Purification of antisense oligonucleotides using hydrophobic interaction chromatography.

Mixed-mode separation of antisense oligonucleotides using a single column with complementary anion-exchange and hydrophobic interaction chromatography approaches

Hydrophobic interaction chromatography (HIC) uses weakly hydrophobic resins and requires a salting-out salt to promote protein-resin interaction. The salting-out effects increase with protein and salt concentration. Dynamic binding capacity (DBC) is dependent on the binding constant, as well as on the flow characteristics during sample loading. DBC increases with the salt concentration but decreases with increasing flow rate. Dynamic and operational binding capacity have a major raw material cost/processing time impact on commercial scale production of monoclonal antibodies. In order to maximize DBC the highest salt concentration without causing precipitation is used. We report here a novel method to maintain protein solubility while increasing the DBC by using a combination of two salting-out salts (referred to as dual salt). In a series of experiments, we explored the dynamic capacity of a HIC resin (TosoBioscience Butyl 650M) with combinations of salts. Using a model antibody, we developed a system allowing us to increase the dynamic capacity up to twofold using the dual salt system over traditional, single salt system. We also investigated the application of this novel approach to several other proteins and salt combinations, and noted a similar protein solubility and DBC increase. The observed increase in DBC in the dual salt system was maintained at different linear flow rates and did not impact selectivity.

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

Macroporous microspheres were prepared through suspension polymerization, based on a copolymer of glycidyl methacrylate and ethylene glycol dimethacrylate , which were used for functional monomer and crosslinking agent, respectively. The effect of porogen on microspheres structure was evaluated in terms of pore size and surface area. The anion exchanged supports were prepared through derivation of microspheres with poly ( ethylene imine). The relation of the microspheres structure and the protein capacity was examined on these anion exchanged media. The results indicated that the pore size of microspheres increased with the poor solvent in the porogen ( good solvent/poor solvent = 1 : 1-1 : 3. 5 ) , however, the surface area showed a contrary trend. The ion exchanged capacity ( 0. 11-0. 27 mmol/mL) increased with the surface area of the microspheres (4-38 m(2)/g) , and the responding static binding capacity of proteins also show a positive correlation with the surface area. The dynamic binding capacity of proteins firstly increased and then retained a changeless value in the pore range of 301-1524 nm. This value was retained at 13 mg/mL when the pore size was more than 410 nm. It indicated that the surface area could not influence the dynamic binding capacity while the pore size of media was beyond some value. Furthermore, the large biomolecular transport in the microspheres was observed through laser scanning confocal microscopy. The results indicated that hepatitis B virus surface antigen ( HBsAg) could enter freely the microsphere with all of above pore size. The above results provide a reference for fabrication of the chromatographic supports.

Hydrophobic interaction chromatography (HIC) is one of the most frequently used purification methods in downstream processing of biopharmaceuticals. During HIC, salts are the governing additives contributing to binding strength, binding capacity, and protein solubility in the liquid phase. A relatively recent approach to increase the dynamic binding capacity (DBC) of HIC adsorbers is the use of salt mixtures. By mixing chaotropic with kosmotropic salts, the DBC can strongly be influenced. For salt mixtures with a higher proportion of chaotropic than kosmotropic salt, higher DBCs were achieved compared with single salt approaches. By measuring the surface tensions of the protein salt solutions, the cavity theory-proposed by Melander and Horváth-that higher surface tensions lead to higher DBCs, was found to be invalid for salt mixtures. Aggregation temperatures of lysozyme in the salt mixtures, as a degree of hydrophobic forces, were correlated to the DBCs. Measuring the aggregation temperatures has proven to be a fast analytical methodology to estimate the hydrophobic interactions and thus can be used as a measure for an increase or decrease in the DBCs. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:346-354, 2016.

The ideal model of liquid chromatography in gradient elution was solved by using the characteristic approach on the assumption of a linear solvent strength model. By considering the influence of the dwelling time of the chromatographic system on retention time, the retention time formulae suited for any combination of isocratic, linear and stepwise gradients were obtained. It was found that the values of the retention time obtained from these formulae were in well accordance with those computed by using the finite-difference method, which confirms the validity of the formulae. Due to the simplicity and broad scope of applications, these formulae can be easily applied in practice.

Grafting chromatographic monoliths with charged linear polymers for highly productive and selective protein or plasmid DNA purification

Influence of binding pH and protein solubility on the dynamic binding capacity in hydrophobic interaction chromatography

The large scale production of monoclonal antibodies presents a challenge to design efficient and cost effective downstream purification processes. We explored a two stage resin screening approach to identify the best candidates to be utilized for the platform purification of monoclonal antibodies. The study focused on commercially available affinity resins including Protein A, mimetic and mixed-mode interaction resins as well as ion exchangers used in polishing steps. An initial screening using pure proteins was followed by a final screening where selected resins were utilized for the purification of MAbs in complex mixtures. Initial screenings aimed to measure the theoretical upper limit for dynamic binding capacity (DBC) at 1% breakthrough and productivity. We confirmed that DBC of affinity, mimetic and mixed-mode resins was a strong function of the linear velocity used for loading. Productivities >27 g/(L-h), were obtained for rProtein A FF, Mabselect and Prosep rA Ultra at 2 min residence time. For the cation exchangers, we identified UNOsphere S and Fractogel SO(3) as the best candidates for our purification based on DBC. For anion exchangers operated in flowthrough mode, Q Sepharose XL and UNOsphere Q were selected from the initial screening based on DBC and resolution of IgG from BSA. Finally, a three step purification scheme was implemented using the selected affinity and ion exchangers for the purification of IgG from complex feedstocks. We found that Mabselect followed by UNOsphere Q and UNOsphere S provided the best purification scheme for our applications based on productivity.

A large-scale immunoaffinity (IA) purification process was developed for the isolation of recombinant soluble antigen CD4 (sCD4) from Escherichia coli fermentations. The monoclonal antibody used for IA purification of sCD4 recognized a conformation-dependent epitope on the surface of domain 1 of CD4. IA chromatography was used to purify both sCD4-183, consisting of the N-terminal 183 amino acids of human CD4, and sCD4-PE40, a fusion protein consisting of the N-terminal 178 amino acids of CD4 and amino acids 1-3 and 253-613 of Pseudomonas exotoxin A (PE40). sCD4-183 was purified from E. coli cell pellets using cell disruption, protein solubilization, oxidation, Q-Sepharose anion-exchange and IA chromatography steps. sCD4-PE40 was purified from cell pellets using cell disruption, protein solubilization, oxidation, Cu(2+)-immobilized metal-affinity chromatography, anion-exchange and IA chromatography steps. The IA-purified sCD4 analogues demonstrated the correct apparent molecular masses on SDS/PAGE. The immobilized monoclonal antibody appeared to select for correctly folded CD4 protein, since sCD4-183 and sCD4-PE40 purified by the IA method bound human-immunodeficiency-virus glycoprotein gp120 (HIV gp120) in vitro. sCD4-PE40 purified by IA chromatography also inhibited protein synthesis in CV-1 cells expressing HIV gp120/160 at the cell surface. Relatively high recoveries of sCD4-183 and sCD4-PE40 were observed in the IA step of the purification process (71 and 79% recovery respectively). The results demonstrate that immobilized monoclonal antibodies directed against conformational epitopes may be used for rapid purification of gram amounts of correctly folded protein from mixtures of oxidized E. coli proteins.

Study of the dynamic binding capacity of two anion exchangers using bovine serum albumin as a model protein

Deploying two salts in hydrophobic interaction chromatography can significantly increase dynamic binding capacities. Nevertheless, the mechanistic understanding of this phenomenon is lacking. Here, we investigate whether surface tension or ionic strength govern dynamic binding capacities of the chromatographic resin Toyopearl Butyl-650 M in dual salt systems. Small-angle X-ray scattering was employed to analyze the model proteins and the protein-resin adduct in the respective dual salt systems. The dual salt systems incorporate sodium citrate and a secondary sodium salt (acetate, sulfate, or phosphate). As model proteins, we used lysozyme, GFP, and a monoclonal antibody (adalimumab).Moreover, for the protein-resin adduct, we determined the model parameters of a self-avoiding random walk model fitted into the pair density distribution function of the SAXS data. Ionic strength is more predictive for dynamic binding capacities in HIC dual salt systems than surface tension. However, dynamic binding capacities still differ by up to 30 % between the investigated dual salt systems. The proteins exhibit extensive protein-protein interactions in the studied dual salt HIC buffers. We found a correlation of protein-protein interactions with the well-known Hofmeister series. For systems with elevated protein-protein interactions, adsorption isotherms deviate from Langmuirian behavior. This highlights the importance of lateral protein-protein interactions in protein adsorption, where monomolecular protein layers are usually assumed. SAXS analysis of the protein-resin adduct indicates an inverse correlation of the binding capacity and the excluded volume parameter. This is indicative of the deposition of proteins in the cavities of the stationary phase. We hypothesize that increasing protein-protein interactions allow the formation of attractive clusters and multilayers in the cavities, respectively.

A new and simplified anion exchange chromatographic process for the purification of cell-grown influenza A H1N1 virus

The demand for plasmid DNA (pDNA) has increased in recent years, but due to their physical properties there are some inherent challenges to the purification of these molecules. A typical downstream process for plasmids normally has multiple steps after fermentation, and anion exchange followed by hydrophobic interaction chromatography are commonly utilized. Thermo Fisher Scientific has developed a variety of resins well-suited for these steps, designed to simplify workflows and increase purity and yield. A series of experiments were conducted in order to evaluate POROSTM AEX resins for pDNA capture, with the goals of optimizing process conditions to maximize purity and recovery, determining the dynamic binding capacity (DBC) of POROS AEX resins for pDNA, and confirming optimal operating parameters.  Some highlights of these studies, performed in collaboration with the Fraunhofer Institute for Molecular Biology, Germany, are presented here.  To find out more, read the full discussion here.

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.