Ultra scale‐down approaches for clarification of mammalian cell culture broths in disc‐stack centrifuges

Ultra‐scale down (USD) methodology developed by University College London for cell broth clarification with industrial centrifuges was applied to two common cell lines (NS0 and GS‐CHO) expressing various therapeutic monoclonal antibodies. A number of centrifuges at various scales were used with shear devices operating either by high speed rotation or flow‐through narrow channels. The USD methodology was found effective in accounting for both gravitational and shear effects on clarification performance with three continuous centrifuges at pilot and manufacturing scales. Different shear responses were observed with the two different cell lines and even with the same cell line expressing different products. Separate particle size analysis of the treated broths seems consistent with the shear results. Filterability of the centrifuged solutions was also evaluated to assess the utility of the USD approach for this part of the clarification operation. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Repeated hybridoma batch culture with cell recycle

At the end of a hybridoma batch culture, the cells are usually discarded after separation from the culture broth. If, however, they are aseptically recycled into the reactor, the production process can be resumed simply by the addition of fresh medium. This cycle can then be repeated several times consecutively. In a test case, with a mouse hybridoma, we found antibody yields for each cycle in the same range as for a standard batch. In a 15 1 stirred tank reactor we could, within 6 days, produce 2.8 g of monoclonal antibody (MAb). This type of reactor operation allowed a doubling in the reactor volumetric productivity (mg/l/day).     

An effective,simple and low-cost pretreatment for culture clarification in tetanus toxoid production

Abstract

Chemically inactivated tetanus toxin (tetanus toxoid, TT), purified from cultures of a virulent Clostridium tetani strain, is the active pharmaceutical ingredient of anti-tetanus vaccines. Culture clarification for TT production and is usually performed by filtration-based techniques. Final clarification of the culture supernatant is achieved by passage through 0.2?µm pore size filtering membranes. Large particles removal (primary clarification) before final filtration (secondary clarification) reduces costs of the overall clarification process. With this aim, chitosan-induced particle aggregation was assessed as an alternative for primary clarification. Three chitosan variants were tested with similar results. Optimal clarification of culture supernatant was achieved by the addition of 8?mg chitosan per l of culture. Extrapolation analysis of filter sizing results indicate that 100?l of chitosan-treated supernatant can be finally filtered with a 0.6 m2 normal filtration cartridge of 0.45?+?0.2?µm pore size. The clarified material is compatible with current standard downstream processing techniques for TT purification. Thus, chitosan-induced particle aggregation is a suitable operation for primary clarification.     

Selective removal of ammonia from animal cell culture broth

Serum-free perfusion cultures of hybridoma TO-405 cells were carried out in spinner flasks coupled with zeolite A-3 packed beads. Ammonia was selectively removed from the culture broth by passing cell free permeate from ceramic cross flow filtration, through the zeolite packed bed. Ammonia concentration in the culture broth was effectively maintained between 1 to 4 mmol/l which was below the inhibitory concentration for cell growth. Maximum cell density levels of 10⁷ cells/ml as well as improved percentage cell viability higher than in serum-supplemented cultures were feasible in this system.The possible effects of shear stress, generated by variation of the flow rates of the broth through the ceramic filter module, on the growth of the hybridoma cells were investigated. Backwashing, by reversing the direction of the permeate, was found necessary to prolong the life of the filter. Variation of the flow rates of the broth through the ceramic module between 0.29 m/s to 0.59 m/s did not cause immediate cell damage but growth was repressed at the higher flow rate.This study also showed that glutamine appears to be one of the factors limiting the growth of the hybridoma cells.     

Interaction of cell culture with downstream purification: a case study

Separation of product from secreting mammalian cells in the culture broth means the transition from product generation to product isolation. This interface within a biotech production process has to perform a proper solid/liquid phase separation of the cell suspension to make the product containing fluid amenable for further purification. These subsequent steps require fluid with low occurence of contaminants in order to function properly. The goal of this study was to evaluate some economic and fast cell separation methods for the preparation of a product fluid ready for use in further ultrafiltration and chromatographic processes. We have performed experiments to test the usefulness of disc stack centrifuges and tangential flow microfiltration units at large scale. Both systems revealed outstanding prospects with regard to throughput and scale up properties. However, the centrificgation did not lead to a fluid sufficiently free of particles for direct ultrafiltration or chromatography. Thus, an additional filtration step was necessary. On the other hand microfiltration led to an acceptable quality of process fluid directly. By optimisation of process parameters an effective, reproducible and robust cell separation can be obtained. However, our experience has been that such optimal conditions are somewhat specific for a narrow range. Thus, even the equipment functioning well with one type of cell would possibly not perform as well with another cell or even with the same cell under conditions slightly different to the usual situation.     

Clinical considerations for the development of biosimilars in oncology

Despite availability of biologic therapies, limited patient access to many of the most-effective cancer treatments affects overall health outcomes. To address this issue, many governments have enacted legislation for the approval of biosimilars. The term “biosimilar” refers to a biologic product that is developed to be highly similar, as opposed to identical, to a licensed biologic product (the reference or innovator product), such that, per US Food and Drug administration draft guidelines, “no clinically meaningful differences [exist] between the biological product and the reference product in terms of safety, purity, and potency.” This article presents some considerations about the development of biosimilars in cancer treatment through an overview of biosimilars from a clinical perspective. Topics covered include the development requirements and unique regulatory requirements for biosimilars, labeling considerations, potential limitations to the uptake of biosimilars, and review of some biosimilars in development for oncology indications.     

Clinical considerations for the development of biosimilars in oncology

Despite availability of biologic therapies, limited patient access to many of the most-effective cancer treatments affects overall health outcomes. To address this issue, many governments have enacted legislation for the approval of biosimilars. The term “biosimilar” refers to a biologic product that is developed to be highly similar, as opposed to identical, to a licensed biologic product (the reference or innovator product), such that, per US Food and Drug administration draft guidelines, “no clinically meaningful differences [exist] between the biological product and the reference product in terms of safety, purity, and potency.” This article presents some considerations about the development of biosimilars in cancer treatment through an overview of biosimilars from a clinical perspective. Topics covered include the development requirements and unique regulatory requirements for biosimilars, labeling considerations, potential limitations to the uptake of biosimilars, and review of some biosimilars in development for oncology indications.     

Hydroxocobalamin association during cell culture results in pink therapeutic proteins

Process control of protein therapeutic manufacturing is central to ensuring the product is both safe and efficacious for patients. In this work, we investigate the cause of pink color variability in development lots of monoclonal antibody (mAb) and Fc-fusion proteins. Results show pink-colored product generated during manufacturing is due to association of hydroxocobalamin (OH-Cbl), a form of vitamin B₁₂. OH-Cbl is not part of the product manufacturing process; however we found cyanocobalamin (CN-Cbl) in cell culture media converts to OH-Cbl in the presence of light. OH-Cbl can be released from mAb and Fc-fusion proteins by conversion with potassium cyanide to CN-Cbl, which does not bind. By exploiting the differential binding of CN-Cbl and OH-Cbl, we developed a rapid and specific assay to accurately measure B₁₂ levels in purified protein. Analysis of multiple products and lots using this technique gives insight into color variability during manufacturing.     

Hybridoma growth and antibody production as a function of cell density and specific growth rate in perfusion culture

Steady state metabolic parameters for hybridoma cell line H22 were determined over a wide range of cell densities and specific growth rates in a filtration based homogeneous perfusion reactor. Operating the reactor at perfusion rates of 0.75, 2.0, and 2.9 day(-1)(each at four different specific growth rates), viable cell densities as high as 2 x 10(7) cells/mL were obtained. For the cell line under investigation, the specific monoclonal antibody production rate was found to be a strong function of the viable cell density, increasing with increasing cell density. In contrast, most of the substrate consumption and product formation rates were strong functions of the specific growth rate. Substrate metabolism became more efficient at high cell densities and low specific growth rates. The Specific rates of metabolite formation and the apparent yields of lactate from glucose and ammonia from glutamine decreased at low specific growth rates and high cell densities. While the specific oxygen consumption rate was independent of the specific growth rate and cell density, ATP production was more oxidative at lower specific growth rate and higher cell density. These observed shifts are strong indications of the production potential of high-density perfusion culture. (c) 1995 John Wiley & Sons, Inc.     

Long-term perfusion culture of hybridoma: a "grow or die" cell cycle system

In order to elucidate the hybridoma life cycle and the limiting factors in perfusion systems, we performed cultures in a stirred tank bioreactor, coupled to an external tangential flow filtration unit. Cell density and antibody production in perfusion were consistent with previous studies. The average life span of the cells (2.1-2.2 days), antibody, productivity per cell produced (30-38 mg/10(9) cells) and cell size diameter evolution appeared similar to values observed in batch cultures. These observations highly suggest a similar "grow or die" life cycle. Cell and antibody production, strictly related to the medium perfusion rate, seem to be under the control of the nutrient availability. A hypothesis to explain such a life cycle of hybridoma cells in perfusion systems and a model for viable and dead cell density is proposed.     

Fermentanomics informed amino acid supplementation of an antibody producing mammalian cell culture

Fermentanomics, or a global understanding of a culture state on the molecular level empowered by advanced techniques like NMR, was employed to show that a model hybridoma culture supplied with glutamine and glucose depletes aspartate, cysteine, methionine, tryptophan, and tyrosine during antibody production. Supplementation with these amino acids prevents depletion and improves culture performance. Furthermore, no significant changes were observed in the distribution of glycans attached to the IgG3 in cultures supplemented with specific amino acids, arguing that this strategy can be implemented without fear of impact on important product quality attributes. In summary, a targeted strategy of quantifying media components and designing a supplementation strategy can improve bioprocess cell cultures when enpowered by fermentanomics tools. Published 2013 American Institute of Chemical Engineers Biotechnol. Prog., 29:745–753, 2013     

Phenolics removal from transgenic Lemna minor extracts expressing mAb and impact on mAb production cost

Transgenic Lemna minor has been used successfully to produce several biotherapeutic proteins. For plant-produced mAbs specifically, the cost of protein A capture step is critical as the economic benefits of plant production systems could be erased if the downstream processing ends up being expensive. To avoid potential modification of mAb or fouling of expensive protein A resins, a rapid and efficient removal of phenolics from plant extracts is desirable. We identified major phenolics in Lemna extracts and evaluated their removal by adsorption to PVPP, XAD-4, IRA-402, and Q-Sepharose. Forms of apigenin, ferulic acid, and vitexin comprised ～ 75% of the total phenolics. Screening of the resins with pure ferulic acid and vitexin indicated that PVPP would not be efficient for phenolics removal. Analysis of the breakthrough fractions of phenolics adsorption to XAD-4, IRA-402, and Q-Sepharose showed differences in adsorption with pH and in the type of phenolics adsorbed. Superior dynamic binding capacities (DBC) were observed at pH 4.5 than at 7.5. To evaluate the cost impact of a phenolics removal step before protein A chromatography, a mAb purification process was simulated using SuperPro Designer 7.0. The economic analysis indicated that addition of a phenolics adsorption step would increase mAb production cost only 20% by using IRA-402 compared to 35% for XAD-4 resin. The cost of the adsorption step is offset by increasing the lifespan of protein A resin and a reduction of overall mAb production cost could be achieved by using a phenolics removal step.     

Hybridoma cell behaviour in continuous culture under hyperosmotic stress

In this paper, we propose an alternative strategy to the ones proposed before (Oh et al., 1993; Øyaas et al., 1994a) to get real increases of global final antibody titer and production at hyperosmotic stress, by reducing the detrimental effect of such a stress on cell growth, and conserving the stimulating effect on antibody production. It consists of cultivating the cells in continuous culture and increasing the osmolality stepwise. In this way, the cells could progressively adapt to the higher osmolality at each step and antibody titers could be nearly doubled at 370 and 400 mOsm kg-1, compared to the standard osmolality of 335 mOsm kg-1. Surprisingly, the stimulation of antibody production was not confirmed for higher osmolalities, 425 and 450 mOsm kg- 1, despite the minor negative effect on cell growth. Intracellular IgG analysis by flow cytometry revealed at these osmolalities a significant population of non-producing cells. However, even when taking into account this non-producing population, a stimulating effect on antibody production could not be shown at these highest osmolalities. It seems to us that osmolality has a significant effect on the appearance of these non-producing cells, since they were not observed in continuous cultures at standard osmolality, of comparable duration and at an even higher dilution rate. The appearance of the non-producing cells coincides furthermore with modifications of the synthesised antibody, as shown by electrophoretic techniques. It is however not really clear if these two observations reflect actually the same phenomenon. Hyperosmolality affects the cell behaviour in continuous culture in multiple ways, independently of the growth rate, counting all at least partially for the observed stimulation of antibody production: acceleration of the amino acid, and in particular the glutamine metabolism, increase of the cell volume, increase of the intracellular pH and accumulation of cells in the G1 cell cycle phase.     

Role of iron and sodium citrate in animal protein-free CHO cell culture medium on cell growth and monoclonal antibody production

Chemically defined iron compounds were investigated for the development of animal protein-free cell culture media to support growth of CHO cells and production of monoclonal antibodies (mAb). Using a multivessel approach of 96-well plates, shake flasks, and bioreactors, we identified iron and its chemical partner citrate as critical components for maintenance of continuous cell growth and mAb production. The optimized iron concentration range was determined to be 0.1-0.5 mM and that for citrate 0.125-1 mM. This complete formulation is able to maintain cell growth to similar levels as those supplemented with iron compounds alone; however, mAb productivity was enhanced by 30-40% when citrate was present. The addition of sodium citrate (SC) did not affect product quality as determined by size exclusion chromatography, ion exchange chromatography, reversed phase and normal phase-HPLC. No significant changes in glucose and lactate profiles, amino acid utilization, or mAb heavy and light chain expression ratios were observed. Cellular ATP level was ～30% higher when SC was included suggesting that SC may have a role in enhancing cellular energy content. When cell lysates were analyzed by LC-MS to assess the overall cellular protein profile, we identified that in the SC-containing sample, proteins involved in ribosome formation and protein folding were upregulated, and those functions in protein degradation were downregulated. Taken together, this data demonstrated that iron and citrate combination significantly enhanced mAb production without altering product quality and suggested these compounds had a role in upregulating the protein synthetic machinery to promote protein production.     

Process control in cell culture technology using dielectric spectroscopy

In the biopharmaceutical industry, mammalian and insect cells as well as plant cell cultures are gaining worldwide importance to produce biopharmaceuticals and as products themselves, for example in stem cell therapy. These highly sophisticated cell-based production processes need to be monitored and controlled to guarantee product quality and to satisfy GMP requirements. With the process analytical technology (PAT) initiative, requirements regarding process monitoring and control have changed and real-time in-line monitoring tools are now recommended. Dielectric spectroscopy (DS) can serve as a tool to satisfy some PAT requirements. DS has been used in the medical field for quite some time and it may allow real-time process monitoring of biological cell culture parameters. DS has the potential to enable process optimization, automation, cost reduction, and a more consistent product quality. Dielectric spectroscopy is reviewed here as a tool to monitor biochemical processes. Commercially available dielectric sensing systems are discussed. The potential of this technology is demonstrated through examples of current and potential future applications in research and industry for mammalian and insect cell culture.     

High‐throughput miniaturized bioreactors for cell culture process development: Reproducibility,scalability, and control

Decreasing the timeframe for cell culture process development has been a key goal toward accelerating biopharmaceutical development. Advanced Microscale Bioreactors (ambr?) is an automated micro‐bioreactor system with miniature single‐use bioreactors with a 10–15 mL working volume controlled by an automated workstation. This system was compared to conventional bioreactor systems in terms of its performance for the production of a monoclonal antibody in a recombinant Chinese Hamster Ovary cell line. The miniaturized bioreactor system was found to produce cell culture profiles that matched across scales to 3 L, 15 L, and 200 L stirred tank bioreactors. The processes used in this article involve complex feed formulations, perturbations, and strict process control within the design space, which are in‐line with processes used for commercial scale manufacturing of biopharmaceuticals. Changes to important process parameters in ambr? resulted in predictable cell growth, viability and titer changes, which were in good agreement to data from the conventional larger scale bioreactors. ambr? was found to successfully reproduce variations in temperature, dissolved oxygen (DO), and pH conditions similar to the larger bioreactor systems. Additionally, the miniature bioreactors were found to react well to perturbations in pH and DO through adjustments to the Proportional and Integral control loop. The data presented here demonstrates the utility of the ambr? system as a high throughput system for cell culture process development. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:718–727, 2014     

Bioreactor productivity and media cost comparison for different intensified cell culture processes

Process intensification in biomanufacturing has attracted a great deal of interest in recent years. Manufacturing platform improvements leading to higher cell density and bioreactor productivity have been pursued. Here we evaluated a variety of intensified mammalian cell culture processes for producing monoclonal antibodies. Cell culture operational modes including fed‐batch (normal seeding density or high seeding density with N‐1 perfusion), perfusion, and concentrated fed‐batch (CFB) were assessed using the same media set with the same Chinese Hamster Ovary (CHO) cell line. Limited media modification was done to quickly fit the media set to different operational modes. Perfusion and CFB processes were developed using an alternating tangential flow filtration device. Independent of the operational modes, comparable cell specific productivity (fed‐batch: 29.4 pg/cell/day; fed‐batch with N‐1 perfusion: 32.0 pg/cell/day; perfusion: 31.0 pg/cell/day; CFB: 20.1 – 45.1 pg/cell/day) was reached with similar media conditions. Continuous media exchange enabled much higher bioreactor productivity in the perfusion (up to 2.29 g/L/day) and CFB processes (up to 2.04 g/L/day), compared with that in the fed‐batch processes (ranging from 0.39 to 0.49 g/L/day), largely due to the higher cell density maintained. Furthermore, media cost per gram of antibody produced from perfusion was found to be highly comparable with that from fed‐batch; and the media cost for CFB was the highest due to the short batch duration. Our experimental data supports the argument that media cost for perfusion process could be even lower than that in a fed‐batch process, as long as sufficient bioreactor productivity is achieved. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 33:867–878, 2017     

Evaluation of options for harvest of a recombinant E. Coli fermentation producing a domain antibody using ultra scale‐down techniques and pilot‐scale verification

Ultra scale‐down (USD) methods operating at the millilitre scale were used to characterise full‐scale processing of E. coli fermentation broths autolysed to different extents for release of a domain antibody. The focus was on the primary clarification stages involving continuous centrifugation followed by depth filtration. The performance of this sequence was predicted by USD studies to decrease significantly with increased extents of cell lysis. The use of polyethyleneimine reagent was studied to treat the lysed cell broth by precipitation of soluble contaminants such as DNA and flocculation of cell debris material. The USD studies were used to predict the impact of this treatment on the performance and here it was found that the fermentation could be run to maximum productivity using an acceptable clarification process (e.g., a centrifugation stage operating at 0.11 L/m² equivalent gravity settling area per hour followed by a resultant required depth filter area of 0.07 m²/L supernatant). A range of USD predictions was verified at the pilot scale for centrifugation followed by depth filtration. © 2016 The Authors Biotechnology Progress published by Wiley Periodicals, Inc. on behalf of American Institute of Chemical Engineers Biotechnol. Prog., 32:382–392, 2016     

High cell density perfusion culture of hybridoma cells recycling high molecular weight components

We have developed a high cell density and high product concentration culture system recycling high molecular weight components. The production of monoclonal antibodies in high concentration was performed by this culture system with mouse human hybridoma H2 and V6 cells in serum-free defined media.The concentration of IgG after 48 days culture of H2 cells in ITES-eRDF reached 2 mg/ml and the purity of IgG in culture fluid was 61%. In addition, high molecular weight components in serum-free media, such as transferrin or BSA, could be reduced to 5% of the original concentration.     

Characterisation of a generic monoclonal antibody harvesting system for adsorption of DNA by depth filters and various membranes

The physical parameters governing adsorption of DNA by various positively charged depth filters and membranes have been assessed. Buffers that reduced or neutralised the depth filter or membrane charge, and those that impeded hydrophobic interactions were shown to affect their operational capacity, demonstrating that DNA was adsorbed by a combination of electrostatic and hydrophobic interactions. The adsorption profile of DNA by a Sartobind Q anion exchange membrane showed immediate breakthrough, irrespective of challenge DNA concentration or flow rate, and in this case adsorption was by electrostatic interactions only. The production-scale removal of DNA from harvest broths containing therapeutic protein by partitioning of cells and debris from protein in sequential centrifugation and filtration steps, and the concentration of DNA in process supernatant were assessed. Centrifugation reduced the quantity of DNA in the process material from 79.8 g ml^-1 to 9.3 g ml^-1 whereas the concentration of DNA in the supernatant of pre- and post-filtration samples had only marginally reduced DNA content: from 6.3 to 6.0 g ml^-1 respectively. DNA was concentrated to 27.3 g ml^-1 along with monoclonal antibody in the ultrafiltration step. Similar effects were observed in the harvest step for a second antibody.