Pressure-flow relationships for packed beds of compressible chromatography media at laboratory and production scale

Pressure drop across chromatography beds employing soft or semirigid media can be a significant problem in the operation of large-scale preparative chromatography columns. The shape or aspect ratio (length/diameter) of a packed bed has a significant effect on column pressure drop due to wall effects, which can result in unexpectedly high pressures in manufacturing. Two types of agarose-based media were packed in chromatography columns at various column aspect ratios, during which pressure drop, bed height, and flow rate were carefully monitored. Compression of the packed beds with increasing flow velocities was observed. An empirical model was developed to correlate pressure drop with the aspect ratio of the packed beds and the superficial velocity. Modeling employed the Blake-Kozeny equation in which empirical relationships were used to predict bed porosity as a function of aspect ratio and flow velocity. Model predictions were in good agreement with observed pressure drops of industrial scale chromatography columns. A protocol was developed to predict compression in industrial chromatography applications by a few laboratory experiments. The protocol is shown to be useful in the development of chromatographic methods and sizing of preparative columns.     

The effects of processing scale on the pressure drop of compressible gel supports in liquid chromatographic columns

Experimental data are given for the solid pressure distributions in liquid chromatographic columns for two commercially available agarose-based compressible gel supports. The data show that for a given liquid velocity the pressure drop increases exponentially with height from the top surface. However, beyond a threshold liquid velocity, flow instability develops rapidly and the pressure drop rises sharply as the gel matrix compresses under the applied vertical pressures. The threshold liquid velocity at the point of criticality is examined in the light of the experimental data and the numerical simulations based on a one dimensional elemental slice force balance of the gel mass. The result of this analysis shows that matrix rigidity, column diameter and bed height significantly affect the point of criticality.     

Membrane adsorbers as purification tools for monoclonal antibody purification

Downstream purification processes for monoclonal antibody production typically involve multiple steps; some of them are conventionally performed by bead-based column chromatography. Affinity chromatography with Protein A is the most selective method for protein purification and is conventionally used for the initial capturing step to facilitate rapid volume reduction as well as separation of the antibody. However, conventional affinity chromatography has some limitations that are inherent with the method, it exhibits slow intraparticle diffusion and high pressure drop within the column. Membrane-based separation processes can be used in order to overcome these mass transfer limitations. The ligand is immobilized in the membrane pores and the convective flow brings the solute molecules very close to the ligand and hence minimizes the diffusional limitations associated with the beads. Nonetheless, the adoption of this technology has been slow because membrane chromatography has been limited by a lower binding capacity than that of conventional columns, even though the high flux advantages provided by membrane adsorbers would lead to higher productivity. This review considers the use of membrane adsorbers as an alternative technology for capture and polishing steps for the purification of monoclonal antibodies. Promising industrial applications as well as new trends in research will be addressed.     

Demonstration of the use of windows of operation to visualize the effects of fouling on the performance of a chromatographic step

The high resolution afforded by packed bed chromatography makes it an indispensable operation in the downstream processing of therapeutic molecules. Packed bed performance is however inherently susceptible to changes in feed stream characteristics and fouling processes. The impact of fouling is seldom considered during the early stages of bioprocess development which is concerned with the selection of purification conditions. Instead these are performed with rigorously clarified feeds. Under such conditions, chromatography is effectively treated as an isolated step, independent from its preceding unit operations. In this study, we demonstrate how windows of operation could be used to visualize the impact of changes in the preceding clarification step on the fouling response of a subsequent cation exchange capture step. Laboratory columns (2,5 and 12 cm height) were subjected to varying fouling challenges of Escherichia coli lysate containing different amounts of solids carried over from the previous step. Changes in trans‐column pressure drop and breakthrough of the target protein (Fab′) were monitored. The limits of operability of the resin were determined with respect to the process material's properties. This information was used to extract the parameters for the adsorption kinetics used in the general rate (GR) model to create windows of operation for manufacturing scale operation. © 2011 American Institute of Chemical Engineers Biotechnol. Prog., 2011     

Pressure drop increase by biofilm accumulation in spiral wound RO and NF membrane systems: role of substrate concentration,flow velocity,substrate load and flow direction

In an earlier study, it was shown that biofouling predominantly is a feed spacer channel problem. In this article, pressure drop development and biofilm accumulation in membrane fouling simulators have been studied without permeate production as a function of the process parameters substrate concentration, linear flow velocity, substrate load and flow direction. At the applied substrate concentration range, 100–400 μg l^?1 as acetate carbon, a higher concentration caused a faster and greater pressure drop increase and a greater accumulation of biomass. Within the range of linear flow velocities as applied in practice, a higher linear flow velocity resulted in a higher initial pressure drop in addition to a more rapid and greater pressure drop increase and biomass accumulation. Reduction of the linear flow velocity resulted in an instantaneous reduction of the pressure drop caused by the accumulated biomass, without changing the biofilm concentration. A higher substrate load (product of substrate concentration and flow velocity) was related to biomass accumulation. The effect of the same amount of accumulated biomass on the pressure drop increase was related to the linear flow velocity. A decrease of substrate load caused a gradual decline in time of both biomass concentration and pressure drop increase. It was concluded that the pressure drop increase over spiral wound reverse osmosis (RO) and nanofiltration (NF) membrane systems can be reduced by lowering both substrate load and linear flow velocity. There is a need for RO and NF systems with a low pressure drop increase irrespective of the biomass formation. Current efforts to control biofouling of spiral wound membranes focus in addition to pretreatment on membrane improvement. According to these authors, adaptation of the hydrodynamics, spacers and pressure vessel configuration offer promising alternatives. Additional approaches may be replacing heavily biofouled elements and flow direction reversal.     

Studies on scale-up parameters of an immunoglobulin separation system using protein A affinity chromatography.

Effects of operational and system parameters on process scale-up of murine immunoglobulin (IgG2a kappa) purification using Protein A affinity chromatography are investigated. Parameters studied are those related to sample application, elution, ligand concentration on support, and column size change. Between sample application velocities of 0.004 and 0.030 cm/s (16-108 cm/h), the product concentration profiles in eluate did not show significant differences. With given system parameters, the retention time and bandwidth of the peak could be predicted by moment theory. The mean equilibrium constant during elution showed a strong effect of pH between 2 and 4. Within the range of protein A concentrations studied, 0.15-1.22 mg/mL of gel, the column capacity shows a linear relationship with the concentration of protein A immobilized. Dimensional scale-up of the column in the radial direction increased the total purification capacity linearly as the cross-sectional area increased without increasing pressure drop; however, the product concentration was diluted. Scale-up of the column dimension in the axial direction enables higher concentrations of product in the eluate, although the retention time increases linearly as the gel height increases.     

Realities of automating OPA HPLC amino acid analyses

The levels of free amino acids in culture medium can easily be monitored by reversed-phase HPLC chromatography on a C18 column following pre-column derivatization with o-pthaladehyde. The method does not require the prior removal of proteins. A guard column does that. When this method was automated, problems started to occur after about eight injections. Peak resolution rapidly degraded. Unidentified matter was retained by the column and produced both interfering peaks and high back pressures. Better resolution of the closely eluting amino acids occurred when both the pH of the loading buffer was increased and the gradient time was lengthened. Special washes and a carefully controlled time of equilibration with the loading buffer helped to minimize back pressure and interfering substances. Other often skipped routine maintenance and solvent handling procedures were also necessary for optimal performance. These modifications made routine runs of 40 plus samples possible as well as dramatically increased the lifetime of the column.     

Development of a process for large-scale purification of C-phycocyanin from Synechocystis aquatilis using expanded bed adsorption chromatography

In this paper a large and scaleable method for purification of C-phycocyanin (C-PC) from the cyanobacteria Synechocystis aquatilis has been developed. Phycobiliproteins are extracted from the cells by osmotic shock and separated by passing the centrifuged cell suspension through an expanded bed adsorption chromatography (EBAC) column using Streamline-DEAE as adsorbent. The eluted C-PC rich solution is finally purified by packed-bed chromatography using DEAE-cellulose. Optimal extraction is achieved using phosphate 0.05 M buffer pH 7.0 twice. The operation of EBAC is optimized on a small scale using a column of 15 mm internal diameter (I.D.). The optimal conditions are a sample load of 4.9 mg C-PC/mL adsorbent, an expanded bed volume twice the settled bed volume and a sample viscosity of 1.020 mP. The EBAC process is then scaled up by increasing the column I.D. (15, 25, 40, 60 and 90 mm) and the success of the scale-up process is verified by determining the protein breakthrough capacity and product recovery. The yield of the EBAC step is in the range of 90-93% for every column diameter. To obtain pure C-PC, conventional ion-exchange chromatography with DEAE-cellulose is utilized and a yield of 74% is obtained. The overall yield of the process, comprising all steps, is 69%. The purification steps are monitored using SDS-PAGE and the purity of recovered C-PC is confirmed by absorption and emission spectroscopy and RP-HPLC. Results show that EBAC method is a scalable technology that allows large quantities of C-PC to be obtained without product loss, maintaining a high protein recovery while reducing both processing cost and time.     

Operational parameters for packed beds in solid-state cultivation

Packed bed cultivation systems have potential for widespread application in solid-state cultivation (SSC), but they are poorly characterized. The effects of particle size and substrate loading on the growth of Rhizopus oligosporus on sago-beads in packed bed bioreactors were investigated. Pressure drop and protein were monitored as indicators of fungal growth in cultivations performed in a large column (4.9 cm internal diameter and 60 cm height) and a system of small columns (4.2 cm internal diameter and 5.2 cm height). The differential pressure drop increased to a maximum between 34 and 44 h and then decreased again. The maximum differential pressure drop attained was greatest for the smallest particle size and for the lower substrate loadings. However, since the protein content continued to increase throughout the cultivation, pressure drop could not be used to monitor growth directly.     

Automated kinetic analysis of pyruvate kinase

An apparatus for the automatic determination of enzyme kinetics of pyruvate kinase is described. A continuous plit of velocity versus substrate concentration is obtained using quantities of enzyme and substrates comparable to manual determinations. The automated procedure offers a number of advantages over manual methods including elimination of repetitive pipetting, simpler reaction temperature regulation, reduced analysis time, and possible on-line computer analysis. The apparatus utilizes a commercially available column uv flow monitor to measure NADH/NAD changes in the coupled lactic dehydrogenase reaction at 340 nm in a continuous flow system. The optical density changes are directly related to the velocity of the enzyme-catalyzed reaction. A linear substrate gradient is generated from a density gradient maker to provide the required relationship between velocity and substrate concentration. The system is calibrated by forming a gradient from a hemoglobin solution of known concentration. The procedure has been evaluated by determination of the kinetic parameters of three of the isozymes of pyruvate kinase. Values obtained by the continuous flow method are in close agreement with those obtained by individual point determination in a recording spectrophotometer.     

The role of the surrounding tissue in the propagation of waves through the arterial system.

A theoretical analysis of the flow in arteries is presented, taking into consideration the role played by the surrounding tissues in determining the speed of propagatoion and the damping of the blood pressure pulse. This study was undertaken (a) to exhibit a method of computing the flow properties with a more nearly accurate model, (b) to see if the displacement on the skin would be related to the arterial wall displacement, and hence to pressure, velocity and flow rate of blood in the artery, and if it is likely to be measurable. It was found that the pressure of the 'viscous' part in the surrounding tissue increases the pulse velocity and the damping of the wave over the values found by other models which considered only thick-walled elastic tubes with no surrounding tissue. This study also shows that measurements on the skin can provide information about changes in arterial circulation due to diseases such as: edema, arteriosclerosis and others where the Young's modulus for either the arterial wall or the surrounding tissues is altered.     

舟山眼镜蛇毒CTX1层析分离的流速优化

目的 比较3种流速的CM-Sepharose FF阳离子交换层析柱分离舟山眼镜蛇(Naja naja atra)蛇毒(snake venom,SV)的柱效,为SV的分离纯化提供实验依据.方法 (1)采用3种流速CM-Sepharose FF阳离子交换层析柱分离舟山眼镜蛇蛇毒;(2)反向高效液相法分析各组分的纯度及内标法...     

Dynamic behavior of adsorber membranes for protein recovery

In recent years there has been a considerable interest in developing membrane chromatography systems that function as a short, wide chromatographic column in which the adsorptive packing consists of one or more microporous membranes. This study reports the use of new adsorber membranes prepared by the incorporation of various types of ion exchange resins into an EVAL porous membrane for protein recovery. The obtained heterogeneous matrixes composed of solid particles surrounded by the polymeric film possess a good accessibility for the protein to the adsorptive sites. Furthermore, small particles can be embedded into porous polymeric structures without the disadvantages of classical chromatographic columns (high pressure drop, fouling and plugging sensitivity, low flow rate), but with the advantages of membrane technology (easy scale-up, low-pressure drop, high flow rate). The adsorptive membranes feature high static as well as dynamic protein adsorption capacities for operating flow rates ranging from 200 to 400 L h bar per m(2) and ionic strength of 20-200 mM. In a sequential desorption step by changing the pH and/or the ionic strength of the eluent, up to 90% protein recovery was obtained. Next to the separation, the mixed matrix adsorber membrane functions as a concentration medium since the protein can be concentrated up to 20-fold in the eluent. The adsorber membranes can be reused in multiple adsorption/desorption cycles with good adsorption performances.     

利用FPLC系统结合自装层析柱纯化兔血清IgG

为了建立一种简便、成本低的纯化兔血清IgG的实用方法,采用FPLC系统结合实验室常规手段填充的Sephacryl-S200凝胶柱和DEAE-Sephadex A-50离子交换柱进行兔血清IgG的纯化,结果表明,在流速为0．5ml／min时,此方法可以纯化得到高纯度的兔IgG;脱盐柱Sephadex G-25重复实验证明此实验方法具有很好的稳定性;并且与商品化的层析柱相比,成本大为下降;此方法主要的不足之处是层析柱的流速较低,为0．5ml／min左右。该方法可以推广到其他生物大分子的纯化中去。     

Modeling of transient flow through a viscoelastic preparative chromatography packing

The common method for purification of macromolecular bioproducts is preparative packed‐bed chromatography using polymer‐based, compressible, viscoelastic resins. Because of a downstream processing bottleneck, the chromatography equipment is often operated at its hydrodynamic limit. In this case, the resins may exhibit a complex behavior which results in compression–relaxation hystereses. Up to now, no modeling approach of transient flow through a chromatography packing has been made considering the viscoelasticity of the resins. The aim of the present work was to develop a novel model and compare model calculations with experimental data of two agarose‐based resins. Fluid flow and bed permeability were modeled by Darcy's law and the Kozeny–Carman equation, respectively. Fluid flow was coupled to solid matrix stress via an axial force balance and a continuity equation of a deformable packing. Viscoelasticity was considered according to a Kelvin–Voigt material. The coupled equations were solved with a finite difference scheme using a deformable mesh. The model boundary conditions were preset transient pressure drop functions which resemble simulated load/elution/equilibration cycles. Calculations using a homogeneous model (assuming constant variables along the column height) gave a fair agreement with experimental data with regard to predicted flow rate, bed height, and compression–relaxation hysteresis for symmetric as well as asymmetric pressure drop functions. Calculations using an inhomogeneous model gave profiles of the bed porosity as a function of the bed height. In addition, the influence of medium wall support and intraparticle porosity was illustrated. The inhomogeneous model provides insights that so far are not easily experimentally accessible. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 29:958–967, 2013     

Determination of a new antifungal agent, voriconazole, by multidimensional high-performance liquid chromatography with direct plasma injection onto a size-exclusion column

A fully automated method has been developed for the analysis of a new antifungal agent, voriconazole, in human plasma. Multidimensional chromatography was used with size-exclusion chromatography as the first step to separate plasma protein from the drug and internal standard which were then trapped on a precolumn of pellicular ODS. A reversed-phase column, Spherisorb ODS2, then separated drug and internal standard from one another and from remaining plasma components. With an injection of 0.56 ml plasma the limit of quantitation of the method was 5 ng/ml.     

Estimation of valvular resistance of segmented aortic valves using computational fluid dynamics

Aortic valve stenosis is associated with an elevated left ventricular pressure and transaortic pressure drop. Clinicians routinely use Doppler ultrasound to quantify aortic valve stenosis severity by estimating this pressure drop from blood velocity. However, this method approximates the peak pressure drop, and is unable to quantify the partial pressure recovery distal to the valve. As pressure drops are flow dependent, it remains difficult to assess the true significance of a stenosis for low-flow low-gradient patients. Recent advances in segmentation techniques enable patient-specific Computational Fluid Dynamics (CFD) simulations of flow through the aortic valve. In this work a simulation framework is presented and used to analyze data of 18 patients. The ventricle and valve are reconstructed from 4D Computed Tomography imaging data. Ventricular motion is extracted from the medical images and used to model ventricular contraction and corresponding blood flow through the valve. Simplifications of the framework are assessed by introducing two simplified CFD models: a truncated time-dependent and a steady-state model. Model simplifications are justified for cases where the simulated pressure drop is above 10 mmHg. Furthermore, we propose a valve resistance index to quantify stenosis severity from simulation results. This index is compared to established metrics for clinical decision making, i.e. blood velocity and valve area. It is found that velocity measurements alone do not adequately reflect stenosis severity. This work demonstrates that combining 4D imaging data and CFD has the potential to provide a physiologically relevant diagnostic metric to quantify aortic valve stenosis severity.     

Efficient purification of small unsaturated oligoglucuronides by reversed-phase chromatography

Ion-exchange chromatography has been applied to purification of unsaturated oligoglucuronans. After an isocratic elution on a strong anion-exchange column, the collected fractions were desalted by low pressure size exclusion chromatography. However, this efficient separation was limited by the time required to desalt. So, we developed a reversed-phase chromatography method using back ionization of oligomers. Two C18 columns were tested with trifluoroacetic acid (TFA 0.7%) as eluent. Different selectivities and column stabilities were observed in this acidic condition. The scale up for semi-preparative applications enabled us to recover pure unsaturated oligoglucuronans without desalting step.     

Effect of different operating modes and biomass concentrations on the recovery of recombinant hepatitis B core antigen from thermal-treated unclarified Escherichia coli feedstock

Expanded bed adsorption chromatography (EBAC) is a single pass operation that has been used as primary capture step in various protein purifications. The most common problem in EBAC is often associated with successful formation of a stable fluidized bed during the absorption stage, which is critically dependent on parameters such as liquid velocity, bed height, particle (adsorbent) size and density as well as design of column and type of flow distributor. In this study, residence time distribution (RTD) test using acetone as non-binding tracer acetone was performed to evaluate liquid dispersion characteristics of the EBAC system. A high B(o) number was obtained indicating the liquid dispersion in the system employed is very minimal and the liquid flow within the bed was close to plug flow, which mimics a packed bed chromatography system. Evaluation on the effect of flow velocities and bed height on the performance of Streamline DEAE using feedstock containing heat-treated crude Escherichia coli homogenate of different biomass concentrations was carried out in this study. The advantages and disadvantages as well as the problems encountered during recovery of HBcAg with aforementioned parameters are also discussed in this paper.     

Design of a new automatic chromatography system for efficient enzyme purification equipped with a time-shared multiple activity analyzer

A new system equipped with a computer-controlled multiple activity analyzer has been developed for the efficient purification of multiple enzymes. The system consists of the following units: conventional enzyme fractionation system with a peristaltic pump, liquid chromatographic column, fraction collector, and uv monitor; computer-operated uv-vis spectrophotometer equipped with a thermo-regulated metal block and a flow-through type silica cuvette; personal computer; dot matrix printer; cooling facility; and automatic sampling-mixing system. The whole system is operated by a newly designed time-sharing computer program for periodic and repetitive sampling of the column eluants containing multiple kinds of enzymes and of designated assay mixtures for each enzyme and for measurement of the initial velocity of spectrophotometric signals. For example, a mixture of aspartase (EC 4.3.1.1) and malate dehydrogenase (EC 1.1.1.39) and also a mixture of these two enzymes and glutamate dehydrogenase (EC 1.4.1.3 or EC 1.4.1.4) were analyzed by the above system using gel permeation chromatography, and the two or three enzyme activities were repeatedly monitored within 4 min. Based on the above results further possibilities for the application of the system for a variety of purposes are discussed.