Effects of intermolecular thiol-disulfide interchange reactions on bsa fouling during microfiltration

Several studies have shown that one of the critical factors governing protein fouling of microfiltration membranes is the presence of denaturedand/or aggregated protein in the bulk solutions. Experiments were performed to evaluate the role of intermolecular disulfide interchange reactionson protein aggregation and membrane fouling during stirred cell microfiltration of bovine serum albumin (BSA). The flux decline during BSA filtration was quite dramatic due to the formation of a protein deposit thatfully covered the membrane pores. This flux decline could be completely eliminated by capping the free sulfhydryl group present on the BSA with eithera carboxymethyl or cysteinyl group, demonstrating the critical importance of this free thiol in the intermolecular aggregation reactions and, in turn, protein fouling. BSA aggregation during storage could be reduced by the addition of metal chelators (EDTA and citrate) or dithiothreitol, orby storage at lower pH (7.0) these solutions all had a significantly lower rate of fouling upon subsequent filtration. This behavior is completely consistent with the known chemistry of the thiol-disulfide interchange reaction, demonstrating that an understanding of these intermolecular (aggregation) reactions can provide a rational framework for the analysis and control of protein fouling in these membrane systems. (c) 1994 John Wiley & Sons, Inc.     

Membrane fouling by cell-protein mixtures: in situ characterisation using multi-photon microscopy

Fouling of the membrane by cell and protein mixtures can result in severe flux declines, leading to the eventual need to clean or replace the membrane. In this study multi-photon microscopy, a fluorescence-based technique is used to 3-D image in situ the fouling of microfiltration membranes by suspensions containing combinations of washed yeast, bovine serum albumin (BSA) and ovalbumin. Appropriate fluorescent labelling allows the three foulant species to be clearly identified. Images correlate well with filtration data and clearly show the cake of yeast cells capturing protein aggregates. The proteins exhibited very different filtration behaviour. When filtering washed yeast together with ovalbumin and/or a 50:50 mixture by mass of BSA and ovalbumin, the ovalbumin fouling dominates the system. Capture of aggregates by the cake did not reduce fouling of the membrane by the protein and increased the resistance of the cake. For mixtures of BSA and washed yeast, the presence of a cake of yeast cells did reduce fouling of the membrane by the protein, however, the extra resistance due to the cake resulted in a flux lower than that when filtering BSA alone.     

Protein fouling of virus filtration membranes: effects of membrane orientation and operating conditions

The capacity of virus filters used in the purification of therapeutic proteins is determined by the rate and extent of membrane fouling. Current virus filtration membranes have a complex multilayer structure that can be used with either the skin-side up or with the skin-side facing away from the feed, but there is currently no quantitative understanding of the effects of membrane orientation or operating conditions on the filtration performance. Experiments were performed using Millipore's Viresolve 180 membrane under both constant pressure and constant flux operation with sulfhydryl-modified BSA used as a model protein. The capacity with the skin-side up was greater during operation with constant flux and at low transmembrane pressures, with the flux decline or pressure rise due primarily to osmotic pressure effects. In contrast, data obtained with the skin-side down showed a slower, steady increase in total resistance with the cumulative filtrate volume, with minimal contribution from osmotic pressure. The capacity with the skin-side down was significantly greater than that with the skin-side up, reflecting the different fouling mechanisms in the different membrane orientations. These results provide important insights for the design and operation of virus filtration membranes.     

Membrane fouling in sterile filtration of recombinant human growth hormone

The most troublesome problem encountered during the sterile filtration of protein solutions is membrane fouling. This article presents our study on sterile filtration of a model protein, recombinant human growth hormone (rhGH). Scanning electron microscopy (SEM) analysis shows that 0.22-mum membranes, when used to filter the mannitol-formulated protein solution under a 0.35-bar transmembrane pressure, were plugged to a great extent. When zinc ions were added to induce aggregates, the fouling tendency of rhGH solutions increased with increasing amount and size of the aggregates, indicating that the aggregates present before filtration might be responsible for membrane fouling. However, repeated filtration of the same solution using a fresh filter each time cannot reduce membrane fouling, and all filtrates contain the same trace amount of hGH particulates as the prefiltered solution. Particulate size was determined to be between 0.03 and 0.15 mum by dynamic light scattering. Also, in view of the fact that protein formulations significantly affected the tendency of fouling with the same preexisting aggregates, it is likely that fouling was more attributed to the aggregation taking place in the filter pores during filtration (secondary aggregation) than to the aggregates present before filtration. Adding a surfactant to or increasing the pH of the protein solution improves the filtration, whereas increasing ionic strength slows down the filtration. This result suggests that the balance of the protein's interaction and electrostatic repulsion plays an important role in the protein's fouling tendency. Many factors might change the microenvironment in the pores and disturb this balance. Those considerations and the aggregation tendency of rhGH in the filter pores will be discussed in detail separately. (c) 1996 John Wiley & Sons, Inc.     

Evaluation of membranes for use in on-line cell separation during mammalian cell perfusion processes

In this study two microporous hollow fibre membranes were evaluated for their use as cell retention device in continuous perfusion systems. A chemically modified permanent hydrophillic PTFE membrane and a hydrophilized PP membrane were tested. To investigate the filtration characteristics under process conditions each membrane was tested during a long term perfusion cultivation of a hybridoma cell line. In both cultivations the conditions influencing membrane filtration (e.g. transmembrane flux) were kept constant. Filtration behaviour was investigated by monitoring transmembrane pressure and protein permeability. Transmembrane pressure was measured on-line with an autoclavable piezo-resistive pressure sensor. Protein permeability was determined by quantitative evaluation of unreduced, Coomassie stained SDS-PAGE. The membrane fouling process influences the filtration characteristics of both membranes in a different way. After fermentation the PP membrane was blocked by a thick gel layer located in the big outer pores of the asymmetric membrane structure. The hydraulic resistance was higher but the protein permeability was slightly better than of the PTFE membrane. For this reason the PP membrane should be preferred. On the other hand, transmembrane pressure decreases slower when the PTFE membrane is used, which favours this membrane for long term cultivations, especially when low molecular weight proteins (<30 KD) are produced.Abbreviations PP Polypropylene - PTFE Polytetrafluoroethylene     

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.     

Paper-PEG-based membranes for hydrophobic interaction chromatography: purification of monoclonal antibody

This article discusses the preparation of novel Paper-PEG interpenetrating polymer network-based membranes as inexpensive alternative to currently available adsorptive membranes. The Paper-PEG membranes were developed for carrying out hydrophobic interaction membrane chromatography (HIMC). PEG is normally very hydrophilic but can undergo phase separation and become hydrophobic in the presence of high antichaotropic salt concentrations. Two variants of the Paper-PEG membranes, Paper-PEG 1 and Paper-PEG 2 were prepared by grafting different amounts of the polymer on filter paper and these were tested for their hydraulic properties and antibody binding capacity. The better of the two membranes (Paper-PEG 1) was then used for purifying the monoclonal antibody hIgG1-CD4 from simulated mammalian cell culture supernatant. The processing conditions required for purification were systematically optimized. The dynamic antibody binding capacity of the Paper-PEG 1 membrane was about 9 mg/mL of bed volume. A single step membrane chromatographic process using Paper-PEG 1 membrane gave high monoclonal antibody purity and recovery. The hydraulic permeability of the paper-based membrane was high and was maintained even after many runs, indicating that membrane fouling was negligible and the membrane was largely incompressible.     

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.     

Water quality and daily temperature cycle affect biofilm formation in drip irrigation devices revealed by optical coherence tomography

Drip irrigation is a water-saving technology. To date, little is known about how biofilm forms in drippers of irrigation systems. In this study, the internal dripper geometry was recreated in 3-D printed microfluidic devices (MFDs). To mimic the temperature conditions in (semi-) arid areas, experiments were conducted in a temperature controlled box between 20 and 50°C. MFDs were either fed with two different treated wastewater (TWW) or synthetic wastewater. Biofilm formation was monitored non-invasively and in situ by optical coherence tomography (OCT). 3-D OCT datasets reveal the major fouling position and illustrate that biofilm development was influenced by fluid dynamics. Biofilm volumetric coverage of the labyrinth up to 60% did not reduce the discharge rate, whereas a further increase to 80% reduced the discharge rate by 50%. Moreover, the biofilm formation rate was significantly inhibited in daily temperature cycle independent of the cultivation medium used.     

Magnetization influence on the performance of ferrosoferric oxide: polyacrylonitrile membranes in ultrafiltration of pig blood solution

Three kinds of membranes were prepared from suspensions containing polyacrylonitrile, dimethyl sulfoxide, polyethylene glycol and different amount of Fe₃O₄ by the phase inversion process. The rejection rate and the flux of membrane were investigated in the filtration of pig blood solution. SEM also studied the morphologies of fouled membranes. The permeate flux and the rejection rate decline fast in the initial several minutes and then change slowly. The magnetized membrane has a higher flux and a relative flux than the corresponding non-magnetized membrane. And the magnetized membrane containing about 3 wt% Fe₃O₄ has a prominent anti-fouling performance with above 52% relative flux. The results indicate that the magnetized ferrosoferric oxide–polyacrylonitrile membranes are promising in the recovery of blood proteins in the slaughterhouse effluents. In addition, the hydraulic resistance model explained results and the fouling mechanism was also given.The National Natural Science Foundation of China (Project No.20476023) and the Education Department of Hubei Province (Project No. 2001A02003) funded this work.     

Impact of antibody aggregation on a flowthrough anion‐exchange membrane process

The impact of typical anion‐exchange flowthrough conditions on the IgG mass loading of an anion‐exchange membrane scale‐down unit (Mustang® Q coin) was investigated. High performance size‐exclusion chromatography and multiangle laser light scattering results suggested the presence of a small fraction of IgG aggregates with average radius >100 nm under anion‐exchange flowthrough conditions. The small filtration area presented by the 0.35 mL membrane volume Mustang® Q coin limited the membrane throughput due to fouling from the aggregates at higher antibody loading. Data in this report indicated that a 0.2 μm hybrid polyethersulfone and polyvinylidene fluoride membrane in‐line prefilter with a minimum filtration area of 20 sq cm alleviated the Mustang® Q coin fouling. The combined cake filtration and intermediate blocking model was proposed as the most likely membrane pore blocking mechanism. Increasing the filtration area in the in‐line prefilter resulted in higher IgG mass throughput. Thus, using an appropriately sized in‐line prefilter could provide more robust antibody throughput performance on scale‐down membrane anion‐exchange units. © 2010 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

Removal versus fragmentation of amyloid-forming precursors via membrane filtration

The presence of even minute amounts of protein aggregates in solution can significantly alter the kinetics of amyloid formation. Removal of such pre-existing aggregates is critical for reproducible analysis of amyloid formation. Here we examine the effects of membrane filtration on insulin fibrillization. We find that filtration of insulin with large pore membranes (≥ 100 nm) generally slows fibril formation relative to unfiltered solutions by removing pre-aggregated protein. Unexpectedly, filtration with small pore membranes (< 100 nm) showed no beneficial effect and, in some cases, accelerated insulin fibril formation. This effect may be due to fragmentation of pre-existing aggregates during filtration through small pore membranes, which can increase the number of amyloid-forming precursors. These findings reveal the complexity of removing protein aggregates via filtration and suggest optimal filtration protocols for conducting fibril formation analysis of insulin and similar amyloidogenic proteins.     

Virus harvesting in perfusion culture: Choosing the right type of hollow fiber membrane

The use of bioreactors coupled to membrane-based perfusion systems enables very high cell and product concentrations in vaccine and viral vector manufacturing. Many virus particles, however, are not stable and either lose their infectivity or physically degrade resulting in significant product losses if not harvested continuously. Even hollow fiber membranes with a nominal pore size of 0.2 µm can retain much smaller virions within a bioreactor. Here, we report on a systematic study to characterize structural and physicochemical membrane properties with respect to filter fouling and harvesting of yellow fever virus (YFV; ~50 nm). In tangential flow filtration perfusion experiments, we observed that YFV retention was only marginally determined by nominal but by effective pore sizes depending on filter fouling. Evaluation of scanning electron microscope images indicated that filter fouling can be reduced significantly by choosing membranes with (i) a flat inner surface (low boundary layer thickness), (ii) a smooth material structure (reduced deposition), (iii) a high porosity (high transmembrane flux), (iv) a distinct pore size distribution (well-defined pore selectivity), and (v) an increased fiber wall thickness (larger effective surface area). Lowest filter fouling was observed with polysulfone (PS) membranes. While the use of a small-pore PS membrane (0.08 µm) allowed to fully retain YFV within the bioreactor, continuous product harvesting was achieved with the large-pore PS membrane (0.34 µm). Due to the low protein rejection of the latter, this membrane type could also be of interest for other applications, that is, recombinant protein production in perfusion cultures.     

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.     

Filtration-based perfusion of hybridoma cultures in protein-free medium: Reduction of membrane fouling by medium supplementation with DNase I

In this study, a filtration-based perfusion process was developed for the production of monoclonal antibodies (IgM) by suspended hybridoma cells grown in protein-free medium. It was found that the use of protein-free medium for perfusion culture generated the formation of numerous visible suspended particles consisting of dead cells and cellular debris aggregated into fibrous material. Surprisingly high apparent viabilities were observed in such protein-free cultures. In addition, membrane fouling occurred more rapidly in protein-free medium than in conventional serum-supplemented medium. By the addition of deoxyribonuclease I (DNase I) to the protein-free medium, it was possible to prevent the formation of aggregates and to follow the evolution of the total cell population more accurately. Moreover, DNase I significantly reduced the fouling of filtration membranes, and that, for two different types of separation systems (cross-flow and vortex-flow filtration) and two different types of membranes (polycarbonate and hydrophilized polysultone). From these results, it is clear that the presence of DNA fragments liberated following cellular death is playing an important role in membrane fouling. Longevity of filtration membranes was found to be considerably greater using a vortex-flow filtration module than with a static plate-and-frame cross-flow filtration module. The use of vortex-flow filtration of conjuction with DNase I allowed maintenance of perfusion cultures for more than 1 month without membrane fouling or antibody retention and with a constant permeate IgM concentration of 250 mg/L. Hybridomacells appeared to gradually adapt to increasing rotational speed in the vortex-flow filtration module.     

CFD-aided design of a dynamic filter for mammalian cell separation

In the present work, a rotating disk filter was designed for mammalian cell separation with the aim of avoiding both cell damage and membrane fouling. Different geometric and operational variables of the rotating disk filter were studied using computational fluid dynamics (CFD) by varying rotor radius, rotor angle, membrane-rotor distance, and angular velocity. The combinations of these variables followed a statistical design, so that an analysis of the CFD results provided correlations describing the average shear stress on the membrane surface and the maximum shear stress in the whole module as a function of the variables studied. Based on these correlations, and on the shear resistance levels of Chinese hamster ovary (CHO) and baby hamster kidney (BHK) cell lines, which were investigated using a cone-and-plate viscosimeter, it was possible to determine the geometry and angular velocity that would minimize both cell damage and membrane fouling. After construction, the filter was tested in filtration experiments at increasing permeate fluxes. Cell viability remained >90% for the duration of the experiments (2.5 h), and no indication of fouling was observed. It was shown that the designed dynamic filter is able to effectively avoid both cell damage and membrane fouling, and thus can be used for mammalian cell harvesting and perfusion.     

Selective protein separations using Formed-In-Place anion exchange membranes.

Anion exchange membranes prepared by adsorption of polymers on Formed-In-Place microfiltration substrates were formed and ion-exchange separations of solutions containing two proteins were determined by ion exchange membrane sequential separation procedures, similar to affinity membrane separation procedures. Representative ion exchange separation processes utilizing adsorbed poly(ethylene imine) (PEI) as the ion exchange membrane for the separation of the components of solutions containing two proteins, bovine serum albumin (BSA) and lysozyme and ovalbumin and lysozyme, are described. The stability of the PEI adsorbed layer, binding characteristics of the BSA to the membrane and purification properties of the procedure were determined.     

Effect of protein fouling on filtrate flux and virus breakthrough behaviors during virus filtration process

Virus filtration process is used to ensure viral safety in the biopharmaceutical downstream processes with high virus removal capacity (i.e., >4 log₁₀). However, it is still constrained by protein fouling, which results in reduced filtration capacity and possible virus breakthrough. This study investigated the effects of protein fouling on filtrate flux and virus breakthrough using commercial membranes that had different symmetricity, nominal pore size, and pore size gradients. Flux decay tendency due to protein fouling was influenced by hydrodynamic drag force and protein concentration. As the results of prediction with the classical fouling model, standard blocking was suitable for most virus filters. Undesired virus breakthrough was observed in the membranes having relatively a large pore diameter of the retentive region. The study found that elevated levels of protein solution reduced virus removal performance. However, the impact of prefouled membranes was minimal. These findings shed light on the factors that influence protein fouling during the virus filtration process of biopharmaceutical production.     

Evidence for a water-soluble intermediate in exchange of cholesterol between membranes

The mechanism of inter-membrane cholesterol exchange has been a matter of some debate. Evidence from kinetic studies indicates that cholesterol must transfer to and from membranes in a water-soluble form. In this study attempts have been made to demonstrate that this occurs using either dialysis membranes or a barrierless multiphase polymer system to physically separate the membranes. In both systems small amounts of cholesterol were seen to transfer from one membrane pool to another using both liposomes and erythrocyte membranes as donors or acceptors. The cholesterol transfer was shown to be independent of the movement of other membrane components. The amount of transfer observed was limited by the physical properties of the systems employed. The barrier to cholesterol transfer in the dialysis membrane system is primarily the pore size of the membrane, while in the multiphase polymer system the transfer was limited by the viscosity of the medium and the distance between the lower and upper phases containing the membranes. Nevertheless, the results provide evidence that cholesterol transfer is by a dissociation of molecules from membranes into the aqueous medium and does not require the formation of a collision complex between the membranes.     

Trypsin-enabled construction of anti-fouling and self-cleaning polyethersulfone membrane

Constructing anti-fouling and self-cleaning membrane surfaces based on covalent attachment of trypsin on poly(methacrylic acid)-graft-polyethersulfone (PMAA-g-PES) membrane was reported. The carboxylic acid groups enriched on asymmetric PMAA-g-PES membrane surface were activated with 1-ethyl-(3-3-dimethylaminopropyl)-carbodiimide hydrochloride (EDC)/N-hydroxysuccinimide (NHS) and employed as chemical anchors for the conjugation with amino groups of trypsin. Activity assays showed that such chemically immobilized trypsin was much more active and stable than that of the physically adsorbed counterpart. Trypsin covalently attached on membrane surface could substantially resist protein fouling in dynamic flow process. The considerable enhancement of protein solution permeation flux was observed as a consequence of rapid enzymatic degradation of protein deposited onto membrane surface. The permeation flux of the membrane could be recovered upon simple hydraulic flush after protein filtration, suggesting superior self-cleaning property. After multi-cycle BSA filtration over 15-day period, the active self-cleaning membrane maintained more than 95.0% of its initial flux.