 EUCARION CELL PACKING CULTIVATION METHODS
专利摘要:
Methods for Batch Cultivation of Eukaryotic Cells The present invention relates to an apparatus and method for maintaining ph within a conductive range for cell growth in a bicarbonate-containing cell culture system without the addition of base. The method is based on the gas transfer characteristics of the bioreactor system to modulate the transfer of co2 to and from cell culture so that the ph of cell culture can be maintained within a desired range. 公开号:BR112012000242B1 申请号:R112012000242-2 申请日:2010-07-06 公开日:2019-07-09 发明作者:Dinesh Baskar；Inn H Yuk；Jenny Hsiung；Woon-Lam Susan Leung 申请人:Genentech Inc； IPC主号:
专利说明:
“METHODS FOR CULTIVATING BOTTLES OF EUCARIONTES CELLS” [001] This application claims benefit from the provisional patent application US 61 / 223,313, filed on July 6, 2009, which is incorporated in this application as a reference. Field of the Invention [002] The present invention relates to an apparatus and method for culturing eukaryotic cells in a medium containing bicarbonate that allows the maintenance of the pH of the cell culture without adding bases directly to the culture medium. Background of the Invention [003] The culture of cells for cell banks, for the production of cellular products, such as the production of recombinant protein is hampered by changing the conditions under which cells grow. Although stainless steel bioreactors are often used for the production of cells, disposables are increasingly used at all stages in the production of biological products (Rao et al., 2009). In upstream processing, disposable bioreactors offer many advantages over their stainless steel counterparts (ranging from reduced risks of cross contamination to cost and time savings). WAVE Bioreactor ™ is a well-documented example of disposable upstream technology used for the production of recombinant protein in the biopharmaceutical industry (Cronin et al., 2007; Haldankar et al., 2006; Ling et al., 2003; Ye et al. , 2009). [004] The WAVE Bioreactor ™ system, developed by Singh (Singh, 1999), comprises a pre-sterilized, flexible and disposable culture chamber (Cellbag ™), controllers for mixing CO2 and / or O2 in the air and a platform with pneumatic control for balance and heating, Cellbag ™. O Petition 870180128492, of 10/09/2018, p. 13/79 2/45 rocking motion generated by this platform provides mixing and transfer of gas in Cellbag ™. [005] The WAVE Bioreactor ™ system can be further equipped to provide pH and online dissolved oxygen (DO) monitoring and real-time feedback command control (Mikola et al., 2007; Tang et al., 2007) . However, the necessary additional devices, as well as the need for specially designed bags to accommodate the pH and DO probes, increase the cost and operational complexity of the system. In addition, the addition of base required to raise the pH of the culture to the set point defined in the bioreactor with controlled pH increases the osmolality of the culture. Depending on the amplitude of the increase in osmotic pressure in the bioreactor, the associated decrease in cell growth and viability (deZengotita et al., 2002; Zhu et al., 2005) can negate the benefits of pH control. In addition, if the pH probe fails, the resulting pH disturbances can alter cell metabolism and promote cell death (Miller et al., 1988; Osman et al., 2002). [006] Tight pH and DO controls may not be necessary for applications of certain cell cultures, such as the routine of passing cells in small-scale culture systems, such as agitated flasks and shakers, for cell maintenance and expansion. However, extreme pH and DO are detrimental to cell growth and viability (Lin etal., 1993; Link et al., 2004; Miller et al., 1988; Osman et al., 2001), and can affect product quality (Restelli et al., 2006; Yoon et al., 2005). Therefore, it is extremely important to maintain some control over these cell growth conditions for all stages of making biological products. Researchers have previously demonstrated success in Petition 870180128492, of 10/09/2018, p. 14/79 3/45 CHO cells in a pH range of 6.8 to 7.3 and in the OD range of 10 to 100% air saturation (Link et al. 2004; Restelli et al. 2006; Trummer et al. 2006 ; Yoon et al. 2005). [007] The additional features of conventional bioreactors, such as real-time pH monitors and DO monitoring control significantly increase the cost and intensity of cell culture work in the manufacture of biological products. In addition, the failure or malfunction of these resources can cause unacceptable variations and loss of potential of the cell culture, which has a high cost of time and resources. [008] Thus, there is a need for improved methods for culturing eukaryotic cells, without the need to introduce strong bases, and without additional monitoring and control of pH and DO in real time. Brief Description of the Invention [009] The present invention provides an apparatus and method for maintaining the pH in a cell culture system without the addition of base. In a cell culture medium containing bicarbonate, the amount of CO2 in the medium affects the pH of the medium, based on the acid-bicarbonate buffer balance (Equation 1): CO2 + HOH <===> H2CO3 <===> H + + HCOspH = pK - log ([CO 2 ] / [HCO3]) [010] Thus, the present invention explores this relationship to adjust the pH of the medium cell culture without the need to add strong acids or bases, by increasing or decreasing the concentration of dissolved CO2 using the dynamic interface of a liquid and gas phase of a cell culture system. The present invention provides a method for achieving such modulation and an apparatus for practicing the method. Petition 870180128492, of 10/09/2018, p. 15/79 4/45 [011] In general, the apparatus of the present invention is supplied with air, oxygen or a combination of these gases to maintain the dissolved oxygen from the cell culture. By supplying a gas mixture (which can be manipulated in terms of its composition and the rate of introduction) into the void of the apparatus, CO2 can be either added to or removed from the cell culture medium, depending on the differential CO2 concentration between the liquid phase and the gas phase. Removing CO2 from the void increases the pH of the culture as the CO2 dissolved in the medium diffuses out of the void. On the other hand, when 0 CO2 is added to the apparatus at a concentration that is greater than that of the medium, the CO2 dissolves in the medium and the pH of the culture decreases. This present invention provides a method that allows the transfer of CO2 into and out of the cell culture to maintain the pH of the culture without the addition of base. [012] Accordingly, the present invention provides a method for culturing eukaryotic cells that comprises eukaryotic cells in a culture liquid containing bicarbonate in a container, where the container has walls that encapsulate the cell culture and an empty gas phase space ( gas phase head space) above said cell culture. The container also comprises at least one door that provides a gas inlet and outlet from said empty space. The container is agitated to provide a dynamic interface between the liquid phase and the gas phase. The pH of the culture can be monitored and a gas is supplied to the void space through said port, where the gas contains an amount of CO2 to cause a decrease in pH the more CO2 dissolves in the cell culture, or accumulated CO2 is removed of empty space through the door to cause an increase in the pH of the cell culture. The pH is thus kept within a predetermined range. Petition 870180128492, of 10/09/2018, p. 16/79 5/45 [013] Generally, the partial pressure of CO2 dissolved in the cell culture medium is maintained in an amount of 1 to 200 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 10 to 180 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 20 to 150 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 100 to 180 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 20 to 80 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 30 to 60 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 35 to 50 mmHg. In some embodiments, the partial pressure of dissolved CO2 is 40 mmHg. [014] The empty space can be released continuously or intermittently. [015] In general, OD is kept above 10%. In some embodiments, OD is maintained above 20%. In some embodiments, OD is maintained above 30%. In some embodiments, OD is maintained above 40%. In some embodiments, OD is maintained above 50%. In some embodiments, OD is maintained above 60%. [016] In some embodiments, the gas flow rate inside the container is 0.001 of the volume of the empty space per minute (hvm). In some embodiments, the gas flow rate within the container is 0.005 hvm. In some embodiments, the gas flow rate within the container is 0.01 hvm. In some embodiments, the gas flow rate within the container is 0.02 hvm. In some embodiments, the gas flow rate within the container is 0.05 hvm. In some embodiments, the gas flow rate within the container is 0.1 hvm. In some embodiments, the gas flow rate within the container is 0.2 hvm. In some embodiments, the gas flow rate within the container is 0.5 hvm. In some embodiments, the rate of Petition 870180128492, of 10/09/2018, p. 17/79 6/45 gas flow within the container is 0.9 hvm. In some embodiments, the gas flow rate within the container is 1.0 hvm. [017] Eukaryotic cells can be vertebrate cells like, but are not limited to cells of frogs, rabbits, rodents, sheep, goats, dogs, cats, cows, horses, pigs, non-human primates, or humans. [018] The method can be carried out in a container that has rigid or foldable walls, such as a plastic reservoir or disposable culture bag. [019] The container can be agitated by any means that provides a dynamic interface between the liquid phase and the gas phase in the container. This agitation can be, for example, by swinging, orbital movement, a figure eight in motion, rotation movement, agitation and the like. [020] In some embodiments, agitation is carried out by rocking. The swing speed and angle can be adjusted to achieve a desired agitation. In some embodiments the swing angle is 20 °, 19 °, 18 °, 17 °, 16 °, 15 °, 14 °, 13 °, 12 °, 11 °, 10 °, 9 o , 8 o , 7 o , 6, 5, 4, 3, 2 or 1 °. In certain embodiments, the swing angle is between 6 to 16 °. In other embodiments, the swing angle is between 7 to 16 °. In other embodiments, the swing angle is between 8 to 12 °. [021] In some embodiments, the balance rate is 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11,1 12, 13, 14 15, 16, 17, 18, 19, 20, 21,22, 23, 24, 25, 26, 27, 28, 29, 30, 31,32, 33, 34, 35, 36, 37, 38, 39, 40 rpm. In other embodiments, the swing rate is between 19 to 25 rpm. In some embodiments, the swing rate is between 20 to 24 rpm. In some embodiments, the swing rate is between 21 to 23 rpm. Petition 870180128492, of 10/09/2018, p. 18/79 7/45 [022] The method can be carried out in which the container contains a single port that allows gas to enter and exit from the empty space of the culture. Alternatively, the container can contain a plurality of doors. [023] The pH of the culture is monitored both continuously and intermittently and the gas is introduced into the void so that the CO2 level of the gas in the void is provided both to increase and to decrease the concentration of CO2 dissolved in the liquid phase of the culture, so that the pH of the liquid phase is adjusted to a predetermined value. [024] In an alternative embodiment, the method may include a step of infusing fresh culture medium into the cell culture through a medium port. The fresh medium has a pH that allows adjustment of the general pH of the cell culture upon addition, so that the pH of the fresh medium is partially maintained in the cell culture in a predetermined pH range. Modulating the pH using fresh medium with a predetermined pH is useful in the culture method, but it is not sufficient to completely control the pH. [025] The method is adaptable to any size of culture. In some embodiments, the method is carried out on disposable bioreactor bags that are commercially available. These disposable bioreactor bags are available in 500 ml, 1 L, 2 L, 10 L, 20 L, 50 L, 100 L, 200 L, 500 Le 1000 L. [026] Various culture parameters can be monitored and controlled. These parameters can be controlled in an automated process as the calculations are performed by a computer. Some parameters that can be controlled alone or in combination include, but are not limited to, gas flow, pH, dissolved CO2 concentration, temperature and agitation. Petition 870180128492, of 10/09/2018, p. 19/79 8/45 [027] The present invention also provides an apparatus for carrying out the method of the present invention. Brief Description of the Figures [028] Figure 1 shows an example of an apparatus of the invention that includes an infusion filter. The apparatus includes a gas inlet and outlet port, a port to supply fresh medium to the culture, a perfusion filter to remove used medium, a swing deck and a base. The rocking motion allows the stirring to provide sufficient transfer of O2 and CO2 inside and outside the cell culture medium. [029] Figure 2 shows free cell studies to measure oxygen transfer in the WAVE Bioreactor ™. (Panel A) Effect of the swing rate and swing angle on the ki_a on the air flow rate of 0.2 l / min; (Panel B) Effect of the swing rate, swing angle and air flow rate on ki_a; (Panel C) raw OD data for different swing angles, swing rate and constant gas flow rate of 0.2 l / min (also referred to in this application as LPM); (Panel D) course data in relation to the gross OD time for two different established balance points with different gas flow rates. [030] Figure 3 shows free cell studies to assess the transfer rate of CO2 depletion in the WAVE Bioreactor ™. (Panel A); raw pH elevation data for different swing angles, swing rate with a constant gas flow rate of 0.2 LPM; (Panel B) data of course in relation to the time of the rise in crude pH for two different established balance points with different gas flow rates. (Panel C) calculated rate of pH change for different balance conditions shown in Panel A; (Panel D) calculated rate of pH change for different swing conditions and different gas flow rates shown in Panel B. The full bars are the rate of change in pH for Petition 870180128492, of 10/09/2018, p. 20/79 9/45 first 5 minutes and the empty bars are the calculated rate of change in pH for the next 55 minutes. [031] Figure 4 shows (Panel A) VCC, (Panel B) pH offline, (Panel C) pCO2 offline, and (Panel D) offline OD profiles for batch cultures in the WAVE Bioreactor ™ . The process conditions are shown in Table 2, below. Only the inoculation stage was evaluated for (i) cell line that produces MAb B, although both the inoculation stages and scaling up (during which the volume increased from 6 I to 20 I) were evaluated for (ii ) cell line that produces MAb C. During each stage, the air pumped into the empty space was supplemented with 8% (v / v) CO2 for the first day, 5% (v / v) for the second day, and the 2% (v / v) subsequently. [032] Figure 5 shows (Panel A) VCC, (Panel B) culture viability (Panel C) offline pH, and (Panel D) DO concentration for two perfusion cultures in the WAVE Bioreactor ™ using lineage cell that produces MAb A performed under non-optimized conditions. The cells were cultured in batch mode for the first 6 days and in perfusion mode subsequently. During batch cultivation, the working volume in the Cellbag ™ was first inoculated with 6 I of culture, and on day 3, this culture volume was increased to 25 I by the addition of fresh medium. During the perfusion culture, the culture volume was maintained at 25 I at an infusion rate of 1 volume per day. For this set of experiments, the swing rate was 18 rpm and the swing angle was 8 degrees, while the air flow rate in the void was 0.2 l / min. This air was supplemented with 5% CO2 (v / v) for the complete duration of the culture. [033] Figure 6 shows the growth profile of the cell culture and the pH profile for a batch (days 0 to 6) / perfusion process (days 6 to Petition 870180128492, of 10/09/2018, p. 21/79 10/45 14). (Panel A)% PCV packed cell volume; (Panel B) cell viability; (Panel C) pH profile; (Panel D) cell growth in viable cell count (VCC) measured by ViCell ™ AS. [034] Figure 7 shows the performance of the crop based on variations in the empty space release rates (hvm). (Panel A) shows 2 experiments with an airflow increase step that causes an increase in the clearance rate of the empty space (0.1 hvm in (♦) and 0.02 hvm (-A-). The other strategy the clearance rate of the empty space is many steps of increase (0.007 hvm to 0.013 hvm to 0.02 hvm) (-) on days 10 and 11. (Panel B) the partial pressure of dissolved CO2 measured by NOVA BioProfile® 400. [035] Figure 8 shows (Panel A) VCC, (Panel B) culture viability (Panel C) offline pH, and (Panel D) DO concentration for cultures in the WAVE Bioreactor ™ of six different cell lines - each one producing a different MAb - using the optimized process. During each 6 I inoculation stage, cultures were balanced at 21 rpm, and the air flow rate in the void was 0.2 l / min. The air was supplemented with 8% CO2 (v / v) for the first day, 5% (v / v) for the second day, and 2% (v / v) subsequently. This airflow strategy was repeated for a 20 I scale-up stage (days 3 to 6). During the cultivation in the 20 I perfusion mode (day 6 onwards), the air flow rate in the empty space was maintained at 0.6 l / min without CO2 supplementation, although the O2 mixture in the air at the air inlet has been increased from 0% (v / v) to 30% (v / v) on day 8, and maintained at 30% (v / v) for the remainder of the culture. The batch of 20 l and the perfusion cultures were balanced at 23 rpm. The balance angle for all cultures was constant at 10 s . Petition 870180128492, of 10/09/2018, p. 22/79 11/45 [036] Figure 9 shows (Panel A) VCC, (Panel B) viability, (Panel C) Offline pH, and (Panel D) Offline OD for parallel cell line cultures that produces MAb E in WAVE Bioreactor ™ (·) and bioreactor with mixing tank (□). Detailed Description of the Invention [037] The person skilled in the art is well acquainted with many protocols and methods for culturing eukaryotic cells and can use culture media for the same. These protocols and culture media are described in the literature and books as in Animal Cell Culture, A Practical Approach 2- Ed., Rickwood, D. and Hames, B.D., eds., Oxford University Press, New York (1992). General-purpose methods are also available on the internet at: protocolonline.org/prot/Cell_Biology/Cell_Culture. Cell culture medium is also commercially available from a variety of well-known sources. All literature cited in this application is incorporated by reference. Definitions [038] The cell culture techniques and procedures in general described or mentioned in this application are well understood and commonly used using conventional methodology by technicians in the subject. As appropriate, procedures involving the use of commercially available kits and reagents are generally performed in accordance with the protocols and / or parameters defined by the manufacturer unless otherwise noted. [039] Before the present methods are described, it should be understood that this invention is not limited to the specific methodology, protocols, cell lines, animal species or genera, constructs and reagents as described, can, of course, vary. It should be understood that the terminology used in this application is for the purposes of describing Petition 870180128492, of 10/09/2018, p. 23/79 12/45 only specific embodiments, and is not intended to limit the scope of the present invention which will be limited only by the appended claims. [040] It should be noted that as used in the present application and the appended claims, the singular forms "one", "e", and "o / a" include plural referents, unless the context clearly dictates otherwise. All numbers recited in the specification and associated claims (for example, 1 to 200 mm Hg, etc.) are understood to be modified by the term "about". [041] All publications mentioned in this application are incorporated into this application as a reference for disclosure and describe the methods and / or materials in connection with which the publications are cited. The publications cited in this application are cited for their previous disclosures for the date of filing of this application. Nothing here is to be construed as an admission that inventors are not designed to precede publications by virtue of an earlier priority date or an earlier date of the invention. In addition, current publication dates may differ from those shown and require independent verification. [042] As used in the present application, "about" refers to a value that is more or less 10% of a declared value. [043] As used in the present application, "stir" refers to the disturbance so that the liquid phase of the culture is a dynamic interaction with the gas phase above the culture. Shaking may refer to a movement, such as shaking, moving, rocking, orbital shaking, rotation, shaking in the form of eight or any means to make the liquid phase non-static and increase the diffusion of gases into and out of the liquid phase. Petition 870180128492, of 10/09/2018, p. 24/79 13/45 [044] As used in the present application, “gas” either refers to a pure gas or a mixture of gases that may include nitrogen, oxygen and carbon dioxide. Typically, nitrogen is present in an amount of about 60 to 90% of the total gas concentration, oxygen is present in an amount of about 10 to 40% of the total gas concentration, and carbon dioxide is present in a amount of about 0 to 50% of the total gas concentration. [045] As used in the present application, "cell culture liquid containing bicarbonate" refers to a culture medium suitable for the culture of eukaryotic cells that contains, as part of its composition, a bicarbonate buffer system. The medium may also contain additional buffering agents, such as HEPES or MOPS or the like, but it must also contain a bicarbonate-based system. [046] As used in the present application, "cell culture" refers to a liquid preparation containing eukaryotic cells in a liquid medium containing buffering agents and nutrients necessary for the growth and / or maintenance of viable cells. [047] As used in the present application, "dissolved CO2 concentration" is expressed by the relative measurement of the partial pressure of CO2 in mm Hg. Therefore, the partial pressure of dissolved CO2 is used as a reflection of the concentration of dissolved CO2. [048] "DO" refers to dissolved oxygen. [049] As used in the present application, "dynamic interface" refers to an enhanced active exchange of gases between the liquid phase and the gas phase provided by the agitation of the cell culture. [050] As used in the present application, "eukaryotic cells" refer to animal cells that can be invertebrate or vertebrate cells. Petition 870180128492, of 10/09/2018, p. 25/79 14/45 [051] As used in the present application, "head space" refers to a gas phase above the liquid phase of the cell culture with the container used for cell culture. [052] As used in the present application, hvm refers to the volume of the void space per minute and indicates the rate at which the gas in the void is released. [053] ki_a refers to the volumetric oxygen transfer coefficient. [054] ki_a CO2 refers to the volumetric transfer coefficient of carbon dioxide. [055] LPM refers to liters per minute of gas flow. [056] As used in the present application, “modular” refers to the execution of an increase or decrease in a value. [057] As used in this application, “monitor” refers to the monitoring of a specific value by sampling and analysis to determine that value both intermittently and continuously. [058] pCO 2 refers to the partial pressure of dissolved CO2 concentration. [059] As used in the present application, "door" refers to an access point to another form of closed system. [060] As used in the present application, “predetermined” refers to a value previously selected for a given parameter that is used as an objective value. [061] As used in this application, “rpm” refers to balances per minute. [062] VCC refers to the concentration of viable cells. [063] As used in this application, "container" refers to a reservoir. As used in the present application, such a container may, for Petition 870180128492, of 10/09/2018, p. 26/79 15/45 example, a flask, bioreactor, disposable bioreactor bag, culture chamber and the like. [064] As used in the present application, “wm” refers to the volume of the container per minute. Theoretical Aspects Transfer of O2 in Culture WAVE Bioreactor ™ [065] To determine the transfer rate of O2 in the WAVE Bioreactor ™, we assume a sufficiently fast response time for the online DO probe, ideal mixture in the Cellbag ™ and resistance domination of mass transfer through the liquid phase interface. Under these assumptions, the following mass balance equation would approximate the transfer rate of O2 from the gas phase to the liquid phase: ^^ = k L a »(0 2 * -O 2 ) dt (1) where O2 * is the concentration of saturated DO in the medium and O2 is the concentration of OD in the middle. Taking O2 to be zero in time zero, the equation would produce: = k L a · t (2) ln O * -0 Plotting v 2 2 'as a function of time, the slope of the best fit line would provide 0 kLa for 0 system. [066] To increase the O2 transfer rate in the WAVE Bioreactor ™ (equation 1), we can either increase 0 kLa for the system or increase the concentration gradient (O2 * - O2), or increase both. To increase 0 kLa to the WAVE Bioreactor ™ system, we could increase the swing rate, the swing angle, or the air flow rate (Mikola, 2007; Singh, 1999). To increase the concentration gradient (O2 * - O2) that provides the driving force for the transfer of O2 from the gas to the phase Petition 870180128492, of 10/09/2018, p. 27/79 16/45 net, we could increase the percentage of O2 in the gas inlet to increase O2 *. Cultivated CO2 Transfer in WAVE Bioreactor ™ [067] In a simplified model, CO2 (CO2 (g)) gas in the Cellbag ™ exists in equilibrium with 0 dissolved CO2 (CO2 (aq)) in the culture medium: CÜ2 (g) <-> CO2 (aq) (3) [068] CO2 (aq) one by one exists in equilibrium with carbonic acid (H2CO3), which can dissociate into bicabornate (HCO3): H2O + CO2 (aq) θ H2CO3 θ HCO3 · + H + (4) [069] Furthermore, the dissociation of HCO3 · in carbonate (CO3 2 ) must be insignificant in the pH range from 4 to 8 (Royce and Thornhill, 1991 ). [070] The limiting rate step for the evolution of CO2 from the culture medium must be the transfer of liquid gas mass (equation 3). Assuming that the concentration of CO2 in the liquid at the interface is in equilibrium with 0 bulk gas, the following mass balance equation would approximate the rate of CO2 transfer from the liquid to the gas phase: r C < 2 where 1 is 0 volumetric transfer coefficient of dissolved carbon dioxide. [071] Without a CO2 probe dissolved in the WAVE Bioreactor ™, we could not make CO2 measurements in real time to directly calculate the CO2 transfer rate (aq). However, based on our knowledge of the bicarbonate buffering system in our culture medium, we expect CO2 removal to increase the pH of the culture, because the balance in equations 3 and 4 would shift to the left. Assuming one Petition 870180128492, of 10/09/2018, p. 28/79 17/45 response time fast enough for the online pH probe, the pH profile that generates a dynamic CO2 transfer (aq) study should provide an indirect estimate of the CO2 removal rate (aq). [072] To increase the pH of the culture, we could increase the CO2 removal rate in the WAVE Bioreactor ™ (equation 5) both by increasing the ki_a C02 for the system, and by increasing the driving force (CO2 (aq) - CO2 ( g)) for CO2 transfer, or increasing both. Specifically, to increase the WAVE Bioreactor ™ system, we could increase the swing rate and the swing angle. To increase the driving force (CO2 (aq) CO2 (g)), we could decrease the percentage of CO2 at the gas inlet to decrease CO2 (g). Consequently, with Henry's law, the partial pressure of CO2 (g) (pCO2 (g)) in Cellbag ™ void space would limit the concentration of CO2 (aq) in the middle: CO 2 {aq) (6) where H = Henry's law constant for CO2. [073] On the other hand, to decrease the pH of the culture, we could increase the concentration of CO2 (g) in the gas inlet to increase CO2 (aq) and thereby change the balance in equation 4 to the right. Method of the Present Invention [074] In the method of the invention, eukaryotic cells are grown in an appropriate culture medium and temperature to allow for cell viability. As is known in the art, different types of cells can be grown in different media. The person skilled in the art can easily choose which medium is most suitable for a specific cell type and / or specific application. In the method of the invention, the medium must contain a bicarbonate buffer system in order to allow the modulation of the pH by CO2. The medium can contain additional agents that act as a buffer. Petition 870180128492, of 10/09/2018, p. 29/79 18/45 [075] Eukaryotic cells that can be used in the method of the invention include animal cells, which can be invertebrates, as well as vertebrate cells. Invertebrate cells include insect cells (for example, Spodoptera frugiperda, Bombyx mori and Tríchoplusia ni cells). Vertebrate cells include mammalian and non-mammalian cells. Vertebrate cells include, but are not limited to, frog cells (eg, Xenopus laevis), lagomorphs (eg, rabbit and hares), rodents (eg, rats, hamsters, Meriones persicus, gerbils and mice), cats , dogs, sheep, cattle, goats, pigs, horses, non-human and human primates. [076] The cells used in the method of the invention can be recombinant or non-recombinant cells. Recombinant cells can include cells engineered to express specific proteins (such as stable or transiently transfected cells) or cells engineered to produce specific RNAs (eg, siRNA, ribozymes, and the like). [077] The cells in the appropriate medium are placed inside the culture and gas container and are infused in the empty space. In some embodiments, the clearance rate of the empty space is within a range of about 0.002 to 0.1 hvm. In some embodiments, the clearance rate of the empty space is within a range of about 0.007 to 0.08 hvm. In some embodiments, the clearance rate of the void is within the range of about 0.009 to 0.06 hvm. In some embodiments, the clearance rate of the empty space is within a range of about 0.01 to 0.04 hvm. In some embodiments, the clearance rate of empty space is within a range of about 0.02 to 0.03 hvm. In still other embodiments, the clearance rate of the void is within the range of about 0.009 to 0.024 hvm. In additional achievements, the space clearance rate Petition 870180128492, of 10/09/2018, p. 30/79 19/45 void is within a range of about 0.007 to 0.02 hvm. The "hvm" is the ratio of volumetric gas flow rate (l / min) and the volume of the empty space (D [078] In some embodiments, for example, in a 50 I WAVE Bioreactor ™ bag, with a volume of 20 I culture and a void volume of 30 I, the gas flow rate within the container is 0.1 l / min to 1 l / min. In some embodiments, the gas flow rate within the bag is 0.2 l / min In some embodiments, the flow rate is 0.3 l / min In some embodiments, the gas flow rate is 0.4 l / min In still other embodiments , the gas flow rate is 0.5 l / min In other embodiments, the gas flow rate is 0.6 l / min In other embodiments, the gas flow rate is 0.7 l / min In still other embodiments, the flow rate is 0.8 l / min In other embodiments, the flow rate is 0.9 l / min. [079] In general, cell culture should be kept within a range of about 6 to 8. In some embodiments, the pH is maintained within a range of about 6.6 to 7.6. In some embodiments, the pH is kept within a range of about 6.9 to 7.5. In some embodiments, the pH is kept within a range of about 6.8 to 7.2. In some embodiments, the pH is kept within a range of about 7.0 to 7.3. While the method of the invention does not require pH monitoring to maintain a pH that is conducive to the growth of cells in culture, in some embodiments of the method of the invention, the pH of the culture can be monitored (intermittently or continuously). The measurement can be taken in situ or outside the natural environment. [080] In some embodiments of the method of the invention, the OD is maintained above 10%. In other projects, the OD is maintained above 20%. In other projects, the OD is maintained above 30%. In other projects, the OD is maintained above 40%. In other embodiments, the OD is maintained above 50%. In other projects, the OD is maintained above 60%. In others Petition 870180128492, of 10/09/2018, p. 31/79 20/45 achievements, the OD is kept above 70%. In other embodiments, the OD is maintained above 80%. In other embodiments, the OD is maintained above 90%. [081] The monitoring of CO2 concentration in liquid medium is well known in the art and can be performed using commercially available technology. The measurement can be taken in situ or outside the natural environment. [082] In a specific illustrative embodiment of the method of the present invention, a batch process is used, the cells being cultured in a staggered manner. In this method a WAVE Bioreactor ™ system with a 50 I bag is used with a 20 I culture workload in which the empty space is infused with gas supplemented with 8% CO2 (v / v) gas for the first day , 5% CO2 gas (v / v) on the second day and 2% CO2 (v / v) gas subsequently. The WAVE Bioreactor ™ is balanced at 21 rpm at 10 s and 0.2 l / min for inoculation and then at 23 rpm, 10 s of swing angle and 0.2 l / min for the step of scaling. In this arrangement, it is not necessary to monitor 0 pH as the pH will be maintained by the parameters used. [083] In a specific embodiment illustrating the method of the present invention, an perfusion process is used. In this method, a WAVE Bioreactor ™ with 50 I bag is used with a 20 I workload of culture. The bag is infused with gas that is supplemented with 30% O2 (v / v), two days after the start of the infusion. The gas flow rate is increased step by step from 0.2 l / min on day 0, and then increased to 0.4 l / min on day 3, and then increased to 0.6 l / min on day 6. In this arrangement, it is not necessary to monitor 0 pH as the pH will be maintained by the parameters used. [084] In another illustrative embodiment specific to the method of the present invention, an infusion process is used. In this method, a Petition 870180128492, of 10/09/2018, p. 32/79 21/45 WAVE Bioreactor ™ with 50 I bag is used with a 20 I workload of culture. The bag is infused with gas that is supplemented with 30% O2 (v / v, two days after the start of the infusion. The gas flow rate is maintained at a constant flow rate of 0.6 l / min. arrangement, it is not necessary to monitor 0 pH as the pH will be maintained by the parameters used. [085] In yet another illustrative embodiment specific to the method of the invention, an infusion process is used. In this method, a WAVE Bioreactor ™ with 50 I bag is used with a 20 I workload of culture. The bag is infused with gas that is supplemented with 30% O2 (v / v), two days after the start of the infusion. The gas flow rate is maintained at a constant flow rate of 1.0 l / min. In this arrangement, it is not necessary to monitor 0 pH as the pH will be maintained by the parameters used. [086] It will be apparent to a person skilled in the art that the parameters of the culture conditions (gas concentrations, flow rates, hvm, swing rate, swing angles, etc.) can be adjusted using the teachings of the present application to achieve a pH with the desired range. Apparatus [087] The container for containing the cell culture medium is not limited to any specific size. The container of the present invention can be adapted to the size of disposable bioreactors and culture bags frequently used as used in the art and can be adapted for larger or smaller cultures. [088] The container is not limited to the material used to create the container. The container can be made of a solid material, like glass or rigid plastic, or it can be made of a foldable material like plastic Petition 870180128492, of 10/09/2018, p. 33/79 22/45 soft as well as that used to produce disposable bioreactor bags. [089] The container can optionally contain deflectors to increase the turbulence of the medium when stirred. [090] The container can be equipped with one or more ports to allow the addition or removal of gases and liquids. The gas can be charged into the void and removed from the void through one or more doors. In one embodiment, there is a single door that allows both gas to enter and exit. In other projects, there are two doors: one for gas inlet and one for gas outlet. In other embodiments, a plurality of ports are used to allow gas to enter and exit. [091] In some embodiments, the device may also comprise a pH monitor that continuously or intermittently monitors the pH of the cell culture medium. The pH monitor can be used to communicate with an automated system to insert gas or remove gas from the empty space of the container to change the concentration of CO2 and thereby adjust the pH of the cell culture medium. [092] In some embodiments, the apparatus of the invention comprises a CO2 monitor that continuously or intermittently monitors the partial pressure of dissolved CO2 as an indication of the concentration of CO2 in the medium. The CO2 monitor can be used to communicate with an automated system to insert gas or remove gas from the empty space of the container to change the concentration of dissolved CO2 so that the current CO2 concentration, as measured by the CO2 monitor, is modulated to adjust the concentration to a predetermined value. [093] In some embodiments, the apparatus also of the invention comprises a temperature monitor that continuously or intermittently monitors the temperature of the cell culture medium. The monitor Petition 870180128492, of 10/09/2018, p. 34/79 23/45 temperature can be used in communication with an automated system to increase or decrease the temperature so that the current temperature measured by the monitor is modulated to adjust a predetermined value. [094] The various parameter monitors can be used alone or in combination and can be controlled using an automated system controlled by a computer. The computer can be programmed to perform the calculations necessary to determine the amount of CO2 to be infused with 0 gas or removed from the gas in the empty space, in order to adjust the pH of the cell culture medium. The computer can also perform calculations with respect to temperature, agitation rate, medium perfusion and other parameters, as well as control the means to adjust parameters automatically. [095] Optionally, the apparatus of the invention includes an agitator for shaking the container so that the cell culture medium is not static, but is in dynamic interface with the gas in the void. Stirring facilitates the diffusion of gas into and out of the cell culture medium. The agitator can be any form known in the art, but includes such non-limiting examples of agitators, orbital agitators, rotators, eight-form agitators, rocking platforms, rotating platforms, and the like. [096] The automated gas supply and gas purge system may include a valve and a pump system to deliver pressurized gas through sterile filters with a control meter to control the rate of gas flow within the container. Any means known in the art for gas supply and gas removal can be employed. The gas can be introduced in response to a signal calculated on a computer when the concentration of CO2 dissolved in the cell culture medium deviates from a predetermined value. If the measured CO2 concentration Petition 870180128492, of 10/09/2018, p. 35/79 24/45 deviates from the predetermined value, the automated system calculates the amount of CO2 needed to be added to the system or removed from the system and gas with the proper amount of CO2 is introduced into the empty space as the resident gas is purged out through the exit door. The computer can perform calculations involving Equations 1, 2 and / or 3, as defined in this application and other calculations for regulating the system, as would be known to a person skilled in the art based on the available literature, commercially available systems and the teachings in this application. [097] Alternatively or in conjunction with a response system using a monitored CO2 concentration, the automated system can also measure the pH of the culture medium and respond when the measured pH deviates from a predetermined pH for growing the cells. The automated system can respond to a deviation in the concentration of CO2 and / or pH and introduce an appropriate amount of CO2 with 0 gas while the resident gas is purged out in order to correctly modulate the pH of the culture medium. [098] The apparatus and method will now be described in a non-limiting example with reference to Figure 1. Culture vessel (40) contains cell culture medium and cells (110) and empty space (130). A gas inlet port (70) with filter (50) is connected to the container (40) to allow the infusion of gas into the void (130). A gas outlet port (80) with filter (60) is connected to the container (40) to allow gas to escape out of the void (130). Container rests on the platform (30) which is connected to the balancer (20) and base (10) to allow a rocking and shaking movement of the cell culture medium (110). Stirring and flow of gas within the head space (130) allows the diffusion of O2 and CO2 into an outlet of the cell culture medium (110). The optional infusion filter (90) for Petition 870180128492, of 10/09/2018, p. 36/79 25/45 retaining the cells in the culture vessel is connected via tubing (100) to a medium port (120) to allow removal of the used culture medium from the cell culture as needed. [099] The cells are grown in cell culture medium (110) in a container (40). The empty space (130) in the container (40) is filled with gas. The flow of gas through the gas inlet port (70) and the outlet of the gas outlet port (80) allows gas to flow through the void (130) and the outflow of CO2 that diffuses through the cell culture (110) inside the empty space (130) as the culture is agitated by the rocking movement of the platform (30) on the rocker (20) attached to the base (10). The reduction of dissolved CO2 in the cell culture medium (110) causes an increase in the pH of the cell culture medium (110). [0100] The cell culture medium (110) can optionally be supplemented with the fresh medium supplied through the medium tube (140) through the medium port (150) and removed through the perfusion filter (90) rising through the tube middle (100) and out through the middle exit port (120). In this optional feature of the method of the invention, the fresh medium is supplied according to the original cell culture medium is depleted of nutrients and according to the accumulation of cellular waste products and a decrease in pH. The fresh medium is provided with a predetermined pH which is sufficient to cause an increase in the pH of the total cell culture medium after mixing to bring the cell culture medium to a predetermined ideal pH range. Examples A. Principles [0101] Since most mammalian cell culture systems use a cell culture medium containing bicarbonate, pH control in mammalian cell culture is predominantly performed by Petition 870180128492, of 10/09/2018, p. 37/79 26/45 basic additions / C02. PH control takes advantage of the carbonic acid-bicarbonate buffer system. It has been shown that in such a system, for example, a disposable bioreactor bag, the pH of the culture can be modulated by manipulating the concentration of CO2 dissolved in the medium, which can be modulated by modulating the concentration of CO2 in the void. The bi-directional pH adjustment is shown possible in the examples of the present application by modulating the CO2 concentration in the void. This method will eliminate the use of base to increase the pH in a cell culture bioreactor system. If the pH of the cell culture in the disposable bioreactor needs to be lowered, the CO2 concentration in the void can be increased by supplementing the input gas with CO2. This will allow the CO2 to be transferred to the cell culture. If the pH of the cell culture in the disposable bag needs to be increased, the CO2 concentration in the void can be decreased or the clearance rate of the void can be increased to facilitate the removal of CO2 from the cell culture. [0102] This pH maintenance method can be extended to a bioreactor system and where the transfer of gas in the bioreactor is facilitated mainly by the large surface area created in the bioreactor. Adding / Removing CO2 Based on the pH Maintenance Strategy in a Cell Bank Process [0103] During the early stages of cell culture, when there are relatively fewer cells, the pH of the cell culture typically increases. To control the pH, CO2 is typically added to the bioreactor to reduce the pH. Usually, this addition is carried out by spraying CO2 gas through the cell culture in a bioreactor with a normal stirring tank. In a disposable bioreactor of the invention, the concentration of CO2 in the void is changed so that the direction of CO2 transfer is from the gas phase to the liquid phase. As the concentration of cells increases in the Petition 870180128492, of 10/09/2018, p. 38/79 During the culture, the concentration of CO2 in the cell culture also increases and, therefore, the pH typically decreases. In a bioreactor with a normal stirring tank with 0 normal pH feedback control, a base to control 0 pH will be added. Addition of base increases the pH of the cell culture. In the disposable bioreactor of the invention, the pH increase can be accomplished by reversing the direction of CO2 transfer, decreasing the concentration of CO2 in the void, as well as increasing the clearance rate of void. This method of maintaining the pH of the cell culture, by managing the concentration of CO2 in the medium allows the elimination of base use. Based on the requirement (both increase and decrease in pH) the concentration of CO2 in the void can be decreased or increased, respectively. [0104] A disposable bioreactor system can be used as a bioreactor system to generate high cell density cell banks, such as, but not limited to Master Cell Banks (MCB) and Working Cell Banks (WCB). A perfusion cell culture process is considered to allow the production of high cell density cell banks in the disposable bioreactor. The CO2 addition / removal method is proposed to maintain the pH although the cell culture process for the generation of MCBs and WCBs has been developed. In addition, the gas transfer method to maintain 0 pH, the perfusion of the cell culture allows extra opportunities to maintain 0 pH. In a perfusion cell culture process, the fresh cell culture medium is continuously added to the bioreactor, while the used culture medium is continuously removed. The perfusion allows the removal of by-products from the cell culture that can potentially affect the pH of the cell culture. In addition, the removal of cell culture by-products, the entry of pH into the fresh cell culture medium can also change the pH of the cell culture. If you know that the pH of the cell culture will decrease, the pH of the Petition 870180128492, of 10/09/2018, p. 39/79 28/45 input medium can be increased to compensate for the decrease in pH. Alternatively, the perfusion rate can also be changed to manage the pH of the culture. All of the above approaches have an impact on pH, but the most important factor that will affect pH is the CO2 transfer method. CO2 transfer is also a more reliable approach to gas flow rate and CO2 supplementation in a disposable bioreactor can be controlled effectively without many problems. [0105] During our initial attempts to culture CHO cells in the WAVE Bioreactor ™ without pH and DO feedback controls, we identified several challenges (Figure 5): (1) slow growth during the batch culture step (days 0 to 6 ) in approximately 0.3 day 1 , (2) progressively slower growth during the perfusion cultivation stage (day 6 onwards), decreasing from approximately 0.5 day -1 during the first 3 days to less than 0.3 day 1 , thereafter, (3) pH of the initial culture sometimes exceeded 7.3, and the pH of the subsequent culture often fell below pH 6.8 and (4) OD levels were often below 20 % air saturation after 0 start of infusion on day 6. We encountered the same challenges using CHO cell lines producing other MAbs (data not shown). We attribute the slow growth of the batch culture to the high initial pH and the decline in the growth rate in the perfused culture to the decrease in pH and OD. [0106] In the absence of pH feedback control in the WAVE Bioreactor ™, the pH in these bicarbonate buffered cultures should depend on the CO2 content in the Cellbag ™ void. Despite the presence of bicarbonate buffers and HEPES in the medium, the pH of the culture should eventually drop with time as a result of the accumulation of lactate. To maintain the pH of the culture in our desired range of 6.8 to 7.2, our strategy was to manipulate the concentration of CO2 in the Cellbag ™. We would like to increase the Petition 870180128492, of 10/09/2018, p. 40/79 29/45 CO2 transfer in the medium to decrease the pH during the initial stages of batch cultivation. On the other hand, we would like to remove CO2 from the medium to increase the pH during the subsequent batch or perfusion cultivation stages. In the absence of DO feedback control in the WAVE Bioreactor ™, DO levels are expected to drop with increasing cell densities. To maintain OD> 20% air saturation, we would increase the transfer of O2 to the cultures by increasing the volumetric oxygen transfer coefficient (ki_a) for the WAVE Bioreactor ™ system and supplementing the inlet gas with O2. B. Materials and Methods 1. CHO Cell Lines and Culture Medium [0107] All cell lines used in the Examples were obtained from a CHO deficient in dihydrofolate reductase (DHFR-) host adapted to grow in suspension culture without serum. Each cell line that produces a specific monoclonal antibody (MAb) was generated by transfecting the host DHFR with a plasmid DNA that encodes genes for DHFR, light chain MAb (LC) and heavy chain MAb (HC). Stably transfected cells were subsequently maintained by passing every 2 to 5 days in exclusive chemically defined selective media containing methotrexate. The same medium that contains 1.0 g / l of Pluronic F-68, 2.44 g / l of sodium bicarbonate, and 15 mM of HEPES, plus a proprietary blend of nutrients - were used to grow WAVE Bioreactor ™ cells in both batch and infusion modes. 2. WAVE Bioreactor ™ System [0108] The WAVE Bioreactor ™ system (GE Healthcare, Piscataway, NJ, USA) used to grow CHO cells in batch or perfusion mode consisted of a balance platform, a control unit and a prepackaged - sterilized, flexible and disposable with filters Petition 870180128492, of 10/09/2018, p. 41/79 30/45 gas at the inlet and outlet and multiple sampling ports (Singh, 1999; Tang et al., 2007). Each system was equipped with a heating pad and a gas mixing box to provide temperature control and composition of the required input gas (O2 and / or CO2 mixed with 0 air), respectively. All cell culture experiments were conducted using a 50 I Cellbag ™ in a 6 or 20 I working volume, a 37 S C temperature setpoint, a 19 to 25 rpm swing rate and a swing angle from 8 to 12. PH online or DO probes were not installed on the WAVE Bioreactor ™, instead different gas flow rate and gas mix strategies were tested for their ability to maintain levels pH and OD of the culture within the target range. 3. Batch culture in the WAVE Bioreactor ™ [0109] Batch culture was started in a 6 I WAVE Bioreactor ™ by inoculation in either a regular Cellbag ™ or an infusion at ~ 7.5 x 10 5 cells / ml. A few days after inoculation, when the culture has accumulated sufficient cell mass, fresh medium was added to increase the working volume to 20 I. For each pass, the culture was maintained for 2 to 5 days in batch mode. 4. Perfusion Culture at WAVE Bioreactor ™ [0110] Unless otherwise stated, perfusion culture was initiated after the batch culture had accumulated sufficient cell mass in 20 I of working volume in a perfusion Cellbag ™ with a swing rate of 23 rpm and a swing angle of 10 s and an infusion rate of 1 workload per day. The cell retention device in the perfusion Cellbag ™ consisted of a filter that floated on the surface of the liquid during the culture process (Tang et al., 2007). The infusion filter retained the cells in the Cellbag ™ while both fresh medium was added and the filtrate was removed continuously. Was Petition 870180128492, of 10/09/2018, p. 42/79 31/45 maintained a constant volume in the perfusion WAVE Bioreactor ™ by matching the rate of addition of fresh medium with the rate of filtrate removal from a workload per day. 5. Cultivation in a Bioreactor with an Agitator Tank [0111] To compare the performance between cultures in a WAVE Bioreactor ™ and a bioreactor with an agitator tank, cells from the same germinal source were inoculated both in a WAVE Bioreactor ™ bioreactor and in a bioreactor with stainless steel stirring tank (Applikon, Foster City, CA, USA) up to ~ 7.5 x 10 5 cells / ml. The cells were first cultured in batch mode and then perfusion was started on the accumulation of sufficient cell mass. The workload was 7 l in batch mode and 15 l in perfusion mode in the bioreactor with agitator tank. The culture temperature, DO and agitation were maintained at set points of 37 S C, 30% air saturation and 125 rpm, respectively. The pH of the culture was maintained at 7.15, with a dead zone of 0.03, both by adding 1M sodium carbonate to increase the pH and by spraying CO2 gas to decrease the pH. During the perfusion operation, the Centritech centrifuge system (Centritech AB, Norsborg, Sweden) was used to separate cells from the growth medium, the cells were retained by the centrifuge and returned to the bioreactor, while the supernatant was removed (Johnson et al ., 1996). A constant volume in the bioreactor was maintained by matching the rate of addition of fresh medium with the rate of supernatant removal of one work volume per day. 6. Analysis of Off-Line Samples [0112] Cultures were sampled and analyzed for viable cell concentration (VCC) and viability (Vi Cell-AS, Beckman Petition 870180128492, of 10/09/2018, p. 43/79 32/45 Coulter, Fullerton, CA, USA), as well as for pH, OD, pCO2, glucose and lactate (Bioprofile 400, Nova Biomedical, Waltham, MA, USA). Example 1 Cell-Free Studies Gas Transfer Measurements [0113] The gas transfer characteristics in Cellbag ™ affect the performance of the culture due to its effects on OD and pH levels. As the first step aimed at maintaining pH and OD within our desired ranges, Cellbag ™ cell-free studies were performed to measure the transfer of O2 and CO2. A. O2 Transfer Studies [0114] O2 transfer was characterized in 50 I Cellbag ™ using a simulated culture medium by calculating the volumetric O2 transfer coefficient (ki_a) in various balance rate combinations (20 , 30 and 40 rpm), balance angles (8 S , 10 s and 12 s ) and gas flow rates (0.1,0.2 and 0.3 l / min). The classic dynamic purge method was used to calculate 0 ki_a (Dunn and Einsele, 1975). The test medium used for these studies was designed to simulate the patented cell culture medium: it was composed of 1.0 g / l of Pluronic F-68, 2.44 g / l of sodium bicarbonate and 15 mM of HEPES. An OD OxyProbe® probe connected to a Model 40 transmitter from the same manufacturer (BroadleyJames Corporation, Irvine, CA, USA) was used to provide OD measurements online. [0115] In preparation for the O2 transfer test, after filling a 50I Cellbag ™ with 25 I of simulated medium, the gas inlet port underwent an experiment with nitrogen (N2). The bag was balanced to facilitate the transfer of N2 in the simulation medium. The flow of N2 in the void was interrupted when the DO content of the simulation medium dropped below 10% saturation Petition 870180128492, of 10/09/2018, p. 44/79 33/45 of the air. Following this deoxygenation process, the bag was pressed to expel ο N2 residual empty space. Compressed gas was then added to the empty space of the bag, while reducing the disturbance of the liquid-gas interface. As soon as the bag was fully inflated, the O2 transfer test was started under the test conditions defined for the swing rate, swing angle and gas flow rate. The resulting increase in DO concentration was recorded and was used to determine 0 ki_a of the system. In addition, offline OD was measured every minute for the first five minutes, and every five minutes thereafter to check the accuracy of online O D readings. [0116] At a constant air flow rate, increasing the swing rate or swing angle increased by 0 kLa (Figure 2A), presumably by increasing the surface area for oxygen transfer. The kLa numbers we obtained at the lowest tested swing rate (20 rpm) are comparable to those that other researchers reported for WAVE Bioreactor ™ (Mikola et al., 2007; Singh, 1999). These kLa numbers are also comparable to those obtained for our domestic agitator tank bioreactor (data not shown). [0117] In an O2 transfer study of the WAVE Bioreactor ™ system at a constant swing rate of 20 rpm, increasing the air flow rate from 0.01 vvm to 0.05 vvm increased 0 kLa from ~ 2 Ir 1 to ~ 3 h 1 on the 2 I scale and increasing the air flow rate from 0.01 vvm to 0.1 vvm increased 0 kLa from ~ 0.5 h 1 to ~ 3 h 1 on the 20 I scale, ( Singh, 1999). On the other hand, in our study on the 50 I scale, increasing the air flow rate from 0 vvm to 0.02 vvm in two different swing rate and swing angle combinations, did not increase 0 kLa (Figure 2B) . The maximum airflow rates we use Petition 870180128492, of 10/09/2018, p. 45/79 34/45 may have been too low to affect liquid mobility at the gasHiquid interface to have any significant effect on ki_a. [0118] The oxygen transfer capacity of the 50 I disposable bag was assessed by determining the mass transfer coefficient, ki_a. Figure 2C shows the DO concentration over time for a constant gas flow rate and Figure 2D shows the effect of the gas flow rate on dissolved oxygen. For aggressive swing conditions (higher swing rate and swing angle) the mass transfer coefficient is high. Surprisingly, the clearance rate of empty space, however, has no effect on ki_a in relation to oxygen transfer. The simulated medium was deoxygenated before the experiment started. The oxygen concentration in the gas was higher than the oxygen concentration in the simulated medium. Then, the oxygen was transferred from the gas phase to the liquid phase. With aggressive balance conditions, the gas-liquid interface increases due to the fact of more waveforms (this is mentioned in the present order as having a dynamic interface). This increase in surface area appears to cause the high rate of oxygen transfer. When the gas flow rate is increased or decreased, the clearance rate of the empty space is accordingly changed. The change in empty space release does not change the differential oxygen concentration between the gas and the liquid phase. So, this gas flow rate appears to have no effect on the mass transfer coefficient for oxygen. When the oxygen concentration in the simulated medium is equal to that of the empty space, the oxygen transfer will stop. B. CO2 Transfer Studies [0119] After the simulated medium was deoxygenated by the method used for O2 transfer studies, CO2 was provided Petition 870180128492, of 10/09/2018, p. 46/79 35/45 to Cellbag ™ via the same gateway used to supply N2. The CO2 supply was interrupted when the online pH probe read 7.0 and the empty space was released using the same method described in the O2 transfer studies. When the bag was fully inflated, the CO2 transfer test was started under the test conditions defined for the swing rate, swing angle and gas flow rate. The resulting increase in pH was recorded with a disposable online pH probe connected to a pH20 transmitter supplied by the same manufacturer (GE Healthcare, Piscataway, NJ, USA). The pH increased because the CO2 was removed from the simulated bicarbonate medium. To check the accuracy of the pH readings online, the simulated medium was measured at the offline pH every minute for the first five minutes and thereafter every five minutes. Plotting online pH measurements against time, the slope of the best fit line provided the rate of change in pH and thereby indicated the rate of CO2 transfer from the simulated medium to the empty space in the Cellbag ™. [0120] Although other researchers have characterized the transfer of O2 in the WAVE Bioreactor ™ (Mikola et al., 2007; Singh, 1999), we have not found reports on the transfer of CO2 in cell culture systems with wave-induced agitation. To characterize the transfer of CO2 in the WAVE Bioreactor ™, we used simulated medium containing sodium bicarbonate in the same concentration (2.44 g / l) as in our cell culture medium. In this cell-free system buffered with bicarbonate, the removal of CO2 from the liquid phase would increase the pH of the system in the absence of active pH control. Instead of relying on CO2 probes for direct CO2 measurements in the simulated medium, the pH profile of an online pH probe in the WAVE Bioreactor ™ was used to assess the relative CO2 depletion rate. Petition 870180128492, of 10/09/2018, p. 47/79 36/45 [0121] In this study, the pH profile in the WAVE Bioreactor ™ separated into two phases (Figures 3A and 3B). In the first stage, the pH increased rapidly between 0 and 5 minutes at ~ 1 to 4 pH units per hour. In the second phase, the pH increased more gradually from 5 to 60 minutes at 0.5 pH units per hour. During this second phase (5 to 60 minutes), different swing rates and swing angles had a negligible impact on the rate of pH increase: at a constant air flow rate of 0.2 l / min, the pH increased at 0.2 units per hour, without considering the balance condition (Figure 3A). In contrast, higher air flow rates increased the rate of change of pH during this second phase (5 to 60 minutes): when the air flow rate increased from 0 l / min to 0.6 l / min, the rate pH variation increased from 0 to 0.1 units per hour to 0.4 units per hour (Figure 3B). In the absence of air flow (0 l / min), the minimum pH increase (<0.1 units per hour) observed during the second phase (5 to 60 minutes) suggests that the exchange of CO2 between the simulated medium and 0 empty space in Cellbag ™ approached equilibrium in approximately 5 minutes. In order to increase the additional 0 pH beyond the first 5 minutes, the driving force for CO2 emptying can be increased by increasing the air flow rate to increase the clearance rate of empty space and thereby minimize the CO2 concentration in empty space. [0122] Figure 3C shows the calculated rate of pH change for data in Figure 3A. Figure 3D shows the calculated rate of pH change for data in Figure 3B. The biphasic behavior can be explained by the high transfer rates of gas created both by the large surface area of the waves and by the continuous sweep of the empty space by the incoming gas. The large surface area facilitates the rapid transfer of CO2 from the liquid to the gas phase. The quick Petition 870180128492, of 10/09/2018, p. 48/79 37/45 transfer is a result of the differential concentration of CO2 between the gas and the liquid phase. This difference in concentration was at its maximum during the beginning of the experiment and this difference was continually reduced as more CO2 was transferred from the liquid phase to the gas phase. As the differential concentration of CO2 between the gas and the liquid phase was reduced, the rate of change in pH was also reduced. In Figure 3A, the rate of change in pH was very high for the first phase (0 to 5 minutes) compared to the second phase (5 to 60 minutes). The gas flow rate was kept the same for the cases shown in Figure 3A. After the initial CO2 transfer, the CO2 transfer rate depends on the concentration of CO2 in the void. For the same empty space clearance rate, the rate of change in pH after the initial 5 minutes was the same, regardless of balance conditions. The calculated value for the rate of change in pH is shown in Figure 3C. [0123] When the gas flow rate was changed, the clearance rate of the empty space was also changed. The data for increasing the pH for different gas flow rates is shown in Figure 3B. Biphasic behavior was also observed for these cases. However, between cases with the same gas flow rate and cases where the gas flow rate was varied, the difference is that the rate of change in the pH of the second phase (5 to 60 minutes) varied depending on the rate gas flow rate compared to similar for cases with the same gas flow rate. Since changing the gas flow rate changes the clearance rate of empty space, 0 CO2 in the empty space was removed at different rates. [0124] The rapid transfer of initial gas is the result of the property of the disposable bag to create a large surface area. This initial gas transfer depends mainly on the conditions of Petition 870180128492, of 10/09/2018, p. 49/79 38/45 swing (swing rate and swing angle). However, the sustained removal of CO2 from the medium depends on the concentration of CO2 in the void. The clearance rate of empty space depends on the gas flow rate. Example 2 Studies of Cell Growth Characteristics A. Batch cultivation 1. Initial Experiment Cell Culture Medium [0125] A serum free cell culture medium was used for culturing Chinese Hamster Ovary (CHO) cells. The cell culture medium was derived from a 1: 1 mixture of Ham-based DMEM and F-12 medium by modifying some of the components, such as amino acids, salts, sugars and vitamins. This medium lacks glycine, hypoxanthine and thymidine. This medium consisted of 15 mM HEPES (4- (2-hydroxyethyl) -1-piperazineethanesulfonic acid) and 2.44 g / l sodium bicarbonate. The concentration of these salts can be modified. The medium was supplemented with trace elements, recombinant human insulin and a cell protective agent, Lutrol F68 Prill (an equivalent can be used). Cultivation of Mammalian Cells [0126] Transfected Chinese Hamster Ovary (CHO) cells were cultured from a 1 ml flask or 10 ml bank stored in liquid nitrogen. The selected frozen flask was melted in a culture medium containing sodium bicarbonate, both in a rotating flask, in a shaking flask and in a bioreactor with stirring tank. The cells were passaged every 2 to 7 days. This culture was referred to as a “germinal series”. Germinal series cells were transferred to the disposable bag to initiate cell culture in the disposable bag. Petition 870180128492, of 10/09/2018, p. 50/79 39/45 Analysis [0127] A blood gas analyzer (NOVA BioProfile® 400) was used for offline analysis. The pH of the cell culture, partial pressure of dissolved oxygen and CO2, concentration of glucose, lactate and ammonia were measured using this off-line analyzer. Measurements of cell viability and viable cell concentration (VCC) were made using Beckman-Coulter’s ViCell ™ AS or ViCell ™ XR. In addition to cell concentration measurements, the amount of biomass was also measured by recording the percentage of the volume of packed cells (% of PCV). Example 3 Detailed Analysis Using Various CHO Cell Lines A. Batch Process [0128] By decreasing the concentration of CO2 in the gas supplied to Cellbag ™ over the course of batch cultivation, we should be able to decrease the initial high pH (> 7.3) and minimize the subsequent pH decrease in the WAVE Bioreactor ™ system. After testing different CO2 gas coating strategies in batch cultivation at WAVE Bioreactor ™ using several CHO cell lines (data not shown), we defined a staggered strategy “8- 5-2 ”for both the inoculation steps and for increased scale: The air pumped inside the Cellbag ™ was supplemented with 8% (v / v) CO2 gas for the first day, at 5% (v / v) for 0 second day and 2% (v / v) later. [0129] Based on the results of cell-free studies, we have selected the following swing rates, swing angle and air flow rate according to the process setpoints for our batch cultivation at WAVE Bioreactor ™: 21 rpm, 10 s of swing angle and Petition 870180128492, of 10/09/2018, p. 51/79 40/45 0.2 l / min for inoculation; 23 rpm, 10 s of swing angle and 0.2 l / min at increased scale step. To test the reliability of these process setpoints, we designed a complete factorial design (Table 1). When the process conditions deviated from the central points, we observed a negligible effect on cell growth and pCO2 profiles, and the pH of the culture remained within 6.8 to 7.2 and OD> 50% for both cell lines tested (Figure 4). Table 1 Conditions Tested in Batch Cultivation at WAVE Bioreactor ™ for Cell Lines that Produce MAb B and MAb C (Figure 4) [0130] The complete factorial design was designed around three process parameters - swing rate, swing angle and rate of air flow within the empty space - both for inoculation steps and for increased scale in batch cultivation. Inoculation Increased scale Symbol Swing rate (rpm) Swing angle ( s ) Air Flow Rate in Empty Space (l / min) Symbol Swing rate (rpm) Swing angle ( a ) Air Flow Rate in Empty Space (l / min) - -D · - 19 8 0.1 - -u- - 21 8 0.1 O 19 12 0.1 - -O- 21 12 0.1 - - 19 8 0.3 - - 21 8 0.3 - - 19 12 0.3 - - 21 12 0.3 r-1 23 8 0.1 r-1 25 8 0.1 23 12 0.125 12 0.1 23 8 0.325 8 0.3 ♦ 23 12 0.3 ♦ 25 12 0.321 10 0.223 10 0.2 B. Perfusion cultivation [0131] In our perfusion cultivation attempts at WAVE Bioreactor ™, the pH of the culture typically dropped below 6.8 and the OD dropped below 30% air saturation after the start of the infusion on day 6 (Figure 5). To minimize the pH drop without increasing the infusion rate, we investigated Petition 870180128492, of 10/09/2018, p. 52/79 41/45 the possibility of increasing the airflow rate in the Cellbag ™ because studies of cell-free gas transfer showed that the airflow rate increased the pH (Figure 3). To overcome the decline in DO, we supplemented the airflow in the Cellbag ™ with 30% O2 (v / v) two days after the start of the infusion. We selected this moment because it coincided with the OD decline observed previously (Figure 5). Example 4 A Batch Perfusion Process [0132] This perfusion process comprised two batch steps followed by an infusion step. A 50 I disposable pouch was inoculated with a 6 I working volume at a target cell density of 5 to 7.5 x 10 5 cells / ml in the inoculation step. Three days after inoculation, fresh medium was added to increase the volume of the disposable pouch to 20 l for the scaling up step. The inoculation stage and the scale increase stage constituted the batch stages. The CO2 drop strategy for the batching steps was employed as described in the Batching Process. At the end of the 3 days of the scale-up step, the perfusion was started. The fresh medium was continuously added to the disposable bag and the used culture medium was continuously removed from the disposable bag, while retaining the cells. The cell culture medium was perfused at a rate of 20 liters per day (1 volume per day). The pH set point of the perfusion medium was 7.2 units. At the beginning of the infusion, the CO2 concentration in the incoming gas was set to zero. The clearance rate of the empty space has been increased to facilitate CO2 removal. The increase in the clearance rate of the empty space, either followed by a single step of increase or a multi-step of increase, is shown in Figure 7. The range of the swing rate was between 19 to 25 rpm. The swing angle range was between 8 to 12 degrees. The temperature was Petition 870180128492, of 10/09/2018, p. 53/79 42/45 maintained at 37 ° C. Oxygen was supplemented 48 hours after the start of the infusion to meet the oxygen demand of the cells. The oxygen concentration in the inlet gas was established at 30% within 48 hours after the start of the infusion. [0133] Figure 6 shows the performance of cell culture for the batch perfusion process (batch step (days 0 to 6) and perfusion step (days 6 to 14)) (Figure 6A). Figure 6B shows the% cell viability. Figure 7A shows the set points for empty space release rates for three different experiments. The set points of the empty space release rates for the perfusion stage followed different profiles (days 6 to 14): (1) two constant empty space release rates: 0.02 hvm (-A-) and 0, 1 hvm (♦); and (2) a step to increase the clearance rate of the empty space: 0.007 hvm to 0.013 hvm to 0.02 hvm (-). Both the single-step increase and the multi-step increase were studied. Figure 7B shows the dissolved CO2 concentration offline. Figure 6D shows cell growth in viable cell count (VCC). Legend for Figures 6 and 7: ♦,, ▲ show three different executions. As shown in Figure 6C, the pH could be maintained within a desired range by modulating CO2 by releasing the void. Example 5 Behavior of Six Cellular CHO Strains under Conditions “8-5-2” [0134] To test the reliability of this WAVE Bioreactor ™ process to support cell growth and maintain 0 pH and OD in the desired ranges, six strains of cells that cover the cell growth range and metabolic behaviors typically seen in our internal CHO cell lines. Petition 870180128492, of 10/09/2018, p. 54/79 43/45 [0135] With the conditions of the process optimized, all six cell lines grew with high viability throughout the entire batch and the stages of perfusion culture (Figure 8). In all cases, the pH remained within the desired range of 6.8 to 7.2, and the DO did not exceed 20% air saturation. Example 6 Comparison between the WAVE Bioreactor ™ Method “8-5-2” and the Cultures in a Bioreactor with Conventional Shaker Tank [0136] To compare the cultivation performance between the WAVE Bioreactor ™ process of the invention and the bioreactor process with controlled shaker tank pH and OD, we performed parallel cultures in both systems (Figure 9). The growth and viability profiles were similar between the two bioreactor systems: the growth rates in the WAVE Bioreactor ™ and in the bioreactor with agitator tank were similar in ~ 0.5 day -1 . Despite the lack of online feedback control for pH and DO in the WAVE Bioreactor ™ system, the pH and DO profiles did not differ significantly between the two cultivation bioreactors. [0137] The invention provides a process control method to maintain the culture pH in the range of 6.8 to 7.2, and OD> 20% air saturation in the WAVE Bioreactor ™ system - operated in both batch and batch mode perfusion - without relying on pH and DO feedback control. After identifying the challenges in culturing CHO cells in the WAVE Bioreactor ™ system without pH and OD control, we conducted cell-free studies to determine the effects of the swing rate, swing angle and gas flow rate on O2 transfer and CO2 in the WAVE Bioreactor ™ system. By adjusting these process parameters, together with the concentration of CO2 and O2 in the input gas, we maintained the pH and OD of the culture within our desired range for batch cultivation and perfusion of six cell lines of Petition 870180128492, of 10/09/2018, p. 55/79 44/45 Recombinant CHO. By eliminating the need for pH and DO probes, this process provides a simpler and more economical method for growing cells in the WAVE Bioreactor ™ system. It also provides an alternative method for culturing cells in case of a pH or OD probe failure in WAVE Bioreactors ™ equipped with these probes. [0138] It is also necessary to understand that the specific examples described in the present application are illustrative only and are not intended to limit the scope of the invention. The invention is limited only by the appended claims.
权利要求:
Claims (16) [1] Claims 1. METHOD FOR CULTIVATING BOTTLES OF EUCARIONTES CELLS, characterized by comprising: providing cell culture inoculant comprising eukaryotic cells in a culture liquid containing bicarbonate to a container; said container having walls that encapsulate said cell culture and an empty gas phase space above said cell culture, and wherein said container comprises a door that provides a gas inlet and outlet to and from said empty space; stirring said container; and supplying gas to said empty space through said port, in which said gas contains an amount of CO2, and in which said amount of CO2 in said gas is modulated over time to adjust the pH of said cell culture to maintain a pH predetermined cell culture between 6.8 and 7.2 without continuous pH monitoring, in which said CO2 is supplied in an amount of 8% (v / v) of said gas on day 1, in an amount of 5% (v / v) of said gas on day 2, and in an amount of 2% (v / v) of said gas subsequently. [2] 2. The method according to claim 1, characterized by said stirring is by rocking said container at a rate of 15 sheet at 30 rpm and a swing angle of 5 0 to 15 °. [3] 3. The method according to claim 2, characterized in that the rocking rate is between 19 and 25 rpm and 0 rocking angle is between 8 to 12 °. [4] 4. METHOD, according to claim 1, characterized in that the clearance rate of said gas is between 0.002 to 0.1 volume of free space per minute (hvm). Petition 870180128492, of 10/09/2018, p. 58/79 2/3 [5] 5. METHOD, according to claim 4, characterized in that the clearance rate of said gas is between 0.007 to 0.08 hvm. [6] 6. METHOD, according to claim 5, characterized in that the clearance rate of said gas is 0.007 to 0.02 hvm. [7] 7. METHOD, according to claim 1, characterized in that said eukaryotic cells are vertebrate cells. [8] 8. METHOD, according to claim 7, characterized in that said vertebrate cells are selected from the group consisting of frog cells, rabbit cells, rodent cells, sheep cells, goat cells, dog cells, cat cells, cow cells, horse cells, non-human primate cells and human cells. [9] 9. METHOD according to claim 1, characterized in that said container is a rigid reservoir. [10] 10. METHOD according to claim 1, characterized in that said container is a foldable reservoir. [11] 11. METHOD, according to claim 10, characterized in that said container is a disposable culture bag. [12] 12. METHOD, according to claim 1, characterized by additionally comprising the intermittent monitoring of the pH of the cell culture. [13] 13. METHOD, according to claim 1, characterized in that said gas is supplied to said void space so that the cell culture maintains a partial pressure of dissolved CO2 at a level of about 1 to 200 mmHg (0.13 to 26 , 66 kPa). [14] 14. METHOD, according to claim 13, characterized in that said gas is supplied to said void space so that the cell culture maintains a partial pressure of dissolved CO2 at a level of about 10 to 150 mmHg (1.33 to 19 , 99 kPa). Petition 870180128492, of 10/09/2018, p. 59/79 3/3 [15] 15. METHOD, according to claim 14, characterized in that said gas is supplied to said void space so that the cell culture maintains a partial pressure of dissolved CO2 at a level of about 20 to 120 mmHg (2.66 to 15 , 99 kPa). [16] 16. METHOD, according to claim 1, characterized in that said gas is supplied to said void space so that the cell culture maintains a partial pressure of dissolved CO2 at a level of about 20 to 80 mmHg (2.66 to 10 , 66 kPa).
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引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题 US3941662A|1971-06-09|1976-03-02|Max-Planck-Gesellschaft Zur Forderung Der Wissenschaften E.V.|Apparatus for culturing cells| JPS5538112B2|1975-09-13|1980-10-02| JPS60141286A|1983-12-28|1985-07-26|Ajinomoto Co Inc|Method and apparatus for culturing animal cell| US4680267A|1985-03-01|1987-07-14|New Brunswick Scientific Company, Inc.|Fermentor control system| DE3515753C2|1985-05-02|1987-03-05|Harry Prof. Dr. 4006 Erkrath De Rosin| JPH0310679A|1989-06-09|1991-01-18|Shimadzu Corp|Cell culture bag| EP0567738A3|1992-05-01|1995-09-06|American Cyanamid Co|Controlling perfusion rates in continuous bioreactor culture of animal cells| US6190913B1|1997-08-12|2001-02-20|Vijay Singh|Method for culturing cells using wave-induced agitation| US8026096B1|1998-10-08|2011-09-27|Protein Sciences Corporation|In vivo active erythropoietin produced in insect cells| US6544788B2|2001-02-15|2003-04-08|Vijay Singh|Disposable perfusion bioreactor for cell culture| KR101021203B1|2004-06-04|2011-03-11|크셀렉스, 인크.|Disposable bioreactor systems and methods| US7195394B2|2004-07-19|2007-03-27|Vijay Singh|Method for resonant wave mixing in closed containers| US20060196501A1|2005-03-02|2006-09-07|Hynetics Llc|Systems and methods for mixing and sparging solutions and/or suspensions| US7745209B2|2005-07-26|2010-06-29|Corning Incorporated|Multilayered cell culture apparatus| US9109193B2|2007-07-30|2015-08-18|Ge Healthcare Bio-Sciences Corp.|Continuous perfusion bioreactor system| US8215238B2|2007-10-10|2012-07-10|The Texas A&M University System|Guideway coupling system| CN102482633A|2009-07-06|2012-05-30|弗·哈夫曼-拉罗切有限公司|Method of culturing eukaryotic cells|NZ597334A|2006-09-13|2014-02-28|Abbott Lab|Cell culture improvements| US8911964B2|2006-09-13|2014-12-16|Abbvie Inc.|Fed-batch method of making human anti-TNF-alpha antibody| JP5808249B2|2008-10-20|2015-11-10|アッヴィ・インコーポレイテッド|Antibody isolation and purification using protein A affinity chromatography| KR101722423B1|2008-10-20|2017-04-18|애브비 인코포레이티드|Viral inactivation during purification of antibodies| CN102482633A|2009-07-06|2012-05-30|弗·哈夫曼-拉罗切有限公司|Method of culturing eukaryotic cells| JP5926747B2|2011-02-24|2016-05-25|ジーイー・ヘルスケア・バイオサイエンス・アクチボラグ|A bioreactor having a feed flow and a recovery flow through a filter assembly| US9376654B2|2011-03-03|2016-06-28|Meissner Filtration Products, Inc.|Biocontainer| US9062106B2|2011-04-27|2015-06-23|Abbvie Inc.|Methods for controlling the galactosylation profile of recombinantly-expressed proteins| CN202786257U|2011-08-31|2013-03-13|通用电气健康护理生物科学股份公司|Exhaust filtration device for bioreactor| CN104619827A|2011-12-09|2015-05-13|帕尔技术英国有限公司|Filtration apparatus for continuous perfusion| US9228166B2|2011-12-20|2016-01-05|Pall Corporation|Rockable biocontainer| EP2639294A1|2012-03-15|2013-09-18|CellProthera|Automaton and automated method for cell culture| WO2013158273A1|2012-04-20|2013-10-24|Abbvie Inc.|Methods to modulate c-terminal lysine variant distribution| US9334319B2|2012-04-20|2016-05-10|Abbvie Inc.|Low acidic species compositions| JP2013237644A|2012-05-16|2013-11-28|Mitsubishi Gas Chemical Co Inc|Cell activating carbonated water| US9249182B2|2012-05-24|2016-02-02|Abbvie, Inc.|Purification of antibodies using hydrophobic interaction chromatography| KR20150043523A|2012-09-02|2015-04-22|애브비 인코포레이티드|Methods to control protein heterogeneity| US9512214B2|2012-09-02|2016-12-06|Abbvie, Inc.|Methods to control protein heterogeneity| CN104870629A|2012-10-26|2015-08-26|麻省理工学院|Control of carbon dioxide levels and pH in small volume reactors| MX2015005285A|2012-10-26|2015-11-16|Massachusetts Inst Technology|Humidity control in chemical reactors.| CA2905010A1|2013-03-12|2014-09-18|Abbvie Inc.|Human antibodies that bind human tnf-alpha and methods of preparing the same| WO2014159579A1|2013-03-14|2014-10-02|Abbvie Inc.|MUTATED ANTI-TNFα ANTIBODIES AND METHODS OF THEIR USE| US9067990B2|2013-03-14|2015-06-30|Abbvie, Inc.|Protein purification using displacement chromatography| US9499614B2|2013-03-14|2016-11-22|Abbvie Inc.|Methods for modulating protein glycosylation profiles of recombinant protein therapeutics using monosaccharides and oligosaccharides| DK2970843T3|2013-03-15|2021-11-22|Genzyme Corp|HIGH DENSITY CELL BANK PROCEDURES| EP3036317A4|2013-08-23|2017-04-12|Massachusetts Institute of Technology|Small volume bioreactors with substantially constant working volumes and associated systems and methods| EP3052640A2|2013-10-04|2016-08-10|AbbVie Inc.|Use of metal ions for modulation of protein glycosylation profiles of recombinant proteins| US9181337B2|2013-10-18|2015-11-10|Abbvie, Inc.|Modulated lysine variant species compositions and methods for producing and using the same| US8946395B1|2013-10-18|2015-02-03|Abbvie Inc.|Purification of proteins using hydrophobic interaction chromatography| US9017687B1|2013-10-18|2015-04-28|Abbvie, Inc.|Low acidic species compositions and methods for producing and using the same using displacement chromatography| US9085618B2|2013-10-18|2015-07-21|Abbvie, Inc.|Low acidic species compositions and methods for producing and using the same| US20150139988A1|2013-11-15|2015-05-21|Abbvie, Inc.|Glycoengineered binding protein compositions| GB201416362D0|2014-07-25|2014-10-29|Ge Healthcare Bio Sciences Ab|Method and system for suspension culture| US10617070B2|2014-10-06|2020-04-14|Life Technologies Corporation|Methods and systems for culturing microbial and cellular seed cultures| US9944894B2|2015-01-16|2018-04-17|General Electric Company|Pluripotent stem cell expansion and passage using a rocking platform bioreactor| GB201509202D0|2015-05-28|2015-07-15|Ge Healthcare Bio Sciences Ab|Semi-static cell culture| CN105176815B|2015-10-20|2017-03-22|哈尔滨工业大学|Gas-liquid interface perfusion bioreactor for artificial skin tissue culture and preparation method and application method of gas-liquid interface perfusion bioreactor| CA2996468A1|2015-10-30|2017-05-04|F. Hoffmann-La Roche Ag|Identification of calibration deviations of ph-measuring devices| CN108699502A|2016-02-23|2018-10-23|康宁股份有限公司|Bioreactor and its method for carrying out successive cell culture is perfused| CN105802851B|2016-03-25|2018-06-19|苏州诺普再生医学有限公司|A kind of dynamic tilt curled curved surface of 3D printing skin| CN105820948B|2016-03-31|2018-06-01|上海高机生物工程有限公司|A kind of swing platform for biological respinse bag| EP3484993B1|2016-07-12|2020-10-07|Global Life Sciences Solutions USA LLC|Microfluidic device for cell culture monitoring| GB2569000B|2016-07-12|2021-05-19|Emulate Inc|Removing bubbles in a microfluidic device| CA3035829A1|2016-09-12|2018-03-15|Juno Therapeutics, Inc.|Perfusion bioreactor bag assemblies| JP2019526288A|2016-09-14|2019-09-19|ブイビーシー ホールディングス エルエルシー|System, apparatus, and method for optimizing cell growth by controlling cell culture operations| CN110139923A|2016-12-29|2019-08-16|通用电气公司|The fault recovery of biological reactor for cell culture| KR101895195B1|2017-03-17|2018-09-05|인제대학교 산학협력단|Bioreactor for ex vivo expansion of cells| US11193103B2|2017-10-16|2021-12-07|Regeneran Pharmaceuticals, Inc.|Perfusion bioreactor and related methods of use| WO2021069287A1|2019-10-11|2021-04-15|Cytiva Sweden Ab|Bioreactor apparatus and operation method thereof|
法律状态:
2017-12-12| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]| 2018-06-12| B07A| Technical examination (opinion): publication of technical examination (opinion) [chapter 7.1 patent gazette]| 2019-05-07| B09A| Decision: intention to grant [chapter 9.1 patent gazette]| 2019-05-21| B09X| Decision of grant: republication| 2019-07-09| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 06/07/2010, OBSERVADAS AS CONDICOES LEGAIS. (CO) 20 (VINTE) ANOS CONTADOS A PARTIR DE 06/07/2010, OBSERVADAS AS CONDICOES LEGAIS |
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