Comparison of ceramic hydroxy- and fluoroapatite versus Protein A/G-based resins in the isolation of a recombinant human antibody from cell culture supernatant

A recombinant human antibody (IgG(1)-subtype) was produced in Chinese Hamster Ovary (CHO) cells. Alternatives to the established isolation by Protein A affinity chromatography were investigated. Neither an alternative elution agent (Arginine) nor an alternative affinity ligand (Protein G) resulted in an improvement in yield and/or purity. Subsequently, apatite stationary phases including a novel ceramic fluoroapatite material were tested. By applying a double gradient (first 0 to 1M NaCl, then 0.01 to 0.4M phosphate) the culture supernatant was separated into three fractions: the flow through, which contained no active antibody, the NaCl-eluate, which contained the antibody and no other discernible protein contaminants, and a fraction that eluted in the phosphate gradient and contained several proteins, but no active antibody. In case of the hydroxyapatite, retention of the antibody decreased and yield increased when the pH was raised from 6.0 to 8.2 (isoelectric point (pI) of the antibody: 8.3), to reach a yield of 71% at pH of 8.2. In case of the fluoroapatite, retention was also found to increase with increasing mobile phase pH, but the yields went through a maximum (of ca. 90%) at a mobile phase pH of 7.0. No traces of contaminants were seen in the corresponding gel. This is the first time that yields of 90% and such high purities have been reported as the result of a single chromatographic step for the antibody in question with either (Protein A) affinity or apatite chromatography.     

Gellan beads as a transparent media for protein immobilization and affinity capture

Gellan gum beads are presented as a novel substrate for protein immobilization and immobilized protein activity measurements. The optical transparency of the gellan beads down to 200 nm provides a method for direct quantitation of the amount of protein immobilized onto the beads. The ability to utilize these beads in a non-aqueous activation step allowed for a fourfold increase in the amount of protein immobilized, and this method was used to immobilize Protein A onto gellan beads at a final yield of 1.42+/-0.07 mg of Protein A/g of beads. The optical transparency also allowed for detection of the activity of the immobilized Protein A simply by measuring the absorbance of the beads following capture of rabbit IgG. This activity measurement method was compared with a traditional method utilizing the amount of protein remaining in solution after the IgG capture step. The traditional method yielded an activity measurement of 10.9+/-0.2 mg IgG/mg of Protein A, while the absorbance method showed an activity of only 7.5+/-0.3 mg IgG/mg of Protein A. The difference can be explained by the more direct measurement used in the absorbance method. The optical transparency of the beads was also evaluated in a fluorescence based IgG capture experiment, showing that detection of fluorescent IgG captured on the beads was possible with no interference from the beads.     

Accelerated purification process development of monoclonal antibodies for shortening time to clinic. Design and case study of chromatography processes

For accelerating the purification process development of human monoclonal antibodies (hmAbs) for pharmaceutical drugs, we designed a standardized method for setting the conditions of the purification process, which could be applied to hmAbs for the early phase of pharmaceutical development. The process includes three sequential chromatography steps: Protein A affinity chromatography (AFC), anion-exchange chromatography (AIEC) and cation-exchange chromatography (CIEC), and also includes a low pH virus inactivation step after the AFC step. We predicted the elution pH in the AFC and elution salt concentration in the CIEC from the amino acid sequences of hmAbs, as described in our previous paper. The mobile phase pH in AIEC and the pH for virus inactivation were also predicted based on the amino acid sequence of hmAb. As a case study, six hmAbs (two of IgG(1), two of IgG(2) and two of IgG(4)) were purified with the standardized method. The recovery, purity and clearance of impurities (DNA, host cell proteins (HCP), and Protein A) were examined. All the six hmAbs were purified with high recovery and high clearance of the impurities. Factors affecting the impurities level in the purified products are also discussed.     

Factorial screening of antibody purification processes using three chromatography steps without protein A

Protein A affinity chromatography is often employed as a capture step to meet the purity, yield, and throughput requirements for pharmaceutical antibody purification. However, a trade-off exists between step performance and price. Protein A resin removes 99.9% of feed stream impurities; however, its price is significantly greater than those of non-affinity media. With many therapeutic indications for antibodies requiring high doses and/or chronic administration, the consideration of process economics is critical. We have systematically evaluated the purification performance of cation-exchange, anion-exchange, hydroxyapatite, hydrophobic interaction, hydrophobic charge induction, and small-molecule ligand resins in each step of a three-step chromatographic purification process for a CHO-derived monoclonal antibody. Host cell proteins were removed to less-than-detectable for three processes (cation-exchange-anion-exchange-hydrophobic interaction chromatography, cation-exchange-anion-exchange-mixed cation-exchange chromatography, and cation-exchange-mixed cation-exchange-anion-exchange chromatography). The order of the process steps affected purification performance significantly.     

Single-step method for purification of human transferrin from a by-product of chromatographic fractionation of plasma.

A rapid, simple and convenient method is described for the isolation, on a pilot scale, of pure and functional human transferrin from an unexploited by-product of chromatographic fractionation of plasma. In a single chromatographic step on DEAE-Spherodex, 97% pure transferrin was obtained in 75% yield. A virus inactivation treatment was included in the preparative process in order to guarantee the safety of the final product, which could be used in culture media.     

Quantification of immunoglobulin G and characterization of process related impurities using coupled Protein A and size exclusion high performance liquid chromatography

The present work describes two HPLC-UV methods for multi-protein quantification using (i) only a Protein A sensor cartridge (Protein A HPLC) and (ii) the same Protein A cartridge in combination with a size exclusion HPLC column (PSEC-HPLC). The possibility to simultaneously quantify immunoglobulin G (IgG) besides a non-binding protein such as bovine serum albumin (BSA) increases the applicability of Protein A HPLC. Its most pronounced feature is its independence of the buffer system, pH-value and salt content of the investigated sample solvent, which includes cell media. A comparison with the state-of-the-art, the photometrical Bradford method, shows that Protein A HPLC is as sensitive as Bradford, but that it comes with an extended linear range of 4 orders of magnitude, ranging from 0.15 [μg abs] to 1 [mg abs] absolute injected protein amount. The applicability of the PSEC-HPLC method is demonstrated for the analysis of real cell culture feed samples. While Protein A binds IgG, the SEC-column distributes the feed impurities by their molecular weight. The peak area ratios of IgG and the feed impurities of interest are then plotted against the collected sample fraction. These Protein A-Size-Exclusion-Chromatographic diagrams (PSEC-plot) combine the performance information of feed impurities and IgG in a single plot. Further it is shown that both methods are suitable for the performance evaluation of antibody purification media using static as well as dynamic binding experiments performed on DEAE-Fractogel and Capto Adhere. The investigated test samples were “mock” protein solutions with increasing complexity ranging from simple PBS buffer to serum free cell media and “real” cell culture feed solutions.     

Effect of primary metabolites on protein utilization byAgaricus bisporus,Coprinus cinereus,andVolvariella volvacea

Protein is probably a major nitrogen constituent in the natural habitats of basidiomycete fungi. The ability of two commercial crop species, Agaricus bisporus and Volvariella volvacea, and a common weed, Coprinus cinereus, to degrade protein was investigated. Mycelia were incubated at 25‡C in static liquid cultures on completely defined media supplemented with 1% (w/v) soluble casein as the protein source. Glucose, ammonium, or sulfate were added as alternative sources of the major elements. Tests were also made on media devoid of protein. Alternative nitrogen or sulfur sources had little or no effect on the rate of protein degradation, pH, medium glucose, or ammonium concentrations or mycelial dry weight yields. However, addition of glucose affected these parameters markedly, with a 3–4-fold increase in the dry weights of all three organisms and a two-fold increase in the rate of protein degradation by C. cinereus and V. volvacea. A. bisporus degraded protein at the same rate in both the presence or absence of glucose. Growth of the organisms was similar whether glucose or protein was the sole source of carbon. With glucose present, the pH decreased during the early stages of growth, being correlated with glucose utilization. Upon glucose disappearance, the pH increased in the presence of protein, but no subsequent change occurred with the glucose as a sole carbon source. In the absence of protein, the pH decreased to pH 3. At this pH no subsequent changes occurred in dry weight yields, glucose, or ammonium. With protein present, changes in medium ammonium concentration were correlated with dry weight yield, protein utilization, and pH. Thus, a strong correlation appears to exist between protein and glucose utilization and changes in pH and ammonium as well as dry weight yield. The increase in medium ammonium is probably caused by the deamination of the protein in the absence of glucose and its utilization as an energy source. However, the protein is utilized as efficiently as is glucose as a sole source of carbon.     

Evaluation of Sample Preparation Strategies for Human Milk and Plasma Proteomics

Sample preparation is the most critical step in proteomics as it directly affects the subset of proteins and peptides that can be reliably identified and quantified. Although a variety of efficient and reproducible sample preparation strategies have been developed, their applicability and efficacy depends much on the biological sample. Here, three approaches were evaluated for the human milk and plasma proteomes. Protein extracts were digested either in an ultrafiltration unit (filter-aided sample preparation, FASP) or in-solution (ISD). ISD samples were desalted by solid-phase extraction prior to nRPC-ESI-MS/MS. Additionally, milk and plasma samples were directly digested by FASP without prior protein precipitation. Each strategy provided inherent advantages and disadvantages for milk and plasma. FASP appeared to be the most time efficient procedure with a low miscleavage rate when used for a biological sample aliquot, but quantitation was less reproducible. A prior protein precipitation step improved the quantitation by FASP due to significantly higher peak areas for plasma and a much better reproducibility for milk. Moreover, the miscleavage rate for milk, the identification rate for plasma, and the carbamidomethylation efficiency were improved. In contrast, ISD of both milk and plasma resulted in higher miscleavage rates and is therefore less suitable for targeted proteomics.     

Initial evaluation of protein A modified capillary‐channeled polymer fibers for the capture and recovery of immunoglobulin G

A novel protein A affinity chromatography stationary phase has been developed from polypropylene capillary‐channeled polymer fibers modified with a recombinant protein A ligand for the capture and recovery of immunoglobulin G (IgG) with high specificity and yield. An SPE micropipette tip format was employed so that solvent, protein, and antibody consumption was minimized. The adsorption modification of the fiber surfaces with protein A was evaluated as a function of feed concentration and volume. Optimal modification of the fiber surface with protein A yielded a 5.7 mg/mL (bed volume) ligand capacity with the modified fibers showing stability across numerous solvent environments. Performance was evaluated through exposure to human IgG and myoglobin, individually and as a mixture. Myoglobin was used as a surrogate for host cell proteins common to growth media. The efficacy of the selective binding to the ligand is demonstrated by the 2.9:1 (IgG/protein A) binding stoichiometry. Elution with 0.1 M acetic acid yielded an 89% recovery of the captured IgG based on absorption measurements of the collected eluents. Regeneration was possible with 10 mM NaOH. Protein A modified polypropylene capillary‐channeled polymer fibers show promising initial results as an affinity phase for efficient capture and purification of IgG.     

The simultaneous analysis of proteins, lipids, and diterpenoid resins found in cultural objects

We report a GC-MS method for the simultaneous analysis of proteins oil, and diterpenoid resins found in cultural objects. The method was initially designed for protein analysis of protenaceous paints and adhesives and involves acid hydrolysis as the first step. The amino acids in the protein hydrolysates, thus obtained, are treated with propan-l-ol/ hydrogen chloride and then pentafluoropropionic anhydride. The procedure was found also to yield the propyl esters of fatty acids derived from lipids and diterpenoid acids derived from natural resins, and thus allows the choice of a single method for the analysis of artists media which contain either oil s or proteins or mixtures of both proteins and oils or even resins. Thus natural mixtures such as egg yolk and also mixtures made by the artist such as animal glue/seed oil emulsions can be analysed. Coupled with FTIR analysis of paints and the staining of cross sections, to indicate layer structure the method can help to elucidate the paints and adhesives used by artists.     

Comparison of protein A affinity sorbents II. Mass transfer properties

Protein A affinity chromatography is the standard purification method for isolation of therapeutic antibodies. Due to improvements in expression technology and optimization of fermentation, culture supernatants with high antibody content must be processed. Recently protein A affinity media with improved adsorption characteristics have been developed. The agarose media MabSelect Xtra and MabSelect SuRe are recent developments of the existing protein A affinity medium MabSelect. MabSelect Xtra is designed to exhibit a higher binding capacity for IgG, and MabSelect SuRe is functionalized with an alkaline stabilized protein A. ProSep-vA Ultra is a porous glass medium with a pore size of 70 nm, also developed to improve the binding capacity. Adsorption was measured in a finite and infinite bath. Mass transfer in these systems could be well described by a model including film and pore diffusion. Mass transfer parameters were used to accurately predict IgG breakthrough in packed bed mode. The dynamic binding capacity of all three media did not change when residence time was at least 4 min. All three media are suited for capture of feed stocks with high antibody content.     

Scale-up of free-flow electrophoresis: II. Purification of alcohol dehydrogenase from a crude yeast extract by field step electrophoresis and combined field step-zone electrophoresis

Results of the purification of alcohol dehydrogenase (ADH) by field step electrophoresis and combined field step-zone electrophoresis are presented. In field step electrophoresis, optimization of voltage, residence time and pH of the sample solution led to a maximal purification factor of 2.8 and a yield of 89% ADH. The limit of loading capacity was reached at a protein concentration of the sample solution of approximately 4 g/L, allowing a maximal throughput of 1.14 g/h with a yield of 86% and a 2.8-fold purification in the Elphor VaP 22 apparatus. With a production scale apparatus a throughput of 2.07 g/h without any loss of separation quality could be achieved. By introducing the sample solution into the separation chamber through 3 inlets, simultaneously, the throughput was increased to 3.2 g/h with a purification factor of 2.7 and a yield of 82% ADH. For the combined field step-zone electrophoresis method a maximum purification factor of 3.6 and a yield of 80% ADH were achieved. The loading capacity was limited to a 4.13 g/L protein concentration of the sample solution, resulting in a throughput of 440 mg/h. Injecting the sample solution simultaneously into 3 inlets resulted in a maximum throughput of 1.92 g/h with 3.1-fold purification and a yield of 80% ADH. Zone electrophoresis, field step electrophoresis and a combination of both are compared with respect to resolution, throughput and the application potential in a protein purification scheme. A scale-up to 3 g/h is possible in zone electrophoresis and field step electrophoresis.(ABSTRACT TRUNCATED AT 250 WORDS)     

Separation of influenza virus‐like particles from baculovirus by polymer‐grafted anion exchanger

The baculovirus expression vector system is a very powerful tool to produce virus‐like particles and gene‐therapy vectors, but the removal of coexpressed baculovirus has been a major barrier for wider industrial use. We used chimeric human immunodeficiency virus‐1 (HIV‐1) gag influenza‐hemagglutin virus‐like particles produced in Tnms42 insect cells using the baculovirus insect cell expression vector system as model virus‐like particles. A fast and simple purification method for these virus‐like particles with direct capture and purification within one chromatography step was developed. The insect cell culture supernatant was treated with endonuclease and filtered, before it was directly loaded onto a polymer‐grafted anion exchanger and eluted by a linear salt gradient. A 4.3 log clearance of baculovirus from virus‐like particles was achieved. The absence of the baculovirus capsid protein (vp39) in the product fraction was additionally shown by high performance liquid chromatography‐mass spectrometry. When considering a vaccination dose of 10⁹ particles, 4200 doses can be purified per L pretreated supernatant, meeting the requirements for vaccines with <10 ng double‐stranded DNA per dose and 3.4 µg protein per dose in a single step. The process is simple with a very low number of handling steps and has the characteristics to become a platform for purification of these types of virus‐like particles.     

Predictive chromatographic simulations for the optimization of recovery and aggregate clearance during the capture of monoclonal antibodies

Predictive chromatographic simulations were used to assess whether significant aggregate clearance, in addition to high step recovery and limited eluate pool volumes, can be achieved during protein A affinity chromatography capture steps. Such aggregates of the antibody monomer are commonly found in manufacturing processes. A lumped desorption-kinetic limiting model was used to describe the elution from the chromatography column, as batch isotherm measurements indicated no adsorption under elution conditions. In order to quantify the trade-off between step recovery and aggregate clearance, independent experiments were first performed to obtain the key kinetic parameters. These parameters were used in simulations to predict the behavior of bench-scale protein A column runs and identify robust operating windows within which good yields and significant aggregate clearance can be achieved. Two examples are described. For antibody A, a robust window of operation was identified. In this case, the optimal conditions were transferred to pilot-plant scale, and the resulting experimental data were shown to be in good agreement with model predictions. For antibody B, it was found that conditions resulting in high recovery and good aggregate clearance were not robust: at the optimal elution conditions, changes of ±0.1 units in pH or ±1 mS/cm in conductivity affected the results substantially.     

Catalytic air oxidation of manganese in synthetic waters

An attempt was made to study the oxidation of manganese by air in synthetic waters. A series of batch experments were performed at differnet values of concentration, temperature and pH. Unoxidized manganese in the solution was determined by formaldoxime spectrometric method. Results of these studies indicated that the air oxidation of manganese soluble in water can be effectively performed in basic media and that oxidation yield increasedwith an increase in pH and concentration. The yield was very high in the presence of manganese dioxide, sepiolite or clinoptilolite in solution and, the oxidation was almost completed especially at high values of pH and concentration. The reaction was found to be first order with respect to Mn²⁺ with a very low activation energy. A yield of 62% was obtained for the air oxidation of wastewater taken from the treatment plant of Corum Municipality.     

Efficient on-column conversion of IgG1 trisulfide linkages to native disulfides in tandem with Protein A affinity chromatography

Protein trisulfide linkages are generated by the post-translational insertion of a sulfur atom into a disulfide bond. Molecular heterogeneity was detected in a recombinant IgG₁ monoclonal antibody (mAb) and attributed to the presence of a protein trisulfide moiety. The predominant site of trisulfide modification was the bond between the heavy and light chains. The trisulfide was eliminated during purification of the IgG₁ mAb via a cysteine wash step incorporated into Protein A affinity column chromatography. Analysis of the cysteine-treated mAb by electrophoresis and peptide mapping indicated that the trisulfide linkages were efficiently converted to intact disulfide bonds (13% trisulfide decreased consistently to 1% or less) without disulfide scrambling or an increase in free sulfhydryls. The on-column trisulfide conversion caused no change in protein folding detectable by hydrogen/deuterium exchange or differential scanning calorimetry. Consistent with this, binding of the mAb to its antigen in vitro was insensitive to the presence of the trisulfide modification and to its removal by the on-column cysteine treatment. Similar, high efficiency trisulfide conversion was achieved for a second IgG₁ mAb using the column wash strategy (at least 7% trisulfide decreased to 1% or less). Therefore, trisulfide/disulfide heterogeneity can be eliminated from IgG₁ molecules via a convenient and inexpensive procedure compatible with routine Protein A affinity capture.     

Modeling of protein interactions with surface-grafted charged polymers. Correlations between statistical molecular modeling and a mean field approach

Ion exchange media involving charge groups attached to flexible polymers are widely used for protein purification. Such media often provide enhanced target protein purity and yield. Yet, little is understood about protein interaction with such media at the molecular level, or how different media architectures might affect separation performance. To gain a better understanding of such adsorptive systems, statistical mechanical perturbation calculations, utilizing a Debye-Hückel potential, were performed on surface-grafted charged polymers and their interaction with model proteins. The studied systems were weakly charged, and the polymers were linear and relatively short (degree of polymerization is 30). Segment distributions from the surface were also determined. The interaction of spherical model protein particles of 12-30 A radius were investigated with respect to polymer grafting density, distance from matrix surface, protein charge, and ionic strength. The partitioning coefficient of the model proteins was determined for different distances from the surface. An empirical mean field theory that scales the entropy of the protein with the square of the protein radius correlates well to Monte Carlo statistical modeling results. Upon adsorption to the polymer layers, the model proteins exhibit a critical surface charge density that is proportional to the ionic strength, independent of the grafting density, and appears to be a fundamental determinant of protein adsorption. Partitioning of protein-like nanoparticles to the charged polymer surface is only favored above the particle critical charge density.     

Exploration of overloaded cation exchange chromatography for monoclonal antibody purification

Cation exchange chromatography using conventional resins, having either diffusive or perfusive flow paths, operated in bind-elute mode has been commonly employed in monoclonal antibody (MAb) purification processes. In this study, the performance of diffusive and perfusive cation exchange resins (SP-Sepharose FF (SPSFF) and Poros 50HS) and a convective cation exchange membrane (Mustang S) and monolith (SO(3) Monolith) were compared. All matrices were utilized in an isocratic state under typical binding conditions with an antibody load of up to 1000 g/L of chromatographic matrix. The dynamic binding capacity of the cation exchange resins is typically below 100 g/L resin, so they were loaded beyond the point of anticipated MAb break through. All of the matrices performed similarly in that they effectively retained host cell protein and DNA during the loading and wash steps, while antibody flowed through each matrix after its dynamic binding capacity was reached. The matrices differed, though, in that conventional diffusive and perfusive chromatographic resins (SPSFF and Poros 50HS) demonstrated a higher binding capacity for high molecular weight species (HMW) than convective flow matrices (membrane and monolith); Poros 50HS displayed the highest HMW binding capacity. Further exploration of the conventional chromatographic resins in an isocratic overloaded mode demonstrated that the impurity binding capacity was well maintained on Poros 50HS, but not on SPSFF, when the operating flow rate was as high as 36 column volumes per hour. Host cell protein and HMW removal by Poros 50HS was affected by altering the loading conductivity. A higher percentage of host cell protein removal was achieved at a low conductivity of 3 mS/cm. HMW binding capacity was optimized at 5 mS/cm. Our data from runs on Poros 50HS resin also showed that leached protein A and cell culture additive such as gentamicin were able to be removed under the isocratic overloaded condition. Lastly, a MAb purification process employing protein A affinity chromatography, isocratic overloaded cation exchange chromatography using Poros 50HS and anion exchange chromatography using QSFF in flow through mode was compared with the MAb's commercial manufacturing process, which consisted of protein A affinity chromatography, cation exchange chromatography using SPSFF in bind-elute mode and anion exchange chromatography using QSFF in flow through mode. Comparable step yield and impurity clearance were obtained by the two processes.     

A new general approach to purify proteins from complex mixtures

The selection of chromatography media and their sequential use represent a major difficulty to isolate a single protein from very crude protein extracts. The process described here consists of two main steps: (i) a rational selection of few media from a relatively large collection and (ii) the definition of the sequence of columns to get the best purity of the target protein. From the first step, one sorbent is selected for its properties to capture the protein to purify, regardless whether other protein impurities are also co-adsorbed; then 5-7 other complementary sorbents are identified to remove impurities but without interacting with the target protein under the same buffering conditions. The second step consists in superimposing sorbents under a cascade manner with the sorbent in charge to capture the target protein located in the last position. Non-adsorbed proteins are eliminated in the flowthrough; other impurities are progressively removed by the sorbent sequence and the target protein is finally desorbed and isolated from the last sorbent using an optimized gradient. All operations are performed with a single adsorption buffer for all columns and all monitoring performed by means of mass spectrometry associated with ProteinChip arrays and polyacrylamide gel electrophoresis. Examples of protein isolation/identification from human serum are described namely thyroxin-binding proteins and transferrin. The first is isolated thanks to a series of dye chromatography media, the second (transferrin) using current chromatographic media. In both cases the target proteins were purified at a level estimated of about 95% and 85%, respectively. Isolated proteins were pure enough for the purpose of formal identification by either peptide fingerprinting or sequencing.