Classifications

• • 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
  • 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
  • A61K9/16—Agglomerates; Granulates; Microbeadlets ; Microspheres; Pellets; Solid products obtained by spray drying, spray freeze drying, spray congealing,(multiple) emulsion solvent evaporation or extraction
  • A61K9/1682—Processes
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K31/00—Medicinal preparations containing organic active ingredients
  • A61K31/33—Heterocyclic compounds
  • A61K31/395—Heterocyclic compounds having nitrogen as a ring hetero atom, e.g. guanethidine or rifamycins
  • A61K31/435—Heterocyclic compounds having nitrogen as a ring hetero atom, e.g. guanethidine or rifamycins having six-membered rings with one nitrogen as the only ring hetero atom
  • A61K31/44—Non condensed pyridines; Hydrogenated derivatives thereof
  • A61K31/4427—Non condensed pyridines; Hydrogenated derivatives thereof containing further heterocyclic ring systems
  • A61K31/4439—Non condensed pyridines; Hydrogenated derivatives thereof containing further heterocyclic ring systems containing a five-membered ring with nitrogen as a ring hetero atom, e.g. omeprazole
• • 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
  • A61K47/30—Macromolecular organic or inorganic compounds, e.g. inorganic polyphosphates
  • A61K47/36—Polysaccharides; Derivatives thereof, e.g. gums, starch, alginate, dextrin, hyaluronic acid, chitosan, inulin, agar or pectin
  • A61K47/38—Cellulose; 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
  • A61K9/16—Agglomerates; Granulates; Microbeadlets ; Microspheres; Pellets; Solid products obtained by spray drying, spray freeze drying, spray congealing,(multiple) emulsion solvent evaporation or extraction
• • 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
  • A61K9/48—Preparations in capsules, e.g. of gelatin, of chocolate
  • A61K9/4816—Wall or shell material
• • 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
  • A61K9/48—Preparations in capsules, e.g. of gelatin, of chocolate
  • A61K9/4841—Filling excipients; Inactive ingredients
  • A61K9/485—Inorganic compounds
• • 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
  • A61K9/48—Preparations in capsules, e.g. of gelatin, of chocolate
  • A61K9/4841—Filling excipients; Inactive ingredients
  • A61K9/4866—Organic macromolecular compounds
• • 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
  • A61K9/48—Preparations in capsules, e.g. of gelatin, of chocolate
  • A61K9/50—Microcapsules having a gas, liquid or semi-solid filling; Solid microparticles or pellets surrounded by a distinct coating layer, e.g. coated microspheres, coated drug crystals
  • A61K9/5073—Microcapsules having a gas, liquid or semi-solid filling; Solid microparticles or pellets surrounded by a distinct coating layer, e.g. coated microspheres, coated drug crystals having two or more different coatings optionally including drug-containing subcoatings
  • A61K9/5078—Microcapsules having a gas, liquid or semi-solid filling; Solid microparticles or pellets surrounded by a distinct coating layer, e.g. coated microspheres, coated drug crystals having two or more different coatings optionally including drug-containing subcoatings with drug-free core
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
  • A61P7/00—Drugs for disorders of the blood or the extracellular fluid
  • A61P7/02—Antithrombotic agents; Anticoagulants; Platelet aggregation inhibitors

Definitions

• the invention relates to an improved fluidised bed process for preparing a new medicament formulation of the active substance dabigatran etexilate of formula I
• the compound of formula 1 is known from the prior art and was first disclosed in WO98/37075. It is a potent thrombin inhibitor which can be used for example for the post-operative prevention of deep vein thromboses and in stroke prevention, particularly for preventing strokes in patients with atrial fibrillation.
• WO 03/074056 discloses the methanesulphonic acid addition salt of dabiagtran-etexilate (ie: dabigatran etexilate methanesulphonate) to be particularly useful.
• pellet formulations may be used, as disclosed for example in WO 03/074056.
• These formulations are compositions, in which an active substance layer containing binder and optionally separating agent and surrounding a core material is applied to the substantially spherical core material, which consists of or contains a pharmaceutically acceptable organic acid.
• the core layer and the active substance layer are separated from one another by a so-called isolating layer.
• the schematic structure of an active substance formulation of this kind is shown in FIG. 1 of WO 03/074056.
• the present invention relates to a process that can be used on an industrial scale for preparing active substance pellets containing dabigatran, which allows the formulation to be manufactured on a large scale.
• a further aim of the invention is to provide a process which allows the formulation to be manufactured with a reproducible quality.
• the methanesulphonic acid addition salt of dabiagtran etexilate exists in different polymorphic forms. It is another aim of the invention to provide for a manufacturing process which allows the manufacture of a pharmaceutical formulation that contains only one polymorphic form of the active ingredient dabigatran etexilate methanesulphonate.
• polymorph I of dabigatran etexilate methanesulphonate is advantageous over polymorph II in view of its crystallisation properties. This allows polymorph I to be easier isolated and handled in and after the manufacturing process of the active ingredient. According to the invention, polymorph I is therefore the preferred polymorph.
• polymorphic forms of a substance may be characterized by different properties (including but not limited to stability, efficacy, processing properties during manufacture etc). As a matter of principle it is, therefore, advisable to produce a pharmaceutical composition that contains essentially only one polymorph.
• the invention relates to manufacturing process which allows the manufacture of a pharmaceutical formulation that contains essentially polymorph I of the active ingredient dabigatran etexilat methanesulphonate.
• the process according to the invention is characterised by a series of partial steps.
• the core 1 is produced from pharmaceutically acceptable organic acid.
• tartaric acid is used to prepare the core 1.
• the core material 1 thus obtained is then converted into so-called isolated tartaric acid cores 3 by spraying on an isolating suspension 2.
• a dabigatran suspension 4 prepared subsequently is sprayed onto these coated cores 3 in one or more process steps by means of a coating process.
• the active substance pellets 5 thus obtained are 1 packed into suitable capsules.
• the isolated tartaric acid cores 3 should have a uniform, quasi-spherical geometry. Moreover they should have only minor potential defects in the isolation caused by satellites.
• the so-called satellites are small particles adhering to the outside of the otherwise rounded pellets and detracting from the otherwise quasi-spherical geometry of the pellets.
• the ideally spherical shape and low surface roughness is of particular importance for acid-sensitive active substances such as for example dabigatran etexilate, in which defects in the isolation caused by satellites that have broken off or by the excessively rough surface of over-large particles of tartaric acid powder may lead to significantly impaired storage stability and hence durability of the finished product. For this reason, with acid-sensitive active substances it is also essential to apply the isolating layer as such with high reproducibility and consistently high quality.
• the core 1 is prepared from tartaric acid particles with a particle size in the range from 0.2-0.8 mm, preferably 0.3-0.7 mm, particularly preferably 0.4-0.6 mm (determined by air jet screening) onto which a solution of tartaric acid and binder is sprayed.
• the following method is used to prepare the solution.
• Tartaric acid is first of all dissolved in water together with a suitable binder, preferably with acacia (gum arabic) at elevated temperature, preferably at a temperature in the range from 30-70° C., particularly preferably in the range from 40-60° C.
• 0.1-0.3 kg, particularly preferably 0.15-0.25 kg, particularly about 0.2 kg acacia are used per kilogram of tartaric acid put in.
• the amount of water is preferably 0.6-1.0 kg, preferably 0.7-0.9 kg, particularly about 0.8 kg per kilogram of tartaric acid put in.
• a clear solution of acacia in water is prepared at the above-mentioned temperature.
• the tartaric acid is then added preferably at constant temperature and while stirring continues. After the addition has ended the mixture is stirred for at least 1 hour, preferably between 3 and 10, particularly preferably 4-8, particularly preferably 5-6 hours.
• the solution thus obtained is sprayed onto tartaric acid particles with a particle size of 0.2-0.8 mm, preferably 0.3-0.7 mm, particularly preferably 0.4-0.6 mm.
• the proportion of particles with the above-mentioned particle size should be at least 90%, preferably at least 95%, particularly preferably at least 97%.
• the tartaric acid particles are placed in a suitable container.
• the container is preferably a pan in which the particles are mixed and moved about by the rotation of the pan.
• Various designs of pan are known in the art and may optionally also be referred to as drum coaters. On this subject reference is made for example to the disclosures of EP 80199, WO 83/03052, WO 95/19713 or WO 06/134133.
• pans that may be used in the process according to the invention are optionally also known as horizontal pans.
• the acid gum solution prepared by the method described hereinbefore is then sprayed onto the particles kept moving by rotation.
• the material supplied for spraying is optionally also referred to as the pellet bed.
• the term pellet is to be regarded as equivalent to the term particle or core within the scope of the present invention.
• preferably 0.8-1.6 kg, particularly preferably 1.0-1.4 kg, particularly preferably 1.2 kg of the above-mentioned acid gum solution are sprayed on per kilogram of tartaric acid particles supplied.
• the amount of supply air in the process according to the invention is dependent on the batch size.
• the standardised amount of supply air per kilogram of tartaric acid cores supplied according to the invention is preferably in the range from 0.5-2 (m 3 /h)/kg, preferably 0.75-1.5 (m 3 /h)/kg, particularly preferably 0.9-1.1 (m 3 /h)/kg.
• the amount of supply air is meant the amount of dry air introduced into the rotating pellet bed per hour.
• a standardised amount of supply air of 1.0 (m 3 /h)/kg corresponds to an actual amount of supply air of 1000 m 3 /h.
• the temperature of the supply air fed in for drying according to the invention is preferably below 90° C., particularly preferably below 80° C. Ideally the temperature of the supply air should be in the range from 35°-75° C.
• the pellet temperature (the temperature of the pellet bed formed) according to the invention is preferably in the range from 30-50° C., particularly preferably 36-44° C., ideally 38-42° C.
• the differential pressure is preferably 1-3 mbar, particularly preferably 1.5-2.5 mbar, particularly preferably 1.8-2.2 mbar.
• the differential pressure is the pressure difference between the pan pressure and ambient pressure.
• the pan should preferably be at reduced pressure so that no acid dust escapes.
• Spraying is carried out at a defined spray rate.
• the spray rate is meant the amount of acid gum solution that is sprayed onto the rotating pellet bed per hour.
• the spray rate is dependant on the batch size in the process according to the invention.
• the standardised spray rate according to the invention per kilogram of tartaric acid crystals supplied is preferably in the range from 0.2-0.4 (kg/h)/kg, preferably 0.25-0.35 (kg/h)/kg, particularly preferably 0.28-0.32 (kg/h)/kg. If for example 1000 kg tartaric acid crystals are placed in one batch, a standardised spray rate of 0.3 (kg/h)/kg corresponds to an actual spray rate of 300 kg/h.
• This tartaric acid powder consists of fine tartaric acid particles with a particle size of ⁇ 100, preferably ⁇ 75, particularly preferably ⁇ 50 microns (determined by air jet screening).
• the proportion of particles with the above-mentioned particle size should be at least 85%, preferably at least 90%, particularly preferably at least 94%.
• preferably 0.4-1.2 kg, particularly preferably 0.6-1.0 kg, particularly preferably 0.8 kg of the above-mentioned tartaric acid powder are used per kilogram of tartaric acid particles supplied.
• the material for spraying is dried until a product temperature of about 30-50° C., preferably about 40° C. is reached. After this, the acid gum solution is sprayed on again.
• the spraying on of the acid gum solution and the sprinkling with tartaric acid powder are carried out alternately.
• the total amounts of acid gum solution and tartaric acid powder are supplied in at least 100, preferably 150 to 350, particularly preferably 200 to 300, particularly preferably about 250 batches of similar size and the process steps described hereinbefore are repeated a corresponding number of times.
• the cores 1 obtained are dried.
• the drying is preferably carried out at a temperature of 50-70° C., preferably 55-65° C. over a period of 24-72 hours, preferably 36-60 hours.
• the core material is isolated by spraying an isolating suspension 2 onto the tartaric acid cores 1 obtained by the process described hereinbefore.
• ethanol is placed in the batch container and hydroxypropylmethylcellulose and dimethylpolysiloxane are added and dissolved therein with stirring, then talc is added and suspended.
• hydroxypropylmethylcellulose and talc have proved superior to the use of gum arabic and talc, for example.
• hydroxypropylmethylcellulose together with talc it is possible to produce an isolating layer of constant quality in a reproducible manner. This quality and reproducibility has been tested on an industrial scale.
• hydroxypropylmethylcellulose are used per kilogram of ethanol.
• dimethylpolysiloxane is added to the isolating suspension 2 to prevent foaming.
• the amount of dimethylpolysiloxane which is added with stirring to the preparation of the isolating suspension 2 is preferably 0.6-1.2 g, particularly preferably 0.8-0.9 g per kilogram of ethanol.
• talc is added and suspended therein with stirring.
• 0.04-0.06 kg, particularly preferably 0.046-0.05 kg talc are used per kilogram of ethanol.
• the isolating suspension 2 thus prepared is sprayed onto the previously prepared tartaric acid pellets 1 in a continuous spray process in a conventional horizontal coater.
• 0.5-0.8 kg, preferably 0.55-0.75 kg, particularly preferably 0.6-0.7 kg of isolating suspension are sprayed on per kilogram of tartaric acid cores 1 supplied.
• the spraying is carried out at a defined spray rate.
• the spray rate is meant the amount of isolating suspension 2 sprayed onto the pellets 1 per hour.
• the spray rate in the process according to the invention is dependent on the batch size.
• the standardised spray rate according to the invention is preferably in the range from 0.01-0.1 (kg/h)/kg, preferably 0.02-0.04 (kg/h)/kg, particularly preferably 0.025-0.035 (kg/h)/kg per kilogram of tartaric acid pellets 1 supplied. If for example 1200 kg tartaric acid cores are placed in one batch, a standardised spray rate of 0.027 (kg/h)/kg corresponds to an actual spray rate of 32 kg/h. If for example 600 kg tartaric acid cores are placed in one batch, a standardised spray rate of 0.035 (kg/h)/kg corresponds to an actual spray rate of 21 kg/h.
• the cores are dried continuously with a supply of air at up to 70° C., preferably from 25-70° C.
• the amount of supply air is meant the amount of dry air that is introduced into the rotating pellet bed per hour.
• the amount of supply air in the process according to the invention is dependant on the batch size.
• the standardised amount of supply air according to the invention is preferably in the range from 1.0-2.5 (m 3 /h)/kg. Preferably 1.2-2.0 (m 3 /h)/kg, particularly preferably 1.40-1.85 (m 3 /h)/kg per kilogram of tartaric acid cores 2 originally supplied. If for example 600 kg tartaric acid cores 2 are placed in one batch, a standardised amount of supply air of 1.83 (m 3 /h)/kg corresponds to an actual amount of supply air of 1100 m 3 /h. If for example 1200 kg tartaric acid cores 3 are placed in one batch, a standardised amount of supply air of 1.42 (m 3 /h)/kg corresponds to an actual amount of supply air of 1700 m 3 /h.
• the pellets 5 containing active substance are prepared by spraying an active substance suspension 4 onto the isolated tartaric acid cores 3 obtained by the method described hereinbefore.
• the preparation of the active substance suspension 4 is of particular importance according to the invention as both the homogeneity and the temperature of the active substance suspension 4 are pertinent to the quality of the pellets containing the active substance.
• the active substance suspension 4 is prepared using dabigatran etexilate methanesulphonate in the form of its polymorph I.
• the targeted production of polymorph I is possible for example using the method described in WO 05/028468 (cf. particularly Example 1). Where the term active substance is used within the scope of the present invention, unless stated otherwise, this is to be understood as being a reference to polymorph I of dabigatran etexilate methanesulphonate.
• isopropyl alcohol is taken and adjusted to a temperature range of 12-22° C. under a nitrogen atmosphere. Then hydroxypropylcellulose is sucked into the prepared substance using vacuum or circulatory dispersal with stirring.
• the preparation is carried out using a special dispersion device (rotor-stator principle; e.g. Ultra Turrax® made by Jahnke & Kunkel or CONTI TDS 4® made by Ystral GmbH).
• Circulatory dispersal denotes that the dispersion device is connected to the batch container and the prepared isopropyl alcohol is circulated through the disperser.
• the rotor-stator principle generates the suction vacuum required to suck in the solid.
• the liquid and solid enter the dispersing chamber by separate routes and are wetted therein during the suction process. As the process takes place during circulation, it is referred to as circulatory dispersal.
• the batch container in which the process takes place is in turn provided with a mixer which achieves the optimum stirring action of the dabigatran etexilate suspension with low energy input (e.g. Visco Jet® stirring system made by Visco Jet GmbH or an air jet mixer). Furthermore, the batch container is optionally provided with a double jacket. Isopropyl alcohol is preferably used in substantially anhydrous form (99.5%). The hydroxypropylcellulose is sucked in by vacuum or circulatory dispersal at 2000-4000 rpm, preferably at 2900 rpm, and incorporated with stirring. The stirring performance of the mixer in the batch container is e.g. 600 rpm.
• the active substance is ground up before the preparation of the suspension.
• the preferred particle size distribution of the active substance is at an X 90 of less than 14 ⁇ m.
• the characteristic value X 90 denotes the median value of the particle size below which are found 90% of the quantity of particles with regard to the distribution by volume of the individual particles.
• the particle sizes may for example be determined within the scope of the present invention by laser diffraction (Fraunhofer diffraction).
• stirring and swelling phase lasting 30 minutes during which the mixer is operated at a stirring speed of 400-800 rpm, preferably 600 rpm. Then the suspension is dispersed for 3-10 minutes by the circulatory process at 2000-4000 rpm, preferably at 2900 rpm.
• the dispersing stirring cycle is optionally repeated up to six times.
• 0.05 to 0.5 kg, preferably 0.1 to 0.3 kg, particularly preferably 0.15-0.25 kg active substance are used per kilogram of isopropyl alcohol put in.
• the amount of hydroxypropylcellulose used is 0.01 to 0.1 kg, preferably 0.02 to 0.07 kg particularly preferably 0.03-0.05 kg, per kilogram of isopropyl alcohol put in.
• the amount of talc used is 0.005 to 0.07 kg, preferably 0.01 to 0.05 kg, particularly preferably 0.02-0.04 kg, per kilogram of isopropyl alcohol put in.
• the ratio of active substance to hydroxypropylcellulose is preferably in the range from 3:1 to 7:1, preferably 4:1 to 6:1, particularly preferably about 5:1, with regard to the mass of the two constituents in the active substance suspension according to the invention.
• the ratio of active substance to talc is preferably in the range from 4:1 to 8:1, preferably 5:1 to 7:1, particularly preferably 6:1 to 6.5:1 with regard to the mass of the two constituents in the active substance suspension according to the invention.
• the concentration of the active substance is preferably at 10-25% (w/w), preferably at 11-20% (w/w), particularly preferably at 12-19% (w/w) in the active substance suspension according to the invention.
• the total concentration of the constituents active substance, hydroxypropylcellulose and talc in the active substance suspension according to the invention is preferably 14-40% (w/w), preferably 15-30% (w/w), particularly preferably 16-25% (w/w).
• the temperature selected for the preparation of the suspension 4 has a decisive effect on the characteristics of the final product.
• the temperature should best be kept below 30° C. throughout the entire manufacturing process. If the suspension 4 is produced or even stored at too high a temperature, this may lead to a change in the polymorphic form of the active substance, which may have negatively affect the efficacy of the final formulation.
• the temperature of the manufacturing process is in the range from 0-30° C., particularly preferably in the range from 5-30° C.
• the stirring power of the mixer in the batch container is preferably 300-500 rpm, particularly preferably 400 rpm.
• the active substance suspension 4 is stored at below 30° C. until further processing is carried out.
• the suspension 4 is processed further in the course of not more than 48 h. If the suspension is prepared and stored at 22° C., for example, it is preferably further processed within 60 hours.
• the present invention relates to a process for preparing a suspension 4 of the polymorph I of dabigatran etexilate methanesulphonate in isopropyl alcohol, which is characterised in that the temperature during the manufacture and storage of the suspension is always below 30° C., preferably in the range from 0-30° C., particularly preferably in the range from 5-30° C., the ingredients of the suspension being added by circulatory dispersion.
• the present invention relates to the suspension 4 of the polymorph I of dabigatran etexilate methanesulphonate in isopropyl alcohol, which may be obtained by the manufacturing process mentioned above.
• the present invention relates to the use of the suspension 4 of the polymorph I of dabigatran etexilate methanesulphonate in isopropyl alcohol as starting material for preparing a medicament formulation of dabigatran etexilate methanesulphonate.
• the present invention relates to the use of the active substance suspension 4 according to the invention as starting material for preparing a medicament formulation of dabigatran etexilate methanesulphonate, the suspension 4 having been reacted within 48 h at a storage temperature of less than 30° C.
• the present invention relates to the use of the active substance suspension 4 according to the invention as starting material for preparing a medicament formulation of dabigatran etexilate methanesulphonate, the suspension 4 having been reacted within 60 h at a storage temperature of less than 22° C.
• the active substance suspension 4 obtained by the above process is sprayed onto the isolated tartaric acid cores 3 described hereinbefore.
• the present invention relates to a process for preparing a medicament formulation of dabigatran etexilate methanesulphonate 5, characterised in that the active substance suspension 4 according to the invention is sprayed onto isolated tartaric acid cores 3.
• the present invention relates to a medicament formulation of dabigatran etexilate methanesulphonate 5, obtainable by spraying the active substance suspension 4 according to the invention onto isolated tartaric acid cores 3.
• a fluidised bed apparatus By a fluidised bed apparatus is meant according to the invention that the product to be coated has a fluid, preferably air, flowing through it. The material put in is set in motion and kept in motion by this fluid, the nature of the movement being controlled by different equipment-specific inserts.
• Precision Coater Alomatic
• Kugelcoater Heüttlin
• Aircoater Innojet
• Wurster Coater as described for example in EP 0711 593 has proved particularly suitable for carrying out the fluidised bed process according to the invention.
• the isolated tartaric acid starter pellets are placed in the product container, fluidised using process air and at the same time pre-heated.
• the process air current is generated by a ventilator provided downstream (vacuum method), but may also be generated by the pressure method.
• the supply air needed may be fed in directly from the outside air and heated or adjusted to a specific moisture level or water content by conditioning. Preferably the moisture level of the supply air is adjusted to 3 g/kg.
• the product container is closed off by a perforated base plate in the supply air region.
• a filter cloth or screen insert prevents the pellets from escaping from the product chamber.
• the base plate there are one or more spray nozzles.
• the high degree of perforation in the base plate in the region of the spray nozzles causes the tartaric acid starter pellets 3 which are to be sprayed to be accelerated upwards and thereby sprayed with the active substance suspension according to the co-current principle.
• the pellets may be forcibly carried by an air current guided vertically through one or more tubes (Wurster-Coater or Precision-Coater), or they may follow a helical or toroidal motion of the process air in the product container and relaxation zone (Kugelcoater or Aircoater). Before and during the falling back of the sprayed pellets the volatile constituents are dried or eliminated. A uniform structure of the active substance layer is ensured by the circulating movement of the pellets.
• a low spray pressure and a low spray rate are used to begin with.
• the parameters of spray rate and spray pressure as well as supply air volume and supply air temperature are increased step by step to ensure optimum movement of the pellets and optimum product temperature.
• the product temperature, spray pressure, spray rate, temperature of supply air and amount of supply air in particular should be kept within specified ranges. Monitoring these parameters according to the present invention also ensures limited decomposition of the active substance, a reproducible content of active substance in the pellets 5, associated reduced spray losses and also reduced formation of multiples (clumps of several pellets). A reduced formation of multiples directly influences the yield as clumps would be separated off during the final screening of the active substance pellets 5.
• the product temperature is meant the temperature that prevails in the p, die in the pellet bed.
• the product container is first of all charged with the isolated tartaric acid pellets 3 described hereinbefore and the isolated tartaric acid pellets 3 are heated. They are preferably heated to a temperature of 30-50° C., preferably 30-48° C., particularly preferably 34-44° C. Once this temperature has been reached, the active substance suspension 4 described hereinbefore is sprayed on.
• the temperature of the air supplied according to the invention is preferably below 90° C., particularly preferably below 80° C. Ideally the temperature of the supply air should be in the range from 40°-80° C., particularly preferably between 55-75° C.
• the spray pressure is meant the pressure of compressed air which is used for atomisation at the nozzle through which the active substance suspension 4 is sprayed on.
• the spray pressure according to the invention is preferably in the range from 1.0-4.0 bar, preferably 1.5-4.0 bar, particularly preferably 2.0-4.0 bar.
• the spray rate is meant the amount of active substance suspension 4 that is sprayed onto the fluid pellet bed per hour.
• the spray rate is dependant on the batch size in the process according to the invention.
• the standardised spray rate according to the invention per kilogram of isolated tartaric acid pellets 3 supplied is preferably in the range from 2-30 (g/min)/kg, preferably 4.5-30 (g/min)/kg, particularly preferably 6-26 (g/min)/kg.
• a standardised spray rate of 7.39 (g/min)/kg corresponds to an actual spray rate of about 2000 g/min.
• the amount of supply air is meant the amount of dry air that is introduced into the fluid pellet bed per hour.
• the amount of supply air is dependant on the batch size in the process according to the invention.
• the standardised amount of supply air per kilogram of isolated tartaric acid pellets 3 supplied according to the invention is preferably in the range from 10-30 (m 3 /h)/kg, preferably 14-30 (m 3 /h)/kg, particularly preferably 18-28 (m 3 /h)/kg.
• a standardised amount of supply air of 20 (m 3 /h)/kg corresponds to an actual amount of supply air of 5411 m 3 /h.
• the active substance pellets are dried for a specified length of time, preferably 10-30 minutes, particularly preferably 20 minutes.
• the product temperature should preferably be adjusted to between 20 and 40° C. during the drying. Continuous fluidisation is also ensured during drying.
• the product container is emptied gravimetrically and the dabigatran etexilate pellets are screened through a suitable screen, e.g. a vibrating screen (mesh size 1600 ⁇ m).
• a suitable screen e.g. a vibrating screen (mesh size 1600 ⁇ m).
• the amount of active substance suspension 4 sprayed on under the prevailing conditions depends not only on the active substance concentration in the suspension 4 but also on the batch size of the isolated tartaric acid pellets 3 supplied and the desired quantity of active substance per final active substance pellet (so-called charge).
• the active substance charge per active substance pellet 5 is in the range from 15-50% (w/w).
• Particularly preferred active substance pellets 5 according to the invention have a charge of active substance of 20-45% (w/w), particularly preferably 36-42% (w/w).
• a particularly preferred active substance suspension 4 with an active substance concentration of about 15% (w/w) and an overall concentration of the constituents active substance, hydroxypropylcellulose and talc of about 25% (w/w) is used according to the invention
• a desired charge of for example 40% of active substance per active substance pellet 5 with a supply of 1 kg of isolated tartaric acid pellets 3 requires the use of about 4.83 kg of active substance suspension 4 according to the invention. It may possibly make sense to use active substance suspension 4 in an excess of up to 5%, to compensate for any spray losses that may occur.
• the total weight of the batch and, in the present case, in particular the volume naturally increases constantly during the spraying of the active substance suspension 4.
• a charge of for example 40% of the isolated tartaric acid pellets 3 with active substance leads to roughly a doubling of the total weight and an increase in bulk density by a factor of approx. 1.4 (i.e. an even greater increase in volume in relation to the mass) of the material for spraying 5.
• This sharp increase in the mass and particularly the volume of the material for spraying 5 may negatively affect the spray process in large industrial batches, as for example uniform drying of the spray material 5 can no longer be achieved easily or without complex technical procedures.
• the present invention relates to a medicament formulation of dabigatran etexilate methanesulphonate 5, obtainable by spraying the active substance suspension 4 according to the invention onto isolated tartaric acid cores 3 by the method described hereinbefore.
• the active substance pellets thus obtained are screened through screens of a defined mesh size.
• the active substance pellets obtained are packed into commercially obtainable capsules, preferably into commercially obtainable HPMC capsules.
• Measuring device Air jet screen, e.g. Alpine A 200 LS Screens: As required Weight put in: 10 g/screen Duration: 1 min/screen, then 1 min each up to the maximum weight loss of 0.1 g
• the substance is transferred into a mortar and any lumps present are destroyed by intensive pounding.
• the screen with rubber seal and cover is placed on a balance, set to zero and 10.0 g of the pounded substance are weighed onto the screen.
• the screen together with its contents, rubber seal and cover are placed on the device.
• the timer is set to 1 minute and the material is treated by air jet screening for this time.
• the residue is weighed out and documented. This process is repeated until the decrease in the weight of the residue after air jet screening is ⁇ 0.1 g.
• a sample of the acid is taken for screening analysis.
• the acid in question is tartaric acid particles with a particle size in the range from 0.4-0.6 mm.
• the acid rubber solution obtained by the above method is sprayed onto the tartaric acid particles thus provided.
• the quantity of air supplied is adjusted to 1000 m 3 /h and 35°-75° C.
• the differential pressure is 2 mbar and the speed of rotation of the pan is 9 revolutions per minute.
• the nozzles should be arranged at a distance of 350-450 mm from the filling.
• the acid rubber solution is sprayed on by alternating with the following steps. After about 4.8 kg of the acid rubber solution has been sprayed onto the tartaric acid particles of particle size 0.4-0.6 mm and the solution has been distributed, about 3.2 kg tartaric acid powder are sprinkled onto the damp tartaric acid particles.
• the tartaric acid powder in question consists of fine tartaric acid particles with a particle size of ⁇ 50 microns. In all, 800 kg tartaric acid powder are required. After the said tartaric acid powder has been sprinkled on and distributed the spray material is dried until a product temperature of about 40° C. is reached. This is in turn followed by the spraying on of the acid rubber solution.
• the acid pellets are dried in the pan at 3 rpm for 240 minutes.
• an intermittent program is run at 3 rpm for 3 minutes every hour. In the present instance this means that the pan is rotated at 3 rpm for 3 minutes at intervals of one hour and then left to stand.
• the acid pellets are then transferred into a dryer. They are then dried at 60° C. over a period of 48 hours.
• the particle size distribution is determined by screen analysis. The particle size with a diameter of 0.6-0.8 mm corresponds to the product. This fraction should make up >85%.
• the acid pellets 1200 (600) kg are poured into the coating apparatus (e.g. GS-Coater Mod. 600/Mod. 1200) and sprayed therein in the rotating pan with the isolating suspension described above in a continuous spraying process lasting several hours at a spraying rate of 32 kg/h for the 1200 kg mixture or 21 kg/h for the 600 kg mixture.
• the pellets are also dried continuously with an air supply at up to 70° C.
• the isolated starter pellets are fractionated by screening.
• the product fraction with a diameter ⁇ 1.0 mm is stored and used further.
• the batch container is inertised with nitrogen and nitrogen is passed over it throughout the entire process.
• the addition of the active substance dabigatran etexilate methanesulphonate can be started. 252.006 kg of the active substance and 40.359 kg talc are sucked in successively by circulatory dispersal. After a stirring phase of 30 minutes the active substance suspension is dispersed for up to 10 minutes at 2900 rpm. Depending on the quality of the active substance suspension the dispersing-stirring cycle may be repeated up to 6 times. The quality of the active substance suspension is monitored by adding 100 ml of active substance suspension through a 500 ⁇ m screen after each dispersing-stirring cycle. The temperature of the suspension should not exceed 30° C. throughout the entire process.
• the storing and spraying temperature of the finished active substance suspension is adjusted to ⁇ 18° C. If the suspension is stored at below 30° C., it should be further processed within at most 48 h. If for example the suspension is manufactured and stored at 22° C., it may should be further processed within 60 hours. If the suspension is stored for example at 35° C. it should be further processed within at most 24 h.
• the active substance suspension is stirred throughout the entire manufacturing and spraying process.
• a fluidised bed apparatus is used (GPCG PRO 300). Spraying is carried out through nozzles 2.2 mm in diameter.
• the product container is charged with 270.561 kg of the tartaric acid pellets obtained according to Example 2 and the pellet bed is heated up. Once a pellet bed temperature of 39° C. is reached, spraying starts.
• the suspension prepared according to Example 3 is sprayed on in seven 10-minute spray phases at increasing spray rates of 120 kg/h up to 420 kg/h.
• the suspension is stirred constantly.
• the supply air temperature is not more than 75° C.
• the amount of supply air is about 7500 m 3 /h.
• the spray pressure is in the range from 3-4 bar.
• the pellets are dried in the product container at a supply air temperature of at least 20° C., at most 70° C. and with an amount of supply air of 6000 m 3 /h for a period of about 20 minutes.
• the dried pellets are then screened through a vibrating 1.6 mm screen and stored in containers with desiccants until required for further processing.
• the present invention relates to one of the above-mentioned medicament formulations as such.
• the present invention relates to a medicament formulation which contains 60-90 mg, preferably 70-80 mg, particularly preferably about 75 mg of dabigatran etexilate of formula I.
• the present invention relates to a medicament formulation which contains 90-130 mg, preferably 100-120 mg, preferably 105-115 mg, particularly preferably about 110 mg of dabigatran etexilate of formula I.
• the present invention relates to a medicament formulation which contains 60-90 mg, preferably 70-80 mg, particularly preferably about 75 mg of dabigatran etexilate of formula I in the form of the polymorph I of its methanesulphonate.
• a medicament formulation which contains 90-130 mg, preferably 100-120 mg, preferably 105-115 mg, particularly preferably about 110 mg of dabigatran etexilate of formula I in the form of the polymorph I of its methanesulphonate.
• the present invention relates to a medicament formulation which also contains hydroxymethylpropylcellulose, besides dabigatran etexilate of formula I in the form of the polymorph I of its methanesulphonate.
• the present invention relates to a medicament formulation which also contains dimethylpolysiloxane besides dabigatran etexilate of formula I in the form of the polymorph I of its methanesulphonate.
• the present invention relates to a medicament formulation which also contains the constituents gum arabic, tartaric acid, hydroxymethylpropylcellulose, dimethylpolysiloxane, talc as well as hydropropylcellulose, besides dabigatran etexilate of formula I in the form of the polymorph I of its methanesulphonate.
• the present invention relates to a medicament formulation which contains exclusively the constituents gum arabic, tartaric acid, hydroxymethylpropylcellulose, dimethylpolysiloxane and talc as well as hydropropylcellulose, besides dabigatran etexilate of formula I in the form of the polymorph I of its methanesulphonate.
• the present invention relates to a medicament formulation which contains 60-90 mg, preferably 70-80 mg, particularly preferably about 75 mg of dabigatran etexilate of formula I, for the post-operative prevention of deep vein thromboses and in stroke prevention, particularly for preventing strokes in patients with atrial fibrillation.
• a medicament formulation which contains 90-130 mg, preferably 100-120 mg, preferably 105-115 mg, particularly preferably about 110 mg of dabigatran etexilate of formula I, for the post-operative prevention of deep vein thromboses and in stroke prevention, particularly for preventing strokes in patients with atrial fibrillation.

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