WO1999054048A1 - Fluid energy milling process and apparatus - Google Patents

Fluid energy milling process and apparatus Download PDF

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Publication number
WO1999054048A1
WO1999054048A1 PCT/GB1999/001189 GB9901189W WO9954048A1 WO 1999054048 A1 WO1999054048 A1 WO 1999054048A1 GB 9901189 W GB9901189 W GB 9901189W WO 9954048 A1 WO9954048 A1 WO 9954048A1
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WO
WIPO (PCT)
Prior art keywords
compressed air
humidity
milling
process according
monitoring
Prior art date
Application number
PCT/GB1999/001189
Other languages
French (fr)
Inventor
Anthony Guy Hatton
Original Assignee
Smithkline Beecham Plc
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
Priority to EP99918105A priority Critical patent/EP1073524B1/en
Priority to KR1020007011637A priority patent/KR20010042863A/en
Priority to CA002329732A priority patent/CA2329732A1/en
Priority to HU0102244A priority patent/HUP0102244A3/en
Application filed by Smithkline Beecham Plc filed Critical Smithkline Beecham Plc
Priority to BR9909806-7A priority patent/BR9909806A/en
Priority to IL13887499A priority patent/IL138874A0/en
Priority to AT99918105T priority patent/ATE255466T1/en
Priority to PL99343563A priority patent/PL343563A1/en
Priority to JP2000544437A priority patent/JP2002512117A/en
Priority to NZ507489A priority patent/NZ507489A/en
Priority to AU36149/99A priority patent/AU748262B2/en
Priority to DE1999613331 priority patent/DE69913331T2/en
Publication of WO1999054048A1 publication Critical patent/WO1999054048A1/en
Priority to NO20005235A priority patent/NO20005235L/en
Priority to HK01104886A priority patent/HK1034216A1/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C19/00—Other disintegrating devices or methods
    • B02C19/06—Jet mills
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C25/00—Control arrangements specially adapted for crushing or disintegrating

Definitions

  • This invention is concerned with a process and apparatus for producing finely divided powders, especially of drug substances.
  • the present invention relates to improvements in fluid energy milling.
  • Fluid energy milling also known as micronising, is a procedure commonly used for producing finely divided powders. It is especially suitable for drug substances because there are no grinding media to contaminate the product.
  • the reduction in particle size in the fluid energy mill is caused by attrition between the particles of the substance being milled, using energy imparted by compressed air.
  • the compressed air used in fluid energy milling has a very low humidity because of the increased potential for condensation in compressed air systems. Moisture is removed from the air after compression to avoid problems with condensation in apparatus in which the compressed air is used. It is customary to remove moisture by condensation, by cooling the compressed air after compression, and then to pass the compressed air through a desiccant tower before it is fed into a fluid energy mill.
  • the compressed air used in fluid energy milling has a pressure of around 6 bar and will have a dew point (at atmospheric pressure) below -40 °C, and which may be as low as -70 °C.
  • the process of micronisation may disrupt the crystal structure of substances being processed due to attrition during the milling.
  • crystalline hydrates and solvates the combination of attrition and very dry air may cause additional damage, by stripping water/solvate molecules from the crystal structure during processing.
  • the micronised material After milling the micronised material may be able to re-attain its original crystal structure over a period of time, depending on storage conditions. Therefore, a drug substance which is a crystalline hydrate may possibly not be at its original specification after fluid energy milling and may return to its original specification only after an unpredictable length of time in storage.
  • the damage caused by attrition/desolvation may affect the intended properties of the product, for example, surface energy, stability, bioavailability.
  • a milled powder agglomerated during further processing rather than dispersing uniformly.
  • the present invention is based on the discovery that controlling the humidity of the compressed air used in fluid energy milling in a range which is considerably higher than that generally used, but still below the humidity which would lead to condensation problems in the mill, results in less damage to the crystallinity in the milled product.
  • the consequent reduction in or avoidance of desiccation of the substance during the milling process also facilitates re-attainment of the original level of crystallinity after milling. Therefore, this invention provides micronised output that is more consistent and with improved control of quality attributes. This gives much reduced inter-batch variation, leading to less reworking or failure of batches.
  • theprocess of the invention does not have a detrimental effect on the particle size reduction achieved by the micronisation process.
  • the present invention provides a fluid energy milling apparatus including means for adjusting humidity of the compressed air used for milling.
  • the invention also provides a milling process which comprises feeding compressed air into a mill chamber containing particulate material and subjecting the material to fluid energy milling, characterised in that the humidity of the compressed air is monitored and, if necessary, the humidity is adjusted to reduce damage to the milled product.
  • the adjustment made in accordance with this invention will typically be to increase the humidity. However, once the optimum value has been determined, and the apparatus has been set up to produce the desired increase in humidity of the compressed air source, it may be necessary to make adjustments during milling to correct humidity levels up or down in order to retain the optimum value.
  • a typical fluid energy milling system comprises a source of compressed air, a desiccant tower and a mill including a milling chamber and a collection device.
  • the collection device may be a filter sock in the exit air stream or an expansion chamber in which the energy of the air stream is dissipated allowing milled material to settle out.
  • the humidity of the process air in the mill may be increased by arranging that the desiccant tower is bypassed, so that the compressed air is fed directly from the source to the mill.
  • the system is preferably made controllable by providing a by-pass loop around the desiccant tower and a control valve to split the air flow between the by-pass loop and the desiccant tower, and by which the relative proportions of compressed air travelling through the by-pass and the tower can be varied.
  • a control valve to split the air flow between the by-pass loop and the desiccant tower, and by which the relative proportions of compressed air travelling through the by-pass and the tower can be varied.
  • undried air may be mixed with the dried air at a particular compressed air outlet in order to apply the humidity adjustment only to the process air supplying a particular piece of equipment.
  • humidity can be adjusted by injecting water, preferably as a mist or spray, into the compressed air-lines at an upstream location which allows moisture to be dispersed throughout the air stream before it reaches the mill.
  • the humidity is preferably assessed by measurement of dew point.
  • the present invention includes any process in which the humidity is adjusted so that the process air in the mill has a dew point above the dew point of the compressed air as produced.
  • the humidity is increased to a dew point (at atmospheric pressure) of from -30 °C to 5 °C preferably about -15 °C to 0 °C.
  • Optimal values for specific materials can be determined by routine testing, varying the dew point and assessing product quality.
  • the humidity is typically measured by a dew-point hygrometer.
  • the measurement may be made continuously, for example, by a sensor placed in the air stream prior to entry into the milling chamber; or intermittently, for example, by sampling the air in the air stream prior to entry into the milling chamber.
  • the present invention may be applied to any fluid-energy milling process, for example in a system in which an internal classifier releases particles as they reach a pre-determined size or in a system without a classifier in which product may be passed through the mill more than onceuntil all particles are within a desired size range.
  • An additional advantage of the present invention in addition to its beneficial effect on the quality of the micronised output, is that it appears to improve the micronisation process itself, making maintenance of feed rate and balancing of air pressures more easy. Furthermore, the process of the invention improves the consistency and quality of micronised drug substance output demonstrated over a period of continued production.
  • the present invention is particularly effective for the preparation of finely divided drug substance for use in a pharmaceutical composition. Accordingly, in a further aspect, the present invention provides for a pharmaceutical composition comprising a drug substance obtainable by a process as hereinbefore described.
  • the invention will improve the quality of micronised output for most substances, but is of particular applicability to the micronisation of substances susceptible to crystal damage during the process. Since removal of water of crystallinity (if present) in itself can destabilise a crystal structure, potential for crystal damage during traditional micronisation processing of crystalline hydrates is a serious problem, which the invention will overcome.
  • the procedures of the present invention are used in the preparation of micronised calcium mupirocin dihydrate (EP 0 167 856-A2, Beecham Group pic).
  • micronised calcium mupirocin dihydrate EP 0 167 856-A2, Beecham Group pic.
  • fluid energy milling of this substance has produced micronised product that forms undesirable aggregates when compounded into an ointment base. It has been postulated that this is caused by surface energy changes resulting from loss of water of crystallisation and damage to the crystal structure by milling in very dry air. Controlling the humidity of the process air to an atmospheric pressure dew point from about -15 to about 0 °C has overcome this problem.
  • Micronised calcium mupirocin dihydrate produced according to the procedures of this invention preferably has a moisture content of from 3.0 to 4.0, more preferably 3.4 to 3.7% and a low amorphous content, preferably 5% or less after recovery of crystallinity.
  • the present invention provides for a pharmaceutical composition
  • a pharmaceutical composition comprising micronised calcium mupirocin dihydrate obtainable by a process as hereinbefore described.
  • Such compositions will benefit from containing drug substance of more consistent quality attributes, avoiding, in an ointment, for example, formation of aggregates of calcium mupirocin dihydrate .
  • compositions include ointments, creams and nasal sprays, such as those described in EP 0 231 621-A2 (Beecham Group pic), EP 0 251 434- A2 (Beecham Group pic), WO 95/10999 (SmithKline Beecham Corp) and WO 98/14189 (SmithKline Beecham).
  • a preferred composition is an ointment comprising calcium mupirocin dihydrate in a white soft paraffin base containing a glycerine ester, available as the product Bactroban Nasal, from SmithKline Beecham.
  • a further preferred composition is a cream comprising calcium mupirocin dihydrate in a base comprising mineral oil, polyethylene glycol (1000) monocetyl ether, cetyl alcohol, stearyl alcohol, xanthan gum and water, available as the product Bactroban Cream, from SmithKline Beecham.
  • a commercial scale plant for micronising calcium-mupirocin dihydrate passes compressed air through silica gel columns to a micronising mill.
  • a loop by-passing the silica gel drying columns was installed in the process air feed to the mill.
  • the proportion of the air by-passing the drying columns was varied using a valve, so that the humidity of the process air could be controlled.
  • a single batch of calcium mupirocin was taken and divided into three portions to carry out three separate micronisations performed.
  • the first micronisation (sub-batch A) was undertaken using the processing air as routinely delivered by the plant compressor.
  • the dew point of the air was -58 °C.
  • Two further portions of the input material were micronised, one (sub-batch B) using air controlled to a dew point target of -10 °C, one (sub-batch C) to a dew point of 0 °C (the upper limit of humidity obtainable in this plant).
  • Each run produced ca. 5kg of micronised product.
  • the dew point was measured by sampling air upstream of the mill adjacent the air inlet, and assessed as the dew point at atmospheric pressure.
  • sub-batches A and B were blended with an ointment base.
  • the ointment made from sub- batch A showed large numbers of aggregates; no aggregates were found in the ointment made from sub-batch B.

Abstract

A fluid energy milling apparatus including means for adjusting humidity of the compressed air used for milling provides improved micronised product, in particular hydrates for use as drug substance in pharmaceutical compositions.

Description

FUID ENERGY MILL ING PROCESS AND APPARATUS
This invention is concerned with a process and apparatus for producing finely divided powders, especially of drug substances. In particular, the present invention relates to improvements in fluid energy milling.
Fluid energy milling, also known as micronising, is a procedure commonly used for producing finely divided powders. It is especially suitable for drug substances because there are no grinding media to contaminate the product. The reduction in particle size in the fluid energy mill is caused by attrition between the particles of the substance being milled, using energy imparted by compressed air.
The compressed air used in fluid energy milling has a very low humidity because of the increased potential for condensation in compressed air systems. Moisture is removed from the air after compression to avoid problems with condensation in apparatus in which the compressed air is used. It is customary to remove moisture by condensation, by cooling the compressed air after compression, and then to pass the compressed air through a desiccant tower before it is fed into a fluid energy mill.
Typically, the compressed air used in fluid energy milling has a pressure of around 6 bar and will have a dew point (at atmospheric pressure) below -40 °C, and which may be as low as -70 °C.
The process of micronisation may disrupt the crystal structure of substances being processed due to attrition during the milling. When milling crystalline hydrates and solvates the combination of attrition and very dry air may cause additional damage, by stripping water/solvate molecules from the crystal structure during processing. After milling the micronised material may be able to re-attain its original crystal structure over a period of time, depending on storage conditions. Therefore, a drug substance which is a crystalline hydrate may possibly not be at its original specification after fluid energy milling and may return to its original specification only after an unpredictable length of time in storage. In addition, the damage caused by attrition/desolvation may affect the intended properties of the product, for example, surface energy, stability, bioavailability.
1 In a particular case, a milled powder agglomerated during further processing rather than dispersing uniformly.
The present invention is based on the discovery that controlling the humidity of the compressed air used in fluid energy milling in a range which is considerably higher than that generally used, but still below the humidity which would lead to condensation problems in the mill, results in less damage to the crystallinity in the milled product.The consequent reduction in or avoidance of desiccation of the substance during the milling processalso facilitates re-attainment of the original level of crystallinity after milling. Therefore, this invention provides micronised output that is more consistent and with improved control of quality attributes. This gives much reduced inter-batch variation, leading to less reworking or failure of batches. In addition, theprocess of the invention does not have a detrimental effect on the particle size reduction achieved by the micronisation process.
In its broadest aspect, the present invention provides a fluid energy milling apparatus including means for adjusting humidity of the compressed air used for milling.
The invention also provides a milling process which comprises feeding compressed air into a mill chamber containing particulate material and subjecting the material to fluid energy milling, characterised in that the humidity of the compressed air is monitored and, if necessary, the humidity is adjusted to reduce damage to the milled product.
The adjustment made in accordance with this invention will typically be to increase the humidity. However, once the optimum value has been determined, and the apparatus has been set up to produce the desired increase in humidity of the compressed air source, it may be necessary to make adjustments during milling to correct humidity levels up or down in order to retain the optimum value.
A typical fluid energy milling system comprises a source of compressed air, a desiccant tower and a mill including a milling chamber and a collection device. The collection device may be a filter sock in the exit air stream or an expansion chamber in which the energy of the air stream is dissipated allowing milled material to settle out. The humidity of the process air in the mill may be increased by arranging that the desiccant tower is bypassed, so that the compressed air is fed directly from the source to the mill. However, the system is preferably made controllable by providing a by-pass loop around the desiccant tower and a control valve to split the air flow between the by-pass loop and the desiccant tower, and by which the relative proportions of compressed air travelling through the by-pass and the tower can be varied. By monitoring the humidity of the air entering the mill, the amounts of air passing through the by-pass and through the desiccation tower can be adjusted using the control valve so as to achieve the desired humidity in the milling chamber.
In an alternative embodiment, undried air may be mixed with the dried air at a particular compressed air outlet in order to apply the humidity adjustment only to the process air supplying a particular piece of equipment.
In a further embodiment, humidity can be adjusted by injecting water, preferably as a mist or spray, into the compressed air-lines at an upstream location which allows moisture to be dispersed throughout the air stream before it reaches the mill.
The humidity is preferably assessed by measurement of dew point. The present invention includes any process in which the humidity is adjusted so that the process air in the mill has a dew point above the dew point of the compressed air as produced. Typically the humidity is increased to a dew point (at atmospheric pressure) of from -30 °C to 5 °C preferably about -15 °C to 0 °C. Optimal values for specific materials can be determined by routine testing, varying the dew point and assessing product quality.
The humidity is typically measured by a dew-point hygrometer. The measurement may be made continuously, for example, by a sensor placed in the air stream prior to entry into the milling chamber; or intermittently, for example, by sampling the air in the air stream prior to entry into the milling chamber. The present invention may be applied to any fluid-energy milling process, for example in a system in which an internal classifier releases particles as they reach a pre-determined size or in a system without a classifier in which product may be passed through the mill more than onceuntil all particles are within a desired size range.
An additional advantage of the present invention, in addition to its beneficial effect on the quality of the micronised output, is that it appears to improve the micronisation process itself, making maintenance of feed rate and balancing of air pressures more easy. Furthermore, the process of the invention improves the consistency and quality of micronised drug substance output demonstrated over a period of continued production.
In addition, the present invention is particularly effective for the preparation of finely divided drug substance for use in a pharmaceutical composition. Accordingly, in a further aspect, the present invention provides for a pharmaceutical composition comprising a drug substance obtainable by a process as hereinbefore described.
The invention will improve the quality of micronised output for most substances, but is of particular applicability to the micronisation of substances susceptible to crystal damage during the process. Since removal of water of crystallinity (if present) in itself can destabilise a crystal structure, potential for crystal damage during traditional micronisation processing of crystalline hydrates is a serious problem, which the invention will overcome.
In a preferred embodiment, the procedures of the present invention are used in the preparation of micronised calcium mupirocin dihydrate (EP 0 167 856-A2, Beecham Group pic). Previously, fluid energy milling of this substance has produced micronised product that forms undesirable aggregates when compounded into an ointment base. It has been postulated that this is caused by surface energy changes resulting from loss of water of crystallisation and damage to the crystal structure by milling in very dry air. Controlling the humidity of the process air to an atmospheric pressure dew point from about -15 to about 0 °C has overcome this problem. Micronised calcium mupirocin dihydrate produced according to the procedures of this invention preferably has a moisture content of from 3.0 to 4.0, more preferably 3.4 to 3.7% and a low amorphous content, preferably 5% or less after recovery of crystallinity.
Accordingly, in a further aspect, the present invention provides for a pharmaceutical composition comprising micronised calcium mupirocin dihydrate obtainable by a process as hereinbefore described. Such compositions will benefit from containing drug substance of more consistent quality attributes, avoiding, in an ointment, for example, formation of aggregates of calcium mupirocin dihydrate .
Preferred such compositions include ointments, creams and nasal sprays, such as those described in EP 0 231 621-A2 (Beecham Group pic), EP 0 251 434- A2 (Beecham Group pic), WO 95/10999 (SmithKline Beecham Corp) and WO 98/14189 (SmithKline Beecham). A preferred composition is an ointment comprising calcium mupirocin dihydrate in a white soft paraffin base containing a glycerine ester, available as the product Bactroban Nasal, from SmithKline Beecham. A further preferred composition is a cream comprising calcium mupirocin dihydrate in a base comprising mineral oil, polyethylene glycol (1000) monocetyl ether, cetyl alcohol, stearyl alcohol, xanthan gum and water, available as the product Bactroban Cream, from SmithKline Beecham.
This invention is illustrated by the following Examples.
Example 1
A commercial scale plant for micronising calcium-mupirocin dihydrate passes compressed air through silica gel columns to a micronising mill. A loop by-passing the silica gel drying columns was installed in the process air feed to the mill. The proportion of the air by-passing the drying columns was varied using a valve, so that the humidity of the process air could be controlled.
A single batch of calcium mupirocin was taken and divided into three portions to carry out three separate micronisations performed. The first micronisation (sub-batch A) was undertaken using the processing air as routinely delivered by the plant compressor. The dew point of the air was -58 °C. Two further portions of the input material were micronised, one (sub-batch B) using air controlled to a dew point target of -10 °C, one (sub-batch C) to a dew point of 0 °C (the upper limit of humidity obtainable in this plant). Each run produced ca. 5kg of micronised product. In each case, the dew point was measured by sampling air upstream of the mill adjacent the air inlet, and assessed as the dew point at atmospheric pressure.
All three micronised sub-batches met the required particle size specifications. The outputs were then assessed for crystallinity by solution calorimetry and the moisture contents measured by Karl Fischer analysis. The sub-batch A micronised at a dew point of -58 °C showed desiccation (Moisture Content: 3.1-3.2%> w/w) and an amorphous content of ca. 15% (cf. 2% in the unmicronised dihydrate). Sub-batches B & C, produced at dew points of -10 °C and 0 °C respectively, showed no desiccation (Moisture contents: 3.6%) w/w) and had amorphous contents of ca. 9%>. Continued monitoring of sub-batches showed that the amorphous content steadily decreased over the next few weeks for the sub-batches B & C, whereas, due to the desiccation, sub-batch A failed to recover from the crystal damage. Sub-batches A and B were blended with an ointment base. The ointment made from sub- batch A showed large numbers of aggregates; no aggregates were found in the ointment made from sub-batch B.
Example 2
In another experiment, the effect on moisture content and crystal damage (amorphous drug content) was compared for portions of a batch of calcium mupirocin when micronised using air controlled in a dew point range of-15°C to -5°Cwith air as generally produced from the compressed air system, of dew point ca. -50°C, whilst varying other micronisation parameters to simulate stressing of the process. The portions of the batch micronised using controlled dew point air (-15°C to -5°C) gave a mean moisture content of 3.5% w/w and a mean amorphous drug content of 16.5%). The portions of the batch micronised using standard compressed air (dew point ca. -50°C) gave a mean moisture content of 2.9% w/w and a mean amorphous drug content of 38.3%. When utilising the controlled humidity process, the output drug substance was of a much more consistent quality than with the generally produced compressed air, demonstrating that the invention improves the ruggedness of the micronisation process.

Claims

1. A fluid energy milling apparatus including means for adjusting humidity of the compressed air used for milling.
2. Apparatus according to claim 1 further including means for monitoring the humidity of the compressed air upstream of the inlet to the milling chamber.
3. A fluid energy milling system comprising a compressed air source, a desiccant tower, a milling chamber and a collection device including means for monitoring the humidity of the compressed air upstream of the milling chamber and means for adjusting the humidity of the compressed air to a desired level.
4. Apparatus according to claim 3 in which the means for monitoring humidity is a hygrometer sensor positioned in contact with the compressed air stream.
5. Apparatus according to claim 3 in which the means for monitoring the humidity includes means for sampling the compressed air stream upstream of the milling chamber and a hygrometer located off-line.
6. Apparatus according to any one of claims 3 to 5 in which the means for adjusting humidity of the compressed air is an injector for introducing a water, mist or spray into the compressed air line.
7. Apparatus according to any one of claims 3 to 6 in which a by-pass loop diverts compressed air around the desiccant tower and a control valve is provided to switch the airflow between the desiccant tower and the by-pass loop.
8. Apparatus according to claim 7 in which the control valve is adjustable so that varying proportions of compressed air can be sent through the desiccant tower and bypass loop.
8
9. A milling process which comprises feeding compressed air into a mill chamber containing particulate material and subjecting the material to fluid energy milling, characterised in that the humidity of the compressed air is monitored and, if necessary, the humidity is adjusted to reduce damage to the milled product.
10. A process according to claim 9 in which milling is carried out in a system comprising a compressed air source, a desiccant tower, a milling chamber and a collection device.
11. A process according to claim 9 or 10 in which means for monitoring humidity is a hygrometer sensor positioned in contact with the compressed air stream.
12. A process according to claim 9 or 10 in which the means for monitoring the humidity includes means for sampling the compressed air stream upstream of the milling chamber and a hygrometer located off-line.
13. A process according to any one of claims 9 to 12 in which the means for adjusting humidity of the compressed air is an injector for introducing a water, mist or spray into the compressed air line.
14. A process according to any one of claims 9 to 13 in which a by-pass loop diverts compressed air around the desiccant tower and a control valve is provided to switch the airflow between the desiccant tower and the by-pass loop.
15. A process according to claim 14 in which the control valve is adjustable so that varying proportions of compressed air can be sent through the desiccant tower and bypass loop.
16. A process according to any one of claims 9 to 15 in which the substance subjected to milling is a drug substance.
17. A process according to claim 16 in which the drug substance is a crystalline hydrate.
18. A process according to claim 10 or 17 in which the crystalline hydrate is calcium mupirocin dihydrate.
19. Calcium mupirocin dihydrate having a moisture content of from 3.0 to 4.0%, more preferably 3.4 to 3.7%, and a low amorphous content.
20. Micronised calcium mupirocin dihydrate obtainable by a process as defined in any one of claims 9 to 18.
21. A pharmaceutical composition comprising a drug substance milled by a process according to any one of claims 9 to 18 dispersed in a pharmaceutically acceptable carrier.
22. A pharmaceutical composition as claimed in claim 21 in which the drug substance is calcium mupirocin dihydrate.
10
PCT/GB1999/001189 1998-04-22 1999-04-19 Fluid energy milling process and apparatus WO1999054048A1 (en)

Priority Applications (14)

Application Number Priority Date Filing Date Title
IL13887499A IL138874A0 (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
CA002329732A CA2329732A1 (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
HU0102244A HUP0102244A3 (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus for it
PL99343563A PL343563A1 (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
BR9909806-7A BR9909806A (en) 1998-04-22 1999-04-19 Grinding process with fluid energy and apparatus
KR1020007011637A KR20010042863A (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
AT99918105T ATE255466T1 (en) 1998-04-22 1999-04-19 METHOD AND APPARATUS FOR JET GRINDING
EP99918105A EP1073524B1 (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
JP2000544437A JP2002512117A (en) 1998-04-22 1999-04-19 Fluid energy grinding method and apparatus
NZ507489A NZ507489A (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
AU36149/99A AU748262B2 (en) 1998-04-22 1999-04-19 Fluid energy milling process and apparatus
DE1999613331 DE69913331T2 (en) 1998-04-22 1999-04-19 METHOD AND DEVICE FOR BEAM GRINDING
NO20005235A NO20005235L (en) 1998-04-22 2000-10-18 Fluid energy process and apparatus
HK01104886A HK1034216A1 (en) 1998-04-22 2001-07-12 Fluid energy milling process and apparatus.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GBGB9808470.0A GB9808470D0 (en) 1998-04-22 1998-04-22 Novel process and apparatus
GB9808470.0 1998-04-22

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WO1999054048A1 true WO1999054048A1 (en) 1999-10-28

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EP (1) EP1073524B1 (en)
JP (1) JP2002512117A (en)
KR (1) KR20010042863A (en)
CN (1) CN1108151C (en)
AR (3) AR015000A1 (en)
AT (1) ATE255466T1 (en)
AU (1) AU748262B2 (en)
BR (1) BR9909806A (en)
CA (1) CA2329732A1 (en)
CO (1) CO4820444A1 (en)
CZ (1) CZ292385B6 (en)
DE (1) DE69913331T2 (en)
ES (1) ES2211073T3 (en)
GB (1) GB9808470D0 (en)
HK (1) HK1034216A1 (en)
HU (1) HUP0102244A3 (en)
IL (1) IL138874A0 (en)
NO (1) NO20005235L (en)
NZ (1) NZ507489A (en)
PL (1) PL343563A1 (en)
TR (1) TR200003035T2 (en)
TW (1) TW558453B (en)
WO (1) WO1999054048A1 (en)
ZA (1) ZA200005739B (en)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2000032165A1 (en) * 1998-12-01 2000-06-08 Aventis Pharma Limited Milling process for the production of finely milled medicinal substances
WO2000044352A1 (en) * 1999-01-28 2000-08-03 Schering Corporation Method of preparing particles for agglomeration
US6623760B1 (en) 1999-01-28 2003-09-23 Schering Corporation Method of preparing particles for agglomeration
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WO2012120284A1 (en) 2011-03-04 2012-09-13 Sosei R&D Ltd Use of glycopyrrolate for treating tachycardia
EP2702983A1 (en) 2012-08-31 2014-03-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the preparation of a bispyridiniumalkane-containing semisolid preparation
EP2218509A3 (en) * 2009-02-12 2017-02-08 Linde AG Nonequilibrium humidity control for jet milling
WO2017042341A1 (en) 2015-09-09 2017-03-16 Vectura Limited Jet milling method
EP2968152B1 (en) 2013-03-15 2018-11-28 Pearl Therapeutics, Inc. Methods and systems for conditioning of particulate crystalline materials
US10532041B2 (en) 2014-09-09 2020-01-14 Vectura Limited Formulation comprising glycopyrrolate, method and apparatus

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WO2000032165A1 (en) * 1998-12-01 2000-06-08 Aventis Pharma Limited Milling process for the production of finely milled medicinal substances
AU763352B2 (en) * 1998-12-01 2003-07-17 Aventis Pharma Limited Milling process for the production of finely milled medicinal substances
US6641063B2 (en) 1998-12-01 2003-11-04 Aventis Pharma Limited Milling process for the production of finely milled medicinal substances
WO2000044352A1 (en) * 1999-01-28 2000-08-03 Schering Corporation Method of preparing particles for agglomeration
US6623760B1 (en) 1999-01-28 2003-09-23 Schering Corporation Method of preparing particles for agglomeration
EP1516614A1 (en) * 1999-01-28 2005-03-23 Schering Corporation Method of preparing particles for agglomeration
EP2422767A2 (en) 2004-04-30 2012-02-29 Vectura Limited Methods for preparing dry powder compositions of glycopyrrolate
EP2422766A2 (en) 2004-04-30 2012-02-29 Vectura Limited Methods for preparing dry powder compositions of glycopyrrolate
WO2007144901A1 (en) * 2006-06-12 2007-12-21 Jubilant Organosys Limited Process for stabilization of olanzapine polymorphic form i
EP2218509A3 (en) * 2009-02-12 2017-02-08 Linde AG Nonequilibrium humidity control for jet milling
MD4369C1 (en) * 2011-03-04 2016-04-30 Sosei R&D Ltd Use of glycopyrrolate for treating tachycardia, unit dose, delivery device, method of treatment and prophylaxis of tachycardia
WO2012120284A1 (en) 2011-03-04 2012-09-13 Sosei R&D Ltd Use of glycopyrrolate for treating tachycardia
EP2702983A1 (en) 2012-08-31 2014-03-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the preparation of a bispyridiniumalkane-containing semisolid preparation
DE102012215511A1 (en) 2012-08-31 2014-06-12 Schülke & Mayr GmbH Process for the preparation of a semi-solid preparation containing bispyridiniumalkane
EP2968152B2 (en) † 2013-03-15 2022-06-22 Pearl Therapeutics, Inc. Methods and systems for conditioning of particulate crystalline materials
EP2968152B1 (en) 2013-03-15 2018-11-28 Pearl Therapeutics, Inc. Methods and systems for conditioning of particulate crystalline materials
US11471468B2 (en) 2013-03-15 2022-10-18 Pearl Therapeutics, Inc. Methods and systems for conditioning of particulate crystalline materials
US10532041B2 (en) 2014-09-09 2020-01-14 Vectura Limited Formulation comprising glycopyrrolate, method and apparatus
EP3191081B1 (en) 2014-09-09 2020-03-25 Vectura Limited Formulation comprising glycopyrrolate, method and apparatus
EP3689332A1 (en) 2014-09-09 2020-08-05 Vectura Limited Formulation comprising glycopyrrolate, method and apparatus
WO2017042341A1 (en) 2015-09-09 2017-03-16 Vectura Limited Jet milling method
US11229915B2 (en) 2015-09-09 2022-01-25 Vectura Limited Jet milling method
EP3689339A1 (en) 2015-09-09 2020-08-05 Vectura Limited Jet milling method
US11759791B2 (en) 2015-09-09 2023-09-19 Vectura Limited Jet milling method

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