Dispersion effects in preparative polymethacrylate monoliths operated in radial-flow columns

Monolithic media have found widespread use as excellent tools for fast analytical separations of small molecules, proteins, pDNA and viruses. Polymethacrylate monoliths with large channels are attractive for capturing large molecules, like immunoglobulins, DNA, and viruses. For preparative purposes, these monoliths are operated in radial flow mode. Band spreading in monoliths is extremely low and mostly dominated by the contribution of extra column effects. The model used here had a single axial dispersion coefficient which lumps together extra column effects and the intrinsic band spreading of the monolithic material to characterize the adsorption of proteins and pDNA on polymethacrylate ion-exchange monoliths. Due to the fact that the performance of the monolith was unaffected by the velocity within the applied range, and due to highly favourable adsorption isotherms, a constant pattern model could be applied to predict preparative runs on radial flow units assuming axial flow for modelling.     

Experimental characterization and modelling of analytical monolithic column

Hydrodynamics, equilibrium and kinetics of adsorption in a silica-based monolithic column Chromolith Performance RP-18e (Merck KgaA, Germany) have been studied. The column permeability was calculated according to the Darcy law for laminar flow. The efficiency of the monolithic column was characterized through the height equivalent to a theoretical plate (HETP) for myoglobin, phenol and progesterone. The 2-D single channel mathematical model has been applied to describe the adsorption dynamics. Parabolic velocity profile, axial and radial diffusion in the monolith channel, linear driving force model for the mass transfer in the monolith channel skeleton wall and linear adsorption equilibrium were assumed. The mathematical model gives good prediction of the experimental elution peaks.     

Experimental characterization and modelling of analytical monolithic column

Hydrodynamics, equilibrium and kinetics of adsorption in a silica-based monolithic column Chromolith Performance RP-18e (Merck KgaA, Germany) have been studied. The column permeability was calculated according to the Darcy law for laminar flow. The efficiency of the monolithic column was characterized through the height equivalent to a theoretical plate (HETP) for myoglobin, phenol and progesterone. The 2-D single channel mathematical model has been applied to describe the adsorption dynamics. Parabolic velocity profile, axial and radial diffusion in the monolith channel, linear driving force model for the mass transfer in the monolith channel skeleton wall and linear adsorption equilibrium were assumed. The mathematical model gives good prediction of the experimental elution peaks.     

Chromatography of hen egg-white proteins on anion-exchange cellulose at high flow rates using a radial flow column.

The influence of column configuration on the separation of hen egg-white proteins using Whatman DE52 and QA52 anion-exchange cellulose has been investigated. Using a 100 ml volume axial flow column (6.6 cm x 4.4 cm i.d.) we achieved flow rates of up to 25 ml/min i.e. 15 bed volumes/h after which higher flow was restricted due to pressure constraints within the system. Under radial flow conditions using a 100 ml column flow rates of up to 150 ml/min i.e. 90 bed volumes/h were achieved using DE52 and QA52. While chromatographic resolution was superior under axial flow at the lower flow rates excellent resolution was maintained at up to 150 ml/min using the radial flow column. This is a consequence of the fast kinetics of adsorption/desorption exhibited by DE52 and QA52. The data indicate that it is the column configuration and not the cellulose matrix which influences flow performance.     

Zonal rate model for axial and radial flow membrane chromatography. Part I: Knowledge transfer across operating conditions and scales

The zonal rate model (ZRM) has previously been applied for analyzing the performance of axial flow membrane chromatography capsules by independently determining the impacts of flow and binding related non‐idealities on measured breakthrough curves. In the present study, the ZRM is extended to radial flow configurations, which are commonly used at larger scales. The axial flow XT5 capsule and the radial flow XT140 capsule from Pall are rigorously analyzed under binding and non‐binding conditions with bovine serum albumin (BSA) as test molecule. The binding data of this molecule is much better reproduced by the spreading model, which hypothesizes different binding orientations, than by the well‐known Langmuir model. Moreover, a revised cleaning protocol with NaCl instead of NaOH and minimizing the storage time has been identified as most critical for quantitatively reproducing the measured breakthrough curves. The internal geometry of both capsules is visualized by magnetic resonance imaging (MRI). The flow in the external hold‐up volumes of the XT140 capsule was found to be more homogeneous as in the previously studied XT5 capsule. An attempt for model‐based scale‐up was apparently impeded by irregular pleat structures in the used XT140 capsule, which might lead to local variations in the linear velocity through the membrane stack. However, the presented approach is universal and can be applied to different capsules. The ZRM is shown to potentially help save valuable material and time, as the experiments required for model calibration are much cheaper than the predicted large‐scale experiment at binding conditions. Biotechnol. Bioeng. 2013; 110: 1129–1141. © 2012 Wiley Periodicals, Inc.     

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

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

Use of ceramic monoliths as stationary phase in affinity chromatography

The use of coated ceramic monoliths as support for affinity chromatography is described. Ceramic monoliths are robust active matrix supports and present a very small pressure drop. Monoliths are coated with a very thin agarose gel layer and activated using a standard activation process for agarose beads. Experiments demonstrate that enzyme adsorption occurs exclusively on the outside surface of the agarose coating since enzyme molecules are too large to fit into the porous matrix. Adsorption and desorption rates are large and production of enzyme per unit monolith volume justifies further exploring this separation process for large throughput operation.     

Adsorptive purification of pDNA on superporous rigid cross-linked cellulose matrix

Use of plasmid DNA (pDNA) in the emerging gene therapy requires pure DNA in large quantities requiring production of safe DNA on large scale. While a number of kit-based DNA purification techniques have become popular, large scale cost effective purification of DNA remains a technological challenge. Most traditional, as well as newly developed methods for DNA purification are expensive, tedious, use toxic reagents, and/or generally not amenable for scaled up production. Our attempts to develop a scalable adsorptive separation technology resulted in successful use of indigenously developed rigid cross-linked cellulose beads for single step purification of pDNA from alkaline cell lysates. This mode of purification employs a combination of intra-particle interactions that could give a product plasmid DNA free from chromosomal DNA, RNA and host proteins in a single scalable chromatographic step. The technology can be employed as a batch adsorption step on small scale, or on a large scale column chromatography. A high copy number 9.8 kb plasmid (from an Escherichia coli strain) was purified in yields of 77 and 52%, respectively in batch and column modes. The product obtained was homogeneous supercoiled plasmid with no RNA and protein contamination confirmed by quantitative analysis, agarose gel electrophoresis and SDS-PAGE.     

New system for preparative electrochromatography of proteins

Electrochromatography employs an axial electric field across a chromatographic stationary phase to separate proteins and other molecules based on differences in electrophoretic mobility. Because the separation is electrically driven, the need for additional chemical reagents is reduced. Two major impediments to scale-up of electrochromatography columns, removal of heat and electrolysis gases, have historically limited the diameter of packed columns to 2.5 cm ID with volumes of approximately 55 mL. We report a novel electrochromatography column that effectively removes electrolysis gases and minimizes heating. A vital component of this system is a new electrode design that couples a platinum gauze with an ultrafiltration membrane across both ends of the column. Use of a methacrylate base stationary phase enabled axial voltage gradients of 10 to 20 V/cm. Thermocouples inserted radially in the column at four axial positions showed that the flow of a 4 degrees C mobile phase coupled with heat conduction through the column walls controlled the temperature to 28 degrees C. The new column design, with dimensions of 3.81 cm ID x 38.1 cm long and bed volume of 400 mL, was demonstrated by separating mixtures of BSA and myoglobin. The column was operated in a horizontal position with radial sample injection and withdrawal at the ends of the packed bed. These experiments are a first step in demonstrating that scale-up of electrochromatography columns can be achieved by choosing appropriate flow rates, voltage gradients, and stationary phase.     

Modeling of scale-down effects on the hydrodynamics of expanded bed adsorption columns

Expanded-bed adsorption (EBA) is a technique for primary recovery of proteins starting from unclarified broths. This process combines centrifugation, concentration, filtration, and initial capturing of the proteins in a single step. An expanded bed (EB) is comparable to a packed bed in terms of separation performance but its hydrodynamics are that of a fluidized bed. Downstream process development involving EBA is normally carried out in small columns to minimize time and costs. Our purpose here is to characterize the hydrodynamics of expanded beds of different diameters, to develop scaling parameters that can be reliably used to predict separation efficiency of larger EBA columns. A hydrodynamic model has been developed which takes into account the radial liquid velocity profile in the column. The scale-down effect can be characterized in terms of apparent axial dispersion, D(axl,app), and plate number, N(EB), adapted for expanded bed. The model is in good agreement with experimental results obtained from 1- and 5-cm column diameters with buffer solutions of different viscosities. The model and the experiments show an increase of apparent axial dispersion with an increase in column diameter. Furthermore, the apparent axial dispersion is affected by an increase in liquid velocity and viscosity. Supported by visual observations and predictions from the model, it was concluded that operating conditions (liquid viscosity and superficial velocity) resulting in a bed-void fraction between 0.7 and 0.75 would provide the optimal separation efficiency in terms of N(EB).     

Toward a robust model of packing and scale-up for chromatographic beds. 1. Mechanical compression

The packing of compressible biochromatographic resins at large scale suffers from a poor understanding of how column packing method, resin properties, and column geometry impact column performance. To improve understanding, we develop and evaluate a one-dimensional, continuum mechanics model of column packing by mechanical compression. We show that the model can quantitatively predict the change in bed height, applied stress, and internal axial porosity profile without adjustable parameters when the modulus and wall friction coefficients are determined independently. The model possesses theoretical relationships for wall support and resin rigidity that should enable it to describe the mechanical compression of any biochromatographic resin for any column diameter. Moreover, this framework could provide a path to analogous models for flow packing and dynamic axial compression.     

Morphological analysis of tumor cell/endothelial cell interactions under shear flow

In the process of hematogenous cancer metastasis, tumor cells (TCs) must shed into the blood stream, survive in the blood circulation, migrate through the vascular endothelium (extravasation) and proliferate in the target organs. However, the precise mechanisms by which TCs penetrate the endothelial cell (EC) junctions remain one of the least understood aspects of TC extravasation. This question has generally been addressed under static conditions, despite the important role of flow induced mechanical stress on the circulating cell-endothelium interactions. Moreover, flow studies were generally focused on transient or firm adhesion steps of TC-EC interactions and did not consider TCs spreading or extravasation. In this paper, we used a parallel-plate flow chamber to investigate TC-EC interactions under flow conditions. An EC monolayer was cultured on the lower plate of the flow chamber to model the endothelial barrier. Circulating TCs were introduced into the flow channel under a well-defined flow field and TC cell shape changes on the EC monolayer were followed in vitro with live phase contrast and fluorescence microscopy. Two spreading patterns were observed: radial spreading which corresponds to TC extravasation, and axial spreading where TCs formed a mosaic TC-EC monolayer. By investigating the changes in area and minor/major aspect ratio, we have established a simple quantitative basis for comparing spreading modes under various shear stresses. Contrary to radial spreading, the extent of axial spreading was increased by shear stress.     

High-performance affinity chromatography with immobilization of protein A and L-histidine on molded monolith

Reactive monoliths of macroporous poly(glycidyl methacrylate-co-ethylene dimethacrylate) have been prepared by "in-situ" copolymerization of the monomers in the presence of porogenic diluents. Protein A and L-histidine were immobilized on the monoliths directly or through a spacer arm, respectively. The properties of these two kinds of affinity columns were characterized, and the results showed that the columns with coupling of ligands by a spacer arm have some extent of non-specific adsorption for bovine serum albumin. The affinity column based on the monolithic polymer support provided us with good hydrodynamic characteristic, low flow resistance, and easy preparation. These two affinity columns were used for the purification of immunoglobulin G from human serum. The purity of the purified IgG was detected by matrix-assisted laser desorption ionization time-of-flight mass spectrometry (MALDI-TOF-MS). The stability of the protein A affinity column was investigated, and its performance remained invariable after half a year. The effects of the nature and the pH of the buffer system on the adsorption capacity of human IgG on histidyl affinity column were also investigated. The protein A affinity column is favorable for rapid analysis of human IgG samples. In contrast, the advantages of mild elution conditions, high stability, as well as low cost provide the histidyl column further potential possibility for fast removal of IgG from human plasma in clinical applications.     

Breakthrough performance of plasmid DNA on ion-exchange membrane columns

Breakthrough performance of plasmid DNA adsorption on ion-exchange membrane columns was theoretically and experimentally investigated using batch and fixed-bed systems. System dispersion curves showed the absence of flow non-idealities in the experimental arrangement. Breakthrough curves (BTC) were significantly affected by inlet flow rate and solute concentration. In the theoretical analysis, a model was integrated by the serial coupling of the membrane transport model and the system dispersion model. A transport model that considers finite kinetic rate and column dispersed flow was used in the study. A simplex optimization routine, coupled to the solution of the partial differential model equations, was employed to estimate the maximum adsorption capacity constant, the equilibrium desorption constant, and the forward interaction rate constant, which are the parameters of the membrane transport model. The analysis shows that as inlet concentration or flow rate increases, the deviation of the model from the experimental behavior decreases. The BTCs displacement as inlet concentration increases was explained in terms of a greater degree of column saturation reached and more efficient operation accomplished. The degree of column saturation was not influenced by inlet flow rate. It was necessary to consider in the column model the slight variation in the BTC produced by the axial dispersion, in order to accomplish the experimental curve dispersion. Consequently, the design criteria that for Pe > 40 the column axial dispersion can be neglected should be taken with precaution.     

Chromatography of human prothrombin from Nitschmann fraction III on Q Sepharose Fast Flow using axial and radial flow column

An axial column (Hitrap Q 5 ml, 2.5 2 1.6 cm) and a radial flow column (3.5 2 5 cm) packed with Q Sepharose Fast Flow media had been evaluated for the separation of human prothrombin. Nitschmann fraction III dissolved in buffered saline (0.10 M sodium chloride buffered with 0.06 M Tris/HCl to pH 7.5) was the starting material. Effects of sample flow rate of the two columns were screened. Under radial flow conditions using the radial column, sample flow rate up to 15 ml/min (i.e. 18 bed volumes/h) was achieved and the operating pressure was below 0.2 MPa eventhough the elution velocity was 30 ml/min. Breakthrough capacity was determined by analyzing the total protein and prothrombin activity of the target protein-containing fraction under subsaturating conditions and both columns had almost the same breakthrough capacity per ml media, indicating that the sample loading was independent of radial column geometry. It was concluded that the radial column is an attractive alternate to traditional axial packed bed column, exhibiting very good potential for use in the separation of human prothrombin.     

Virus-binding proteins recovered from bacterial culture derived from activated sludge by affinity chromatography assay using a viral capsid peptide

The contamination of water environments by pathogenic viruses has raised concerns about outbreaks of viral infectious diseases in our society. Because conventional water and wastewater treatment systems are not effective enough to inactivate or remove pathogenic viruses, a new technology for virus removal needs to be developed. In this study, the virus-binding proteins (VBPs) in a bacterial culture derived from activated sludge were successfully recovered. The recovery of VBPs was achieved by applying extracted crude proteins from a bacterial culture to an affinity column in which a custom-made peptide of capsid protein from the poliovirus type 1 (PV1) Mahoney strain (H(2)N-DNPASTTNKDKL-COOH) was immobilized as a ligand. VBPs exhibited the ability to adsorb infectious particles of PV1 Sabin 1 as determined by enzyme-linked immunosorbent assay. The evaluation of surface charges of VBPs with ion-exchange chromatography found that a majority of VBP molecules had a net negative charge under the conditions of affinity chromatography. On the other hand, a calculated isoelectric point implied that the viral peptide in the affinity column was also charged negatively. As a result, the adsorption of the VBPs to the viral peptide in the affinity column occurred with a strong attractive force that was able to overcome the electrostatic repulsive force. Two-dimensional electrophoresis revealed that the isolated VBPs include a number of proteins, and their molecular masses were widely distributed but smaller than 100 kDa. Amino acid sequences of N termini of five VBPs were determined. Homology searches for the N termini against all protein sequences in the National Center for Biotechnology Information (NCBI) database showed that the isolated VBPs in this study were newly discovered proteins. These VBPs that originated with bacteria in activated sludge might be stable, because they are existing in the environment of wastewater treatments. Therefore, a virus removal technology utilizing VBPs as viral adsorbents can be developed, since it is possible to replicate VBPs by protein cloning techniques.     

Virus-Binding Proteins Recovered from Bacterial Culture Derived from Activated Sludge by Affinity Chromatography Assay Using a Viral Capsid Peptide

The contamination of water environments by pathogenic viruses has raised concerns about outbreaks of viral infectious diseases in our society. Because conventional water and wastewater treatment systems are not effective enough to inactivate or remove pathogenic viruses, a new technology for virus removal needs to be developed. In this study, the virus-binding proteins (VBPs) in a bacterial culture derived from activated sludge were successfully recovered. The recovery of VBPs was achieved by applying extracted crude proteins from a bacterial culture to an affinity column in which a custom-made peptide of capsid protein from the poliovirus type 1 (PV1) Mahoney strain (H₂N-DNPASTTNKDKL-COOH) was immobilized as a ligand. VBPs exhibited the ability to adsorb infectious particles of PV1 Sabin 1 as determined by enzyme-linked immunosorbent assay. The evaluation of surface charges of VBPs with ion-exchange chromatography found that a majority of VBP molecules had a net negative charge under the conditions of affinity chromatography. On the other hand, a calculated isoelectric point implied that the viral peptide in the affinity column was also charged negatively. As a result, the adsorption of the VBPs to the viral peptide in the affinity column occurred with a strong attractive force that was able to overcome the electrostatic repulsive force. Two-dimensional electrophoresis revealed that the isolated VBPs include a number of proteins, and their molecular masses were widely distributed but smaller than 100 kDa. Amino acid sequences of N termini of five VBPs were determined. Homology searches for the N termini against all protein sequences in the National Center for Biotechnology Information (NCBI) database showed that the isolated VBPs in this study were newly discovered proteins. These VBPs that originated with bacteria in activated sludge might be stable, because they are existing in the environment of wastewater treatments. Therefore, a virus removal technology utilizing VBPs as viral adsorbents can be developed, since it is possible to replicate VBPs by protein cloning techniques.     

The variance of the distribution of traversal times in a capillary bed

A random walk model of capillary tracer transit times is developed that treats simulataneously: plug flow in the capillary, radial and axial diffusion in the capillary cylinder and tissue annulus, and endothelial barriers to solute transport. The mean transit time is simply the volume of distribution divided by blood flow. Variance of transit times has additive terms for radial, axial, and barrier influences that are reduceable to variances of simpler models of capillary exchange. The dependence of variance on the solute diffusion coefficient is not monotonic, but has a minimum near 0·5 × 10?6 cm²/s for reasonable parameters and no barrier, Small molecules like inert gases are expected to have larger variances with higher diffusion coefficients, while larger molecules and barrier limited solutes will have the reverse dependence. Available literature data indicates that capillary heterogeneity will have a major influence on whole-body variance of transit times.     

Isolation of potato proteins using simulated moving bed technology

The simulated moving bed (SMB) concept of chromatography was applied to treat potato juice from production of starch. The aim was to harvest proteins. SMB offers possibilities to operate with different process strategies and in this study it was shown possible to harvest up to 80% of the protein in a process utilizing very little extra water besides that already present in the juice. After depleting protein from the juice in the adsorption step, the flow through was used to recondition the column after elution. The present study illustrates a new concept of applying chromatography as a capturing step of bulk products.     

Experimental measurement of particle size distribution and voidage in an expanded bed adsorption system

This paper presents an experimental analysis of matrix bead size distribution and voidage variations with axial height in an expanded bed adsorption system. Use of a specially constructed expanded bed with side ports has enabled sampling from within the expanded bed along the vertical axis. Particles removed from within the bed were measured for their size distributions. Residence time distribution studies were used to estimate bed voidage. Measurements of axial and radial particle size distributions and axial voidage distribution have been made at different flow rates. Particle size was found to be radially constant, indicating constant stratification in the column. The particle size was found to decrease with increasing axial height. Voidage increased with axial height from a settled bed value of 0.39 to approaching unity for high liquid velocities and increased at a constant axial position with increased flowrate. This information provides key insight into bed stability and data for the improved modeling of this important unit operation.