WO2000053282A1 - Crystallization process for producing fine crystal products - Google Patents

Crystallization process for producing fine crystal products Download PDF

Info

Publication number
WO2000053282A1
WO2000053282A1 PCT/GB2000/000866 GB0000866W WO0053282A1 WO 2000053282 A1 WO2000053282 A1 WO 2000053282A1 GB 0000866 W GB0000866 W GB 0000866W WO 0053282 A1 WO0053282 A1 WO 0053282A1
Authority
WO
WIPO (PCT)
Prior art keywords
solvent
process according
compound
methanesulphonate
eprosartan
Prior art date
Application number
PCT/GB2000/000866
Other languages
French (fr)
Inventor
Stephen Thomas Carpenter
George Robert Wellman
Original Assignee
Smithkline Beecham P.L.C.
Smithkline Beecham Corporation
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Smithkline Beecham P.L.C., Smithkline Beecham Corporation filed Critical Smithkline Beecham P.L.C.
Priority to AU29326/00A priority Critical patent/AU2932600A/en
Priority to JP2000603770A priority patent/JP2002538227A/en
Priority to EP00907864A priority patent/EP1165197A1/en
Publication of WO2000053282A1 publication Critical patent/WO2000053282A1/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D409/00—Heterocyclic compounds containing two or more hetero rings, at least one ring having sulfur atoms as the only ring hetero atoms
    • C07D409/02—Heterocyclic compounds containing two or more hetero rings, at least one ring having sulfur atoms as the only ring hetero atoms containing two hetero rings
    • C07D409/06—Heterocyclic compounds containing two or more hetero rings, at least one ring having sulfur atoms as the only ring hetero atoms containing two hetero rings linked by a carbon chain containing only aliphatic carbon atoms
    • 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
    • A61K9/1688—Processes resulting in pure drug agglomerate optionally containing up to 5% of excipient
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0004—Crystallisation cooling by heat exchange
    • B01D9/0009—Crystallisation cooling by heat exchange by direct heat exchange with added cooling fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/005—Selection of auxiliary, e.g. for control of crystallisation nuclei, of crystal growth, of adherence to walls; Arrangements for introduction thereof

Definitions

  • the present invention relates to a process for the crystallisation of a chemical substance, and more particularly a substance to be used as a pharmaceutically active agent.
  • Crystallisation is a well known technique for the purification of chemical compounds. Crystalline products prepared using traditional batch methodology may vary; for example in the degree of agglomeration experienced and the habit and size of individual crystals so formed. Moreover, in some circumstances, conventional batch mode crystallisation may give poor results, i.e. produces oils or crystals containing occluded impurities. There is therefore a need for a crystallisation process that gives rise to products of uniform and consistently small crystal size without the problems of batch processing, especially oiling or solvent inclusion. This is particularly true for pharmaceutically active compounds which might otherwise have to be milled to improve their bio-availability, or to increase their suitability in processing, e.g. the electrostatic deposition of active ingredients in tablet manufacture.
  • a process for the continuous crystallisation of an organic chemical compound which comprises contacting a stream of either the compound or a salt thereof dissolved in a solvent with a stream of anti-solvent or colder solvent, or a solution of an appropriate acid or base, and separating off the crystals formed.
  • the solute/solvent/antisolvent system will be one which has a fast precipitation time, as this gives rise to particularly small crystals.
  • 'precipitation time' we mean the time taken to observe precipitation in a mixed system e.g. cloudiness.
  • Precipitation times can be determined by mixing and observing precipitation in individual solvent systems.
  • the precipitation time will be less than 1 minute, especially less than 5 seconds, and particularly less than 1 second.
  • Precipitation times may be varied by adjusting the concentration of solute, the rates of flow of solution and anti-solvent, and the temperatures of the solvent and anti-solvent. It should be recognised that the process of crystallisation can involve the initial formation of amorphous solid particles which rapidly change into a crystalline form.
  • the contacting process may prove satisfactory for the contacting process to be undertaken using a simple three-way pipe connection (for example a T or ⁇ - connection) provided that appropriate flow rates are used.
  • a simple three-way pipe connection for example a T or ⁇ - connection
  • the contacting process is undertaken using conditions of high shear and turbulence.
  • Mixing devices suitable for use in this invention include known in-line mixers, e.g. of the type in which one or more turbulence-creating elements are located within a pipeline through which the components are caused to flow.
  • Another suitable type of mixer is a homogeniser, e.g. of the type in which two liquid phases are forced under pressure through a biased valve.
  • Suitable mixing devices may also include cavities subjected to high turbulence and or shear stress by means of turbines, propellers etc.
  • mixers for creating conditions of high shear and turbulence are a chamber wherein introduced fluids are subjected to intense rotational swirling, for example a vortex chamber of the type disclosed generally in EP-
  • the vortex chamber comprises a chamber of substantially circular cross section, e.g. generally cylindrical in shape, and having tangential inlets and an axial outlet.
  • the components are introduced via the tangential inlets where they experience swirling and intense mixing as they radially accelerate towards the centrally located outlet.
  • a vortex mixer e.g. a Power Fluidics mixer
  • the mixing is carried out under controlled residence times in the mixer as this gives rise to a product of uniform crystal size. Fast precipitation times give rise to particularly small crystals.
  • Each stream is fed at high velocity into the central mixing chamber where it is mixed and accelerated towards to the central exit orifice.
  • the internal diameter of such a vortex chamber is about 8 mm, and its height about 1mm.
  • a combination of small mixing chamber volume (approx. 0.05-0. lml) and high throughputs preferably between 0.5L and 2L/min) generate typical residence times of less than 10ms in a steady-state environment where all elements of the mixed stream experience
  • the mixed stream of solute in solvent and anti-solvent is cooled during the mixing process and/or subsequent to it before the crystalline material is separated from the solvent stream.
  • the outlet flow from the mixer e.g. the Power Fluidic mixer
  • the tubular reactors e.g. a flexible tubular reactor
  • such tubular reactors are cooled.
  • the compound to be crystallised is an active ingredient for a pharmaceutical composition.
  • Particularly preferred compounds for crystallisation in accordance with the process of this invention are: Eprosartan methanesulphonate - (-(E)-(-[[2-butyl-l-[(4-carboxyphenyl)methyl]-lH- imidazol-5-yl]methylene]-2-thiophenepropanoic acid methanesulphonate); and Nabumetone - 4-(6-methoxy-2-naphthalenyl)-2-butanone.
  • the process is one in which the compound to be crystallised is the same as the compound dissolved in the solvent prior to addition of the anti-solvent (e.g. neutral molecule, free acid or base, acid-addition salt or base-addition salt).
  • the process can also be used where a solution containing the free acid or base of a compound is mixed under conditions of high turbulence with a solvent containing either acid or base to form a salt, or alternatively where a solution of a salt of a compound is rapidly mixed under conditions of high turbulence with a solvent containing an acid or base.
  • Figure 1 Shows a mixing device in the form of a vortex chamber having two tangential inlets and an axial outlet;
  • Figure 2 Shows crystals of Eprosartan methanesulphonate obtained bv batch crystallisation;
  • Figure 3 Shows crystals of Eprosartan methanesulphonate prepared by continuous crystallisation using a vortex mixer
  • Figure 4 Shows a comparison of particle sizes of Eprosartan methane sulphonate produced by continuous crystallisation and batch crystallisation;
  • Figure 5 Shows crystals of Nabumetone obtained by batch crystallisation
  • Figure 6 Shows crystals of Nabumetone prepared by continuous crystallisation using a vortex mixer
  • Figure 7 Shows a comparison of particle sizes of Nabumetone crystals produced by continuous crystallisation and batch crystallisation.
  • Eprosartan methanesulphonate (-(E)-(-[[2-butyl-l-[(4-carboxyphenyl)methyl]-lH- imidazol-5-yl]methylene]-2-thiophenepropanoic acid methanesulphonate) is described in U.S. 5,185,351/EP 0 403 159.
  • the crystallised eprosartan methanesulphonate has a ago of less than 10 microns.
  • the solution of the solute is a solution of Eprosartan methanesulphonate in acetic acid, preferably at an elevated temperature for example from 20°C to 100°C, preferably 70°C to 90°C and especially between 75 to 85°C.
  • the solution of the solute is reasonably concentrated, for example between 5 and 40% w/v, preferably between 10 and 30% w/v and especially between 15% and 25% w/v.
  • the anti-solvent is ethyl acetate or tert-butyl methyl ether (TBME), especially TBME.
  • TBME tert-butyl methyl ether
  • the anti-solvent is used in a significant excess to the solution of solute, for example from a 3-fold to a 30-fold excess, preferably 6-fold to a 25 -fold excess.
  • the anti-solvent is mixed at a temperature from -20°C to 80°C, preferably 0°C to 30°C. most preferably around 10 °C to 20°C.
  • the contacting process is undertaken in a vortex mixer. It has been found that using a solution of Eprosartan methanesulphonate (concentration of 20%w/v) dissolved in acetic acid at around 80°C and using an anti- solvent of tert-butyl methyl ether at around 20°C, that crystals of a particularly advantageous small and uniform size and consistency are obtained ( see Figure 3). Particle size distributions were found to be narrow, uni-modal and near symmetrical with d, 0 , d 50 and d 90 values of 1. 3.5 and 7 micron respectively. There is good demonstrated reproducibility with no observed agglomeration.
  • Nabumetone - (4-(6-methoxy-2-naphthalenyl)-2-butanone) is described in US patent 4,061 ,779.
  • the crystallised Nabumetone has a needle length of less than 20 microns.
  • the solution of the solute is a solution of Nabumetone in propan-2-ol, preferably at an elevated temperature for example from 20°C to 82°C and more preferably between 50°C to 77°C.
  • the solution of the solute is at a concentration of 5 to 30%w/v, more preferably between 5 and 10%w/v.
  • the anti-solvent is water.
  • the anti-solvent is used in an excess to the solution of solute, for example from a 4-fold to a 30-fold excess, preferably 4- fold to 10-fold.
  • the anti-solvent is mixed at a temperature from 0°C to 50°C, more preferably 6°C to 27 ⁇ >C.
  • the contacting process is undertaken in a vortex mixer.

Abstract

The invention relates to a process for the crystallisation of a chemical substance, and more particularly a substance to be used as a pharmaceutically active agent.

Description

CRYSTALLIZATION PROCESS FOR PRODUCING FINE CRYSTAL PRODUCTS
The present invention relates to a process for the crystallisation of a chemical substance, and more particularly a substance to be used as a pharmaceutically active agent.
Crystallisation is a well known technique for the purification of chemical compounds. Crystalline products prepared using traditional batch methodology may vary; for example in the degree of agglomeration experienced and the habit and size of individual crystals so formed. Moreover, in some circumstances, conventional batch mode crystallisation may give poor results, i.e. produces oils or crystals containing occluded impurities. There is therefore a need for a crystallisation process that gives rise to products of uniform and consistently small crystal size without the problems of batch processing, especially oiling or solvent inclusion. This is particularly true for pharmaceutically active compounds which might otherwise have to be milled to improve their bio-availability, or to increase their suitability in processing, e.g. the electrostatic deposition of active ingredients in tablet manufacture.
According to the present invention there is provided, in a first aspect, a process for the continuous crystallisation of an organic chemical compound which comprises contacting a stream of either the compound or a salt thereof dissolved in a solvent with a stream of anti-solvent or colder solvent, or a solution of an appropriate acid or base, and separating off the crystals formed.
Preferably the solute/solvent/antisolvent system will be one which has a fast precipitation time, as this gives rise to particularly small crystals. By 'precipitation time', we mean the time taken to observe precipitation in a mixed system e.g. cloudiness. Precipitation times can be determined by mixing and observing precipitation in individual solvent systems. Preferably the precipitation time will be less than 1 minute, especially less than 5 seconds, and particularly less than 1 second.
Precipitation times may be varied by adjusting the concentration of solute, the rates of flow of solution and anti-solvent, and the temperatures of the solvent and anti-solvent. It should be recognised that the process of crystallisation can involve the initial formation of amorphous solid particles which rapidly change into a crystalline form.
For some applications it may prove satisfactory for the contacting process to be undertaken using a simple three-way pipe connection (for example a T or Υ- connection) provided that appropriate flow rates are used. Preferably, however, the contacting process is undertaken using conditions of high shear and turbulence.
Mixing devices suitable for use in this invention include known in-line mixers, e.g. of the type in which one or more turbulence-creating elements are located within a pipeline through which the components are caused to flow. Another suitable type of mixer is a homogeniser, e.g. of the type in which two liquid phases are forced under pressure through a biased valve. Suitable mixing devices may also include cavities subjected to high turbulence and or shear stress by means of turbines, propellers etc.
Another and preferred type of mixer for creating conditions of high shear and turbulence is a chamber wherein introduced fluids are subjected to intense rotational swirling, for example a vortex chamber of the type disclosed generally in EP-
0153843-A (UK Atomic Energy Authority), the contents of which are incorporated herein by reference. The vortex chamber comprises a chamber of substantially circular cross section, e.g. generally cylindrical in shape, and having tangential inlets and an axial outlet. In such a mixer, the components are introduced via the tangential inlets where they experience swirling and intense mixing as they radially accelerate towards the centrally located outlet.
Preferably a vortex mixer (e.g. a Power Fluidics mixer) is used to create the conditions of high shear and turbulence. Preferably, the mixing is carried out under controlled residence times in the mixer as this gives rise to a product of uniform crystal size. Fast precipitation times give rise to particularly small crystals. Each stream is fed at high velocity into the central mixing chamber where it is mixed and accelerated towards to the central exit orifice. The internal diameter of such a vortex chamber is about 8 mm, and its height about 1mm. A combination of small mixing chamber volume (approx. 0.05-0. lml) and high throughputs (preferably between 0.5L and 2L/min) generate typical residence times of less than 10ms in a steady-state environment where all elements of the mixed stream experience
? minimal forward and backmixing. This effectively fixes supersaturation levels within the device with resultant tight control of particle size. Alternative dimensioned mixers may be used provided that the flow-rates can be sufficiently modulated to maintain high turbulence and uniform supersaturation conditions at similar residence times. By way of contrast, changes in supersaturation levels will typically occur in a conventional batch stirred reactor due to non-ideal mixing behaviour and both axial and radial heat gradients throughout the system.
Optionally the mixed stream of solute in solvent and anti-solvent is cooled during the mixing process and/or subsequent to it before the crystalline material is separated from the solvent stream. Optionally, in order to selectively control the size of the particles produced, the outlet flow from the mixer (e.g. the Power Fluidic mixer) can be passed through one or more tubular reactors (e.g. a flexible tubular reactor) before the crystals are separated off. Optionally such tubular reactors are cooled.
Preferably the compound to be crystallised is an active ingredient for a pharmaceutical composition. Particularly preferred compounds for crystallisation in accordance with the process of this invention are: Eprosartan methanesulphonate - (-(E)-(-[[2-butyl-l-[(4-carboxyphenyl)methyl]-lH- imidazol-5-yl]methylene]-2-thiophenepropanoic acid methanesulphonate); and Nabumetone - 4-(6-methoxy-2-naphthalenyl)-2-butanone.
Preferably, the process is one in which the compound to be crystallised is the same as the compound dissolved in the solvent prior to addition of the anti-solvent (e.g. neutral molecule, free acid or base, acid-addition salt or base-addition salt). However the process can also be used where a solution containing the free acid or base of a compound is mixed under conditions of high turbulence with a solvent containing either acid or base to form a salt, or alternatively where a solution of a salt of a compound is rapidly mixed under conditions of high turbulence with a solvent containing an acid or base.
The utility of the invention will now be described by way of example and with reference to the accompanying drawings, in which:
Figure 1 Shows a mixing device in the form of a vortex chamber having two tangential inlets and an axial outlet; Figure 2 Shows crystals of Eprosartan methanesulphonate obtained bv batch crystallisation;
Figure 3 Shows crystals of Eprosartan methanesulphonate prepared by continuous crystallisation using a vortex mixer; Figure 4 Shows a comparison of particle sizes of Eprosartan methane sulphonate produced by continuous crystallisation and batch crystallisation;
Figure 5 Shows crystals of Nabumetone obtained by batch crystallisation; Figure 6 Shows crystals of Nabumetone prepared by continuous crystallisation using a vortex mixer;
Figure 7 Shows a comparison of particle sizes of Nabumetone crystals produced by continuous crystallisation and batch crystallisation.
Example 1 Eprosartan methanesulphonate - (-(E)-(-[[2-butyl-l-[(4-carboxyphenyl)methyl]-lH- imidazol-5-yl]methylene]-2-thiophenepropanoic acid methanesulphonate) is described in U.S. 5,185,351/EP 0 403 159. Preferably the crystallised eprosartan methanesulphonate has a ago of less than 10 microns.
Preferably the solution of the solute is a solution of Eprosartan methanesulphonate in acetic acid, preferably at an elevated temperature for example from 20°C to 100°C, preferably 70°C to 90°C and especially between 75 to 85°C.
Preferably the solution of the solute is reasonably concentrated, for example between 5 and 40% w/v, preferably between 10 and 30% w/v and especially between 15% and 25% w/v.
Preferably the anti-solvent is ethyl acetate or tert-butyl methyl ether (TBME), especially TBME. Preferably the anti-solvent is used in a significant excess to the solution of solute, for example from a 3-fold to a 30-fold excess, preferably 6-fold to a 25 -fold excess.
Preferably the anti-solvent is mixed at a temperature from -20°C to 80°C, preferably 0°C to 30°C. most preferably around 10 °C to 20°C.
Preferably the contacting process is undertaken in a vortex mixer. It has been found that using a solution of Eprosartan methanesulphonate (concentration of 20%w/v) dissolved in acetic acid at around 80°C and using an anti- solvent of tert-butyl methyl ether at around 20°C, that crystals of a particularly advantageous small and uniform size and consistency are obtained ( see Figure 3). Particle size distributions were found to be narrow, uni-modal and near symmetrical with d,0, d50 and d90 values of 1. 3.5 and 7 micron respectively. There is good demonstrated reproducibility with no observed agglomeration. By comparison, the slow controlled addition of Eprosartan methanesulphonate /acetic acid solution to excess tert-butyl methyl ether with vigorous stirring in a semi-batch mode environment without use of a vortex mixer leads to a much broader size distribution of the generated particles (see Figure 4).
Example 2
Nabumetone - (4-(6-methoxy-2-naphthalenyl)-2-butanone) is described in US patent 4,061 ,779. Preferably the crystallised Nabumetone has a needle length of less than 20 microns.
Preferably the solution of the solute is a solution of Nabumetone in propan-2-ol, preferably at an elevated temperature for example from 20°C to 82°C and more preferably between 50°C to 77°C.
Preferably the solution of the solute is at a concentration of 5 to 30%w/v, more preferably between 5 and 10%w/v.
Preferably the anti-solvent is water. Preferably the anti-solvent is used in an excess to the solution of solute, for example from a 4-fold to a 30-fold excess, preferably 4- fold to 10-fold.
Preferably the anti-solvent is mixed at a temperature from 0°C to 50°C, more preferably 6°C to 27<>C.
Preferably the contacting process is undertaken in a vortex mixer.
It has been found that using a solution of Nabumetone (concentration of 5%w/v) dissolved in hot propan-2-ol and using water as an anti-solvent, that crystals of a particularly advantageous small and near-uniform size and consistency are obtained. Particle size distributions were found to be narrow, uni-modal and near symmetrical with d]0. d50 and d,)0 values of 2. 5 and 12 micron respectively (Figures 6 & 7). There is good demonstrated reproducibility with no observed agglomeration.

Claims

Claims:
1. A process for the continuous crystallisation of an organic chemical compound which comprises contacting a stream of either the compound or a salt thereof dissolved in a solvent with a stream of anti-solvent or colder solvent, or a solution of an appropriate acid or base, and separating off the crystals formed.
2. A process according to Claim 1 in which the contacting process is undertaken using conditions of high shear and turbulence.
3. A process according to Claims 1 or 2 in which the solute/solvent/antisolvent system has a precipitation time of less than 5 seconds.
4. A process according to any one of Claims 1 to 3 in which a vortex mixer or a three-way pipe connection is used to effect mixing.
5. A process according to any one of Claims 1 to 4 in which the compound is not converted into a different salt form.
6. A process according to any one of Claims 1 to 5 in which the compound is Eprosartan methanesulphonate using acetic acid as solvent and tert- butyl methyl ether as anti-solvent.
7. A process according to any one of Claims 1 to 5 in which the compound is Nabumetone using propan-2-ol as solvent and water as antisolvent.
8. A process according to any one of Claims 1 to 7 in which the compound to be crystallised is an active ingredient for a pharmaceutical composition.
9. A crystalline compound having small and uniform crystal size prepared by a process according to any one of Claims 1 to 8.
10. Crystalline Eprosartan methanesulphonate with a d90 value of less than 10 micron.
11. Crystalline Nabumetone with a d90 value of less than 20 micron.
PCT/GB2000/000866 1999-03-10 2000-03-09 Crystallization process for producing fine crystal products WO2000053282A1 (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU29326/00A AU2932600A (en) 1999-03-10 2000-03-09 Crystallization process for producing fine crystal products
JP2000603770A JP2002538227A (en) 1999-03-10 2000-03-09 Crystallization method for producing microcrystalline product
EP00907864A EP1165197A1 (en) 1999-03-10 2000-03-09 Crystallization process for producing fine crystal products

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9905512.1 1999-03-10
GBGB9905512.1A GB9905512D0 (en) 1999-03-10 1999-03-10 Process

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US09936194 A-371-Of-International 2001-12-07
US10/427,025 Continuation US20040028582A1 (en) 1999-03-10 2003-04-30 Crystallization process for producing fine crystal products

Publications (1)

Publication Number Publication Date
WO2000053282A1 true WO2000053282A1 (en) 2000-09-14

Family

ID=10849355

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB2000/000866 WO2000053282A1 (en) 1999-03-10 2000-03-09 Crystallization process for producing fine crystal products

Country Status (5)

Country Link
EP (1) EP1165197A1 (en)
JP (1) JP2002538227A (en)
AU (1) AU2932600A (en)
GB (1) GB9905512D0 (en)
WO (1) WO2000053282A1 (en)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001013889A1 (en) * 1999-08-25 2001-03-01 Smithkline Beecham P.L.C. Pharmaceutical composition comprising nabumetone
WO2001014036A1 (en) * 1999-08-19 2001-03-01 Aventis Pharma Limited Process for producing fine medicinal substances
WO2003032951A1 (en) * 2001-08-29 2003-04-24 Dow Global Technologies Inc. A process for preparing crystalline drug particles by means of precipitation
JP2003155214A (en) * 2001-09-10 2003-05-27 Lion Corp Pearly brightener dispersion and method for producing the same
US6939515B2 (en) 2001-08-10 2005-09-06 Symyx Technologies, Inc. Apparatuses and methods for creating and testing pre-formulations and systems for same
JP2006519700A (en) * 2003-03-04 2006-08-31 ファイブ・スター・テクノロジーズ・インコーポレイテッド Hydrodynamic cavitation crystallization apparatus and method
US7199242B2 (en) 2001-08-02 2007-04-03 Lg Life Sciences Limited Processes for the production of amino-protected derivatives of 4-aminomethylene-pyrrolidin-3-one and/or 4-aminomethylene-pyrrolidin-3-alkoxyimino derivatives and/or gemifloxacin or a salt thereof
US8361507B2 (en) 2007-07-25 2013-01-29 Hetero Drugs Limited Eprosartan mesylate crystalline particles and a process for preparing pure eprosartan

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4617687B2 (en) * 2004-03-12 2011-01-26 和光純薬工業株式会社 Method for crystallizing halogenated alkylpyridinium salts
CN101784258B (en) * 2007-07-06 2013-07-17 M技术株式会社 Method of producing microparticles to be ingested into the body, microparticles to be ingested into the body and dispersion and medicinal composition containing the same

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0461930A1 (en) * 1990-06-15 1991-12-18 Merck & Co. Inc. A crystallization method to improve crystal structure and size
WO1994007582A1 (en) * 1992-10-06 1994-04-14 Merck & Co., Inc. Dual jet crystallizer apparatus
WO1996032095A1 (en) * 1995-04-13 1996-10-17 Astra Aktiebolag Process for the preparation of respirable particles

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0461930A1 (en) * 1990-06-15 1991-12-18 Merck & Co. Inc. A crystallization method to improve crystal structure and size
WO1994007582A1 (en) * 1992-10-06 1994-04-14 Merck & Co., Inc. Dual jet crystallizer apparatus
WO1996032095A1 (en) * 1995-04-13 1996-10-17 Astra Aktiebolag Process for the preparation of respirable particles

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001014036A1 (en) * 1999-08-19 2001-03-01 Aventis Pharma Limited Process for producing fine medicinal substances
WO2001013889A1 (en) * 1999-08-25 2001-03-01 Smithkline Beecham P.L.C. Pharmaceutical composition comprising nabumetone
US7199242B2 (en) 2001-08-02 2007-04-03 Lg Life Sciences Limited Processes for the production of amino-protected derivatives of 4-aminomethylene-pyrrolidin-3-one and/or 4-aminomethylene-pyrrolidin-3-alkoxyimino derivatives and/or gemifloxacin or a salt thereof
US6939515B2 (en) 2001-08-10 2005-09-06 Symyx Technologies, Inc. Apparatuses and methods for creating and testing pre-formulations and systems for same
US7549978B2 (en) 2001-08-10 2009-06-23 Symyx Technologies, Inc. Needle assembly
WO2003032951A1 (en) * 2001-08-29 2003-04-24 Dow Global Technologies Inc. A process for preparing crystalline drug particles by means of precipitation
JP2003155214A (en) * 2001-09-10 2003-05-27 Lion Corp Pearly brightener dispersion and method for producing the same
JP2006519700A (en) * 2003-03-04 2006-08-31 ファイブ・スター・テクノロジーズ・インコーポレイテッド Hydrodynamic cavitation crystallization apparatus and method
US8361507B2 (en) 2007-07-25 2013-01-29 Hetero Drugs Limited Eprosartan mesylate crystalline particles and a process for preparing pure eprosartan

Also Published As

Publication number Publication date
EP1165197A1 (en) 2002-01-02
JP2002538227A (en) 2002-11-12
AU2932600A (en) 2000-09-28
GB9905512D0 (en) 1999-05-05

Similar Documents

Publication Publication Date Title
JP3386470B2 (en) Method and apparatus for forming particles
JP4876208B2 (en) Apparatus and method for crystallization by hydrodynamic cavitation
US7041144B2 (en) Hydrodynamic cavitation crystallization process
WO2000053282A1 (en) Crystallization process for producing fine crystal products
EP1180941B1 (en) Method of producing seed crystal suspensions based on melted fat
JP2006510484A (en) Apparatus and method for producing crystals / precipitates / particles
JP3282731B2 (en) Crystallization method for improving crystal structure and size
KR100408949B1 (en) Reactive crystallization method to improve particle size
JP4490016B2 (en) Particle formation method
AU2004284904B2 (en) Process for making sterile aripiprazole of desired mean particle size
US20040187770A1 (en) Rotor-stator apparatus and process for the formation of particles
US20080194868A1 (en) Hydrodynamic cavitation crystallization device and process
US9352339B2 (en) Method and pulverisation head, associated method and apparatus to manufacture a product in powder form
AU668246B2 (en) Dual jet crystallizer apparatus
US20040028582A1 (en) Crystallization process for producing fine crystal products
Othman et al. Preparation of microcrystals of piroxicam monohydrate by antisolvent precipitation via microfabricated metallic membranes with ordered pore arrays
AU7684898A (en) Continuous crystallization system with controlled nucleation for milk fat fractionation
CN108588449A (en) A kind of crystallization apparatus and method of high purity gallium
AU693561B2 (en) Method for the preparation of pearls and pearls obtained containing an active ingredient with an undefined melting point
EP1603652B1 (en) Hydrodynamic cavitation crystallization process
Kwon et al. Integrated membrane emulsification and solution cooling crystallization to obtain a narrow and predictable crystal size distribution
Zhiyi et al. Preparation of griseofulvin microparticles by supercritical fluid expansion depressurization process
WO2006018644A1 (en) Process for preparing particles and apparatus
Zhong et al. Microfluidic Crystallization for Screening of Spherical Particles of Pyraclostrobin
CN114394981A (en) Micro-fluidic continuous crystallization method for dorivivir sodium

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AL AM AT AU AZ BA BB BG BR BY CA CH CN CR CU CZ DE DK DM DZ EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
ENP Entry into the national phase

Ref country code: JP

Ref document number: 2000 603770

Kind code of ref document: A

Format of ref document f/p: F

WWE Wipo information: entry into national phase

Ref document number: 2000907864

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 09936194

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 2000907864

Country of ref document: EP

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWW Wipo information: withdrawn in national office

Ref document number: 2000907864

Country of ref document: EP