Visualizing two-component protein diffusion in porous adsorbents by confocal scanning laser microscopy.

The use of confocal scanning laser microscopy (CSLM) has recently been described for the visualization of intraparticle protein profiles during single-protein finite bath uptake experiments. By coupling of fluorescent molecules to proteins the penetration of porous media by labeled macromolecules could be detected by scanning single adsorbent particles for fluorescence emission after laser excitation. Thus the internal protein distribution profile, which is a central element in modeling of protein transport in porous adsorbents, became experimentally accessible. Results from the simultaneous visualization of two proteins by this technology are shown here. The use of two different fluorescent dyes for protein labeling and two independent detectors in the CSLM allowed for the first time ever the direct observation of a two-component diffusion process within a porous stationary phase. The finite bath uptake of human immunoglobulin G (hIgG) and bovine serum albumin (BSA) to two different ion exchange adsorbents (SP Sepharose Fast Flow and Source 30S) and to an affinity adsorbent (Protein A Sepharose) was measured using Cy5 and Oregon Green as labels. Single adsorbent particles were scanned for intensity distribution of fluorescence emission from the two fluorophors. The intraparticle profiles obtained from the confocal images were translated into a relative protein concentration thus allowing the calculation of protein uptake kinetics from direct measurement in the stationary phase. The confocal technique may prove to be a very powerful means of data generation for modeling of multi-component mass transfer phenomena in protein adsorption.     

Kinetic study of the concentration dependence of the mass transfer rate coefficient in anion-exchange chromatography of bovine serum albumin.

The experimental results of a previous study of the mass transfer kinetics of bovine serum albumin (BSA) in ion-exchange chromatography under nonlinear conditions are reevaluated. The analysis of the concentration dependence of the lumped mass-transfer rate coefficient (k(m,L)) provides information on the kinetics of axial dispersion, fluid-to-particle mass transfer, intraparticle mass transfer, and adsorption/desorption. The new analysis shows that the contribution of intraparticle mass transfer is the dominant one. Similar to k(m,L), the surface diffusivity (D(s)) of BSA increases with increasing concentration. The linear concentration dependence of k(m,L) seems to originate in a similar dependence of D(s). The use of an heterogeneous-surface model for the anion-exchange resin provides an explanation of the positive concentration dependence of D(s). This work illustrates how frontal analysis data can be used for a detailed investigation of the kinetics of mass transfer between the phases of a chromatographic column, in addition to its conventional use in the determination of the thermodynamic characteristics of the phase equilibrium.     

Expanded and packed bed albumin adsorption on fluoride modified zirconia

The expanded bed characteristics of 75-103microm fluoride-modified zirconia (FmZr) particles synthesized by a fed batch oil emulsion process were investigated. These particles are distinguished from commercially available expanded-bed adsorbents by virtue of their high density (2.8 g/cc) and the mixed mode protein retention mechanism which allows for the retention of both cationic and anionic proteins. The linear velocity versus bed porosity data agree with the Richardson-Zaki relationship with the terminal velocity in infinite medium of 2858.4 cm/h and a bed expansion index of 5.1. Residence time distribution (RTD) studies and bovine serum albumin (BSA) adsorption studies were performed as a function of the height of the settled bed to the column diameter (H:D) ratio and degree of bed expansion with superficial velocities of 440 to 870 cm/h. The settled bed, a 2x expanded bed, and a 3x expanded bed were studied for the H:D ratios of 1:1, 2:1, and 3:1. The dynamic binding capacity (DBC) at 5% breakthrough was low (2-8 mg BSA/mL settled bed) and was independent of the H:D ratio or the degree of bed expansion. The saturation DBC was 32.3 +/- 7.0 mg BSA/mL settled bed. The adsorption-desorption kinetics and intraparticle diffusion for protein adsorption on FmZr (38-75 micrometer) were investigated by studying the packed bed RTD and BSA adsorption as a function of temperature and flow rate. The data show that the adsorption-desorption kinetics along with intraparticle diffusion significantly influence protein adsorption on FmZr. Low residence times ( approximately 0.8 min) of BSA result in a DBC at 5% breakthrough which is 3.5-fold lower compared to that at 6-fold higher protein residence time. At low linear velocity (45 cm/h) the breakthrough curve is nearly symmetrical and becomes asymmetrical and more dispersed at higher linear velocity (270 cm/h) due to the influence of slow adsorption-desorption kinetics and intraparticle diffusion.Copyright 1998 John Wiley & Sons, Inc. Bioeng 60: 333-340, 1998.     

Adsorption kinetics and equilibria of bovine serum albumin on rigid ion-exchange and hydrophobic interaction chromatography matrices in a stirred cell

Rigid adsorbents have advantages over soft gel media for downstream processing of proteins. The adsorption of bovine serum albumin (BSA) has been investigated on a rigid adsorbent based on a wide-pore, hydrophilically coated, silica-gel matrix. The effects of surface chemistry (weak anion exchanger and hydrophobic interaction chromatography) and particle size have been studied on the physical properties of the adsorbent and on the adsorption equilibria and adsorption kinetics. The rates of adsorption of BSA have been measured in a stirred cell and are found to be satisfactorily described by a two-step theoretical model, in which the mass transfer involves a pore diffusion resistance and an extra-particle film resistance. On the anion exchanger, the effective pore diffusivity decreases substantially with increasing protein concentration, approximately halving as the initial concentration rises from 0.7 to 2g/l. In the hydrophobic interaction chromatography medium, the pore diffusivity is less sensitive to protein concentration and is also reduced by a factor of about 4 by aggregation of the protein. Effective pore diffusivities with the "wide-pore" silica adsorbents in anion-exchange form are 36-94 times lower than the diffusivity in free solution and are comparable with the lower of the wide range of values published for soft gels.     

Characterization of very dense mineral oxide–gel composites for fluidized-bed adsorption of biomolecules

Efficient design of fluidized-bed biomolecule adsorption from crude feed stock requires particles with elevated density, large adsorption capacity and broad chemical stability. Moreover, combinations of small particle diameters with high densities allow for high fluidization velocities while preserving a rapid mass transfer.This approach has been implemented by combining stable porous mineral oxide of high density (2.2, 4.7, 5.7, 9.4 g/ml) with functionalized hydrogels. The cross-linked hydrogel derivative fills the internal porosity of the beads and provides a high equilibrium binding capacity.Various porous mineral oxides (silica, titania, zirconia and hafnia) have been characterized in term of fluidization behavior, surface reactivity and chemical resistance to harsh CIP procedures. Porous zirconia particles were also modified into ion-exchangers by suitable surface modification and intraparticle polymerization of functionalized stable derivatives of acrylic monomers. Back-mixings in fluidized bed columns were analyzed by residence time distribution analysis of inert tracers. 328 and 218 mixing plates per meter were found for respectively, bed expansions of 1.7 and 2.9. The dynamic protein adsorption behaviors of zirconia-based polymeric anion-exchange sorbents were obtained in fluidized-bed, using BSA as model protein. A dynamic binding capacity of 62 mg/ml was observed at a fluidizing velocity of 320 cm/h. These investigations substantiate the favorable physical and chemical characteristics anticipated for dense composite beads for use as fluidized bed adsorbents.     

Evaluation of three expanded bed adsorption anion exchange matrices with the aid of recombinant enhanced green fluorescent protein overexpressed in Escherichia coli

Three anion exchanger expanded bed adsorption (EBA) matrices: Streamline DEAE, Streamline Q XL and Q Hyper Z were evaluated with the aid of EFGP from an ultrasonic homogenate of Escherichia coli. Two pH of buffer were tested. Capture was done in an expanded mode whereas elution was done in a packed mode. The same conditions were chosen for evaluation of the three matrices. We observed a loss of EGFP (8-15%) in the through flow fraction especially with the Streamline Q XL matrix, probably due to an aggregation of beads during sample application. The beads of this matrix possess tentacles which probably retain a lot of cellular and molecular debris. The two other matrices gave a good purification of the EGFP (7-15-fold) but the Q Hyper Z matrix appeared to give the best results. It is composed of little size and density beads which lead to a higher exchange surface and then a better mass transfer.     

Nanofiber adsorbents for high productivity downstream processing

Electrospun polymeric nanofiber adsorbents offer an alternative ligand support surface for bioseparations. Their non‐woven fiber structure with diameters in the sub‐micron range creates a remarkably high surface area. To improve the purification productivity of biological molecules by chromatography, cellulose nanofiber adsorbents were fabricated and assembled into a cartridge and filter holder format with a volume of 0.15 mL, a bed height of 0.3 mm and diameter of 25 mm. The present study investigated the performance of diethylaminoethyl (DEAE) derivatized regenerated cellulose nanofiber adsorbents based on criteria including mass transfer and flow properties, binding capacity, and fouling effects. Our results show that nanofibers offer higher flow and mass transfer properties. The non‐optimized DEAE‐nanofiber adsorbents indicate a binding capacity of 10% that of packed bed systems with BSA as a single component system. However, they operate reproducibly at flowrates of a hundred times that of packed beds, resulting in a potential productivity increase of 10‐fold. Lifetime studies showed that this novel adsorbent material operated reproducibly with complex feed material (centrifuged and 0.45 µm filtered yeast homogenate) and harsh cleaning‐in‐place conditions over multiple cycles. DEAE nanofibers showed superior operating performance in permeability and fouling over conventional adsorbents indicating their potential for bioseparation applications. Biotechnol. Bioeng. 2013; 110: 1119–1128. © 2012 Wiley Periodicals, Inc.     

Mass transfer kinetics in the chromatography of insulin variants under nonlinear conditions

Experimental data regarding the thermodynamics and kinetics of adsorption of lispro, an insulin variant, onto a YMC ODS-A column, from an aqueous solution of acetonitrile (31%) and TFA are reinterpreted, using a more complex model of the mass transfer kinetics. The adsorption behavior follows the Toth isotherm model, suggesting either a strongly heterogeneous surface or, rather, that when insulin molecules adsorb they contact the surface along different areas of the molecule. The lumped pore diffusion (POR) model of chromatography accounts well for the band profiles. The internal mass transfer resistances are higher than expected, which suggests that intraparticle diffusion is slower. Furthermore, the pore diffusion coefficient increases with decreasing sample size. That surface diffusion accounts for the mass transfer kinetics inside particles explains these results. Assuming that the gradient of the surface concentration is the driving force of surface diffusion, it is possible to account very well for the band profiles of samples of widely different sizes, using a single value of the surface diffusivity.     

Residence time distribution in the chromatographic column: Applications in the separation engineering of DNA

Experimental and theoretical works were performed for the separation of large polyelectrolyte, such as DNA, in a column packed with gel particles under the influence of an electric field. Since DNA quickly orient in the field direction through the pores, this paper presents how intraparticle convection affects the residence time distribution of DNAs in the column. The concept is further illustrated with examples from solid-liquid systems, for example, from chromatography showing how the column efficiency is improved by the use of an electric field. Dimensionless transient mass balance equations were derived, taking into consideration both diffusion and electrophoretic convection. The separation criteria are theoretically studied using two different Peclet numbers in the fluid and solid phases. These criteria were experimentally verified using two different DNAs via electrophoretic mobility measurements, which showed how the separation position of the DNAs varies in the column in relation to the Peg/Pef values of an individual DNA. The residence time distribution was solved by an operator theory and the characteristic method to yield the column response.     

Separation of ϕX HAE III DNA with electrochromatography

Experimental and theoretical works were performed for the separation of large polyelectrolytes such as DNA in the column packed with gel particles under an electric field. This paper shows how intraparticle convection effects the separation of DNAs in the column because DNAs quickly oriented through the pores in the field direction. Dimensionless transient mass balance equations were derived considering diffusion and electrophoretic convection. The separation criteria is theoretically studied using two different Peclet numbers in the fluid and solid phases and these criteria were verified uing two different DNAs by electrophoretic mobilities measured experimentally, showing how the separation position of DNAs varies in the column according to values ofPe _f/Pe_g of individual DNA. Governing equations are simultaneously solved by operator theoretic and characteristic methods to yield the column response.     

Enzyme immobilized in a packed-bed reactor: kinetic parameters and mass transfer effects.

To describe axial dispersion, particle film mass transfer, intraparticle diffusion, and the chemical reaction of the substrate for enzymes immobilized in porous particles in packed columns, we have developed mathematical models for first- and zero-order limits of Michaelis-Menten kinetics. Steady-state solutions were derived for both long and short column boundary conditions and for plug flow. Theory was compared to experiments by hydrolysis of sucrose catalyzed by invertase bound to porous glass particles. Steady-state conversions were measured for a range of flow rates. Pulse response experiments with inert packing were used to determine values of bed void fraction and particle porosity.     

Packed bed bioreactor with porous ceramic beads for animal cell culture

A packed bed bioreactor was investigated as means for the cultivation of mammalian cells. The packed bed is comprised of porous ceramic particles with pores sufficiently large for cell immobilization as well as for intraparticle convective flow. In this way, the transport of limiting nutrients such as oxygen can be significantly enhanced, allowing maintenance of cell viability and productivity in an environment protective of adverse shear effects. The extent of intraparticle convective medium flow was experimentally quantified relative to the reactor operating conditions, and was found to be the dominant mechanism of nutrient transport to cells immobilized in the particle interior. An approximate linear relationship was obtained between overall reactor productivity and the extent of intraparticle convection. As the latter can be controlled at the single-particle level through total flow rate control, this relationship is a useful scale-up tool for the design of bioreactors. The high cell densities and the high volumetric productivities achieved by using small lab-scale reactors underline the potential of this simple bioreactor configuration for large-scale cell culture applications. (c) 1993 John Wiley & Sons, Inc.     

Radiotracer measurements of protein mass transfer: kinetics in ion exchange media

We describe a method to measure protein mass transfer kinetics in ion exchange adsorbents for preparative chromatography based on the use of radioactively labeled protein. The method was developed and evaluated using lysozyme as a test protein with the three commercial strong-acid cation exchangers SP-Sepharose-FF, SP-Sepharose-XL, and S-HyperD. Iodination with 125I was used to label the protein, which was added in trace amounts (approximately 0.1%) to an unlabeled protein solution. The solution was recirculated through a shallow bed of the adsorbent particles and the radioactivity accumulated in the bed measured with a gamma-counter as a function of time. Radiotracer-based kinetics measurements were found to be in good agreement with results obtained with a conventional shallow-bed technique, provided that freshly labeled protein solutions were used. The method has advantages in terms of simplicity, ability to deal with adsorption from complex mixtures, and the potential for measurements under tracer diffusion conditions. Kinetics results obtained for the three different stationary phases were generally consistent with previous studies. Protein mass transfer can be described by a pore diffusion model with a nearly salt-independent pore diffusivity for SP-Sepharose-FF and by a homogeneous diffusion model with a saltindependent adsorbed phase diffusivity for S-HyperD. However, it appears that a more complex model, accounting for parallel pore and surface diffusion, is needed to describe protein mass transfer in SP-Sepharose-XL. The modeling results were found to be correlated with the apparent pore sizes determined by inverse SEC.     

Separation of DNA by mass-transfer properties in the presence of an electric field

Experimental and theoretical works were performed for the separation of large polyelectrolyte such as DNA in the column packed with gel particles under influence of an electric field. Since DNA quickly orients through the pores in the field direction, this paper presents how intraparticle convection affects the separation of DNAs in the column. Dimensionless transient mass balance equations were derived considering diffusion and electrophoretic convection. The separation criteria are theoretically studied using two different Peclet numbers in the fluid and solid phases and these criteria were verified using two different DNAs by electrophoretic mobilities measured experimentally, showing how the separation position of DNAs varies in the column according to values of Pe_f/Pe_g of individual DNA. Governing equations are solved by an operator theory and the characteristic method to yield the column response.     

Analysis of protein adsorption characteristics to nano-pore silica particles by using confocal laser scanning microscopy

The effect of average pore size of nano-pore silica particles on protein adsorption characteristics was determined experimentally by the dissociation constant and the adsorption capacity determined from the Langmuir equation. As the average pore size was increased from 2.2 to 45 nm, the BSA adsorption capacity increased from 16.8 to 84.3 mg/g-silica so as the equilibrium constant (from 2.6 to 9.4 mg/ml). Using confocal microscopy with fluorescence labeling, we could visualize the protein adsorption in situ and determine the minimum pore size required for efficient intraparticle adsorption. The confocal microscopy analysis revealed that BSA was adsorbed mainly on the surface of the particles with a smaller pore size, but diffused further into the interstitial surface when it was sufficiently large. It was concluded that for BSA whose Stoke's diameter is ca. 3.55 nm the minimum pore size of about 45 nm or larger was required for a sufficient adsorption capacity.     

Protein-binding capacity of microquantities of tannins

The physiological effect of tannins is studied in terms of their protein-binding or precipitation capacity. A number of assays based on binding of hemoglobin or bovine serum albumin (BSA) and subsequent determination of unbound protein in supernatant or tannin in a protein-tannin complex are available but with various limitations. These methods are unable to estimate protein-binding capacity, if the quantity of tannin available is low. In the method reported here, tannins or other phenolics were applied on chromatography paper and reacted with BSA and unbound BSA was washed off. The protein in the tannin-protein complex was measured spectrophotometrically after staining with Ponceau S. It required microquantities of sample. Using this method the protein-binding capacity of total leaf extract and hydrolyzable and condensed tannins of Quercus incana, Q. semecarpofolia, and Q. dilatata was determined. The protein binding capacities of ellagic acid and quercetin (microgram BSA/mg) were 297.3 and 78.0, respectively.     

Sorptive removal of Methylene blue from aqueous solution using palm kernel fibre: Effect of fibre dose

The use of palm kernel fibre, a readily available agricultural waste product for the sorption of Methylene blue from aqueous solution and the possible mechanism of sorption has been investigated at various fibre doses. The extent of dye removal and the rate of sorption were analyzed using two kinetic rate models (pseudo-first and pseudo-second-order kinetic models) and two diffusion models (intraparticle and external mass transfer models).

Analysis of the kinetic data at different sorbent dose revealed that the pseudo-first order kinetics fitted to the kinetic data only in the first 5 min of sorption and then deviated from the experimental data. The pseudo-second-order kinetic model was found to better fit the experimental data with high correlation coefficients at the various fibre dose used. The dye sorption was confirmed to follow the pseudo-second-order model by investigating the relationship between the amount of dye sorbed and the change in hydrogen ion concentration of the dye solution and also the dependence of dye uptake with solution temperature. It was found that the change in hydrogen ion concentration and increase in sorption temperature were directly related to the amount of dye sorbed, and activation energy was calculated to be −39.57 kJ/mol, indicating that the dye uptake is chemisorption, involving valence forces through sharing or exchange of electrons between sorbent and sorbate as covalent forces.

The intraparticle diffusion plots showed three sections indicating that intraparticle diffusion is not solely rate controlling. The intraparticle diffusion and mass transfer rate constants where observed to be well correlated with sorbent dose in the first 5 min of sorption, indicating sorption process is complex. It was found that at low sorbent dose the mass transfer is the main rate controlling parameter. However at high sorbent dose, intraparticle diffusion becomes rate controlling.     

Parameter estimation of perillyl alcohol in RP-HPLC by moment analysis

Parameter estimations were made for the reversed-phase adsorption of perillyl alcohol (POH), a potent anti-cancer agent, on octadecylsilyl-silica gel (ODS). The average particle diameter of ODS was about 15 μm, and the particles were packed in the column (3.9 × 300 mm). The mobile phase used was a mixture of acetonitrile and water, in which the acetonitrile ranged between 50 and 70 (v/v %). The first absolute moment and the second central moment were determined from the chromatographic elution curves by moment analysis. Experiments were carried out using POH solutions within the linear adsorption range. The fluid-to-particle mass transfer coefficient was estimated using the Wilson-Geankoplis equation. The axial dispersion coefficient and the intraparticle diffusivity were determined from the slope and intercept of a plot ofH vs 1/u ₀, respectively. The contributions of each mass-transfer step were axial dispersion, fluid-toparticle mass transfer, and intraparticle diffusion.     

Mathematical modeling of elution curves for a protein mixture in ion exchange chromatography applied to high protein concentration

Protein elution curves in ion exchange chromatography (IEC) were simulated with a rate model. Three pure proteins and their mixture were used (α‐lactalbumin, BSA, and conalbumin) under different operational conditions. The anionic matrix Q‐Sepharose FF was used packed in a 1 mL column. A high protein concentration (37.5 mg/mL of total protein injected into the column) was used in order to extend the utility of the model. Mass transfer parameters were calculated using empiric correlations, where the axial dispersion was negligible (Pe > 300) and the mass transfer was controlled by the intraparticle diffusion (Bi > 10). The model assumes a modulator–eluite relationship were the equilibrium constant of the Langmuir isotherm was a function of salt concentration. Adsorption kinetic parameters were estimated from experimental data. The parameters for pure proteins were determined, and elution curves for changes in flow rate, ionic strength gradient, concentration, and sample size were predicted by the model. Then the kinetic parameters of the mixture were determined under the same operational conditions and some of the parameters had to be modified to take into account effects such as protein–protein interactions, competition, and displacement. Experimental elution curves obtained for changes in operational conditions such as flow rate and ionic strength gradient were simulated by the rate model for the protein mixture with a relative error in retention time of visible peaks <5%. IEC operational conditions and the peak fraction collection can be selected using a cost function of the production process which considers yield, purity, concentration, and process time that are obtained from simulations. Operational conditions that gave the minimum cost were selected. Simulations allows to diminish experimental time and cost. Biotechnol. Bioeng. 2009; 104: 572–581 © 2009 Wiley Periodicals, Inc.     

Structural and performance characteristics of representative anion exchange resins used for weak partitioning chromatography

Weak partitioning chromatography (WPC) has been proposed for the purification of monoclonal antibodies using an anion exchange (AEX) resin to simultaneously remove both acidic and basic protein impurities. Despite potential advantages, the relationship between resin structure and WPC performance has not been evaluated systematically. In this work, we determine the structure of representative AEX resins (Fractogel® EMD TMAE HiCap, Q Sepharose FF, and POROS 50 HQ) using transmission electron microscopy and inverse size exclusion chromatography and characterize protein interactions while operating these resins under WPC conditions using two mAb monomers, a mAb dimer, mAb multimers, and BSA as model products and impurities. We determine the isocratic elution behavior of the weakly bound monomer and dimer species and the adsorptive and mass transfer properties of the strongly bound multimers and BSA by confocal laser scanning microscopy. The results show that for each resin, using the product K_p value as guidance, salt, and pH conditions can be found where mAb multimers and BSA are simultaneously removed. Isocratic elution and adsorption mechanisms are, however, different for each resin and for the different components. Under WPC conditions, the Fractogel resin exhibited very slow diffusion of both mAb monomer and dimer species but fast adsorption for both mAb multimers and BSA with high capacity for BSA, while the Sepharose resin, because of its small pore size, was unable to effectively remove mAb multimers. The POROS resin was instead able to bind both multimers and BSA effectively, while exhibiting a greater resolution of mAb monomer and dimer species. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:425–434, 2017