WO2024163861A2 - Procédé d'électroporation multisystème - Google Patents

Procédé d'électroporation multisystème Download PDF

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Publication number
WO2024163861A2
WO2024163861A2 PCT/US2024/014193 US2024014193W WO2024163861A2 WO 2024163861 A2 WO2024163861 A2 WO 2024163861A2 US 2024014193 W US2024014193 W US 2024014193W WO 2024163861 A2 WO2024163861 A2 WO 2024163861A2
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Prior art keywords
electroporation
bag
cells
cell
semi
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WO2024163861A3 (fr
Inventor
Joseph Dizon ABAD
Jeraldine Casino MENDOZA
Matthew Rachmat HIDAJAT
Yuqi Wu ZHU
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Maxcyte Inc
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Maxcyte Inc
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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M35/00—Means for application of stress for stimulating the growth of microorganisms or the generation of fermentation or metabolic products; Means for electroporation or cell fusion
    • C12M35/02—Electrical or electromagnetic means, e.g. for electroporation or for cell fusion
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • C12M23/14—Bags

Definitions

  • the present disclosure relates generally to a system for electroporating large volumes of cells simultaneously using multiple electroporation systems simultaneously.
  • Electroporation is a well-known method of introducing compositions into Cells. Those of skill in the art are familiar with methods of electroporation. The electroporation may be, for example, flow electroporation or static electroporation. Methods and devices for electroporation are also described in, for example, published PCT Application Nos. WO 03/018751 and WO 2004/031353; U.S. patent application Ser. Nos. 10/781 ,440; 10/080,272; and 10/675,592; and U.S. Pat. Nos. 5,720,921 ;
  • the present disclosure provides a semi-closed system for electroporating cells, comprising, (a) an electroporation machine, (b) an electroporation processing assembly, (c) a cell resting bag; and (d) an electroporation buffer or cell media bag, wherein (a) to (d) are all connected together by silicone-plated tubing manifold.
  • a semi-closed system for electroporating cells comprising: (a) at least one scalable electroporation machine configured to enable up to 20 billion cell transfection runs for the production of recombinant proteins, antibodies, virus-like particles (VLPs), virus-replicon particles (VRPs), and toxic and apoptotic proteins; (b) a processing assembly; (c) a cell resting bag; and (d) at least one bag comprising therein at least one electroporation buffer, at least one cell media, or combinations thereof, wherein (a) to (d) are all connected together by silicon-plated tubing manifold.
  • VLPs virus-like particles
  • VRPs virus-replicon particles
  • a semi-closed system for electroporating cells comprising: (a) an electroporation machine, configured to enable up to 200 billion cell transfection runs for the production of recombinant proteins, antibodies, virus-like particles (VLPs), virus-replicon particles (VRPs), and toxic and apoptotic proteins; (b) a processing assembly configured to work with the electroporation machine in (a); (c) a cell resting bag; and (d) at least one bag comprising therein at least one electroporation buffer, at least one cell media, or combinations thereof, wherein (a) to (d) are all connected together by silicon-plated tubing manifold.
  • VLPs virus-like particles
  • VRPs virus-replicon particles
  • the system and methods disclosed herein can enable up to 200 billion cell transfection runs for the production of biological products such as, but not limited to, recombinant proteins, antibodies, viruslike particles (VLPs), virus-replicon particles (VRPs), and toxic and apoptotic proteins.
  • biological products such as, but not limited to, recombinant proteins, antibodies, viruslike particles (VLPs), virus-replicon particles (VRPs), and toxic and apoptotic proteins.
  • FIG. 1 is an embodiment of a tube used to connect the electroporation processing units to the manifold.
  • FIG. 2 is an embodiment of the MaxCyte CL2 processing assembly.
  • FIG. 3 Is an embodiment of the complete multi-system (MaxCyte ExPERT STx/Gtx) using CL-2 processing assemblies connected by a manifold.
  • FIG. 4 Is an embodiment of the complete MaxCyte R1-L processing assembly using multiple MaxCyte ExPERT VLx electroporation systems.
  • FIG. 5 is an embodiment of the tubing assembly sets that may be used with the invention.
  • FIG. 6 is an alternative embodiment of the tubing assembly that may be used with the invention.
  • FIG. 7 is an embodiment of 3 MaxCyte ExPERT STx/GTx electroporation devices in parallel with 3 processing assemblies connected to a tubing set.
  • FIG. 8 is an embodiment of 3 MaxCyte ExPERT VLx electroporation devices in parallel with 3 R-1 L processing assemblies connected to a tubing set.
  • FIG. 9 is a graph showing viable cell density numbers using the claimed method as detailed in example 2 on a 50 liter and 10 liter bioreactor.
  • FIG. 10 is a graph showing cell viability numbers using the claimed method as detailed in example 2 on a 50 liter and 10-liter bioreactor.
  • FIG. 11 is a graph showing the glutamine concentration level of the bioreactors used in example 2.
  • FIG. 12 is a graph showing the glucose concentration level of the bioreactors used in example 2.
  • FIG. 13 is a graph showing the lactate concentration level of the bioreactors used in example 2.
  • FIG. 14 is a graph showing the ammonia (NH4+) concentration level of the bioreactors used in example 2.
  • FIG. 15 is a graph showing the titer concentration level of the bioreactors used in example 2.
  • FIG. 16 is a collection of graphs analyzing glycan profiles of the bioreactors used in example 2.
  • FIG. 17 and FIG.18 are a collection of graphs analyzing the change variant of the bioreactor used in example 2.
  • FIG. 19 and FIG.20 are a collection of graphs analyzing the size exclusion chromatography (SEC) of the bioreactor used in example 2.
  • FIG. 21 and FIG. 22 are a collection of graphs analyzing the change variant of the bioreactor used in example 2.
  • One embodiment of the present invention is a semi-closed system for electroporating cells, comprising, (a) an electroporation machine, (b) an electroporation processing assembly (c) a cell resting bag; and (d) an electroporation buffer or cell media ban, wherein (a) to (d) are all connected together by silicone-plated tubing manifold and allows for the transfection of up to 200 billion cells per electroporation machine.
  • an electroporation machine comprising, (a) an electroporation machine, (b) an electroporation processing assembly (c) a cell resting bag; and (d) an electroporation buffer or cell media ban, wherein (a) to (d) are all connected together by silicone-plated tubing manifold and allows for the transfection of up to 200 billion cells per electroporation machine.
  • Those skilled in the art understand that a wide range of biological products can be grown and harvested using the claimed system and method, such as antibodies and proteins.
  • the term “semi-closed system” refers to a system in which the seed train expansion step is an open step but the seed train bioreactor, cell concentration buffer exchange, electroporation, cell resting, and bioreactor production steps are closed.
  • the disclosed system and method can be used on a wide range of cell types, including but not limited to primary cells, CHO cells, mammalian cell lines, insect cell lines, iPS cells, and other stem cells.
  • processing assembly refers to the MaxCyte products that are used on the MaxCyte STx/GTx and VLx systems.
  • the processing assembly for CL-2 and R-1 L processing assemblies comes with sample and collection bags and the process assembly housing that is inserted into the system. Cells that are mixed with the plasmid DNA of choice in an electroporation buffer and loaded into the sample bag, processed in the housing containing electrodes that deliver an electronic pulse, and then collected into the collection bag.
  • air refers to compressed air that is of standard atmospheric makeup.
  • cell resting vessel refers to any vessel used to rest the cells directly after electroporation.
  • suitable cell resting vessels include, but are not limited to, a 22L Meissner biocontainer, a 50L biocontainer, and a 5L multi-port Thomson Optimum Growth® shake flask.
  • the disclosed system is designed to be compatible with at least one scalable electroporation machine configured to enable up to 20 billion cells to be transfected for the production of recombinant proteins, antibodies, virus-like particles (VLPs), virus-replicon particles (VRPs), and toxic and apoptotic proteins.
  • VLPs virus-like particles
  • VRPs virus-replicon particles
  • the scalable electroporation machines described herein are sold by MaxCyte under the tradename “ExPERT STx”, or “ExPERT GTX”, electroporation systems.
  • the present invention is also designed to be compatible with at least one large scale electroporation machine used for protein production in any desired cell type, including CHO and Vero.
  • These large-scale electroporation machines are configured to enable up to 200 billion cells to be transfected for the production of recombinant proteins, antibodies, virus-like particles (VLPs), virus-replicon particles (VRPs), and toxic and apoptotic proteins.
  • the very large scale electroporation machine described herein is sold by MaxCyte under the tradename “ExPERT VLx”.
  • a MaxCyte ExPERT STx, GTx, or VLx electroporation system is used for the electroporation step.
  • the claimed method and individual components can be used with any electroporation platform.
  • each electroporation system uses a unique assembly.
  • a CL-2 processing assembly is configured for an ExPERT STx or GTx
  • an R-1 L processing assembly is configured for the ExPERT VLx. It is understood that any assembly can be used if it is compatible with the selected electroporation platform.
  • the MaxCyte CL-2 and R-1 L processing assemblies allow for a direct cell resting step into a cell culture vessel post-electroporation, without the use of a syringe or the need to bring the electroporated cell into a biosafety cabinet to transfer the cells to a resting bag.
  • the processing assembly is a solution for the aseptic integration of the CL-2 harvest bag to an appropriate cell culture vessel for the cell resting step.
  • the CL-2 connection assembly reduces contamination risk and human error during the cell resting step and could be configured in several ways, allowing process flexibility without the use of a biowelder.
  • the CL-2 connection assembly is configured for the ExPERT GTX or STx by attaching a CL-2 processing assembly and sample bag to the tubing manifold.
  • the sample bag holds the cell before electroporation and the collection bag collects the cells after they undergo electroporation.
  • the collection bag is further connected to a male lure lock with 1/4 inch ID (internal diameter), the male lure lock is attached to thermoplastic elastomer tubing or a silicon-plated tube with 1/4 inch ID.
  • a clamp can be placed on the silicon-plated tube to control the flowthrough rate.
  • the silicon-plated tube can be connected to a wide range of third-party sterile connectors for downstream vessel integration including but not limited to, a Male Kleenpack sterile connector, a CPC AseptiQuick S Connector, a male quick disconnect, or a male lure lock.
  • Multiple CL-2s can be placed on multiple electroporation systems so that a large volume of cells can undergo electroporation at the same time with all the electroporated cells from each machine ending up in the same resting vessel.
  • Each individual system can be connected to a single cell resting bag through a tubing manifold further attached to a cell media bag used to recover cells stuck in the manifold during cell resting.
  • a R-1 L processing assembly is configured for electroporation using an ExPERT VLx electroporation system. Unlike the CL-2 processing assembly, the R-1 L assembly is configured by connecting the collection line directly to the manifold instead of connecting it to a collection bag.
  • the collection bag of the CL-2 is connected directly to the tubing manifold.
  • cells undergo a seed train expansion train to reach the desired number of cells.
  • the media used to help grow the cells and maintain cell viability is any commercially available media that is chemically defined and animal- origin-free.
  • the cell passaging schedule to scale up the cells prior to electroporation for all cell types is as follows:
  • the flask that contains the cells during each cell passage is incubated with a vent cap in a shaking incubator at 37°C with 130 rpm, 5% CO2, and 80% relative humidity for up to 3 days.
  • multiple stirred bioreactors can be set up and inoculated simultaneously to reach the desired number of cells.
  • the cell culture from the bioreactor(s) is transferred to multiple 20L, 2D bags through gravity flow via biowelding, KleenPakTM, or CPC AseptiQuick® S Connector sterile connectors.
  • multiple ExPERT STx or GTx electroporation instruments can be assembled to electroporate a large volume of cells at the same time by preparing a multi-CL-2 electroporation tubing manifold with the appropriate amount of branches to support the number of CL-2 processing assemblies needed.
  • the manifold refers to the part of the system that connects the electroporation processing assembly to the cell resting bag. At one end of the manifold there is a 50L cell resting vessel inflated with 1 :1 air:C>2 gas for cell resting and the other end will be connected to a bag containing electroporation (EP) buffer or medium to wash the manifold lines after electroporation.
  • EP electroporation
  • the CL-2 connection assembly can be attached to the female lure lock of the collection bag.
  • a gas line can be connected to the inlet gas line of the 50-L cell resting vessel with 1 :1 air/O2 gas at 0.3 standard liters per minute (SLPM) flow for cell resting.
  • SLPM standard liters per minute
  • the manifold lines can be washed with the EP buffer or media connected to the end of the manifold to recover additional cells to the 50L cell resting vessel.
  • multiple ExPERT VLx electroporation instruments are used to electroporate a large volume of cells at the same time using multiple R-1 L processing assemblies.
  • VLx machines To do so, one can place the appropriate amount of VLx machines next to each other and prepare a multi-R-1 L EP tubing manifold with the appropriate amount of branches to support the number of R-1 L processing assemblies needed.
  • One end of the manifold will be connected to a 50L cell resting vessel inflated with 50:50 air: O2 gas for cell resting and the other end will be connected to a bag containing EP buffer or medium to wash the manifold lines after electroporation.
  • sterile To an inflated 50L cell resting vessel, sterile connect one end of a multi-EP tubing manifold and connect a bag of EP buffer or media to the other end. Connect a gas line to the inlet gas line of the 50-L cell resting vessel with 1 : 1 Air/02 gas at 0.3 SLPM flow for cell resting.
  • a gas line to the inlet gas line of the 50-L cell resting vessel with 1 : 1 Air/02 gas at 0.3 SLPM flow for cell resting.
  • the rested cells are placed into a production bioreactor to produce the desired target, such as, but not limited to, a protein or antibody.
  • Example 1 Electroporation of CHO cells using multiple STx/GTx and VLx systems in parallel
  • a vial of CHOZN cells was thawed and maintained in EX-CELL Advanced CHO Fed-batch Medium supplemented with 12mM L-glutamine and an additional 4g/L glucose. The cells were incubated at 37°C, 5% CO2, with 80% humidity. Working volume and agitation speed varied based on vessel size (see Table 1 below). Cells were passaged every 2 to 3 days at an initial cell density of 3e5 cells/mL and viabilities >98%. The cells were scaled up in volume as needed.
  • a 50L bioreactor (BioBLU® 50c Single-Use Bioreactor, macrosparger, 1 pitched-blade impeller, optical pH) was used as a seed train bioreactor to grow a large number of cells for electroporation.
  • the bioreactor was batched 1 day prior to inoculation with 18L of EX-CELL® Advanced CHO Fed-batch Medium supplemented with 12mM L-glutamine and an additional 4g/L glucose After the parameters were stable, the bioreactor was inoculated with CHOZN cells at a seeding density of 5x105 cells/mL and final volume of 20L. The cells were cultivated in the seed train bioreactor for 3 days.
  • plasmids (light chain, heavy chain, and EBNA) were mixed together with equal weight of light chain and heavy chain plasmids for a total of 95% of the total target weight of plasmid DNA.
  • the EBNA plasmid was added to the mix in the amount of 10% of the total target weight of plasmid DNA.
  • the plasmid mix was then added to the concentrated cells prior to electroporation.
  • the CL-2 processing assemblies were set up using the prompts from the on-screen or computer systems.
  • the cells were electroporated using the CHO EP protocol.
  • the electroporated cells were allowed to flow into the tubing manifold and collect in the 5L Thomson shake flask. Once the electroporation was completed for all CL-2 processing assemblies, the cells were rested for 30 minutes at room temperature.
  • the set up of 3 ExPERT STx/GTx systems in parallel with 3 CL-2 processing assemblies connected to the Multi GTx tubing set is shown in FIG. 7.
  • the calculated amount of DNA was added to each of the 3 R-1 L sample bags filled with a volume of 220 mL of concentrated cells in the biosafety cabinet (final volume ⁇ 250mL). Plasmid DNA mixture was added to the R-1 L sample bags and thoroughly mixed. The sample bags were taken out from the biosafety cabinet and were then connected via CPC AseptiQuik connector to the sample line of the R-1 L. The collection lines of the R-1 L processing assemblies were connected to a multi VLx tubing set by using Biowelder. The upstream line was biowelded to a bag with medium and the downstream line was biowelded to a 22L bioprocess container filled with 1 :1 air:O2 for cell resting post electroporation.
  • the R-1 L processing assemblies were set up using the prompts from the on-screen systems.
  • the cells were electroporated.
  • the electroporated cells were allowed to flow into the tubing manifold and were collected in the 22L bioprocess container.
  • the cells were rested for 30 minutes at room temperature with 0.1 SLPM of 1 :1 air:O2 flowing into the bag.
  • the set up of 3 VLx systems in parallel with 3 R-1 L processing assemblies connected to the Multi VLx tubing set is shown in FIG. 8.
  • a 10L bioreactor (BioBLU® 10c Single-Use Bioreactor, macrosparger, 1 pitched-blade impeller, optical pH) was used as a production bioreactor.
  • the bioreactor was batched 1 day prior to inoculation with EX-CELL® Advanced CHO Fed-batch medium supplemented with 12mM L-glutamine, an additional 4g/L glucose, and 30mL per liter of 20% Kolliphor® P188 as production media.
  • the bioreactor was inoculated with the electroporated cells from the 5L shake flask to a density of 6.7x10 6 cells/mL and viability of 97.5%.
  • the pH was maintained at 7.0 with a dead band of +/-0.2, and the dissolved oxygen (DO) setpoint was 30%.
  • DO dissolved oxygen
  • the temperature was shifted from 37°C to 32°C, and sodium butyrate was supplemented to a final concentration of 2mM.
  • feeding of EX-CELL® Advanced CHO Feed 1 from day 1 to the end of the process (day 12) is detailed in Table 2 below.
  • Samples were taken daily for cell count and nutrient and metabolite concentration. Glutamine and glucose were supplemented to maintain a concentration above 4mM and 2g/L, respectively. Samples for titer were taken starting on day 3. Samples for product quality were taken on day 9. Production was ended on day 12 when viability dropped below 50%.
  • a 50L bioreactor (BioBLU® 50c Single-Use Bioreactor, macrosparger, 1 pitched-blade impeller, optical pH) was used as a production bioreactor. The bioreactor was batched 1 day prior to inoculation. The bioreactor was inoculated with the electroporated cells from the 5L Thomson shake flask to a density of 6.4x10 6 cells/mL and viability of 98.3%.
  • the bioreactor was batched 1 day prior to inoculation with EX-CELL® Advanced CHO Fed-batch medium supplemented with 12mM L-glutamine, an additional 4g/L glucose and 30mL per liter of 20% Kolliphor® P188 as production media.
  • the bioreactor was inoculated with the electroporated cells from the 5L Thomson shake flask to a density of 6.7x10 6 cells/mL and viability of 97.5%.
  • the pH was maintained at 7.0 with a dead band of +/-0.2, and the DO setpoint was 30%.
  • the temperature was shifted from 37°C to 32°C, and sodium butyrate was supplemented to a final concentration of 2mM.
  • feeding of EX-CELL® Advanced CHO Feed 1 from day 1 to the end of process (day 15) is detailed in Table 3 below.
  • FIG. 9 and viabilities FIG. 10 were measured daily using a ViCell Blu automated cell counter. The bioreactors were inoculated at ⁇ 6e6 cells/mL at high viabilities above 97% post transfection. The 50L bioreactor grew to a peak density of around 15x10 6 cells/mL. The 10L bioreactor grew to a peak density of around 11x10 5 cells/mL. Foaming issues in the 10L bioreactor on day 1 impacted cell growth. The trends for cell growth and viability were as expected based on historical data.
  • Nutrients and metabolites were measured daily using a Nova® Biomedical Flex2 Analyzer. Glutamine concentration FIG. 11 and glucose concentration FIG. 12 were monitored closely to ensure that concentrations remained above 4mM and 2g/L respectively. Lactate concentration FIG. 13 and ammonia concentration FIG. 14 were tracked to ensure that the buildup of cell culture byproducts was within tolerable process ranges.
  • Titer was measured using the Biolayer Interferometry method using a GatorBio instrument. Titer in the 50L and 10L bioreactors demonstrates that the cells were successfully electroporated and are producing the intended product FIG. 15.
  • FIG. 1 is an embodiment of tube 100 used to connect the electroporation processing units to the manifold.
  • the figure demonstrates that a male lure lock 101 is attached to the top of the tube which connects to either a collection bag or the output line of the electroporation processing unit.
  • Tube 102 is silicon plated with an internal diameter of 0.25 inches.
  • a clamp 103 is placed on the tube to control the flowthrough rate.
  • the bottom of the tube is attached to a CPC AseptiQuick® S Connector 104 which can be attached to the manifold.
  • FIG. 2 Is an embodiment of the CL2 processing assembly 200.
  • a CL2 electroporation processing unit 201 is connected to an airbag 202, a sample bag 203 to hold the cells before electroporation, and a collection bag 204 used to capture the cells immediately after electroporation.
  • the collection bag 205 can be connected to tube 206, which is also shown in FIG. 1 , through a male lure lock.
  • the bottom of the processing assembly is attached to CPC AsepticQuick S connector 207 which is used to connect the processing assembly to a tubing manifold.
  • the connector shown in 207 can be substituted for a male Kleenpack® sterile connector, a male disconnect, or a male lure lock shown in 208.
  • FIG. 3 Is an embodiment of the complete CL2 processing assembly 300 wherein the CL-2 processing assembly 301 , also shown in FIG. 2, is attached to multiple ExPERT GTX electroporation systems 302.
  • the figure demonstrates that the assembly 301 is installed onto the GTx 302 and further connected to the manifold line 304 by using CPC AsepticQuick® S connectors 303.
  • the manifold line 304 is attached to a cell media bag 303 and a cell resting bag 305.
  • FIG. 4 Is an embodiment of the complete R1-L processing assembly 400 using multiple ExPERT VLx electroporation systems 404.
  • the figure shows an R-1 L electroporation processing wherein an R-1 L electroporation processing unit 401 is attached to a sample bag 402 that holds the cell before electroporation and is further attached to the CPC AsepticQuick S Connector 403.
  • the R-1 L is attached to the manifold line 407 by connecting adjoining CPC AsepticQuick S Connectors 405.
  • the manifold line is further attached to a cell media bag 406 and a cell resting vessel 408.
  • FIG. 5 shows the tubing sets for Multi ExPERT STx/GTx systems that were created to connect to the collection lines of the CL-2 processing assembly.
  • 5(a) is the tubing line that connects the female lure lock on the CL-2 collection bag processing assembly.
  • 5(b) is the manifold tubing used to connect up to 3 CL-2 processing assemblies together.
  • 501 is the male lure that is connected to the CL-2 processing assembly
  • 502 is the silicon plated tubing with 1/8 inch internal diameter x 1/4 inch outer diameter
  • 503 is the filter part of the tube that is welded to 506 which is 1/8 inch internal diameter x 1/4 inch outer diameter.
  • 504 is the part of the tube that is welded to the media bag and is 1/4 inch internal diameter x 3/8 inch outer diameter
  • 506 demonstrates that the entire tube is made of silicone
  • 507 is that part of the tube that is welded to either a shake flask or cell resting vessel and is 1/4 inch internal diameter x 7/16 inch outer diameter.
  • FIG. 6 shows the tubing sets for multi ExPERT VLx electroporation systems that were created to connect to the collection lines of the R-1 L processing assembly.
  • 601 is the part of the tube that is welded to the media bag and 1/4 inch internal diameter x 3/8 inch outer diameter
  • 602 shows that the tube is made of silicone
  • 603 is that part of the tube assembled to the R-1 L processing assembly
  • 604 is the part of the tube that connects to the cell resting vessel and is 1/4 inch internal diameter x 7/16 inch outer diameter.
  • FIG. 7 is a drawing of the set up used in example 2 using 3 MaxCyte ExPERT STX/GTX systems in parallel with 3 CL-2 processing assemblies connected to the Multi GTx tubing set.
  • 701 is a depiction of a computer used to control the electroporation systems
  • 702 is a depiction of the three electroporation systems set up in parallel, each containing a processing assembly, 707, connected together by the tubing manifold 706, all placed on a flat surface or table, 705.
  • the system further depicts a cell resting bag, 704, and a cell loading bag, 703.
  • FIG. 8, 800 is a drawing of the set up used in example 2 using 3 MaxCyte
  • Multi VLx tubing set 801 depicts the three MaxCyte ExPERT VLx systems all set on a flat surface or table, 801 .
  • 802 depicts the sample bag used to load the cells into the system, and 806 depicts the R-1 L processing assembly connected together by the tubing manifold of 804.
  • 805 depicts the cell resting bag used to collect cells post electroporation.
  • FIG. 9 is a measure of viable cell densities over time in each of the bioreactors used in example 2.
  • the data were measured daily using a ViCell Blu automated cell counter.
  • the bioreactors were inoculated at ⁇ 6e6 cells/mL at high viabilities above 97% post transfection.
  • the 50L bioreactor grew to a peak density of ⁇ 15e6 cells/mL.
  • the 10L bioreactor grew to a peak density of ⁇ 11e5 cells/mL.
  • FIG 10. Is a measure of cell viability over time in each of the bioreactors used in example 2. The data were measured daily using a ViCell Blu automated cell counter and shows that the cell viability in each reactor was maintained above 40% from inoculation to harvest.
  • FIG. 11 is a graph showing the measurement of glutamine in both bioreactors used in example 1. The data was measured using Biomedical Flex2 Analyzer and shows that the glutamine concentrations were maintained above 4mM throughout the experiment in both bioreactors.
  • FIG. 12 is a graph showing the measurement of glutamine in both bioreactors used in example 1. The data was measured using Biomedical Flex2
  • FIG. 13 is a graph showing the measurement of lactate in both bioreactors used in example 1. The data was measured using a Biomedical Flex2 Analyzer and shows that the lactate concentrations were maintained below 4g/L throughout the experiment in both bioreactors.
  • FIG. 14 is a graph showing the measurement of ammonia (NH4+) in both bioreactors used in example 1. The data was measured using Biomedical Flex2 Analyzer and shows that the ammonia concentrations were kept below 9.2 g/L throughout the experiment in both bioreactors.
  • FIG. 15 is a graph showing titer concentrations in both bioreactors used in example 1. The data was measured using the BLI method using a GatorBio instrument. Titer in the 50L and 10L bioreactors demonstrates that the cells were successfully electroporated and are producing the intended product.
  • FIG. 16 is a collection of graphs comparing glycan profiles of the bioreactor used in example 1 in the “Experimental Data” box to control data in the “Historical Data” box.
  • the data shows the identification and quantitation of different glycoforms in the product.
  • Studies 8, 9, 10, and 11 in the “Historical Data” box are control studies showing the glycan profiles of a bioreactor from experiments running the same protocol as example 1 but on a single electroporation device. Comparing the experimental data to the control group, it is clear that there was no significant difference between the groups, demonstrating that the multisystem electroporation results in similar product quality.
  • FIG. 17 and FIG.18 are a collection of graphs analyzing the change variant of the bioreactor used in example 1.
  • Studies 8 and 10 were used as control groups and refer to experiments using the same protocol in example 1 on a single electroporation system. The data shows the heterogeneity of the charge variant forms which needs to be characterized and monitored as changes can potentially affect biological activity and safety. Comparing the experimental data to the control group, it is clear that there was no significant difference between the groups, demonstrating that the multisystem electroporation results in similar product quality.
  • FIG. 19 and FIG.20 are a collection of graphs analyzing the SEC of the bioreactor used in example 1 .
  • Studies 8, 9, 10, and 11 were used as control groups and refer to experiments using the same protocol in example 1 on a single electroporation system.
  • the data shows the distribution of aggregation in the monoclonal antibody/protein. Comparing the experimental data to the control group, it is clear that there was no significant difference between the groups, demonstrating that the multisystem electroporation results in similar product quality.
  • FIG. 21 and FIG. 22 are a collection of graphs analyzing the change variant of the bioreactor used in example 1. Studies 8, 9, 10, and 11 were used as control groups and refer to experiments using the same protocol in example 2 on a single electroporation system. Comparing the experimental data to the control group, it is clear that there was no significant difference between the groups, demonstrating that the multisystem electroporation results in similar product quality. [0089] Other embodiments of the invention will be apparent to those skilled in the art from consideration of the specification and practice of the invention disclosed herein. It is intended that the specification and examples be considered as exemplary only, with the true scope and spirit of the invention being indicated by the following claims.

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Abstract

La présente invention concerne de manière générale un système d'électroporation de grands volumes de cellules utilisant simultanément de multiples systèmes d'électroporation.
PCT/US2024/014193 2023-02-03 2024-02-02 Procédé d'électroporation multisystème Ceased WO2024163861A2 (fr)

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WO2026068956A1 (fr) * 2024-09-27 2026-04-02 St Andrews Pharmaceutical Technology Limited Procédé et/ou appareil de production d'un inoculum cellulaire destiné à être utilisé dans un processus de biofabrication ou de culture cellulaire

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Publication number Priority date Publication date Assignee Title
WO2026068956A1 (fr) * 2024-09-27 2026-04-02 St Andrews Pharmaceutical Technology Limited Procédé et/ou appareil de production d'un inoculum cellulaire destiné à être utilisé dans un processus de biofabrication ou de culture cellulaire

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