WO2005095578A1 - Process for cell culturing by continuous perfusion and alternating tangential flow - Google Patents

Process for cell culturing by continuous perfusion and alternating tangential flow Download PDF

Info

Publication number
WO2005095578A1
WO2005095578A1 PCT/EP2005/002374 EP2005002374W WO2005095578A1 WO 2005095578 A1 WO2005095578 A1 WO 2005095578A1 EP 2005002374 W EP2005002374 W EP 2005002374W WO 2005095578 A1 WO2005095578 A1 WO 2005095578A1
Authority
WO
WIPO (PCT)
Prior art keywords
cells
cell culture
cell
process according
perfusion
Prior art date
Application number
PCT/EP2005/002374
Other languages
French (fr)
Inventor
John Crowley
Maike WÜBBEN
Jose Manuel Coco Martin
Original Assignee
Dsm Ip Assets B.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=34961830&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2005095578(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority to KR1020067018075A priority Critical patent/KR101050585B1/en
Priority to US10/591,118 priority patent/US8206981B2/en
Priority to ES05715787.7T priority patent/ES2456015T3/en
Priority to EP05715787.7A priority patent/EP1720972B1/en
Priority to CNA2005800071754A priority patent/CN1930281A/en
Priority to DK05715787.7T priority patent/DK1720972T3/en
Priority to JP2007501239A priority patent/JP2007525984A/en
Priority to CA002557046A priority patent/CA2557046A1/en
Priority to SI200531842T priority patent/SI1720972T1/en
Priority to PL05715787T priority patent/PL1720972T3/en
Application filed by Dsm Ip Assets B.V. filed Critical Dsm Ip Assets B.V.
Priority to AU2005229359A priority patent/AU2005229359C1/en
Publication of WO2005095578A1 publication Critical patent/WO2005095578A1/en
Priority to IL177724A priority patent/IL177724A/en
Priority to IL205606A priority patent/IL205606A/en
Priority to US13/478,307 priority patent/US20130266985A1/en
Priority to US14/052,878 priority patent/US9260695B2/en

Links

Classifications

    • 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
    • C12M3/00—Tissue, human, animal or plant cell, or virus culture apparatus
    • C12M3/06—Tissue, human, animal or plant cell, or virus culture apparatus with filtration, ultrafiltration, inverse osmosis or dialysis means
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C12N5/06—Animal cells or tissues; Human cells or tissues
    • C12N5/0602—Vertebrate cells
    • C12N5/0618—Cells of the nervous system
    • C12N5/0621—Eye cells, e.g. cornea, iris pigmented cells
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/14—Fungi; Culture media therefor
    • C12N1/16—Yeasts; Culture media therefor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K16/00—Immunoglobulins [IGs], e.g. monoclonal or polyclonal antibodies
    • 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
    • C12M25/10—Hollow fibers or tubes
    • 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
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C12N5/06—Animal cells or tissues; Human cells or tissues
    • C12N5/0602—Vertebrate cells
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/26—Preparation of nitrogen-containing carbohydrates
    • C12P19/28—N-glycosides
    • C12P19/30—Nucleotides
    • C12P19/34—Polynucleotides, e.g. nucleic acids, oligoribonucleotides
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P21/00—Preparation of peptides or proteins
    • 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
    • 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
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/44—Means for regulation, monitoring, measurement or control, e.g. flow regulation of volume or liquid level
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N2521/00—Culture process characterised by the use of hydrostatic pressure, flow or shear forces

Definitions

  • the present invention relates to perfusion culturing of cells.
  • the present invention discloses a process for the culturing of cells by perfusion culturing of a cell culture comprising cell culture medium and cells, wherein cell culture medium is added to the cell culture, wherein the cell culture is circulated over a filter module comprising hollow fibers resulting in an outflow of liquid having a lower cell density than the cell culture and wherein the flow within the filter module is an alternating tangential flow. It has surprisingly been found that by perfusion culturing of animal, in particular mammalian, cells or yeast cells according to the invention, extremely high viable cell densities can be obtained, whereas the cell culture further displays an extremely high cell viability.
  • the perfusion process of the invention leads to less cell aggregation in the culture, and even to a culture being a suspension of single cells without visible aggregates.
  • Cell aggregation during perfusion cell culturing is disadvantageous, because process control is more difficult, due to, for example, the heterogeneity in metabolic profiles of cells within the cell aggregates. This is especially troublesome if cells form aggregates of 5 cells or more and when the aggregates comprise in total 5 % or more of the total amount of cells.
  • a perfusion process is described in US 6,544,424.
  • Perfusion culturing of cells has its conventional meaning in the art, i.e. it means that during culturing cells are retained by a separation device in which there is an outflow of liquid having a lower cell density than prior to separation and in which there is an inflow of the cell culture medium.
  • the separation device is a filter module comprising hollow fibers.
  • Perfusion culturing includes, but is not limited to continuous flow and semi- continuous flow, for example step-wise flow or staggered flow.
  • With the term “hollow fiber” is meant a tubular membrane. The internal diameter of the tube is preferably between 0.3 and 6.0 mm, more preferably between 0.5 and 3.0 mm, most preferably between 0.5 and 2.0 mm.
  • the mesh size in the membrane is chosen such that the size of the pores in the mesh is close to the diameter of the cells, ensuring a high retention of cells while cell debris can pass the filter.
  • the mesh size is between 3-30 ⁇ m.
  • Filter modules comprising hollow fibers are commercially available from for example General Electric (formerly Amersham). With "alternating tangential flow within the filter module” is meant that there is one flow in the same direction as (i.e. tangential to) the membrane surfaces of the hollow fibers, which flow is going back and forth, and that there is another flow in a direction substantially perpendicular to said filter surface. Tangential flow can be achieved according to methods known to the person skilled in the art.
  • alternating tangential flow can be achieved using one pump to circulate the cell culture over a filter module comprising hollow fibers and another pump to remove the liquid having a lower cell density than prior to the filter separation.
  • any type of cell culture medium suitable for the culturing of cells can in principle be used. Guidelines for choosing a cell culture medium and cell culture conditions are well known in the art and are for instance provided in Chapter 8 and 9 of Freshney, R. I. Culture of animal cells (a manual of basic techniques), 4th edition 2000, Wiley-Liss and in Doyle, A., Griffiths, J. B., Newell, D. G. Cell &Tissue culture: Laboratory Procedures 1993, John Wiley & Sons.
  • a cell culture medium for mammalian cells comprises salts, amino acids, vitamins, lipids, detergents, buffers, growth factors, hormones, cytokines, trace elements and carbohydrates.
  • salts include magnesium salts, for example MgCI 2 .6H 2 O, gSO 4 and MgSO 4 .7H 2 O iron salts, for example FeSO 4 .7H 2 O, potassium salts, for example KH 2 PO 4 , KCI; sodium salts, for example NaH 2 PO 4 , Na 2 HPO 4 and calcium salts, for example CaCI 2 .2H 2 O.
  • amino acids are all 20 known proteinogenic amino acids, for example hystidine, glutamine, threonine, serine, methionine.
  • vitamins include: ascorbate, biotin, choline.CI, myo-inositol, D-panthothenate, riboflavin.
  • lipids include: fatty acids, for example linoleic acid and oleic acid; soy peptone and ethanol amine.
  • detergents include Tween 80 and Pluronic F68.
  • An example of a buffer is HEPES.
  • growth factors/hormones/cytokines include IGF, hydrocortisone and (recombinant) insulin.
  • trace elements are known to the person skilled in the art and include Zn, Mg and Se.
  • carbohydrates include glucose, fructose, galactose and pyruvate.
  • the pH, temperature, dissolved oxygen concentration and osmolarity of the cell culture medium are in principle not critical and depend on the type of cell chosen.
  • the pH, temperature, dissolved oxygen concentration and osmolarity are chosen such that it is optimal for the growth and productivity of the cells.
  • the person skilled in the art knows how to find the optimal pH, temperature, dissolved oxygen concentration and osmolarity for the perfusion culturing.
  • the optimal pH is between 6.6 and 7.6, the optimal temperature between 30 and 39°C, the optimal osmolarity between 260 and 400mOsm/kg.
  • Cells that are advantageously subjected to the process of the invention may be any cell type benefiting from this process, i.e.
  • an extremely high viable cell density is a density of at least 80 x 10 6 cells per mL, preferably at least 100 x 10 6 cells per mL, more preferably at least 110 x 10 6 cells per mL, more preferably at least 120 x 10 6 cells per mL, more preferably at least 130 x 10 6 cells per mL, most preferably at least 140 x 10 6 cells per mL.
  • a suitable upper limit in the cell density may lie around 500 x 10 6 cells per mL.
  • the extremely high cell density of the process of the invention is accompanied by an extremly high cell viability.
  • An extremely high cell viability is a viability of at least 90%, preferably at least 95%, more preferably at least 97%, most preferably at least 99%. It is to be understood that the very high viable cell density and very high cell viability are reached after a certain period of perfusion culturing, generally when the cells have reached a steady state, for mammalian cells typically 12 to 25 days after the initiation of perfusion culturing.
  • the process of the invention is suitable for culturing animal cells or yeast cells, especially for culturing mammalian cells.
  • the process of the invention is further especially suitable for culturing cells that easily or inherently form aggregates during culturing, especially during perfusion culturing (so-called aggregating cells).
  • the process of the invention not only diminishes aggregate disposal on the filter membrane, but also diminishes aggregation of cells during the perfusion culture process, even aggregation of cells with an inherent tendency to form aggregates.
  • the culturing of aggregating cells according to the invention results in a culture wherein aggregates of at least 5 cells comprise at the most 5 % of the total amount of cells, preferably at the most 4 %, more preferably at the most 3 %, even more preferably at the most 2 % of the total amount of cells.
  • the culturing of aggregating cells according to the invention results in a culture that is a real single cell suspension.
  • Aggregating cells are cells that form aggregates of at least 5 cells, the aggregates comprising in total at least 5 % of the total amount of cells.
  • the aggregates consist of at least 6, more preferably at least 7, even more preferably at least 8, even more preferably at least 9, even more preferably at least 10 cells.
  • the aggregates comprise in total at least 7%, more preferably at least 10 %, most preferably at least 15% of the total amount of cells.
  • mammalian cells examples include: CHO (Chinese Hamster Ovary) cells, hybridomas, BHK (Baby Hamster Kidney) cells, myeloma cells, human cells, for example HEK-293 cells, human lymphoblastoid cells, PER.C6® cells, mouse cells, for example NS0 cells.
  • yeast cells include Saccharomyces cerevisiae, Phaffia rhodozyma, Kluyveromyces lactis, or yeast cells from the genus Pichia .
  • mammalian cells are used, more preferably CHO, NS0, PER.C6® cells.
  • aggregating cells cells known for their aggregating behaviour during culturing.
  • PER.C6® cells are used.
  • Cell aggregation may for example be determined under a microscope.
  • the rate of addition of cell culture medium to the culture influences the viability and the density of the cells.
  • the perfusion rate is expressed in liters per day
  • the SPR is the specific perfusion rate, i.e. the rate in which the cell culture medium is fed to the cell culture expressed as the volume of medium added per viable cell per time unit and wherein the viable cell density is the number of viable cells per unit of volume.
  • the number of viable cells can be determined by the person skilled in the art, for example via the trypan blue exclusion method.
  • the specific perfusion rate is preferably chosen between 0.01 and 0.3 nL/cell/day, more preferably between 0.01 and 0.2 nL/cell/day. It may be of advantage to take into account additional parameters when adjusting the perfusion rate, for example the amount of glucose to be fed to the culture and/or the oxygen concentration.
  • the glucose perfusion rate is preferably chosen between 3 and 20 mmoles/L, more preferably between 5 and 15 mmoles/L, as part of the medium perfusion rate.
  • the outflow rate of the liquid is determined by the perfusion rate and is generally chosen at an equal value.
  • the outflow liquid is substantially devoid of viable cells.
  • biomass i.e. cells in cell culture
  • additional cell culture medium is added to the cell culture to compensate for the biomass removal. Biomass removal may lead to higher cell densities. Biomass may be removed continuously or step-wise.
  • biomass is removed continuously for a defined time period. If a step-wise approach is used, biomass removal is preferably started just before or just after the cells have reached a steady state. If a step-wise approach is used, a volume of biomass of preferably between 2 and 40 % of the working volume per day, more preferably between 5 and 30% of the working volume per day, even more preferably between 10 and 25% of the working volume per day is removed per biomass removal step.
  • working volume is meant the total volume of the cell culture.
  • biomass removal step is meant the time from the start to the stop of the biomass removal. If a continuous approach is used, the biomass is removed continuously until the end of the cell culturing.
  • the continuous removal of biomass is started just before or just after the cells have reached a steady state.
  • a volume of biomass is removed of between 2 and 40 % of the working volume per day, more preferably between 3 and 30% of the working volume per day, even more preferably between 4 and 15% of the working volume per day.
  • the addition of the additional cell culture medium is done to compensate for the biomass removal.
  • the feed wherein additional cell culture medium is added to the cell culture may be merged into the perfusion feed, but may also be added in a separate feed.
  • the person skilled in the art is aware how much additional cell culture medium is needed to compensate for the biomass removal.
  • the rate of addition of the additional cell culture medium to the cell culture will be the same as the biomass removal rate.
  • a biological substance is produced by the cells.
  • the biological substances that can suitably be produced in the perfusion culturing of the cell are in principle all biological substances that can be produced by animal, especially mammalian, and yeast cells, for example therapeutic and diagnostic proteins, such as monoclonal antibodies, growth factors or peptide hormones, enzymes, polynucleotides, such as viral vectors used in gene therapy, vaccines, etc.
  • the outflow liquid will have a lower cell density but the same concentration of the biological substance than the liquid prior to separation.
  • the process according to the invention is used for the production of a biopharmaceutical product, which is a biological substance with a medical application.
  • biopharmaceutical products are as follows (with examples of brand names of the corresponding biopharmaceutical product between brackets): Tenecteplase (TN KaseTM), (recombinant) antihemophilic factor (ReFactoTM), lymphoblastoid Interferon ⁇ -n1 (WellferonTM), (recombinant) Coagulation factor (NovoSevenTM), Etanercept, (EnbrelTM), Trastuzumab (HerceptinTM), Infliximab (RemicadeTM), Basiliximab (SimulectTM), Daclizumab (ZenapazTM), (recombinant) Coagulation factor IX (BenefixTM), erythropoietin alpha (Epogen®), G-CSF (Neupogen®Filgrastim), Interferon alpha-2b (Infergen®), recombinant insulin (Humulin®), Interferon beta 1a (Avonex®), Factor VIII (K
  • polynucleotides with a possible medical application are gene therapeutic plasmid DNAs. Some gene therapeutic DNAs are presently tested in clinical trials for their medical application.
  • vaccines are live, oral, tetravalent Rotavirus vaccine (RotaShieldTM), rabies vaccine (RanAvertTM), Hepatitis B vaccin (RECOMBIVAX HB®, Engerix®) and inactivated hepatitis A vaccine (VAQTATM).
  • the biological substance in the outflow may be further purified in so-called downstream processing. Downstream processing usually comprises several purification steps in varying combinations and order. Examples of purification steps in the downstream processing are separation steps (e.g.
  • Example 1 Process Optimisation of the Human Cell Line PER.C6® for the production of Biopharmaceuticals
  • a perfusion culture setup was developed for the PER.C6® cell line, a human cell line that possesses a number of features that makes it favourable for the production of biopharmaceuticals.
  • a perfusion setup involves the separation of various components of the culture broth so that cells are retained, harvest is captured and medium refreshment occurs. The performance of a spinfilter, an acoustic device and an Alternating Tangential Flow (ATF) unit within a continuous perfusion culture of the
  • PER.C6® cell line was assessed.
  • a PER.C6® cell line was used in this study that produces a human IgG. Cells were maintained in a serum free commercial medium (EX-CELLTM
  • VPRO medium JRH Biosciences
  • 6 mM L-glutamine Gibco
  • PER.C6® cell line is a human embryonic cell-line immortalised with adenovirus type-5 (ad5) E1 gene using a phosphoglyceratekinase promoter.
  • Bioreactor Set-up 1L and 4L working volume reactors (Applikon, Netherlands and B.Braun, Germany) were used during this study.
  • a Braun DCU3 controller B. Braun, Germany
  • Temperature was maintained at 36.5°C (range 35.5-37.5 ° C).
  • Dissolved oxygen concentration was controlled at 50% (range 40-60%) of air saturation by automatic adjustment of inlet gas composition through the headspace and intermittent sparging through a microporous sparger.
  • the pH setpoint was 7.1 (range 6.7-7.5) and controlled by the flow of CO 2 via the headspace.
  • Cells were inoculated in the fermenter with an inoculum viable cell density range of 0.2-0.5 * 10 6 cells/mL. Perfusion started at a viable cell density in the range of 1-3*10 6 cells/mL.
  • Cell Retention Cells were retained in the reactor using three different devices. First a spinfilter with a 10 ⁇ m pore size (GKD, D ⁇ ren Germany) was used. Secondly, a Biosep ADM 015 cell retention system and controller (AppliSens, the Netherlands) was used. Finally an ATF-4 control unit and housing with associate hollow fiber membrane module (Refine Technology, USA) was assessed. The hollow fiber filter used was model CFP-2-E-8SIP (0.2 micron, Area: 4600cm 2 , Amersham Bioscience obtained from Magellan instruments, USA). To maintain a constant culture volume a level sensor control loop was in operation.
  • a cell count from the bioreactor was performed using the trypan blue exclusion method.
  • the number of viable cells was determined as follows: An amount of cells stained with trypan blue was transferred to a Fuchs Rosenthal haemacytometer. The chamber of the haemacytometer was placed under a microscope and an appropriate number of boxes was counted. The viable cell density was calculated using the following formula:
  • A number of non-stained cells in square
  • B number of non-stained cells in square
  • E dilution factor
  • Antibody concentration was determined by a analytical protein A column using a HPLC with UV280nm absorption detection; the actual concentration was determined on basis of a calibration curve of a lgG1 reference standard.
  • Figure 1 Viable cell density (x10 ⁇ 3 cells/ml) versus culture time (days) for two different continuous perfusion fermentations of an lgG1 producing PER.C6® clone using a spinfilter separation device. Stirrer speed setting of the 1 L Applikon fermenter was 100- 150rpm. The perfusion runs were performed in 1 L working volume. The specific perfusion rate (SPR) for both perfusion runs was 0.1-0.3 nL/cell/day. In both cases the perfusion runs had to be terminated because of spin filter clogging .
  • Figure 2 Growth of lgG1 producing PER.C6® cells in a continuous perfusion system with an acoustic device as a cell retention system.
  • Stirrer speed setting of the 1 L Applikon fermenter was 100-150rpm.
  • the settings used for the run/stop cycle were 300s forward and 4.5s backwards. During the run this was adapted to a 300s/3s cycle (day 15).
  • the specific perfusion rate (SPR) for the perfusion run was between 0.1-0.3 nL/cell/day.
  • Figure 3 Growth of lgG1 producing PER.C6® cells in a continuous perfusion system with an ATF-4 unit as a cell retention system. The experiment was performed in a 4L Applikon fermenter. Setting for the stirrer speed was 125 rpm.
  • the ATF-4 operated between 0.5 and 3 working volumes per day.
  • the SPR was set at 0.03-0.08 nL/cell/day.
  • the inset shows the high cell density of the culture, being completely devoid of aggregating cells.
  • Figure 4 Productivity of lgG1 versus culture time (days) for two different continuous perfusion fermentations of a lgG1 producing PER.C6® clone using a spinfilter separation device.
  • Figure 5 Productivity of lgG1 producing PER.C6TM cells in a continuous perfusion system with an acoustic device as a cell retention system.
  • Figure 6 Productivity of lgG1 producing PER.C6® cells in a continuous perfusion system with an ATF unit as a cell retention system. Summary See Table 1 for an overview of the data obtained for the different types of perfusion.
  • Table 1 Overview of the viable cell density, volumetric production rate (based on reactor volume) and the yield improvement of the perfusion runs using the three different retention devices. Batch and fed-batch results are added for comparison (data not shown).
  • Example 2 Culturing of PER.C6® cells by perfusion.
  • B.Braun fermenter control unit (Braun, Germany), 7L Braun vessel and headplate with associated pH, dissolved oxygen (DO) and level sensor probes (Braun, Germany), ATF-4 control unit and housing with associate hollow fiber membrane module (Refine Technology, USA).
  • PER.C6® cell line expressing a model IgG was investigated in this study.
  • the PER.C6® cell line is generated from retina-derived primary human cells.
  • the PER.C6® cell line is able to generate complete human monoclonal antibodies (including the glycans) (ref 1, ref 2).
  • Cells were cultured in shaking Erlenymer flasks at 110 rpm and 36.5°C. The headspace of these flasks was controlled using a mixture of 5% CO 2 /Air.
  • Ref 1 Jones, D. H., van Berkel, P. H. O, Logtenberg, T. and Bout, A., 2002, 'PER.C6 cell line for human antibody production', Gen. Eng. News 22, 50-54.
  • Ref 2 Jones, D. et al., 2003, 'High-level expression of recombinant IgG in the human cell line PER.C6', Biotechnol. Prog. 19, 163-168.
  • Fermenter Cells were cultured in a fermenter where dissolved oxygen tension, pH, temperature and agitation rate were controlled as detailed below.
  • Cells are inoculated in a fermenter with an inoculation viable cell density range of 0.2 - 0.5 x 10 6 cells/ml and a setpoint of 0.3 x 10 6 cells/ml. Perfusion is begun when the viable cell density > 2 x 10 6 cells /ml or at day 5 of the culture whichever is achieved first. The perfusion rate is dependent on the cell density of the culture and the rates used are described in the table below. Both the flow rate and the dilution rate are adjusted as the cell density in the fermenter increases.
  • Figure 7 Culture time (days) versus flow (L/day) and specific perfusion rate (SPR in nl/cell/day) for PER.C6® cells cultured using a perfusion process.
  • Figure 8 Viable cell density and cell viability using the procedure described in example 2. Table 2. Raw data obtained for example 2

Abstract

The invention relates to a process for the culturing of cells by continuous perfusion culturing of a cell culture comprising cell culture medium and cells, wherein cell culture medium is added to the cell culture, the cell culture is circulated over a filter module comprising hollow fibers resulting in an outflow of liquid having a lower cell density than the cell culture and the flow within the filter module is an alternating tangential flow. Preferably, culture medium is added at a particular perfusion rate and/or biomass is removed form the culture at least once. The method is especially suitable for the culturing of aggregating cells. The invention also relates to such a process wherein a biological substance, preferably an antibody, is produced by the cells, which biological substance may be further purified in downstream processing.

Description

PROCESS FOR CELL CULTURING BY CONTINUOUS PERFUSION AND ALTERNATING TANGENTIAL FLOW
The present invention relates to perfusion culturing of cells. The present invention discloses a process for the culturing of cells by perfusion culturing of a cell culture comprising cell culture medium and cells, wherein cell culture medium is added to the cell culture, wherein the cell culture is circulated over a filter module comprising hollow fibers resulting in an outflow of liquid having a lower cell density than the cell culture and wherein the flow within the filter module is an alternating tangential flow. It has surprisingly been found that by perfusion culturing of animal, in particular mammalian, cells or yeast cells according to the invention, extremely high viable cell densities can be obtained, whereas the cell culture further displays an extremely high cell viability. Furthermore, it was found that the perfusion process of the invention leads to less cell aggregation in the culture, and even to a culture being a suspension of single cells without visible aggregates. This is a surprising finding because the use of low shear conditions, such as in perfusion cell culturing, typically does not lead to disaggregation of cells. Cell aggregation during perfusion cell culturing is disadvantageous, because process control is more difficult, due to, for example, the heterogeneity in metabolic profiles of cells within the cell aggregates. This is especially troublesome if cells form aggregates of 5 cells or more and when the aggregates comprise in total 5 % or more of the total amount of cells. A perfusion process is described in US 6,544,424. Although this document mentions that this process may be used for perfusion culturing of animal cells, it does neither disclose nor suggest the extremely high cell densities found in the present invention. Furthermore, US 6,544,424 B1 discloses that the perfusion process could diminish the attachment and growth of an obstruction on the membrane surface of the hollow fibers, but it does neither disclose nor suggest that cells in the cell culture itself would aggregate less. Voisier et al. (Biotechnol. Bioeng. 82 (2003), 751-765) review various cell retention techniques in high-density perfusion culture of suspended mammalian cells. None of the reviewed cell retention systems is able to provide the extremely high viable cell densities combined with the extremely high cell viability, of the present invention. Perfusion culturing of cells has its conventional meaning in the art, i.e. it means that during culturing cells are retained by a separation device in which there is an outflow of liquid having a lower cell density than prior to separation and in which there is an inflow of the cell culture medium. In the process of the present invention, the separation device is a filter module comprising hollow fibers. Perfusion culturing includes, but is not limited to continuous flow and semi- continuous flow, for example step-wise flow or staggered flow. With the term "hollow fiber" is meant a tubular membrane. The internal diameter of the tube is preferably between 0.3 and 6.0 mm, more preferably between 0.5 and 3.0 mm, most preferably between 0.5 and 2.0 mm. Preferably, the mesh size in the membrane is chosen such that the size of the pores in the mesh is close to the diameter of the cells, ensuring a high retention of cells while cell debris can pass the filter. Preferably, the mesh size is between 3-30 μm. Filter modules comprising hollow fibers are commercially available from for example General Electric (formerly Amersham). With "alternating tangential flow within the filter module" is meant that there is one flow in the same direction as (i.e. tangential to) the membrane surfaces of the hollow fibers, which flow is going back and forth, and that there is another flow in a direction substantially perpendicular to said filter surface. Tangential flow can be achieved according to methods known to the person skilled in the art. For example, in US 6,544,424 it is described that alternating tangential flow can be achieved using one pump to circulate the cell culture over a filter module comprising hollow fibers and another pump to remove the liquid having a lower cell density than prior to the filter separation. In the process of the invention, any type of cell culture medium suitable for the culturing of cells can in principle be used. Guidelines for choosing a cell culture medium and cell culture conditions are well known in the art and are for instance provided in Chapter 8 and 9 of Freshney, R. I. Culture of animal cells (a manual of basic techniques), 4th edition 2000, Wiley-Liss and in Doyle, A., Griffiths, J. B., Newell, D. G. Cell &Tissue culture: Laboratory Procedures 1993, John Wiley & Sons. Generally, a cell culture medium for mammalian cells comprises salts, amino acids, vitamins, lipids, detergents, buffers, growth factors, hormones, cytokines, trace elements and carbohydrates. Examples of salts include magnesium salts, for example MgCI2.6H2O, gSO4 and MgSO4.7H2O iron salts, for example FeSO4.7H2O, potassium salts, for example KH2PO4, KCI; sodium salts, for example NaH2PO4, Na2HPO4 and calcium salts, for example CaCI2.2H2O. Examples of amino acids are all 20 known proteinogenic amino acids, for example hystidine, glutamine, threonine, serine, methionine. Examples of vitamins include: ascorbate, biotin, choline.CI, myo-inositol, D-panthothenate, riboflavin. Examples of lipids include: fatty acids, for example linoleic acid and oleic acid; soy peptone and ethanol amine. Examples of detergents include Tween 80 and Pluronic F68. An example of a buffer is HEPES. Examples of growth factors/hormones/cytokines include IGF, hydrocortisone and (recombinant) insulin. Examples of trace elements are known to the person skilled in the art and include Zn, Mg and Se. Examples of carbohydrates include glucose, fructose, galactose and pyruvate. The pH, temperature, dissolved oxygen concentration and osmolarity of the cell culture medium are in principle not critical and depend on the type of cell chosen. Preferably, the pH, temperature, dissolved oxygen concentration and osmolarity are chosen such that it is optimal for the growth and productivity of the cells. The person skilled in the art knows how to find the optimal pH, temperature, dissolved oxygen concentration and osmolarity for the perfusion culturing. Usually, the optimal pH is between 6.6 and 7.6, the optimal temperature between 30 and 39°C, the optimal osmolarity between 260 and 400mOsm/kg. Cells that are advantageously subjected to the process of the invention may be any cell type benefiting from this process, i.e. culturing to an extremely high viable cell density and an extremely high cell viability. According to the process of the invention, an extremely high viable cell density is a density of at least 80 x 106 cells per mL, preferably at least 100 x 106 cells per mL, more preferably at least 110 x 106 cells per mL, more preferably at least 120 x 106 cells per mL, more preferably at least 130 x 106 cells per mL, most preferably at least 140 x 106 cells per mL. Typically, a suitable upper limit in the cell density may lie around 500 x 106 cells per mL. Surprisingly, the extremely high cell density of the process of the invention is accompanied by an extremly high cell viability. An extremely high cell viability is a viability of at least 90%, preferably at least 95%, more preferably at least 97%, most preferably at least 99%. It is to be understood that the very high viable cell density and very high cell viability are reached after a certain period of perfusion culturing, generally when the cells have reached a steady state, for mammalian cells typically 12 to 25 days after the initiation of perfusion culturing. The process of the invention is suitable for culturing animal cells or yeast cells, especially for culturing mammalian cells. The process of the invention is further especially suitable for culturing cells that easily or inherently form aggregates during culturing, especially during perfusion culturing (so-called aggregating cells). Surprisingly, the process of the invention not only diminishes aggregate disposal on the filter membrane, but also diminishes aggregation of cells during the perfusion culture process, even aggregation of cells with an inherent tendency to form aggregates. The culturing of aggregating cells according to the invention results in a culture wherein aggregates of at least 5 cells comprise at the most 5 % of the total amount of cells, preferably at the most 4 %, more preferably at the most 3 %, even more preferably at the most 2 % of the total amount of cells. Especially preferably, the culturing of aggregating cells according to the invention results in a culture that is a real single cell suspension. Aggregating cells are cells that form aggregates of at least 5 cells, the aggregates comprising in total at least 5 % of the total amount of cells. Preferably, the aggregates consist of at least 6, more preferably at least 7, even more preferably at least 8, even more preferably at least 9, even more preferably at least 10 cells. Preferably, the aggregates comprise in total at least 7%, more preferably at least 10 %, most preferably at least 15% of the total amount of cells. Examples of mammalian cells include: CHO (Chinese Hamster Ovary) cells, hybridomas, BHK (Baby Hamster Kidney) cells, myeloma cells, human cells, for example HEK-293 cells, human lymphoblastoid cells, PER.C6® cells, mouse cells, for example NS0 cells. Examples of yeast cells include Saccharomyces cerevisiae, Phaffia rhodozyma, Kluyveromyces lactis, or yeast cells from the genus Pichia . Preferably, mammalian cells are used, more preferably CHO, NS0, PER.C6® cells. Also preferably, cells known for their aggregating behaviour during culturing (aggregating cells) are used. Most preferably, PER.C6® cells are used. Cell aggregation may for example be determined under a microscope. The rate of addition of cell culture medium to the culture (the inflow rate or perfusion rate) influences the viability and the density of the cells. In one embodiment of the invention, the cell culture medium is added at a perfusion rate according to the following formula 1 : Perfusion rate = SPR*total cell culture volume*viable cell density (1 )
wherein the perfusion rate is expressed in liters per day, wherein the SPR is the specific perfusion rate, i.e. the rate in which the cell culture medium is fed to the cell culture expressed as the volume of medium added per viable cell per time unit and wherein the viable cell density is the number of viable cells per unit of volume. The number of viable cells can be determined by the person skilled in the art, for example via the trypan blue exclusion method. The specific perfusion rate is preferably chosen between 0.01 and 0.3 nL/cell/day, more preferably between 0.01 and 0.2 nL/cell/day. It may be of advantage to take into account additional parameters when adjusting the perfusion rate, for example the amount of glucose to be fed to the culture and/or the oxygen concentration. For example, for PER.C6® the glucose perfusion rate is preferably chosen between 3 and 20 mmoles/L, more preferably between 5 and 15 mmoles/L, as part of the medium perfusion rate. A person skilled in the art knows how to determine the outflow rate. The outflow rate of the liquid is determined by the perfusion rate and is generally chosen at an equal value. In one embodiment of the invention, the outflow liquid is substantially devoid of viable cells. In another embodiment of the invention, biomass (i.e. cells in cell culture) is removed at least once from the cell culture and additional cell culture medium is added to the cell culture to compensate for the biomass removal. Biomass removal may lead to higher cell densities. Biomass may be removed continuously or step-wise. In the step-wise approach, biomass is removed continuously for a defined time period. If a step-wise approach is used, biomass removal is preferably started just before or just after the cells have reached a steady state. If a step-wise approach is used, a volume of biomass of preferably between 2 and 40 % of the working volume per day, more preferably between 5 and 30% of the working volume per day, even more preferably between 10 and 25% of the working volume per day is removed per biomass removal step. With "working volume" is meant the total volume of the cell culture. With "biomass removal step" is meant the time from the start to the stop of the biomass removal. If a continuous approach is used, the biomass is removed continuously until the end of the cell culturing. Preferably, the continuous removal of biomass is started just before or just after the cells have reached a steady state. Preferably, a volume of biomass is removed of between 2 and 40 % of the working volume per day, more preferably between 3 and 30% of the working volume per day, even more preferably between 4 and 15% of the working volume per day. The addition of the additional cell culture medium is done to compensate for the biomass removal. The feed wherein additional cell culture medium is added to the cell culture may be merged into the perfusion feed, but may also be added in a separate feed. The person skilled in the art is aware how much additional cell culture medium is needed to compensate for the biomass removal. Generally, the rate of addition of the additional cell culture medium to the cell culture will be the same as the biomass removal rate. In yet another embodiment of the invention, a biological substance is produced by the cells. The biological substances that can suitably be produced in the perfusion culturing of the cell are in principle all biological substances that can be produced by animal, especially mammalian, and yeast cells, for example therapeutic and diagnostic proteins, such as monoclonal antibodies, growth factors or peptide hormones, enzymes, polynucleotides, such as viral vectors used in gene therapy, vaccines, etc. In the perfusion culturing process of the invention, the outflow liquid will have a lower cell density but the same concentration of the biological substance than the liquid prior to separation. Preferably, the process according to the invention is used for the production of a biopharmaceutical product, which is a biological substance with a medical application. Examples of biopharmaceutical products are as follows (with examples of brand names of the corresponding biopharmaceutical product between brackets): Tenecteplase (TN Kase™), (recombinant) antihemophilic factor (ReFacto™), lymphoblastoid Interferon α-n1 (Wellferon™), (recombinant) Coagulation factor (NovoSeven™), Etanercept, (Enbrel™), Trastuzumab (Herceptin™), Infliximab (Remicade™), Basiliximab (Simulect™), Daclizumab (Zenapaz™), (recombinant) Coagulation factor IX (Benefix™), erythropoietin alpha (Epogen®), G-CSF (Neupogen®Filgrastim), Interferon alpha-2b (Infergen®), recombinant insulin (Humulin®), Interferon beta 1a (Avonex®), Factor VIII (KoGENate®), Glucocerebrosidase (Cerezyme™), Interferon beta 1 b (Betaseron®), TNF alpha receptor (Enbrel®), Follicle stimulating hormone (Gonal-F®), Mab abcixmab (Synagis®, ReoPro®), Mab ritiximab (Rituxan®), tissue plasminogen activator (Activase ®, Actilyase®), human growth hormone (Protropin®, Norditropin®, GenoTropin™). Examples of polynucleotides with a possible medical application are gene therapeutic plasmid DNAs. Some gene therapeutic DNAs are presently tested in clinical trials for their medical application. Examples of vaccines are live, oral, tetravalent Rotavirus vaccine (RotaShield™), rabies vaccine (RanAvert™), Hepatitis B vaccin (RECOMBIVAX HB®, Engerix®) and inactivated hepatitis A vaccine (VAQTA™). The biological substance in the outflow may be further purified in so-called downstream processing. Downstream processing usually comprises several purification steps in varying combinations and order. Examples of purification steps in the downstream processing are separation steps (e.g. by affinity chromatography and/or ion exchange chromatography), steps for the concentration of the biological substance (e.g. by ultrafiltration or diafiltration), steps to exchange buffers and/or steps to remove or inactivate viruses (e.g. by virusfiltration, pH shift or solvent detergent treatment). The invention will now be elucidated by way of the following examples, without however being limited thereto.
Example 1: Process Optimisation of the Human Cell Line PER.C6® for the production of Biopharmaceuticals
Introduction
A number of expression platforms now exist for the production of biopharmaceuticals. Most of the new products must choose a mammalian system due in main part to the glycosylation machinery which these cells contain and others lack. However to date the cell mass and resulting productivity of these cells is a factor of 10 -100 times less than a corresponding microbial system if these cells had the machinery to make such products. A perfusion culture setup was developed for the PER.C6® cell line, a human cell line that possesses a number of features that makes it favourable for the production of biopharmaceuticals. A perfusion setup involves the separation of various components of the culture broth so that cells are retained, harvest is captured and medium refreshment occurs. The performance of a spinfilter, an acoustic device and an Alternating Tangential Flow (ATF) unit within a continuous perfusion culture of the
PER.C6® cell line was assessed.
Materials & Methods
Cell line and maintenance : A PER.C6® cell line was used in this study that produces a human IgG. Cells were maintained in a serum free commercial medium (EX-CELL™
VPRO medium, JRH Biosciences), supplemented with 6 mM L-glutamine (Gibco). The
PER.C6® cell line is a human embryonic cell-line immortalised with adenovirus type-5 (ad5) E1 gene using a phosphoglyceratekinase promoter.
Bioreactor Set-up: 1L and 4L working volume reactors (Applikon, Netherlands and B.Braun, Germany) were used during this study. A Braun DCU3 controller (B. Braun, Germany) was used to operate the process at defined setpoints. Temperature was maintained at 36.5°C (range 35.5-37.5 °C). Dissolved oxygen concentration was controlled at 50% (range 40-60%) of air saturation by automatic adjustment of inlet gas composition through the headspace and intermittent sparging through a microporous sparger. The pH setpoint was 7.1 (range 6.7-7.5) and controlled by the flow of CO2 via the headspace. Cells were inoculated in the fermenter with an inoculum viable cell density range of 0.2-0.5 *106 cells/mL. Perfusion started at a viable cell density in the range of 1-3*106 cells/mL.
Cell Retention: Cells were retained in the reactor using three different devices. First a spinfilter with a 10μm pore size (GKD, Dϋren Germany) was used. Secondly, a Biosep ADM 015 cell retention system and controller (AppliSens, the Netherlands) was used. Finally an ATF-4 control unit and housing with associate hollow fiber membrane module (Refine Technology, USA) was assessed. The hollow fiber filter used was model CFP-2-E-8SIP (0.2 micron, Area: 4600cm2, Amersham Bioscience obtained from Magellan instruments, USA). To maintain a constant culture volume a level sensor control loop was in operation.
Analytical methods: A cell count from the bioreactor was performed using the trypan blue exclusion method. The number of viable cells was determined as follows: An amount of cells stained with trypan blue was transferred to a Fuchs Rosenthal haemacytometer. The chamber of the haemacytometer was placed under a microscope and an appropriate number of boxes was counted. The viable cell density was calculated using the following formula:
Viable cell density (X105 cells/ml) = (A+B) x E/320 (2)
Wherein A = number of non-stained cells in square A B = number of non-stained cells in square B E = dilution factor
Antibody concentration was determined by a analytical protein A column using a HPLC with UV280nm absorption detection; the actual concentration was determined on basis of a calibration curve of a lgG1 reference standard. Results
Perfusion Cultures Results obtained with the above materials and methods are shown in Figures 1-6.
Legends to the Figures:
Figure 1 : Viable cell density (x10<3 cells/ml) versus culture time (days) for two different continuous perfusion fermentations of an lgG1 producing PER.C6® clone using a spinfilter separation device. Stirrer speed setting of the 1 L Applikon fermenter was 100- 150rpm. The perfusion runs were performed in 1 L working volume. The specific perfusion rate (SPR) for both perfusion runs was 0.1-0.3 nL/cell/day. In both cases the perfusion runs had to be terminated because of spin filter clogging . Figure 2: Growth of lgG1 producing PER.C6® cells in a continuous perfusion system with an acoustic device as a cell retention system. Stirrer speed setting of the 1 L Applikon fermenter was 100-150rpm. The settings used for the run/stop cycle were 300s forward and 4.5s backwards. During the run this was adapted to a 300s/3s cycle (day 15). The specific perfusion rate (SPR) for the perfusion run was between 0.1-0.3 nL/cell/day. Figure 3: Growth of lgG1 producing PER.C6® cells in a continuous perfusion system with an ATF-4 unit as a cell retention system. The experiment was performed in a 4L Applikon fermenter. Setting for the stirrer speed was 125 rpm. The ATF-4 operated between 0.5 and 3 working volumes per day. The SPR was set at 0.03-0.08 nL/cell/day. The inset shows the high cell density of the culture, being completely devoid of aggregating cells.
Figure 4: Productivity of lgG1 versus culture time (days) for two different continuous perfusion fermentations of a lgG1 producing PER.C6® clone using a spinfilter separation device. Figure 5: Productivity of lgG1 producing PER.C6TM cells in a continuous perfusion system with an acoustic device as a cell retention system.
Figure 6: Productivity of lgG1 producing PER.C6® cells in a continuous perfusion system with an ATF unit as a cell retention system. Summary See Table 1 for an overview of the data obtained for the different types of perfusion.
Table 1. Overview of the viable cell density, volumetric production rate (based on reactor volume) and the yield improvement of the perfusion runs using the three different retention devices. Batch and fed-batch results are added for comparison (data not shown).
Figure imgf000011_0001
It can be concluded that continuous perfusion experiments using the ATF unit show significant potential to achieve very high cell densities and product concentrations (100x106 cells/mL and 0.9 g/L/day), while no aggregation of the PER.C6® cells was observed.
Example 2: Culturing of PER.C6® cells by perfusion.
Equipment: B.Braun fermenter control unit (Braun, Germany), 7L Braun vessel and headplate with associated pH, dissolved oxygen (DO) and level sensor probes (Braun, Germany), ATF-4 control unit and housing with associate hollow fiber membrane module (Refine Technology, USA).
Filter Filter model: CFP-2-E-8SIP Type: 0.2 micron Area: 4600 cm2 Amersham Bioscience Working volume Setpoint: 4.1 L Range: 3.8 - 4.7 L ATF settings
Figure imgf000012_0001
Bleed rate No biomass removal was applied to this process.
Materials: 6 mM (final volume) L-glutamine (Gibco) in Ex-CELL™ VPRO medium (JRH Bioscience, USA), 12% Na2CO3 is used to control the pH.
Cell Lines and Culture Conditions A PER.C6® cell line expressing a model IgG was investigated in this study. The PER.C6® cell line is generated from retina-derived primary human cells. The PER.C6® cell line is able to generate complete human monoclonal antibodies (including the glycans) (ref 1, ref 2). Cells were cultured in shaking Erlenymer flasks at 110 rpm and 36.5°C. The headspace of these flasks was controlled using a mixture of 5% CO2/Air.
Ref 1 : Jones, D. H., van Berkel, P. H. O, Logtenberg, T. and Bout, A., 2002, 'PER.C6 cell line for human antibody production', Gen. Eng. News 22, 50-54. Ref 2: Jones, D. et al., 2003, 'High-level expression of recombinant IgG in the human cell line PER.C6', Biotechnol. Prog. 19, 163-168.
Operation of Fermenter Cells were cultured in a fermenter where dissolved oxygen tension, pH, temperature and agitation rate were controlled as detailed below.
Figure imgf000013_0001
Process Description: Cells are inoculated in a fermenter with an inoculation viable cell density range of 0.2 - 0.5 x 106 cells/ml and a setpoint of 0.3 x 106 cells/ml. Perfusion is begun when the viable cell density > 2 x 106 cells /ml or at day 5 of the culture whichever is achieved first. The perfusion rate is dependent on the cell density of the culture and the rates used are described in the table below. Both the flow rate and the dilution rate are adjusted as the cell density in the fermenter increases.
Perfusion rates utilized for culture of PER.C6® cells
Figure imgf000013_0002
The actual data and results from this example (amongst others flow rates and specific perfusion rates used in this example) are shown in Table 2 below and in Figures 7 and 8.
Figure 7: Culture time (days) versus flow (L/day) and specific perfusion rate (SPR in nl/cell/day) for PER.C6® cells cultured using a perfusion process. Figure 8: Viable cell density and cell viability using the procedure described in example 2. Table 2. Raw data obtained for example 2
Figure imgf000014_0001

Claims

1. Process for the culturing of cells by continuous perfusion culturing of a cell culture comprising cell culture medium and cells, wherein: cell culture medium is added to the cell culture, the cell culture is circulated over a filter module comprising hollow fibers resulting in an outflow of liquid having a lower cell density than the cell culture, and the flow within the filter module is an alternating tangential flow.
2. Process according to claim 1 , wherein the cell culture medium is added at a perfusion rate calculated according to Formula 1 :
Perfusion rate = SPR*total cell culture volume*viable cell density (1 ) wherein the perfusion rate is expressed in liters per day, wherein the SPR is the specific perfusion rate, i.e. the rate in which the cell culture medium is fed to the cell culture expressed as the volume of medium added per viable cell per time unit and wherein the viable cell density is the number of viable cells per unit of volume.
3. Process according to claim 2, wherein the SPR is between 0.01 and 0.3 nL/cell/day.
4. Process according to any one of the preceding claims, wherein biomass is removed at least once from the cell culture and additional cell culture medium is added to the cell culture.
5. Process according to claim 4, wherein the biomass removal is started just before or just after the cells have reached a steady state
6. Process according to claim 4 or 5, wherein a volume of biomass is removed of between 2 and 40% of the total volume of the cell culture per day.
7. Process according to any one of the preceding claims, wherein the alternating tangential flow is achieved using one pump to circulate the cell culture over a filter module comprising hollow fibers and using another pump to remove the liquid having a lower cell density than the cell culture prior to the filter separation.
8. Process according to any one of the preceding claims, wherein the cells are > cultured to a viable cell density of at least 80 x 106 cells per ml and a cell viability of at least 90%.
9. Process according to any one of the preceding claims, wherein the aggregates of at least 5 cells comprise at the most 5 % of the total amount of cells.
10. Process according to any one of the preceding claims, wherein the cells are animal cells, preferably mammalian cells, or yeast cells.
11. Process according to claim 10, wherein the cells are mammalian cells.
12. Process according to claim 11 , wherein the mammalian cells are PER.C6® cells.
13. Process according to any one of the preceding claims, wherein the cells produce a biological substance.
14. Process according to claim 13, wherein the biological substance is a therapeutic or diagnostic protein, such as a monoclonal antibody, a growth factor or a peptide hormone, an enzyme, a polynucleotide, such as a viral vector used in gene therapy, or a vaccine, preferably a monoclonal antibody.
15. Process according to claim 13 or 14, wherein the biological substance is further purified in downstream processing.
PCT/EP2005/002374 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow WO2005095578A1 (en)

Priority Applications (15)

Application Number Priority Date Filing Date Title
AU2005229359A AU2005229359C1 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
PL05715787T PL1720972T3 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
SI200531842T SI1720972T1 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
EP05715787.7A EP1720972B1 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
US10/591,118 US8206981B2 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
DK05715787.7T DK1720972T3 (en) 2004-03-05 2005-03-04 METHOD OF CELL CULTIVATION USING CONTINUOUS PERFUSION AND ALTERNATIVE TANGENTIAL FLOW
JP2007501239A JP2007525984A (en) 2004-03-05 2005-03-04 Cell culture method by continuous perfusion and alternating tangential flow
KR1020067018075A KR101050585B1 (en) 2004-03-05 2005-03-04 Cell culture method by continuous spreading and alternating tangential flow
ES05715787.7T ES2456015T3 (en) 2004-03-05 2005-03-04 Procedure for culturing cells by continuous perfusion and alternating tangential flow
CNA2005800071754A CN1930281A (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
CA002557046A CA2557046A1 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
IL177724A IL177724A (en) 2004-03-05 2006-08-28 Methods for reducing the degree of aggregation of aggregating cells in a cell culture
IL205606A IL205606A (en) 2004-03-05 2010-05-06 Perfusion cultures comprising a cell culture medium and aggregating animal cells
US13/478,307 US20130266985A1 (en) 2004-03-05 2012-05-23 Process for Cell Culturing by Continuous Perfusion
US14/052,878 US9260695B2 (en) 2004-03-05 2013-10-14 Process for cell culturing by continuous perfusion

Applications Claiming Priority (8)

Application Number Priority Date Filing Date Title
EP04075703.1 2004-03-05
EP04075702 2004-03-05
EP04075702.3 2004-03-05
EP04075703 2004-03-05
EP04077657 2004-09-27
EP04077656.9 2004-09-27
EP04077656 2004-09-27
EP04077657.7 2004-09-27

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US10/591,118 A-371-Of-International US8206981B2 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow
US13/478,307 Continuation US20130266985A1 (en) 2004-03-05 2012-05-23 Process for Cell Culturing by Continuous Perfusion

Publications (1)

Publication Number Publication Date
WO2005095578A1 true WO2005095578A1 (en) 2005-10-13

Family

ID=34961830

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2005/002374 WO2005095578A1 (en) 2004-03-05 2005-03-04 Process for cell culturing by continuous perfusion and alternating tangential flow

Country Status (14)

Country Link
US (3) US8206981B2 (en)
EP (3) EP2540815A1 (en)
JP (6) JP2007525984A (en)
KR (1) KR101050585B1 (en)
CN (3) CN104593277A (en)
AU (1) AU2005229359C1 (en)
CA (1) CA2557046A1 (en)
DK (1) DK1720972T3 (en)
ES (1) ES2456015T3 (en)
IL (2) IL177724A (en)
PL (1) PL1720972T3 (en)
PT (1) PT1720972E (en)
SI (1) SI1720972T1 (en)
WO (1) WO2005095578A1 (en)

Cited By (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1870450A1 (en) * 2006-06-21 2007-12-26 DSMIP Assets B.V. Process for the culturing of E1-immortalized HER cells
WO2008006494A1 (en) * 2006-07-14 2008-01-17 Dsm Ip Assets B.V. Improved process for the culturing of cells
WO2010003759A2 (en) * 2008-06-17 2010-01-14 Dsm Ip Assets B.V. Cell culturing method
WO2011006823A1 (en) 2009-07-16 2011-01-20 Crucell Holland B.V. Production of polio virus at high titers for vaccine production
WO2011045381A1 (en) 2009-10-15 2011-04-21 Crucell Holland B.V. Process for adenovirus purification from high cell density cultures
WO2011045378A1 (en) 2009-10-15 2011-04-21 Crucell Holland B.V. Method for the purification of adenovirus particles
US20110207202A1 (en) * 2008-11-03 2011-08-25 Crucell Holland Bv Method for the production of adenoviral vectors
WO2011144561A1 (en) 2010-05-18 2011-11-24 Crucell Holland B.V. Methods for welding ethylene vinyl acetate (eva) tubing, tubing obtained thereby and use of such tubing for sterile transfer of content into a bioreactor
WO2012045769A1 (en) * 2010-10-05 2012-04-12 Novo Nordisk Health Care Ag Process for protein production
US8206981B2 (en) 2004-03-05 2012-06-26 Dsm Ip Assets B.V. Process for cell culturing by continuous perfusion and alternating tangential flow
CN102762721A (en) * 2010-02-15 2012-10-31 克鲁塞尔荷兰公司 Method for the production of Ad26 adenoviral vectors
US20120315696A1 (en) * 2010-02-15 2012-12-13 Alfred Luitjens METHOD FOR THE PRODUCTION OF Ad26 ADENOVIRAL VECTORS
AU2011211462B2 (en) * 2006-07-14 2013-04-18 Dpx Holdings B.V. Improved process for the culturing of cells
US8679778B2 (en) 2007-06-13 2014-03-25 Cmc Biologics A/S Method for producing a biopolymer (e.g. polypeptide) in a continuous fermentation process
WO2014073967A1 (en) 2012-11-09 2014-05-15 Biosana Pty Ltd. Discontinuous fed batch processing with the use of alternating bioreactors
JP2014100148A (en) * 2007-12-27 2014-06-05 Baxter Internatl Inc Cell culture processes
WO2014160790A1 (en) * 2013-03-26 2014-10-02 Coherus Biosciences, Inc. Protein production method
WO2015095809A1 (en) * 2013-12-20 2015-06-25 Biogen Idec Ma Inc. Use of perfusion seed cultures to improve biopharmaceutical fed-batch production capacity and product quality
US9587253B2 (en) 2006-02-24 2017-03-07 Toray Industries, Inc. Method of producing chemical product with continuous fermentation and filtering
EP2501822B1 (en) 2009-11-17 2017-08-16 E. R. Squibb & Sons, L.L.C. Methods for enhanced protein production
RU2668796C2 (en) * 2013-03-15 2018-10-02 Джензим Корпорейшн Methods for creation of high density cell bank (variants)
US10092888B2 (en) 2014-11-07 2018-10-09 Genesis Technologies, Llc Linear reciprocating actuator
KR20180133487A (en) * 2016-04-14 2018-12-14 트리젤 엘티디. Fixed-bed bioreactor with constant flow pump / tubing system
EP3152317B1 (en) 2014-06-04 2019-01-02 Amgen Inc. Methods for harvesting mammalian cell cultures
US10213508B2 (en) 2011-10-18 2019-02-26 Coherus Biosciences, Inc. Etanercept formulations stabilized with xylitol
WO2019055796A1 (en) * 2017-09-15 2019-03-21 Bristol-Myers Squibb Company Online biomass capacitance monitoring during large scale production of polypeptides of interest
US10294460B2 (en) 2014-07-24 2019-05-21 Janssen Vaccines & Prevention B.V. Process for the purification of poliovirus from cell cultures
US10421986B2 (en) 2013-09-30 2019-09-24 Janssen Vaccines & Prevention B.V. Method for the clarification of high-density crude cell culture harvest
US10493151B2 (en) 2011-10-18 2019-12-03 Coherus Biosciences, Inc. Etanercept formulations stabilized with sodium chloride
WO2020165873A1 (en) * 2019-02-15 2020-08-20 Oncosimis Biotech Private Limited Method and system for enhanced continuous production, secretion and separation of recombinant polypeptides from bacteria
EP2976418B1 (en) 2013-03-19 2020-09-30 CMC Biologics A/S A method for producing a product (e.g. polypeptide) in a continuous cell culture fermentation process.
US10822429B2 (en) 2012-07-09 2020-11-03 Coherus Biosciences, Inc. Etanercept formulations exhibiting marked reduction in sub-visible particles
US10947306B2 (en) 2012-09-11 2021-03-16 Coherus Biosciences, Inc. Correctly folded etanercept in high purity and excellent yield
US11193103B2 (en) 2017-10-16 2021-12-07 Regeneran Pharmaceuticals, Inc. Perfusion bioreactor and related methods of use
WO2022027013A1 (en) 2020-07-28 2022-02-03 Seagen Inc. Methods and systems for producing polypeptides
US11242504B2 (en) 2016-04-14 2022-02-08 Trizell Ltd. Aseptic bioreactor sampling system
US11492578B2 (en) 2016-06-30 2022-11-08 Fujifilm Corporation Membrane separation method of cell suspension, and cell culture device
EP3626737B1 (en) * 2011-05-13 2023-11-29 Octapharma AG A method of increasing the productivity of eucaryotic cells in the production of recombinant fviii

Families Citing this family (33)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102282249A (en) 2008-09-02 2011-12-14 普拉里斯坦有限公司 Adherent cells from placenta tissue and use thereof in therapy
CN107988166B (en) * 2011-07-01 2022-03-15 美国安进公司 Mammalian cell culture
CN103305417A (en) * 2012-03-07 2013-09-18 无锡药明康德生物技术有限公司 High-yield reactor for protein production, and production method and application thereof
GB201211256D0 (en) 2012-06-25 2012-08-08 Glaxosmithkline Biolog Sa Fermentation process
EP2900804B1 (en) 2012-09-27 2019-09-18 GE Healthcare Bio-Sciences AB Tangential flow perfusion system
US9790465B2 (en) 2013-04-30 2017-10-17 Corning Incorporated Spheroid cell culture well article and methods thereof
AU2014318420B2 (en) * 2013-09-16 2020-01-16 Genzyme Corporation Methods and systems for processing a cell culture
CN103525756B (en) * 2013-10-23 2015-04-08 南京农业大学 Method for separating and culturing primary chicken hepatocytes
SG10201912081RA (en) * 2014-01-29 2020-02-27 Amgen Inc Overexpression of n-glycosylation pathway regulators to modulate glycosylation of recombinant proteins
CN106414490A (en) * 2014-02-17 2017-02-15 爱德技术生物科学有限公司 Enhancement of recombinant protein expression using a membrane-based cell retention system
JP6530171B2 (en) * 2014-09-09 2019-06-12 旭化成メディカル株式会社 Method of collecting culture product
JP6930914B2 (en) 2014-10-29 2021-09-01 コーニング インコーポレイテッド Perfusion bioreactor platform
SG11201703493SA (en) 2014-10-29 2017-05-30 Corning Inc Cell culture insert
CN107532132A (en) * 2015-02-09 2018-01-02 优尼沃赛尔斯公司 For producing the systems, devices and methods of cell and/or cell products
AU2017249402A1 (en) 2016-04-12 2018-10-04 Artemis Biosystems, Inc. Perfusion filtration systems
EP3443064A1 (en) * 2016-04-15 2019-02-20 Boehringer Ingelheim International GmbH Cell retention device and method
US20200080050A1 (en) * 2016-07-11 2020-03-12 Yaakov Nahmias Systems and methods for growing cells in vitro
JP7245222B2 (en) 2017-07-14 2023-03-23 コーニング インコーポレイテッド 3D cell culture vessel for manual or automatic medium exchange
US11857970B2 (en) 2017-07-14 2024-01-02 Corning Incorporated Cell culture vessel
WO2019014610A1 (en) 2017-07-14 2019-01-17 Corning Incorporated Cell culture vessel for 3d culture and methods of culturing 3d cells
CN111065729B (en) 2017-07-14 2024-04-26 康宁股份有限公司 Cell culture vessel
CN111051496B (en) 2017-09-06 2024-03-08 富士胶片株式会社 Method for producing product
CN111344558A (en) 2017-10-06 2020-06-26 龙沙有限公司 Automated control of cell culture using raman spectroscopy
BR112020011627A2 (en) * 2017-12-11 2020-11-17 Amgen Inc. continuous manufacturing process for bispecific antibody products
AU2019231885B2 (en) 2018-03-08 2022-03-24 Repligen Corporation Tangential flow depth filtration systems and methods of filtration using same
CN110241012B (en) * 2018-03-09 2022-11-01 嘉和生物药业有限公司 Production method and production module for upstream staged interception of biomacromolecules and application of production module in production
CN111868249A (en) * 2018-03-19 2020-10-30 富士胶片株式会社 Method for producing product
AU2019273030B2 (en) 2018-05-25 2022-08-18 Repligen Corporation Tangential flow filtration systems and methods
CN108504562A (en) * 2018-06-21 2018-09-07 江苏澳创生物科技有限公司 A kind of system of production of L-threonine by fermentation and its application
WO2020013845A1 (en) 2018-07-13 2020-01-16 Corning Incorporated Cell culture vessels with stabilizer devices
CN111065725B (en) 2018-07-13 2024-03-29 康宁股份有限公司 Fluidic device comprising microplates with interconnected walls
JP7171695B2 (en) 2018-07-13 2022-11-15 コーニング インコーポレイテッド A microcavity dish having sidewalls containing a liquid medium delivery surface
CN114127260A (en) * 2019-07-16 2022-03-01 信达生物制药(苏州)有限公司 Cell culture method for high-density continuous inoculation and application thereof

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993005145A1 (en) 1991-08-30 1993-03-18 Celltech Limited Cell culture process and medium for the growth of adherent animal cells
US20030054544A1 (en) * 2001-09-14 2003-03-20 Medcell Biologics, Inc. Oxygen enriched bioreactor and method of culturing cells
US6544424B1 (en) 1999-12-03 2003-04-08 Refined Technology Company Fluid filtration system

Family Cites Families (44)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US54544A (en) * 1866-05-08 Improvement in low-water detecters
JPS61199788A (en) 1985-02-28 1986-09-04 Mitsubishi Rayon Co Ltd Separation and concentration of fermentation product, and method for continuous fermentation
US5286646A (en) 1985-11-25 1994-02-15 Boehringer Mannheim Gmbh Method for mammalian cell culture
GB8617646D0 (en) 1986-07-18 1986-08-28 Manchester Inst Science Tech Recovery of biological material
US4806484A (en) 1987-08-07 1989-02-21 Igb Products, Ltd. Perfusion airlift bioreactor
JPH0797982B2 (en) 1987-09-24 1995-10-25 東洋紡績株式会社 Cell culture device
US4921792A (en) * 1987-11-27 1990-05-01 Miles Inc. Continuous cell dispersion, cultivation and substance recovery process
JPH01243985A (en) 1988-03-25 1989-09-28 P C C Technol:Kk Method for culturing plant organ and culture vessel therefor
US5595909A (en) * 1988-05-23 1997-01-21 Regents Of The University Of Minnesota Filter device
DE68917642T2 (en) 1988-05-25 1995-02-09 Teijin Ltd Process for the continuous cultivation of adherent animal cells.
JPH02113896A (en) * 1988-10-24 1990-04-26 Snow Brand Milk Prod Co Ltd Human anti-ricin monoclonal antibody and hybridoma secreting same antibody
US5019512A (en) * 1989-03-17 1991-05-28 Baxter International Inc. Spin filter for removing substantially cell-free culture medium from suspension cell culture system
JPH0541984A (en) * 1990-09-07 1993-02-23 Dow Chem Co:The Cell multiplication in hollow fiber in stirring container
US5256294A (en) 1990-09-17 1993-10-26 Genentech, Inc. Tangential flow filtration process and apparatus
JPH05153973A (en) 1991-12-03 1993-06-22 Hitachi Ltd Cell culture method and apparatus therefor
US6204000B1 (en) 1995-04-28 2001-03-20 The United States Of America As Represented By The Department Of Health And Human Services Diagnostic methods and gene therapy using reagents derived from the human metastasis suppressor gene KAI1
JP2752918B2 (en) * 1995-05-16 1998-05-18 ユーエイチティー株式会社 Microcarrier culture method for animal cells
US6001585A (en) 1997-11-14 1999-12-14 Cellex Biosciences, Inc. Micro hollow fiber bioreactor
JP2997771B2 (en) * 1998-06-29 2000-01-11 金沢大学長 Cell suspension culture method
US8026096B1 (en) * 1998-10-08 2011-09-27 Protein Sciences Corporation In vivo active erythropoietin produced in insect cells
US6103526A (en) 1998-10-08 2000-08-15 Protein Sciences Corporation Spodoptera frugiperda single cell suspension cell line in serum-free media, methods of producing and using
US6667176B1 (en) 2000-01-11 2003-12-23 Geron Corporation cDNA libraries reflecting gene expression during growth and differentiation of human pluripotent stem cells
CA2252972C (en) 1998-11-26 2012-09-18 National Research Council Of Canada Serum-free production of recombinant proteins and adenoviral vectors
ES2319254T3 (en) 1999-01-26 2009-05-06 Schering-Plough Ltd. PROPAGATION OF BOVINE CORONAVIRUS IN OVARY CELLS OF CHINESE HAMSTER
US6855544B1 (en) * 1999-04-15 2005-02-15 Crucell Holland B.V. Recombinant protein production in a human cell
ATE447617T1 (en) 1999-04-15 2009-11-15 Crucell Holland Bv USE OF RECOMBINANT PROTEINS IN HUMAN CELLS
JP2001149099A (en) 1999-11-26 2001-06-05 Olympus Optical Co Ltd Preparation of specimen of nucleus-containing cell for analysis of chromosome abnormality
EP1103610A1 (en) 1999-11-26 2001-05-30 Introgene B.V. Production of vaccines from immortalised mammalian cell lines
US6168941B1 (en) * 2000-04-07 2001-01-02 Genvec, Inc. Method of producing adenoviral vector stocks
JP4138209B2 (en) 2000-06-29 2008-08-27 エーザイ・アール・アンド・ディー・マネジメント株式会社 Pravastatin-containing composition
JP2002113896A (en) 2000-10-05 2002-04-16 Seiko Epson Corp Imaging apparatus
WO2002086133A1 (en) * 2001-04-17 2002-10-31 Seiren Kabushiki Kaisha Medium additives and media for culturing animal cells
DE10120835C2 (en) 2001-04-27 2003-04-10 Sifin Inst Fuer Immunpraeparat Process for the production of monoclonal antibodies
CA2351156A1 (en) 2001-07-04 2003-01-04 Peter W. Zandstra A bioprocess for the generation of pluripotent cell derived cells and tissues
AU2002333739B2 (en) * 2001-08-31 2007-08-02 Bayer Intellectual Property Gmbh A unit and a process for carrying out high cell density fermentation
JP3968347B2 (en) 2001-09-05 2007-08-29 ヤマサ醤油株式会社 Pharmaceutical composition for diabetic neuropathy
JP2003219873A (en) 2002-01-24 2003-08-05 Japan Science & Technology Corp Immortalized cell derived from chinook salmon of salmonidae
US20030186335A1 (en) 2002-03-28 2003-10-02 National Institute Of Advanced Industrial Science And Technology Monoclonal antibodies, hybridomas, cell isolation method, isolated cells and immunological diagnostic method
DE10237082B4 (en) * 2002-08-09 2014-12-31 Sartorius Stedim Biotech Gmbh Method and device for the biotechnological production of recyclables
CN101328473B (en) 2003-05-09 2012-05-02 克鲁塞尔荷兰公司 Cultures of E1-immortalized cells and processes for culturing the same to increase product yields therefrom
JP2005041984A (en) 2003-07-22 2005-02-17 Shin Kobe Electric Mach Co Ltd Method of manufacturing water-crosslinking polyolefin sheet
EP2540815A1 (en) 2004-03-05 2013-01-02 DSM IP Assets B.V. Perfusion cell culture
PL2343362T3 (en) * 2006-07-14 2016-11-30 Improved process for the culturing of cells
JP2008308560A (en) 2007-06-13 2008-12-25 Tohcello Co Ltd Method for producing surface stain resistant composite film

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993005145A1 (en) 1991-08-30 1993-03-18 Celltech Limited Cell culture process and medium for the growth of adherent animal cells
US6544424B1 (en) 1999-12-03 2003-04-08 Refined Technology Company Fluid filtration system
US20030054544A1 (en) * 2001-09-14 2003-03-20 Medcell Biologics, Inc. Oxygen enriched bioreactor and method of culturing cells

Non-Patent Citations (13)

* Cited by examiner, † Cited by third party
Title
BANIK G.G., HEATH C.A.: "Partial and total cell retention in a filtration-based homogeneous perfusion reactor", BIOTECHNOL. PROG., vol. 11, 1995, pages 584 - 588, XP002332439 *
DOYLE, A.; GRIFFITHS, J. B.; NEWELL, D. G.: "Cell &Tissue culture: Laboratory Procedures", 1993, JOHN WILEY & SONS
FRESHNEY, R.: "Culture of animal cells", 2000, WILEY-LISS
FUREY, J.: "Continuous Cell Culture Using the ATF System", GENETIC ENGINEERING NEWS, vol. 20, no. 10, 15 May 2000 (2000-05-15), pages 52 - 53, XP002317547 *
J. FUREY: "Continuous Cell Culture Using the ATF System", GENETIC ENGINEERING NEWS, vol. 20, no. 10, 15 May 2000 (2000-05-15), pages 52 - 53
JONES D H ET AL: "PER.C6 CELL LINE FOR HUMAN ANTIBODY PRODUCTION CRUCELL'S TECHNOLOGY MAINTAINS HUMAN GLYCOSYLATION PATTERNS", GENETIC ENGINEERING NEWS, MARY ANN LIEBERT, NEW YORK, US, vol. 22, no. 10, 15 May 2002 (2002-05-15), pages 50,54, XP009018783, ISSN: 1270-6377 *
JORJANI, P. AND OZTURK S.S.: "Effects of cell density and temperature on oxygen consumption rate for different mammalian cell lines", BIOTECHNOLOGY AND BIOENGINEERING, vol. 64, no. 3, 5 August 1999 (1999-08-05), pages 349 - 356, XP002332438 *
KYUNG ET AL., CYTOTECHNOLOGY, vol. 14, 1994, pages 183 - 190
See also references of EP1720972A1
VELEZ D ET AL: "USE OF TANGENTIAL FLOW FILTRATION IN PERFUSION PROPAGATION OF HYBRIDOMA CELLS FOR PRODUCTION OF MONOCLONAL ANTIBODIES", BIOTECHNOLOGY AND BIOENGINEERING. INCLUDING: SYMPOSIUM BIOTECHNOLOGY IN ENERGY PRODUCTION AND CONSERVATION, JOHN WILEY & SONS. NEW YORK, US, vol. 33, no. 7, 20 February 1989 (1989-02-20), pages 938 - 940, XP000005263, ISSN: 0006-3592 *
VOISARD D ET AL: "Potential of cell retention techniques for large-scale high-density perfusion culture of suspended mammalian cells.", BIOTECHNOLOGY AND BIOENGINEERING, vol. 82, no. 7, 30 June 2003 (2003-06-30), pages 751 - 765, XP002317548, ISSN: 0006-3592 *
VOISIER ET AL., BIOTECHNOL. BIOENG., vol. 82, 2003, pages 751 - 765
WOODSIDE S M ET AL: "Mammalian cell retention devices for stirred perfusion bioreactors", CYTOTECHNOLOGY, KLUWER ACADEMIC PUBLISHERS, DORDRECHT, NL, vol. 28, no. 1-3, 1998, pages 163 - 175, XP002301951, ISSN: 0920-9069 *

Cited By (106)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9260695B2 (en) 2004-03-05 2016-02-16 Dpx Holdings B.V. Process for cell culturing by continuous perfusion
US8206981B2 (en) 2004-03-05 2012-06-26 Dsm Ip Assets B.V. Process for cell culturing by continuous perfusion and alternating tangential flow
EP1988170B1 (en) 2006-02-24 2019-05-01 Toray Industries, Inc. Method of producing chemical product and continuous fermentation apparatus
US9587253B2 (en) 2006-02-24 2017-03-07 Toray Industries, Inc. Method of producing chemical product with continuous fermentation and filtering
EP1870450A1 (en) * 2006-06-21 2007-12-26 DSMIP Assets B.V. Process for the culturing of E1-immortalized HER cells
AU2011211462B2 (en) * 2006-07-14 2013-04-18 Dpx Holdings B.V. Improved process for the culturing of cells
WO2008006494A1 (en) * 2006-07-14 2008-01-17 Dsm Ip Assets B.V. Improved process for the culturing of cells
EP2343362B2 (en) † 2006-07-14 2024-04-03 Patheon Holdings I B.V. Improved process for the culturing of cells
JP2009543565A (en) * 2006-07-14 2009-12-10 ディーエスエム アイピー アセッツ ビー．ブイ． Improved method of culturing cells
EP2343362A1 (en) 2006-07-14 2011-07-13 DSM IP Assets B.V. Improved process for the culturing of cells
TWI512102B (en) * 2006-07-14 2015-12-11 Dpx Holdings Bv Improved process for the culturing of cells
AU2007272054B2 (en) * 2006-07-14 2011-09-08 Dpx Holdings B.V. Improved process for the culturing of cells
EP2041259B1 (en) 2006-07-14 2015-10-14 DPx Holdings B.V. Improved process for the culturing of cells
US8119368B2 (en) 2006-07-14 2012-02-21 Dsm Ip Assets B.V. Process for the culturing of cells
TWI627274B (en) * 2006-07-14 2018-06-21 荷蘭商培森控股公司 Improved process for the culturing of cells
US8440458B2 (en) 2006-07-14 2013-05-14 Dsm Ip Assets B.V. Process for the culturing of cells
EA016451B1 (en) * 2006-07-14 2012-05-30 ДСМ АйПи АССЕТС Б.В. Improved process for the suspension culturing of cells
EP2634242B1 (en) 2006-07-14 2017-04-05 Patheon Holdings I B.V. Improved process for the culturing of cells
US8222001B2 (en) 2006-07-14 2012-07-17 Dsm Ip Assets B.V. Process for the culturing of cells
JP2012165764A (en) * 2006-07-14 2012-09-06 Dsm Ip Assets Bv Improved process for culturing cell
EP2634243B1 (en) 2006-07-14 2017-09-06 Patheon Holdings I B.V. Improved process for the culturing of cells
US9670520B2 (en) 2006-07-14 2017-06-06 Patheon Holdings | B.V. Process for the culturing of cells
CN102876628A (en) * 2006-07-14 2013-01-16 帝斯曼知识产权资产管理有限公司 Improved process for the culturing of cells
KR20130014640A (en) * 2006-07-14 2013-02-07 디에스엠 아이피 어셋츠 비.브이. Improved process for the culturing of cells
EP2343362B1 (en) 2006-07-14 2016-03-30 DPx Holdings B.V. Improved process for the culturing of cells
KR101143796B1 (en) * 2006-07-14 2012-05-21 디에스엠 아이피 어셋츠 비.브이. Improved process for the culturing of cells
AU2013204016B2 (en) * 2006-07-14 2015-06-04 Dpx Holdings B.V. Improved process for the culturing of cells
US9469865B2 (en) 2006-07-14 2016-10-18 Dpx Holdings B.V. Process for the culturing of cells
EP2634250B1 (en) 2006-07-14 2017-04-05 Patheon Holdings I B.V. Improved process for the culturing of cells
EP2634243A1 (en) 2006-07-14 2013-09-04 DSM IP Assets B.V. Improved process for the culturing of cells
EP2634242A1 (en) 2006-07-14 2013-09-04 DSM IP Assets B.V. Improved process for the culturing of cells
EP2634250A1 (en) 2006-07-14 2013-09-04 DSM IP Assets B.V. Improved process for the culturing of cells
AU2011211462C1 (en) * 2006-07-14 2015-01-22 Dpx Holdings B.V. Improved process for the culturing of cells
TWI413689B (en) * 2006-07-14 2013-11-01 Dsm Ip Assets Bv Improved process for the culturing of cells
CN104263700A (en) * 2006-07-14 2015-01-07 帝斯曼知识产权资产管理有限公司 Improved Process For The Culturing Of Cells
US8685731B2 (en) 2006-07-14 2014-04-01 Dsm Ip Assets B.V. Process for the culturing of cells
JP2011067222A (en) * 2006-07-14 2011-04-07 Dsm Ip Assets Bv Improved process for culturing of cell
JP2014217395A (en) * 2006-07-14 2014-11-20 ディーエスエム アイピー アセッツ ビー．ブイ． Improved process for culturing cells
AU2007272054C1 (en) * 2006-07-14 2014-08-28 Dpx Holdings B.V. Improved process for the culturing of cells
KR101685246B1 (en) 2006-07-14 2016-12-09 디피엑스 홀딩스 비.브이. Improved process for the culturing of cells
US8679778B2 (en) 2007-06-13 2014-03-25 Cmc Biologics A/S Method for producing a biopolymer (e.g. polypeptide) in a continuous fermentation process
JP2014100148A (en) * 2007-12-27 2014-06-05 Baxter Internatl Inc Cell culture processes
WO2010003759A3 (en) * 2008-06-17 2010-03-04 Dsm Ip Assets B.V. Cell culturing method
WO2010003759A2 (en) * 2008-06-17 2010-01-14 Dsm Ip Assets B.V. Cell culturing method
US10041049B2 (en) * 2008-11-03 2018-08-07 Janssen Vaccines & Prevention B.V. Method for the production of adenoviral vectors
US20110207202A1 (en) * 2008-11-03 2011-08-25 Crucell Holland Bv Method for the production of adenoviral vectors
US8546123B2 (en) 2009-07-16 2013-10-01 Crucell Holland B.V. Production of poliovirus at high titers for vaccine production
US9022240B2 (en) 2009-07-16 2015-05-05 Crucell Holland B.V. Production of poliovirus at high titers for vaccine production
WO2011006823A1 (en) 2009-07-16 2011-01-20 Crucell Holland B.V. Production of polio virus at high titers for vaccine production
US8460920B2 (en) 2009-10-15 2013-06-11 Crucell Holland B.V. Method for the purification of adenovirus particles
WO2011045381A1 (en) 2009-10-15 2011-04-21 Crucell Holland B.V. Process for adenovirus purification from high cell density cultures
WO2011045378A1 (en) 2009-10-15 2011-04-21 Crucell Holland B.V. Method for the purification of adenovirus particles
US8470585B2 (en) 2009-10-15 2013-06-25 Crucell Holland B.V. Process for adenovirus purification from high cell density cultures
EP3431608A3 (en) * 2009-11-17 2019-02-20 E. R. Squibb & Sons, L.L.C. Method for enhanced protein production
EP3431608A2 (en) 2009-11-17 2019-01-23 E. R. Squibb & Sons, L.L.C. Method for enhanced protein production
EP2501822B1 (en) 2009-11-17 2017-08-16 E. R. Squibb & Sons, L.L.C. Methods for enhanced protein production
CN102762721A (en) * 2010-02-15 2012-10-31 克鲁塞尔荷兰公司 Method for the production of Ad26 adenoviral vectors
CN102762721B (en) * 2010-02-15 2015-03-11 克鲁塞尔荷兰公司 Method for the production of Ad26 adenoviral vectors
US20120315696A1 (en) * 2010-02-15 2012-12-13 Alfred Luitjens METHOD FOR THE PRODUCTION OF Ad26 ADENOVIRAL VECTORS
WO2011144561A1 (en) 2010-05-18 2011-11-24 Crucell Holland B.V. Methods for welding ethylene vinyl acetate (eva) tubing, tubing obtained thereby and use of such tubing for sterile transfer of content into a bioreactor
CN103154233A (en) * 2010-10-05 2013-06-12 诺沃—诺迪斯克保健股份有限公司 Process for protein production
EP2957628A1 (en) * 2010-10-05 2015-12-23 Novo Nordisk Health Care AG Process for protein production
WO2012045769A1 (en) * 2010-10-05 2012-04-12 Novo Nordisk Health Care Ag Process for protein production
US10138290B2 (en) 2010-10-05 2018-11-27 Novo Nordisk Healthcare Ag Process for protein production
EP3626737B1 (en) * 2011-05-13 2023-11-29 Octapharma AG A method of increasing the productivity of eucaryotic cells in the production of recombinant fviii
US10213508B2 (en) 2011-10-18 2019-02-26 Coherus Biosciences, Inc. Etanercept formulations stabilized with xylitol
US10772963B2 (en) 2011-10-18 2020-09-15 Coherus Biosciences, Inc. Etanercept formulations stabilized with xylitol
US11000588B2 (en) 2011-10-18 2021-05-11 Coherus Biosciences, Inc. Etanercept formulations stabilized with sodium chloride
US10493151B2 (en) 2011-10-18 2019-12-03 Coherus Biosciences, Inc. Etanercept formulations stabilized with sodium chloride
US10293049B2 (en) 2011-10-18 2019-05-21 Coherus Biosciences, Inc. Etanercept formulations stabilized with amino acids
US11129876B2 (en) 2011-10-18 2021-09-28 Coherus Biosciences, Inc. Etanercept formulations stabilized with amino acids
US10822429B2 (en) 2012-07-09 2020-11-03 Coherus Biosciences, Inc. Etanercept formulations exhibiting marked reduction in sub-visible particles
US10954295B2 (en) 2012-09-11 2021-03-23 Coherus Biosciences, Inc. Correctly folded etanercept in high purity and excellent yield
US10947306B2 (en) 2012-09-11 2021-03-16 Coherus Biosciences, Inc. Correctly folded etanercept in high purity and excellent yield
US11001627B2 (en) 2012-09-11 2021-05-11 Coherus Biosciences, Inc. Correctly folded etanercept in high purity and excellent yield
US10954293B2 (en) 2012-09-11 2021-03-23 Coherus Biosciences, Inc. Correctly folded etanercept in high purity and excellent yield
US10954294B2 (en) 2012-09-11 2021-03-23 Coherus Biosciences, Inc. Correctly folded etanercept in high purity and excellent yield
WO2014073967A1 (en) 2012-11-09 2014-05-15 Biosana Pty Ltd. Discontinuous fed batch processing with the use of alternating bioreactors
RU2668796C2 (en) * 2013-03-15 2018-10-02 Джензим Корпорейшн Methods for creation of high density cell bank (variants)
EP2976418B1 (en) 2013-03-19 2020-09-30 CMC Biologics A/S A method for producing a product (e.g. polypeptide) in a continuous cell culture fermentation process.
EP3391942A1 (en) * 2013-03-26 2018-10-24 Coherus Biosciences, Inc. Protein production method
US10975138B2 (en) 2013-03-26 2021-04-13 Coherus Biosciences, Inc. Correctly folded etanercept composition
EP2978498A4 (en) * 2013-03-26 2016-10-05 Coherus Biosciences Inc Protein production method
AU2019201129B2 (en) * 2013-03-26 2020-12-24 Coherus Biosciences, Inc. Protein production method
WO2014160790A1 (en) * 2013-03-26 2014-10-02 Coherus Biosciences, Inc. Protein production method
AU2014241259B2 (en) * 2013-03-26 2018-12-06 Coherus Biosciences, Inc. Protein production method
AU2014241259B9 (en) * 2013-03-26 2018-12-20 Coherus Biosciences, Inc. Protein production method
US10421986B2 (en) 2013-09-30 2019-09-24 Janssen Vaccines & Prevention B.V. Method for the clarification of high-density crude cell culture harvest
WO2015095809A1 (en) * 2013-12-20 2015-06-25 Biogen Idec Ma Inc. Use of perfusion seed cultures to improve biopharmaceutical fed-batch production capacity and product quality
EP3152317B1 (en) 2014-06-04 2019-01-02 Amgen Inc. Methods for harvesting mammalian cell cultures
US11384378B2 (en) 2014-06-04 2022-07-12 Amgen Inc. Methods for harvesting mammalian cell cultures
US11427848B2 (en) 2014-06-04 2022-08-30 Amgen Inc. Methods for harvesting mammalian cell cultures
US10294460B2 (en) 2014-07-24 2019-05-21 Janssen Vaccines & Prevention B.V. Process for the purification of poliovirus from cell cultures
US10092888B2 (en) 2014-11-07 2018-10-09 Genesis Technologies, Llc Linear reciprocating actuator
US11781102B2 (en) 2016-04-14 2023-10-10 Trizell Ltd. Large-scale PEI-mediated plasmid transfection
US11242504B2 (en) 2016-04-14 2022-02-08 Trizell Ltd. Aseptic bioreactor sampling system
US11261416B2 (en) 2016-04-14 2022-03-01 Trizell Ltd. Fixed-bed bioreactor with constant-flow pump / tubing system
KR102535013B1 (en) * 2016-04-14 2023-05-22 트리젤 엘티디. Fixed bed bioreactor with constant flow pump/tubing system
KR20180133487A (en) * 2016-04-14 2018-12-14 트리젤 엘티디. Fixed-bed bioreactor with constant flow pump / tubing system
US11492578B2 (en) 2016-06-30 2022-11-08 Fujifilm Corporation Membrane separation method of cell suspension, and cell culture device
WO2019055796A1 (en) * 2017-09-15 2019-03-21 Bristol-Myers Squibb Company Online biomass capacitance monitoring during large scale production of polypeptides of interest
CN111868223A (en) * 2017-09-15 2020-10-30 百时美施贵宝公司 Online biomass capacitance monitoring during large-scale production of target polypeptides
US11193103B2 (en) 2017-10-16 2021-12-07 Regeneran Pharmaceuticals, Inc. Perfusion bioreactor and related methods of use
US11965153B2 (en) 2017-10-16 2024-04-23 Regeneron Pharmaceuticals, Inc. Perfusion bioreactor and related methods of use
WO2020165873A1 (en) * 2019-02-15 2020-08-20 Oncosimis Biotech Private Limited Method and system for enhanced continuous production, secretion and separation of recombinant polypeptides from bacteria
WO2022027013A1 (en) 2020-07-28 2022-02-03 Seagen Inc. Methods and systems for producing polypeptides

Also Published As

Publication number Publication date
US9260695B2 (en) 2016-02-16
JP2016039817A (en) 2016-03-24
AU2005229359A1 (en) 2005-10-13
EP1720972A1 (en) 2006-11-15
PT1720972E (en) 2014-04-07
CN104593277A (en) 2015-05-06
KR101050585B1 (en) 2011-07-19
US20130266985A1 (en) 2013-10-10
US20140087424A1 (en) 2014-03-27
JP2017225443A (en) 2017-12-28
US20080131934A1 (en) 2008-06-05
IL177724A (en) 2011-01-31
JP2011125348A (en) 2011-06-30
IL177724A0 (en) 2006-12-31
EP2308958A2 (en) 2011-04-13
JP2007525984A (en) 2007-09-13
JP2012090632A (en) 2012-05-17
CA2557046A1 (en) 2005-10-13
AU2005229359B2 (en) 2009-01-08
EP1720972B1 (en) 2014-01-08
US8206981B2 (en) 2012-06-26
JP2014128272A (en) 2014-07-10
DK1720972T3 (en) 2014-04-14
KR20070022221A (en) 2007-02-26
PL1720972T3 (en) 2014-06-30
EP2540815A1 (en) 2013-01-02
CN1930281A (en) 2007-03-14
ES2456015T3 (en) 2014-04-21
SI1720972T1 (en) 2014-06-30
CN104388324A (en) 2015-03-04
IL205606A (en) 2011-08-31
JP5719947B2 (en) 2015-05-20
AU2005229359C1 (en) 2011-07-28
EP2308958A3 (en) 2011-08-10

Similar Documents

Publication Publication Date Title
US9260695B2 (en) Process for cell culturing by continuous perfusion
US9670520B2 (en) Process for the culturing of cells
AU2013203993C1 (en) Process for cell culturing by continuous perfusion and alternating tangential flow

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SM SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): BW GH GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 2005715787

Country of ref document: EP

Ref document number: 2557046

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 177724

Country of ref document: IL

WWE Wipo information: entry into national phase

Ref document number: 2005229359

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 2007501239

Country of ref document: JP

Ref document number: 1020067018075

Country of ref document: KR

Ref document number: 200580007175.4

Country of ref document: CN

Ref document number: 5130/DELNP/2006

Country of ref document: IN

NENP Non-entry into the national phase

Ref country code: DE

WWW Wipo information: withdrawn in national office

Ref document number: DE

ENP Entry into the national phase

Ref document number: 2005229359

Country of ref document: AU

Date of ref document: 20050304

Kind code of ref document: A

WWP Wipo information: published in national office

Ref document number: 2005229359

Country of ref document: AU

WWP Wipo information: published in national office

Ref document number: 2005715787

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: 1020067018075

Country of ref document: KR

WWE Wipo information: entry into national phase

Ref document number: 10591118

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 10591118

Country of ref document: US

WWE Wipo information: entry into national phase

Ref document number: 205606

Country of ref document: IL