Ion-exchange Chromatography Of Proteins Research Articles

An accelerated approach for mechanistic model based prediction of linear gradient elution ion-exchange chromatography of proteins

With growing demands for therapeutic monoclonal antibodies, in silico downstream process development based on mechanistic modeling of chromatography separation process is being increasingly used for process optimization and process characterization. Application of mechanistic modeling in biopharmaceutical industry has been sparse due to the significant investment of time and resources that are required for performing model calibration. Mechanistic modeling of the chromatography process involves a large number of mass transport and binding parameters and their initial input values are required for simulations. These input values of column parameters can be easily obtained either from experiments or from empirical correlations available in literature. On the other hand, obtaining the model input valves for binding kinetic parameters is usually a cumbersome process as it involves performing batch experiments which are not only tedious but also require significant quantities of purely isolated main product and its related impurities, which is challenging as the product related impurities are typically present in smaller quantities and hence are difficult to obtain as pure species. In the present work, a mechanistic model that is based on the general rate model coupled with extended Langmuir binding model has been used for prediction of linear gradient elution peaks of monoclonal antibody on cation exchanger chromatography. The present work describes an accelerated approach for obtaining the input values for binding kinetic parameters in the extended Langmuir binding model from the two Yamamoto coefficient A and B values obtained by Yamamoto method directly from the model calibration linear gradient elution runs of different gradient slopes and at low to moderate protein loadings. The equations that can relate the two coefficients to the extended Langmuir model equation binding kinetic parameters were derived. Therefore, once A and B are determined, the binding kinetic parameter values were determined straightforward, thereby avoiding the problem of multiple solutions for the model parameters. The estimated binding parameters were successfully validated from isocratic elution experiments performed at low loading. What we demonstrate is that the proposed approach allows us to estimate binding kinetic parameters in a significantly more efficient and accelerated manner than presently used approaches, thereby accelerating development and implementation of mechanistic modeling for process chromatography.

Robust mechanistic modeling of protein ion-exchange chromatography

Mechanistic models for ion-exchange chromatography of proteins are well-established and a broad consensus exists on most aspects of the detailed mathematical and physical description. A variety of specializations of these models can typically capture the general locations of elution peaks, but discrepancies are often observed in peak position and shape, especially if the column load level is in the non-linear range. These discrepancies may prevent the use of models for high-fidelity predictive applications such as process characterization and development of high-purity and -productivity process steps. Our objective is to develop a sufficiently robust mechanistic framework to make both conventional and anomalous phenomena more readily predictable using model parameters that can be evaluated based on independent measurements or well-accepted correlations. This work demonstrates the implementation of this approach for industry-relevant case studies using both a model protein, lysozyme, and biopharmaceutical product monoclonal antibodies, using cation-exchange resins with a variety of architectures (SP Sepharose FF, Fractogel EMD SO3−, Capto S and Toyopearl SP650M). The modeling employs the general rate model with the extension of the surface diffusivity to be variable, as a function of ionic strength or binding affinity. A colloidal isotherm that accounts for protein-surface and protein-protein interactions independently was used, with each characterized by a parameter determined as a function of ionic strength and pH. Both of these isotherm parameters, along with the variable surface diffusivity, were successfully estimated using breakthrough data at different ionic strengths and pH. The model developed was used to predict overloads and elution curves with high accuracy for a wide variety of gradients and different flow rates and protein loads. The in-silico methodology used in this work for parameter estimation, along with a minimal amount of experimental data, can help the industry adopt model-based optimization and control of preparative ion-exchange chromatography with high accuracy.

Empirical correction of non-linear pH gradients and a tool for application to protein ion exchange chromatography

This concept article reports a practical solution to improve the linearity of effluent pH response as observed in pH gradient cation exchange chromatography (CEX). When performing pH gradient CEX, it is not easy to develop buffer systems that will universally provide pH response proportional with the mobile phase (buffer) composition. It is an especially challenging pursuit when exploring MS compatible buffers (e.g. ammonium-acetate, ammonium-carbonate). In addition to „non-proportional” behavior from the mobile phase composition, the chromatographic column itself will sometimes impose an unpredictable impact on the effluent pH. Here, we propose a simple approach based on the on-line measurement of effluent pH response, conversion of pH to mobile phase volume fraction (φ) and then generation of the inverse response function in the time domain. In the end, when setting the inverse function as the gradient program instead of a linear gradient, an improved – ideally linear - pH response can be produced. A simple Excel tool was developed to assist analysts with this correction procedure, and it has been made available by download for public use.

Adsorption of colloidal proteins in ion-exchange chromatography under consideration of charge regulation

Mechanistic modeling of protein adsorption has gained increasing importance in the development of ion-exchange (IEX) chromatography processes. The most common adsorption models use a stoichiometric representation of the adsorption process based on the law of mass action. Despite the importance of these models in model-based development, the stoichiometric representation of the adsorption process is not accurate for the description of long-range electrostatic interactions in IEX chromatography, limiting the application and mechanistic extension of these models.In this work an adsorption model is introduced describing the non-stoichiometric electrostatic interaction in IEX chromatography based on the linear Poisson–Boltzmann equation and a simplified colloidal representation of the protein. In contrast to most recent non-stoichiometric models, the introduced model accounts for charge regulation during the adsorption process. Its capability of describing the adsorption equilibrium is demonstrated by simulating partitioning coefficients of multiple proteins on different adsorber systems as a function of ionic strength and pH. Despite model simplifications the physical meaning and predictive value of the model could be preserved. By transferring model parameters of a monoclonal antibody (mAb) from one adsorber system to another, it could be demonstrated that protein parameters are theoretically not only valid on a specific adsorber system but freely transferable to other adsorbers. The predictive value of the mechanistic model on the new adsorber system was highlighted by predicting the elution behavior of charge variants of the mAb.

Prediction tool for loading, isocratic elution, gradient elution and scaling up of ion exchange chromatography of proteins

An efficient mathematical tool for the design and scaling up of protein chromatography is suggested, in which the model parameters can be determined quickly over a wide operating space without large material investments. The design method is based on mathematical modelling of column dynamics and moment analysis. The accuracy of the dynamic models that are most frequently used for simulations of chromatographic processes is analyzed, and possible errors that can be generated using the moment analysis are indicated. The so-called transport dispersive model was eventually employed for the process simulations. The model was modified to account for the protein dispersion in void volumes of chromatographic systems. The manner of the model calibration was suggested, which was based on a few chromatographic runs and verified over a wide space of the operating parameters, including composition and flow rate of the mobile phase, column dimensions, residence time, and mass loading. The model system for the study was ion-exchange chromatography. The analysis was performed based on the elution profiles of basic fibroblast growth factor 2 and lysozyme, on two different IEX media.

Protein ion-exchange chromatography on a biomacromolecule-immobilized monolithic cryogel

Protein ion-exchange chromatography on a biomacromolecule-immobilized monolithic cryogel

High uptake rate and extremely salt-tolerant behavior of protein adsorption to 900 kDa poly(allylamine)-modified Sepharose FF

This work reports poly(allylamine) of 900 kDa (PAA-L) as a polymeric ligand for protein ion-exchange chromatography. PAA-L-modified Sepharose FF with 9 ionic capacities (ICs) from 80 to 880 mmol/L were prepared and bovine serum albumin adsorption and chromatography were investigated. With increasing IC, protein adsorption capacity increased somewhat in the IC range of 80–420 mmol/L, and then increased twice in the IC range of 420–740 mmol/L, and finally kept unchanged till 880 mmol/L; the uptake rate (De/D0) increased about 14 times (from 0.029 to 0.42) in the IC range of 420–700 mmol/L, and finally kept almost unchanged till 880 mmol/L. The maximum adsorption capacity and uptake rate of the resins reached 336 mg/mL and 0.42, which were 24% and 2.5 times respectively larger than those of 17.5 kDa PAA-grafted resins. The selected PAA-L resin of IC = 740 mmol/L was salt-tolerant up to 750 mmol/L NaCl. The dynamic binding capacity (DBC) of this resin showed a maximum of 142 mg/mL at 350 mmol/L NaCl, and kept over 90 mg/mL in the range of 150–500 mmol/L NaCl. Linear gradient elution on the column of this resin proved high protein recovery (>97%) and stability of the column. Taken together, the results indicate that the PAA-L resin was a promising anion exchanger for high-performance protein chromatography for use at extended ionic strengths.

Ion-exchange chromatography of proteins: the inside story

Despite its inherent inefficiencies, chromatography remains the workhorse for protein purification in the pharmaceutical and biotechnology industries, with ion exchange the most widely used mode. Many aspects of a chromatographic process are still optimized empirically, but modeling is increasingly used to aid in scale-up and optimization. An overview is presented here of the needs that remain for greater insights that can inform truly predictive modeling of preparative protein separations by ion-exchange chromatography as well as guiding rational design considerations and effective heuristics. These needs can be addressed by a more complete mechanistic understanding of the relation between adsorbent and protein structure and the values of key functional parameters describing adsorption and transport. A principal focus is on specialized experimental and modeling approaches to obtain such insights; these include molecular-level models, various modes of microscopy, and chromatographic and other methods for inferring intracolumn and intraparticle behavior. The principal findings revolve around the critical role for fundamental principles of classical chemical engineering, albeit specialized for the peculiar physicochemical properties of protein solutions.

High ionic strength narrows the population of sites participating in protein ion-exchange adsorption: A single-molecule study

The retention and elution of proteins in ion-exchange chromatography is routinely controlled by adjusting the mobile phase salt concentration. It has repeatedly been observed, as judged from adsorption isotherms, that the apparent heterogeneity of adsorption is lower at more-eluting, higher ionic strength. Here, we present an investigation into the mechanism of this phenomenon using a single-molecule, super-resolution imaging technique called motion-blur Points Accumulation for Imaging in Nanoscale Topography (mbPAINT). We observed that the number of functional adsorption sites was smaller at high ionic strength and that these sites had reduced desorption kinetic heterogeneity, and thus narrower predicted elution profiles, for the anion-exchange adsorption of α-lactalbumin on an agarose-supported, clustered-charge ligand stationary phase. Explanations for the narrowing of the functional population such as inter-protein interactions and protein or support structural changes were investigated through kinetic analysis, circular dichroism spectroscopy, and microscopy of agarose microbeads, respectively. The results suggest the reduction of heterogeneity is due to both electrostatic screening between the protein and ligand and tuning the steric availability within the agarose support. Overall, we have shown that single molecule spectroscopy can aid in understanding the influence of ionic strength on the population of functional adsorbent sites participating in the ion-exchange chromatographic separation of proteins.

Hydrophobic interaction chromatography of proteins. IV. Protein adsorption capacity and transport in preparative mode

The adsorption isotherms of four model proteins (lysozyme, α-lactalbumin, ovalbumin, and BSA) on eight commercial phenyl hydrophobic interaction chromatography media were measured. The isotherms were softer than those usually seen in ion-exchange chromatography of proteins, and the static capacities of the media were lower, ranging from 30 to 110mg/mL, depending on the ammonium sulfate concentration and the protein and adsorbent types. The protein-accessible surface area appears to be the main factor determining the binding capacity, and little correlation was seen with the protein affinities of the adsorbents. Breakthrough experiments showed that the dynamic capacities of the adsorbents at 10% breakthrough were 20–80% of the static capacities, depending on adsorbent type. Protein diffusivities in the adsorbents were estimated from batch uptake experiments using the pore diffusion and homogeneous diffusion models. Protein transport was affected by the adsorbent pore structures. Apparent diffusivities were higher at lower salt concentrations and column loadings, suggesting that adsorbed proteins may retard intraparticle protein transport. The diffusivities estimated from the batch uptake experiments were used to predict column breakthrough behavior. Analytical solutions developed for ion-exchange systems were able to provide accurate predictions for lysozyme breakthrough but not for ovalbumin. Impurities in the ovalbumin solutions used for the breakthrough experiments may have affected the ovalbumin uptake and led to the discrepancies between the predictions and the experimental results.

Electrostatic model for protein adsorption in ion-exchange chromatography and application to monoclonal antibodies, lysozyme and chymotrypsinogen A

A model for the adsorption equilibrium of proteins in ion-exchange chromatography explicitly accounting for the effect of pH and salt concentration in the limit of highly diluted systems was developed. It is based on the use of DLVO theory to estimate the electrostatic interactions between the charged surface of the ion-exchanger and the proteins. The corresponding charge distributions were evaluated as a function of pH and salt concentration using a molecular approach. The model was verified for the adsorption equilibrium of lysozyme, chymotrypsinogen A and four industrial monoclonal antibodies on two strong cation-exchangers. The adsorption equilibrium constants of these proteins were determined experimentally at various pH values and salt concentrations and the model was fitted with a good agreement using three adjustable parameters for each protein in the whole range of experimental conditions. Despite the simplifications of the model regarding the geometry of the protein–ion-exchanger system, the physical meaning of the parameters was retained.

The Isoelectric Region of Proteins: A Systematic Analysis

BackgroundBinding of proteins in ion exchange chromatography is dominated by electrostatic interactions and can be tuned by adjusting pH and ionic strength of the solvent. Therefore, the isoelectric region (IER), the pH region of almost zero charge near the pI, has been used to predict the binding properties of proteins.Principal findingsUsually the IER is small and binding and elution is carried out at pH values near to the pI. However, some proteins with an extended IER have been shown to bind and elute far away from its pI. To analyze factors that mediate the size of the IER and to identify proteins with an extended IER, two protein families consisting of more than 7000 proteins were systematically investigated. Most proteins were found to have a small IER and thus are expected to bind or elute near to their pI, while only a small fraction of less than 2% had a large IER.ConclusionsOnly four factors, the number of histidines, the pI, the number of titratable amino acids and the ratio of acidic to basic residues, are sufficient to reliably classify proteins by their IER based on their sequence only, and thus to predict their binding and elution behaviour in ion exchange chromatography.

Functionalization of epoxy‐based monoliths for ion exchange chromatography of proteins

Macroporous epoxy-based monoliths prepared by emulsion polymerization have been modified for use in ion exchange chromatography (IEC) of proteins. Strong anion exchange functionality was established by iodomethane quaternization of tertiary amine present on the monolith surface as a part of the polymer backbone. The modification pathway to cation exchange materials was via incorporation of glycidyl methacrylate (GMA) brushes which were coated using atom transfer radical polymerization (ATRP). Strong (SO(3)(-)) and weak (COO(-)) cation exchange groups were thereafter introduced onto the GMA-grafted monoliths by reactions with sodium hydrogen sulfite and iminodiacetic acid, respectively. Grafting was confirmed by XPS, gravimetric measurement, and chromatographic behavior of the modified materials toward model proteins. In incubation experiments the proteins were recovered quantitatively with no obvious signs of unfolding after contact with the stationary phase for >2 h. Chromatographic assessments on the functionalized columns as well as problems associated with flow-through modification by ATRP are discussed.

Ion Exchange Chromatography of Proteins and Clearance of Aggregates

Clearance of product related aggregates in therapeutic proteins is a major focus of purification process development. A typical purification process will have one or two chromatographic steps that remove these product related aggregates to an acceptable level. Both cation exchange and anion exchange chromatography can provide robust clearance of aggregates. The primary factors that are critical for aggregate clearance are: resin chemistry, binding and elution condition, peak collection and column load factor. This review covers how these factors can be optimized to increase the effectiveness of ion exchange chromatography in removing aggregates.

Effect of ionic capacity on dynamic adsorption behavior of protein in ion-exchange electrochromatography

Four anion-exchangers of different ion-exchange capacities (21–129 μmol/mL) were prepared by coupling diethylaminoethyl to Sepharose 6FF. The adsorbents were used to study the dynamic protein adsorption in ion-exchange electrochromatography with an oscillatory transverse electric field perpendicular to the mobile-phase flow (IEEC). The static adsorption capacity of bovine serum albumin (BSA) increased from 67 to 186 mg/mL in the ionic capacity range, but the effective pore diffusion coefficient of the protein decreased from 10.9 × 10 −12 to 1.85 × 10 −12 m 2/s with increasing the ionic capacity due to the hindrance effect of the bound protein molecules at the pore entrance. So, the dynamic binding capacity (DBC) of protein in ion-exchange chromatography decreased with increasing the ionic capacity. By applying an electric field of 30 mA, the DBC in IEEC packed with ion-exchangers of high ionic capacities (53 and 129 μmol/mL) increased significantly (over 30% and 100%, respectively). This was because the high surface charge density led to high electroosmotic flow that enhanced intraparticle mass transfer in IEEC. In comparison, the DBC in IEEC packed with ion-exchangers of low ionic capacities (21 and 35 μmol/mL) increased only slightly (ca. 10%) under the same condition. The results indicated the minor effect of electrophoretic mobility on the intraparticle mass transfer. Hence, it is beneficial to use ion-exchangers of high ionic capacity for high-capacity purification of proteins by IEEC.

Behavior of the Inadvertent pH Transient Formed by a Salt Gradient in the Ion-Exchange Chromatography of Proteins

The inadvertent pH transient produced when a stepwise change in salt concentration is used as the eluent in ion-exchange chromatography was studied theoretically using a local-equilibrium theory and experimentally using both strong-base and weak-base anion-exchange column packings. The accuracy of the local-equilibrium theory was verified by comparing it to a full numerical solution of the governing partial differential equations obtained using the method of characteristics. The predictions from the local-equilibrium theory were observed to largely agree with experimental results. Detailed comparisons of experimental results and the local-equilibrium theory permitted the observed trends for the pH transients to be interpreted in terms of the physical properties of the column packing and mobile phase. The results of this study are useful for the design of ion-exchange processes using salt gradient elution where it is desired to limit the exposure of eluted proteins to the inadvertent pH transient caused by the salt gradient.

Application of a chromatography model with linear gradient elution experimental data to the rapid scale-up in ion-exchange process chromatography of proteins

We applied the model described in our previous paper to the rapid scale-up in the ion exchange chromatography of proteins, in which linear flow velocity, column length and gradient slope were changed. We carried out linear gradient elution experiments, and obtained data for the peak salt concentration and peak width. From these data, the plate height (HETP) was calculated as a function of the mobile phase velocity and iso-resolution curve (the separation time and elution volume relationship for the same resolution) was calculated. The scale-up chromatography conditions were determined by the iso-resolution curve. The scale-up of the linear gradient elution from 5 to 100 mL and 2.5 L column sizes was performed both by the separation of β-lactoglobulin A and β-lactoglobulin B with anion-exchange chromatography and by the purification of a recombinant protein with cation-exchange chromatography. Resolution, recovery and purity were examined in order to verify the proposed method.

Computer-aided model analysis for ionic strength-dependent effective charge of protein in ion-exchange chromatography

A packed-bed chromatographic model developed in this study includes adsorption isotherms considering steric mass action (SMA) as well as non-linearity in liquid/solid phases, adsorption kinetics and mass transport. For solving the nonlinear and nonequilibrium adsorption model described by a partial differential algebraic equation (PDAE) system, a fast and accurate numerical method (i.e., conservation element/solution element (CE/SE) method), is proposed. Sensitivity and elasticity of the model parameters (e.g., steric/shape factors, adsorption heat coefficient, effective protein charge, equilibrium constant, mass transfer coefficient, axial dispersion coefficient and bed voidage) are analyzed for a BSA–salt system in a low protein concentration range. Within a low concentration range of bovine serum albumin (BSA) where linear adsorption isotherms are shown, the adsorption heat coefficient, shape and steric factors have little effect on adsorption isotherms and the retention time. However, the effective protein charge which is related to pH and ionic strength affects the retention time significantly even if the change is slight. The mass transfer coefficient (i.e., adsorption rate coefficient) has an effect on the peak height of the elution curve at the same retention time. Sensitivity of the retention time to the bed voidage is relatively large, since the bed voidage changes the fluid velocity of the mobile phase. Comparing the proposed model with experimental elution curves obtained at different salt concentrations, it is proposed that the effective protein charge could depend upon the salt concentration (or ionic strength). The reason for this dependence may be a steric hindrance of protein binding sites combined with a salt shielding effect neutralizing the surface charges of the protein.

Charge regulation in protein ion-exchange chromatography: development and experimental evaluation of a theory based on hydrogen ion Donnan equilibrium.

An extension of the stoichiometric displacement (SD) model for the ion-exchange adsorption of dilute proteins is developed which accounts for the effects of hydrogen ion Donnan equilibrium on the protein charge. The ability of the new model to fit retention data when the fluid phase pH is near the protein pI and the effects of hydrogen ion Donnan equilibrium are important is examined using four different proteins and four different column packings. The results indicate that the model is able to fit retention data using values for the protein pI and the change in protein charge with pH at the pI, i.e., (dz/dpH)pI, that are significantly closer to the values of these parameters determined by isoelectric focusing and acid-base titrametry in free solution, respectively, as compared to the values obtained by determining the characteristic binding change as a function of pH using the traditional stoichiometric displacement model. This suggests that when the fluid phase pH is near the protein pI, charge regulation is an important cause of the discrepancy between the electrical charge of a protein in free solution and the characteristic binding charge from the stoichiometric displacement model. The results also indicate that for the case where the fluid phase pH is near the protein pI, the new model accounts for the effect of charge regulation during protein ion-exchange adsorption more accurately than previous models in the literature.

Effect of chromatographic conditions on resolution in high-performance ion-exchange chromatography of proteins on macroporous anion-exchange resin

We explored chromatographic conditions to obtain high resolution in protein separations by ion-exchange chromatography (IEC) on a macroporous anion-exchange resin of 10 μm in particle diameter. We studied effects of flow-rate, gradient time (steepness of salt concentration gradient) and column length on resolution in wide ranges. It was found that very high resolutions are attainable at long gradient times with long columns. The resolution continuously became higher as the gradient time and the column length became longer except in some special cases. The dependence of resolution on gradient time was particularly great when the column was long and the gradient time for the change of 0–0.5 M NaCl was longer than 2 h. On the other hand, the effect of flow-rate on resolution was very small. Although the separations at long gradient times with long columns have not been popular in high-performance IEC and it takes several hours for one separation, such separations should be advantageous when very high resolutions are required like in proteomics research.