WO2016122722A1 - Process for manufacturing glatiramer acetate product - Google Patents

Process for manufacturing glatiramer acetate product Download PDF

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Publication number
WO2016122722A1
WO2016122722A1 PCT/US2015/051203 US2015051203W WO2016122722A1 WO 2016122722 A1 WO2016122722 A1 WO 2016122722A1 US 2015051203 W US2015051203 W US 2015051203W WO 2016122722 A1 WO2016122722 A1 WO 2016122722A1
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Prior art keywords
aqueous pharmaceutical
pharmaceutical solution
temperature
filter
solution
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Ceased
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PCT/US2015/051203
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French (fr)
Inventor
Rakefet Cohen
Sasson Habbah
Muhammad Safadi
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Teva Pharmaceutical Industries Ltd
Teva Pharmaceuticals USA Inc
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Teva Pharmaceutical Industries Ltd
Teva Pharmaceuticals USA Inc
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Priority to KR1020167028604A priority Critical patent/KR101737295B1/en
Priority to AU2015380381A priority patent/AU2015380381B2/en
Priority to NZ724875A priority patent/NZ724875B2/en
Priority to EP15880609.1A priority patent/EP3113785A4/en
Priority to MX2016011219A priority patent/MX352734B/en
Priority to KR1020177012458A priority patent/KR102268210B1/en
Priority to CA2945537A priority patent/CA2945537C/en
Priority to UAA201610444A priority patent/UA116060C2/en
Priority to RU2017104222A priority patent/RU2669769C2/en
Priority to CN201580071551.XA priority patent/CN107530394B/en
Priority to EA201691790A priority patent/EA028484B1/en
Priority to US15/510,156 priority patent/US20170312331A1/en
Application filed by Teva Pharmaceutical Industries Ltd, Teva Pharmaceuticals USA Inc filed Critical Teva Pharmaceutical Industries Ltd
Priority to BR112016023736A priority patent/BR112016023736A2/en
Priority to JP2017534813A priority patent/JP2018503627A/en
Publication of WO2016122722A1 publication Critical patent/WO2016122722A1/en
Priority to IL247851A priority patent/IL247851A0/en
Priority to ZA2016/06903A priority patent/ZA201606903B/en
Anticipated expiration legal-status Critical
Priority to IL267152A priority patent/IL267152A/en
Priority to IL277601A priority patent/IL277601B/en
Ceased legal-status Critical Current

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    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K38/00—Medicinal preparations containing peptides
    • A61K38/02—Peptides of undefined number of amino acids; Derivatives thereof
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K9/00—Medicinal preparations characterised by special physical form
    • A61K9/14—Particulate form, e.g. powders, Processes for size reducing of pure drugs or the resulting products, Pure drug nanoparticles
    • A61K9/19—Particulate form, e.g. powders, Processes for size reducing of pure drugs or the resulting products, Pure drug nanoparticles lyophilised, i.e. freeze-dried, solutions or dispersions
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K38/00—Medicinal preparations containing peptides
    • A61K38/03—Peptides having up to 20 amino acids in an undefined or only partially defined sequence; Derivatives thereof
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K38/00—Medicinal preparations containing peptides
    • A61K38/16—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
    • A61K47/06—Organic compounds, e.g. natural or synthetic hydrocarbons, polyolefins, mineral oil, petrolatum or ozokerite
    • A61K47/26—Carbohydrates, e.g. sugar alcohols, amino sugars, nucleic acids, mono-, di- or oligo-saccharides; Derivatives thereof, e.g. polysorbates, sorbitan fatty acid esters or glycyrrhizin
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K9/00—Medicinal preparations characterised by special physical form
    • A61K9/0012—Galenical forms characterised by the site of application
    • A61K9/0019—Injectable compositions; Intramuscular, intravenous, arterial, subcutaneous administration; Compositions to be administered through the skin in an invasive manner
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K9/00—Medicinal preparations characterised by special physical form
    • A61K9/08—Solutions
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
    • A61M5/00—Devices for bringing media into the body in a subcutaneous, intra-vascular or intramuscular way; Accessories therefor, e.g. filling or cleaning devices, arm-rests
    • A61M5/178—Syringes
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P21/00—Drugs for disorders of the muscular or neuromuscular system
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P25/00—Drugs for disorders of the nervous system
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P25/00—Drugs for disorders of the nervous system
    • A61P25/14—Drugs for disorders of the nervous system for treating abnormal movements, e.g. chorea, dyskinesia
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P25/00—Drugs for disorders of the nervous system
    • A61P25/28—Drugs for disorders of the nervous system for treating neurodegenerative disorders of the central nervous system, e.g. nootropic agents, cognition enhancers, drugs for treating Alzheimer's disease or other forms of dementia
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P37/00—Drugs for immunological or allergic disorders

Definitions

  • Copaxone® is a clear, colorless to slightly yellow, sterile, nonpyrogenic solution for subcutaneous injection.
  • Each 1 mL of Copaxone® solution contains 20mg or 40mg of GA, the active ingredient, and 40mg of mannitol.
  • the pH of the solutions is approximately 5.5 to 7.0.
  • Copaxone® 20mg/mL in a prefilled syringe (PFS) is an approved product, the safety and efficacy of which are supported by over two decades of clinical research and over a decade of post-marketing experience.
  • Copaxone® 40mg/mL in a PFS was developed as a new formulation of the active ingredient GA.
  • This patent also provides a prefilled syringe containing 40mg of glatiramer acetate and 40mg mannitol, which syringe is prepared by a process of the invention.
  • the aqueous pharmaceutical solution is passed through the second filter at a rate of 3-25 liters/hour.
  • the pressure during the filtering step (ii) and the pressure during the filling step (iii) is maintained below 2.0 bar.
  • the temperature of the aqueous pharmaceutical solution is between 0°C and 14°C, or the temperature of the aqueous pharmaceutical solution is reduced to a temperature between 0°C and 14°C.
  • the process further comprises a step of lyophilizing the filtrate after it has been filled into the suitable container so as to form a lyophilized powder of glatiramer acetate and mannitol in the suitable container.
  • the aqueous pharmaceutical solution comprises glatiramer acetate having a viscosity in the range of 2.3-3.2 cPa.
  • the obtaining step (i) comprises compounding the aqueous pharmaceutical solution in a compounding vessel.
  • the process further comprises the step of reducing the temperature of the first filter to a temperature from above 0°C up to 17.5 °C.
  • compositions of Copaxone® 20mg/mL and Copaxone® 40mg/mL are detailed in Table 1.
  • Water for injection is the most widely used solvent and inert vehicle in parenteral formulations. Water is chemically stable in all physical states. It is the base for many biological life forms, and its safety in pharmaceutical formulations is unquestioned.
  • the first objective of Experiment No. 2 was to evaluate whether local cooling of GA 40mg/mL solution using a Heat Exchanger (HE) could improve the filterability through cooled Filter B compared to filterability of the same bulk solution at controlled room temperature.
  • HE Heat Exchanger
  • Reducing the temperature of the GA 40mg/mL bulk solution in the receiving vessel significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution held under controlled room temperature.

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  • Nuclear Medicine, Radiotherapy & Molecular Imaging (AREA)
  • Proteomics, Peptides & Aminoacids (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
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  • Hospice & Palliative Care (AREA)
  • Psychiatry (AREA)
  • Orthopedic Medicine & Surgery (AREA)
  • Medicinal Preparation (AREA)
  • Medicines That Contain Protein Lipid Enzymes And Other Medicines (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
  • Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)

Abstract

The patent provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of: (i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol; (ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and (iii) filling the suitable container with the filtrate obtained after performing step (ii), so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container. This patent further provides an aqueous pharmaceutical solution comprising 40mg/ml glatiramer acetate and 40mg/ml mannitol, wherein the aqueous pharmaceutical solution a) has a viscosity in the range of 2.0-3.5 cPa; or b) has an osmolality in the range of 275-325 mosmol/Kg. This patent also provides a prefilled syringe, an automated injector and a method of treatment of a human patient.

Description

PROCESS FOR MANUFACTURING GLATIRA ER ACETATE PRODUCT
This application claims priority of U.S. Nonprovisional Application No. 14/608,126, filed January 28, 2015, the entire content of which is hereby incorporated by reference herein.
Throughout this application, various publications are referred to by first author and year of publication. Full citations for these publications are presented in a References section immediately before the claims. The disclosures of these documents and publications referred to herein are hereby incorporated in their entireties by reference into this application in order to more fully describe the state of the art to which this invention pertains.
BACKGROUND OF THE INVENTION
Glatiramer acetate (GA) , the active ingredient of Copaxone®, consists of the acetate salts of synthetic polypeptides, containing four naturally occurring amino acids: L-glutamic acid, L-alanine, L- tyrosine, and L-lysine with an average molar fraction of 0.141, 0.427, 0.095, and 0.338, respectively. The peak average molecular weight of glatiramer acetate is between 5,000 and 9,000 daltons. Glatiramer acetate is identified by specific antibodies (Copaxone, Food and Drug Administration Approved Labeling (Reference ID: 3443331) [online], TEVA Pharmaceutical Industries Ltd., 2014 [retrieved on December 24, 2014], Retrieved from the Internet: <URL: www. accessdata. fda.gov/drugsatfda_docs/label/2014/020622s089lbl .pdf> ) .
Chemically, glatiramer acetate is designated L-glutamic acid polymer with L-alanine, L-lysine and L-tyrosine, acetate (salt) . Its structural formula is:
(Glu,Ala,Lys,Tyr)x.X CH3C00H
(C5H9NO4 . C3H7NO2 . C6H14N2O2. C9HiiN03) x . XC2H4O2
CAS-147245-92-9 Copaxone® is a clear, colorless to slightly yellow, sterile, nonpyrogenic solution for subcutaneous injection. Each 1 mL of Copaxone® solution contains 20mg or 40mg of GA, the active ingredient, and 40mg of mannitol. The pH of the solutions is approximately 5.5 to 7.0. Copaxone® 20mg/mL in a prefilled syringe (PFS) is an approved product, the safety and efficacy of which are supported by over two decades of clinical research and over a decade of post-marketing experience. Copaxone® 40mg/mL in a PFS was developed as a new formulation of the active ingredient GA. Copaxone® 40mg/mL is a prescription medicine used for the treatment of people with relapsing forms of multiple sclerosis (Copaxone, Food and Drug Administration Approved Labeling (Reference ID: 3443331) [online] , TEVA Pharmaceutical Industries Ltd. , 2014 [retrieved on December 24, 2014], Retrieved from the Internet: <URL: www. accessdata. fda.gov/drugsatfda_docs/label/2014/020622s0891bl .pdf> ) .
It is an object of the present invention to provide an improved process for manufacturing GA drug products .
SUMMARY OF THE INVENTION
The patent provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of: (i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and (iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container.
This patent also provides a prefilled syringe containing 40mg of glatiramer acetate and 40mg mannitol, which syringe is prepared by a process of the invention.
This patent further provides an aqueous pharmaceutical solution comprising 40mg/ml glatiramer acetate and 40mg/ml mannitol, wherein the aqueous pharmaceutical solution a) has a viscosity in the range of 2.0-3.5 cPa; or b) has an osmolality in the range of 275-325 mosmol/Kg.
This patent also provides a prefilled syringe containing 1ml of an aqueous pharmaceutical solution prepared by a process of the invention. This patent also provides an automated injector comprising the prefilled syringe prepared by a process of the invention.
Aspects of the present invention relate to a method of treatment of a human patient suffering from a relapsing form of multiple sclerosis comprising administration to the human patient of three subcutaneous injections of a 40 mg/ml dose of glatiramer acetate per week using the prefilled syringe of this invention, using the aqueous pharmaceutical solution of this invention, or using the automated injector of this invention so as to treat the human patient .
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1. Schematic description of filtration process by cooled receiving vessel and filter housing.
Figure 2. Schematic description of filtration process by heat exchanger and cooled filter housing.
Figure 3. Pressure record for Experiment No. 1. * Filtration of GA solution at controlled room temperature was stopped and the remaining solution was transferred to the cooled receiving vessels.
Figure 4. Pressure record for Experiment No. 2. * Pauses of 3 hours and 5 hours for GA solutions filtered at controlled room temperature and at reduced temperature, respectively. ** Pause of 10 hours for both GA solutions. *** Filtration of GA solution at controlled room temperature was stopped. Remaining GA solution was filtered at reduced temperature. Figure 5. Pressure record for Experiment No. 3.
Figure 6. Schematic description of filtration process by cooled compounding vessel and cooled filter housings on both Filter A and Filter B.
Figure 7. Schematic description of filtration process by heat exchanger and cooled filter housings on both Filter A and Filter B.
Figure 8. Schematic description of filtration process by cooled filter housing on only Filter B.
Figure 9. Schematic description of filtration process by cooled filter housings on both Filter A and Filter B. Figure 10. Schematic description of filtration process by cooled compounding vessel .
Figure 11. Schematic description of filtration process by cooled receiving vessel. DETAILED DESCRIPTION OF THE INVENTION
This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of:
(i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and (iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container.
In some embodiments the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, or a first filter and a second filter.
In some embodiments the process further comprises the step of reducing the temperature of the second filter to a temperature from above 0°C up to 17.5°C. In some embodiments the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C before passing through the second filter.
In some embodiments the filtering step (ii) further comprises the step of receiving the aqueous pharmaceutical solution filtered through the first filter in a receiving vessel.
In some embodiments the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C after leaving the receiving vessel and before entering into the second filter. In some embodiments the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the receiving vessel . In some embodiments the process further comprises the step of reducing the temperature of the first filter to a temperature from above 0°C up to 17.5°C.
In some embodiments the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C before passing through the first filter.
In some embodiments the obtaining step (i) comprises compounding the aqueous pharmaceutical solution in a compounding vessel .
In some embodiments the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C after leaving the compounding vessel and before entering into the first filter.
In some embodiments the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the compounding vessel.
In some embodiments the aqueous pharmaceutical solution is passed through the second filter at a rate of 3-25 liters/hour.
In some embodiments the aqueous pharmaceutical solution is passed through the second filter preferably at a rate of 3-22 liters/hour.
In some embodiments the aqueous pharmaceutical solution is passed through the second filter more preferably at a rate of 3-15 liters/hour.
In some embodiments the aqueous pharmaceutical solution is passed through the second filter at a rate more preferably at a rate of 3- 10 liters/hour. In some embodiments the pressure during the filtering step (ii) and the pressure during the filling step (iii) is maintained below 5.0 bar.
In some embodiments the pressure during the filtering step (ii) and the pressure during the filling step (iii) is maintained preferably below 3.0 bar.
In some embodiments the pressure during the filtering step (ii) and the pressure during the filling step (iii) is maintained below 2.0 bar. In some embodiments the temperature of the aqueous pharmaceutical solution is between 0°C and 14°C, or the temperature of the aqueous pharmaceutical solution is reduced to a temperature between 0°C and 14°C.
In some embodiments the temperature of the aqueous pharmaceutical solution is between 0°C and 12 °C, or the temperature of the aqueous pharmaceutical solution is reduced to a temperature between 0°C and 12°C.
In some embodiments the temperature of the aqueous pharmaceutical solution is 2°C - 12°C, or the temperature of the aqueous pharmaceutical solution is reduced to 2°C - 12°C.
In some embodiments the temperature of the aqueous pharmaceutical solution is 4°C - 12°C, or the temperature of the aqueous pharmaceutical solution is reduced to 4°C - 12 °C.
In some embodiments the filtering is performed using a sterilizing filter having a pore size of 0.2μπι or less, wherein the first, the second or both filters are a sterilizing filter having a pore size of 0.2μπι or less.
In some embodiments the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution comprising 20mg/ml glatiramer acetate and 40mg/ml mannitol . In some embodiments the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution comprising 40mg/ml glatiramer acetate and 40mg/ml mannitol.
In some embodiments the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution having a pH in the range of 5.5-7.0.
In some embodiments the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution which is a sterilized aqueous solution which has been sterilized by filtration and without subjecting the aqueous pharmaceutical solution to heat, chemicals, or radiation exposure.
In some embodiments the pharmaceutical preparation is a lyophilized powder of glatiramer acetate and mannitol .
In some embodiments the process further comprises a step of lyophilizing the filtrate after it has been filled into the suitable container so as to form a lyophilized powder of glatiramer acetate and mannitol in the suitable container.
In some embodiments the suitable container is a syringe, vial, ampoule, cartridge or infusion. In some embodiments the suitable container is a syringe.
In some embodiments the syringe contains 1ml of an aqueous pharmaceutical solution.
This invention provides a prefilled syringe containing 40mg of glatiramer acetate and 40mg mannitol, which syringe is prepared by a process of the invention.
According to any embodiment of the prefilled syringe disclosed herein, the prefilled syringe contains 1ml of an aqueous pharmaceutical solution of 40mg/ml of glatiramer acetate and 40mg/ml mannitol . According to any embodiment of the prefilled syringe disclosed herein, the aqueous pharmaceutical solution a) has a viscosity in the range of 2.0-3.5 cPa; or b) has an osmolality in the range of 270-330 mosmol/Kg.
According to any embodiment of the prefilled syringe disclosed herein, the aqueous pharmaceutical solution a) has a viscosity in the range of 2.2-3.0 cPa; or b) has an osmolality in the range of 275-325 mosmol/Kg.
This invention provides an aqueous pharmaceutical solution comprising 40mg/ml glatiramer acetate and 40mg/ml mannitol, wherein the aqueous pharmaceutical solution a) has a viscosity in the range of 2.0-3.5 cPa; or b) has an osmolality in the range of 275-325 mosmol/Kg.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution has a viscosity in the range of 2.0-3.5 cPa. According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution has a viscosity in the range of 2.61-2.92 cPa.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution has an osmolality in the range of 275-325 mosmol/Kg.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution has an osmolality in the range of 300-303 mosmol/Kg.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution comprises glatiramer acetate having a viscosity in the range of 2.3-3.2 cPa.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution comprises glatiramer acetate having a viscosity in the range of 2.6-3.0 cPa. According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution comprises glatiramer acetate having an osmolality in the range of 290-310 mosmol/Kg.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution comprises glatiramer acetate having an osmolality in the range of 295-305 mosmol/Kg.
According to some embodiments of the aqueous pharmaceutical solution, the aqueous pharmaceutical solution has a pH in the range of 5.5-7.0. This invention provides a prefilled syringe containing 1ml of an aqueous pharmaceutical solution prepared by the invention.
This invention provides an automated injector comprising the prefilled syringe prepared by the invention.
This invention provides a method of treatment of a human patient suffering from a relapsing form of multiple sclerosis comprising administration to the human patient of three subcutaneous injections of a 40 mg/ml dose of glatiramer acetate per week using the prefilled syringe of this invention, using the aqueous pharmaceutical solution of this invention, or using the automated injector of this invention so as to treat the human patient.
In some embodiments, the human patient is suffering from relapsing-remitting multiple sclerosis.
In some embodiments, the human patient has experienced a first clinical episode and has MRI features consistent with multiple sclerosis.
This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of:
(i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol; (ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and
(iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container.
In an embodiment, the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, and a second filter.
In an embodiment, the obtaining step (i) comprises compounding the aqueous pharmaceutical solution in a compounding vessel.
In an embodiment, the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the compounding vessel .
In an embodiment, the process further comprises the step of reducing the temperature of the first filter to a temperature from above 0°C up to 17.5°C. In an embodiment, the process further comprises the step of reducing the temperature of the second filter to a temperature from above 0°C up to 17.5°C.
This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of:
(i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and (iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container. In an embodiment, the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, and a second filter.
In an embodiment, the obtaining step (i) comprises compounding the aqueous pharmaceutical solution in a compounding vessel. In an embodiment, the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C after leaving the compounding vessel and before entering into the first filter.
In an embodiment, the process further comprises the step of reducing the temperature of the first filter to a temperature from above 0°C up to 17.5°C.
In an embodiment, the process further comprises the step of reducing the temperature of the second filter to a temperature from above 0°C up to 17.5°C. This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of:
(i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at temperature of from above 0°C up to 17.5°C to produce filtrate; and
(iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container. In an embodiment, the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, and a second filter.
In an embodiment, the process further comprises the step of reducing the temperature of the second filter to a temperature from above 0°C up to 17.5°C.
This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of:
(i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and
(iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container.
In an embodiment, the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, and a second filter.
In an embodiment, the process further comprises the step of reducing the temperature of the first filter to a temperature from above 0°C up to 17.5 °C.
In an embodiment, the process further comprises the step of reducing the temperature of the second filter to a temperature from above 0°C up to 17.5 °C.
This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of: (i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and
(iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container. In an embodiment, the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, and a second filter.
In an embodiment, the obtaining step (i) comprises compounding the aqueous pharmaceutical solution in a compounding vessel. In an embodiment, the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the compounding vessel.
This invention provides a process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of:
(i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and
(iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container. In an embodiment, the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, and a second filter.
In an embodiment, the filtering step (ii) further comprises the step of receiving the aqueous pharmaceutical solution filtered through the first filter in a receiving vessel.
In an embodiment, the process further comprises the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the receiving vessel.
Automated Injection Device
The mechanical workings of an automated injection assisting device can be prepared according to the disclosure in European application publication No. EP0693946 and U.S. Patent No. 7,855,176, which are incorporated herein by reference.
All combinations of the various elements described herein are within the scope of the invention.
Definitions
As used herein, "glatiramer acetate" is a complex mixture of the acetate salts of synthetic polypeptides, containing four naturally occurring amino acids: L-glutamic acid, L-alanine, L-tyrosine, and L-lysine. The peak average molecular weight of glatiramer acetate is between 5,000 and 9,000 daltons . Chemically, glatiramer acetate is designated L-glutamic acid polymer with L-alanine, L-lysine and L- tyrosine, acetate (salt). Its structural formula is:
(Glu,Ala,Lys,Tyr)x.X CH3COOH
(C5H9N04.C3H7N02.C6H14N202.C9H11N03) x.x C2H402 CAS-147245-92-9
As used herein "glatiramer acetate drug substance" is the glatiramer acetate active ingredient prior to its formulation into a glatiramer acetate drug product .
As used herein, a "glatiramer acetate drug product" is a formulation for pharmaceutical use which contains a glatiramer acetate drug substance. Copaxone® is a commercial glatiramer acetate drug product manufactured by TEVA Pharmaceutical Industries Ltd. (Israel) , which is described in Copaxone, Food and Drug Administration Approved ■ Labeling (Reference ID: 3443331) [online], TEVA Pharmaceutical Industries Ltd., 2014 [retrieved on December 24, 2014], Retrieved from the Internet : <URL : www. accessdata. fda.gov/drugsatfda_docs/label/2014/020622s0891bl .pdf> , the contents of which are hereby incorporated by reference. Copaxone® is available as 20mg/mL administered once per day, and/or 40mg/ml administered three times per week.
As used herein, a "sterilizing filter" is a filter with a pore size of 0.2 μηι or less which will effectively remove microorganisms.
By any range disclosed herein, it is meant that all hundredth, tenth and integer unit amounts within the range are specifically disclosed as part of the invention. Thus, for example, 1 mg to 50 mg means that 1.1, 1.2 . . . 1.9; and 2, 3 . . . 49 mg unit amounts are included as embodiments of this invention.
This invention will be better understood by reference to the Experimental Details which follow, but those skilled in the art will readily appreciate that the specific experiments detailed are only illustrative of the invention as described more fully in the claims which follow thereafter.
Experimental Details
Methods
Glatiramer Acetate (GA) Injection 40mg/mL in a prefilled syringe (GA injection 40mg/mL in PFS or Copaxone® 40mg/mL) was developed as a new formulation of the active ingredient glatiramer acetate, which is also used in the marketed product Copaxone® 20mg/mL solution for injection in a prefilled syringe. Copaxone® 40mg/mL is to be administered three times a week by subcutaneous injection to patients with Relapsing Remitting Multiple Sclerosis. The new formulation is based on the formulation of the marketed Copaxone® 20mg/mL solution for injection in a prefilled syringe. Copaxone® 20mg/mL is an approved product, the safety and efficacy of which are supported by over two decades of clinical research and over a decade of post -marketing experience. The only difference between the formulations is the double amount of the active substance used, which results in a solution with double the concentration of glatiramer acetate (40mg/mL vs. 20mg/mL) . The amount of mannitol in both Copaxone® formulations remains unchanged (40mg/mL) .
The compositions of Copaxone® 20mg/mL and Copaxone® 40mg/mL are detailed in Table 1.
Table 1. Compositions of Copaxone® 20mg/mL and Copaxone® 40xtvg/mL
Figure imgf000020_0001
1. Calculated on the dry basis and 100% assay
Studies were conducted in order to verify that the formulation of Copaxone® 40mg/mL, its manufacturing process and chemical, biological and microbiological attributes are appropriate for commercialization. Studies were also conducted to confirm the suitability of the proposed container closure system for packaging Copaxone® 40mg/mL.
Mannitol was chosen as the tonicity agent for the initially formulated Copaxone® (freeze dried product, reconstituted prior to administration) as it is also a bulking agent. When the currently marketed ready-to-use formulation of Copaxone® 20mg/mL solution for injection prefilled syringe was developed, mannitol was used in this formulation as well, as the osmoregulator . Finally, when the new 40mg/mL formulation was developed, based on the Copaxone® 20mg/mL formulation, mannitol remained as the osmoregulator.
Mannitol is widely used in parenteral formulations as an osmoregulator. It is freely soluble in water and stable in aqueous solutions. Mannitol solutions may be sterilized by filtration. In solution, mannitol is not affected by atmospheric oxygen in the absence of catalysts. The concentration of mannitol in the Copaxone® 40mg/mL is 40mg/mL. Maintaining the mannitol concentration in Copaxone® 40mg/mL resulted in an essentially isotonic solution.
Water for injection (WFI) is the most widely used solvent and inert vehicle in parenteral formulations. Water is chemically stable in all physical states. It is the base for many biological life forms, and its safety in pharmaceutical formulations is unquestioned.
Example 1
The manufacturing process of Copaxone® 40mg/mL comprises: · Compounding a bulk solution of GA and mannitol in water for injections ( FI) .
• Sterilizing filtration of the bulk solution yielding the sterile GA solution in bulk.
• Aseptic filling of sterile bulk solution into syringe barrels and stoppering.
• Inspection and final assembly of the filled syringes.
Initially, filtration of bulk solution from the compounding vessel was performed through a sequential filter train consisting of two sequential sterilizing filters (filters named Ai and A2, respectively) to a receiving vessel. From the receiving vessel it was transferred to the intermediate vessel in the filling machine and further through dosing pumps and needles into prefilled syringes. However, due to a Health Authority request to place the sterilizing filter as close as possible to the filling point, the second sterilizing filter was moved between the receiving and intermediate vessels. In the current filtration train, the first sterilizing filter was named Filter A, and the second relocated sterilizing filter was named Filter B. See, Figure 1.
In line with the process for the approved Copaxone® 20mg/mL formulation, all processing steps of the new Copaxone® 40mg/mL formulation were originally conducted at controlled room temperature. However, filtration of the higher concentration solution resulted in a pressure build-up on the second filter, Filter B. Despite the observed pressure increase on Filter B, a high-quality drug product could be obtained by filtration of GA 40mg/mL at controlled room temperature, as confirmed by release and stability data. Nevertheless, an improved filtration process was needed which avoided the build-up on the second filter.
Flow rate for fluids can be defined by the differential pressure, and inversely moderated by viscosity. Viscosity, in turn, is usually reciprocal in relation to temperature (Meltzer and Jornitz, Filtration and Purification in the Biopharmaceutical Industry, Second Edition, CRC Press, 2007, page 166) . Increasing the temperature of a solution will normally decrease the viscosity, thereby enhancing the flow rate . In an attempt to solve the pressure build-up problem on the second filter, the temperature condition of the filtration was raised above controlled room temperature. Although the viscosity decreased, the filterability decreased, resulting in a failed attempt.
The following studies were performed: · Filter Validation Study: Determination of ranges for the manufacturing parameters related to sterilizing Filter A and sterilizing Filter B of the bulk solution, as well as confirmation of filter compatibility with the drug product.
• Filtration Process: Selection of the sterilizing filtration conditions best suitable for the manufacturing process and the quality of the drug product.
Filters Used for Copaxone® 20mg/mL and Copaxone® 40mg/mL Manufacturing
The manufacturing process of Copaxone® 40mg/mL was based on the process used to produce the marketed Copaxone® 20mg/mL solution for injection in a prefilled syringe. Therefore the same filters used for filtration of marketed product were used.
Two sterilizing filters were used, each of which having a pore size of 0.2μπν or less, to effectively remove microorganisms. Sterilization is achieved only by filtration using sterilizing filters and not by using other methods, e.g. sterilization is achieved without using heat, chemicals, or radiation exposure. Filter Validation Study - Confirmation and Setting of Parameters Associated with Filter Compatibility and with Sterilizing Filtration
The following tests were performed in order to confirm the filter validity: · Extractables testing - assessment of extractables released from the filter upon steam sterilization and their removal from the filter by a model solvent, thus assessing the volume to be discarded after the filtration through the Filter B, prior to beginning of the aseptic filling. · Compatibility/adsorption testing - assessment of the chemical compatibility of GA 20mg/mL and GA 40mg/mL solution with the filter material and the extent of its adsorption to the filter, thus assessing the volume to be discarded after the filtration through Filter B, prior to beginning of the aseptic filling in order to provide assay within specifications.
• Residual effect - To ensure that no significant residual GA 20mg/mL or GA 40mg/mL solution that might affect the post use integrity test remains on the filter after filtration.
• Bacterial challenge - To ensure that the filtration process does not affect the ability of the filter to provide a sterile solution.
The above tests were conducted using maximum pressure (up to 5.0 bar) . The validation study demonstrated that the selected filtration system is capable of providing a high quality Copaxone® 20mg/mL and Copaxone® 4Omg/mL . Given the strict and well-defined operational and equipment parameters of the GA 4Omg/mL solution filtration process, a plan to mitigate the potential increase in pressure by reducing the filtration temperature was developed.
Without much expectations, it was decided to examine the filtration process of GA 40mg/mL sterile bulk solution through Filter B under reduced temperature conditions, using the same filters and filtration train as for the filtration at controlled room temperature .
Accordingly, experiments were performed in order to compare the filtration of GA 40mg/mL sterile bulk solution through Filter B under reduced temperature and controlled room temperature in the production environment and to ensure that there is no difference with regard to the quality and stability profiles of the filtered solutions. In all experiments, the sterile bulk solution was prepared according to the standard compounding and filtration train (see Figure 1) and filtered through two filters: Filter A and Filter B.
The experiments tested two different cooling technologies (cooled receiving vessels vs heat exchanger) with cooled filter. The studies are schematically depicted in Figure 1 and Figure 2. Further details about these experiments and their outcomes are provided hereafter.
Filtration Process - Experiment No. 1
The objective of Experiment No. 1 was to compare the filterability of a batch of bulk solution held and filtered through Filter B at either controlled room temperature or under reduced temperature conditions (cooling by double-jacketed receiving vessel and cooled Filter B housing) .
The study is schematically depicted in Figure 1. The experimental design and the obtained results are summarized in Table 2 and Figure 3.
Table 2. Experimental Design and Results for Experiment No. 1.
Experiment Outline Reduced Temperature Controlled Room
Filtration Temperature Filtration
Compounding According to standard manufacturing procedure1
Holding time 13 hours 13 hours
the receiving
vessel
Temperature of 6.6-10.7°C2 17.8-24.6°C
solution held in
the receiving
vessel
Planned regimen Intermittent filtration:
for filtration Stage 1 - 5 filtration steps of filtration of though Filter B3
about 10 liters of bulk solution - followed by- pauses of about 50 minutes each, followed by a pause of 5 hours.
Stage II - 4 filtration steps of filtration of about 10 liters of bulk solution - followed by pauses of about 50 minutes each, followed by a pause of about 10 hours.
Stage III - Filtration of remaining solution.
Total volume of About 125L. Filtration About 85 liters.
bulk solution was completed. Filtration was stopped filtered due to increase in
pressure on Filter B.
One bulk solution was prepared and divided into two portions . Bulk solution size: 230 liters. Filtration of solution at controlled room temperature was stopped after 85 liters have been pushed through the filter due to increased pressure and the remaining solution was transferred to the cooled receiving vessels.
The temperature increased (to 14.9°C) once during the filtration following the addition of the remaining solution kept at ambient temperature .
The filtrations were carried out in parallel.
Surprisingly, filtration at reduced temperature allowed filtration to be completed without the pressure increase associated with filtration at controlled room temperature.
Example 2 Filtration Process - Experiment No. 2
The first objective of Experiment No. 2 was to evaluate whether local cooling of GA 40mg/mL solution using a Heat Exchanger (HE) could improve the filterability through cooled Filter B compared to filterability of the same bulk solution at controlled room temperature.
The second objective of Experiment No. 2 was to confirm that there is no difference in the quality of the drug product filled into syringes at controlled room temperature and drug product filled into syringes at reduced temperature . Cooling by heat exchanger was evaluated as it seemed to be much easier to steam sterilize than using the double jacketed receiving vessels. The HE was located between the receiving vessel and Filter B. Consequently, as opposed to Experiment No. 1 (in which the solution was cooled by the double-jacketed receiving vessels following filtration through Filter A and kept cooled prior to filtration through Filter B) , the solution in this experiment was held at controlled room temperature prior to filtration of the locally cooled (by HE) GA solution through Filter B.
The study is schematically depicted in Figure 2. The experimental design and the obtained results are summarized in Table 3. The pressure observed over the course of the filling process of Experiment No. 2 is shown in Figure 4. Table 3. Experimental Design and Results for Experiment No. 2 .
Figure imgf000027_0001
1 One bulk solution was prepared and divided into two portions. Bulk solution size: 230 liters.
2 Both filtration processes (reduced and controlled room temperature) were carried out in parallel for comparison. At each stage, filtration was carried out at controlled room temperature, followed by filtration at reduced temperature.
3 Filtration of solution at controlled room temperature was stopped due to pressure increase and the remaining solution was filtered at reduced temperature. Example 3
Filtration Process - Experiment No. 3
One objective of Experiment No. 3 was to confirm whether cooling of GA 40mg/mL bulk solution prior to filtration, using HE and cooled filter housing, allows filtration and filling of batches of 130L size within various manufacturing regimens.
Another objective of Experiment No. 3 was to evaluate the influence of holding time at various stages of the manufacturing process on filterability of GA 40mg/mL. Another objective of Experiment 3 was to demonstrate with a high degree of assurance that locally cooled GA 40mg/mL solution filtered through Filter B is not different in its quality and stability profile from GA 40mg/mL solution filtered through Filter B at controlled room temperature conditions with regard to pre-determined parameters and limits.
A series of three batches of bulk solution, manufactured at various regimens, were prepared. Each bulk solution was prepared from an identical combination of the same three drug substance batches .
The experimental design and results are summarized in Table 4.
Table 4. Experimental Design and Results for Experiment No. 3
Figure imgf000029_0001
1 Batches A and A-2 are from the same bulk solution. Filter B was replaced with a new filter prior to filtration of A-2.
2 Compounding and subsequent holding time in the compounding vessel (incl. filtration through filter A) .
3 Time from end of filtration through Filter A to beginning of filtration through Filter B and filling.
4 Since A-2 was filtered and filled into syringes subsequent to the filtration and filling of A, the stated holding time represents the sum of the holding time of A in addition to the time A-2 was held until the filtration at controlled room temperature was initiated.
5 Throughout the filling, gradual increase of filtration pressure was required in order to maintain flow rate that would correspond to the rate required for continuous filling. Based on the results of Experiment No. 3, it was confirmed that local cooling by heat exchanger is sufficient in order to enable filtration of a 130L batch. In addition, the quality and stability- profile of GA 40mg/mL solutions filtered at controlled room temperature and reduced temperature were found to be substantially identical .
Example 4
Cooling of GA 40mg/mL bulk solution below 17.5°C in the compounding vessel before passing through cooled Filter A and cooled Filter B in sequence (see Figure 6) results in lower pressure during the filtration step of both Filter A and Filter B as compared to the holding the same bulk solution in the compounding vessel and passing it through Filter A and Filter B at controlled room temperature (Cooling of the bulk solution by using double jacketed compounding vessel and cooling the filters by using double jacketed filter housings) .
Reducing the temperature of the GA 40mg/mL bulk solution in the compounding vessel and passing it through cooled Filter A and Filter B in sequence (see Figure 6) significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution held and filtered under controlled room temperature.
Example 5
Local cooling of GA 40mg/mL bulk solution by a heat exchanger and passing the solution through cooled Filter A and cooled Filter B in sequence (see Figure 7) results in lower pressure during the filtration step of both Filter A and Filter B as compared to passing the same bulk solution held and filtered under controlled room temperature . Reducing the temperature of the GA 40mg/mL bulk solution using a heat exchanger and passing it through cooled Filter A and cooled Filter B in sequence (see Figure 7) significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution held and filtered under controlled room temperature .
Example 6 Passing the sterilized GA 40mg/mL bulk solution from the receiving vessel through cooled Filter B (see Figure 8) significantly results in lower pressure during the filtration step compared to passing the same bulk solution filtered through Filter B under controlled room temperature . Passing the sterilized GA 40mg/mL bulk solution from the receiving vessel through cooled Filter B (see Figure 8) significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution held and filtered under controlled room temperature.
Example 7
Passing GA 40mg/mL bulk solution from the compounding vessel through cooled Filter A and cooled Filter B in sequence (see Figure 9) results in lower pressure during the filtration step of both Filter A and Filter B as compared to passing the same bulk solution filtered under controlled room temperature.
Passing GA 40mg/mL bulk solution from the receiving vessel through cooled Filter A and Filter B in sequence (see Figure 9) significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution filtered under controlled room temperature.
Example 8
Cooling of GA 40mg/mL bulk solution below 17.5°C in the compounding vessel before passing through Filter A and Filter B in sequence (see Figure 10) results in lower pressure during the filtration step of both Filter A and Filter B as compared to the holding the same bulk solution in the compounding vessel and passing it through Filter A and Filter B at controlled room temperature (Cooling of the bulk solution by using double jacketed compounding vessel) .
Reducing the temperature of the GA 40mg/mL bulk solution in the compounding vessel and passing it through Filter A and Filter B in series (see Figure 10) significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution held and under controlled room temperature. Example 9
Cooling of GA 40mg/mL bulk solution below 17.5°C in the receiving vessel before passing through Filter B (see Figure 11) results in lower pressure during the filtration step of Filter B as compared to the holding the same bulk solution , in the compounding vessel at controlled room temperature (Cooling of the bulk solution by using double jacketed compounding vessel) .
Reducing the temperature of the GA 40mg/mL bulk solution in the receiving vessel (see Figure 10) significantly reduces impairment of filterability caused by the total duration of the process (holding time) as well as by filtering larger volume, compared to the same bulk solution held under controlled room temperature.
Discussion of Examples 1-9
Reducing the temperature of GA 40mg/mL sterile bulk solution significantly improved its filterability, as demonstrated by the much lower increase in pressure on Filter B during filtration and filling and by the larger volume that can be filtered at reduced temperature. Pressure increases were observed when the sterile bulk solution was held and filtered at controlled room temperature, while there was no significant increase in the pressure when the solution was filtered under reduced temperature conditions.
The holding time of the bulk solution during filtration through Filter B negatively affects the filterability of the solution. However, the total duration of the process (holding time) impaired the filterability significantly less when filtration was performed under reduced temperature conditions. Consequently, longer holding time can be used with reduced temperature filtration.
Both cooling of the solution by passing it through a heat exchanger (local cooling) and/or cooling of the whole bulk (e.g. by double- jacketed receiving vessel) before filtration through cooled Filters A or B or A and B were found to be suitable solutions for reduced temperature filtration.
Accumulated stability data indicate that there is no substantial difference with regard to quality and stability profile between the solution filtered under reduced temperature conditions and the solution filtered at controlled room temperature.
In sum, the performed experiments show that reduced temperature filtration through Filter B significantly improved the filterability of GA 40mg/mL solution compared to the filterability of the solution when filtered at controlled room temperature. Moreover, reducing the temperature of the bulk solution during the compounding stage or before passing through Filter A, or reducing the temperature of Filter A also improves the filterability of GA 40mg/mL solution compared to the filterability of the solution at controlled room temperature .
Consequently, the proposed manufacturing process for commercial batches of GA 20mg/mL and GA 40mg/mL includes cooling of the solution prior to filtration of the bulk solution through Filter B. Example 10
Container Closure System
The container closure systems selected for the Copaxone® 40mg/mL are the same as those used for the marketed product Copaxone® 20mg/mL PFS. The container closure system consists of a colorless glass barrel, a plastic plunger rod and a grey rubber stopper.
Long Term and Accelerated Stabilit Studies Satisfactory stability data after up to 36 months storage under long-term storage conditions (5°C ± 3°C) and after 6 months storage under accelerated conditions (25° ± 2°C/60± 5% RH) are available. The data demonstrate that the proposed container closure systems are suitable for protection and maintenance of the drug product quality throughout its proposed shelf-life.
Protection from Light
Marketed Copaxone® should be stored protected from light. Based on this recommendation, it is proposed that Copaxone® 40mg/mL be similarly packed in PVC transparent blisters inside a carton box, which provides light protection. The light protection of the proposed packaging when used for the Copaxone® 40mg/mL is recommended in accordance with the results obtained from a photostability study comparing the following packaging configurations:
1. Glass barrel syringe and plunger rod (Primary package);
Glass barrel syringe and plunger rod in a transparent blister (partial secondary package) ;
Glass barrel syringe and plunger rod in a transparent blister inside carton box (complete intended packaging configuration) .
As a reference, the following configurations were added:
2. Glass barrel syringe and plunger rod wrapped in aluminum foil;
Glass barrel and plunger rod in a transparent blister wrapped in aluminum foil.
All packages were simultaneously exposed to standardized sunlight (5 KLUX) for 10 days and to near UV light for additional 5 days.
All the obtained results from the photostability study are within the specifications. However, the impurity peak detected is lower when the drug product is packed in its complete packaging configuration. The carton box was shown to improve the photostability and gives light protection as good as that of aluminum foil, which is regarded as a complete light protector. The intended packaging configuration is therefore considered suitable for its use.
A storage statement to protect the product from light exposure should be added to the product label .
Microbiological Attributes
The medicinal product is a sterile, single dose, parenteral dosage form. Sterilization is achieved by sterile filtration.
A microbial limits test is performed for the drug substance. The sterility and bacterial endotoxins are monitored upon release and throughout stability studies of the drug product, using pharmacopoeia methods. The limits applied are identical to those applied for the marketed Copaxone®.
The same container closure systems are used for the Copaxone® 20mg/mL and Copaxone® 40mg/mL. The integrity testing studies performed to demonstrate the efficacy of the container closure systems on use for the marketed product are also considered relevant for Copaxone® 40mg/mL.
Example 11 Viscosity
The average viscosity of batches of Copaxone® 20mg/mL filtered under controlled room temperature and the average viscosity of batches of Copaxone® 40mg/mL filtered under reduced temperature were obtained and compared. The average viscosity of different batches of Copaxone® 20mg/mL filtered under controlled room temperature are reported in Table 5. The average viscosity of different batches of Copaxone® 40mg/mL filtered under reduced temperature are reported in Table 6.
Table 5. Viscosity of Batches of Copaxone® 20mg/mL Filtered Under Controlled Room Temperature Batch No. Average Standard
Viscosity [cPa] Deviation
1 1.921 0.03
2 1.581 0.00
3 1.581 0.00
4 1.572 0.00
5 1.672 0.01
Water for 0.932 0.00
Injection
Average 1.664
1 Each value is an average of 3 individual results. Values obtained using Rheocalc V2.5 Model LV, Spindle CP40, speed 80 rpm, Shear Rate 600 1/sec, Temperature 25°C±0.1
2 Each value is an average of 6 individual results. Values obtained using Rheocalc V2.5 Model LV, Spindle CP40, speed 80 rpm, Shear Rate 600 1/sec, Temperature 25"C±0.1
Table 6. Viscosity of Batches of Copaxone® 40mg/mL Filtered Under Reduced Temperature
Figure imgf000036_0001
1 Each value is an average of 6 individual results. Values obtained using Rheocalc V2.5 Model LV, Spindle CP40, speed 80 rpm, Shear Rate 600 1/sec, Temperature 25°C±0.1
Osmolality
The osmolality of batches of Copaxone® 20mg/mL filtered under controlled room temperature and the osmolality of batches of Copaxone® 0mg/mL filtered under reduced temperature were measured. Samples from each batch were tested in triplicates . The results are reported in Table 7 .
Table 7. Osmolality of Batches of Copaxone® 20mg/mL Filtered Under Controlled Room Temperature and Batches of Copaxone® 40mg/mL Filtered Under Reduced Temperature
Figure imgf000038_0001
1 Calculated from 4 measurements. The results show that the osmolality of batches of Copaxone® 40mg/mL were well within the ranges of an isotonic solution. The results also show that the batches of Copaxone® 40mg/mL conformed to the general parenteral drug product osmolality limits of 300 ±30 mosmol/Kg. Further, the results indicate that batches of Copaxone® 20mg/mL were slightly hypotonic.

Claims

What is claimed:
1. A process of preparing a pharmaceutical preparation of glatiramer acetate and mannitol in a suitable container comprising the steps of: (i) obtaining an aqueous pharmaceutical solution of glatiramer acetate and mannitol;
(ii) filtering the aqueous pharmaceutical solution at a temperature of from above 0°C up to 17.5°C to produce a filtrate; and
(iii) filling the suitable container with the filtrate obtained after performing step (ii) , so as to thereby prepare the pharmaceutical preparation of glatiramer acetate and mannitol in the suitable container.
2. The process of claim 1, wherein the filtering step (ii) comprises filtering the aqueous pharmaceutical solution through a first filter, or a first filter and a second filter.
3. The process of claim 2 further comprising the step of reducing the temperature of the second filter to a temperature from above 0°C up to 17.5°C.
4. The process of claim 2 or claim 3 further comprising the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C before passing through the second filter.
5. The process of any one of claims 2-4, wherein the filtering step (ii) further comprises the step of receiving the aqueous pharmaceutical solution filtered through the first filter in a receiving vessel .
6. The process of claim 5 further comprising the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C after leaving the receiving vessel and before entering into the second filter.
The process of claim 5 or claim 6 further comprising the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the receiving vessel.
The process of any one of claims 2-7 further comprising the step of reducing the temperature of the first filter to a temperature from above 0°C up to 17.5°C.
The process of any one of claims 2-8 further comprising the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C before passing through the first filter.
The process of any one of claims 2-9, wherein the obtaining step (i) comprises compounding the aqueous pharmaceutical solution in a compounding vessel.
The process of claim 10 further comprising the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C after leaving the compounding vessel and before entering into the first filter.
The process of claim 10 or claim 11 further comprising the step of reducing the temperature of the aqueous pharmaceutical solution to a temperature from above 0°C up to 17.5°C while in the compounding vessel.
The process of any one of claims 2-14, wherein the aqueous pharmaceutical solution is passed through the second filter at a rate of 3-25 liters/hour; preferably at a rate of 3-22 liters/hour; more preferably at a rate of 3-15 liters/hour; or more preferably at a rate of 3-10 liters/hour.
The process of any one of claims 1-12, wherein the pressure during the filtering step (ii) and the pressure during the filling step (iii) is maintained below 5.0 bar; or preferably below 3.0 bar .
The process of any one of claims 1-13, wherein the pressure during the filtering step (ii) and the pressure during the filling step (iii) is maintained below 2.0 bar.
The process of any one of claims 1-15, wherein the temperature of the aqueous pharmaceutical solution is between 0°C and 14 °C, or the temperature of the aqueous pharmaceutical solution is reduced to a temperature between 0°C and 14°C.
The process of any one of claims 1-15, wherein the temperature of the aqueous pharmaceutical solution is between 0°C and 12°C, or the temperature of the aqueous pharmaceutical solution is reduced to a temperature between 0°C and 12°C.
The process of any one of claims 1-15, wherein the temperature of the aqueous pharmaceutical solution is 2°C - 12 °C, or the temperature of the aqueous pharmaceutical solution is reduced to 2°C - 12 °C.
The process of any one of claims 1-15, wherein the temperature of the aqueous pharmaceutical solution is 4°C - 12 °C, or the temperature of the aqueous pharmaceutical solution is reduced to 4°C - 12 °C.
The process of any one of claims 1-19, wherein the filtering is performed using a sterilizing filter having a pore size of 0.2μπι or less, wherein the first, the second or both filters are a sterilizing filter having a pore size of 0.2μπι or less.
The process of any one of claims 1-20, wherein the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution comprising 20mg/ml glatiramer acetate and 40mg/ml mannitol .
The process of any one of claims 1-20, wherein the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution comprising 40mg/ml glatiramer acetate and 40mg/ml mannitol.
The process of any one of claims 1-22, wherein the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution having a pH in the range of 5.5-7.0.
The process of any one of claims 1-23, wherein the pharmaceutical preparation in the suitable container is an aqueous pharmaceutical solution which is a sterilized aqueous solution which has been sterilized by filtration and without subjecting the aqueous pharmaceutical solution to heat, chemicals, or radiation exposure.
The process of any one of claims 1-20, wherein the pharmaceutical preparation is a lyophilized powder of glatiramer acetate and mannitol.
The process of any one of claims 1-20 or 25 further comprising a step of lyophilizing the filtrate after it has been filled into the suitable container so as to form a lyophilized powder of glatiramer acetate and mannitol in the suitable container.
The process of any one of claims 1-26, wherein the suitable container is a syringe, vial, ampoule, cartridge or infusion.
The process of claim 27, wherein the suitable container is a syringe .
The process of claim 28, wherein the syringe contains 1ml of an aqueous pharmaceutical solution.
A prefilled syringe containing 40mg of glatiramer acetate and 40mg mannitol, which syringe is prepared by the process of any one of claims 1-29.
The prefilled syringe of claim 30, wherein the prefilled syringe contains 1ml of an aqueous pharmaceutical solution of 40mg/ml of glatiramer acetate and 40mg/ml mannitol.
The prefilled syringe of claim 31, wherein the aqueous pharmaceutical solution a) has a viscosity in the range of 2.0-3.5 cPa; or b) has an osmolality in the range of 270-330 mosmol/Kg.
33. The prefilled syringe of claim 32, wherein the aqueous pharmaceutical solution a) has a viscosity in the range of 2.2-3.0 cPa; or b) has an osmolality in the range of 275-325 mosmol/Kg.
34. An aqueous pharmaceutical solution comprising 40mg/ml glatiramer acetate and 40mg/ml mannitol, wherein the aqueous pharmaceutical solution a) has a viscosity in the range of 2.0-3.5 cPa; or b) has an osmolality in the range of 275-325 mosmol/Kg.
35. The aqueous pharmaceutical solution of claim 34, wherein the aqueous pharmaceutical solution has a viscosity in the range of 2.0-3.5 cPa.
36. The aqueous pharmaceutical solution of claim 34 or 35, wherein the aqueous pharmaceutical solution has a viscosity in the range of 2.61-2.92 cPa.
37. The aqueous pharmaceutical solution of claim 34, wherein the aqueous pharmaceutical solution has an osmolality in the range of 275-325 mosmol/Kg.
38. The aqueous pharmaceutical solution of any one of claims 34-
37, wherein the aqueous pharmaceutical solution has an osmolality in the range of 300-303 mosmol/Kg.
39. The aqueous pharmaceutical solution of any one of claims 34-
38, wherein the aqueous pharmaceutical solution has a pH in the range of 5.5-7.0.
40. A prefilled syringe containing 1ml of the aqueous pharmaceutical solution of any one of claims 34-39.
41. An automated injector comprising the prefilled syringe of any one of claims 30-33 or 40.
42. A method of treatment of a human patient suffering from a relapsing form of multiple sclerosis comprising administration to the human patient of three subcutaneous injections of a 40 mg/ml dose of glatiramer acetate per week using the prefilled syringe of any one of claims 30-33 or 40, using the aqueous pharmaceutical solution of any one of claims 34-39, or using the automated injector of claim 41 so as to treat the human patient .
43. The method of claim 42, wherein the human patient is suffering from relapsing-remitting multiple sclerosis.
44. The method of claim 42, wherein the human patient has experienced a first clinical episode and has MRI features consistent with multiple sclerosis.
PCT/US2015/051203 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product Ceased WO2016122722A1 (en)

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JP2017534813A JP2018503627A (en) 2015-01-28 2015-09-21 Method for producing glatiramer acetate
EA201691790A EA028484B1 (en) 2015-01-28 2015-09-21 Process for preparing a prefilled syringe containing glatiramer acetate
NZ724875A NZ724875B2 (en) 2015-09-21 Process for manufacturing glatiramer acetate product
EP15880609.1A EP3113785A4 (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product
MX2016011219A MX352734B (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product.
KR1020177012458A KR102268210B1 (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product
CA2945537A CA2945537C (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product
UAA201610444A UA116060C2 (en) 2015-01-28 2015-09-21 METHOD OF PREPARATION OF THE PRODUCT BASED ON ACETATE GLATIRAMER
RU2017104222A RU2669769C2 (en) 2015-01-28 2015-09-21 Method for obtaining glatiramer acetate product
KR1020167028604A KR101737295B1 (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product
US15/510,156 US20170312331A1 (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product
AU2015380381A AU2015380381B2 (en) 2015-01-28 2015-09-21 Process for manufacturing glatiramer acetate product
CN201580071551.XA CN107530394B (en) 2015-01-28 2015-09-21 Method for preparing glatiramer acetate product
BR112016023736A BR112016023736A2 (en) 2015-01-28 2015-09-21 process for manufacturing glatiramer acetate product
IL247851A IL247851A0 (en) 2015-01-28 2016-09-15 Process for manufacturing glatiramer acetate product
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IL267152A IL267152A (en) 2015-01-28 2019-06-06 Process for manufacturing glatiramer acetate product
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