Formation of transient highly-charged mAb clusters strengthens interactions with host cell proteins and results in poor clearance of host cell proteins by protein A chromatography.

Protein A chromatography with a high salt wash usually leads to robust clearance of host cell proteins (HCPs) in most recombinant monoclonal antibodies (mAbs), but a small subset of recalcitrant mAbs show significant HCP copurification. In this study, we carried out systematic studies using 4 different mAbs to explore the HCP copurification mechanism. HCP identification results revealed that the 3 high-HCP mAbs had many common HCPs which do not copurify with the low-HCP mAb, suggesting a similar mechanism is at play. Through wash evaluation, surface patch analysis, chain-swapping, domain evaluation, and structure-guided mutations, several charged residues in each mAb were found which correlated with HCP copurification. Surprisingly, these residues are also critical for self-association propensity. We observed an inverse correlation between diffusion interaction parameter and HCP copurification. Each of the high-HCP mAbs could form dynamic clusters consisting of 3∼6 mAb molecules. Therefore, a mAb cluster can exhibit higher net positive charges on the order of 3 to 6, compared with the individual mAb. In Protein A chromatography, high-HCP mAbs had elution tailing which contained high level of HCPs. Addition of Arginine-HCl or point mutations preventing cluster formation effectively reduced HCP copurification and elution tailing. Based on these results, we propose a novel HCP-copurification mechanism that formation of mAb clusters strengthens charge-charge interactions with HCPs and thus compromises HCP removal by Protein A chromatography. Besides arginine, histidine under acidic pH conditions prevented cluster formulation and resulted in effective HCP removal. Finally, structure-guided protein engineering and solution screening by using cluster size as indicator are useful tools for managing mAbs with high-HCP issues.

Role of configurational flexibility on the adsorption kinetics of bivalent bispecific antibodies on porous cation exchange resins.

The adsorption kinetics of a monoclonal antibody (mAb) used as a reference and of bivalent bispecific antibodies (BiSAb) on a macroporous cation exchanger is studied experimentally by examining the transient patterns of bound protein within the particles using confocal microscopy for a range of protein concentrations, buffer concentrations and pH, and temperatures. The mAb adsorption kinetics is controlled by pore diffusion and conforms to the classical shrinking core model. While the mAb adsorption rate increases with temperature, the ratio of effective and free solution diffusivity, De /D0, remains constant and has a value of 0.20. The BiSAb's structure is comprised of scFv domains that are genetically fused to a framework IgG through flexible peptide linkers which results in conformational flexibility leading to multiple binding forms with varying affinity for the adsorbent surface. As a result, adsorption of the BiSAbs shows complex patterns of total bound protein within the particles. These BiSAb adsorption patterns are influenced by buffer ionic strength, pH, and temperature in unique ways. Sharper intraparticle profiles are observed for conditions where the binding strength is greater (lower buffer concentration and/or pH) or when the protein is chemically crosslinked to restrict configurational flexibility. Temperature affects the BiSAb pore diffusivity as well as the interconversion kinetics. While the effects of temperature on BiSAb transport are also described by a constant De /D0 = 0.15, the temperature also affects the rate of interconversion between binding forms leading to faster equilibration at higher temperatures. A phenomenological model indicates that the interplay of pore diffusion and adsorption with the kinetically limited interconversion between binding forms is responsible for the experimental trends.

Chromatographic and adsorptive behavior of a bivalent bispecific antibody and associated fragments.

The elution and adsorptive behavior of a bivalent bispecific antibody (BiSAb), comprising an IgG1 framework with a scFv domain genetically fused to each heavy chain C-terminus via flexible linkers, and of two associated fragments were studied on two cation exchange chromatography media - ProPac WCX-10, which is pellicular and suitable for analytical use, and Nuvia HR-S, which is macroporous and suitable for preparative and process scale uses. Both fragments were identified by MS as missing one of the two scFv domains and its flexible linker, but one of them also contains an additional C-terminal lysine. The separation of these fragments on both resins occurs as a result of differences in non-specific ligand-protein interactions that are modulated by the salt concentration. For the ProPac WCX-10 column, complex, multipeak elution behaviors are observed, since, as a result of the linker flexibility, both the intact molecule and the fragments appear to exist in multiple binding configurations with each scFv domains either collapsed onto the IgG framework or extended away from it. With a residence time of 2.5 min and at 21 °C, two peak elution is observed for the fragments which contain a single linked scFv and three peak elution for the intact molecule which contains two linked scFvs. This behavior is affected by residence time, temperature, and hold time. Increasing the residence time to 25 min or increasing temperature to 40°C results in elution of a single, merged peak for each of the protein species. For Nuvia HR-S, the broader peaks, obtained as a result of mass transfer limitations, tend to obscure the multipeak elution behavior. Nevertheless, even for this resin, the effects of configurational flexibility are still manifested at the single-particle scale and affect the evolution of the patterns of protein binding within individual resin particles as evident from confocal microscopy observations.

Safety risk management for low molecular weight process-related impurities in monoclonal antibody therapeutics: Categorization, risk assessment, testing strategy, and process development with leveraging clearance potential.

Process-related impurities (PRIs) derived from manufacturing process should be minimized in final drug product. ICH Q3A provides a regulatory road map for PRIs but excludes biologic drugs like monoclonal antibodies (mAbs) that contain biological PRIs (e.g. host cell proteins and DNA) and low molecular weight (LMW) PRIs (e.g., fermentation media components and downstream chemical reagents). Risks from the former PRIs are typically addressed by routine tests to meet regulatory expectations, while a similar routine-testing strategy is unrealistic and unnecessary for LMW PRIs, and thus a risk-assessment-guided testing strategy is often utilized. In this report, we discuss a safety risk management strategy including categorization, risk assessment, testing strategy, and its integrations with other CMC development activities, as well as downstream clearance potentials. The clearance data from 28 mAbs successfully addressed safety concerns but did not fully reveal the process clearance potentials. Therefore, we carried out studies with 13 commonly seen LMW PRIs in a typical downstream process for mAbs. Generally, Protein A chromatography and cation exchange chromatography operating in bind-and-elute mode showed excellent clearances with greater than 1,000- and 100-fold clearance, respectively. The diafiltration step had better clearance (greater than 100-fold) for the positively and neutrally charged LMW PRIs than for the negatively charged or hydrophobic PRIs. We propose that a typical mAb downstream process provides an overall clearance of 5,000-fold. Additionally, the determined sieving coefficients will facilitate diafiltration process development. This report helps establish effective safety risk management and downstream process design with robust clearance for LMW PRIs.

Chromatographic behavior of bivalent bispecific antibodies on hydrophobic interaction chromatography columns.

The elution behavior of bivalent bispecific antibodies (BiSAb) comprising an immunoglobulin G framework genetically fused to a pair of single chain variable fragments (scFvs) was studied on hydrophobic interaction chromatography (HIC) columns using ammonium sulfate gradients. Each of the BiSAb molecules studied exhibited a three-peak elution behavior regardless of the location of scFv attachment to the framework IgG. Collecting and re-injecting each of the isolated peaks and eluting with the same gradient resulted in the same three-peak profile indicating that the behavior is reversible. Analogous behavior was observed for HIC resins with different functional ligands, matrix structures, and particle sizes. Residence time, operating temperature, and hold time were shown to affect the elution behavior. While three peaks were obtained at short residence times and room temperature, residence times longer than about 27 min or operating at 45 °C resulted in a single merged peak indicating that the underlying mechanism occurs on time scales comparable to that of chromatographic separation. Holding the protein on the resins prior to elution enriched the late eluting peak indicating that multiple binding states formed on the chromatographic surface are responsible for this behavior. Tryptophan auto-fluorescence measurements show that stronger binding forms have increased solvent exposure indicating that surface-catalyzed conformational changes play a role. A model was developed to describe the interplay of chromatographic separation and slow conformational changes.

Chromatographic behavior of bivalent bispecific antibodies on cation exchange columns. I. Experimental observations and phenomenological model.

The cation exchange chromatographic behavior of three homologous bivalent bispecific antibodies (BiSAb) is characterized for two different resins, Source 15S and ProPac WCX-10, having different base matrix, particle size, pore structure, and ligand chemistry. For both resins, elution with a salt gradient results in multiple peaks for each of the three BiSAb molecules at short residence times. The peaks gradually merge into two peaks and then into one peak eluting at intermediate salt concentrations when the residence time is gradually increased. Re-injecting fractions of each the individual peaks obtained at short residence time results in nearly the same multiple peak elution pattern. This behavior, which is contrary to the behavior normally encountered in ion exchange chromatography, appears to be related to the reversible, surface -catalyzed interconversion between different conformational states of each BiSAb that interact with different strength with the chromatographic surface. This behavior is qualitatively independent of pH in the range 5-8.5, protein load in the range 0.06-5.0 mg/ml, and gradient slope, and is not associated with the formation of aggregates. Gradually increasing temperature, however, reduces the multiple peak behavior eventually resulting into a single peak at 55 °C A phenomenological model is developed that predicts the experimental behavior over a broad range of conditions using fitted rate and equilibrium constants.

Chromatographic behavior of bivalent bispecific antibodies on cation exchange columns. II. Biomolecular perspectives.

In Part I of this work we determined the experimental cation exchange behavior of bivalent bispecific antibodies (BiSAb) comprising a pair of single chain variable fragment (scFv) domains flexibly linked to a framework immunoglobulin G (IgG), which exhibit a complex, three-peak elution pattern dependent on the residence time. A phenomenological model was developed assuming that the BiSAb molecules exist in multiple configurations that interact differently with the resin surface and interconvert at finite rates. In Part II of this work we provide relevant biomolecular perspectives that shed light on the underlying mechanisms. Firstly, we show that crosslinking the BiSAb molecules with a bifunctional reagent, which limits conformational flexibility, suppresses multiple peak elution. Secondly, we show that of the fragments obtained by enzymatic digestion of the BiSAb molecules only those that exhibit a pair of scFv domains show three-peak elution, while only two peaks are observed if a single scFv is present. Thirdly, we analyze the roles of electrostatic and hydrophobic surface properties of the BiSAb domains, identifying regions that are likely responsible for inter-domain and protein-surface interactions. The results demonstrate that the complex elution behavior catalyzed by the combination of surface charge and hydrophobicity of the stationary phase is associated with outstretched and collapsed configurations of the scFv domains relative to the framework IgG.

Process optimization and protein engineering mitigated manufacturing challenges of a monoclonal antibody with liquid-liquid phase separation issue by disrupting inter-molecule electrostatic interactions.

We report a case study in which liquid-liquid phase separation (LLPS) negatively impacted the downstream manufacturability of a therapeutic mAb. Process parameter optimization partially mitigated the LLPS, but limitations remained for large-scale manufacturing. Electrostatic interaction driven self-associations and the resulting formation of high-order complexes are established critical properties that led to LLPS. Through chain swapping substitutions with a well-behaved antibody and subsequent study of their solution behaviors, we found the self-association interactions between the light chains (LCs) of this mAb are responsible for the LLPS behavior. With the aid of in silico homology modeling and charged-patch analysis, seven charged residues in the LC complementarity-determining regions (CDRs) were selected for mutagenesis, then evaluated for self-association and LLPS properties. Two charged residues in the light chain (K30 and D50) were identified as the most significant to the LLPS behaviors and to the antigen-binding affinity. Four adjacent charged residues in the light chain (E49, K52, R53, and R92) also contributed to self-association, and thus to LLPS. Molecular engineering substitution of these charged residues with a neutral or oppositely-charged residue disrupted the electrostatic interactions. A double-mutation in CDR2 and CDR3 resulted in a variant that retained antigen-binding affinity and eliminated LLPS. This study demonstrates the critical nature of surface charged resides on LLPS, and highlights the applied power of in silico protein design when applied to improving physiochemical characteristics of therapeutic antibodies. Our study indicates that in silico design and effective protein engineering may be useful in the development of mAbs that encounter similar LLPS issues.

Cathepsin L Causes Proteolytic Cleavage of Chinese-Hamster-Ovary Cell Expressed Proteins During Processing and Storage: Identification, Characterization, and Mitigation.

A stochastic approach of copurification of the protease Cathepsin L that results in product fragmentation during purification processing and storage is presented. Cathepsin L was identified using mass spectroscopy, characterization of proteolytic activity, and comparison with fragmentation patterns observed using recombinant Cathepsin L. Cathepsin L existed in Chinese hamster ovary cell culture fluids obtained from cell lines expressing different products and cleaved a variety of recombinant proteins including monoclonal antibodies, antibody fragments, bispecific antibodies, and fusion proteins. Therefore, characterization its chromatographic behavior is essential to ensure robust manufacturing and sufficient shelf life. The chromatographic behaviors of Cathepsin L using a variety of techniques including affinity, cation exchange, anion exchange, and mixed mode chromatography were systematically evaluated. Our data demonstrates that copurification of Cathepsin L on nonaffinity modalities is principally because of similar retention on the stationary phase and not through interactions with product. Lastly, Cathespin L exhibits a broad elution profile in cation exchange chromatography (CEX) likely because of its different forms. Affinity purification is free of fragmentation issue, making affinity capture the best mitigation of Cathepsin L. When affinity purification is not feasible, a high pH wash on CEX can effectively remove Cathepsin L but resulted in significant product loss, while anion exchange chromatography operated in flow-through mode does not efficiently remove Cathepsin L. Mixed mode chromatography, using Capto™ adhere in this example, provides robust clearance over wide process parameter range (pH 7.7 ± 0.3 and 100 ± 50 mM NaCl), making it an ideal technique to clear Cathepsin L. © 2018 American Institute of Chemical Engineers Biotechnol. Prog., 35: e2732, 2019.

Evaluation of recent Protein A stationary phase innovations for capture of biotherapeutics.

We describe a comprehensive evaluation of 12 Protein A stationary phases for capture of biotherapeutics. We first examine the morphological properties of the stationary phases using a variety of orthogonal techniques including electron microscopy, particle sizing, pressure-flow behavior, and isocratic pulse response. A panel of nine proteins spanning a wide range of structures and biochemical properties was then used to assess equilibrium uptake, mass transport, dynamic binding capacity, and elution pH. Process performance and product quality were also examined under realistic bioprocess conditions using clarified mammalian cell culture broth. Equilibrium isotherms were found to be highly favorable, with equilibrium binding capacity for monoclonal and bispecific antibodies ranging from 47-100 mg/mL packed bed across all stationary phases tested. Effective pore diffusivities, De, were obtained by fitting the chromatography general rate model to breakthrough data. The fitted De values for monoclonal antibodies ranged from 1.1-5.7 × 10-8 cm2/s. The stationary phases had high dynamic binding capacities for the model proteins. The highest dynamic capacities for monoclonal and bispecific antibodies were seen with MabSelect SuRe pcc and MabSelect PrismA, which ranged from 58-74 mg/mL packed bed at 4 min residence times. Product capture using clarified cell culture broth as a feedstock showed high yields and elution pool volumes that ranged from 2-3 column volumes in most cases. Host cell protein, DNA, and aggregate levels in the elution pool were dependent on the specific nature of protein being purified, and levels were consistent between stationary phases. Lastly, we perform an analysis of bivariate correlations and discuss considerations for process design and optimization.

Separation of antibody monomer-dimer mixtures by frontal analysis.

The removal of aggregates, particularly soluble dimers, from monoclonal antibodies (mAbs) remains a persistent challenge in downstream processing. In this work, we have examined the separation of an antibody monomer from its dimer on the cation exchange resin Nuvia HR-S (Bio-Rad Laboratories) using frontal analysis. In this process, a mixture of monomer and dimer is continuously fed to the column under conditions where the mixture is favorably bound, resulting in two breakthrough fronts whose monomer and dimer compositions are determined by the multi-component equilibrium and kinetics of the system. Experimentally, the selectivity for dimer was found to vary substantially with ionic strength, being lowest when conditions favor the strongest binding, and increasing to a maximum at intermediate ionic strengths where rapid exchange with the bound monomer can occur. A mechanistic model is developed to describe the competitive binding frontal analysis process, assuming pore diffusion and a significant kinetic resistance to binding as a function of ionic strength. The model was solved numerically and was able to describe both the frontal analysis processes and batch adsorption experimental data, accounting for process parameters such as feed composition and salt concentration. The resulting model can be used to optimize column operating conditions for yield and purity.

Camelid VH H affinity ligands enable separation of closely related biopharmaceuticals.

Interest in new and diverse classes of molecules such as recombinant toxins, enzymes, and blood factors continues to grow for use a biotherapeutics. Compared to monoclonal antibodies, these novel drugs typically lack a commercially available affinity chromatography option, which leads to greater process complexity, longer development timelines, and poor platformability. To date, for both monoclonal antibodies and novel molecules, affinity chromatography has been mostly reserved for separation of process-related impurities such as host cell proteins and DNA. Reports of affinity purification of closely related product variants and modified forms are much rarer. In this work we describe custom affinity chromatography development using camelid VH H antibody fragments as "tunable" immunoaffinity ligands for separation of product-related impurities. One example demonstrates high selectivity for a recombinant immunotoxin where no binding was observed for an undesired deamidated species. Also discussed is affinity purification of a coagulation factor through specific recognition of the gamma-carboxylglutamic acid domain.

Adsorption equilibrium and kinetics of monomer-dimer monoclonal antibody mixtures on a cation exchange resin.

Adsorption equilibrium and kinetics are determined for a monoclonal antibody (mAb) monomer and dimer species, individually and in mixtures, on a macroporous cation exchange resin both under the dilute limit of salt gradient elution chromatography and at high protein loads and low salt based on batch adsorption equilibrium and confocal laser scanning microscopy (CLSM) experiments. In the dilute limit and weak binding conditions, the dimer/monomer selectivity in 10mM phosphate at pH 7 varies between 8.7 and 2.3 decreasing with salt concentration in the range of 170-230mM NaCl. At high protein loads and strong binding conditions (0-60mM NaCl), the selectivity in the same buffer is near unity with no NaCl added, but increases gradually with salt concentration reaching high values between 2 and 15 with 60mM added NaCl. For these conditions, the two-component adsorption kinetics is controlled by pore diffusion and is predicted approximately by a dual shrinking core model using parameters based on single component equilibrium and kinetics measurements.

Engineering of novel Staphylococcal Protein A ligands to enable milder elution pH and high dynamic binding capacity.

We describe novel Staphylococcal Protein A ligands that enable milder elution pH for use in affinity chromatography. The change in elution pH is the result of point mutations to the protein sequence. Two novel ligands are investigated in this study. The first, designated Z(H18S)4, represents a histidine to serine substitution single mutation. The second, designated Z(H18S, N28A)4, is a double mutant comprising histidine to serine and asparagine to alanine mutations. Both are compared against the unmutated sequence, designated Z4, which is currently utilized in a commercially available Protein A stationary phase for the purification of molecules containing Fc domains. The ligands are coupled to a chromatography support matrix and tested against a panel of antibodies and an Fc fusion protein for elution pH, dynamic binding capacity, step-wise elution, and capture from clarified culture media. Results demonstrate that the novel ligands result in milder elution pH, on average >0.5 pH units, when tested in a pH gradient. For step-wise elution at pH 4.0, the Z(H18S, N28A)4 ligand showed on average a greater than 30% increase in yield compared to Z4. Importantly, for the antibodies tested the mutations did not result in a decrease in dynamic binding capacity or other desirable attributes such as selectivity. A potential application of the novel ligands is shown with a pH sensitive molecule prone to aggregation under acidic conditions.

Development and scale-up of a commercial fed batch refolding process for an anti-CD22 two chain immunotoxin.

We describe the development and scale-up of a novel two chain immunotoxin refolding process. This work provides a case study comparing a clinical manufacturing process and the commercial process developed to replace it. While the clinical process produced high quality material, it suffered from low yield and high yield variability. A systematic approach to process development and understanding led to a number of improvements that were implemented in the commercial process. These include a shorter inclusion body recovery process, limiting the formation of an undesired deamidated species and the implementation of fed batch dilution refolding for increased refold titers. The use of a combination of urea, arginine and DTT for capture column cleaning restored the binding capacity of the capture step column and resulted in consistent capture step yields compared to the clinical process. Scalability is shown with data from 250 L and 950 L scale refolding processes. Compared to the clinical process it replaces, the commercial process demonstrated a greater than fivefold improvement in volumetric productivity at the 950 L refolding scale.

Process-scale purification and analytical characterization of highly gamma-carboxylated recombinant human prothrombin.

Prothrombin (coagulation Factor II) is a complex multidomain glycoprotein that plays a central role in blood coagulation. It is the zymogen precursor to the protease thrombin that catalyzes the formation of the fibrin clot and regulates a multitude of other cellular responses related to coagulation and hemostasis. For the biological activity of prothrombin, the vitamin K dependent posttranslational modification of glutamic acid residues to gamma-carboxylglutamic acid is of crucial importance. Prothrombin can be recombinantly expressed using mammalian cell culture. However, the product is a heterogeneous mixture of variants with different degrees of carboxylation, requiring separation of closely related charge isoforms. A second challenge for purification is the need to remove traces of the product-related impurity thrombin, a protease, to extremely low levels. In this work, we describe a purification strategy that provides solutions to both challenges and results in an efficient and robust process for active recombinant prothrombin. We also describe the analytical characterization of recombinant prothrombin by HPLC, LC-MS/MS, and complementary biochemical assays.

Binding and elution behavior of proteins on strong cation exchangers.

This work provides a broad survey of binding and elution behavior of proteins on strong cation exchangers. Four proteins comprising two monoclonal antibodies, lysozyme, and cytochrome c were used as models in the investigation. Seven chromatography resins with different base matrices were compared. Dynamic binding capacity as a function of salt concentration was examined for a monoclonal antibody and lysozyme. Elution behavior as a function of gradient slope was modeled to determine the characteristic charge, essentially a measure of the number of sites involved in binding, for each protein on each resin. Trends with respect to dynamic binding capacity and elution behavior are analyzed and discussed.

Comparison of agarose and dextran-grafted agarose strong ion exchangers for the separation of protein aggregates.

The control of aggregate levels in recombinant protein based drugs is a primary concern during process development and manufacture. In recent years, a novel class of dextran-grafted ion exchange matrices has gained popularity for process scale protein purification due to increased mass transfer rates and higher dynamic binding capacity compared to conventional matrices. Using bovine serum albumin and a monoclonal antibody as model proteins, we studied Sepharose FF and Sepharose XL ion exchangers for the separation of protein aggregates. Experimental results comparing linear gradient elution, stepwise elution, and flow-through chromatography for aggregate separation are described. Differences in performance for the various ion exchangers are discussed and modeled. Strategies for the optimization of protein aggregate separation are provided.

Protein separations with induced pH gradients using cation-exchange chromatographic columns containing weak acid groups.

The behavior of chromatographic columns packed with resins containing both weak and strong cation-exchange groups is investigated in order to obtain protein separations by means of internally generated pH gradients in response to step changes in buffer composition. A local equilibrium model is developed to predict pH transitions using non-adsorbed buffers, i.e. containing neutral and negatively charged buffering species, based exclusively on the resin titration curve. In agreement with experimental results, the model predicts practical, fairly linear gradients between pH 5 and 7, which are formed using suitable mixtures of acetate and phosphate buffers. The separation of mixtures of ovalbumin, albumin, and transferrin is used as a model system, but, unlike most previous work, we consider preparative conditions. Near baseline resolution is obtained with protein loads as high as 10mg/mL and mobile phase velocities at high as 460 cm/h using porous, 70-microm diameter particles. The peaks obtained with this approach are much sharper than could be obtained isocratically or using externally generated, unretained gradients as a result of the peak compression caused by the axial pH gradient formed along the column. Moreover, separation is obtained at very low ionic strengths (2-3 mS/cm). The effects of flow velocity, mobile phase composition, time of injection, and protein load on retention and elution pH are investigated systematically demonstrating a range of ways in which the separation can be controlled and optimized.

Separation of protein charge variants with induced pH gradients using anion exchange chromatographic columns.

This work concerns the chromatographic separation of protein charge variants using pH gradients generated by step changes in buffer composition with weak base anion exchange columns. A local equilibrium model is first developed to describe pH transitions occurring in the column using buffers comprising neutral, zwitterionic or positively charged species. Model predictions, based solely on the resins' titration curves and obtained with the method of characteristics, show, in excellent agreement with experiments, that induced pH gradients of varying durations and shapes can be obtained with a broad range of buffer systems including Tris, Bis-Tris propane, histidine, and their mixtures and ethanolamine. The separation of protein charge variants is then demonstrated for bovine apo-transferrin and for a monoclonal antibody. The resolution of the charge variants present in these proteins, demonstrated via isoelectric focusing analyses, is obtained for conditions amenable to scale-up for preparative purposes; that is larger particle sizes (90 mum), higher flow rates (100-600 cm/h), and higher protein loads (2-5 mg/mL). Because the approach requires only step changes in buffer composition and commonly available, unretained buffers species, practical implementation is straightforward. The focusing effect of the induced pH gradient results in relatively sharp peaks and substantial resolution even for these conditions.