Clarified Cell Culture Research Articles

Kinetic plots in aqueous size exclusion chromatography of monoclonal antibodies and virus particles

The growing importance of monoclonal antibodies and virus particles has led to a pressure for faster size exclusion chromatography. In recent years, numerous small particle columns for size exclusion chromatography of biologicals have been introduced. Small particles are a strategy to reduce analysis time. In the following study, opportunities of small particles in size exclusion chromatography of large biomolecules are investigated. Poppe plots reveal that the lower particle size limit depends on the size of the sample molecule. Hydrodynamic radii of monoclonal antibody monomer, aggregates and H1N1 as well as the diffusion coefficients were determined. Considering this sample compound dependency, kinetic plots referring to the resolution of a distinct compound pair instead of the plate number of a single analyte are more meaningful. Plate times were found to be equivalent with 4 and 2μm particles for a monoclonal antibody aggregate separation at resolutions smaller than 1.8. Quantification of a H1N1 in clarified cell culture can be accomplished with 17μm and 13μm particles at equal plate times at resolutions smaller than 2.5. Virus polydispersity is likely to be affected by run times of several hours at room temperature and shear forces resulting from particles smaller than 10μm. Comparatively high flow rates should be applied in size exclusion chromatography of the 100nm H1N1 virions.

Evaluation of predictive tools for cell culture clarification performance.

Recent advances in the productivity of industrial mammalian cell culture processes have resulted in part in increased cell density. This increase and the associated increase in cellular debris are known to challenge harvest operations, however this understanding is limited and largely qualitative. Part of the issue arises from the heterogeneous size and composition of cellular debris, which makes harvest feed stream extremely difficult to characterize. Improved characterization methods would facilitate the development of clarification approaches that are consistent and scalable. This work describes how both particle size and cholesterol analysis can be used to characterize the feed stream. Particle size analysis by focused beam reflectance and dynamic light scattering are shown to be predictive of centrate filterability under certain harvest conditions. Because of the particle size range limitations of each detector, their applicability is limited to a particular stage or method of clarification. The measurement of cholesterol present in the cell culture supernatant or centrate was successfully used in providing relative amount of lysed cellular debris and enabled us to predict clarification performance of acid precipitated harvest regardless of particle size distribution profile.

Purification of monoclonal antibodies from clarified cell culture fluid using Protein A capture continuous countercurrent tangential chromatography

Recent studies using simple model systems have demonstrated that continuous countercurrent tangential chromatography (CCTC) has the potential to overcome many of the limitations of conventional Protein A chromatography using packed columns. The objective of this work was to optimize and implement a CCTC system for monoclonal antibody purification from clarified Chinese Hamster Ovary (CHO) cell culture fluid using a commercial Protein A resin. Several improvements were introduced to the previous CCTC system including the use of retentate pumps to maintain stable resin concentrations in the flowing slurry, the elimination of a slurry holding tank to improve productivity, and the introduction of an “after binder” to the binding step to increase antibody recovery. A kinetic binding model was developed to estimate the required residence times in the multi-stage binding step to optimize yield and productivity. Data were obtained by purifying two commercial antibodies from two different manufactures, one with low titer (∼0.67g/L) and one with high titer (∼6.9g/L), demonstrating the versatility of the CCTC system. Host cell protein removal, antibody yields and purities were similar to those obtained with conventional column chromatography; however, the CCTC system showed much higher productivity. These results clearly demonstrate the capabilities of continuous countercurrent tangential chromatography for the commercial purification of monoclonal antibody products.

Process cost and facility considerations in the selection of primary cell culture clarification technology

The bioreactor volume delineating the selection of primary clarification technology is not always easily defined. Development of a commercial scale process for the manufacture of therapeutic proteins requires scale-up from a few liters to thousands of liters. While the separation techniques used for protein purification are largely conserved across scales, the separation techniques for primary cell culture clarification vary with scale. Process models were developed to compare monoclonal antibody production costs using two cell culture clarification technologies. One process model was created for cell culture clarification by disc stack centrifugation with depth filtration. A second process model was created for clarification by multi-stage depth filtration. Analyses were performed to examine the influence of bioreactor volume, product titer, depth filter capacity, and facility utilization on overall operating costs. At bioreactor volumes <1,000 L, clarification using multi-stage depth filtration offers cost savings compared to clarification using centrifugation. For bioreactor volumes >5,000 L, clarification using centrifugation followed by depth filtration offers significant cost savings. For bioreactor volumes of ∼ 2,000 L, clarification costs are similar between depth filtration and centrifugation. At this scale, factors including facility utilization, available capital, ease of process development, implementation timelines, and process performance characterization play an important role in clarification technology selection. In the case study presented, a multi-product facility selected multi-stage depth filtration for cell culture clarification at the 500 and 2,000 L scales of operation. Facility implementation timelines, process development activities, equipment commissioning and validation, scale-up effects, and process robustness are examined.

Feasibility study of semi‐selective protein precipitation with salt‐tolerant copolymers for industrial purification of therapeutic antibodies

We present a feasibility study for an antibody capturing process from clarified cell culture fluid using semi-selective protein precipitation with salt-tolerant copolymers. Protein precipitation is mediated by hydrophobic and electrostatic interactions with the copolymer that can be customized for the respective target. Precipitation yield with different copolymers at ionic strength of 2-22.5 mS cm⁻¹ and pH 5.0-pH 5.7 was evaluated using pure monoclonal antibody solutions. Optimized parameters were used to elucidate yield and purity of various antibodies precipitated at physiological conditions from cell culture fluid of CHO, NS0, and SP2/0 cell culture fluid. Precipitated protein was easily redissolved in small volume, enabling concentrating monoclonal antibodies (mAb) more than 40-fold and up to 100-fold, while residual polymer was removed to >98% using cationic polymer attached to silica flakes. mAb recovery of >90% and host cell protein clearance of >80% were achieved, not requiring any pre-dilution of cell culture fluid. Precipitation showed no impact on mAb binding affinity when compared to non-precipitated mAb. The obtained yield and purity were lower compared to a protein A based purification and loss of mAb was factor 1.5-3.0 higher. Yet, for high titer mAb purification processes being implemented in the future, precipitation is an attractive option due to its ease of scalability and cost-effectiveness.

Coupled affinity and sizing chromatography: A novel in-process analytical tool to measure titer and trend Fc-protein aggregation

The expanding use of monoclonal antibodies in the biopharmaceuticals industry has brought the need for new analytical tools. We have developed a coupled affinity and gel-filtration high-performance liquid chromatography method to simultaneously analyze titer and quality of monoclonal antibodies. Before this assay, available analytical methods for protein aggregation required highly purified proteins. This assay can qualitatively describe a protein from a clarified cell culture solution by trending protein aggregation over time while measuring protein titer. It can be used to assess proteins in both early- and late-stage culture due to its dynamic range and sensitivity. This assay is a sensitive technique that overcomes the time limitations of previous approaches. It provides an essential tool to accomplish process optimization.

Association indépendante entre l’hypoxémie intermittente et la dyslipidémie métabolique dans le syndrome d’apnées-hypopnées obstructives du sommeil

This work describes the adsorption–desorption behavior of a histidine-tagged single-chain Fragment variable antibody (D1.3 scFv) on a commercial immobilized metal ion affinity chromatography (IMAC) column. A clarified cell culture supernatant originating from Bacillus megaterium was characterized using single column experiments in a pH-gradient elution mode. The cell culture supernatant containing the antibody fragment D1.3 scFv could be treated in the chromatographic separation process as a pseudo-binary mixture. Adsorption equilibrium constants of the antibody fragment fraction (ABF) and the non-specifically retained protein impurity fraction (IMP) were determined experimentally at constant pH by reinjecting pulses of pooled fractions collected in preliminary batch gradient elution runs. Based on the estimated adsorption equilibrium constants a possible multicolumn open-loop three-zone two-step pH-gradient simulated moving bed (SMB) process is suggested and designed, which possesses the potential to isolate continuously the antibody fragment fraction (ABF) containing the single-chain antibody fragment D1.3 scFv.

Discontinuous and continuous purification of single-chain antibody fragments using immobilized metal ion affinity chromatography

This work describes the adsorption–desorption behavior of a histidine-tagged single-chain Fragment variable antibody (D1.3 scFv) on a commercial immobilized metal ion affinity chromatography (IMAC) column. A clarified cell culture supernatant originating from Bacillus megaterium was characterized using single column experiments in a pH-gradient elution mode. The cell culture supernatant containing the antibody fragment D1.3 scFv could be treated in the chromatographic separation process as a pseudo-binary mixture. Adsorption equilibrium constants of the antibody fragment fraction (ABF) and the non-specifically retained protein impurity fraction (IMP) were determined experimentally at constant pH by reinjecting pulses of pooled fractions collected in preliminary batch gradient elution runs. Based on the estimated adsorption equilibrium constants a possible multicolumn open-loop three-zone two-step pH-gradient simulated moving bed (SMB) process is suggested and designed, which possesses the potential to isolate continuously the antibody fragment fraction (ABF) containing the single-chain antibody fragment D1.3 scFv.

Host cell protein quantification by fourier transform mid infrared spectroscopy (FT‐MIR)

Process development in up- and downstream processing requires enhanced, non-time-consuming, and non-expensive monitoring techniques to track product purity, for example, the level of endotoxins, viral particles, and host cell proteins (HCPs). Currently, HCP amounts are measured by laborious and expensive HCP-enzyme-linked immunosorbent assay (ELISA) assays best suited for measuring HCP amounts in the low concentration regime. The measurement of higher HCP amounts using this method requires dilution steps, adding dilution errors to the measurement. In this work we evaluated the suitability of attenuated total reflection spectroscopy for HCP quantification in process development, using clarified cell culture fluid from monoclonal antibody producing Chinese hamster ovary-cells after treatment with different polyelectrolytes for semi-selective clarification. Forty undiluted samples were chosen for multivariate data analysis in the middle infrared range and predicted HCP-values were in good agreement with results obtained by an ELISA-assay, suggesting the suitability of this new method for HCP-quantification. As this method is able to quantify HCP titers ranging from approximately at least 20,000-200,000 ng mL(-1), it is suitable especially for monitoring of process development steps with higher HCP concentrations, omitting dilution errors associated with ELISA assays.

Mammalian Cell Culture Clarification: A Case Study Using Chimeric Anti-CEA Monoclonal Antibodies

The extracellular expression of monoclonal antibodies (mAbs) in mammalian cell culture provides both opportunities and restrictions for the design of robust harvest and clarification operations. With advances in cell culture media and cell lines, it is now possible to achieve high titers of over 5 g/l for mAbs. However, Mammalian cells are sensitive to breakage due to shear stress that can result in release of proteases and other host cell proteins (HCPs) which eventually affects product stability and purity. There is larger number of mAbs undergoing clinical development and it has placed significant importance on platform technologies of process development. Generally, Centrifugation and microfiltration are the primary harvest techniques used in the industry and depth filtration is also used as a step operation on clarification. This study compares the unit operations; centrifugation, microfiltration and depth filtration for maximum recovery of monoclonal antibodies. The results have shown that the depth filtration as more suitable operation for mammalian cell culture clarification since it gives 96% recovery of mAbs in comparison to centrifugation and microfiltration. ABSTRAK: Pengungkapan luar sel dari antibodi monoklon (monoclonal antibodies ((mAbs) dalam kultur sel mamalia memberi ruang dan batasan terhadap reka bentuk penuaian yang cekap dan penerangan operasi. Dengan kemajuan dalam media sel kultur dan cell lines (produk yang berupa sel kekal yang digunakan untuk tujuan kajian biologi), kini adalah berkemungkinan untuk memperolehi titer tinggi melebihi 5g/l untuk mAbs [2]. Walaupun begitu, sel mamalia sensitif terhadap retakan disebabkan tegasan ricih yang menyebabkan pengeluaran protease dan hos sel protein yang lain, (host cell proteins (HCPs)) akhirnya mempengaruhi kestabilan dan keaslian produk. Terdapat mAbs dalam jumlah besar yang masih menjalani pembangunan klinikal dan sesungguhnya ini penting sebagai satu landasan teknologi dalam proses pembangunan. Umumnya pengemparan dan mikropenurasan merupakan teknik asas tuaian dalam industri dan penurasan dalam juga digunakan sebagai satu pengendalian langkah dalam penjelasannya. Kajian ini membandingkan operasi unit: pengemparan, mikropenurasan dan penurasan dalam untuk perolehan antibodi monoklon yang maksima. Keputusan menunjukkan penurasan dalam adalah operasi yang lebih sesuai untuk penjelasan kultur sel mamalia kerana ia memberikan perolehan 96 % mAbs berbandingkan dengan cara pengemparan dan mikropenurasan.

Structural refinement of protein A mimetic peptide

A novel dendrimeric peptide ligand dubbed D-PAM-Φ was designed to achieve a high capacity for human IgG through the decoration of the D-PAM scaffold. The design criteria based on the introduction of small hydrophobic groups on the D-PAM structure were supported by the recently published solid-state structure of D-PAM complexed to the Fc fragment of a recombinant human IgG1 and by molecular dynamic simulations that provided information on the mode of binding of phenylacetyl-D-PAM (D-PAM-Φ). D-PAM-Φ was immobilised on an activated solid support and compared with the parent D-PAM affinity matrix. The newly obtained affinity sorbent was evaluated for its capacity to selectively capture polyclonal human IgG; the binding capacity was approximately 10 mg/ml, an almost 10-fold enhancement with respect to the D-PAM-functionalised matrices without the specificity of binding being reduced. The new ligand was also effective in the capturing of recombinant humanised IgG1 from a clarified cell culture supernatant. Under a typical laboratory-scale affinity chromatography assembly and preliminarily optimised binding conditions, the affinity purification of humanised IgG1 from culture supernatants rendered the desired product, with purity higher than 90%. The results suggest that the application of the computational approach on the structure of the D-PAM-Fc complex may be very valuable in the development of novel lead molecules for the downstream processing of human or humanised antibodies used in therapy.

Downstream antibody purification using aqueous two‐phase extraction

The extraction of antibodies using a polyethylene glycol (PEG)-citrate aqueous two-phase system (ATPS) was investigated. Studies using purified monoclonal antibody (mAb) identified operating ranges for successful phase formation and factors that significantly affected antibody partitioning. The separation of antibody and host cell protein (HCP) from clarified cell culture media was examined using statistical design of experiments (DOE). The partitioning of antibody was nearly complete over the entire range of the operating space examined. A model of the HCP partitioning was generated in which both NaCl and citrate concentrations were identified as significant factors. To achieve the highest purity, the partitioning of HCP from cell culture fluid into the product containing phase was minimized using a Steepest Descent algorithm. An optimal ATPS consisting of 14.0% (w/w) PEG, 8.4% (w/w) citrate, and 7.2% (w/w) NaCl at pH 7.2 resulted in a product yield of 89%, an approximate 7.6-fold reduction in HCP levels relative to the clarified cell culture fluid before extraction and an overall purity of 70%. A system consisting of 15% (w/w) PEG, 8% (w/w) citrate, and 15% (w/w) NaCl at pH 5.5 reduced product-related impurities (aggregates and low molecular product fragments) from ∼40% to less than 0.5% while achieving 95% product recovery. At the experimental conditions that were optimized in the batch mode, a scale-up model for the use of counter-current extraction technology was developed to identify potential improvements in purity and recovery that could be realized in the continuous operational mode.

Two step capture and purification of IgG2 using multicolumn countercurrent solvent gradient purification (MCSGP)

A two-step chromatography process for monoclonal antibody (mAb) purification from clarified cell culture supernatant (cCCS) was developed using cation exchange Multicolumn Countercurrent Solvent Gradient Purification (MCSGP) as a capture step. After an initial characterization of the cell culture supernatant the capture step was designed from a batch gradient elution chromatogram. A variety of chromatographic materials was screened for polishing of the MCSGP-captured material in batch mode. Using multi-modal anion exchange in bind-elute mode, mAb was produced consistently within the purity specification. The benchmark was a state-of-the-art 3-step chromatographic process based on protein A, anion and cation exchange stationary phases. The performance of the developed 2-step process was compared to this process in terms of purity, yield, productivity and buffer consumption. Finally, the potential of the MCSGP process was investigated by comparing its performance to that of a classical batch process that used the same stationary phase.

Capture of human monoclonal antibodies from a clarified cell culture supernatant by phenyl boronate chromatography

In this work, we investigated the feasibility of using phenyl boronate (PB) chromatography for the direct capture of monoclonal antibodies from a CHO cell supernatant. Preliminary results, using pure protein solutions have shown that PB media can bind to human antibodies, not only at strong alkaline conditions but also at acidic pH values. In fact, antibodies have been found to bind in the pH range 5.5-8.5. On the other hand, insulin and human serum albumin did not bind at alkaline pH but at lower pH, which reflects the importance of non-specific interactions with the matrix. Different binding and eluting buffers were evaluated for the capture of immunoglobulin G (IgG) from a CHO cell supernatant and the most promising results were obtained using 20 mM 4-(2-hydroxyethyl)-1-piperazineethanesulfonic acid at pH 8.5 as binding buffer and 1.5 M Tris-HCl as eluting buffer. Using a step elution, all IgG was recovered in the elution pool with a maximum purification factor of 56. A gradient elution allowed a further increase of the final purity, yet achieving a slightly lower yield. IgG recovery was around 85% and the purification factor was 76. The highest purity was obtained when the pH of the cell supernatant feed was previously adjusted to 8.5. Starting from an initial protein purity of 1.1% and high-performance liquid chromatography (HPLC) purity of 2.2%, after PB adsorption, a final protein purity of 85% and a HPLC purity of 88% was achieved.

Application of mixed mode resins for the purification of antibodies

The downstream processing of monoclonal antibodies from cell culture supernatant is usually done by a number of chromatographic and non-chromatographic steps. Efforts are taken to reduce the costs associated to those steps, while maintaining a high product purity. A possibility to reach this goal is the reduction of the number of chromatographic steps using mixed mode resins that offer more than one functionality in one chromatographic step. In this work, a commercially available mixed mode resin was evaluated systematically with respect to the adsorption of proteins. The Henry coefficient, which quantifies the adsorption strength, was measured for the full working range of the stationary phase as a function of the salt concentration and the pH. The results were compared to a conventional anion exchange and a hydrophobic interaction resin. Furthermore, the resin was applied for the polishing step of an antibody from an industrial clarified cell culture supernatant.

High‐throughput screening techniques for rapid PEG‐based precipitation of IgG4 mAb from clarified cell culture supernatant

Locating optimal protein precipitation conditions for complex biological feed materials is problematic. This article describes the application of a series of high-throughput platforms for the rapid identification and selection of conditions for the precipitation of an IgG(4) monoclonal antibody (mAb) from a complex feedstock using only microliter quantities of material. The approach uses 96-microwell filter plates combined with high-throughput analytical methods and a method for well volume determination for product quantification. The low material, time and resource requirements facilitated the use of a full factorial Design of Experiments (DoE) for the rapid investigation into how critical parameters impact the IgG(4) precipitation. To aid the DoE, a set of preliminary range-finding studies were conducted first. Data collected through this approach describing Polyethylene Glycol (PEG) precipitation of the IgG(4) as a function of mAb concentration, precipitant concentration, and pH are presented. Response surface diagrams were used to explore interactions between parameters and to inform selection of the most favorable conditions for maximum yield and purification. PEG concentrations required for maximum yield and purity were dependant on the IgG(4) concentration; however, concentrations of 14 to 20% w/v, pH 6.5, gave optimal levels of yield and purity. Application of the high-throughput approach enabled 1,155 conditions to be examined with less than 1 g of material. The level of insights gained over such a short time frame is indicative of the power of microwell experimentation in allowing the rapid identification of appropriate processing conditions for key bioprocess operations.

Application of a novel affinity adsorbent for the capture and purification of recombinant Factor VIII compounds

Recombinant Factor VIII (FVIII) therapies have been created to provide treatment for Hemophilia A, an inherited bleeding disorder caused by mutation in the FVIII gene. A major challenge in the purification of recombinant FVIII molecules is the development of an affinity chromatography step. Such a step must be highly specific and selective for the FVIII molecule, but also must be designed appropriately to ensure the FVIII molecule can be effectively recovered without resorting to harsh elution conditions which may be harmful to the product. Additionally, it is desirable to have affinity adsorbents designed to be reusable over a large number of column cycles while maintaining consistent purification performance. In this work, we describe the use of VIIISelect, a commercially available affinity adsorbent designed specifically for the purification of FVIII compounds. The VIIISelect adsorbent consists of a 13 kDa recombinant protein ligand attached to a cross-linked agarose base matrix. The structure of the recombinant ligand is based upon Camelid-derived single domain antibody fragments. The VIIISelect adsorbent is produced using a process free of animal-derived raw materials, which is a highly desirable attribute for adsorbents used in the purification processes of recombinant protein therapeutics. The VIIISelect adsorbent was used as the initial capture column to purify a FVIII compound directly from clarified cell culture fluid prior to further downstream purification. The purification performance of the VIIISelect was evaluated, which included measurement of the static binding capacity, dynamic binding capacity, product recovery, impurity clearance, and adsorbent reuse. Following laboratory-scale process development, the VIIISelect adsorbent was scaled up and used in the large scale manufacturing of a FVIII compound.

Systematic Analysis of Proteoglycan Modification Sites in Caenorhabditis elegans by Scanning Mutagenesis

Proteoglycan modification is essential for development and early cell division in Caenorhabditis elegans. The specification of proteoglycan attachment sites is defined by the Golgi enzyme polypeptide xylosyltransferase. Here we evaluate the substrate specificity of this xylosyltransferase for its downstream targets by using reporter proteins containing proteoglycan modification sites from C. elegans syndecan/SDN-1. The N terminus of the SDN-1 contains a Ser-Gly proteoglycan site at Ser(71), flanked by potential mucin and N-glycosylation sites. However, Ser(71) was exclusively used as a proteoglycan site in vivo, based on mapping studies with a Ser(71) reporter protein, glycosyltransferase RNA interference, and co-expression of worm polypeptide xylosyltransferase. To elucidate the substrate requirements of this enzyme, a library of 42 point mutants of the Ser(71) reporter was expressed in tissue culture. The nematode proteoglycan modification site in SDN-1 required serine (not threonine), two flanking glycine residues (positions -1 and +1), and either one proximal acidic N-terminal amino acid (positions -4, -3, and -2) or a pair of distal N-terminal acidic amino acids (positions -6 and -5). C-terminal acidic amino acids, although present in many proteoglycan modification sites, had minimal impact on xylosylation at Ser(71). Proline inhibited glycosylation when present at -1, +1, or +2. The position of glycine, proline, and acidic amino acids allows the glycosylation machinery to discriminate between mucin and proteoglycan modification sites. The key residues that define proteoglycan modification sites also function with the Drosophila polypeptide xylosyltransferase, indicating that the specificity in the glycosylation process is evolutionarily conserved. Using a neural network method, a preliminary proteoglycan predictor has been developed.

Purification, Characterization, and Cloning of a Spodoptera frugiperda Sf9 β-N-Acetylhexosaminidase That Hydrolyzes Terminal N-Acetylglucosamine on the N-Glycan Core

Paucimannosidic glycans are often predominant in N-glycans produced by insect cells. However, a beta-N-acetylhexosaminidase responsible for the generation of paucimannosidic glycans in lepidopteran insect cells has not been identified. We report the purification of a beta-N-acetylhexosaminidase from the culture medium of Spodoptera frugiperda Sf9 cells (Sfhex). The purified Sfhex protein showed 10 times higher activity for a terminal N-acetylglucosamine on the N-glycan core compared with tri-N-acetylchitotriose. Sfhex was found to be a homodimer of 110 kDa in solution, with a pH optimum of 5.5. With a biantennary N-glycan substrate, it exhibited a 5-fold preference for removal of the beta(1,2)-linked N-acetylglucosamine from the Man alpha(1,3) branch compared with the Man alpha(1,6) branch. We isolated two corresponding cDNA clones for Sfhex that encode proteins with >99% amino acid identity. A phylogenetic analysis suggested that Sfhex is an ortholog of mammalian lysosomal beta-N-acetylhexosaminidases. Recombinant Sfhex expressed in Sf9 cells exhibited the same substrate specificity and pH optimum as the purified enzyme. Although a larger amount of newly synthesized Sfhex was secreted into the culture medium by Sf9 cells, a significant amount of Sfhex was also found to be intracellular. Under a confocal microscope, cellular Sfhex exhibited punctate staining throughout the cytoplasm, but did not colocalize with a Golgi marker. Because secretory glycoproteins and Sfhex are cotransported through the same secretory pathway and because Sfhex is active at the pH of the secretory compartments, this study suggests that Sfhex may play a role as a processing beta-N-acetylhexosaminidase acting on N-glycans from Sf9 cells.

491. Development of Fast and Efficient Methods for the Purification and Concentration of Lentiviral Vectors

Top of pageAbstract Lentiviral vectors are proving to be promising tools for gene therapy. However, the relatively low titres of these vectors mean that they must be substantially concentrated before use. In addition, as with any pharmaceutical product, the final preparation must have a high and definable purity. Therefore, we are developing methods to concentrate and purify virus preparations. To facilitate processing, virus was collected in serum free medium, then clarified by low speed centrifugation and 0.45 |[igrave]|m filtration. As an initial purification step, several ultrafiltration systems with different molecular weight (Mw) cut-offs were evaluated and a hollow fibre system with a 750 kDa Mw cut-off was chosen as the most appropriate. Systems with membranes having a larger Mw cut-off allowed significant amounts of virus particles to pass through, while membranes with smaller Mw cut-offs resulted in slower processing and would presumably also be less effective at removing contaminants. Ultrafiltration allowed the clarified cell culture supernatant to be concentrated 20-fold in 2-3 hours, with virus recoveries of approximately 50% and a greater than 10-fold reduction of total protein. Ultracentrifugation was then used to pellet the virus, allowing it to be resuspended in a small volume (approximately 1000th of the starting volume) of the buffer of choice. Recovery of virus was again about 50% and total protein was reduced a further 10-fold. The combination of ultrafiltration and ultracentrifugation has resulted in the rapid concentration and purification of large volumes (over 3 litres) of virus supernatant, with overall recoveries of >25% of infectious virus and a reduction to <2% of the initial amount of protein per infectious-unit. This approach was also rapid: the overall processing time from collection of viral supernatant to resuspension of the final virus preparation was <8 hours. However, SDS-PAGE analysis suggests the final material is still not 100% pure. We are now exploring the effects of varying ultrafiltration and ultracentrifugation parameters with the aim of raising the overall viable virus particle recovery to at least 50%. In addition, we are investigating the addition of an anion exchange chromatography step to increase virus recovery and simultaneously increase the purity of the final virus preparation.