Tangential flow microfiltration and ultrafiltration for human influenza A virus concentration and purification

Large scale purification of viruses and viral vectors for gene therapy applications and viral vaccines is a major separation challenge. Here tangential flow microfiltration and ultrafiltration using flat sheet membranes has been investigated for concentration of human influenza A virus. Ultrafiltration membranes with molecular weight cutoffs of 100 and 300 kDa as well as 0.1, 0.2 and 0.45 microm microfiltration membranes have been tested. The results indicate that use of 300 kDa membranes not only concentrate the virus particles but also lead to a significant removal of host cell proteins and DNA in the permeate. Tangential flow filtration may be used to fractionate virus particles. Human influenza A virus particles are spherical with an average size of 100 nm. Use of a 0.1 microm membrane leads to passage of virus particles less than 100 nm into the permeate and an increase of larger particles in the retentate. These results suggest that control of the transmembrane pressure, membrane pore size and pore size distribution could enable isolation of intact virus particles from damaged virions. Isolation of the virus particles of interest from viral fragments and other particulate matter could result in simplification of subsequent purification steps. Larger pore size membranes such as 0.45 microm that allow the passage of all virus particles may be used to remove host cell fragments. In addition virus particles attached to these fragments will be removed. Careful selection of membrane morphology and operating conditions will be essential in order to maximize the benefit of tangential flow filtration steps in the purification of viral products from cell cultures.     

The use of ultrafiltration for concentration and purification of beta-galactosidase

A possibility of concentration and purification of culture fluid of Escherichia coli by the ultrafiltration technique using Soviet cellulose acetate membranes were studied. It is established that cellulose acetate membranes may be used for purification from low molecular weight protein and concentration of preliminarily purified culture fluid of Escherichia coli. Membranes YAM-300 are most preferable. At the temperature of 18 degrees C, pressure 0.16-0.24 MPa and 20-fold concentration the yield of the enzyme at the ultrafiltration stage was 84.5%.     

Effect of solution pH on protein transport through ultrafiltration membranes

Although a number of previous studies have demonstrated that solution pH can have a dramatic effect on protein transport through ultrafiltration membranes, the exact origin of this behavior has been unclear. Experimental data were obtained for the transport of a broad range of proteins with different surface charge and molecular weight. The effective hydrodynamic size of the proteins was evaluated using size‐exclusion chromatography. The membrane charge, both before and after exposure to a given protein, was evaluated using streaming potential measurements. In most cases, the electrostatic interactions were dominated by the distortion of the electrical double layer surrounding the protein, leading to a distinct maximum in protein transmission at the protein isoelectric point. Attractive electrostatic interactions did occur when the protein and membrane had a large opposite charge, causing a second maximum in transmission at a pH between the isoelectric points of the protein and membrane. The sieving data were in good agreement with theoretical calculations based on available models for the partitioning of charged solutes in cylindrical pores. © 1999 John Wiley & Sons, Inc. Biotechnol Bioeng 64: 27–37, 1999.     

Separation of protein charge variants by ultrafiltration

The removal of product variants that form during downstream processing remains a challenge in the purification of recombinant therapeutic proteins. We examined the feasibility of separating variants with slightly different net charge using high-performance membrane ultrafiltration. A myoglobin variant was formed by reaction of the lysine epsilon-amino group with succinic anhydride. Sieving data were obtained over a range of solution conditions using commercial polyethersulfone ultrafiltration membranes. Maximum selectivity of about 7-fold was obtained at very low conductivity due to the strong electrostatic repulsion of the more negatively charged variant. Protein separations were performed by diafiltration. A two-stage process generated solutions of the normal myoglobin (in the permeate) and the charge variant (in the retentate), both at greater than 9-fold purification and 90% yield. These results provide the first demonstration that membrane systems can be used to separate proteins that differ by only a single charged amino acid residue.     

Fractionation of bovine serum albumin and monoclonal antibody alemtuzumab using carrier phase ultrafiltration

Protein transmission and hence selectivity of separation can be significantly affected by solution pH and ionic strength in protein fractionation using ultrafiltration. Using parameter scanning ultrafiltration, the transmission of bovine serum albumin (BSA) and monoclonal antibody alemtuzumab (Campath-1H) through 300 kDa polyethersulfone (PES) ultrafiltration membranes were studied over a range of pH and salt concentrations, with focus on the likely conditions for achieving "reverse selectivity," i.e., obtaining purified alemtuzumab (approximately 155 kDa) in the permeate. Experimental results demonstrate that the reverse selectivity could be obtained by manipulating the operating conditions such as the solution pH, ionic strength, permeate flux, and system hydrodynamics. With a two-stage batch ultrafiltration process under suitable conditions, the monoclonal antibody alemtuzumab with a purity of > 98% was obtained in the permeate from a feed solution initially containing 0.50 g/l each of BSA and alemtuzumab. Further purity can be expected by selecting more suitable membranes and optimizing operating conditions.     

Purification of equine IgG using membrane based enhanced hybrid bioseparation technique: a potential method for manufacturing hyperimmune antibody

Hyperimmune equine IgG is widely used as antivenom and anti-rabies agents. This article discusses a membrane based enhanced hybrid bioseparation technique for efficient and scalable purification of equine immunoglobulin G (IgG) from horse serum. This technique is an improved version of a standard hybrid bioseparation technique developed within our group earlier for fractionation of human plasma proteins (Ghosh. 2004. J Membr Sci 237: 109-117). In the presence of a high antichaotropic salt concentration, equine IgG is selectively and reversibly captured within a stirred cell membrane module from horse serum, partly due to precipitation and microfiltration, and partly due to hydrophobic interaction based membrane adsorption, while the impurities are washed out from the device. The reversibly sequestered IgG is then released by lowering the salt concentration which favor both dissolution of the precipitated IgG and desorption of the membrane bound IgG. The enhanced hybrid bioseparation technique improves the IgG recovery from the membrane module by switching from a stirring to non-stirring mode during the IgG release phase. It also reduces membrane fouling by an appropriate pH switch. The effects of operating conditions on equine IgG capture were first systematically studied. The enhanced hybrid bioseparation technique was followed by an ultrafiltration step to remove ammonium sulfate and low molecular weight impurities. The equine IgG purity obtained under optimized conditions was 88% and its recovery was over 90%, both being significantly higher than corresponding values obtained using currently used purification techniques.     

Effect of membrane morphology and operation on protein deposition in ultrafiltration membranes

Membrane morphology is compared to protein depostion under passive adsorption and ultrafiltration conditions. Solute resistance of protein deposits for membranes of varying roughness, structure, and permeability can vary dramatically with operating conditions. Using Brunauer-Emmett-Teller adsorption isotherm (BET), study of the internal area and accessibility of several uttrafiltration membranes to protein deposition allows better understanding of the fouling mechanisms and interpretation of adsorbed protein quantities. (c) 1995 John Wiley & Sons, Inc.     

Purification of singly PEGylated α-lactalbumin using charged ultrafiltration membranes

One of the challenges in producing a PEGylated therapeutic protein is that the PEGylation reaction typically generates a mixture of both singly and multiply PEGylated species. The objective of this study was to examine the feasibility of using ultrafiltration for the purification of a singly PEGylated protein from the multiply PEGylated conjugates. Data were obtained with α‐lactalbumin that was PEGylated with a 20 kDa activated PEG, with the ultrafiltration performed over a range of pH and ionic strength using both unmodified and negatively charged composite regenerated cellulose membranes. Purification of the singly PEGylated α‐lactalbumin from the multiply PEGylated species was accomplished using a diafiltration process with a negatively charged membrane at pH 5 and an ionic strength of 0.4 mM, conditions that maximized the electrostatic exclusion of the multiply PEGylated species from the charged membrane. The diafiltration process provided more than 97% yield with greater than 20‐fold purification between the singly and doubly PEGylated proteins and nearly complete removal of the more heavily PEGylated species. The singly PEGylated α‐lactalbumin was recovered as a dilute filtrate solution, although this dilution could be eliminated using a cascade filtration or the final product could be re‐concentrated in a second ultrafiltration as part of the final formulation. These results demonstrate the feasibility of using ultrafiltration for the purification of singly PEGylated protein therapeutics. Biotechnol. Bioeng. 2011; 108:822–829. © 2010 Wiley Periodicals, Inc.     

Distribution of calmodulin and calmodulin-binding proteins in membranes from bovine epididymal spermatozoa

Reproducible concentrations of calmodulin representing approximately 0.1% of the membrane protein were detected in purified plasma membranes from bovine epididymal spermatozoa. When membranes were isolated in the presence of 1 mM EGTA, the amount of calmodulin associated with the plasma membranes was not reduced. Calmodulin-binding proteins were detected in both purified plasma membranes and in a mixed membrane fraction containing both plasma membranes and cytoplasmic droplet membranes. A calcium-dependent, calmodulin-binding protein of apparent molecular weight 123,000 was detected in both fractions. In the presence of 1 mM EDTA, putative calcium-independent calmodulin-binding proteins of apparent molecular weights 93,000, 32,000, 18,000, and 15,000 were detected in the plasma membrane fraction. The 15,000 Mr polypeptide was also present in the mixed membrane fraction but the three proteins of higher molecular weight were reduced or absent in this fraction.     

Ultrafiltration characteristics of pegylated proteins

There is growing clinical interest in the use of pegylated recombinant proteins with enhanced stability, half-life, and bioavailability. The objective of this study was to develop a quantitative understanding of the ultrafiltration characteristics of a series of pegylated proteins with different degrees of pegylation. Sieving data were compared with available theoretical models and with corresponding results for the partition coefficient in size exclusion chromatography (SEC). The sieving coefficients of the pegylated proteins depended not only on the protein size and the total molecular weight of the polyethylene glycol (PEG) but also on the number of PEG chains. This is in sharp contrast to the partition coefficient in SEC, which was uniquely determined by the total molecular weight of the PEG and protein. This difference is due to the deformation and/or elongation of the PEG chains caused by the convective flow into the membrane pores, an effect that is not present in SEC. These results provide important insights into the transport and separation characteristics of pegylated proteins.     

Separation of monoclonal antibody alemtuzumab monomer and dimers using ultrafiltration

This article examines the feasibility of using ultrafiltration to separate the monomer of the monoclonal antibody alemtuzumab (Campath or Campath-1H) from a mixture of dimer and higher-order oligomers (collectively called "dimers" here). Using parameter scanning ultrafiltration, we initially assessed the suitability of the following membranes: 100 kDa and 300 kDa polyethersulfone (PES) membranes, and a 100 kDa polyvinylidene fluoride (PVDF) membrane. A detailed study was then carried out to examine the effects of operating conditions (such as solution pH, ionic strength, stirring speed, and permeate flux) on the separation of the monomer from the dimers using 300 kDa PES and 100 kDa PVDF membranes. Results of the experiments carried out in the carrier phase ultrafiltration (CPUF) mode indicate that the size-based protein-protein separation critically depends on the membrane used as well as the system hydrodynamics. The separation of the monoclonal antibody monomer and dimers using 100 kDa PVDF membranes in the diafiltration mode was also examined. Experimental results demonstrate that under suitable conditions, it is feasible to obtain the alemtuzumab monomer with a purity of more than 93% and a yield of more than 85% (from a mixture of 75% monomer and 25% dimers, which is the typical composition obtained after affinity chromatography). Simulation study indicates that this could be further improved to a purity of more than 96% and a monomer yield of more than 96% by increasing the selectivity of separation or by employing a two-stage diafiltration process.     

Membrane technology for purification of therapeutic proteins

Membrane systems are used throughout the downstream purification in the commercial production of high value therapeutic proteins. Over the last two decades, new membranes, modules, and systems have been developed specifically to meet the requirements of the biotechnology industry. These developments have been facilitated by an improved fundamental understanding of: (1) the effects of electrostatic interactions and concentration polarization on protein transmission during ultrafiltration and (2) the role of membrane morphology on protein fouling during both sterile and virus filtration. This perspective highlights some of the key work in this area and provides insights into possible future improvements in membrane technology for the purification of recombinant therapeutic proteins. Biotechnol. Bioeng. 2009;103: 227–230. © 2009 Wiley Periodicals, Inc.     

Ultrafiltration,a useful method for isolation of intermediates in native chemical ligation exemplified with the total synthesis of Sortase AΔN59

In this paper, ultrafiltration was employed to facilitate the isolation of intermediates in native chemical ligation. Depending on the molecular weight cutoff of the membrane used, molecules with different sizes could be purified, separated, or concentrated by the ultrafiltration process. Total chemical synthesis of the polypeptide chain of the enzyme Sortase A_ΔN59 was used as an example of the application of ultrafiltration in chemical protein synthesis. Sortase A is a ligase that catalyzes transpeptidation reactions between proteins that have C‐terminal LPXTG recognition sequence and Gly5‐ on the peptidoglycan of bacterial cell walls [3]. Ultrafiltration technique facilitated synthesis of Sortase A_ΔN59 and was a promising tool in isolation of intermediates in native chemical ligation. Copyright © 2015 European Peptide Society and John Wiley & Sons, Ltd.     

Nonaggregating refolding of ribonuclease A using reverse micellar dialysis

A hydrophilic ultrafiltration membrane, regenerated cellulose, facilitates the size-selectable permeability of hydrophilic solutes in reverse micellar solution. By using an ultrafiltration membrane with a molecular weight cutoff of 3,500, we demonstrate a nonaggregating protein refolding technique based on the dialysis of reverse micellar solution. This realizes concurrent removal of denaturants, urea and 2-mercaptoethanol, and the supply of redox reagents, reduced and oxidized glutathione (GSH, GSSG), to promote renaturation of proteins. Two mg/ml ribonuclease A (RNase A) was refolded completely without any dilution and aggregation for 60 h. The refolding behavior of RNase A is strongly influenced by the ratio of GSH and GSSG. Moreover, we recovered 90% of the refolded RNase A from AOT reverse micellar solution with acetone precipitation and beta-cyclodextrin washing. These findings should facilitate the production of a continuous protein refolding membrane reactor.     

Quantitative analysis of membrane fouling by protein mixtures using MALDI-MS

Binary aqueous solutions of bovine serum albumin (BSA) and beta-lactoglobulin (bLG) were subject to flux-stepping and constant flux ultrafiltration to identify the apparent critical flux and to study the mechanisms and factors affecting fouling when the membrane is permeable to one protein component. Membranes from these filtration experiments were analyzed using matrix-assisted laser desorption ionization mass spectrometry (MALDI-MS) to locate and quantify levels of fouling below and above the apparent critical flux. Hydrophilic (PLTK) regenerated cellulose and hydrophobic (PBTK) polysulfone asymmetric membranes were used, both of 30 kDa nominal molecular weight cut-off. For the hydrophilic PLTK membrane, protein deposition was shown to depend on electrostatic forces, exhibiting little or no fouling when the proteins had the same charge sign as that of the membrane. This was found to apply for both dilute equal mass-per-unit-volume and equimolar binary mixtures. For the PBTK membrane, hydrophobic protein-membrane attractive forces were sufficiently strong to cause deposition of bLG even in the presence of repulsive electrostatic forces. For the PBTK membrane deposition exceeded monolayer coverage below and above apparent critical flux conditions but for the PLTK membrane this generally occurred when the apparent critical flux was exceeded. MALDI-MS was shown to be a facile direct analytical technique for individually quantifying adsorbed proteins on membrane surfaces at levels as low as 50 fmol/mm(2). The high levels of compound specificity inherent to mass spectrometry make this approach especially suited to the quantification of individual components in mixed deposits. In this study, MALDI-MS was found to be successful in identifying and quantifying the protein species responsible for fouling.     

尿液蛋白富集方法的比较

人尿液中蛋白含量低,在进行质谱分析时易被高丰度蛋白掩盖。因此,发展高效和高选择性的富集方法,是实现尿蛋白标记物深度覆盖的必要前提。探究不同实验方法对尿液蛋白富集和尿蛋白质组的影响尤为重要。本研究采用超滤法、硝酸纤维素膜富集法和饱和硫酸铵沉淀法,等体积各处理5例健康志愿者和膀胱癌患者10 mL尿液样本,富集尿液蛋白,SDS-PAGE分离尿蛋白,比较不同方法纯化的效率;通过质谱分析,比较不同纯化方法的肽段鉴定效果,确定针对尿液蛋白质组蛋白的最佳富集方法。相对于超滤和硝酸纤维素膜富集法,饱和硫酸铵沉淀法成功地应用于健康人尿蛋白的富集和质谱检测,在保证回收蛋白质量的前提下,可减少高丰度白蛋白的干扰,富集更多低丰度蛋白,提高了质谱鉴定的灵敏度。综上所述,饱和硫酸铵提取尿蛋白的效果较好,该方法具有大规模处理尿液、提高蛋白质组学筛选临床诊断标记物研究的应用潜力。     

Membrane separation of protein precipitates: Studies with cross flow in hollow fibers

Hollow fiber ultrafiltration and microfiltration membranes are examined for the processing of isoelectric soya protein precipitate suspensions. A model based on the various resistances to permeate flux is used to describe membrane performance. The main resistance to permeate flux is due to the interaction between the active membrane and the soluble and precipitated protein; that is, as compared with resistances due to the active membrane itself or the membrane support structure, or arising from concentrated soluble or precipitated protein layers over the membrane surface. Soluble protein rejection and precipitate mean particle diameter are correlated with observed values of this main resistance.In contract to the ultrafiltration of soluble proteins, the flux rates observed when processing protein precipitate suspensions under a similar range of operating conditions do not approach a limiting value with increased transmembrane pressure. At high protein concentrations, greater flux rates may be achieved for precipitated as compared with soluble proteins. The use of a microfiltration membrane does not give further improvement in flux rate; this may be attributed to problems of pore fouling with precipitate particles.     

Separation albumin-PEG: transmission of PEG through ultrafiltration membranes

Transmission of polyethylene glycol (PEG) through ultrafiltration membranes has been studied under various operating conditions of pressure, crossflow, and concentration, using different membranes cut-offs and two module designs with the aim of understanding the separation of PEG from BSA. The influence of protein adsorption and fouling of the choice of a membrane has also been considered. Retention depends in general on the molecule to average pore size ratio, as expected, but also on concentration polarization. Accordingly, all operating and design parameters favoring concentration polarization lead to higher transmission. At high fluxes, flexible macromolecules can pass through the membrane, even if the random coil is larger than the apparent average pore. From a process selectivity point of view, the best way to separate PEG from BSA would be to use a membrane totally retaining BSA and to enhance concentration polarization of PEG. Unfortunately, such conditions also increase fouling and concentration polarization by BSA, which limits flux and thus PEG concentration polarization and transmission. Consequences of such conditions on separation efficiency are discussed. (c) 1993 Wiley & Sons, Inc.     

Purification of densonucleosis virus by tangential flow ultrafiltration

Purification at commercial scale of viruses and virus vectors for gene therapy applications and viral vaccines is a major separations challenge. Tangential flow ultrafiltration has been developed for protein purification. Here tangential flow ultrafiltration of parvoviruses has been investigated. Because these virus particles are small (18-26 nm), removal of host cell proteins will be challenging. The results obtained here indicate that 30, 50, and 100 kDa membranes reject the virus particles, whereas 300 kDa membranes allow some virus particles to pass into the permeate. The decrease in permeate flux for the 300 kDa ultrafiltration membrane is much greater than for the 30, 50, and 100 kDa membranes, indicating possible entrapment of virus particle in the membrane pores. The permeate flux and level of protein rejection is strongly affected by the cell culture growth medium. The results indicate that when developing a new process, it is essential that the cell culture and purification operations be developed in parallel.     

Purification of monoclonal antibodies derived from transgenic goat milk by ultrafiltration

With the goal of recovering heterologous immunoglobulin (IgG), which comprises 10-15% of the total proteins, from transgenic goat milk at 80% yield and 80% purity, we have developed and tested a two-step membrane isolation and purification process. In the first step, reported earlier by Baruah and Belfort, microfiltration was used to fractionate the milk proteins and recover > 90% of the original IgG at a purity of about 15-20% in the permeate stream. Here, we focus on ultrafiltration (UF) to increase the purity of the target protein to 80%, while maintaining a relatively high IgG yield (80%). Tangential flow UF experiments in diafiltration mode were conducted with 100 kDa cellulosic membranes to evaluate the optimal pH, ionic strength, and uniform transmembrane pressure (TMP). The TMP was kept uniform by permeate circulation in co-flow mode. The traditional approach of conducting the UF process close to the pI of the predominant whey proteins (15-40 kDa, pI 5.2), to transmit these proteins while retaining heterologous IgG (155 kDa), could not be applied here because of precipitation of residual casein at pH values lower than 8.5. Instead, the packing characteristics of the cake layer on the membrane wall, as elucidated in the Aggregate Transport Model presented by Baruah et al. was utilized to achieve a selectivity of > 15, which was sufficient to meet the stated goals of purity and yield for this difficult separation. This combined process is expected to reduce the load on subsequent purification and polishing steps for eventual therapeutic use.