Expanded bed protein A affinity chromatography of a recombinant humanized monoclonal antibody: process development, operation, and comparison with a packed bed method.

We show that expanded bed protein A affinity chromatography using Streamline rProtein A media is an efficient method for purifying a recombinant humanized monoclonal antibody from unclarified Chinese hamster ovary cell culture fluid and that it provides purification performance comparable to using a packed bed. We determined that the dynamic capacity of the expanded bed media is related to flow rate (measured in column volumes per hour) by a power function, which allows a high capacity at a low flow rate. At 250 cm h-1 with a 25 cm bed height (10 column volumes h-1), the dynamic capacity is 30 g l-1. The yield and purity (measured by the amount of host cell proteins, DNA, SDS-PAGE, and turbidity) of the antibody purified by expanded bed is comparable to the yield and purity obtained on a standard packed bed method using Prosep A media.     

Performance comparison of protein A affinity resins for the purification of monoclonal antibodies

During the selection of protein A affinity resin for the purification of monoclonal antibodies, dynamic binding capacity (Q(dyn10%)), volumetric production rate (Pr(vol)) and 'process robustness' are essential parameters to be evaluated. In this article, empirical mathematical models describe these parameters as a function of antibody concentration in load (C0), load flow rate (u(load)) and bed height (L). These models allow us to select optimal process conditions for each of the evaluated protein A affinity resins. C0, u(load) and L largely affect dynamic binding capacity (Q(dyn10%)) and volumetric production rate (Pr(vol)). Maximum Q(dyn10%) is generally obtained at high C0 and at low u(load). Maximum Pr(vol) is obtained at high C0 and at lowest L, run at high u(load). All evaluated resins have a relatively high robustness against variations in C0. |DeltaQ(dyn10%)/deltaC0| ranges from 0.0 to 7.8. It is clear that Q(dyn10%), Pr(vol) and 'process robustness' cannot be maximized all at the same time. Furthermore, some other aspects like IgG recovery, protein A leaching, easiness to pack, easiness to clean, number of re-uses and cost of production might be important to be taken into the equation. Certain evaluation parameters may be more important than others, depending on the specific situation. Therefore, a case-by-case evaluation is recommended.     

Purification of antibody against Ara h 2 by a homemade immunoaffinity chromatography column

Antibodies are used extensively in numerous applications both in vivo and in vitro. To purify anti-Ara h 2 polyclonal antibody, a homemade immunoaffinity chromatography (IAC) column method was established. The properties of homemade column were compared with those of the mAb affinity protein G (MPG) agarose high flow, a commercially available column successfully used in capturing polyclonal antibodies. During antibody purification from rabbits’ antiserum against Ara h 2, the column capacity, recovery, and purification factor were characterized for IAC and MPG. The homemade IAC could separate the corresponding antibody with higher specificity and lower cost but with lower recovery and column capacity than those of MPG. Thus, the homemade IAC is a specific, inexpensive, and suitable method that can be used for various laboratory purifications.     

Preparative high speed gel permeation chromatography of proteins on Toyopearl HW55F

A method is described for the rapid separation of protein mixtures by high speed gel permeation chromatography using Toyopearl HW55F, a new semi-rigid hydrophilic polymer. Good resolution of protein mixtures according to molecular size can be achieved on this material with high flow rates and low column pressures. Molecular weight estimations in the range between 10⁴ and 10⁶ daltons can be performed within minutes. Large-scale enzyme purification (up to 1.6 gm of starting material with a 3.2 × 105 cm column) was achieved with 86–110% recovery of enzymatic activity. Data are presented on the optimum column length, flow rate, loading capacity and eluant ionic strength.     

Membrane adsorbers as purification tools for monoclonal antibody purification

Downstream purification processes for monoclonal antibody production typically involve multiple steps; some of them are conventionally performed by bead-based column chromatography. Affinity chromatography with Protein A is the most selective method for protein purification and is conventionally used for the initial capturing step to facilitate rapid volume reduction as well as separation of the antibody. However, conventional affinity chromatography has some limitations that are inherent with the method, it exhibits slow intraparticle diffusion and high pressure drop within the column. Membrane-based separation processes can be used in order to overcome these mass transfer limitations. The ligand is immobilized in the membrane pores and the convective flow brings the solute molecules very close to the ligand and hence minimizes the diffusional limitations associated with the beads. Nonetheless, the adoption of this technology has been slow because membrane chromatography has been limited by a lower binding capacity than that of conventional columns, even though the high flux advantages provided by membrane adsorbers would lead to higher productivity. This review considers the use of membrane adsorbers as an alternative technology for capture and polishing steps for the purification of monoclonal antibodies. Promising industrial applications as well as new trends in research will be addressed.     

Investigation of immunoadsorbent efficiency and capacity for the isolation of tRNAs containing N6-(delta 2-isopentenyl)adenosine derivatives

Antibodies directed to modified nucleosides recognize the nucleoside (antigen) when it is present in an intact tRNA molecule. The general application of anti-nucleoside immunoadsorbent chromatography, however, has been greatly impeded by the apparent inefficiency and low capacity of conventional immunoadsorbents for transfer RNA. Antibodies specific for isopentenyladenosine (i6A) were employed to investigate the efficacy of various immunoadsorbents with respect to immobilization of antibody protein and with respect to their ability to bind i6A-containing tRNAs. Biologically active anti-i6A was recovered in high yield (80-88%) by affinity chromatography on i6A-adipate-Sepharose 4B or i6A-butane diglycidyl ether-Sepharose 4B using either 15% pyridine in phosphate-buffered saline or 0.2 M acetic acid as eluents. The binding capacity of various anti-i6A antibody immunoadsorbents was evaluated. While both anti-i6A antibody-protein A-agarose-iminothiolane (ITL) and anti-i6A antibody-protein A-agarose-dimethyl suberimidate showed a high capacity for i6A-tRNA, the latter column is much less efficient with respect to antibody immobilization. Under optimal conditions, the ITL immunoadsorbent binds 5-6 nmol of i6A/mg of antibody protein. With respect to bulk tRNA, 1 mg of antibody protein (ITL immunoadsorbent) binds all of the i6A-tRNA in a 1-mg sample.     

Performance of a new protein A affinity membrane for the primary recovery of antibodies

Recovery of antibodies with Protein A affinity chromatography columns has become the standard for the biotechnology industry. Membrane affinity chromatography has not yet experienced extensive application due to the lower capacity of membrane supports compared to chromatographic beads. In this work, new affinity membranes endowed with an interesting binding capacity for human IgG are studied in view of their application in the capturing step of a monoclonal antibody production process. The membranes have been extensively tested with pure IgG solutions and with a cell culture supernatant containing IgG1. The effects of feed flow rate and IgG concentration on the separation performances have been studied in detail, considering in particular binding capacity, selectivity and recovery. These new high capacity affinity membranes appear good candidates to avoid the throughput limitations and other well-known drawbacks of traditional bead-based chromatographic columns.     

A simple method for midkine purification by affinity chromatography with a heavy chain variable domain (VH) fragment of antibody

A DNA fragment for a heavy chain variable domain (VH) was prepared from a hybridoma that produces a monoclonal antibody against human midkine (MK). The antibody fragment was produced in Escherichia coli and its affinity for chemically synthesized full length MK or recombinant midkine c-terminus (MKc-half) protein was confirmed by ELISA. An Escherichia coli cell lysate expressing MKc-half was applied to a VH fragment-coupled Sepharose 4B column and eluted with a buffer containing 0.5 M NaCl. SDS-PAGE analysis revealed a high degree of purity of the MKc-half protein in the eluent, showing the utility of a recombinant VH fragment in purification of proteins by affinity chromatography.     

Pore network modelling of affinity chromatography: determination of the dynamic profiles of the pore diffusivity of beta-galactosidase and its effect on column performance as the loading of beta-galactosidase onto anti-beta-galactosidase varies with time.

A three-dimensional pore network model for diffusion in porous adsorbent particles was employed in a dynamic adsorption model that simulates the adsorption of a solute in porous particles packed in a chromatographic column. The solution of the combined model yielded the dynamic profiles of the pore diffusion coefficient of beta-galactosidase along the radius of porous adsorbent particles and along the length of the column as the loading of beta-galactosidase onto anti-beta-galactosidase immobilized on the surface of the pores of the particles occurred, and, the dynamic adsorptive capacity of the chromatographic column as a function of the design and operational parameters of the chromatographic system. It was found that for a given column length the dynamic profiles of the pore diffusion coefficient were influenced by (a) the superficial fluid velocity in the column, (b) the diameter of the adsorbent particles, and (c) the pore connectivity of the porous structure of the adsorbent particles. The effect of the magnitude of the pore connectivity on the dynamic profiles of the pore diffusion coefficient of beta-galactosidase increased as the diameter of the adsorbent particles and the superficial fluid velocity in the column increased. The dynamic adsorptive capacity of the column increased as (i) the particle diameter and the superficial fluid velocity in the column decreased, and (ii) the column length and the pore connectivity increased. In preparative affinity chromatography, it is desirable to obtain high throughputs within acceptable pressure gradients, and this may require the employment of larger diameter adsorbent particles. In such a case, longer column lengths satisfying acceptable pressure gradients with adsorbent particles having higher pore connectivity values could provide high dynamic adsorptive capacities. An alternative chromatographic system could be comprised of a long column packed with large particles which have fractal pores (fractal particles) that have high pore connectivities and which allow high intraparticle diffusional and convective flow mass transfer rates providing high throughputs and high dynamic adsorptive capacities. If large scale monoliths could be made to be reproducible and operationally stable, they could also offer an alternative mode of operation that could provide high throughputs and high dynamic adsorptive capacities.     

Affinity ligand selection from a library of small molecules: assay development, screening, and application

A facile and cost-effective process for screening synthetic libraries for an affinity ligand is described. A high throughput 96-well plate filtration method was designed to screen both discrete compounds and mixtures of compounds attached to a solid support. Human serum albumin (HSA) was used as a target protein to demonstrate the proof of concept. Detection and quantitation by fluorescence was accomplished with the use of fluorescamine to conjugate the protein in the filtrate. It is found that mixtures demonstrating low average binding reflect an overall lower hit rate of the components, whereas deconvolution of mixtures with high protein binding consistently provides a high hit rate. This differs from many of the previous experiences screening solid-phase mixtures in which high false positive rates are noted to occur. A total of 100K compounds were tested: 25K as discrete samples and 75K as mixtures. An overall hit rate of 8% was observed. Secondary screening of compounds measured specificity, recovery, and dynamic binding capacity. The effectiveness of the method is illustrated using an affinity column made with a representative lead compound. A similar purity was achieved in a single-step purification of HSA from serum as compared to that obtained by two steps of ion-exchange chromatography. The process for primary screening of a large number of compounds is simple, inexpensive, and applicable to any soluble target protein of known or unknown function from crude mixtures and may have additional utility as a generic chemical affinity tool for the functional characterization of novel proteins emerging from proteomics work.     

Effect of matrices on affinity purification of protein C

One of the critical problems in scale-up of affinity chromatography is the mechanical strength of the support matrix against pressure. Because the costs of both the gel matrix and the ligand for the affinity chromatography are very high, the reusability of gel matrices is directly related to the total production cost. In certain cases, where the source material is viscous (e.g., blood plasma), irreversible deformation of gel matrices can readily occur, necessitating severe constraints in the flow rate. Consequently, productivity is low.We have characterized the system parameters and investigated the performance of various matrices that are commercially available. The experimental system used for this study was the immunoaffinity purification of protein C (an anticoagulant protein) from human blood plasma. The support matrices studied were cross-linked agarose, polymethyl acrylic, cellulose, and polyvinyl alcohol polymers. The major system parameters studied were pressure tolerance, coupling efficiency, adsorption efficiency, and batch adsorption/desorption kinetics of protein C to/from the monoclonal antibody (MAb)-Matrix complex. In addition, the apparent equilibrium constant and bandwidth of the product concentration profile in the eluate were characterized by performing pulse tests.A methodology was developed for evaluating the immunoaffinity colum performance for the separation of protein C. By utilizing the experimentally measured parameters, the flow rate limitation for each purification step was computed. Then, the purification performance of the matrices were evaluated in terms of productivity per unit time. Among the matrices tested, cellulose was superior in overall performance for the immunoaffinity purification of protein C using a 10 cm x 10 cm column.     

Short columns with molecularly imprinted monolithic stationary phases for rapid separation of diastereomers and enantiomers

Three molecularly imprinted monolithic columns with different length but almost identical column volume had been prepared. It was observed that the separation factors of diastereomers and enantiomers were almost unaffected by column length. However, the short column with dimension of 38 mm x 8 mm i.d. showed much lower resistance to flow rate so that it could be operated at much higher flow rates. By combining stepwise gradient elution with elevated flow rate, the diastereomers of cinchonine and cinchonidine and the enantiomers of Cbz-DL-Trp and Fmoc-DL-Trp were successfully separated within 3 min on the short column with dimension of 38 mm x 8 mm i.d. Based on the above results, a cinchonine imprinted monolithic disk with dimension of 10mm x 16 mm i.d. was further developed. The SEM image and the pore size distribution profile showed that large flow-through pores are present on the prepared monolith, which allowed mobile phase to flow through the disk with very low resistance. Chromatographic performances on the monolithic disk were almost unchanged compared with the long columns. A rapid separation of cinchonine and cinchonidine was achieved in 2.5 min at the flow rate of 9.0 ml/min. Furthermore, it was observed that there was almost no effect of the flow rate on the dynamic binding capacity at high flow rates. In addition, the effect of the loading concentration of analytes on the dynamic binding capacity, namely adsorption isotherm, was also investigated. A non-linear adsorption isotherm of cinchonine was observed on the molecularly imprinted monolith with cinchonine as template, which might be a main reason to result in the peak tailing of template molecule.     

High speed immuno-affinity chromatography on supports with gigapores and porous glass

Immuno-affinity chromatography exploiting the Ca²⁺ dependent interaction of the anti-Flag antibody and Flag-tagged proteins has been investigated. The antibody has been immobilized on porous glass beads (Prosep) containing gigapores and on a monolith, the polymethacrylate based Convective Interactive Media (CIM) column at a ligand density of 2 mg/g and 10 mg/ml respectively. The performance of the columns was assessed by applying clarified yeast culture supernatant containing overexpressed Flag-human serum albumin. Dynamic binding capacity and purity was checked at various flow rates ranging from 100 cm/h to 800 cm/h. 95% purity could be obtained. Anti Flag-CIM columns showed a higher unspecific adsorption, requiring a longer wash cycle to obtain the same purity compared to the Prosep column. Anti Flag-CIM columns showed a flow independent performance, which is explained by its monolithic structure. A decreasing dynamic binding capacity with flow was observed with anti-Flag-Prosep columns. Both columns are suited to purify milligrams of protein out of a yeast culture supernatant within a few minutes. We considered them as promising candidates for high throughput screening, where fast purification is a necessity.     

Assessment of the use of cyanogen bromide-activated Sepharose in analytical and preparative immunoadsorption

Procedures are described for the analytical and preparative purification of antigens based on their specific interaction with their complementary antibody immunoadsorbents prepared from cyanogen bromide-derivatized macroporous agarose matrices. In principle, the antigen to be purified in the affinity chromatography/immunoadsorption process should bind specifically and reversibly to the attached antibody, while other proteins pass through unretarded. In the case of tight binding, elution of the antigen is achieved by the use of eluting solutions of very high or very low pH, or with the use of chaotropic solutions such as 3 m KSCN. The performance of immunoadsorbents prepared from Sepharose 4B have been studied with the aim of improving the efficient utilization of immunoadsorption techniques. As a model, human serum was applied serially to several columns of Sepharose 4B sheep anti-human IgG which were then subjected to a number of successive adsorption/desorption cycles. Loading the columns with increasing amounts of serum showed that the performance was best when the antigen load was approximately threefold the ideal binding capacity. By limiting the amount of immobilized protein and carefully controlling the antigen load, significant improvements in yield and purity have been achieved. Antigen loads of threefold the potential binding capacity of the immunoadsorbent column results in the optimal yield of antigen with high purity and significant concomitant reduction in non-specific interference from other serum proteins. The non-specific adsorption which is an inherent problem and which leads to considerable inactivation of the covalently coupled antibody is highlighted. Although the popularity of such matrices is probably unsurpassed, it is clear that use has been made of them very frequently without an examination of quantitative aspects or side reactions.     

Decision-support software for the industrial-scale chromatographic purification of antibodies

The high therapeutic and financial value offered by polyclonal antibodies and their fragments has prompted extensive commercialization for the treatment of a wide range of acute clinical indications. Large-scale manufacture typically includes antibody-specific chromatography steps that employ custom-made affinity matrices to separate product-specific IgG from the remainder of the contaminating antibody repertoire. The high cost of such matrices necessitates efficient process design in order to maximize their economic potential. Techniques that identify the most suitable operating conditions for achieving desired levels of manufacturing performance are therefore of significant utility. This paper describes the development of a computer model that incorporates the effects of capacity changes over consecutive chromatographic operational cycles in order to identify combinations of protein load and loading flowrate that satisfy preset constraints of product yield and throughput. The method is illustrated by application to the manufacture of DigiFab, an FDA-approved polyclonal antibody fragment purified from ovine serum, which is used to treat digoxin toxicity (Protherics U.K. Limited). The model was populated with data obtained from scale-down experimental studies of the commercial-scale affinity purification step, which correlated measured changes in matrix capacity with the total protein load and number of resin re-uses. To enable a tradeoff between yield and throughput, output values were integrated together into a single metric by multi-attribute decision-making techniques to identify the most suitable flowrate and feed concentration required for achieving target levels of DigiFab yield and throughput. Results indicated that reducing the flowrate by 70% (from the current level) and using a protein load at the midpoint of the range currently employed at production scale (approximately 200-500 g/L) would provide the most satisfactory tradeoff between yield and throughput.     

Purification process development of a recombinant monoclonal antibody expressed in glycoengineered Pichia pastoris

A robust and scalable purification process was developed to quickly generate antibody of high purity and sufficient quantity from glycoengineered Pichia pastoris fermentation. Protein A affinity chromatography was used to capture the antibody from fermentation supernatant. A pH gradient elution was applied to the Protein A column to prevent antibody precipitation at low pH. Antibody from Protein A chromatography contained some product related impurities, which were the misassembling of cleaved heavy chain, heavy chain and light chain. It also had some process related impurities, including Protein A residues, endotoxin, host cell DNA and proteins. Cation exchange chromatography with optimal NaCl gradient at pH 4.5-6.0 efficiently removed these product and process related impurities. The antibody from glycoengineered P. pastoris was comparable to its commercial counterpart in heterotetramer folding, physical stability and binding affinity.     

Purification of the c-fos enhancer-binding protein.

We have purified the c-fos enhancer-binding protein from HeLa cell nuclear extracts. The key purification steps involved chromatography on a nonspecific DNA affinity column, from which binding activity and other protein were eluted at low salt concentrations, followed by chromatography on a specific oligonucleotide affinity column, from which the enhancer binding activity was specifically eluted at high salt concentrations. The purified protein had a strong affinity for the c-fos enhancer dyad symmetry sequence, with an equilibrium dissociation constant of 3.3 x 10(-11) M. This affinity was at least 50,000-fold stronger than that found for nonspecific DNA sequences.     

Comparison of batch and continuous multi‐column protein A capture processes by optimal design

Multi‐column capture processes show several advantages compared to batch capture. It is however not evident how many columns one should use exactly. To investigate this issue, twin‐column CaptureSMB, 3‐ and 4‐column periodic counter‐current chromatography (PCC) and single column batch capture are numerically optimized and compared in terms of process performance for capturing a monoclonal antibody using protein A chromatography. Optimization is carried out with respect to productivity and capacity utilization (amount of product loaded per cycle compared to the maximum amount possible), while keeping yield and purity constant. For a wide range of process parameters, all three multi‐column processes show similar maximum capacity utilization and performed significantly better than batch. When maximizing productivity, the CaptureSMB process shows optimal performance, except at high feed titers, where batch chromatography can reach higher productivity values than the multi‐column processes due to the complete decoupling of the loading and elution steps, albeit at a large cost in terms of capacity utilization. In terms of trade‐off, i.e. how much the capacity utilization decreases with increasing productivity, CaptureSMB is optimal for low and high feed titers, whereas the 3‐column process is optimal in an intermediate region. Using these findings, the most suitable process can be chosen for different production scenarios.     

增殖细胞核抗原蛋白在Spodoptera frugiperda昆虫细胞中的表达及纯化

目的:利用昆虫细胞表达系统生产重组的人增殖细胞核抗原(proliferating cell nuclear antigen,PCNA),并进行纯化和抗体结合特性鉴定。方法:以HeLa细胞逆转录的cDNA为模板,扩增人PCNA基因,并插入杆状病毒载体AcMNPV。利用昆虫细胞得到PCNA基因的重组杆状病毒。病毒感染细胞表达蛋白,联合镍柱亲和层析和离子交换层析获得高纯度的重组人PCNA蛋白。ELISA法测定抗体结合特异性。结果:以HeLa细胞cDNA为模板得到的基因序列同GenBank的人PCNA基因序列一致。草地贪夜蛾细胞(Spodoptera frugiperda,Sf9)表达重组人PCNA(recombinant human PCNA,rPCNA)的最佳感染值(MOI)和感染时间分别为0.05h和144h。rPCNA的产量高达110mg/L细胞,纯度95%。间接ELISA法检测抗体结合特性,rPCNA的敏感性和特异性分别为93.3%和85.0%。结论:建立了rPCNA的表达和纯化方法,获得了高效表达、高度抗体结合特异性的PCNA蛋白,该蛋白质能进一步开发为PCNA相关疾病的体外诊断试剂盒,具较大的应用价值。