaCl supported more than 99% HCP reduction and 87% IgG recovery. The high salt concentration also dramatically diminished the influence of operating pH on selectivity. The nanoparticle step was followed by sample application without buffer exchange to a column packed with multimodal electropositive-hydrophobic particles that reduced HCP to 2 ppm. Aggregate content was reduced from 4.9 to 3.6% at the nanoparticle step, then to less than 0.05% at the multimodal step. The multimodal step also removed residual PEG. Overall IgG recovery was 69%. The ability of the system to achieve purity similar to protein A, but dramatically higher productivity than packed columns, suggests that the technique could evolve as a credible option for industrial purification of monoclonal antibodies.