Downstream processing of human antibodies integrating an extraction capture step and cation exchange chromatography

In this paper we explore an alternative process for the purification of human antibodies from a Chinese hamster ovary (CHO) cell supernatant comprising a ligand-enhanced extraction capture step and cation exchange chromatography (CEX). The extraction of human antibodies was performed in an aqueous two-phase system (ATPS) composed of dextran and polyethylene glycol (PEG), in which the terminal hydroxyl groups of the PEG molecule were modified with an amino acid mimetic ligand in order to enhance the partition of the antibodies to the PEG-rich phase. This capture step was optimized using a design of experiments and a central composite design allowed the determination of the conditions that favor the partition of the antibodies to the phase containing the PEG diglutaric acid (PEG-GA) polymer, in terms of system composition. Accordingly, higher recovery yields were obtained for higher concentrations of PEG-GA and lower concentrations of dextran. The highest yield experimentally obtained was observed for an ATPS composed of 5.17% (w/w) dextran and 8% (w/w) PEG-GA. Higher purities were however predicted for higher concentrations of both polymers. A compromise between yield and purity was achieved using 5% dextran and 10% PEG-GA, which allowed the recovery of 82% of the antibodies with a protein purity of 96% and a total purity of 63%, determined by size-exclusion chromatography. ATPS top phases were further purified by cation exchange chromatography and it was observed that the most adequate cation exchange ligand was carboxymethyl, as the sulfopropyl ligand induced the formation of multi-aggregates or denatured forms. This column allowed the elution of 89% of the antibodies present in the top phase, with a protein purity of 100% and a total purity of 91%. The overall process containing a ligand-enhanced extraction step and a cation exchange chromatography step had an overall yield of 73%.     

Fully automatable two-dimensional reversed-phase capillary liquid chromatography with online tandem mass spectrometry for shotgun proteomics

Herein, we describe the development of a fully automatable technology that features online coupling of high‐pH RP separation with conventional low‐pH RP separation in a two‐dimensional capillary liquid chromatography (2‐D LC) system for shotgun proteomics analyses. The complete analysis comprises 13 separation cycles, each involving transfer of the eluate from the first‐dimension, high‐pH RP separation onto the second RP dimension for further separation. The solvent strength increases across the 13 fractions (cycles) to elute all peptides for further resolution on the second‐dimension, low‐pH RP separation, each under identical gradient‐elution conditions. The total run time per analysis is 52 h. In triplicate analyses of a lysate of mouse embryonic fibroblasts, we used this technology to identify 2431 non‐redundant proteins, of which 50% were observed in all three replicates. A comparison of RP‐RP 2‐D LC and strong cation exchange‐RP 2‐D LC analyses reveals that the two technologies identify primarily different peptides, thereby underscoring the differences in their separation chemistries.     

Simplified NaCl Based (68)Ga Concentration and Labeling Procedure for Rapid Synthesis of (68)Ga Radiopharmaceuticals in High Radiochemical Purity

A simple sodium chloride (NaCl) based (68)Ga eluate concentration and labeling method that enables rapid, high-efficiency labeling of DOTA conjugated peptides in high radiochemical purity is described. The method utilizes relatively few reagents and comprises minimal procedural steps. It is particularly well-suited for routine automated synthesis of clinical radiopharmaceuticals. For the (68)Ga generator eluate concentration step, commercially available cation-exchange cartridges and (68)Ga generators were used. The (68)Ga generator eluate was collected by use of a strong cation exchange cartridge. 98% of the total activity of (68)Ga was then eluted from the cation exchange cartridge with 0.5 mL of 5 M NaCl solution containing a small amount of 5.5 M HCl. After buffering with ammonium acetate, the eluate was used directly for radiolabeling of DOTATOC and DOTATATE. The (68)Ga-labeled peptides were obtained in higher radiochemical purity compared to other commonly used procedures, with radiochemical yields greater than 80%. The presence of (68)Ge could not be detected in the final product. The new method obviates the need for organic solvents, which eliminates the required quality control of the final product by gas chromatography, thereby reducing postsynthesis analytical effort significantly. The (68)Ga-labeled products were used directly, with no subsequent purification steps, such as solid-phase extraction. The NaCl method was further evaluated using an automated fluid handling system and it routinely facilitates radiochemical yields in excess of 65% in less than 15 min, with radiochemical purity consistently greater than 99% for the preparation of (68)Ga-DOTATOC.     

Analytical grade C-phycocyanin obtained by a single-step purification process

C-phycocyanin (C-PC) is a phycobiliprotein that can be used as a natural blue dye in the food and cosmetic industries, as a biomarker or as an agent in medical treatments, depending on its purity grade. Here we described for the first time a single-step purification process of C-PC extracted from the wet biomass of Spirulina (Arthrospira) platensis LEB-52 using ion exchange chromatography with pH gradient elution. Different conditions varying the elution buffers and volumes, the loading pH and the addition of salt in the elution buffer were studied. The chromatographic condition that resulted in high recovery and purity consisted in equilibration and washing with 0.025 mol/L Tris-HCl buffer pH 6.5 and elution combining a step with 0.08 mol/L NaCl in 0.025 mol/L Tris-HCl buffer pH 6.5 and a pH gradient elution with 0.05 mol/L citrate buffer pH 6.2–3.0. This process resulted in C-PC with purities of 4.2 and 3.5 with recoveries of 32.6 and 49.5 %, respectively, in one purification step.     

Advective hydrogel membrane chromatography for monoclonal antibody purification in bioprocessing

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. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:974–982, 2015     

Two step capture and purification of IgG2 using multicolumn countercurrent solvent gradient purification (MCSGP)

A two‐step chromatography process for monoclonal antibody (mAb) purification from clarified cell culture supernatant (cCCS) was developed using cation exchange Multicolumn Countercurrent Solvent Gradient Purification (MCSGP) as a capture step. After an initial characterization of the cell culture supernatant the capture step was designed from a batch gradient elution chromatogram. A variety of chromatographic materials was screened for polishing of the MCSGP‐captured material in batch mode. Using multi‐modal anion exchange in bind‐elute mode, mAb was produced consistently within the purity specification. The benchmark was a state‐of‐the‐art 3‐step chromatographic process based on protein A, anion and cation exchange stationary phases. The performance of the developed 2‐step process was compared to this process in terms of purity, yield, productivity and buffer consumption. Finally, the potential of the MCSGP process was investigated by comparing its performance to that of a classical batch process that used the same stationary phase. Biotechnol. Bioeng. 2010;107: 974–984. © 2010 Wiley Periodicals, Inc.     

A novel twin‐column continuous chromatography approach for separation and enrichment of monoclonal antibody charge variants

Downstream processing of mAb charge variants is difficult owing to their similar molecular structures and surface charge properties. This study aimed to apply a novel twin‐column continuous chromatography (called N‐rich mode) to separate and enrich acidic variants of an IgG1 mAb. Besides, a comparison study with traditional scaled‐up batch‐mode cation exchange (CEX) chromatography was conducted. For the N‐rich process, two 3.93 mL columns were used, and the buffer system, flow rate and elution gradient slope were optimized. The results showed that 1.33 mg acidic variants with nearly 100% purity could be attained after a 22‐cycle accumulation. The yield was 86.21% with the productivity of 7.82 mg/L/h. On the other hand, for the batch CEX process, 4.15 mL column was first used to optimize the separation conditions, and then a scaled‐up column of 88.20 mL was used to separate 1.19 mg acidic variants with the purity of nearly 100%. The yield was 59.18% with the productivity of 7.78 mg/L/h. By comparing between the N‐rich and scaled‐up CEX processes, the results indicated that the N‐rich method displays a remarkable advantage on the product yield, i.e. 1.46‐fold increment without the loss of productivity and purity. Generally, twin‐column N‐rich continuous chromatography displays a high potential to enrich minor compounds with a higher yield, more flexibility and lower resin cost.     

Shotgun proteome analysis utilising mixed mode (reversed phase‐anion exchange chromatography) in conjunction with reversed phase liquid chromatography mass spectrometry analysis

The 2‐D peptide separations employing mixed mode reversed phase anion exchange (MM (RP‐AX)) HPLC in the first dimension in conjunction with RP chromatography in the second dimension were developed and utilised for shotgun proteome analysis. Compared with strong cation exchange (SCX) typically employed for shotgun proteomic analysis, peptide separations using MM (RP‐AX) revealed improved separation efficiency and increased peptide distribution across the elution gradient. In addition, improved sample handling, with no significant reduction in the orthogonality of the peptide separations was observed. The shotgun proteomic analysis of a mammalian nuclear cell lysate revealed additional proteome coverage (2818 versus 1125 unique peptides and 602 versus 238 proteins) using the MM (RP‐AX) compared with the traditional SCX hyphenated to RP‐LC‐MS/MS. The MM analysis resulted in approximately 90% of the unique peptides identified present in only one fraction, with a heterogeneous peptide distribution across all fractions. No clustering of the predominant peptide charge states was observed during the gradient elution. The application of MM (RP‐AX) for 2‐D LC proteomic studies was also extended in the analysis of iTRAQ‐labelled HeLa and cyanobacterial proteomes using nano‐flow chromatography interfaced to the MS/MS. We demonstrate MM (RP‐AX) HPLC as an alternative approach for shotgun proteomic studies that offers significant advantages over traditional SCX peptide separations.     

Strategy for a protein purification design using C-phycocyanin extract

A variety of techniques have been developed for the separation and recovery of proteins. The cost of purifying the product is frequently determined by the desired quality of the final product, which is evaluated by measuring the purity. In this work the design of a protein purification process for C-phycocyanin, a phycobiliprotein that can be used in the food and medical industries, was established. The study evaluated the use of ammonium sulfate precipitation, ion exchange chromatography and gel filtration to purify C-phycocyanin in a variety of sequences. The final design included the C-phycocyanin extraction step, precipitation with ammonium sulfate and ion exchange chromatography. When the elution step was studied, the kind of elution and pH were considered in order to obtain a product with a final purity of 4.0 with a purification factor of 6.35, so that, at the end of the strategy, C-phycocyanin of analytical grade would be obtained.     

High-throughput process development for recombinant protein purification

Methods development in chromatographic purification processes is a complex operation and has traditionally relied on trial and error approaches. The availability of a large number of commercial media, choice of different modes of chromatography, and diverse operating conditions contribute to the challenging task of accelerating methods development. In this paper, we describe a novel microtiter-plate based screening method to identify the appropriate sequence of chromatographic steps that result in high purities of bioproducts from their respective culture broths. Protein mixtures containing the bioproduct were loaded on aliquots of different chromatographic media in microtiter plates. Serial step elution of the proteins, in concert with bioproduct-specific assays, resulted in the identification of "active fractions" containing the bioproduct. The identification of a successful chromatographic step was based on the purity of the active fractions, which were then pooled and used as starting material for screening the next chromatographic dimension. This procedure was repeated across subsequent dimensions until single band purities of the protein were obtained. The sequence of chromatographic steps and the corresponding operating conditions identified from the screen were validated under scaled-up conditions. Various modes of chromatography including hydrophobic interaction, ion exchange (cation and anion exchange) and hydrophobic charge-induction chromatography (HCIC), and different operating conditions (pH, salt concentration and type, etc.) were employed in the screen. This approach was employed to determine the sequence of chromatographic steps for the purification of recombinant alpha-amylase from its cell-free culture broth. Recommendations from the screen resulted in single-band purity of the protein under scaled-up conditions. Similar results were observed for an scFv-beta-lactamase fusion protein. The use of a miniaturized screen enables the parallel screening of a wide variety of actual bioprocess media and conditions and represents a novel paradigm approach for the high-throughput process development of recombinant proteins.     

Reliable detection of deamidated peptides from lens crystallin proteins using changes in reversed-phase elution times and parent ion masses

Identifying deamidated peptides using low-resolution mass spectrometry is difficult because traditional database search programs cannot accurately detect modified peptides when the mass differences are only 0.984 Da. In this study, we utilized differential reversed-phase elution behavior of deamidated and corresponding unmodified peptide forms to significantly improve deamidation detection on a low-resolution LCQ ion trap instrument. We also improved the mass measurements of unmodified and deamidated peptide forms by averaging survey scans across each chromatogram peak. Tryptic digests of a series of normal (3-day old, 2-year old, 18-year old, 35-year old, and 70-year old) and cataractous (93-year old) human lens samples were used to produce large numbers of potentially deamidated peptides. The complex peptide mixtures were separated by strong cation exchange (SCX) chromatography followed by reversed-phase (RP) chromatography. Synthetic peptides were used to show that unmodified and deamidated peptides coeluted during the SCX separation and were completely resolved with the RP conditions used. Retention time shifts (RTS) and mass differences (DeltaM) of deamidated lens peptides and their corresponding unmodified forms were manually determined for the 70-year old lens sample. These values were used to assign correct or incorrect deamidation identifications from SEQUEST searches where deamidation was specified as a variable modification. Manual validation of SEQUEST identifications from synthetic peptides, 3-day old, and 70-year old samples had an overall 42% deamidation detection accuracy. Filtering SEQUEST identifications using RTS and DeltaM constraints resulted in >93% deamidation detection accuracy. An algorithm was developed to automate this method, and 72 Crystallin deamidation sites, 18 of which were not previously reported in human lens tissue, were detected.     

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.     

Protein purification using chromatography: selection of type, modelling and optimization of operating conditions

To achieve a high level of purity in the purification of recombinant proteins for therapeutic or analytical application, it is necessary to use several chromatographic steps. There is a range of techniques available including anion and cation exchange, which can be carried out at different pHs, hydrophobic interaction chromatography, gel filtration and affinity chromatography. In the case of a complex mixture of partially unknown proteins or a clarified cell extract, there are many different routes one can take in order to choose the minimum and most efficient number of purification steps to achieve a desired level of purity (e.g. 98%, 99.5% or 99.9%). This review shows how an initial 'proteomic' characterization of the complex mixture of target protein and protein contaminants can be used to select the most efficient chromatographic separation steps in order to achieve a specific level of purity with a minimum number of steps. The chosen methodology was implemented in a computer- based Expert System. Two algorithms were developed, the first algorithm was used to select the most efficient purification method to separate a protein from its contaminants based on the physicochemical properties of the protein product and the protein contaminants and the second algorithm was used to predict the number and concentration of contaminants after each separation as well as protein product purity. The application of the Expert System approach was experimentally tested and validated with a mixture of four proteins and the experimental validation was also carried out with a supernatant of Bacillus subtilis producing a recombinant beta-1,3-glucanase. Once the type of chromatography is chosen, optimization of the operating conditions is essential. Chromatographic elution curves for a three-protein mixture (alpha-lactoalbumin, ovalbumin and beta-lactoglobulin), carried out under different flow rates and ionic strength conditions, were simulated using two different mathematical models. These models were the Plate Model and the more fundamentally based Rate Model. Simulated elution curves were compared with experimental data not used for parameter identification. Deviation between experimental data and the simulated curves using the Plate Model was less than 0.0189 (absorbance units); a slightly higher deviation [0.0252 (absorbance units)] was obtained when the Rate Model was used. In order to optimize operating conditions, a cost function was built that included the effect of the different production stages, namely fermentation, purification and concentration. This cost function was also successfully used for the determination of the fraction of product to be collected (peak cutting) in chromatography. It can be used for protein products with different characteristics and qualities, such as purity and yield, by choosing the appropriate parameters.     

疏水层析结合冷乙醇沉淀纯化人血清白蛋白

将层析技术与冷乙醇工艺相结合用于人血清白蛋白的纯化 ,对各过程所采用的层析介质及层析条件进行了探索 ,得到了一条从人血浆中制备血清白蛋白的新路线 :将一步冷乙醇沉淀后的血浆上清进行脱盐除乙醇 ,用阳离子交换介质CMSepharoseFF以透过式层析的模式吸附非白蛋白组分 ,最后选用ButylSepharoseFF一步疏水层析后所得样品经SDS-PAGE银染显示一条单带 ,分析其纯度大于 99% ,计算工艺收率为 81.2%。与传统冷乙醇工艺相比较 ,该工艺最终样品纯度更高 ,且层析可以在常温下操作 ,易实现自动化控制.     

Resolution of heterogeneous charged antibody aggregates via multimodal chromatography: A comparison to conventional approaches

Clearance of aggregates during protein purification is increasingly paramount as protein aggregates represent one of the major impurities in biopharmaceutical products. Aggregates, especially dimer species, represent a significant challenge for purification processing since aggregate separation coupled with high purity protein recovery can be difficult to accomplish. Biochemical characterization of the aggregate species from the hydrophobic interaction and cation exchange chromatography elution peaks revealed two different charged populations, i.e. heterogeneous charged aggregates, which led to further challenges for chromatographic removal. This paper compares multimodal versus conventional cation exchange or hydrophobic chromatography methodologies to remove heterogeneous aggregates. A full, mixed level factorial design of experiment strategy together with high throughput experimentation was employed to rapidly evaluate chromatographic parameters such as pH, conductivity, and loading. A variety of operating conditions were identified for the multimodal chromatography step, which lead to effective removal of two different charged populations of aggregate species. This multimodal chromatography step was incorporated into a monoclonal antibody purification process and successfully implemented at commercial manufacturing scale. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:636–645, 2014     

High-throughput protein purification under denaturating conditions by the use of cation exchange chromatography

A high-throughput protein purification strategy using the polycationic Z(basic) tag has been developed. In order for the strategy to be useful both for soluble and less soluble proteins, a denaturating agent, urea, was used in all purification steps. First, four target proteins were genetically fused to the purification tag, Z(basic). These protein constructs were purified by cation exchange chromatography and eluted using a salt gradient. From the data achieved, a purification strategy was planned including stepwise elution to enable parallel protein purification using a laboratory robot. A protocol that includes all steps, equilibration of the chromatography resin, load of sample, wash, and elution, all without any manual handling steps, was handled by the laboratory robot. The program allows automated purification giving milligram amounts of pure recombinant protein of up to 60 cell lysates. In this study 22 different protein constructs, with different characteristics regarding pI and solubility, were successfully purified by the laboratory robot. The data show that Z(basic) can be used as a general purification tag also under denaturating conditions. Moreover, the strategy enables purification of proteins with different pI and solubility using ion exchange chromatography (IEXC). The procedure is highly reproducible and allows for high protein yield and purity and is therefore a good complement to the commonly used His(6)-tag.     

Clarification and capture of high‐concentration refold pools for E. coli‐based therapeutics using expanded bed adsorption chromatography

Expanded bed adsorption (EBA) chromatography was investigated for clarification and capture of high‐concentration refold pools of Escherichia coli‐based therapeutics. Refolding of denatured inclusion bodies (IBs) at high protein concentration significantly improved product throughput; however, direct filtration of the refold materials became very challenging because of high content of protein precipitates formed during refolding. In addition, irreversible protein precipitation caused by high local concentration was encountered in packed bed capture during cation exchange chromatography elution, which limited column loading capacity and capture step productivity. In this study, the two issues are addressed in one unit operation by using EBA. Specifically, EBA can handle feed streams with significant amount of particles and precipitates, which eliminated the need for refold pool clarification through filtration. The relatively broad EBA elution profile is particularly suitable for proteins of low solubility and can effectively avoid product loss previously associated with on‐column precipitation during capture. As the EBA resin (RHOBUST^® FastLine SP IEX) used here has unique properties, it can be operated at high linear velocity (800–1,600 cm/h), while achieving a selectivity and impurity clearance largely comparable to the packed bed resin of the same ligand chemistry (SP Sepharose FF). Furthermore, the filtration of the EBA elution pool is easily manageable within facility capability. Overall, this study demonstrates that the EBA process helps debottleneck the purification of high‐turbidity refold pools by removing precipitates and concurrently capturing the product, which can be applied to other E. coli‐based therapeutics that also requires refolding of IBs. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 30:113–123, 2014     

Reduction of product-related species during the fermentation and purification of a recombinant IL-1 receptor antagonist at the laboratory and pilot scale

Through a parallel approach of tracking product quality through fermentation and purification development, a robust process was designed to reduce the levels of product-related species. Three biochemically similar product-related species were identified as byproducts of host-cell enzymatic activity. To modulate intracellular proteolytic activity, key fermentation parameters (temperature, pH, trace metals, EDTA levels, and carbon source) were evaluated through bioreactor optimization, while balancing negative effects on growth, productivity, and oxygen demand. The purification process was based on three non-affinity steps and resolved product-related species by exploiting small charge differences. Using statistical design of experiments for elution conditions, a high-resolution cation exchange capture column was optimized for resolution and recovery. Further reduction of product-related species was achieved by evaluating a matrix of conditions for a ceramic hydroxyapatite column. The optimized fermentation process was transferred from the 2-L laboratory scale to the 100-L pilot scale and the purification process was scaled accordingly to process the fermentation harvest. The laboratory- and pilot-scale processes resulted in similar process recoveries of 60 and 65%, respectively, and in a product that was of equal quality and purity to that of small-scale development preparations. The parallel approach for up- and downstream development was paramount in achieving a robust and scalable clinical process.     

Polishing approach with fully connected flow‐through purification for therapeutic monoclonal antibody

The biopharmaceutical industry is evolving toward process intensification that can offer increased productivity and improved economics without sacrificing process robustness. A semi‐continuous downstream process linking purification/polishing unit operations in series can reduce or eliminate intermediate holding tanks and reduce overall processing time. Accordingly, we have developed a therapeutic monoclonal antibody polishing template comprised of a connected flow‐through polishing technologies that include activated carbon, cation exchange, and anion‐exchange chromatography. In this report, we evaluated fully‐connected pool‐less polishing with three flow‐through technologies, operating as a single skid to streamline and improve an mAb purification platform. Laboratory‐scale pool‐less processing was achieved without utilizing in‐line pH adjustment and conductivity dilution based on the previously optimized single process parameter. Two connected flow‐through configurations of polishing steps were evaluated: a two‐step process using anion exchange and cation exchange and a three step process using activated carbon, anion exchange and cation exchange chromatography. Laboratory‐scale proof of concept studies showed comparable performance between the batch purification process and the pool‐less process configuration. Three step polishing highly intensified the processes and provided higher process loading and achieved bulk drug specification with higher impurity clearance (>95%) and high overall mAb yield (>95%).