Microfiltration of streptococcal fermentation broths: study of the factors affecting the concentration effect

Streptokinase (SK) recovery from streptococcal fermentation broth by cross-flow microfiltration has been studied. Recovery of SK in the filtrate, independent of the volumetric concentration factor, is approximately two-fold lower than the initial SK activity in the fermentation broth; moreover, the SK activity in the retentate increase during the process, reaching a concentration factor of 2.73. These results show that the membrane works more as an ultrafiltration membrane, with rejection of S = 0.6, than as a microfiltration membrane. Under filtration conditions, the membrane permeation rate decreased with time. This decreased could be explained by deposition and interaction of material onto/with the membrane resulting in the concentration of permeable products. Studies of the individual concentration factors for the main streptococcal exocellular proteins, indicate clearly that the concentration of the proteins during the microfiltration process is independent of the size of the proteins, suggesting that other factors, such as charge and hydrophobicity, along with concentration-polarization, should be taken also into account for the understanding of this phenomenon. (c) 1994 John Wiley & Sons, Inc.     

On-line monitoring of glucose in mammalian cell culture using a flow injection analysis (FIA) mediated biosensor

A flow injection analysis (FIA) biosensor system has been developed for on-line determination of glucose during mammalian cell cultivation. The culture sample was peristaltically withdrawn from the bioreactor and after cell separation by a steam sterilizable ceramic microfilter, the filtrate was continuously fed to the FIA mediated-biosensor system at 4 mLh(-1), whereas the cell-containing retentate was recirculated to the bioreactor. In the amperometric biosensor system, glucose oxidase was covalently immobilized onto a preactivated nylon membrane and attached to the sensing area of a platinum working electrode. The enzyme reaction was coupled with the mediator 1,1'-dimethylferricinium (DMFe(+))-cyclodextrin inclusion complex to recycle the reduced glucose oxidase to its original active state. 1,1'-Dimethylferrocene (DMFe) was then reoxidized to DMFe(+) at the surface of the platinum electrode poised at + 0.15 V vs silver/silver chloride. The FIA mediated-biosensor was linear up to 6 mM glucose, with a detection limit of 0.1 mM, and possessed excellent reproducibility (+/- 0.4 %, 95 % confidence interval) over 123 repeated analyses during a 62 h continuous operation. The immobilized glucose oxidase was stable for up to 7 days when applied to glucose measurement during 5-10 day fed-batch cultivation of 293S mammalian cells. The results obtained from the mediated-biosensor system compared well with the hexokinase and HPLC data. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 497-504, 1997.     

Growth-supporting activity for Legionella pneumophila in tap water cultures and implication of hartmannellid amoebae as growth factors.

Photosynthetic cyanobacteria, heterotrophic bacteria, free-living amoebae, and ciliated protozoa may support growth of Legionella pneumophila. Studies were done with two tap water cultures (WS1 and WS2) containing L. pneumophila and associated microbiota to characterize growth-supporting activity and assess the relative importance of the microbiota in supporting multiplication of L. pneumophila. The water cultures were incubated in the dark at 35 degrees C. The growth-supporting factor(s) was separated from each culture by filtration through 1-micron-pore-size membrane filters. The retentate was then suspended in sterile tap water. Multiplication of L. pneumophila occurred when both the retentate suspension and the filtrate from either culture were inoculated into sterile tap water. L. pneumophila did not multiply in tap water inoculated with only the filtrate, even though filtration did not reduce the concentration of L. pneumophila or heterotrophic bacteria in either culture. Growth-supporting activity of the retentate suspension from WS1 was inactivated at 60 degrees C but unaffected at 0, 25, and 45 degrees C after 30-min incubations. Filtration experiments indicated that the growth-supporting factor(s) in WS1 was 2 to 5 micron in diameter. Ciliated protozoa were not detected in either culture. Hartmannellid amoebae were conclusively demonstrated in WS2 but not in WS1. L. pneumophila multiplied in tap water inoculated with the amoebae (10(3)/ml) and the 1-micron filtrate of WS2. No multiplication occurred in tap water inoculated with the filtrate only. Growth-supporting activity for L. pneumophila may be present in plumbing systems; hartmannellid amoebae appear to be important determinants of multiplication of L. pneumophila in some tap water cultures.     

Growth-supporting activity for Legionella pneumophila in tap water cultures and implication of hartmannellid amoebae as growth factors

Photosynthetic cyanobacteria, heterotrophic bacteria, free-living amoebae, and ciliated protozoa may support growth of Legionella pneumophila. Studies were done with two tap water cultures (WS1 and WS2) containing L. pneumophila and associated microbiota to characterize growth-supporting activity and assess the relative importance of the microbiota in supporting multiplication of L. pneumophila. The water cultures were incubated in the dark at 35 degrees C. The growth-supporting factor(s) was separated from each culture by filtration through 1-micron-pore-size membrane filters. The retentate was then suspended in sterile tap water. Multiplication of L. pneumophila occurred when both the retentate suspension and the filtrate from either culture were inoculated into sterile tap water. L. pneumophila did not multiply in tap water inoculated with only the filtrate, even though filtration did not reduce the concentration of L. pneumophila or heterotrophic bacteria in either culture. Growth-supporting activity of the retentate suspension from WS1 was inactivated at 60 degrees C but unaffected at 0, 25, and 45 degrees C after 30-min incubations. Filtration experiments indicated that the growth-supporting factor(s) in WS1 was 2 to 5 micron in diameter. Ciliated protozoa were not detected in either culture. Hartmannellid amoebae were conclusively demonstrated in WS2 but not in WS1. L. pneumophila multiplied in tap water inoculated with the amoebae (10(3)/ml) and the 1-micron filtrate of WS2. No multiplication occurred in tap water inoculated with the filtrate only. Growth-supporting activity for L. pneumophila may be present in plumbing systems; hartmannellid amoebae appear to be important determinants of multiplication of L. pneumophila in some tap water cultures.     

Large scale isolation of human erythrocyte membranes by high volume molecular filtration

A molecular filtration procedure for preparing large quantities of human erythrocyte ghost membranes is presented. Hemolysate ghost membranes are rapidly cycled in the retantate channel of the filtration apparatus, while hemoglobin is removed s it pass through Pellicon filters into the filtrate. Several-liter quantities of washed packed erythrocytes can be processed in a few hours with this system and the filtration procedure does not appear to alter erythrocyte or ghost membranes. Intact erythrocytes in isotonic solution can be circulated through the retentate channel for 16 h with only 3% hemolysis and with preservation of their orginal morphology in scanning electron microscopy. Ghost membranes isolated by the procedure are virtually identical in morphology, polypeptide composition and acetylcholinesterase content to membranes isolated by conventional centrifugation techniques.     

High performance tangential flow filtration

Conventional tangential flow filtration (TFF) has traditionally been limited to separation of solutes that differ by about ten-fold in size. Wide pore-size distributions, membrane fouling, and concentration polarization phenomena have commonly been cited as reasons for this limitation. The use of TFF in the biotechnology industry has therefore been restricted to cell-protein, virus-protein, and protein-buffer separations. A multi-disciplinary team with industrial and academic members was formed to overcome these limitations and enable protein-protein separations using High Performance TFF (HPTFF) systems. Pore-size distributions have been improved with the development of new membrane formulation and casting techniques. Membrane fouling has been controlled by operating in the transmembrane pressure-dependent regime of the filtrate flux curve and by carefully controlling fluid dynamic start-up conditions. Concentration polarization was exploited to enhance, rather than limit, the resolution of solutes. Concentration polarization has also been controlled by operating a co-current filtrate stream that maintains transmembrane pressure constant along the length of the TFF module. High yields and purification factors were obtained even with small differences in protein sieving. IgG-BSA and BSA monomer-oligomer mixtures have successfully been separated with these systems. HPTFF technology provides a competitive purification tool to complement chromatographic processing of proteins. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 56: 71-82, 1997.     

Zonal rate model for axial and radial flow membrane chromatography,part II: Model‐based scale‐up

Membrane chromatography (MC) systems are finding increasing use in downstream processing trains for therapeutic proteins due to the unique mass‐transfer characteristics they provide. As a result, there is increased need for model‐based methods to scale‐up MC units using data collected on a scaled‐down unit. Here, a strategy is presented for MC unit scale‐up using the zonal rate model (ZRM). The ZRM partitions an MC unit into virtual flow zones to account for deviations from ideal plug‐flow behavior. To permit scale‐up, it is first configured for the specific device geometry and flow profiles within the scaled‐down unit so as to achieve decoupling of flow and binding related non‐idealities. The ZRM is then configured for the preparative‐scale unit, which typically utilizes markedly different flow manifolds and membrane architecture. Breakthrough is first analyzed in both units under non‐binding conditions using an inexpensive tracer to independently determine unit geometry related parameters of the ZRM. Binding related parameters are then determined from breakthrough data on the scaled‐down MC capsule to minimize sample requirements. Model‐based scale‐up may then be performed to predict band broadening and breakthrough curves on the preparative‐scale unit. Here, the approach is shown to be valid when the Pall XT140 and XT5 capsules serve as the preparative and scaled‐down units, respectively. In this case, scale‐up is facilitated by our finding that the distribution of linear velocities through the membrane in the XT140 capsule is independent of the feed flow rate and the type of protein transmitted. Introduction of this finding into the ZRM permits quantitative predictions of breakthrough over a range of industrially relevant operating conditions. Biotechnol. Bioeng. 2014;111: 1587–1594. © 2014 Wiley Periodicals, Inc.     

Separation of alpha-lactalbumin and beta-lactoglobulin using membrane ultrafiltration

There is considerable commercial interest in the preparation of individual whey proteins as high-value food additives, nutraceuticals, and therapeutics. This study examined the use of membrane filtration for the separation of alpha-lactalbumin and beta-lactoglobulin. Stirred cell filtration experiments were performed using both cellulosic and polyethersulfone membranes to determine the optimal pH, ionic strength, and filtration conditions. Selectivities of greater than 55 could be achieved at pH 5.5 and 50 mM ionic strength using a 30-kD cellulose membrane. A diafiltration process was then designed for the protein separation. A 16-diavolume filtration yielded beta-lactoglobulin as the retentate product with a purification factor of 100 and recovery of 90%. The alpha-lactalbumin was recovered in the filtrate with a purification factor of more than 10 and nearly 99% yield. Model calculations were in good agreement with the experimental data.     

Optimizing the rotor design for controlled-shear affinity filtration using computational fluid dynamics

Controlled shear affinity filtration (CSAF) is a novel integrated processing technology that positions a rotor directly above an affinity membrane chromatography column to permit protein capture and purification directly from cell culture. The conical rotor is intended to provide a uniform and tunable shear stress at the membrane surface that inhibits membrane fouling and cell cake formation by providing a hydrodynamic force away from and a drag force parallel to the membrane surface. Computational fluid dynamics (CFD) simulations are used to show that the rotor in the original CSAF device (Vogel et al., 2002) does not provide uniform shear stress at the membrane surface. This results in the need to operate the system at unnecessarily high rotor speeds to reach a required shear stress of at least 0.17 Pa at every radial position of the membrane surface, compromising the scale-up of the technology. Results from CFD simulations are compared with particle image velocimetry (PIV) experiments and a numerical solution for low Reynolds number conditions to confirm that our CFD model accurately describes the hydrodynamics in the rotor chamber of the CSAF device over a range of rotor velocities, filtrate fluxes, and (both laminar and turbulent) retentate flows. CFD simulations were then carried out in combination with a root-finding method to optimize the shape of the CSAF rotor. The optimized rotor geometry produces a nearly constant shear stress of 0.17 Pa at a rotational velocity of 250 rpm, 60% lower than the original CSAF design. This permits the optimized CSAF device to be scaled up to a maximum rotor diameter 2.5 times larger than is permissible in the original device, thereby providing more than a sixfold increase in volumetric throughput.     

Synthesis and characterization of a water-soluble affinity polymer for trypsin purification

A specific ligand bound polymer has been synthesized for the purpose of purification and stabilization of trypsin, an easily autodigestible enzyme. The affinity polymer was formed by copolymerizing N-acryloyl-m-aminobenzamidine, a strong trypsin inhibitor, and acrylamide in the absence of oxygen. Kinetic studies on the trypsin inhibition revealed that there was a strong binding between this enzyme and the polymer and the mechanism was of a competitive manner with an inhibition constant of 0.6 x 10(-3)M. Such an affinity polymer was also very effective in preventing trypsin from auto-digestion at 4 degrees C.Based on this finding and the principle of cross flow filtration, a new process has been developed for purification of trypsin from a solution containing chymotrypsin. The experimental data indicated that trypsin was bound to the polymer (MW > 10(5)) and remained in the retentate while unbound chymotrypsin was collected in the filtrate. This purification process has a capability of recovering 98% pure trypsin at 90% yield.     

Vortex flow filtration of mammalian and insect cells

The use of vortex flow filtration for harvesting cells or conditioned medium from large scale bioreactors has proven to be an efficient, low shear method of cell concentration and conditioned medium clarification. Several 8–10 L batches of the human histiocytic lymphoma U-937 cell line (ATCC CRL 1593) were concentrated to less than 1 L by vortex flow filtration through a 3.0 m membrane. An aggressive filtration regimen caused a 17% loss of cell viability and a 32% loss of IL-4 receptor binding capacity when compared to a batch centrifuged control. A reduction of the rotor speed from 1500 to 500 RPM and reduction of system back pressure from 10 to 0 PSIG resulted in cell viability and IL-4 binding capacity comparable to the control. Several 10 L batches of baculovirus infected Sf-9 cells were also concentrated to less than 1 L by vortex flow filtration through a 3.0 m membrane. SDS-PAGE analysis of filtrate samples showed that aggressive filtration caused cell damage which led to contamination of the process stream by cellular lysate. When rotor speed was reduced to 500 RPM and system back pressure was reduced to 0 PSIG, the amount of contaminating lysate proteins in filtrate samples was comparable to a batch centrifuged control.     

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.     

Biocatalytic membranes for ultrafiltration treatment of wastewater containing dyes

A possibility to prepare the biofunctional membranes showing the biocatalytic properties and use those in post-treatment of wastewater containing synthetic dyes have been established. Selected Pseudomonas mendocina and Bacillus subtilis cultures were used as biocatalysts for dye destruction. It has been established that cells in spore form are able to survive in N-methylpyrrolidone that allow to use method of polymer solution casting for membrane preparation. The optimal conditions for entrapping of whole cells of microorganisms into the polymer matrix have been determined. Membrane biocatalytic activity has been studied depending on method of casting solution preparation, biocatalyst loading and operating parameters. Dye destruction occurs both in membrane pores and on membrane surface. Membrane obtained provide discolouring of treated solutions (permeate). The dye concentration in retentate depends on the trans-membrane fluxes. The concentration in retentate need not be observed at relatively low fluxes (up to 20 l/m² h).     

Viability of an ectomycorrhizal fungus during cross-flow filtration

Factors affecting the viability and infectivity of an ectomycorrhizal fungus during moderate concentration by cross-flow filtration were determined. Mycelial suspensions were concentrated with three commercial membrane filters (Prostak Millipore Co., M14 Tech-Sep Co. and Ceraflo Norton Co.) under aseptic conditions. Medium components may reduce the filtration rate due to their low solubility. An antifoam agent did not reduce the average flux rates as much as did the malt extract. Clear unobstructed channels (I.D. 6mm) of the tubular modules (Tech-Sep) gave the best results both in terms of performance (filtration rate) and cell viability. Shear stresses caused by pumping and flow through narrow retentate channels were probably responsible for lowering viability and infectivity. There was no linear relationship between permeate fluxes and cell concentration. There is an optimum pore size both in terms of performance (filtration rate) and cell viability. Physical blockage of large pores by hyphae could explain lower permeate flux rates than those obtained with lower pore sizes membranes.     

Product concentration during tangential-flow microfiltration

Summary Clarification of fermentation broths by TFMF has been studied using new and “old” membranes. Efficient recovery of SK in the filtrate by simple TFMF process was not possible, 41.9% of the activity remains in the retentate. In situ washes do not solve the problem. Total recovery implies centrifugation of the retentate.     

Investigation of the parameters affecting the separation of bacterial enzymes from cell debris by tangential flow filtration

The effect of organism, enzyme, method of cell breakage and membrane characteristics on the separation of bacterial enzymes from cell debris by tangential flow filtration has been studied. The effectiveness of separation was assessed by process time, enzyme yield and specific activity, and turbidity of the filtrate. For a particular organism and enzyme, method of cell breakage and membrane characteristics significantly influenced separation performance, though results indicate that it is not yet possible to optimize all aspects of performance simultaneously.     

High pressure disruption of yeast cells: The use of scale down operations for the prediction of protein release and cell debris size distribution

Experiments were carried out aimed at establishing the effects of equipment scale down on the disruption of Baker's yeast cells in high pressure homogenisers. Data are reported on the cell debris particle size distribution (PSD) and on total protein release as a function of the applied pressure for two valve geometries and three scales of operation covering flow rates of 28, 60 and 280 L/h. A comparison of the results from the experiments indicates that over the range of parameters investigated both the total protein release and the cell debris PSDs are independent of valve geometry and flow rate through the homogeniser. These observations are discussed in the light of relevant previous publications. The cell debris PSDs have been simulated by using a recently published model and the total protein release data are described by the well-established Hetherington expression (Hetherington et al., 1971). (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 642-649, 1997.     

Removal of RNA impurities by tangential flow filtration in an RNase-free plasmid DNA purification process

Addition of animal-derived ribonuclease A to degrade RNA impurities is not recommended in the manufacture of pharmaceutical-grade plasmid DNA. Tangential flow filtration (TFF) takes advantage of the significant size difference between RNA and plasmid DNA to remove RNA in the permeate while plasmid remains in the retentate, in an RNase-free plasmid purification process. Operating conditions including transmembrane pressure, membrane pore size, conductivity of the diafiltration buffer, and plasmid load on the membrane were investigated to maximize RNA clearance. Although direct TFF of clarified lysate removed substantial amounts of RNA, the RNA levels left in the retentate were still significant. Calcium chloride is a potent precipitant of high-molecular-weight RNA. The addition of calcium chloride to the clarified lysate combined with the clearance of low-molecular-weight RNA by TFF resulted in complete RNA removal and high plasmid recovery.     

Further investigations of red cell deformability with nickel mesh

Although the filtration method has been widely employed in red cell deformability studies, the structural irregularity of the pores of a Nuclepore polycarbonate membrane has always been a major problem. Anegawa, T. et al. (Clin. Hemorheol., 7, 1987) obtained a higher reproducibility with the filtration method using a newly designed thin metal film with pores engraved by the photofabrication technique. We further studied the pressure - flow rate relationship of red cell suspension employing this nickel mesh. The filtration of red cell suspensions through the nickel mesh was not influenced by leukocytes contamination or added leukocytes up to a leukocyte count of 250 cells/mm3 within an experimental limitation. On the other hand, the flow was greatly influenced by leukocytes contamination when the polycarbonate membrane was used. The nickel mesh was found to be useful in detecting major determinants of red cell deformability, such as cell geometry and internal cellular viscosity, and in detecting abnormalities of red cell deformability in a patient with microangiopathic hemolytic anemia. In conclusion, the present study clearly shows that the nickel mesh is preferable for investigating red cell deformability to the polycarbonate membrane from a quantitative point of view. This material should contribute to the physiologic and clinical investigation of red cell deformability.     

Evaluation of performance of white blood cell reduction filters: an original flow cytometric method for detection and quantification of cell-derived membrane fragments.

BACKGROUND: Contamination of blood products by white blood cells leads to a risk of transmission of infectious agents, particularly abnormal prion protein, the probable causative agent of new-variant Creutzfeldt-Jakob disease. Blood product filtration could reduce this risk, but the filtration systems might generate potentially infectious membrane fragments. We developed an original flow cytometric method that allows the detection and quantification of membrane fragments in filtered products and the evaluation of the quantity of destroyed cells. METHODS: This method has four technical requirements: cytofluorometric acquisition of forward scatter parameters on a log scale, use of a fluorescent aliphatic reporter molecule (PKH26-GL) to identify membrane fragments, quantification with fluorescent beads, and the drawing up of a standard curve on the basis of cells destroyed by freezing/thawing to generate cell debris (i.e., quantity of membrane fragments measured versus quantity of destroyed cells). RESULTS AND CONCLUSIONS: This original method can be used to test new filtration devices and it allows optimization of the filtration process or comparison of different filtration systems. We tested the method with three commercial white cell removal filters. We demonstrated that it is possible to evaluate the filter quality, particularly the likelihood of fragment removal during the filtration process.