WO2015118149A1 - Système, appareil et procédé pour anticorps anti-vrs et formules - Google Patents

Système, appareil et procédé pour anticorps anti-vrs et formules Download PDF

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Publication number
WO2015118149A1
WO2015118149A1 PCT/EP2015/052628 EP2015052628W WO2015118149A1 WO 2015118149 A1 WO2015118149 A1 WO 2015118149A1 EP 2015052628 W EP2015052628 W EP 2015052628W WO 2015118149 A1 WO2015118149 A1 WO 2015118149A1
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Prior art keywords
bioreactor
cell
cells
culture medium
downstream unit
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PCT/EP2015/052628
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English (en)
Inventor
José CASTILLO
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Univercells Nv
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Publication of WO2015118149A1 publication Critical patent/WO2015118149A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M25/00—Means for supporting, enclosing or fixing the microorganisms, e.g. immunocoatings
    • C12M25/16—Particles; Beads; Granular material; Encapsulation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K16/00—Immunoglobulins [IGs], e.g. monoclonal or polyclonal antibodies
    • C07K16/08—Immunoglobulins [IGs], e.g. monoclonal or polyclonal antibodies against material from viruses
    • C07K16/10—Immunoglobulins [IGs], e.g. monoclonal or polyclonal antibodies against material from viruses from RNA viruses
    • C07K16/1027—Paramyxoviridae, e.g. respiratory syncytial virus
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/54—Constructional details, e.g. recesses, hinges hand portable
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/04—Filters; Permeable or porous membranes or plates, e.g. dialysis
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/10—Perfusion
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M37/00—Means for sterilizing, maintaining sterile conditions or avoiding chemical or biological contamination
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K2317/00—Immunoglobulins specific features
    • C07K2317/10—Immunoglobulins specific features characterized by their source of isolation or production
    • C07K2317/14—Specific host cells or culture conditions, e.g. components, pH or temperature

Definitions

  • the invention pertains to methods and systems for the production and/or the purification of cells or cell products, such as proteins or peptides. More in particular, the invention provides methods and systems for the production and/or the purification of anti-RSV antibodies and/or formulations.
  • Respiratory syncytial virus is the leading cause of serious lower respiratory tract disease in infants and children.
  • the yearly epidemic nature of RSV infection is evident worldwide, but the incidence and severity of RSV disease in a given season vary by region. In temperate regions of the northern hemisphere, it usually begins in late fall and ends in late spring. It is estimated that RSV illness results in 90,000 hospitalizations and causes 4,500 deaths annually in the United States.
  • Primary RSV infection occurs most often in children from 6 weeks to 2 years old and uncommonly in the first 4 weeks of life during nosocomial epidemics.
  • RSV disease Treatment options for established RSV disease are limited. Severe RSV disease of the lower respiratory tract often requires considerable supportive care, including administration of humidified oxygen and respiratory assistance. Currently, the only approved approach to prophylaxis of RSV disease is passive immunization. A humanized antibody directed to an epitope in the A antigenic site of the F protein of RSV, palivizumab, is approved for intramuscular administration to pediatric patients for prevention of serious lower respiratory tract disease caused by RSV. Due to the high incidence of RSV and the serious risks concerned for infants and newborns, there is need for a more cost-effective and more efficient way of producing anti-RSV antibodies and/or formulations, especially also for developing countries.
  • antibodies or antibody fragments production involves cell culture and/or isolation and/or purification of cell secreted products.
  • Said conventional approaches require numerous manual manipulations that are subject to variations even when conducted by skilled technicians. When used at the scale needed to manufacture large quantities of product, the variability, error or contamination rate may become unacceptable for commercial processes.
  • Production of cell secreted products can be achieved using a bioreactor (fibers, microfibers, hollow fiber, ceramic matrix, fluidizer bed, fixed bed, etc.) or using a stirred tank. This increases product concentration.
  • the systems currently available are general purpose in nature and require considerable time from trained operators to setup, load, flush, inoculate, run, harvest, and unload.
  • Prior art techniques use a large-scale set-up wherein cells are being grown in batch bioreactors of e.g . 10000 liters (L). After a cultivation period, the antibodies of the batch are harvested within about 8 hours. Hereby, the 10000 L of suspension is clarified, the medium is exchanged (cell- culture medium replaced by buffer medium) by diafiltration, and the compounds are separated or purified by chromatography. A further filtration step may follow.
  • the disadvantages of the prior art technique include the use of a big filter, a large amount of buffer medium, a large chromatography column and a considerable necessary amount of purified water. These amounts represent a considerable cost in terms of purified water production and water storage.
  • a major disadvantage is the yield loss in the clarification step which is an essential step of this set-up for obtaining a diafiltration which is efficient enough to exchange the cell-culture medium within the limit of 8 hours.
  • WO 2012/171030 describes an automated integrated system comprising a cell growth unit and purification unit.
  • the system is still quite demanding in use and requires further optimization measures to improve ease of use and to increase output especially that said system is not scalable.
  • One object of the invention is to provide automated and integrated methods and systems for the growth and maintenance of cells but also for variable multiple downstream applications such as harvest and/or purification of cells and/or cell products, in particular anti-RSV antibodies.
  • Another objective of the present invention is to provide anti- RSV formulations. Summary of the invention
  • the present invention provides an integrated automated method for the production of biomolecules such as protein or peptides, in particular for the production of antibodies against RSV.
  • the method comprises the steps of culturing cells in at least one high cell density bioreactor, thereby fluidly connecting said bioreactor with a culture medium supply and a gas or gaseous mixture; fluidly connecting said bioreactor with a downstream unit; and growing cells to a density at least 50 million cells per ml.
  • the bioreactor total volume is at least 10 liters.
  • the method of the present invention further provides anti- RSV formulations comprising anti-RSV antibodies.
  • the present invention provides a system suitable for the implementation of the method of the invention.
  • the system is a small-scale cupboard-sized system and can be placed in a portable clean room.
  • the invention provides a system for the production of biomolecules such as proteins or peptides, in particular for the production of antibodies against RSV.
  • the system comprises a cell culturing unit and a downstream unit which are fluidly connected to each other.
  • Said cell culturing unit comprises at least one perfusion bioreactor, which allows growing cells at a density of at least 50 million cells per ml, and supply means for supplying said bioreactor with cell medium and gas or gaseous mixture.
  • the system is characterized in that the bioreactor total volume is at least 10 liters.
  • the method of the present invention further provides anti-RSV formulations comprising anti-RSV antibodies.
  • Cell products such as antibodies are presently being produced in large-scale facilities.
  • Cells are usually cultured for about 20 days in a considerable volume of culture medium of about 10000 L. Afterwards, cell culture is stopped and the considerable volume of culture medium is then treated to extract the desired molecule. Said facilities are rather expensive and their cost is about $100 million.
  • the present invention provides methods and systems wherein cells are cultured at high density.
  • said high density culture is carried out in a continuous perfusion small size bioreactor. More preferably, high density culture is maintained in the bioreactor.
  • the systems and the methods of the invention provide for an automated, integrated and continuous chain of operations starting from cells growth until obtaining the desired product which can be cells or cells products such as antibodies.
  • a pre-defined small volume of supernatant is further processed in the downstream unit of the system . Processing of the supernatant, in pre-defined small volume, is carried out while maintaining the high cell density culture inside the bioreactor.
  • the advantages of systems and methods of the invention is to provide for high yield cells and/or cell products production, in particular antibodies against RSV, compared to the methods and the systems of the prior art thereby reducing costs of the final product.
  • the systems and methods of the invention also allow production of cells and/or cell products using a significantly smaller amount of purified water than prior art systems and methods.
  • the present invention provides cheaper fully-automated and integrated systems, which cost is at least 5 to 6 times less than the usual large-scale systems. This eventually results in a lower investment and production cost, which is a considerable advantage, e.g. when aiming at manufacturing for third-world countries.
  • the invention allows providing third-world countries with national production systems and also enables pharmaceutical companies without biotech background to produce cell products such as antibodies in bulk in particular antibodies against RSV.
  • Figure 1 shows an embodiment of a bioreactor of the invention.
  • FIG. 2 shows an embodiment of the cell culture unit of the invention.
  • Figure 3 shows the culture unit C which is fluidly connected to a downstream unit D comprising harvest means according to an embodiment of the invention.
  • Figure 4 shows the culture unit C which is fluidly connected to a downstream unit D comprising filtration means and harvest means according to an embodiment of the invention.
  • Figure 5 shows the culture unit C which is fluidly connected to a downstream unit D comprising filtration means and purification means according to an embodiment of the invention.
  • Figure 6 shows the difference between prior art methods used for biomolecules production and the method of the present invention.
  • the present invention concerns a method and system for the production of an anti-RSV antibodies and/or anti-RSV formulation comprising anti-RSV antibodies.
  • the invention specifically aims to provide a method with an optimal efficiency in terms of input of material and products output.
  • the current invention thereto aims to provide a fully integrated and automated methodology and system for the production of anti-RSV antibodies and/or anti-RSV formulation comprising anti- RSV antibodies.
  • a compartment refers to one or more than one compartment.
  • the value to which the modifier "about” refers is itself also specifically disclosed.
  • % by weight refers to the relative weight of the respective component based on the overall weight of the formulation.
  • the present invention provides an integrated automated method for the production of anti-RSV antibodies.
  • the method of the invention is suitable to be carried out by a system comprising a cell culture unit and a downstream unit.
  • the cell culture unit comprises at least one bioreactor for cell growth and/or cells products production.
  • the downstream unit may comprise different components or means suitable for further processing the supernatant, cultured cells and/or cells products, i.e. anti-RSV antibodies.
  • the method and the system of the present invention further provide for the production of anti-RSV formulations comprising anti-RSV antibodies.
  • said anti-RSV formulations comprise palivizumab, motavizumab, MEDI-557 or any combination thereof.
  • the term 'palivizumab' is to be understood as a monoclonal antibody produced by recombinant DNA technology and used in the prevention of respiratory syncytial virus (RSV) infections.
  • Palivizumab is a humanized monoclonal antibody (IgG) directed against an epitope in the A antigenic site of the F protein of RSV.
  • IgG humanized monoclonal antibody
  • Palivizumab reduces the risk of hospitalization due to RSV infection by 55% and 45%.
  • Palivizumab is dosed once a month via intramuscular (IM) injection, to be administered throughout the duration of the RSV season.
  • Palivizumab is also known under the tardename Synagis®.
  • 'motavizumab' is to be understood as a humanized monoclonal antibody for the prevention of respiratory syncytial virus infection.
  • 'MEDI-557' is to be understood as a humanized monoclonal antibody for the prevention of respiratory syncytial virus infection.
  • the method of the current invention comprises the steps of culturing cells in at least one high cell density bioreactor, thereby fluidly connecting said bioreactor with a culture medium supply and a gas or gaseous mixture; fluidly connecting said bioreactor with a downstream u nit; and growing cells to a density at least 50 million cells per ml.
  • the bioreactor total volume is at least 10 L.
  • At least one sensor is preferably provided for measuring the cell density inside the bioreactor.
  • the bioreactor total volume is at least 10 L, preferably at least 20 L, more preferably at least 30 L, even more preferably at least 40 L, most preferably at least 50 L.
  • the bioreactor total volume is at most 1000 L, preferably at most 900 L, more preferably at most 800L, even more preferably at most 700L, most preferably at most 500 L, even most preferably 500 L.
  • the bioreactor total volume is at most 400 L, preferably at most 300 L, more preferably at most 250 L, most preferably at most 100 L.
  • the culture medium volume provided to the bioreactor for culturing cells is sufficient to fill about half of the total volume of said bioreactor.
  • the bioreactor total volume is 1000 L then 400 to 700 L, preferably 450 to 600 L, more preferably 480 to 500 L or any value comprises in the mentioned ranges is provided to the bioreactor for culturing cells.
  • the bioreactor comprises at least 80 L, preferably at least 90 L, more preferably at least 100 L of cultu re medium and at most 200 L, preferably at most 180 L, more preferably at most 150 L, even more preferably at most 140 L and most preferably about 125 L of culture medium .
  • Adapted culture medium refers to the composition of the medium which is required for the growth of the cells. Said compositions are known to the person skilled in the art and generally comprise salts, vitamins, amino acids, sugars or any combination thereof.
  • the culture medium is preferably provided to the bioreactor from an external culture medium container, i.e. not contained in the system of the invention. From said external container, the culture medium is directed to an internal culture medium tank, i .e. positioned inside the system .
  • the culture medium is preheated prior being provided to the bioreactor. More preferably, the culture medium is heated in the internal culture medium tank.
  • the preheat temperature of the culture medium is of from 20 to 40°C, preferably from 25 to 38°C, more preferably from 30 to 37°C. In a most preferred embodiment, said culture medium is pre-heated at about 37°C.
  • a waste collection container into which metabolic wastes are being removed from the bioreactor, is provided.
  • Such containers and the required connections for ensuring waste removal are known to the person skilled in the art.
  • a mixture of culture medium and gas such as pure oxygen, or a mixture of culture medium and gaseous mixture comprising oxygen are provided to the bioreactor through one single supply line or through one inlet of said bioreactor.
  • the use of one single supply line simplifies the setup of the system and method as it reduces the number of required connections and tubings.
  • cells are cultured in the bioreactor for a time period which can vary from few hours to several days depending on the cultured cells.
  • the culture time period is at least 4 hours, at least 10 hours, at least 24 hours, at least 5 days at least 7 days or any time in- between.
  • the cu lture time period is at most 70 days, at most 60 days, at most 50, at most 40 days, at most 25 days, at most 20 days, at most 10 days or any time in-between.
  • viral transduction or introduction of viral vectors can be utilized .
  • Viral replication competent vectors or replicons have been used for a long time as an alternative expression system to increase the yields of therapeutic proteins in mammalian cells.
  • the target gene(s) can be expressed under transcriptional control of viral promoters whereby the mRNAs accumulate to extremely high levels in the cytoplasm after transfection and upon replication, yielding large amounts of target protein.
  • the viral infection can lead to a transduction process without lysis of the cultured cells or to the lysis of the cultured cells thereby bringing the cells content into the supernatant of the bioreactor.
  • hybridoma cells or stably transfected cells can be cultured in order to produce the desired protein or peptide such as an antibody or an antibody fragment.
  • viral replication systems include but are not limiting to polyoma viruses, lentiviral systems, retroviral systems, adenoviral systems, adeno-associated viruses.
  • preferred cells used in the current system include but are not limited to Vero cells, Hek293T cells, COS cells, CHO cells. In a preferred embodiment of the invention, CHO cells are used .
  • bioreactor's supplemented medium is transferred from the bioreactor to or harvested into the downstream unit. It is to be understood that the bioreactor and the downstream u nit are fluidly connected to each other. A pump might be provided for transferring the supernatant into the downstream unit.
  • a preferred embodiment of the cell culture unit C is represented in Figure 2.
  • the bioreactor 1 comprising the cell culture medium 2 is connected to an internal culture medium tank 3. Said connection is provided by at least one in-tubing 4 and an inlet of the bioreactor 1.
  • internal culture medium tank 3 is supplemented with culture medium from an external culture medium container (not represented) which is positioned outside the cupboard-sized system of the invention.
  • Said external culture medium container comprises up to 10 000 L, preferably up to 20 000 L of culture medium which is maintained at room temperature, i.e. about 20°C.
  • the culture medium is preferably pre-heated in the internal culture medium tank 3 to a temperature of about 37°C.
  • Supplemented culture medium also herein called supplemented medium, refers to the supernatant of the bioreactor which might comprise culture medium and/or cultured cells and/or their products.
  • the supernatant of the bioreactor might be devoid of cells and/or their products.
  • Cells product refers to biomolecules such as proteins, peptides, antibodies produced by the cells and/or any other cell biomolecules derived from cell lysis such as cell membranes.
  • At least one pump can be provided for ensuring cell medium transfer from the tank 3 to the bioreactor 1.
  • the medium transfer is performed continuously and/or at a constant rate and/or at variable rates. Said medium transfer can also be performed discontinuously and/or at a constant rate and/or at variable rates.
  • At least one out-tubing 5 which is attached to an outlet of the bioreactor 1 is provided.
  • a control box 9 might be provided in the cell culture unit C for controlling physical and/or chemical parameters of the supernatant collected from the bioreactor.
  • the downstream unit may comprise filtration means and/or harvest means and/or dialysis means and/or biomolecules purification means such as antibodies purification.
  • said downstream unit comprises solely means for harvesting the desired end-product, without any prior filtration/purification/dialysis steps.
  • the components of the downstream unit are easily connected to or disconnected from said unit and can hence be easily replaced, cleaned or sterilized.
  • the downstream unit can be customized depending on the needs and desires of the users, and can be supplied with a combination of any of the aforementioned units.
  • the user is hence provided with multiple end product possibilities, cells, filtered cells, filtered cells products, purified cells products or biomolecules.
  • the user can choose and connect the different compartments of the downstream depending of the desired final product.
  • the downstream unit receives supplemented medium or medium supplemented with biomolecules from said bioreactor in continuous mode.
  • the downstream unit receives at most 1000 ml/min of medium supplemented with biomolecules from said bioreactor in continuous mode.
  • the transfer of the supplemented medium is initiated when a predetermined cell density is reached inside the bioreactor.
  • Said predetermined cell density is at least 30 million/ml, preferably 40 million/ml, more preferably 50 million/ml, most preferably 60 million/ml.
  • culture medium is added from the internal culture medium tank to said bioreactor such as to maintain the initial volume of culture medium in the bioreactor. For instance, if at the start of the process the bioreactor contained 80 L of culture medium, once the transfer of supplemented medium from the bioreactor to the downstream unit is initiated, new culture medium is added to the bioreactor in sufficient volume such as to maintain a volume of 80 L in said bioreactor. If the transfer of supplemented medium from the bioreactor to the downstream unit is performed in continuous mode, the addition of new culture medium from the internal culture medium tank into the bioreactor will be also carried out in continuous mode.
  • the method and the system of the present invention thereby allow the treatment of the supplemented culture medium in the downstream unit in parallel to the growth of the cells in the bioreactor.
  • This provides several advantages compared to processes wherein cells are grown in large bioreactors containing large cell culture volumes followed by stopping said cell culture after a certain time period or when reaching a certain concentration and then starting the downstream processes of the large volume of cell culture. Amongst the advantages we can mention a considerable yield increase and thereby a considerable cost decrease.
  • the medium supplemented with biomolecules received by the downstream unit undergoes at least one process selected from the group comprising filtration, harvesting, dialysis, biomolecules purification and protein concentration or any combination thereof.
  • the supplemented medium harvest is preferably performed in a continuous way at small volume rate.
  • Said volume rate is of at least 100 ml/min, preferably at least 150 ml/min, more preferably at least 200 ml/min, most preferably at least 250 ml/min.
  • Said volume rate is at most 1000 ml/min, preferably at most 800 ml/min, more preferably at most 600 ml/min, most preferably at most 400 ml/min.
  • the supernatant harvest can also be performed in a discontinuous way. The harvested supernatant is then subject to a subsequent treatment selected from simple harvesting, filtering, molecules purification, storage or any combination thereof.
  • the continuous harvest mode of the present invention can be initiated by the operator based on product concentration. The harvest continues until a pre-programmed time interval has passed or until the operator manually terminates the harvesting using a user's interface provided in the system of the invention.
  • Figure 6 shows the difference between prior art methods used for biomolecules production and the method of the present invention.
  • cells are grown for a certain time period or until reaching a certain concentration as shown by curve P of Figure 6.
  • cell culture is stopped and the downstream processes of the large volume of cell culture can be started and some steps such as clarification should be performed in about 8 hours.
  • this methodology leads to an important yield loss and is rather expensive.
  • the method of the present invention starts by culturing cells at high density, of at least 50 million cells per ml. Once the required density is reached, cell culture is maintained through time (curve I of Figure 6) and downstream processing of the supernatant is initiated (Io in Figure 6).
  • Said downstream processing is performed on pre-defined amounts of supernatant and is repeated after fixed or non-fixed time intervals (Ii to I x in Figure 6).
  • the downstream processing is selected from filtration and/or harvesting and/or dialysis and/or biomolecules purification or any combination thereof.
  • the method of the present invention thereby allows a considerable yield increase, cost decrease while using small equipment's requiring less space and easier to entertain.
  • cultured cells are infected and subsequently disrupted/lysed in a thereto designed location in the downstream unit.
  • the supernatant comprising the cell debris and the desired product, anti-RSV antibodies, is then harvested using harvest means from the bioreactor. Harvesting rates are as mentioned above.
  • the supernatant can be harvested and stored for further use into a bag provided in the downstream unit as mentioned above.
  • the harvested supernatant might be subject to a filtration using filtration means prior to storage into a bag of the downstream unit.
  • the collected supernatant can be filtered and/or subject to a purification step for separating a specific molecule, such as an a ntibody, from said supernatant.
  • FIG. 3 shows an embodiment of the system which is adapted for harvesting cells or end product in bulk.
  • the culture unit C is fluidly connected to the downstream unit D through the out-tubing 5.
  • the culture unit C is as described above.
  • a pump or harvest means might be provided for collecting the supernatant of the bioreactor.
  • the pump can be programmed such as to start the supernatant collection from a pre-defined time period from the start of the culture.
  • the pump can be programmed such as to collect a pre-fixed volume of supernatant in an automated continuous mode.
  • the collected supernatant is directed to a bag or a collection tank 6 in which said supernatant will be stored for further applications.
  • FIG. 4 shows an embodiment of the system which is adapted for harvesting and filtering.
  • the culture unit C is fluidly connected to the downstream unit D through the out-tubing 5.
  • the culture unit C is as described above.
  • the out-tubing 5 directs the supernatant to a filtering means 7.
  • a pump, or harvest means, might be provided for collecting the supernatant of the bioreactor.
  • the pump can be programmed such as to start the supernatant collection from a pre-defined time period from the start of the culture.
  • the pump can be programmed such as to collect a pre-fixed volume of supernatant in an automated continuous mode.
  • the collected supernatant is filtered by the filtering means and the filtered supernatant is directed and/or stored into a bag or a collection tank 6 for use in further applications.
  • Purification can be performed using purification means of the downstream unit.
  • Said means can be automated means for obtaining a purified biological product such as protein (e.g., a purified antibody), from the supernatant (e.g ., protein-containing aqueous medium) and harvested as mentioned above.
  • the purification means comprise at least one or any combination of the following : a selection device such a purification chromatography column (affinity purification, ion exchange, etc.), a sequence of purification columns or membrane absorbers at least one liquid reservoir, a device for flowing liquid from the reservoirs and into the selection device, a device for diverting the effluent from the selection device.
  • the purification means are capable of being installed into the small-scale cupboard-sized system of the invention via a single motion or "snap-on” or “quick-load” technique and comprises mechanical and electrical interfaces for communicating with the other components of the system of the invention. It is to be understood that the required buffers and solutions for performing the purification process or step might be provided in at least one bag. Said bag can be positioned inside or outside the downstream unit and is naturally provided with the necessary connections to ensure its connection with to the purification unit.
  • Said purification means can be a combination of clarification, floculation, precipitation of cell debris, lipids, host cell proteins, DNA, as well as ultrafiltration, tangential flow filtration aiming at concentrating the supernatant, or changing the chemical conditions (such as pH, conductivity, ionic strength).
  • Said means can also be chromatographic means, in capture mode or in flow through mode; chromatography can be envisage both in a packed mode, a monolith mode, a membrane based mode or in a fluidized mode; should the chromatography be implemented in a fluidized mode, it can include the use of classical media separated by settling or centrifugation, or (para)magnetic media separated by an external magnetic field . It can be any combination of any of the means described previously.
  • Figure 5 shows an embodiment of the system which is adapted for harvesting, filtering and purifying at least one cell product, such as an antibody.
  • the culture unit C is fluidly connected to the downstream unit D through the out-tubing 5.
  • the culture unit C is as described above.
  • the out-tubing 5 directs the supernatant to a filtering means 7.
  • a pump, or harvest means, might be provided for collecting the supernatant of the bioreactor.
  • the pump can be programmed such as to start the supernatant collection from a pre-defined time period from the start of the culture.
  • the pump can be programmed such as to collect a pre-fixed volume of supernatant in an automated continuous mode.
  • the collected supernatant is then directed to purification means 12 of the downstream unit D.
  • the obtained purified cell product can be stored in a tank connected to the purification means or directed to another component of the downstream for further applications.
  • the selection device can be a chromatography column such as such as affinity chromatography, ionic exchange chromatography (e.g. anion or cation), hydrophobic interaction chromatography, size exclusion chromatography (SEC), immuno-affinity chromatography which is a column packed with an affinity resin, such as an anti-IgM resin, a Protein A, a Protein G, or an anti-IgG resin.
  • Anion exchange exploits differences in charge between the different products contained in the harvested supernatant.
  • the neutrally charged product passes over the anion exchange chromatography column cartridge without being retained, while charged impurities are retained .
  • the size of the column may vary based on the type of protein being purified and/or the volume of the solution from which said protein is to be purified .
  • the purification means e.g., an affinity column, and/or the filtration means are connected to m ultiple liquid reservoirs.
  • the reservoirs each contain liquid, such as a wash buffer, an elution buffer, or a neutralization solution, for delivery to the purification means and/or the filtration means.
  • the purification means further comprise pre-sanitized or pre-sterilized device for flowing liquid from the reservoirs into the chromatography column for instance. For example, pre-sterilized valves and tubing which connect the reservoirs to the column might be used .
  • Purification using a chromatography column is known to the person skilled in the art and can be performed using the adequate buffers for eluting the desired biomolecules.
  • the eluted purified protein can be automatically deposited into a pre- sterilized, disposable collection vessel provided in the downstream unit and removed from the purification means.
  • the eluted purified protein can undergo further automated processing.
  • a purified protein, e.g ., antibody is substantially free from host cell contaminants such as host cell proteins, nucleic acids and endotoxins.
  • the eluted protein is transferred to different solutions.
  • the transfer occurs automatically using a pre-sterilized diafiltration module.
  • Diafiltration is the fractionation process that washes smaller molecules through a membrane and keeps molecules of interest in the retentate. Diafiltration can be used to remove salts or exchange buffers.
  • discontinuous diafiltration the solution is concentrated, and the lost volume is replaced by new buffer. Concentrating a sample to half its volume and adding new buffer four times can remove over 96% of the salt.
  • continuous diafiltration the sample volume is maintained by the inflow of new buffer while the salt and old buffer are removed . At least 99% of the salt can be removed by adding up to seven volumes of new buffer during continuous diafiltration.
  • the diafiltration module is used to further purify the protein (e.g., the antibody) and uses the tangential flow filtration principle whereby molecules over 50,000 Daltons (e.g ., the antibodies, such as IgG and IgM) cannot pass through the membrane but small molecules, such as buffers, can pass through. Accordingly, the diafiltration module can be used to exchange one buffer for another and is a more efficient su bstitute for dialysis. Diafiltration can be used to neutralize pH and as a concentration step (to concentrate the cell product).
  • the protein e.g., the antibody
  • the tangential flow filtration principle whereby molecules over 50,000 Daltons (e.g ., the antibodies, such as IgG and IgM) cannot pass through the membrane but small molecules, such as buffers, can pass through. Accordingly, the diafiltration module can be used to exchange one buffer for another and is a more efficient su bstitute for dialysis. Diafiltration can be used to neutralize pH and as a concentration step (to concentrate
  • the harvest means and/or the filtration means and/or the purification means include at least one monitoring device for monitoring the circulating medium : non-filtered harvested supernatant, filtered supernatant, purified and eluted product, etc.
  • the monitoring device can be a probe or sensor for measuring the conductivity and/or the pH and/or absorbance at a particular wavelength of said circulating medium.
  • One or more pressure sensors may be included for monitoring circulating medium pressure for excessive pressures, or for control of pump speed, e.g ., to maintain the pump speed of the harvest means for instance at a desired pressure.
  • the system is adapted to the desired product. This means that if cells in bulk are to be provided, the system will comprise a cell culture unit C and a downstream unit D in which at least one collection bag is provided. If filtered cells are to be provided, the system will comprise the cell culture unit and the downstream unit in which filtering means and at least one collection bag are provided. If a specific protein is to be provided, the system will comprise the cell culture unit and the downstream unit in which at least filtering means and purification means are provided .
  • the method further comprises the step of measuring physical and/or chemical parameters of the cell culture and/or culture medium.
  • Said parameters are selected from the group comprising temperature, pH, salinity, acidity or any combination thereof. Measurements can be performed on the culture medium before being injected into the bioreactor and/or in the supernatant which is collected from the bioreactor.
  • the method and/or the system of the present invention allows a biomolecules, such as monoclonal antibodies, yield increase compared to the conventional methods.
  • Said biomolecules yield is of from 15 to 100 g/L, preferably from 20 to 60 g/L, more preferably from 25 to 50 g/L, even more preferably from 30 to 45 g/L, most preferably from 35 to 40 g/L of bioreactor or any value comprised within the mentioned ranges.
  • the method and the system of the present invention are devoid of closed loops or recirculation loops. This means that the supplemented culture medium is not returned to the bioreactor at any stage of the process such as after its passage through the downstream unit. This is advantageous as it considerably reduces contamination risks. Furthermore, this simplifies the setup and the installation of the system thereby reducing costs.
  • the present invention provides a system for the production of anti-RSV antibodies and/or anti-RSV formulations comprising anti-RSV antibodies.
  • the system comprises a cell culturing unit and a downstream unit which are fluidly connected to each other.
  • Said cell culturing unit comprises at least one perfusion bioreactor, which allows growing cells at a density of at least 50 million cells per ml, and supply means for supplying said bioreactor with cell medium and gas or gaseous mixture.
  • the system is characterized in that the bioreactor total volume is at least 10 liters. .
  • the downstream unit is separate from and positioned outside the cell culturing unit.
  • the bioreactor allows high density cell growth.
  • Said density is of at least 50 million cells/ml, preferably at least 80 million cells/ml, more preferably at least 100 million cells/ml, most preferably at least 200 million cells/ml. Said density can reach 600, 500, 400 or 300 million cells/ml.
  • the bioreactor total volume is at least 10 L, preferably at least 20 L, more preferably at least 30 L, even more preferably at least 40 L, most preferably at least 50 L.
  • the bioreactor total volume is at most 1000 L, preferably at most 900 L, more preferably at most 800L, even more preferably at most 700L, most preferably 500 L.
  • the bioreactor total volume is at most 400 L, preferably at most 300 L, more preferably at most 250 L, most preferably at most 100 L.
  • the bioreactor total volume and the bioreactor itself according to the invention are smaller compared to the conventional bioreactors used for high cell density culture. This is advantageous in terms of required space for the system and for ease of use.
  • the system is implemented in small-scale cupboard which can be a portable chamber or portable clean room .
  • the dimensions of the small-scale cupboard are 0.8x1.6x1.8m 3 .
  • the system according to an embodiment of the invention can be placed in a portable clean room.
  • the cell culture unit and the downstream unit are physically separate but designed to be placed together in a portable chamber (e.g ., adjacent to one another).
  • the cell culture unit and/or the downstream unit can transfer data and coordinate activity with each other using methods known in the art such as a communication port (e.g ., an infrared communication port, desktop or laptop computer, etc).
  • the downstream unit can be placed next to the cell culture unit towards the end of the production period, or before. At least one tubing line from each unit fluidly connects said units to each other.
  • the operator initiates the culture process and/or harvesting process and/or the purification process through a user interface such as a touch screen interface on portable chamber and/or the cell culture unit.
  • the operating temperature of the cell culture unit is between 20°C and 40°C, more by preference between 25°C and 37°C.
  • the operating temperature of the downstream unit may be between 0°C and 25°C, more preferably between 1°C and 20°C, even more preferably between 2°C and 10°C, most preferably about 4°C.
  • the temperature of both units is maintained by cooling and/or warming units and maintenance of the temperature may be checked by sensors. Integrating components, functions, and operations greatly reduces manpower and cost needed to produce a cells and/or cell-derived product.
  • the integrated system reduces preparation and loading time and reduces the number of operator induced errors which can cause failure.
  • Process sequencing reduces operator time needed and allows sequential operations to be automatically. Modularizing the fu nctions into a cell cu lture unit and a purification unit allows higher utilization of hardware and lower costs.
  • the cell culture unit provides for production of cells and cell derived products in a closed, self- sufficient environment.
  • Said unit may comprise at least one bioreactor for cells and/or their products expansion with minimal need for technician interaction.
  • Said bioreactor may be attached to the system in a fixed manner, or may be removably attached to said system.
  • the bioreactor used in the method and/or the system of the invention can be any type of bioreactor that allows high cell density cultures.
  • Said bioreactor is preferably a perfusion bioreactor.
  • Said bioreactor might be provided with carriers such as fibers, microfibers, hollow fibers or hollow microfibers. Alternatively, those carriers can be microbeads in suspension, in packed bed or in fluidized mode. Said carriers provide for an excellent substrate for the cells to grow on.
  • the bioreactor comprises microcarriers, by preference polyester microfiber carriers.
  • the microfiber carriers are biocompatible. By preference, they are nonwoven polyester carriers.
  • the cell culture unit follows pre- programmed and automated processes to deliver culture media to the bioreactor and/or maintain pH and/or maintain temperature.
  • Standard or unique cell culture growth parameters can be programmed, such that, various cell types can be expanded and such that cells or cell products can be harvested in an efficient, reproducible manner with minimal chance of human error.
  • said carriers have received a plasma treatment in order to make them hydrophilic.
  • the cells will attach to the carriers as a 3D growth substrate.
  • the supernatant may become loaded with the desired end product.
  • the carriers present in the bioreactor provide a cell growth surface of at least 1000 square meters (m 2 ), preferably at least 1200 m 2 , more preferably at least 1500 m 2 , more preferably at least 1800 m 2 .
  • the carriers provide a cell growth surface of at most 3000 m 2 , more preferably at most 2800 m 2 , more preferably at most 2500 m 2 , most preferably at most 2200 m 2 .
  • the cell growth surface provided by the carriers is about 2000 m 2 .
  • the bioreactor used in the method and/or the system of the invention is a small size bioreactor.
  • Said bioreactor can be a circular bioreactor having a diameter of at least 30 cm, preferably at least 40 cm and at most 70 cm, preferably at most 60 cm, more preferably at most 50 cm .
  • Said bioreactor can also be a rectangular or square bioreactor having a height of least 40 cm, preferably at least 50 cm, more preferably at least 60 cm and at most 110 cm, preferably at most 100 cm, more preferably at most 80 cm, most preferably at most 70 cm .
  • the width of said rectangular or square bioreactor is least 40 cm, preferably at least 50 cm, more preferably at least 60 cm and at most 100 cm, preferably at most 90 cm, more preferably at most 80 cm, most preferably at most 70 cm.
  • the bioreactor can be gyrated or motioned thereby increasing oxygen transfer and ensuring gas equilibrium in said bioreactor. This allows to run cultures in a bioreactor which is devoid of sensors thereby providing a simple and less complicated bioreactor installation compared to the bioreactors of the prior art. In addition, the use of a bioreactor devoid of sensors provides for a considerable decrease of contamination risk. Motioning the bioreactor further improves cells harvesting. Indeed, harvesting cells from a carriers-containing bioreactor, such as fibers or microfibers bioreactors has been difficult to accomplish. Typically, cells are sticky and attach themselves to the carriers or to other cells and form clusters.
  • the bioreactor may have a rigid or a non-rigid outer body. Rigid outer body allows for the bioreactor case to be flexed causing microfiber movement. This movement enhances the release of cells that have attached to the side of the bioreactor matrix.
  • the bioreactor is a perfusion bioreactor.
  • the bioreactor is provided with a single inlet. More preferably, gas and culture medium are introduced into the bioreactor through the same inlet. Perfusion of gas and culture medium into the bioreactor via a single inlet minimizes contamination risks as only one inlet of the bioreactor has to be connected to a perfusion line.
  • the bioreactor is thereby provided with an easy connection and disconnection system to the perfusion line thereby simplifying its separation from the system if the bioreactor needs to be replaced for instance.
  • An example of bioreactor suitable to be used in the method and/or the system of the invention is represented in Figure 1.
  • the bioreactor 1 is a perfusion bioreactor having a doughnut shape and is about half filled with culture medium 2 during cell culture.
  • the bioreactor is provided with at least one inlet for the introduction of gas and/or culture medium and at least one outlet for the collection of the culture product and/or the medium contained in the bioreactor.
  • At least one in-tubing is provided for fluidly connecting the bioreactor, via its inlet, to a culture medium tank and/or a gaseous source.
  • At least one out-tubing is provided for fluidly connecting the bioreactor, via its outlet, to a downstream unit and/or any other device.
  • the bioreactor is removably connectable to a cell culture medium container.
  • the culture medium is provided into the bioreactor inlet using at least one pump.
  • the medium is pre-heated to a temperature of between 25°C to 37°C and mixed prior to transfer to the bioreactor. This ensures that the cells will not perceive a cold-shock when being contacted with new medium (which would negatively affect their growth) as well as ensu re that all nutrients in the medium are mixed and present in the required amounts.
  • the medium can be a liquid comprising a well-defined mixture of salts, amino acids, vitamins and one or more protein growth factors.
  • the culture medium serves to deliver nutrients to the cell and conversely, to remove or prevent a toxic build-up of metabolic waste.
  • Gas such as pu re oxygen or a gaseous mixture comprising oxygen is equally provided through the bioreactor inlet.
  • Oxygen is an essential requirement for the normal growth of mammalian cells.
  • said gas or gaseous mixture is supplied under pressure.
  • cells will be exposed to dissolved oxygen concentrations of 300 ⁇ or less (160 mmHg partial pressure), by preference less than 200 ⁇ , most preferably between 20 and 150 ⁇ .
  • gas or gaseous mixture and culture medium will be intermixed prior being supplied to the bioreactor.
  • the mix of gas or gaseous mixture and culture medium are supplied to through one supply line.
  • said gas or gaseous mixture is chosen from air or oxygen.
  • air is being used .
  • Air is to be seen as a gaseous mixture, comprising approximately 78% of nitrogen, 21% of oxygen and argon and carbon dioxide.
  • Supply of air instead of pure oxygen or oxygen enriched atmospheres has as an advantage that the system employing the method can be omitted of supplying units of highly concentrated oxygen, which may otherwise imply a fire or explosion hazard .
  • aqueous medium such as a cell culture medium
  • oxygen transfer rate in a fermentor or bioreactor is described by :
  • K L a is the oxygen transfer coefficient in h _1 ;
  • the oxygen transfer coefficient (K L a) in the current method is at least 20 h _1 , preferably at least 30 h _1 , more preferably at least 35 h _1 .
  • Said oxygen transfer coefficient is at most 100 h _1 , preferably at most 50 h _1 , more preferably at most 40 h _1 .
  • a high oxygen transfer coefficient and therefore also high OTR will have a positive influence on the cell growth/health and hence the yield of the desired end product. It was found by the inventors of the current method that an oxygen transfer coefficient as defined above is particularly beneficial in terms of product yield, even when making use of a rather small amount of cell starter culture.
  • the bioreactor of the system and/or the method of the invention comprise carriers and is subject to motioning.
  • the carriers and the motioning increase in a synergetic way the oxygen transfer coefficient in the bioreactor.
  • Motioning the bioreactor which is at least partially filled with culture medium, makes part of the carriers travel from a liquid phase, in which they are in contact with the culture maxim m, to a gas phase, in which they are not in contact with said medium . This increased oxygen transfer rate by at least 10 times compared to bioreactors of the prior art.
  • the system is provided with necessary and suitable connections for diverting cell culture waste into a waste container.
  • the bioreactor of the system is fluidly connectable to at least one downstream unit.
  • the downstream unit comprises pluggable means selected from the group comprising at least one filtration means, at least one harvest means, at least one dialysis means, at least one biomolecules purification means and at least one protein concentration unit or any combination thereof.
  • the downstream unit comprises at least one harvest means which is provided with at least one inlet and at least one outlet. Said means of the downstream unit is connectable to the cell culture unit of the system . Preferably the connection is provided by connecting the bioreactor out-tubing to said harvest means.
  • the harvest means comprise at least one tubing for directing the collected supernatant to another component of the downstream unit.
  • the harvest means further comprise at least on pump for withdrawing the supernatant from the bioreactor.
  • the downstream unit comprises at least one filtration means which is provided with at least one inlet and at least one outlet. Said means can be fluidly connected to the bioreactor by its out-tubing or fluidly connected to the harvest means of the downstream unit.
  • the filtering means comprises a filter that will selectively retain molecules based on their mass in Dalton for instance.
  • the filtration means might comprise virus hollow filters might be used to filter and remove virus particles from the supernatant. In this case, virus filtration works on the principle of size exclusion. When a protein solution with possible viral contamination is introduced into these hollow filters, the smaller proteins penetrate the filter wall and work their way to the outside of the filter while the larger virus particles are retained .
  • the downstream unit comprises at least one purification means which is provided with at least one inlet and at least one outlet.
  • Said means can be fluidly connected to the bioreactor by its out-tubing or fluidly connected to the harvest means or the filtration means of the downstream unit.
  • the purification means comprises at least one selection de vice as described earlier.
  • the system comprises a cell culture unit and a downstream unit.
  • the cell culture unit comprises at least one bioreactor for culturing cells.
  • Said bioreactor is connected to a culture medium tank for receiving culture medium .
  • at least one out-tubing attached to an outlet of the bioreactor is provided.
  • Said out-tubing is suitable to be connected to the harvest means inlet, filtering means inlet or purification means inlet of a downstream unit thereby fluidly connecting both units to each other.
  • the bioreactor out-tubing is connected to the harvest means inlet.
  • the harvest means outlet is connected to a filtration means inlet and the filtration means outlet is connected to the purification means inlet.
  • tubing and/or pump can be provided within the system for achieving the fluid connection between the different compartments of the cell culture unit and/or of the downstream unit.
  • the system can be provided with a plurality of switch valves used to route the fluids between said different compartments.
  • a software program for running the system and the method according to an embodiment of the invention can be provided .
  • the method and/or the system of the present invention can be used for the culture of any cell line and/or for the production of any desired protein and peptide.
  • Possible cultured cell lines are the Vera cells, the CHO cells, COS cells, 293T cells, HeLa cells, Hep-2 cells, MCF-7 cells, U373 cells or any other cell line.
  • CHO cells are being used.
  • biosimilar' antibodies is to be understood as 'generic' versions of 'originator' antibodies which have the same amino acid sequence as those 'originator' antibodies but which are produced from different clones and/or by different manufacturing processes.
  • the method and/or the system can be used for the production of:
  • Anti-inflammatory biomolecules or any antibody such as infliximab, adalimumab, basiliximab, daclizymab, omalizumab, palivizumab and abciximab
  • - Anti-cancers biomolecules such as gemtuzumab, alemtuzumab, rituximab, transuzumab, nimotuzumab, cetuximab, bevacizumab,
  • the method and/or system is used for the production of anti-RSV formulations. More by preference, such formulations comprise palivizumab, motavizumab or MEDI-557.
  • RSV-antibody based vaccine The methodology and system of the current invention were used for the production of an RSV- antibody based vaccine.
  • liquid formulations of a humanized monoclonal antibody which neutralizes a broad range of RSV (Respiratory Syncytial Virus) isolates In particu lar, the current invention may be used to produce liquid formulations of SYNAGIS®, or an antigen-binding fragment thereof.
  • SYNAGIS® The amino acid sequence of SYNAGIS® is disclosed, e.g ., in Johnson et al., 1997, J. Infectious Disease 176 : 1215-1224, and U.S. Pat. No. 5,824,307.
  • the properties and uses of SYNAGIS® are also disclosed in, e.g ., other applications, see, e.g., U.S. patent application Ser. No. 09/724,396 filed Nov. 28, 2000; U.S. patent application Ser. No. 09/996,265 filed Nov. 28, 2001 and U.S. patent application Ser. No. 10/403,180 filed Mar. 31, 2003, all of which, and in particular the amino acid sequence of SYNAGIS®, are incorporated herein by reference.
  • - cultivating cells by preference CHO cells according to the method and the system of the current invention.
  • Stable cell lines expressing the desired antibody were used,
  • MW molecular weight
  • the liquid formulations comprising the antibody were prepared as unit dosage forms by preparing a vial containing an aliquot of the liquid formulation for a one-time use.
  • a unit dosage per vial may contain 1 ml, 2 ml, 3 ml, 4 ml, 5 ml, 6 ml, 7 ml, 8 ml, 9 ml, 10 ml, 15 ml, or 20 ml of different concentrations of SYNAGIS® or an antigen-fling fragment thereof ranging from about 15 mg/ml to about 300 mg/ml concentration of SYNAGIS® or an antigen-binding fragment thereof which immunospecifically binds to a RSV.
  • these preparations were adjusted to a desired concentration by adding a sterile diluent to each vial.
  • the liquid formulations of the present invention were sterilized by various sterilization methods, including sterile filtration, radiation, etc.
  • the diafiltrated antibody formulation was filter-sterilized with a presterilized 0.2 or 0.22-micron filter.
  • Sterilized liquid formulations of the present invention may be administered to a subject to prevent, treat, manage or ameliorate a RSV infection or one or more symptoms thereof.
  • the formulations may be lyophilized.
  • the invention encompasses lyophilized forms of the formulations of the invention although such lyophilized formulations are not necessary and thus not preferred.
  • the current example may also be applied to other well-known antibody-based formualtions such as, but not limiting infliximab, adalimumab, basiliximab, daclizymab, omalizumab, gemtuzumab, alemtuzumab, rituximab, transuzumab, nimotuzumab, cetuximab, bevacizumab, abciximab, motavizumab, or MEDI-557.
  • infliximab adalimumab
  • basiliximab basiliximab
  • daclizymab omalizumab
  • gemtuzumab alemtuzumab
  • rituximab transuzumab
  • nimotuzumab cetuximab
  • bevacizumab abciximab
  • motavizumab motavizumab
  • MEDI-557

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Abstract

La présente invention concerne un procédé automatisé de production de formules comprenant des anticorps contre le Virus Respiratoire Syncytial (VRS) comprenant les étapes consistant à cultiver des cellules dans au moins un bioréacteur à haute densité cellulaire, reliant ainsi par une connexion fluidique ledit bioréacteur à une alimentation en milieu de culture et un gaz ou un mélange gazeux ; à relier par une connexion fluidique ledit bioréacteur à une unité en aval ; et à réaliser la croissance de cellules à une densité d'au moins 50 millions de cellules par ml. Le volume total du bioréacteur est d'au moins 10 litres. La présente invention concerne également un système adapté à la mise en application du procédé. Le système est un système à petite échelle de la taille d'une armoire et peut être placé dans une salle blanche portative.
PCT/EP2015/052628 2014-02-10 2015-02-09 Système, appareil et procédé pour anticorps anti-vrs et formules WO2015118149A1 (fr)

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US11999929B2 (en) 2020-04-10 2024-06-04 Terumo Bct, Inc. Methods and systems for coating a cell growth surface

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