Purification of human IgG by negative chromatography on ω-aminohexyl-agarose

The ω-aminohexyl diamine immobilized as ligand on CNBr- and bisoxirane-activated agarose gel was evaluated for the purification of human immunoglobulin G (IgG) from serum and plasma by negative affinity chromatography. The effects of matrix activation, buffer system, and feedstream on recovery and purity of IgG were studied. A one-step purification process using Hepes buffer at pH 6.8 allowed a similar recovery (69–76%) of the loaded IgG in the nonretained fractions for both matrices, but the purity was higher for epoxy-activated gel (electrophoretically homogeneous protein with a 6.5-fold purification). The IgG and human serum albumin (HSA) adsorption equilibrium studies showed that the adsorption isotherms of IgG and HSA obeyed the Langmuir–Freundlich and Langmuir models, respectively. The binding capacity of HSA was high (210.4 mg mL^?1 of gel) and a positive cooperativity was observed for IgG binding. These results indicate that immobilizing ω-aminohexyl using bisoxirane as coupling agent is a useful strategy for rapid purification of IgG from human serum and plasma.     

Hydrophobic interaction chromatography of proteins. II. Binding capacity,recovery and mass transfer properties

Hydrophobic interaction chromatography media suited for large scale separations were compared regarding dynamic binding capacity, recovery and mass transfer properties. In all cases, pore diffusion was the rate limiting step. Reduced heights equivalent to a theoretical plate for bovine serum albumin derived from breakthrough curves at reduced velocities between 60 and 1500 ranged from 10 to 700. Pore diffusion coefficients were derived from pulse response experiments for the model proteins alpha-lactalbumin, lysozyme, beta-lactoglobulin, bovine serum albumin and immunoglobulin G. Diffusivity of lysozyme did not follow the trend of decreasing diffusivity with increasing molecular mass, as observed for the rest of the proteins. In general, mass transfer coefficients were smaller compared to ion-exchange chromatography. Dynamic binding capacities for the model protein bovine serum albumin varied within a broad range. However, sorbents based on polymethacrylate showed a lower dynamic capacity than media based on Sepharose. Some sorbents could be clustered regarding binding capacity affected by salt. These sorbents exhibited a disproportional increase of binding capacity with increasing ammonium sulfate concentration. Recovery of proteins above 75% could be observed for all sorbents. Several sorbents showed a recovery close to 100%.     

Ion exchange chromatography of antibody fragments

Effects of pH and conductivity on the ion exchange chromatographic purification of an antigen-binding antibody fragment (Fab) of pI 8.0 were investigated. Normal sulfopropyl (SP) group modified agarose particles (SP Sepharosetrade mark Fast Flow) and dextran modified particles (SP Sepharose XL) were studied. Chromatographic measurements including adsorption isotherms and dynamic breakthrough binding capacities, were complemented with laser scanning confocal microscopy. As expected static equilibrium and dynamic binding capacities were generally reduced by increasing mobile phase conductivity (1-25 mS/cm). However at pH 4 on SP Sepharose XL, Fab dynamic binding capacity increased from 130 to 160 (mg/mL media) as mobile phase conductivity changed from 1 to 5 mS/cm. Decreasing protein net charge by increasing pH from 4 to 5 at 1.3 mS/cm caused dynamic binding capacity to increase from 130 to 180 mg/mL. Confocal scanning laser microscopy studies indicate such increases were due to faster intra-particle mass transport and hence greater utilization of the media's available binding capacity. Such results are in agreement with recent studies related to ion exchange of whole antibody molecules under similar conditions.     

Optimization of a calcium-dependent Protein A-derived domain for mild antibody purification

ABSTRACT

As reported here, we developed and optimized a purification matrix based on a Protein A-derived domain, Z_Ca, displaying calcium-dependent antibody binding. It provides an alternative to the acidic elution conditions of conventional Protein A affinity chromatography for purification of sensitive antibodies and other Fc-based molecules. We describe the multimerization of Z_Ca to generate a chromatography resin with higher binding capacity. The highest order multimeric variant, Z_CaTetraCys, demonstrated a considerably high dynamic binding capacity (35 mg IgG/ml resin) while preserving the specificity for IgG. High recovery was obtained and host cell protein and DNA content in purified fractions proved to be comparable to commercial MabSelect SuRe and MabSelect PrismA. Various elution conditions for use of this domain in antibody purification were investigated. The purification data presented here revealed variations in the interaction of different subclasses of human IgG with Z_CaTetraCys. This resulted in diverse elution properties for the different IgGs, where complete elution of all captured antibody for IgG2 and IgG4 was possible at neutral pH. This optimized protein ligand and the proposed purification method offer a unique strategy for effective and mild purification of antibodies and Fc-fusion proteins that cannot be purified under conventional acidic elution conditions due to aggregation formation or loss of function.     

Characterization and optimization of a chromatographic process based on ethylenediamine-N,N,N',N'-tetra(methylphosphonic) acid-modified zirconia particles

The primary objective of work was to characterize, optimize and model a chromatographic process based on ethylenediamine-N,N,N',N'-tetra(methylphosphonic) acid (EDTPA)-modified zirconia particles. Zirconia particles were produced by spray-drying colloidal zirconia. Zirconia spheres produced were further classified, calcined and modified with EDTPA to yield a solid-phase support for use in bio-chromatography (r_PEZ). Specifically, the ability of r_PEZ to selectively bind and enrich IgG, IgA, and IgM from biological fluids was evaluated and demonstrated. To better understand the force of interaction between the IgG and the r_PEZ, the equilibrium disassociation constant (K(d)) was determined by static binding isotherms, as a function of temperature and by frontal analysis at different linear velocities. The maximum static binding capacity (Q(max)) was found to be in the range 55-65 mg IgG per ml of beads, and unaffected by temperature. The maximum dynamic binding capacity (Q(x)) was found to be in the range 20-12 mg IgG per ml of beads. The adsorption rate constant (k(a)) was determined by a split-peak approach to be between 982 and 3242 l mol(-1) s(-1) depending on the linear velocity. The standard enthalpy and entropy values were estimated for this interaction of IgG with this novel support.     

High-throughput process development: determination of dynamic binding capacity using microtiter filter plates filled with chromatography resin

Steadily increasing demand for more efficient and more affordable biomolecule-based therapies put a significant burden on biopharma companies to reduce the cost of R&D activities associated with introduction of a new drug to the market. Reducing the time required to develop a purification process would be one option to address the high cost issue. The reduction in time can be accomplished if more efficient methods/tools are available for process development work, including high-throughput techniques. This paper addresses the transitions from traditional column-based process development to a modern high-throughput approach utilizing microtiter filter plates filled with a well-defined volume of chromatography resin. The approach is based on implementing the well-known batch uptake principle into microtiter plate geometry. Two variants of the proposed approach, allowing for either qualitative or quantitative estimation of dynamic binding capacity as a function of residence time, are described. Examples of quantitative estimation of dynamic binding capacities of human polyclonal IgG on MabSelect SuRe and of qualitative estimation of dynamic binding capacity of amyloglucosidase on a prototype of Capto DEAE weak ion exchanger are given. The proposed high-throughput method for determination of dynamic binding capacity significantly reduces time and sample consumption as compared to a traditional method utilizing packed chromatography columns without sacrificing the accuracy of data obtained.     

Biosorption of Cr (VI) from aqueous solution by Rhizopus nigricans

The study was aimed to quantify the Cr sorption ability of powdered biomass of Rhizopus nigricans at the best operating conditions. The influence of solution pH, agitation, Cr (VI) concentration, biomass dosage, contact time, biomass particle size and temperature were studied. The optimum pH for biosorption of Cr (VI) was found to be 2.0. Higher adsorption percentage was noted at lower initial concentrations of Cr ions, while the adsorption capacity of the biomass increased with increasing concentration of ions. Optimum biomass dosage was observed as 0.5% (w/v). More than 75% of the ions were removed within 30 min of contact and maximum removal was obtained after 8 h. Biomass particles of smaller size (90 microm) gave maximum adsorption (99.2%) at 100 mg/l concentration. The adsorption capacity increased with increase in temperature and agitation speed and the optimum were determined as 45 degrees C at 120 rpm. Freundlich and Langmuir isotherms were used to evaluate the data and the regression constants were derived. The adsorption rate constant values (Kad) were calculated for different initial concentration of Cr ions and the sorption was found to be higher at lower concentration (100 mg/l) of metal ion.     

Effects of temperature, flow rate and composition of binding buffer on adsorption of mouse monoclonal IgG1 antibodies to protein A Sepharose 4 Fast Flow.

The binding capacity of protein A Sepharose 4 Fast Flow for mouse IgG1 monoclonal antibodies (mabs) appears to be highly dependent on the buffer composition with respect to both concentration and ion type. Depending on the particular mab dynamic binding capacities up to 20 mg mab per ml gel could be obtained, when these mabs were isolated from supernatants of protein free hollow fibre cell culture systems. Variation of linear flow rate from 10 up to 300 cm/h and temperature (4 degrees C versus 25 degrees C) had a slight effect on the dynamic binding capacity, when a high ionic strength buffer was used during adsorption. Applying optimum binding conditions, final IgG fractions with a purity of more than 95% monomeric IgG were obtained. However, as side effect of the use of binding buffers with high ionic strength, the binding of acid proteases was also promoted.     

Maximizing productivity of chromatography steps for purification of monoclonal antibodies

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.     

Pilot scale recovery of monoclonal antibodies by expanded bed ion exchange adsorption

The aim of the investigations was to estimate the scale up properties of an efficient chromatographic first capture step for the recovery of murine IgG₁ from undiluted and unclarified hybridoma cell culture broth using an ion exchange matrix in expanded bed mode. The tested new sulfopropyl-based ion exchange matrix (Streamline^TM SP XL, Amersham Pharmacia Biotech) stands out due to its enhanced capacity compared to its precursor (Streamline^TM SP). Defining the working pH in preliminary electrophoretic analyses (titration curve, SDS-PAGE) and small-scaled chromatographic binding studies showed, that the optimal value for the IgG purification was pH 4.6, where a co-chromatography of the medium supplement albumin (500 mg l^-1, pI = 4.8) could not be avoided. Further scouting experiments dealt with the dynamic capacity of the matrix, which was evaluated by frontal adsorption analysis. In packed bed mode no break-through of the target protein was achieved even after 6.5 mg IgG per ml matrix were applied. These results could not be reproduced in expanded bed mode with cell-free supernatant, where the dynamic capacity was found to be only 1.5 mg IgG/ml SP XL. Processing cell-containing broth resulted in an additional decrease of the value down to 0.5 mg ml^-1, presumably caused by the remarkable biomass adsorption to the matrix. The search for the reasons led to the examination of the hydrodynamic conditions. Buffer experiments with a tracer substance (acetone) pointed out, that the flow in expanded bed was significantly more influenced by back-mixing effects and channel formations than in packed bed. These effects could be compensated with an enhanced viscosity of the liquid phase, which was achieved by the addition of glucose. As a result of the improved hydrodynamic conditions in the expanded bed, the dynamic capacity could be increased from 0.5 to more than 4.5 mg IgG/ml matrix for the processing of cell culture broth with 400 mM glucose. Finally, the scale up from a Streamline^TM 25 to a Streamline^TM 200 column was performed under conditions, which proved to be optimal: 100 L of unclarified hybridoma broth were concentrated with a binding rate of 95% in less than 3.5 hours. Loading the column no break-through of the target protein was achieved. However, the eluate still contained debris and cells, which points out the major disadvantage of the method: the biomass attachment to the matrix.     

Structural refinement of protein A mimetic peptide

A novel dendrimeric peptide ligand dubbed D-PAM-Φ was designed to achieve a high capacity for human IgG through the decoration of the D-PAM scaffold. The design criteria based on the introduction of small hydrophobic groups on the D-PAM structure were supported by the recently published solid-state structure of D-PAM complexed to the Fc fragment of a recombinant human IgG1 and by molecular dynamic simulations that provided information on the mode of binding of phenylacetyl-D-PAM (D-PAM-Φ). D-PAM-Φ was immobilised on an activated solid support and compared with the parent D-PAM affinity matrix. The newly obtained affinity sorbent was evaluated for its capacity to selectively capture polyclonal human IgG; the binding capacity was approximately 10 mg/ml, an almost 10-fold enhancement with respect to the D-PAM-functionalised matrices without the specificity of binding being reduced. The new ligand was also effective in the capturing of recombinant humanised IgG1 from a clarified cell culture supernatant. Under a typical laboratory-scale affinity chromatography assembly and preliminarily optimised binding conditions, the affinity purification of humanised IgG1 from culture supernatants rendered the desired product, with purity higher than 90%. The results suggest that the application of the computational approach on the structure of the D-PAM-Fc complex may be very valuable in the development of novel lead molecules for the downstream processing of human or humanised antibodies used in therapy.     

Continuous cephalosporin C purification: dynamic modelling and parameter validation

A mathematical kinetic model for the adsorption and desorption of cephalosporin C on Amberlite XAD-2 resin is proposed. The model can represent Langmuir, Freundlich or linear isotherms at equilibrium. The intrinsic kinetic parameters and adsorption isotherms as well as physical parameters such as the effective diffusivity and the external mass transfer coefficient were obtained at different temperatures and ethanol concentrations. An unfavourable cephalosporin C adsorption occurred when ethanol was present in the solution. It has been shown that at 25 degrees C the ethanol, at concentrations from 1.5% to 2.5%, decreases the cephalosporin C adsorption. However, this behaviour was not observed at 10 degrees C. The kinetic model fitted the experimental data well under different conditions. The model was validated in a continuous process of cephalosporin C purification using the same resin. The model with the validated parameters is able to predict the behaviour of the reactor system. The continuous process is composed of two stirred tank reactors with adsorber recycle. The adsorption occurs in the first stage, and elution of the product takes place in the second stage with ethanol as eluent. The dynamic behaviour of the process was described using the following parameters: hydraulic residence time for the first (theta(h1)) and second stage (theta(h2)), solid residence time (theta(s)), initial concentration of CPC (C(0)), inlet ethanol concentration (C(ET0)) and kinetics parameters.     

Study of binding between protein A and immunoglobulin G using a surface tension probe

Molecular interactions and binding are one of the most important and fundamental properties in the study of biochemical and biomedical systems. The understanding of such interactions and binding among biomolecules forms the basis for the design and processing of many biotechnological applications, such as bioseparation and immunoadsorption. In this study, we present a novel method to probe molecular interactions and binding based on surface tension measurement. This method complements conventional techniques, which are largely based on optical, spectroscopic, fluorescence polarization, chromatographic or atomic force microscopy measurements, by being definite in determining molecular binding ratio and flexible in sample preparation. Both dynamic and equilibrium (or quasi-equilibrium) information on molecular binding can be obtained through dynamic and equilibrium surface tension measurements. For an important pair of biological ligand and ligate, Protein A and immunoglobulin G (IgG), the existence of molecular interactions and the binding ratio of 1:2 have been determined unequivocally with the proposed surface tension method. These results are confirmed/supported by a mass balance calculation and spectrophotometry experiment. In addition, adsorption isotherms for Protein A and IgG separately at the air/water interface have been established with the dynamic surface tension measurements. The results show that the Langmuir isotherm equation can describe the adsorption data satisfactorily for both Protein A and IgG solutions.     

Evaluation of immobilized metal membrane affinity chromatography for purification of an immunoglobulin G1 monoclonal antibody

The large scale production of monoclonal antibodies (McAbs) has gaining increased relevance with the development of the hybridoma cell culture in bioreactors creating a need for specific efficient bioseparation techniques. Conventional fixed bead affinity adsorption commonly applied for McAbs purification has the drawback of low flow rates and colmatage. We developed and evaluated a immobilized metal affinity chromatographies (IMAC) affinity membrane for the purification of anti-TNP IgG(1) mouse McAbs. We immobilized metal ions on a poly(ethylene vinyl alcohol) hollow fiber membrane (Me(2+)-IDA-PEVA) and applied it for the purification of this McAbs from cell culture supernatant after precipitation with 50% saturation of ammonium sulphate. The purity of IgG(1) in the eluate fractions was high when eluted from Zn(2+) complex. The anti-TNP antibody could be eluted under conditions causing no loss of antigen binding capacity. The purification procedure can be considered as an alternative to the biospecific adsorbent commonly applied for mouse IgG(1) purification, the protein G-Sepharose.     

Preparation and characterization of PEGyated Concanavalin A for affinity chromatography with improved stability

In order to improve its stability, immobilized Concanavalin A (Con A) on Toyopearl adsorbents was conjugated with monomethoxy poly(ethylene glycol) succinimidyl propionate (mPEG-SPA) with different molecular weight. A colorimetric method using ninhydrin is proposed to determine the degree of PEGylation; this method has proved to be easy applicable and reproducible. The PEGylation reaction was studied in detail to elucidate how parameters such as molar ratio of mPEG-SPA to Con A and molecular weight of mPEG-SPA affect the degree of PEGylation. The adsorption isotherms of glucose oxidase (GOD) onto native and PEGylated Con A adsorbents showed that the modification did not alter substantially the specificity of the carbohydrate binding ability of Con A. However, the binding capacity for GOD was slightly reduced probably due to the steric hindrance caused by mPEG chains. Adsorption kinetic studies revealed a lower adsorption rate after PEGylation which was attributed to the steric effect. The dynamic adsorption capacity for modified Con A depended very much on the degree of PEGylation and the molecular weight of mPEG derivatives. The adsorption capacity could be highly preserved for Toyopearl Con A modified by mPEG2k (90% of the original adsorption capacity) even with a degree of PEGylation up to 20% (the ratio of primary amino groups of PEGylated immobilized Con A to that of native immobilized Con A). Studies show that the binding capacity of PEGylated Con A was highly preserved under mild process conditions. PEGylated Con A also exhibited obviously higher stability against more stressful conditions such as the exposure to organic solvents and high temperatures. Conjugation of Con A with mPEG2k provided better adsorption performance thus has greater potential for application in affinity separation processes compared with mPEG5k. The fact that PEGylation stabilizes the properties of Con A may greatly expand the range of applications of unstable proteins to bioprocessing (e.g. biocatalysis and downstream separation) as well as other protein applications (e.g. medication, industrial use, etc.).     

Protein A immunoaffinity hollow fiber membranes for immunoglobulin G purification: experimental characterization

Immunoaffinity adsorption is increasingly used for protein purification and medical applications. Synthetic membranes have advantages as support matrices in comparison to conventional bead supports because they are not compressible and they eliminate internal diffusion limitations. The goal of this study was to explore in detail the performance of microporous hollow fibers composed of modified polysulfone to which protein A was immobilized for adsorption of human IgG. The internal matrix was characterized by scanning electron microscopy. The binding equilibrium constant was measured using both static and dynamic methods. Break-through curves up to ligand saturation were measured and used to study the effects of IgG concentration, presence of contaminant albumin, flow direction, flow mode, and especially filtrate flow rate and maximum IgG binding capacity. The highest binding capacities studied were comparable with that attainable with bead matrices. All of the breakthrough curves could be represented on a single figure when plotted versus the dimensionless relative throughput (the mass of IgG loaded on the membrane divided by the mass that would be bound when the entire fiber is in equilibrium with the feed concentration), and the effect of operating variables on the position and shape of the individual breakthrough curves could be understood in terms of a dimensional performance parameter (the product of membrane volume and maximum binding capacity divided by the filtrate flow rate). The best breakthrough curves were obtained with the highest values of the performance parameter. Based on the results, membranes as solid supports for immunoadsorption can be a useful alternative to the use of traditional columns for protein separations. (c) 1995 John Wiley & Sons, Inc.     

The role of polymer nanolayer architecture on the separation performance of anion-exchange membrane adsorbers: I. Protein separations

This contribution describes the preparation of strong anion-exchange membranes with higher protein binding capacities than the best commercial resins. Quaternary amine (Q-type) anion-exchange membranes were prepared by grafting polyelectrolyte nanolayers from the surfaces of macroporous membrane supports. A focus of this study was to better understand the role of polymer nanolayer architecture on protein binding. Membranes were prepared with different polymer chain graft densities using a newly developed surface-initiated polymerization protocol designed to provide uniform and variable chain spacing. Bovine serum albumin and immunoglobulin G were used to measure binding capacities of proteins with different size. Dynamic binding capacities of IgG were measured to evaluate the impact of polymer chain density on the accessibility of large size protein to binding sites within the polyelectrolyte nanolayer under flow conditions. The dynamic binding capacity of IgG increased nearly linearly with increasing polymer chain density, which suggests that the spacing between polymer chains is sufficient for IgG to access binding sites all along the grafted polymer chains. Furthermore, the high dynamic binding capacity of IgG (>130 mg/mL) was independent of linear flow velocity, which suggests that the mass transfer of IgG molecules to the binding sites occurs primarily via convection. Overall, this research provides clear evidence that the dynamic binding capacities of large biologics can be higher for well-designed macroporous membrane adsorbers than commercial membrane or resin ion-exchange products. Specifically, using controlled polymerization leads to anion-exchange membrane adsorbers with high binding capacities that are independent of flow rate, enabling high throughput. Results of this work should help to accelerate the broader implementation of membrane adsorbers in bioprocess purification steps.     

吸附层析分离麻黄生物碱的过程优化

研究了用吸附层析取代现有的二甲苯萃取麻黄生物碱的工艺,重点考察了洗脱剂和操作条件对产品纯度和回收率的影响,发现在树脂吸附后的洗脱中,0．08M草酸的洗脱率最高,达99．3％,纯化倍数大于20;在操作条件中,进料量、pH和料液在层析柱中的停留时间影响最大：进料量增大导致纯度和收率的下降,树脂的动态吸附容量为27．5mg／mL树脂;停留时间在20rain时纯度较高,而洗脱率随停留时间减少却略有下降;pH=10时吸附性能较好。     

Purification of cell culture‐derived modified vaccinia ankara virus by pseudo‐affinity membrane adsorbers and hydrophobic interaction chromatography

A purification scheme for cell culture‐derived smallpox vaccines based on an orthogonal downstream process of pseudo‐affinity membrane adsorbers (MA) and hydrophobic interaction chromatography (HIC) was investigated. The applied pseudo‐affinity chromatography, based on reinforced sulfated cellulose and heparin‐MA, was optimized in terms of dynamic binding capacities, virus yield and process productivity. HIC was introduced as a subsequent method to further reduce the DNA content. Therefore, two screens were undertaken. First, several HIC ligands were screened for different adsorption behavior between virus particles and DNA. Second, elution from pseudo‐affinity MA and adsorption of virus particles onto the hydrophobic interaction matrix was explored by a series of buffers using different ammonium sulfate concentrations. Eventually, variations between different cultivation batches and buffer conditions were investigated.The most promising combination, a sulfated cellulose membrane adsorber with subsequent phenyl HIC resulted in overall virus particle recoveries ranging from 76% to 55% depending on the product batch and applied conditions. On average, 61% of the recovered virus particles were infective within all tested purification schemes and conditions. Final DNA content varied from 0.01% to 2.5% of the starting material and the level of contaminating protein was below 0.1%. Biotechnol. Bioeng. 2010;107: 312–320. © 2010 Wiley Periodicals, Inc.     

Mercaptoheterocyclic ligands grafted on a poly(ethylene vinyl alcohol) membrane for the purification of immunoglobulin G in a salt independent thiophilic chromatography

In this study, we attempted a limited combinatorial approach for designing affinity ligands based on mercaptoheterocyclic components. The template, divinyl sulfone structure (DVS), which was grafted on poly(ethylene vinyl alcohol) (PEVA) hollow fiber membrane, has served for the tethering of different heterocyclic compounds as pyridine, imidazole, purine and pyrimidine rings. Their ability to adsorb specifically IgG in a salt independent manner out of pure IgG solution, mixture of IgG/albumin and human plasma was demonstrated. Mercapto methyl imidazole (MMI) has shown the best adsorption of IgG in terms of binding capacity. No subclass discrimination was observed on all tested ligands except for mercapto methyl pyrimidine where the major IgG subclass adsorbed was IgG3. MMI gave an IgG binding capacity of 100 microg/cm2 of hollow fiber membrane surface area.