US20130260419A1 - Continuous processing methods for biological products - Google Patents

Continuous processing methods for biological products Download PDF

Info

Publication number
US20130260419A1
US20130260419A1 US13/991,604 US201113991604A US2013260419A1 US 20130260419 A1 US20130260419 A1 US 20130260419A1 US 201113991604 A US201113991604 A US 201113991604A US 2013260419 A1 US2013260419 A1 US 2013260419A1
Authority
US
United States
Prior art keywords
outlet
receptacle
inlet
channel
unit operation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US13/991,604
Other languages
English (en)
Inventor
Thomas C. Ransohoff
Marc A. T. Bisschops
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sartorius Stedim Chromatography Systems Ltd.
Original Assignee
TARPON BIOSYSTEMS Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by TARPON BIOSYSTEMS Inc filed Critical TARPON BIOSYSTEMS Inc
Priority to US13/991,604 priority Critical patent/US20130260419A1/en
Publication of US20130260419A1 publication Critical patent/US20130260419A1/en
Assigned to TARPON BIOSYSTEMS, INC. reassignment TARPON BIOSYSTEMS, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: RANSOHOFF, THOMAS C., BISSCHOPS, MARC A.T.
Assigned to TARPON BIOSYSTEMS, INC. reassignment TARPON BIOSYSTEMS, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: RANSOHOFF, THOMAS C., BISSCHOPS, MARC A.T.
Assigned to PALL CORPORATION reassignment PALL CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TARPON BIOSYSTEMS INC.
Assigned to SARTORIUS STEDIM CHROMATOGRAPHY SYSTEMS LTD. reassignment SARTORIUS STEDIM CHROMATOGRAPHY SYSTEMS LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: PALL CORPORATION
Abandoned legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P21/00—Preparation of peptides or proteins
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
    • B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
    • B01D15/1814—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns recycling of the fraction to be distributed
    • B01D15/1821—Simulated moving beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
    • B01D15/38—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving specific interaction not covered by one or more of groups B01D15/265 - B01D15/36
    • B01D15/3804—Affinity chromatography
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
    • C07K1/14—Extraction; Separation; Purification
    • C07K1/16—Extraction; Separation; Purification by chromatography
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
    • C07K1/14—Extraction; Separation; Purification
    • C07K1/36—Extraction; Separation; Purification by a combination of two or more processes of different types
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K16/00—Immunoglobulins [IGs], e.g. monoclonal or polyclonal antibodies
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/12—Apparatus for enzymology or microbiology with sterilisation, filtration or dialysis means
    • 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
    • C12M23/44—Multiple separable units; Modules
    • 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
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/10—Separation or concentration of fermentation products
    • 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
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/12—Purification
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12Q—MEASURING OR TESTING PROCESSES INVOLVING ENZYMES, NUCLEIC ACIDS OR MICROORGANISMS; COMPOSITIONS OR TEST PAPERS THEREFOR; PROCESSES OF PREPARING SUCH COMPOSITIONS; CONDITION-RESPONSIVE CONTROL IN MICROBIOLOGICAL OR ENZYMOLOGICAL PROCESSES
    • C12Q1/00—Measuring or testing processes involving enzymes, nucleic acids or microorganisms; Compositions therefor; Processes of preparing such compositions
    • C12Q1/02—Measuring or testing processes involving enzymes, nucleic acids or microorganisms; Compositions therefor; Processes of preparing such compositions involving viable microorganisms
    • C12Q1/24—Methods of sampling, or inoculating or spreading a sample; Methods of physically isolating an intact microorganisms
    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N30/00—Investigating or analysing materials by separation into components using adsorption, absorption or similar phenomena or using ion-exchange, e.g. chromatography or field flow fractionation
    • G01N30/02—Column chromatography

Definitions

  • the present invention is directed to the development of continuous processing technology for the production of biopharmaceutical and biological products, such as monoclonal antibodies and vaccines.
  • SMB or related continuous, counter-current chromatographic techniques are the purification of fructose from a mixture of glucose and fructose (which is used in the production of high fructose corn syrup); the recovery of sucrose and betaine from molasses; the purification of various carboxylic acids and amino acids; as well as the production of potassium nitrate for fertilizer.
  • biopharmaceutical industry where the final drug product is usually a large molecule (i.e., ⁇ 3 kD) and must undergo several steps aimed at purification and, ultimately, sterilization.
  • biopharmaceutical and biological products have been manufactured and purified at very modest scale, obviating the need for moving away from inherently inefficient batch processing techniques.
  • the commercial success of the first monoclonal antibody therapeutics coupled with the desire to implement fully disposable or single-use components in manufacturing processes, has driven increased interest in more efficient processing technologies.
  • Production of a biopharmaceutical typically begins with production of the proteinaceous product in a bioreactor, followed by many stages, or unit operations, each designed to separate the product from undesired components and impurities.
  • Continuous processing would permit significant reductions in the scale of equipment needed downstream from the bioreactor, and accordingly the need for novel methods of continuous processing for all phases of biopharmaceutical production is acute.
  • the present invention is related to the development of a novel continuous processing technology (CPT) for the purification of biopharmaceuticals and biological products for increasing manufacturing productivity and efficiency in the biopharmaceutical industry.
  • CPT continuous processing technology
  • a preferred element for the design of continuous processing systems is the utilization of multi-valve arrays, preferably in the form of an integrated valve cassette or manifold.
  • Such valve cassettes are illustrated by the BioSMBTM system, which integrates dozens of diaphragm-style valves into a single disposable block, resulting in an “integrated circuit” approach to fluid control in continuous chromatography applications. See, e.g., FIGS. 10A-10E .
  • the BioSMBTM system design enables sophisticated fluid control with a fully-disposable flowpath that meets the stringent performance and cleanability requirements of the biopharmaceutical industry.
  • FIG. 2 illustrates the multiple processing steps or unit operations of a CPT process of the present invention.
  • FIG. 2 illustrates the purification of a monoclonal antibody product, but it will be readily appreciated that the principles of continuous processing described herein can be applied to the purification of any biological product.
  • the present invention is directed to a process for the production of a biological product comprising:
  • the transferring step comprises directing the flow from the preceding unit operation to an intermediate storage vessel, wherein the vessel has a holding capacity equal to or less than half of the volume received from the preceding unit operation during processing of one entire lot.
  • the present invention is directed to a method for the manufacture of a biological product in a continuous process system comprising the steps of:
  • step (b) the removal of cells and cell debris in step (b) is carried out by a centrifugation process.
  • the first unit operation is a simulated moving bed affinity chromatography process.
  • the present invention is directed to a method for incubating a solution for a controlled period of time, the method comprising:
  • the present invention is directed to a method for incubating a biological product solution at desired solution conditions for a controlled period of time and within a desired tolerance time window, the method comprising:
  • the present invention is directed to an apparatus for connecting two or more unit operations of a manufacturing process for continuous processing, the apparatus comprising:
  • the surge receptacle further comprises a vent outlet communicating the inside of said receptacle with the ambient environment.
  • a filter may be interposed between said vent outlet and the ambient environment, and wherein the vent outlet further comprises a valve for opening and closing the outlet.
  • the surge receptacle outlet may be connected to a pump.
  • bypass channel of the apparatus is connected to a bypass collection receptacle having the capacity to hold the throughput of a unit operation connected to said valve manifold central channel inlet.
  • the present invention is directed to an apparatus for connecting two or more unit operations of a manufacturing process for continuous processing, the apparatus comprising:
  • bypass channel outlet of the apparatus is connected to a bypass collection receptacle having the capacity to hold the throughput of a unit operation connected to the valve manifold central channel inlet.
  • the present invention is directed to a continuous processing system comprising:
  • the at least one surge receptacle and/or the one or more incubation receptacles further comprises a vent outlet communicating the inside of the receptacle with the ambient environment.
  • a filter is interposed between the vent outlet and the ambient environment, and wherein the vent outlet further comprises a valve for opening and closing the outlet.
  • the connection between the surge receptacle outlet and the surge receptacle inlet channel of the valve manifold is equipped with a pump for regulating fluid flow along said connection.
  • bypass channel outlet is connected to a bypass collection receptacle having the capacity to hold the throughput of a unit operation connected to the valve manifold central channel inlet.
  • the plurality of valve modules of the apparatus for carrying out the first unit operation are integrated into a master valve manifold.
  • the one or more incubation receptacles is equipped with means for mixing the contents of the receptacle.
  • the means for mixing the contents of the receptacle may be a rocker table.
  • any of said receptacles may be a single-use receptacle.
  • a preferred element for the design of continuous processing systems is the utilization of multi-valve arrays, preferably in the form of an integrated valve cassette or manifold.
  • Such valve cassettes are illustrated by the BioSMBTM system, which integrates dozens of diaphragm-style valves into a single disposable block, resulting in an “integrated circuit” approach to fluid control in continuous chromatography applications. See, e.g., FIGS. 10A-10E .
  • the BioSMBTM system design enables sophisticated fluid control with a fully-disposable flowpath that meets the stringent performance and cleanability requirements of the biopharmaceutical industry.
  • FIG. 2 illustrates the multiple processing steps or unit operations of a CPT process of the present invention.
  • FIG. 2 illustrates the purification of a monoclonal antibody product, but it will be readily appreciated that the principles of continuous processing described herein can be applied to the purification of any biological product.
  • FIG. 1 is a schematic diagram illustrating the concept of continuous processing according to the invention as an interlinked cascade of processing steps or unit operations (UO).
  • FIG. 2A is a block flow diagram illustrating an example of an interlinked series of unit operations with the object of producing a purified monoclonal antibody product.
  • Continuous processing of an antibody from the production of a crude antibody-containing solution (conditioned medium) in a bioreactor ( 10 ) through several processing steps culminating in bulk storage of purified antibody product ( 18 ) is depicted.
  • FIG. 2B illustrates the compression of net processing time achieved by continuous operation of the unit operations illustrated in FIG. 2A .
  • the continuous processing methods permit the target biological product to be continuously moved through each of the successive processing steps as it begins to emerge from the previous operation.
  • FIG. 3 is a schematic diagram of a continuous processing system showing two additional features, namely, a surge receptacle ( 7 ) for regulating flow between unit operations and relieving back pressure, and an emergency collection receptacle ( 21 ) for providing a means for rescue of partially processed biological product in case of a system failure or upset.
  • a surge receptacle 7
  • an emergency collection receptacle 21
  • FIG. 4 is a schematic diagram of a continuous processing system according to the invention wherein the processing steps (UO) are integrated using multi-valve valve modules ( 33 , 34 , 35 ).
  • the surge receptacle ( 7 ) is connected to a separate valve module ( 30 ), making it an optional operation in the processing path.
  • FIG. 5 is a schematic diagram of an alternative continuous processing system according to the invention wherein flow to a surge receptacle ( 7 ) is not separately regulated by a separately controlled valve system. Instead, the throughput from the preceding unit operation ( 31 ) is either directed to the surge receptacle ( 7 ) or directed to the final unit operation ( 32 ) (bypassing the surge receptacle) using the valve system ( 33 ) of the preceeding unit operation.
  • FIG. 6 is a schematic diagram of an alternative continuous processing system according to the invention, which differs from the systems depicted in FIGS. 4 and 5 , in that a master valve manifold ( 40 ) regulates flow to and from a number (n) of unit operations (UO) ( 31 ), regulates flow direction to a number (n) of surge receptacles ( 7 ), regulates flow from preceeding unit operation(s) ( 31 ) or surge receptacle ( 7 ) to a downstream unit operation ( 32 ), and regulates emergency bypass to a collection receptacle ( 21 ), enabling the rescue of partially processed biological product.
  • UO unit operations
  • FIG. 7 is a schematic diagram of part of a continuous biological product manufacturing process showing four unit operations interconnected via multi-valve regulator modules ( 44 , 45 , 46 ).
  • a surge receptacle ( 7 ) is disposed as a separate unit operation between two processing steps, i.e., unit operations (UO) 42 and 43 .
  • Alternate valving directs flow between any two unit operations to an emergency cutoff receptacle ( 21 ) by directing flow along the bypass line ( 47 ).
  • FIG. 8 is a schematic diagram of part of a continuous biological product manufacturing process showing three unit operations (UO) interconnected in an alternate plan to that of FIG. 7 .
  • the intervening surge receptacle ( 7 ) between unit operation ( 42 ) and unit operation ( 43 ) is a permanent fixture through which the output of preceeding unit operation ( 42 ) must pass prior to transfer to the last unit operation ( 43 ) shown here.
  • the surge receptacle ( 7 ) of this scheme is thus not an optional operation.
  • FIG. 9 is a schematic diagram of part of a continuous biological product manufacturing process showing three unit operations (UO) interconnected in an alternate plan to that of FIG. 7 .
  • flow from one unit operation (UO) to the next is regulated by connection to identical multi-valve valve manifolds ( 44 ) having common inlets ( 48 ), e.g., for priming buffer, and common outlets ( 47 ) leading to a collection receptacle ( 21 ).
  • Each valve manifold has inlets and outlets to effect bypass of the throughput received from the previous unit operation (e.g., 41 ) to a surge receptacle ( 7 ) prior to transfer via pump ( 1 ) to the succeeding unit operation (e.g., 42 ).
  • Repetitive valve modules ( 44 ) may be supplanted by a unitary master valve manifold (not pictured) which would integrate all of the valving represented by valve modules ( 44 ) into a single manifold programmable to accommodate all of the desired transfer and bypass operations.
  • FIGS. 10A-10E is a schematic representation of the use of an integrated valve cassette to regulate operation of a continuous counter-current multi-column simulated moving bed chromatography process.
  • 10 A, 10 B, 10 C, 10 D, and 10 E represent sequential steps in a simulated moving bed chromatography process involving six columns.
  • FIG. 11 is a schematic diagram of a unit operation requiring a product solution to be incubated for a time before being passed to a succeeding unit operation.
  • An incubation unit operation may, for example, be used for protein refolding, for viral inactivation by incubation as lowered pH, or any other operation requiring the solution to be held at one stage for a predetermined incubation period before further processing.
  • the unit operation illustrated in FIG. 11 utilizes a series of holding/incubation receptacles ( 50 , 51 , 52 ) with flow to each receptacle regulated through a common valve manifold ( 40 ).
  • the receptacle may be equipped with means for keeping the contents thoroughly mixed, e.g., via mixing paddles (represented schematically by item 53 ), although any alternative mixing means (stirring bar, rocker table, shaker, etc.) may be used.
  • the notation [ ] n signifies that a sufficient array of valves, , is present in the valve manifold ( 40 ) to direct the flow introduced via the inlet ( 54 ) independently to any of the holding/incubation receptacles and independently from any of the receptacles to an outlet ( 55 ) from the unit operation.
  • flow to receptacle 52 is shown, and independent flow from receptacle 50 to outlet 54 is shown.
  • the dotted lines signify lines (flowpaths) that are not in use.
  • FIGS. 12 and 13 show alternative plans for series-connected holding/incubation receptacles ( 50 ), with flow regulated by the valve array, [ ] n , of a valve manifold ( 40 ).
  • the embodiment of FIG. 12 illustrates that flow between series-connected receptacles ( 50 ) is regulated by the valve manifold ( 40 ).
  • the embodiment of FIG. 13 illustrates a scheme wherein the flow through a series of three holding/incubation receptacles ( 50 ) occurs in succession, without the option for diverting flow to the outlet ( 55 ) before the throughput has passed through all three receptacles ( 50 ).
  • the present invention provides processes that can be adapted to the manufacture of a biological product which make at least two or more steps of the processing of the biological product continuous.
  • Continuous processing allows the manufacturer to conduct the manufacturing process using less material and relying on equipment of a reduced scaled compared to the equipment that would be required for batch operations.
  • Continuous processing reduces downtime in the overall manufacturing process and thus reduces cycle times from the beginning of a manufacturing run to production of bulk drug substance or packaging of the final product.
  • biological product refers to a product of interest created via biological processes or via the chemical or catalytic modification of an existing biological product.
  • Biological processes include cell culture, fermentation, metabolization, respiration, and the like.
  • Biological products are typically comprised of proteins.
  • Biological products of interest include, for example, antibodies, antibody fragments, proteins, hormones, vaccines, fragments of natural proteins (such as fragments of bacterial toxins used as vaccines, e.g., tetanus toxoid), fusion proteins or peptide conjugates (e.g., such as subunit vaccines), virus-like particles (VLPs) and the like.
  • biopharmaceutical refers to a biological product purified and formulated so as to be physiologically acceptable for use as a drug or therapeutic agent.
  • unit operation refers to a manufacturing process step designed to separate an undesired element from a product of interest or designed to ensure that a composition containing a product of interest is substantially free of an undesired component.
  • unit operations in the manufacture of a biopharmaceutical after creation may include, without limitation: primary recovery operations, such as centrifugation, microfiltration, depth filtration, etc., for clarification of the output from a cell culture bioreactor; capture chromatography, for example by affinity chromatography, size exclusion chromatography, ion exchange chromatography, hydrophobic interaction chromatography (HIC), immobilized metal affinity chromatography (IMAC), and the like; incubation at low pH (e.g., pH 3.0-3.5) or other solution conditions for achieving, e.g., inactivation of viruses, protein refolding, aggregate dissociation, and the like; micro- or nano-filtration, etc., for filtration of viruses, bacteria,
  • primary recovery operations such as centrifugation, microfiltration, depth filtration, etc
  • upstream or “upstream process” refers to the step(s) of biopharmaceutical manufacture relating to the creation of the active biological product by a biological process or other reaction.
  • the biological product to be isolated and processed into a biopharmaceutical is the result of a fermentation or is the expression product of a recombinantly transformed host cell.
  • the upstream portion of the manufacturing process typically relates to the production of a target protein (such as an antibody, an active protein or protein fragment, a fusion protein, virus-like particle, etc.) either in a prokaryotic or eukaryotic cell that naturally produces the (endogenous) target protein or, more commonly, in a prokaryotic or eukaryotic host cell which has been transformed by recombinant DNA technology to express an exogenous target protein or proteins.
  • a target protein such as an antibody, an active protein or protein fragment, a fusion protein, virus-like particle, etc.
  • a target protein such as an antibody, an active protein or protein fragment, a fusion protein, virus-like particle, etc.
  • a target protein such as an antibody, an active protein or protein fragment, a fusion protein, virus-like particle, etc.
  • downstream processing refers to the steps following “upstream” processing of a biological product that are required to separate the biological product from impurities and contaminants, typically resulting in production of a bulk drug substance. Downstream processing refers to some or all the steps necessary for capture of a biological product from the original solution in which it was created, for purification of the biological product away from undesired components and impurities, for filtration or deactivation of pathogens (e.g., viruses, endotoxins), and for formulation and packaging.
  • pathogens e.g., viruses, endotoxins
  • continuous process refers to any process having two or more processing steps in series, wherein the output from an upstream step (unit operation) is transferred to a downstream step (unit operation) and wherein it is not necessary for the upstream processing step to run to completion before the next processing step is started.
  • some portion of the target product is always moving through the processing system.
  • the flow through a continuous process is regulated so that, to the greatest extent possible, every step or unit operation of the continuous process is running at the same time and at substantially the same production rate. In this way, compression of the cycle time is maximized and the shortest possible completion time is achieved.
  • the expressions “continuous transfer” or “transferred continuously”, referring to a product stream moving from an upstream unit operation to a downstream unit operation, means that the connections or links between the two unit operations are such that the upstream unit operation transfers a product stream (directly or through other components) to the second (downstream) unit operation, and that the downstream unit operation begins before the upstream unit operation runs to completion (that is, the two successive unit operations are processing the product streams flowing into them simultaneously for at least part of the overall process run of which the two unit operations comprise a part).
  • CPT Continuous Processing Technology
  • the CPT processes described herein provide the means to handle the ton-scale output which is now possible by utilization of multiple disposable bioreactors.
  • manufacturers of a biological product can avoid the typical $500 million/5-year investment required to build a new facility capable of ton-scale biopharmaceutical production by conventional batch methods using large scale, stainless steel equipment.
  • Reduction in capital investment of up to 80% and compression of the time to scaled-up production capacity to approximately 2 years can be achieved based on the reduced scale of equipment required to operate continuous processes.
  • a company that is developing a new biological product faces the challenge of funding the scale-up and manufacture of the product from laboratory scale quantities to the much larger quantities necessary for preclinical experiments and clinical trials.
  • the requirements for GMP manufacturing of clinical supplies for use in human clinical testing translate to a significant cost for most early-stage programs, and delay or failure in achieving GMP standards can contribute to difficulty in financing or gaining approval to proceed with planned clinical studies.
  • the use of continuous processing, coupled with the use of disposable technologies such as described herein, has helped reduce capital outlays and has increased the speed for achieving clinical manufacturing. Construction of a disposables-based clinical manufacturing facility may cost as little as $15-20 million, as compared to a cost of $30-50 million for conventional clinical manufacturing facilities.
  • the CPT processes described herein can further reduce these costs and also speed up the clinical manufacturing process by shrinking the scale of equipment required to produce the needed quantities of product, and by making the entire manufacturing process more flexible and more portable.
  • the return profile for development of early-stage biopharmaceuticals will be improved for both large companies with in-house manufacturing capacity as well as for smaller companies who may outsource the manufacture of their products.
  • This improved return profile will enable more promising biological product candidates to enter clinical testing: larger companies will be able to move more product candidates into early-stage testing, expanding the number of drug candidates entering drug development pipelines; and small or start-up biopharmaceutical companies seeking to demonstrate proof-of-concept based on human clinical studies as a prerequisite to financing or partnering objectives will be more able to pass this hurdle.
  • disposables or single-use technologies
  • biopharmaceutical manufacturing processes constitutes an important shift away from standard reusable technologies.
  • the use of disposables technology is driven by industry-wide needs to reduce capital investment, to increase speed of development, and to reduce contamination due to re-use of production equipment.
  • Adoption of disposable technologies in small-scale, clinical manufacturing applications has been relatively rapid, owing to both the relative ease of implementation as well as to the significant benefits of capital and time savings.
  • the lack of availability of sufficiently large disposable purification equipment presents a “bottleneck” to implementation of larger-scale processes using disposable technology.
  • Continuous processing permits reduction in the scale of equipment necessary to process the currently large and increasing capacity of bioreactors (2,000 liters presently, moving to 5,000 liters and above).
  • Continuous processing allows downstream processing to proceed utilizing available equipment, including single-use (disposable) equipment; also, the flow-through capacity of CPT allows for productivities matching and significantly exceeding that of the largest bioreactors, enabling greater penetration of fully-disposable processes.
  • the switch from traditional batch processing to continuous processing fundamentally changes the way the biopharmaceutical industry develops and manufactures its products.
  • Configurations for continuous processing are disclosed herein which are specifically adapted to the use of disposable components.
  • disposable components will have lower tolerances or reduced capacity in comparison to permanent, reusable equipment, and several features for continuous processing have been designed so that the disposable components can be used and any differences in their properties accommodated by the system.
  • single-use plastic tubing may be used to replace stainless steel tubing, however the tolerance to systemic pressure drops from unit operation to unit operation is much lower for plastic tubing than for stainless steel tubing.
  • features such as surge receptacles useful to vent the system and return a given connection to atmospheric pressure are incorporated so that no tubing failures or loss of system performance results from the substitution of plastic tubing for stainless steel tubing.
  • Unit operations in the manufacturing process of a biological product can benefit from continuous multicolumn or multistage operation. This has been demonstrated for the capture chromatography step by conversion from a batch operation to continuous counter-current simulated moving bed (SMB) chromatography.
  • SMB simulated moving bed
  • the several steps of a capture chromatography operation such as Protein A capture of an IgG target using Protein A affinity chromatography, are performed serially: Clarified conditioned media from a bioreactor is applied to a capture chromatography column, followed by wash, elution, cleaning (regeneration), and equilibration steps, with each step being completed before the next step is begun.
  • a SMB multicolumn system In a SMB multicolumn system, multiple columns are employed and the multiple steps are run simultaneously on different columns Utilizing a continuous flow, multicolumn system permits the capacity of the columns to be reduced, thus allowing a large bioreactor volume to be processed using small diameter columns (instead of scaling up column size to accommodate the feed of a bioreactor by batch capture chromatography).
  • FIGS. 10A-10E The operation of such a SMB multicolumn system is illustrated in FIGS. 10A-10E .
  • a commercial SMB system (BioSMBTM system, Tarpon Biosystems, Inc., Worcester, Mass. (US)) has been developed which provides an integrated array of valves and connections (valve cassette) for coordinating flow of multiple solutions and buffers to a multiplicity of interconnected columns, enabling scalable, continuous chromatography operation using a wide range of separation media.
  • the BioSMBTM system is programmable and adjustable, and it is useful for converting virtually any single-column batch operation to a continuous multicolumn operation.
  • the BioSMBTM system also makes full use of disposable components by featuring replaceable tubing, columns, and valve membrane, all of which can be quickly disconnected from the system for installation of new components, thereby reducing or virtually eliminating system downtime.
  • valve cassette that acts as an integrated circuit for fluid handling, incorporating the many valves required to enable continuous processing into a single disposable-format valve array.
  • FIGS. 10A-10E where each of the square items 108 represents a valve.
  • An array of 54 valves ( 108 ) housed in a single valve cassette or manifold is thus depicted, although it will be appreciated the larger valve cassettes (or smaller, repetitive valve modules) can be employed.
  • the commercial BioSMBTM system valve manifold for instance, features 240 separately actuatable valves.
  • This valve cassette has proven to be a robust and cleanable device, suitable for meeting the stringent requirements of biopharmaceutical applications.
  • FIG. 1 depicts schematically the broadest aspect of continuous processing according to the present invention.
  • a cascade of process steps or unit operations (UO) are directly connected to each other in series.
  • An outlet of the first unit operation ( 3 ) is directly connected via line ( 2 ) to the inlet of the next unit operation ( 4 ), and the flowthrough from a second unit operation ( 4 ) proceeds from an outlet of that unit operation ( 4 ) to an inlet of a third unit operation ( 5 ).
  • This illustration shows three processing stages or unit operations ( 3 , 4 , 5 ), interconnected by a line (tubing or flowpath) ( 2 ), with product flow driven by a single pump ( 1 ).
  • each unit operation is connected in series to the next unit operation: the first unit operation ( 3 ) receives the output from a previous step, which may be a batch step, or the throughput of the pump ( 1 ); the throughput of the first unit operation ( 3 ) is directed to the inlet of the next unit operation ( 4 ), and the throughput that unit operation ( 4 ) is direct to the inlet of a third unit operation ( 5 ).
  • a previous step which may be a batch step, or the throughput of the pump ( 1 )
  • the throughput of the first unit operation ( 3 ) is directed to the inlet of the next unit operation ( 4 )
  • the throughput that unit operation ( 4 ) is direct to the inlet of a third unit operation ( 5 ).
  • each UO of the diagram may represent several processing steps, and it will also be appreciated that additional unit operations may be added to the series of unit operations until a complete process is assembled.
  • the throughput of one unit operation is connected to the input of the next unit operation so that the connected unit operations may run continuously, so that the desired product of interest moves from one unit operation to the next without the necessity of waiting for the one unit operation to be completed before introduction of product to the next unit operation for further processing is started.
  • the size of the bioreactor sets the initial volume of medium that will have to be processed in a biological product manufacturing process.
  • the mass of the product is the most significant factor, however in a continuous process the volume of medium to be processed determines the scale of all the downstream operations. Therefore the greater the titer of product, the greater are the advantages gained by adopting a continuous process.
  • 5 grams of product per liter (5 g/L) is considered a high titer for protein products such as monoclonal antibodies, although optimizing host cell production, media conditions, growth cycles, etc. has yielded titers of 10-13 g/L or higher.
  • continuous processing systems do not require constant flow from one unit operation to the next or constant flow through all of the interconnected unit operations. For any number of reasons, the rate of flow through a unit operation or between unit operations may need to be adjusted or halted.
  • Continuous processing only requires that the links between two unit operations are such that the first or upstream unit operation transfers a product stream (directly or through other components) to the second (downstream) unit operation, and that the downstream unit operation begins before the upstream unit operation runs to completion (that is, for at least part of the manufacturing run, the two successive unit operations are processing product simultaneously).
  • continuous processing does not require uniform or uninterrupted flow through all of a series of connect unit operations, it is preferable if the processing system can be operated so as to maintain as continuous a flow through the system as possible.
  • Features are described herein that allow a high degree of uninterrupted flow between unit operations of an overall continuous process to be achieved.
  • FIG. 2A is a block flow diagram of an exemplary manufacturing process for a biopharmaceutical.
  • the biopharmaceutical is a monoclonal antibody.
  • Each block of the diagram represents a unit operation, and the sequence of operations ( 10 - 18 ) shown represents a cascade of connected unit operations that are running continuously and to the greatest extent possible simultaneously, so that ideally no shutdown or interruption of the process occurs, and no unit operation needs to be delayed to wait for a previous operation to be completed (as in batch processes).
  • the sequence of specific unit operations depicted in FIG. 2A is typical and suitable for monoclonal antibody processing. It will be appreciated that different biological products will be manufactured according to a process comprising different unit operations, or similar unit operations performed in a different order.
  • the primary recovery may involve such unit operations as pelleting of the cells via centrifugation or ultrafiltration, lysing the cells, harvesting the inclusion bodies, dissociation of aggregates (e.g., with a chaotropic agent), and protein refolding, all occurring before a capture chromatography operation.
  • a capture chromatography unit operation will be tailored to the particular protein product and may involve a suitable affinity ligand other than Protein A (which selectively binds the constant fragment (Fc) of immunoglobulins) or may involve a different chromatography altogether (e.g., IMAC, HIC, ion exchange, and the like).
  • downstream processing of different products may suitably involve different steps and a different series of unit operations.
  • suitable processing stages for production of a desired biological product is within the capabilities of practitioners in this field; linking the processing stages (unit operations) so as to be capable of continuous processing of the biological product is the subject of the present invention.
  • the first block ( 10 ) represents a bioreactor in which a cell culture is produced, for example, by growing transformed host cells (e.g., yeast cells, Chinese Hamster Ovary cells, etc.) that express and preferably secrete the antibody into the cell culture medium.
  • transformed host cells e.g., yeast cells, Chinese Hamster Ovary cells, etc.
  • the conditioned medium containing the secreted biological product is usually clarified, e.g., by centrifugation and/or microfiltration or depth filtration, to remove cells and cell debris before being transferred to the next unit operation ( 11 ).
  • the next block ( 11 ) represents a capture chromatography step, which for immunoglobulins is advantageously performed using Protein A affinity chromatography.
  • the throughput of the Protein A chromatography step ( 11 ) is fed continuously to the next unit operation ( 12 ), which in this illustration is a viral inactivation step.
  • the next unit operation ( 12 ) which in this illustration is a viral inactivation step.
  • a viral inactivation step Because antibodies captured on Protein A media are commonly eluted using a low pH eluant (e.g., 100 mM glycine at pH 3.0-pH 3.5), low-pH viral inactivation is a logical unit operation to follow continuously from Protein A capture and elution.
  • the throughput from viral inactivation ( 12 ) is transferred continuously (after adjustment of the solution to suitable conditions (i.e., pH) for loading onto the next chromatography step) to the next unit operation ( 13 ), which in this illustration is cation exchange chromatography, designed to eliminate product-related impurities such as aggregates and degraded or improperly assembled antibodies.
  • Cation exchange is a logical unit operation at this stage for an antibody production process, but for other biological products another type of chromatography operation may be more effective. For example, hydrophobic interaction chromatography (HIC), ceramic hydroxyapatite (CHT), or other types of chromatography steps may be substituted at this stage for particular purposes.
  • HIC hydrophobic interaction chromatography
  • CHT ceramic hydroxyapatite
  • the throughput from the cation exchange chromatography step ( 13 ) is transferred continuously to the next unit operation ( 14 ), which in this illustration is an ultrafiltration/diafiltration step.
  • Ultrafiltration is designed to concentrate the antibody product by retention of the product on a tangential flow membrane, followed by diafiltration used for buffer exchange. Desired new buffer is added at the same rate as removal of water/buffer through the permeate, so the volume and concentration stay constant while buffer is being exchanged.
  • the throughput from the ultrafiltration/diafiltration step ( 14 ) is transferred continuously to the next unit operation ( 15 ), which in this illustration is anion exchange chromatography, designed to eliminate impurities having a net negative charge, such as DNA, endotoxin, viruses, and host cell proteins.
  • Antibodies usually have a relatively high isoelectric point, therefore conditions may be readily adjusted so that the antibody product has a net positive charge while the impurities exhibit a net negative charge (and thus antibody flows through the positively charged medium/membrane of an anion exchange column or membrane).
  • the throughput from the anion exchange chromatography step ( 15 ) is transferred continuously to the next unit operation ( 16 ), which in this illustration is a nanofiltration step, e.g., using a 20 nm-40 nm sterile membrane filter, designed for removal of viruses.
  • the throughput from the nanofiltration step ( 16 ) is transferred to the next unit operation ( 17 ), which in this illustration is an optional concentration/buffer exchange followed by microfiltration (0.2 ⁇ m filter), designed to put the purified monoclonal antibody into a solution for bulk storage ( 18 ).
  • the bulk purified antibody in a storage-stable formulation ( 18 ) is ready for transfer to a sterile fill operation that will perform further operations, such as additional formulation as necessary, sterilizing filtration, and filling the antibody into sterile vials, syringes or other containers for distribution as a biopharmaceutical product.
  • chromatography steps will advantageously be operated using a programmable multicolumn regulatory system, such as the aforementioned BioSMBTM system (Tarpon Biosystems, Inc., Worcester, Mass. (US)), which will enable continuous operation.
  • a programmable multicolumn regulatory system such as the aforementioned BioSMBTM system (Tarpon Biosystems, Inc., Worcester, Mass. (US)
  • a preferred system for the ultrafiltration/diafiltration steps is CadenceTM system (Pall Corp., Port Washington, N.Y. (US)).
  • An integrated valve cassette such as featured in the BioSMBTM system can also be adapted to regulate continuous operation of the final nanofiltration and microfiltration steps.
  • timecourse plots for each of the unit operations diagrammed in FIG. 2A are shown, and the feature that successive unit operations begin before the previous unit operation ends illustrates the advantages gained by continuous processing.
  • each of the timecourses would need to run to completion before a collected product could be transferred to the next batch step, and none of the timecourses would overlap.
  • Batch manufacturing on the scale illustrated would take up to four days or more to complete.
  • the continuous processing methods allow overlapping timecourses, with substantial periods of connected unit operations running simultaneously. When continuous processing is maximized, the four day batch manufacturing process is completed in about 24 hours.
  • a series of four unit operations is illustrated schematically.
  • the system illustrated is equipped with two additional features aiding continuous operation.
  • One feature is a surge receptacle ( 7 ) connected between two unit operations, so that the output of the second unit operation ( 4 ) is collected in receptacle ( 7 ).
  • the receptacle ( 7 ) is equipped with a sterilizing grade filter ( 8 ), e.g., a 0.2 micron filter, that is permeable to air but screens out microorganisms.
  • a sterilizing grade filter e.g., a 0.2 micron filter
  • the contents of the receptacle, at atmospheric pressure, can be fed via pump ( 1 ) to the next unit operation ( 5 ) at a lower pressure drop than would be necessary to overcome back pressure from flow maintained through downstream unit operations ( 5 ) and ( 6 ) in a closed system running without the surge receptacle ( 7 ).
  • suitable surge receptacles ( 7 ) and transmission lines (tubing, 2 ) will commonly be made out of less durable materials, such as plastic.
  • the receptacle ( 7 ) may be a plastic bag (surge bag) or a vented plastic bottle.
  • Such plastic materials and their connections between unit operations will have less resistance to back pressure build-up than, for instance, stainless steel containers and tubing; therefore, the use of surge receptacles to alleviate systemic pressure and lower the pressure drop necessary to maintain flow from one operation to the next is highly advantageous not only for regulating continuity of flow but for preserving the integrity of the system and avoiding material or connection failures.
  • the second feature aiding continuous flow through the entire system is the installation of a bypass collection receptacle ( 21 ), together with the transmission conduits ( 20 ) making it possible to divert the flow from any unit operation (UO) so that the partially processed product is not lost if transfer of the flow to the next intended unit operation is not possible, for example, due to a clog, a downstream contamination, a connection failure, determination of the need for continued incubation, or similar upset in the normal operation of the continuous process.
  • UO unit operation
  • Installation of a bypass collection receptacle ( 21 ) provides a means of rescuing a product that has undergone partial processing in one or more unit operations but that would be lost if the product flow were passed through a downstream stage that had become unsuitable for receiving the product due to contamination, blocked flow, leakage, unprepared downstream unit operations, etc.
  • the partially processed product captured in the bypass receptacle ( 21 ) can be introduced into the cascade of unit operations at the point it was diverted, thus avoiding the loss of yield and cost of reprocessing that would occur if the manufacturing process had to be stopped, reset and started over.
  • a separate return line (not shown) and a pump if necessary may be provided for return of a product solution collected in the bypass receptacle ( 21 ) to any point in the cascade of unit operations.
  • FIG. 4 illustrates a manufacturing process featuring a surge receptacle ( 7 ) and a bypass collection container ( 21 ) as in FIG. 3 , however in this figure the surge receptacle ( 7 ) is connected to the process through a valve module ( 34 ) providing sufficient valves and connections, represented by [ ] n , to direct the flow of upstream unit operations ( 31 ) either directly to the succeeding unit operation ( 32 ), via line ( 2 ), or alternatively to an intermediate surge receptacle ( 7 ).
  • This system thus treats the surge receptacle ( 7 ) as an intermediate optional unit operation between the upstream unit operations ( 31 ) and the downstream unit operation ( 32 ).
  • [UO] n signifies a plurality of n unit operations located upstream, with their input and output regulated by repetitive valve modules ( 33 ).
  • the repetitive valve modules illustrated i.e., 33 , 34 , 35
  • the repetitive valve modules illustrated will be identical modules, which will standardize the connections and flowpaths between unit operations, simplify process programming, and provide a component for regulating unit operation flow that is easily replaceable.
  • FIG. 5 an alternate embodiment of a continuous process according to the invention is illustrated schematically, in which a surge receptacle feature ( 7 ) is connected as a separate unit operation, however the use of the surge receptacle ( 7 ) is made optional by providing connections from upstream unit operations ( 31 ) regulated via the valve module ( 33 ) that lead to the surge receptacle ( 7 ) via input line ( 2 ) or alternatively lead directly to the downstream unit operation ( 32 ) via a separate line ( 20 ).
  • Each unit operation is connected to a series of containers or reservoirs providing the input solutions (buffers, wash solutions, elution buffers, equilibration solutions, solvents, and the like) that are necessary and appropriate for running each step of a unit operation.
  • the collections of input solutions are represented schematically by items 30 and 36 ; each set of input solutions will be different, since they will be tailored to the steps of a particular unit operation, although a solution that is common to a number of unit operations may of course be connected to more than one unit operation.
  • the flow of the various input solutions may advantageously be regulated via an integrated valve manifold (not shown) which may preferably be the same valve manifold that regulates links from one unit operation to the next unit operation (e.g., 33 , 34 ).
  • an emergency bypass collection receptacle ( 21 ) is also provided, and the connections leading from each unit operation to the receptacle ( 21 ) are made via valve modules ( 33 , 34 ).
  • FIG. 6 an alternate embodiment of a continuous process according to the invention is illustrated schematically, in which a plurality of surge receptacles ( 7 ) is connected to the system, and a master valve manifold ( 40 ) having a multiplicity of valves, [ ] n , interconnects the entire series of unit operations (UO), surge receptacles ( 7 ), and a bypass collection tank or receptacle ( 21 ).
  • UO unit operations
  • surge receptacles 7
  • a bypass collection tank or receptacle 21
  • each of the valve modules 44 , 45 , 46 ) has channels and appropriate valves for directing flow to the desired features.
  • the output of the first unit operation ( 41 ) is directed via an input line ( 2 ) leading through a central channel of its associated valve module ( 44 ) directly to the next unit operation ( 42 ). Closure of the central valve and opening the side valve to bypass line ( 47 ) provides a circuit to divert the output of the first unit operation ( 41 ) to bypass collection receptacle ( 21 ).
  • the valve module ( 44 ) also has separate controllable flowpath for priming buffer to aid in maintaining constant flow to the next unit operation ( 42 ) if the feed from the previous unit operation ( 41 ) is not ready, interrupted or diverted.
  • the second unit operation ( 42 ) is connected via its valve module ( 45 ) to a surge receptacle ( 7 ).
  • the output from surge receptacle ( 7 ) can thereafter be pumped with a low pressure drop to the next unit operation ( 43 ) via the pump ( 1 ).
  • the output from the surge receptacle ( 7 ) may be directed through the valve module ( 46 ) directly to the unit operation ( 43 ) or diverted via line ( 47 ) to the bypass collection receptacle by appropriate manipulation of the valves.
  • the final illustrated valve module ( 46 ) a separate flowpath for priming buffer is also provided.
  • FIG. 8 shows an alternative embodiment for a series of three unit operations (UO) in a continuous manufacturing process according to the invention.
  • a surge receptacle ( 7 ) as in FIG. 7 is connected to receive the flowthough from the second unit operation, via a direct input line ( 48 ).
  • the surge receptacle ( 7 ) this is a non-optional step between the upstream unit operation ( 42 ) and the downstream unit operation ( 43 ).
  • FIG. 9 a series of three unit operations (UO) in a manufacturing process is illustrated.
  • the repetitive valve modules ( 44 , 45 ) have additional channels and valves placing a surge receptacle ( 7 ) on a separate circuit, thus making diversion of flow to the surge receptacle ( 7 ) and thence to the downstream unit operations ( 42 or 43 ) optional.
  • Such a circuit allows for delaying flow from an upstream unit operation to the next downstream unit operation or provides a means for equalizing back pressure building from a downstream unit operation.
  • connection schemes illustrated in FIGS. 7 , 8 , and 9 show advantages of utilizing integrated, repetitive valve modules for linking unit operations.
  • the product stream can be diverted to alternative paths for alternative processing, additional processing, or holding, or for emergency rescue of the partially processed product in case of a downstream system failure or upset.
  • the surge receptacles serve to collect product-containing fluid and allow a pump to take said fluid out of the (non-pressurized) surge receptacle in a controlled manner.
  • the cumulative pressure drop across a series of unit operations (which would be the sum of the pressure drops of the individual unit operations) can be kept lower, so that disposable components (usually having a low pressure rating) can be used anywhere in the process.
  • surge receptacles Another function of the surge receptacles is to create a stable flow into the next unit operation (through the pump) even if the previous unit operation does not produce a stable, steady product flow.
  • a product stream is not always continuously running out of the system. Instead, the outflow from a unit operation may instead come in repetitive intervals. On average there is a continuous flow, but the cyclic nature of, e.g., a multicolumn process allows for intermittent flow of product.
  • These fluctuations in the outflowing product stream from a unit operation are dampened by intervening surge receptacles, which gives the operator a means for controlling and making more uniform the input into a downstream unit operation.
  • providing an optional surge bag circuit as depicted in FIG. 9 connecting to each unit operation provides a mechanism for making a series of unit operations into a continuous process, even where one or more of the component operations does not provide a continuous, steady output to be transferred to downstream unit operations.
  • the surge receptacle thus becomes a useful feature for designing continuous processes.
  • the surge receptables will have a volume that permits the operator to minimize the effect of any fluctuations in flow resulting from the previous unit operation.
  • the capacity of the surge receptacle is preferably chosen such that it can accommodate multiple (e.g., three) consecutive peaks of the eluate of the SMB process.
  • the surge receptacle preferably is equipped with means to release air from the surge receptacle without allowing contaminants to enter the surge receptable.
  • a sterilization grade microfilter 8
  • the outlet of that filter is then preferably equipped with a valve ( 9 ), e.g., a pinch valve, for a controlled air release. Releasing air from the system is particularly important during start-up procedures to displace air from all the equipment and instruments.
  • One of the initial unit operations in any biological product manufacturing process will be a capture step, which typically follows the primary recovery step of a manufacturing process.
  • the capture unit operation is commonly an affinity chromatography process, but depending on the target biological product it can also advantageously utilize any other suitable separation technique, such as hydrophobic interaction chromatography (HIC), immobilized metal affinity chromatography (IMAC), ion exchange chromatography, and the like.
  • HIC hydrophobic interaction chromatography
  • IMAC immobilized metal affinity chromatography
  • ion exchange chromatography ion exchange chromatography
  • Affinity capture and elution requires a series of steps, including column loading (i.e., with a feed stream containing the target), washing, and elution, and after elution cleaning (regeneration) of the chromatography media and equilibration is often desired, so that the system can undergo repeated cycles without replacement of columns.
  • Simulated moving bed chromatography provides a way of continuous processing in a capture unit operation.
  • the continuous purification of a capture target is aided by adoption of integrated valve modules, such as the valve manifold featured in the BioSMBTM chromatography system (Tarpon Biosystems, Inc.).
  • the computer-assisted valve manifold can be programmed for automatic switching of column feeds between feed stream, wash buffer, elution buffer, cleaning buffer, and equilibration buffer, to create the simulated moving bed separation.
  • FIGS. 10A-10E shows a four zone SMB chromatography unit operation conducted using six columns loaded with capture media (see, 1 , 2 , 3 , 4 , 5 , 6 in FIG. 10A ).
  • the six columns are interconnected in series through an integrated valve manifold, which is represented as an array of individually actuatable valves ( 108 ), accordingly the array depicted in FIGS. 10A-10E shows 54 valves ( 108 ).
  • the valve manifold has at least five inlets, e.g., so as to accommodate, in the system illustrated, inputs from a product feed stream ( 101 ), a wash solution ( 102 ), an eluant ( 103 ), a cleaning solution ( 104 ), and an equilibration buffer ( 105 ). Output lines for recovery of product and for drawing off waste solutions ( 106 and 107 , respectively) are also shown.
  • FIGS. 10A-10E Continuous operation of a column chromatography purification process is illustrated by consideration of FIGS. 10A-10E in succession.
  • the feed stream ( 101 ) is directed through the valve manifold along a fluid pathway formed by appropriate actuation of valves ( 108 ) leading to the first affinity separation column ( 1 ).
  • the first column ( 1 ) has its outlet connected, through the valve manifold, to the inlet of the second column ( 2 ), and both columns receive input from the feed stream until the bed of at least the first column ( 1 ) becomes saturated with affinity-captured biological product.
  • the valving of the valve manifold is switched to shift the input to the first column ( 1 ) from the feed stream ( 101 ) to a wash solution ( 102 ).
  • the second column ( 2 ) continues to receive the feed stream ( 101 ), although the channel for the feed stream ( 101 ) through the valve manifold has been switched to be a direct input from the feed stream ( 101 ) rather than from the first column ( 1 ).
  • the outlet from the second column ( 2 ) is directed, through the valve manifold by appropriate actuation of valves ( 108 ), to the inlet of the next column ( 3 ) in the series.
  • the continuous flowthrough from the outlets of the columns are diverted through the waste line ( 107 ), except where recoverable product is being eluted from a column, in which case the throughput of the column is directed, through the valve manifold, to a product recovery line ( 106 ).
  • the “waste” line ( 107 ) may in practice be more than one line, giving the operator more control over the output of the columns and providing a means for recovery of more than just the eluted product.
  • auxiliary lines may be used for solvent recovery or recovery of any flowthrough that might be reusable (or might contain a recoverable reusable component).
  • valve actuation and consequent channel switching within the valve manifold is coordinated along the whole series of columns More preferably, the valve switching is controlled by a computer program, so that the switching occurs authomatically, and the successive stages of capture chromatography are performed without interruption or system downtime.
  • programmable switching and automated, coordinated switching is achieved in the aforementioned BioSMBTM purification system.
  • the BioSMBTM system, or a coordinated system having its features may be adapted to other unit operations in a biopharmaceutical purification process and thus provide equipment suitable for making all unit operations of a manufacturing process continuous processes.
  • valves ( 108 ) in the valve manifold changes the input received by the first column ( 1 ) to the elution buffer stream ( 103 ).
  • the captured biological product immobilized on the first column ( 1 ) begins to be eluted from the column, and appropriate switching of valves ( 108 ) downstream of the column ( 1 ) outlet directs the flowthrough (eluate) from the column ( 1 ) to the product recovery line ( 106 ).
  • the solution directed along the product recovery line ( 106 ) is advantageously transferred to the succeeding unit operation (not shown).
  • FIG. 10C programmed switching of valves ( 108 ) in the valve manifold changes the input received by the first column ( 1 ) to the elution buffer stream ( 103 ).
  • the captured biological product immobilized on the first column ( 1 ) begins to be eluted from the column, and appropriate switching of valves ( 108 ) downstream of the column ( 1 ) outlet directs the flowthrough (eluate) from the column ( 1 ) to
  • the columns would be packed with chromatography media suitable for antibody capture, such as Protein A/sepharose, and the solution recovered from the recovery line ( 106 ) will contain the desired product (antibody) but may also be a low pH solution, e.g., if the elution buffer ( 103 ) is a low pH buffer (pH 3.0-pH 3.5), which is a typical means for eluting antibody from a Protein A affinity column
  • the succeeding unit operation may include a buffer exchange to readjust pH (since antibody will eventually denature at low pH), or prior to pH readjustment a low pH unit operation may be fed directly from the capture chromatography unit operation. As illustrated in FIG.
  • an advantageous low pH unit operation for antibody biopharmaceutical processing is continuous low pH viral inactivation. Accordingly, an advantageous pair of successive unit operations in a protein biological product production process will comprise a capture chromatography unit operation followed by a low pH virus inactivation unit operation.
  • the product is being eluted from the first column ( 1 ) after switching its input to the elution buffer ( 103 ), the input to the second column ( 2 ) in the series was switched to the wash buffer ( 102 ).
  • the third column ( 3 ) continues to be loaded with the feed stream ( 101 ) and its flowthrough is directed to the inlet for the fourth column ( 4 ) of the series.
  • next zone shift is illustrated, wherein the first column ( 1 ), now stripped of product, has its inlet switched, through the valve manifold, to receive a cleaning solution designed to regenerate the affinity media for another cycle of use; simultaneously, product-saturated column ( 2 ) after receiving wash buffer for one cycle ( FIG. 10C ), now receives the elution buffer ( 103 ), so that product is eluted from the column ( 2 ) and by appropriate actuation of valves ( 108 ) of the valve manifold is recovered through the product recovery line ( 106 ), and in a continuous processing system may be transferred directly to a downstream unit operation.
  • the third column ( 3 ) in the series receives wash buffer ( 102 ) for the cycle illustrated here, and the fourth column ( 4 ) continues to be loaded with the feed stream ( 101 ) to achieve saturation of the column bed with product.
  • Flowthrough from the fourth column ( 4 ) is connected through the valve manifold directly to the inlet for the fifth column ( 5 ) to begin loading of that column with product.
  • FIG. 10E the next zone shift after the cycle shone in FIG. 10D is illustrated, wherein the first column ( 1 ), now stripped of product and cleaned to reactivate affinity ligand, has its inlet switched, through the valve manifold, to receive an equilibration buffer ( 106 ) designed to prepare the affinity media for another cycle of use, i.e., to receive the feed stream ( 101 ) in the next cycle; simultaneously, the input lines are switched through the valve manifold so that the fully eluted second column ( 2 ) now has its inlet connected to the cleaning solution ( 104 ).
  • the product-saturated third column ( 3 ) after receiving wash buffer for one cycle FIG.
  • the product recovery line ( 106 ) may transfer the product solution directly to a downstream unit operation.
  • the fourth column ( 4 ) in the series receives wash buffer ( 102 ) for the cycle illustrated here, and the fifth column ( 5 ) continues to be loaded with the feed stream ( 101 ) to achieve saturation of the column bed with product. Flowthrough from the fifth column ( 5 ) is connected through the valve manifold directly to the inlet for the sixth column ( 6 ) to begin loading of that column with product.
  • 10A-10E may be used in creating a multicolumn, continuous process for any type of chromatographic operation, including, size exclusion chromatography, ion exchange chromatography, affinity chromatography using another type of ligand than Protein A, metal ion chelation, hydrophobic interaction chromatography, and the like.
  • an early step will commonly be a capture chromatography step.
  • a Protein A capture chromatography step proceeds directly after primary recovery of the antibody from the bioreactor.
  • elution from the affinity capture medium is accomplished by lowering the pH of the buffer flowing through the chromatography column.
  • the Protein A/antibody complex dissociates at low pH, e.g., between about pH 3.0 and pH 3.5. Accordingly the eluate from a Protein A column is a low pH solution.
  • An antibody product will suffer significant degradation if it resides at low pH for longer than 30 min.
  • the unit operation is designed to receive a low pH feed (e.g., via inplet ( 54 ) into an integrated multi-valve valve block or manifold ( 40 )) and transfer the feed to one of a series of holding/incubation receptacles ( 50 , 51 , 52 ).
  • the valve manifold ( 4 ) is equipped with the channelling and valve array, represented by the figure [ ] n , appropriate for independent and alternative transfer to any of the holding/incubation receptacles ( 50 , 51 , 52 ) connected to the valve manifold ( 40 ).
  • the product solution is to be incubated at a pH suitable for inactivation of viruses that might be in the solution.
  • a pH suitable for inactivation of viruses For example, for an antibody product solution, incubation at a preselected, controlled pH (e.g., ⁇ 0.2 pH units) below pH 3.5 for 30 min. ⁇ 5 min., reduces the level of live viruses according to an accepted standard, and degradation or denaturation of the antibody product will be acceptable.
  • Viral inactivation steps are typically designed to provide a log reduction value of 3 or higher, i.e., at least a 10,000-fold reduction in live viruses.
  • an aliquot of the product solution is transferred via the inlet ( 54 ) to an incubation receptacle ( 52 ).
  • the receptacle may be sized to receive the transfer of all or any part of the throughput of the preceeding unit operation.
  • the receptacles ( 50 , 51 , 52 ) may advantageously be plastic bags, bottles, flasks, or the like.
  • the other components of the system, such as the tubing leads to the valve manifold ( 40 ) and parts of the manifold itself may be made of single-use materials.
  • valve system may be formed by a replaceable sheet membrane covering an array of valve actuators and associated channels, where juxtaposition of the flexible membrane results in a close system of valve-controlled channels, the pattern of which is determined by different combinations of opened and closed valves in the array.
  • valve cassette featured in the BioSMBTM purification system (Tarpon Biosystems, Inc., Worcester, Mass. (US)).
  • each receptacle will be equipped with a pH sensor (not shown), as well as inlet ports (not shown) for receiving acidic and/or basic solutions for adjusting the pH to within a desired range. It may be important that the antibody product solution introduced into the receptacles ( 50 , 51 , 52 ) remains well mixed, e.g., so that accurate pH readings may be made and any pH adjustment affects the entire aliquot collected in the receptacle.
  • the receptacles will be equipped with mixing means, which are represented in FIG. 11 schematically by propeller-type mixing paddles ( 53 ), but which may alternatively be any means suitable for effecting the desired level of homogenization of the product solution. Magnetic mixing bars, swirl flasks, rocking tables, and the like are all suitable and contemplated herein.
  • variable intake channels through the valve module ( 40 ) can direct incoming flow to each of the holding/incubation receptacles ( 50 , 51 , 52 ).
  • the contents of each of the incubation receptacles can be separately directed to the outlet ( 55 ) of this unit operation.
  • the solution entering the unit operation via inlet ( 54 ) is directed the third incubation receptacle ( 52 ), while the contents of the first incubation receptacle are being directed to the outlet ( 55 ), e.g., for transfer to the next unit operation.
  • valve module ( 40 ) may be provided with valving and pumps (not shown) for transferring solutions from one receptacle to another. This transfer through a series of receptacles might be implemented, for example, if a step-wise adjustment of pH or other solution condition is desired for this unit operation.
  • a first receptacle ( 52 ) can be used for incubation at a low pH, and then second and subsequent receptacles can be used for further processing, such as buffer exchange (e.g., to raise pH gradually), exposing the product to a chaotropic agent, or incubation to effect protein reassembly or refolding under solution conditions favorable for that.
  • buffer exchange e.g., to raise pH gradually
  • incubation e.g., to raise pH gradually
  • transfer of product solution through a series of three holding/incubation receptacles ( 50 ) in series is illustrated. In FIG.
  • the channels for transfer between holding/incubation receptacles ( 50 ) is depicted as flowing through the valve module ( 40 ), such that the serial transfer is controlled by manipulation of the integrated valve system.
  • the serial transfer from one receptacle ( 50 ) to the next is not controlled using the valve module ( 40 ) but occurs by some other means, e.g., by overflow, manual transfer, or transfer triggered by a sensor in the source receptacle, e.g., a timer, a fill level sensor, or a pH sensor that signals a transfer operation when a particular pH is reached.
  • the acceptable time window for exposure of a proteinaceous product to low pH is typically narrow (e.g., 30 ⁇ 5 minutes). Exposure times that are too short do not provide sufficient viral inactivation, and exposure times that are too long lead to higher levels of degradation of the product.
  • Continuous processing permits operating a low pH viral inactivation unit operation within tight time tolerances.
  • a preferred methodology involves moving “packets” or aliquots of a product solution through the unit operation in a semi-continuous manner. Where the unit operation preceding the low pH viral inactivation step is a capture chromatography operation (e.g., Protein A affinity chromatography, for an antibody product), the product enters the low pH virus inactivation unit operation as a continuous series of eluate peaks.
  • the proper incubation time is imposed and a continuous transfer out to the next unit operation can be implemented.
  • the viral inactivation unit operation may be advantageously conducted as follows:
  • the “movement” of a receptacle containing the pooled Protein A eluate that is described in the sequence above can be achieved with a suitable controller and valve cassette. This is directly analogous to the simulated “movement” of chromatography columns achieved using the valve cassette in the system illustrated in FIG. 10A-FIG . 10 E.
  • the Protein A eluate can be flowed through a cascading series of continuously mixed holding bags (receptacles), the first of which would accomplish the pH adjustment of the Protein A eluate, and the last of which would accomplish the pH readjustment of the inactivated solution prior to the next unit operation.
  • the bags are sized to ensure that the appropriate residence time for low pH viral inactivation is achieved.
  • the design of a multicolumn counter-current continuous chromatography process requires the same basic process information as for a batch process. This includes the product concentration in the feed solution (titer), the equilibrium binding capacity (static binding capacity) and the overall process sequence. Information about the mass transfer kinetics, which depend on the chromatography media, product and solution conditions, is also required for sizing the system. Generally, this can be obtained from breakthrough curve analysis. For this reason, a well-designed batch process is a very good starting point for the design of a continuous multicolumn or multistage purification process.
  • UF/DF ultrafiltration/diafiltration
  • useful data can be obtained from a bench scale tangential flow filtration (TFF) system on flux as a function of transmembrane pressure at varying flow rates and product concentrations.
  • TMF tangential flow filtration
  • useful data can be obtained on pressure drop as a function of flux and on loading capacity for each membrane device.
  • a continuous processing operation can be designed.
  • the first design choice is the processing time. Contrary to a batch process, where the processing time is a result of the process design, a continuous process allows preselection of the processing time. The longer the processing time, the lower the flow rates through the unit operation series and the more compact the overall system can be (in terms of the scale of equipment utilized). On the other hand, processing times that are too long may result in product degradation at some stages that reach unacceptable levels.
  • the feed flow rate is a result of the volume that needs to be processed and the processing time. The volume that needs to be processed is referred to as the “batch” or “lot size”.
  • the minimum feed flow rate into the CPT process, Q m is calculated from the maximum processing time, t, using the following equation:
  • a p is the amount of product required
  • C p is the product concentration in the feed
  • Y is the overall process yield.
  • the minimum feed flow rate to achieve the 3 day, 100 g productivity objective is 39 mL/min.
  • the target CPT process feed flow rate will be set at a value at least 10% higher than the minimum flow rate, or about 45 mL/min.
  • the CPT process design can begin with the design of the first unit operation, for example a capture step such as a Protein A affinity chromatography step.
  • the design algorithm starts with determining the minimum (simulated) transport rate of the chromatography media. This is the transport rate of the media that would allow binding all product in case there would be no mass transfer resistance, in case there would be ideal plug flow and in the absence of any other non-ideal parameters.
  • the actual simulated transport rate of chromatography media is chosen to be above the minimum transport rate. Typically, the practitioner selects safety margins in the range of 5-40%.
  • the volume of chromatography media in the loading zone then depends on the flow rate going through the columns in the loading zone and the required residence time, which mainly depends on mass transfer phenomena such as diffusion. Knowing the required residence time and the feed flow rate, the required resin volume in the loading zone can be calculated.
  • the outlet product flow rate from this step can be set to equal the inlet flow rate for the second unit operation in the process, so that the hydraulic capacities of each connecting step are matched.
  • Similar design algorithms as for the first unit operation can be applied to each unit operation in the process.
  • Batch data for each unit operation can be used to develop a continuous operation design for that unit operation, which allows it to be linked to the previous and subsequent unit operations.
  • each process step can then be optimized through iterative experimentation to maximize any desired attribute, such as volumetric productivity or buffer utilization.
  • the size and throughput of each unit operation will be governed by the flow rate (hydraulic capacity) instead of by total volume or mass to be processed.
  • optimization will involve a study of the principles and phenomena that govern size and hydraulic capacity of the unit operation.
  • the optimization of the chromatography steps using continuous multicolumn SMB will involve a study of the impact of the separation factor, S, and number of transport units, NTU, on performance of the process step.
  • the separation factor, S is a measure of transport capacity caused by the bed transport rate in relation to the product feed rate and is defined as:
  • ⁇ feed and ⁇ bed are the flow rates of the liquid and stationary phases respectively (in the case of the bed, ⁇ bed is the simulated transport rate), Q static is the binding capacity of the media, and C feed is the concentration in the feed.
  • NTU The number of transfer units
  • NTU k oL ⁇ a ⁇ V/ ⁇ feed
  • k oL is the overall mass transfer coefficient of the system
  • V is the column volume
  • a is the specific surface area, which equals the surface area of the particles divided by column volume.
  • the NTU is the ratio of the residence time in the system and the characteristic mass transfer time.
  • the optimal processing conditions can be identified for each step, in order to achieve the desired productivity while meeting the separation or performance objectives (e.g., host cell protein removal for a Protein A chromatography step).
  • the optimal processing conditions may be too close to conditions that would result in unacceptable performance, in which case the conditions are adjusted to provide optimal and acceptably robust performance.
  • samples may be taken at each point in the process to verify that the anticipated product and process attributes (i.e., purity, yield) are being achieved by the CPT process.
  • Final purified bulk product may be analyzed to determine product purity by SDS-PAGE and HPLC, clearance of specific impurities (e.g., host cell proteins) by ELISA, and product concentration to enable overall yield determination.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Biotechnology (AREA)
  • General Health & Medical Sciences (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Biochemistry (AREA)
  • Genetics & Genomics (AREA)
  • Analytical Chemistry (AREA)
  • Microbiology (AREA)
  • General Engineering & Computer Science (AREA)
  • Sustainable Development (AREA)
  • Molecular Biology (AREA)
  • Proteomics, Peptides & Aminoacids (AREA)
  • Biophysics (AREA)
  • Medicinal Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Immunology (AREA)
  • Pathology (AREA)
  • Physics & Mathematics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Clinical Laboratory Science (AREA)
  • General Physics & Mathematics (AREA)
  • Peptides Or Proteins (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Medicines Containing Antibodies Or Antigens For Use As Internal Diagnostic Agents (AREA)
US13/991,604 2010-12-06 2011-12-06 Continuous processing methods for biological products Abandoned US20130260419A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US13/991,604 US20130260419A1 (en) 2010-12-06 2011-12-06 Continuous processing methods for biological products

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US42006610P 2010-12-06 2010-12-06
US13/991,604 US20130260419A1 (en) 2010-12-06 2011-12-06 Continuous processing methods for biological products
PCT/US2011/063598 WO2012078677A2 (en) 2010-12-06 2011-12-06 Continuous processing methods for biological products

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2011/063598 A-371-Of-International WO2012078677A2 (en) 2010-12-06 2011-12-06 Continuous processing methods for biological products

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US17/030,731 Continuation US12012629B2 (en) 2010-12-06 2020-09-24 Continuous processing methods for biological products

Publications (1)

Publication Number Publication Date
US20130260419A1 true US20130260419A1 (en) 2013-10-03

Family

ID=46207692

Family Applications (2)

Application Number Title Priority Date Filing Date
US13/991,604 Abandoned US20130260419A1 (en) 2010-12-06 2011-12-06 Continuous processing methods for biological products
US17/030,731 Active 2034-04-12 US12012629B2 (en) 2010-12-06 2020-09-24 Continuous processing methods for biological products

Family Applications After (1)

Application Number Title Priority Date Filing Date
US17/030,731 Active 2034-04-12 US12012629B2 (en) 2010-12-06 2020-09-24 Continuous processing methods for biological products

Country Status (7)

Country Link
US (2) US20130260419A1 (ja)
EP (2) EP2649016B1 (ja)
JP (2) JP2013544524A (ja)
KR (1) KR102027596B1 (ja)
CN (2) CN105107228B (ja)
BR (1) BR112013013884A2 (ja)
WO (1) WO2012078677A2 (ja)

Cited By (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150064769A1 (en) * 2012-06-29 2015-03-05 Emd Millipore Corporation Methods for Inactivating Viruses During a Protein Purification Process
WO2015148530A1 (en) * 2014-03-24 2015-10-01 Synthace Limited Bioprocess method and system
US20150343332A1 (en) * 2014-05-27 2015-12-03 Artificial Cell Technologies, Inc. Automated layer by layer construction of multilayer coated cores by tff
WO2016025803A1 (en) * 2014-08-15 2016-02-18 Massachusetts Institute Of Technology Systems and methods for synthesizing chemical products, including active pharmaceutical ingredients
US20160115195A1 (en) * 2013-06-25 2016-04-28 Cadila Healthcare Limited Purification process for monoclonal antibodies
WO2016107809A1 (en) * 2014-12-31 2016-07-07 Ge Healthcare Bio-Sciences Ab Valve manifolds for simulated moving bed chromatography
EP3141594A3 (en) * 2016-11-11 2017-06-14 Bayer Pharma Aktiengesellschaft Method for sampling fluid streams for monitoring contaminants in a continuous flow
US20180117495A1 (en) * 2015-05-13 2018-05-03 Bayer Aktiengesellschaft Method for the continuous elution of a product from chromatography columns
WO2018086997A1 (en) * 2016-11-11 2018-05-17 Bayer Pharma Aktiengesellschaft Method for sampling fluid streams for monitoring contaminants in a continuous flow
US20180284079A1 (en) * 2017-03-30 2018-10-04 Shimadzu Corporation Liquid chromatograph
FR3073425A1 (fr) * 2017-11-16 2019-05-17 Novasep Process Procede de separation d’un melange avec mesure de purete ou rendement sur une cuve intermediaire
RU2694327C2 (ru) * 2014-06-09 2019-07-11 Джензим Корпорейшн Способ культивирования в системе посевных ферментеров (варианты)
US10519195B2 (en) * 2013-09-17 2019-12-31 Kaneka Corporation Antibody purification method, antibody obtained therefrom, novel antibody purification method using cation exchanger, and antibody obtained therefrom
US10702481B2 (en) 2017-02-17 2020-07-07 Massachusetts Institute Of Technology Systems and methods for the fabrication of tablets, including pharmaceutical tablets
US10792618B2 (en) 2018-06-19 2020-10-06 Sartorius Stedim Biotech Gmbh Particle separation and/or purification of a fluid
US10919986B2 (en) 2016-04-29 2021-02-16 Nanopareil, Llc Porous polymeric cellulose prepared via cellulose crosslinking
WO2021028658A1 (en) * 2019-08-15 2021-02-18 Fujifilm Diosynth Biotechnologies Uk Limited Process for purifying monoclonal antibodies
WO2021046443A1 (en) * 2019-09-06 2021-03-11 Amicus Therapeutics, Inc. Method for capturing and purification of biologics
US11022586B2 (en) 2014-01-21 2021-06-01 National Nuclear Laboratory Limited Multi-column separation apparatus and method
US11060058B2 (en) 2014-06-06 2021-07-13 Genzyme Corporation Perfusion culturing methods and uses thereof
CN113341014A (zh) * 2021-06-01 2021-09-03 上海药明生物技术有限公司 连续流层析装置和方法
US11185839B2 (en) 2016-05-02 2021-11-30 Massachusetts Institute Of Technology Reconfigurable multi-step chemical synthesis system and related components and methods
WO2022078829A1 (en) 2020-10-14 2022-04-21 Sartorius Stedim Biotech Gmbh A method and system for configuring and/or setup of a downstream process for processing a biomass
US11466386B2 (en) 2016-12-12 2022-10-11 Nanopareil, Llc Spinnerets and spinneret arrays for electrospinning and electrospinning machines
EP4124653A1 (en) * 2021-07-27 2023-02-01 Sartorius Stedim Biotech GmbH Method for producing a bioproduct
USRE49773E1 (en) 2013-02-14 2024-01-02 Nanopareil, Llc Hybrid felts of electrospun nanofibers
US11857892B2 (en) 2017-11-16 2024-01-02 Novasep Process Solutions Regulated method for separating a mixture
EP4130226A4 (en) * 2020-03-23 2024-05-01 Prestige Biologics Co Ltd HYBRID SYSTEM FOR CULTURE AND PURIFICATION PROCEDURES FOR THE PRODUCTION OF ANTIBODY MEDICINES

Families Citing this family (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2578286A1 (en) 2011-10-04 2013-04-10 Merck Patent GmbH Method and apparatus for chromatographic purification
EP2682168A1 (en) * 2012-07-02 2014-01-08 Millipore Corporation Purification of biological molecules
EP2906232A4 (en) * 2012-10-15 2016-09-28 Mark Frings Pittenger DEVICE FOR EXTRACORPORAL CELL THERAPY OF THE LUNG OR OTHER ORGANS
US10421949B2 (en) 2013-02-22 2019-09-24 Genzyme Corporation Microcarrier perfusion culturing methods and uses thereof
CA2901950A1 (en) 2013-02-22 2014-08-28 Genzyme Corporation Microcarrier perfusion culturing methods and uses thereof
SG10201709131UA (en) * 2013-03-08 2017-12-28 Genzyme Corp Continuous purification of therapeutic proteins
KR101891522B1 (ko) 2013-12-12 2018-08-24 이엠디 밀리포어 코포레이션 아크릴아미드 함유 필터를 사용한 단백질 분리
TWI709570B (zh) 2014-01-17 2020-11-11 美商健臻公司 無菌層析法及製法
TWI709569B (zh) * 2014-01-17 2020-11-11 美商健臻公司 無菌層析樹脂及其用於製造方法的用途
EP3105580B1 (en) 2014-02-14 2023-10-04 Cytiva Sweden AB Automated multi-step purification system
EP2907565A1 (de) 2014-02-17 2015-08-19 Bayer Technology Services GmbH Dialyse-Einheit zum kontinuierlichen Puffer- bzw. Medienaustausch aus einer Proteinlösung
EP3613841B1 (en) 2014-03-25 2022-04-20 Terumo BCT, Inc. Passive replacement of media
EP3248122A1 (en) * 2015-01-20 2017-11-29 GE Healthcare Bio-Sciences Corp. Process simulation in cell a processing facility
EP3015542A1 (de) 2015-05-07 2016-05-04 Bayer Technology Services GmbH Modulare anlage und verfahren zur kontinuierlichen, keimreduzierten produktion und/oder aufbereitung eines produktes
EP3093335A1 (de) 2015-05-13 2016-11-16 Bayer Technology Services GmbH Prozessleitsystem zur regelung und steuerung einer modular aufgebauten anlage zur produktion von biopharmazeutischen und biologischen makromolekularen produkten
WO2017004592A1 (en) 2015-07-02 2017-01-05 Terumo Bct, Inc. Cell growth with mechanical stimuli
FR3042793B1 (fr) * 2015-10-26 2019-12-27 Arkema France Synthese de peroxydes organiques a l'aide d'un reacteur agite a ecoulement oscillatoire
US11407981B2 (en) 2016-03-11 2022-08-09 Boehringer Ingelheim International Gmbh Methods for continuously inactivating a virus during manufacture of a protein
EP3464565A4 (en) 2016-05-25 2020-01-01 Terumo BCT, Inc. CELL EXPANSION
US11104874B2 (en) 2016-06-07 2021-08-31 Terumo Bct, Inc. Coating a bioreactor
US11685883B2 (en) 2016-06-07 2023-06-27 Terumo Bct, Inc. Methods and systems for coating a cell growth surface
GB201622343D0 (en) * 2016-12-29 2017-02-15 Ge Healthcare Bio Sciences Ab Method in bioprocess purification system
JP7393945B2 (ja) 2017-03-31 2023-12-07 テルモ ビーシーティー、インコーポレーテッド 細胞増殖
MX2020000353A (es) * 2017-07-10 2020-08-17 Takeda Pharmaceuticals Co Metodos para incubar liquidos e inactivar virus.
JOP20200154A1 (ar) 2017-12-21 2020-06-18 Boehringer Ingelheim Int مركبات ومشتقات بيريدو بيريمينون بها استبدال ببنزيل أمينو جديدة كمثبطات sos1
DE102018107679A1 (de) * 2018-03-29 2019-10-02 Sartorius Stedim Biotech Gmbh Konfigurierbare Vorrichtung zur flexiblen Bereitstellung von Verbindungen und/oder Funktionen in einem biopharmazeutischen Prozess
BR112021003420A2 (pt) 2018-08-31 2021-05-18 Genzyme Corporation resina cromatográfica estéril e uso da mesma em processos de manufatura
SG11202110909XA (en) * 2019-04-03 2021-10-28 Genzyme Corp Continuous production of recombinant proteins
GB201908612D0 (en) * 2019-06-17 2019-07-31 Ge Healthcare Bio Sciences Ab A method for separating biomolecules
FR3099066B1 (fr) 2019-07-26 2021-08-13 Novasep Process Procédé de purification d’une substance cible avec inactivation virale
WO2022137302A1 (ja) * 2020-12-21 2022-06-30 日揮株式会社 液体取扱設備の設計方法、製造方法、及び液体取扱設備
DE102021116377A1 (de) 2021-06-24 2022-12-29 Fresenius Medical Care Deutschland Gmbh Filtersystem, Steuerungsvorrichtung und Platine für dasselbe sowie Verfahren zum Wechsel
DE102021130958A1 (de) * 2021-11-25 2023-05-25 MionTec GmbH Ionenaustauscheranlage zur Verwendung in Ionenaustauschprozessen
US20230277958A1 (en) * 2022-03-04 2023-09-07 Sartorius Stedim Chromatography Systems Ltd. Method for operating a chromatography setup
WO2023188937A1 (ja) * 2022-03-30 2023-10-05 富士フイルム株式会社 バイオ医薬品の原薬の製造方法、バイオ医薬品の原薬の製造システム、およびバイオ医薬品の原薬
WO2023247798A1 (de) 2022-06-24 2023-12-28 Bilfinger Life Science Gmbh Modulare vorrichtung und verfahren zur kontinuierlichen herstellung von biotechnologischen produkten
DE102022208467A1 (de) 2022-06-24 2024-01-04 Bilfinger Life Science Gmbh Modulare Vorrichtung und Verfahren zur kontinuierlichen Herstellung von biotechnologischen Produkten

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5256294A (en) * 1990-09-17 1993-10-26 Genentech, Inc. Tangential flow filtration process and apparatus
US6432630B1 (en) * 1996-09-04 2002-08-13 Scandinanian Micro Biodevices A/S Micro-flow system for particle separation and analysis

Family Cites Families (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DK309184D0 (da) * 1984-06-25 1984-06-25 Nordisk Insulinlab Fremgangsmaade til isolering af insulin eller insulinlignende materiale fra en fermenteringsvaeske
US4722902A (en) * 1985-11-04 1988-02-02 Endotronics, Inc. Apparatus and method for culturing cells, removing waste and concentrating product
US4802981A (en) 1987-11-04 1989-02-07 Oros Systems Limited Automatic chromatography apparatus
US5354655A (en) * 1988-03-29 1994-10-11 Biocontrol Systems, Inc. Method for determining the presence or concentration of a bound enzyme
JP3128347B2 (ja) * 1992-09-21 2001-01-29 日本碍子株式会社 抗体の分取・精製方法
US5429746A (en) 1994-02-22 1995-07-04 Smith Kline Beecham Corporation Antibody purification
US5928516A (en) 1995-01-20 1999-07-27 Pall Corporation Filter package
US6012487A (en) * 1997-03-10 2000-01-11 Brian A. Hauck Prime purge injection valve or multi-route selections valve
US5886154A (en) 1997-06-20 1999-03-23 Lebing; Wytold R. Chromatographic method for high yield purification and viral inactivation of antibodies
JP2000028598A (ja) * 1998-07-14 2000-01-28 Ebara Corp 全自動試料連続精製・分析装置及び精製・分析方法
FI981615A0 (fi) * 1998-07-15 1998-07-15 Xyrofin Oy Mannitolin valmistusmenetelmä immobilisoituja mikro-organismeja käyttäen
US6214221B1 (en) * 1999-02-22 2001-04-10 Henry B. Kopf Method and apparatus for purification of biological substances
US6901956B2 (en) * 1999-06-18 2005-06-07 Danfoss A/S Flow cell having endless loop manifold
CN1169595C (zh) * 2002-03-13 2004-10-06 浙江大学 模拟移动床色谱反应器
US6843854B2 (en) * 2002-05-31 2005-01-18 Purdue Research Foundation Method and apparatus for separating a component from a mixture
SI1545574T1 (sl) 2002-09-13 2014-10-30 Biogen Idec Inc. Postopek za čiščenje polipeptidov s simulirano "moving bed" kromatografijo
JP2007523621A (ja) * 2003-06-18 2007-08-23 オニックス ファーマシューティカルズ，インコーポレイティド ウイルスを精製するための方法
US7169599B2 (en) * 2003-06-20 2007-01-30 Groton Biosystems, Llc Fluid interface for bioprocessor systems
CN1934129B (zh) * 2004-01-21 2010-07-14 东丽株式会社 分级装置和分级方法
US20060273013A1 (en) * 2004-03-01 2006-12-07 Chin Nien-Hwa L Versatile simulated moving bed systems
EP1716900A1 (en) * 2005-04-29 2006-11-02 Eidgenössische Technische Hochschule Zürich Method and device for chromatographic purification
US20080318283A1 (en) * 2006-02-01 2008-12-25 Clague P. Hodgson Fermentation Process for Continuous Plasmid Dna Production
US7975935B2 (en) * 2007-04-11 2011-07-12 Complete Automation, Inc. Cost effective paint system
JP5140721B2 (ja) * 2007-04-17 2013-02-13 イクスエンド、ホールディング、ベスローテン、フェンノートシャップ 連続メンブレン吸着方法および装置
CN100509760C (zh) * 2007-05-24 2009-07-08 江苏汉邦科技有限公司 四区模拟移动床分离纯化发酵液中的谷氨酰胺的方法
US8549934B2 (en) * 2008-03-25 2013-10-08 Flownamics Analytical Instruments, Inc. Segmented online sampling apparatus and method of use
CN201283233Y (zh) * 2008-09-28 2009-08-05 王学群 模拟移动床色谱分离装置
SG10201702922VA (en) * 2008-10-20 2017-06-29 Abbvie Inc Isolation and purification of antibodies using protein a affinity chromatography
AU2010207871B2 (en) * 2009-01-30 2015-01-22 Greenfield Specialty Alcohols Inc. Integrated system for hydrogen and methane production from industrial organic wastes and biomass
WO2010096587A2 (en) * 2009-02-19 2010-08-26 Primafuel, Inc. High efficiency separations method and apparatus
US8951416B2 (en) * 2009-02-25 2015-02-10 Dupont Nutrition Biosciences Aps Separation process
CN101838230B (zh) * 2009-03-17 2011-11-02 南京工业大学 一种尔他培南的分离纯化方法
TWI352615B (en) * 2009-06-09 2011-11-21 Univ Nat Taiwan Science Tech Fluid separation method and fluid seperation appar
EP2488267B1 (en) * 2009-10-13 2017-04-19 Pall Corporation Conversion of fixed-bed liquid chromatography processes to simulated moving bed processes
US8668886B2 (en) * 2011-04-24 2014-03-11 Therapeutic Proteins International, LLC Separative bioreactor

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5256294A (en) * 1990-09-17 1993-10-26 Genentech, Inc. Tangential flow filtration process and apparatus
US6432630B1 (en) * 1996-09-04 2002-08-13 Scandinanian Micro Biodevices A/S Micro-flow system for particle separation and analysis

Non-Patent Citations (6)

* Cited by examiner, † Cited by third party
Title
Bisschops et al, Single-Use, Continuous-Countercurrent, Multicolumn Chromatography, 2009 BioProcess International Supplement, pg 18-23 *
Chin et al, Simulated Moving Bed Equipment Designs, 2004, Separation & Purification Reviews, 33(2): 77-155 *
Fahrner et al, Industrial Purification of Pharmaceutical Antibodies: Development, Operation, and Validation of Chromatography Processes, 2001, Biotechnology and Genetic Engineering Reviews, 18(1): 301-327 *
Liu et al, Recovery and purification process development for monoclonal antibody production, 2010, mAbs 2:5, 480-499 *
of Caillet-Fauquet et al, 2004, Continuous-flow UVC irradiation: a new, effective, protein activity-preserving system for inactivating bacteria and viruses, including erythrovirus B19, Journal of Virological Methods 118: 131–139; *
Wallis et al, CONCENTRATION OF VIRUSES FROM WATER BY MEMBRANE CHROMATOGRAPHY, 1979, Ann. Rev. Microbiol., 33:413-37 *

Cited By (48)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150064769A1 (en) * 2012-06-29 2015-03-05 Emd Millipore Corporation Methods for Inactivating Viruses During a Protein Purification Process
US9809799B2 (en) * 2012-06-29 2017-11-07 Emd Millipore Corporation Methods for inactivating viruses during a protein purification process
USRE49773E1 (en) 2013-02-14 2024-01-02 Nanopareil, Llc Hybrid felts of electrospun nanofibers
US20160115195A1 (en) * 2013-06-25 2016-04-28 Cadila Healthcare Limited Purification process for monoclonal antibodies
US9708365B2 (en) * 2013-06-25 2017-07-18 Cadila Healthcare Limited Purification process for monoclonal antibodies
EP3013849B1 (en) 2013-06-25 2017-09-13 Cadila Healthcare Limited Purification process for monoclonal antibodies
US10519195B2 (en) * 2013-09-17 2019-12-31 Kaneka Corporation Antibody purification method, antibody obtained therefrom, novel antibody purification method using cation exchanger, and antibody obtained therefrom
US11022586B2 (en) 2014-01-21 2021-06-01 National Nuclear Laboratory Limited Multi-column separation apparatus and method
WO2015148530A1 (en) * 2014-03-24 2015-10-01 Synthace Limited Bioprocess method and system
US9977862B2 (en) 2014-03-24 2018-05-22 Synthace Limited Bioprocess method and system
US20150343332A1 (en) * 2014-05-27 2015-12-03 Artificial Cell Technologies, Inc. Automated layer by layer construction of multilayer coated cores by tff
US9975066B2 (en) * 2014-05-27 2018-05-22 Artificial Cell Technologies, Inc. Automated layer by layer construction of multilayer coated cores by TFF
US11060058B2 (en) 2014-06-06 2021-07-13 Genzyme Corporation Perfusion culturing methods and uses thereof
US12006510B2 (en) 2014-06-06 2024-06-11 Genzyme Corporation Perfusion culturing methods and uses thereof
US10570367B2 (en) 2014-06-09 2020-02-25 Genzyme Corporation Seed train processes and uses thereof
RU2694327C2 (ru) * 2014-06-09 2019-07-11 Джензим Корпорейшн Способ культивирования в системе посевных ферментеров (варианты)
AU2019268159B2 (en) * 2014-08-15 2022-01-13 Massachusetts Institute Of Technology Systems and methods for synthesizing chemical products, including active pharmaceutical ingredients
WO2016025803A1 (en) * 2014-08-15 2016-02-18 Massachusetts Institute Of Technology Systems and methods for synthesizing chemical products, including active pharmaceutical ingredients
US10780410B2 (en) 2014-08-15 2020-09-22 Massachusetts Institute Of Technology Systems and methods for synthesizing chemical products, including active pharmaceutical ingredients
US11565230B2 (en) 2014-08-15 2023-01-31 Massachusetts Institute Of Technology Systems and methods for synthesizing chemical products, including active pharmaceutical ingredients
EP3180118A4 (en) * 2014-08-15 2018-04-04 Massachusetts Institute Of Technology Systems and methods for synthesizing chemical products, including active pharmaceutical ingredients
US10888799B2 (en) 2014-12-31 2021-01-12 Cytiva Sweden Ab Valve manifolds for simulated moving bed chromatography
WO2016107809A1 (en) * 2014-12-31 2016-07-07 Ge Healthcare Bio-Sciences Ab Valve manifolds for simulated moving bed chromatography
CN107106929A (zh) * 2014-12-31 2017-08-29 通用电气健康护理生物科学股份公司 用于模拟移动床层析的阀歧管
EP3594679A1 (en) * 2014-12-31 2020-01-15 GE Healthcare Bio-Sciences AB Smb chromatography valve
US11648490B2 (en) 2014-12-31 2023-05-16 Cytiva Sweden Ab Valve manifolds for simulated moving bed chromatography
US20180117495A1 (en) * 2015-05-13 2018-05-03 Bayer Aktiengesellschaft Method for the continuous elution of a product from chromatography columns
US11560438B2 (en) 2016-04-29 2023-01-24 Nanopareil, Llc Porous polymeric cellulose prepared via cellulose crosslinking
US10919986B2 (en) 2016-04-29 2021-02-16 Nanopareil, Llc Porous polymeric cellulose prepared via cellulose crosslinking
US11185839B2 (en) 2016-05-02 2021-11-30 Massachusetts Institute Of Technology Reconfigurable multi-step chemical synthesis system and related components and methods
EP3141594A3 (en) * 2016-11-11 2017-06-14 Bayer Pharma Aktiengesellschaft Method for sampling fluid streams for monitoring contaminants in a continuous flow
WO2018086997A1 (en) * 2016-11-11 2018-05-17 Bayer Pharma Aktiengesellschaft Method for sampling fluid streams for monitoring contaminants in a continuous flow
US11466386B2 (en) 2016-12-12 2022-10-11 Nanopareil, Llc Spinnerets and spinneret arrays for electrospinning and electrospinning machines
US10702481B2 (en) 2017-02-17 2020-07-07 Massachusetts Institute Of Technology Systems and methods for the fabrication of tablets, including pharmaceutical tablets
US11020352B2 (en) 2017-02-17 2021-06-01 Massachusetts Institute Of Technology Systems and methods for the fabrication of tablets, including pharmaceutical tablets
US20180284079A1 (en) * 2017-03-30 2018-10-04 Shimadzu Corporation Liquid chromatograph
US10866217B2 (en) * 2017-03-30 2020-12-15 Shimadzu Corporation Liquid chromatograph flow path switching and control system for columns to a detector
WO2019097181A1 (fr) * 2017-11-16 2019-05-23 Novasep Process Procede de separation d'un melange avec mesure de purete ou rendement sur une cuve intermediaire
US11857892B2 (en) 2017-11-16 2024-01-02 Novasep Process Solutions Regulated method for separating a mixture
FR3073425A1 (fr) * 2017-11-16 2019-05-17 Novasep Process Procede de separation d’un melange avec mesure de purete ou rendement sur une cuve intermediaire
US10792618B2 (en) 2018-06-19 2020-10-06 Sartorius Stedim Biotech Gmbh Particle separation and/or purification of a fluid
WO2021028658A1 (en) * 2019-08-15 2021-02-18 Fujifilm Diosynth Biotechnologies Uk Limited Process for purifying monoclonal antibodies
WO2021046443A1 (en) * 2019-09-06 2021-03-11 Amicus Therapeutics, Inc. Method for capturing and purification of biologics
EP4130226A4 (en) * 2020-03-23 2024-05-01 Prestige Biologics Co Ltd HYBRID SYSTEM FOR CULTURE AND PURIFICATION PROCEDURES FOR THE PRODUCTION OF ANTIBODY MEDICINES
WO2022078829A1 (en) 2020-10-14 2022-04-21 Sartorius Stedim Biotech Gmbh A method and system for configuring and/or setup of a downstream process for processing a biomass
CN113341014A (zh) * 2021-06-01 2021-09-03 上海药明生物技术有限公司 连续流层析装置和方法
WO2023006576A1 (en) * 2021-07-27 2023-02-02 Sartorius Stedim Biotech Gmbh Method for producing a bioproduct
EP4124653A1 (en) * 2021-07-27 2023-02-01 Sartorius Stedim Biotech GmbH Method for producing a bioproduct

Also Published As

Publication number Publication date
KR20140059753A (ko) 2014-05-16
EP3578522A1 (en) 2019-12-11
EP2649016A2 (en) 2013-10-16
CN105107228B (zh) 2017-03-29
JP2018046822A (ja) 2018-03-29
CN103562145B (zh) 2016-09-21
EP2649016A4 (en) 2016-08-10
US20210017561A1 (en) 2021-01-21
WO2012078677A3 (en) 2012-08-02
CN105107228A (zh) 2015-12-02
JP2013544524A (ja) 2013-12-19
WO2012078677A2 (en) 2012-06-14
CN103562145A (zh) 2014-02-05
KR102027596B1 (ko) 2019-10-01
EP2649016B1 (en) 2020-06-10
US12012629B2 (en) 2024-06-18
BR112013013884A2 (pt) 2016-09-13
JP6476528B2 (ja) 2019-03-06

Similar Documents

Publication Publication Date Title
US12012629B2 (en) Continuous processing methods for biological products
Rathore et al. Recent developments in membrane-based separations in biotechnology processes
US6214221B1 (en) Method and apparatus for purification of biological substances
KR101238798B1 (ko) 생물학적 분자의 통합된 연속 제조를 위한 장치 및 방법
US7846335B2 (en) Device for chromatographic separations
US20130248451A1 (en) System and process for biopolymer chromatography
CN116003579A (zh) 用于纯化抗体的连续多步骤方法
Brower et al. Monoclonal antibody continuous processing enabled by single use
JP2022519950A (ja) 組換えタンパク質の連続的生産
Hughson et al. Development of a 3‐step straight‐through purification strategy combining membrane adsorbers and resins
US10843104B2 (en) System and process for biopolymer chromatography
JP2023145471A (ja) 容積測定ローディング流量を低減し、そして結合及び溶出クロマトグラフィー精製の生産性を増大するためのインライン生成物濃縮
Mohanty et al. Novel tangential-flow countercurrent cascade ultrafiltration configuration for continuous purification of humanized monoclonal antibody
US20220333060A1 (en) Process for Purifying Target Substances
US20220275024A1 (en) Process for Purifying Monoclocal Antibodies
Van Reis High Performance Tangential Flow Filtration for Bioprocessing Separations

Legal Events

Date Code Title Description
AS Assignment

Owner name: TARPON BIOSYSTEMS, INC., MASSACHUSETTS

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:RANSOHOFF, THOMAS C.;BISSCHOPS, MARC A.T.;SIGNING DATES FROM 20130913 TO 20131211;REEL/FRAME:031778/0072

AS Assignment

Owner name: TARPON BIOSYSTEMS, INC., MASSACHUSETTS

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:RANSOHOFF, THOMAS C.;BISSCHOPS, MARC A.T.;SIGNING DATES FROM 20130913 TO 20131211;REEL/FRAME:032288/0042

AS Assignment

Owner name: PALL CORPORATION, NEW YORK

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:TARPON BIOSYSTEMS INC.;REEL/FRAME:035014/0468

Effective date: 20150223

STPP Information on status: patent application and granting procedure in general

Free format text: DOCKETED NEW CASE - READY FOR EXAMINATION

STPP Information on status: patent application and granting procedure in general

Free format text: NON FINAL ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER

AS Assignment

Owner name: SARTORIUS STEDIM CHROMATOGRAPHY SYSTEMS LTD., UNITED KINGDOM

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:PALL CORPORATION;REEL/FRAME:052659/0621

Effective date: 20200430

STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION