WO2004062784A1

WO2004062784A1 - Process and device for particle formation

Info

Publication number: WO2004062784A1
Application number: PCT/GB2004/000031
Authority: WO
Inventors: Andreas Kordikowski; Darren John Gilbert
Original assignee: Nektar Therapeutics Uk Limited
Priority date: 2003-01-08
Filing date: 2004-01-07
Publication date: 2004-07-29
Also published as: GB0300338D0

Abstract

Method for preparing a target substance in particulate form, by introducing into a particle formation vessel, through separate first and second fluid inlets respectively, (a) a solution or suspension of the target substance in a fluid vehicle (the 'target solution/suspension') and (b) à compressed fluid anti-solvent for the substance, and allowing the anti-solvent to extract the vehicle from the target solution/suspension so as to form particles of the target substance, the anti-solvent having a sonic, near-sonic or supersonic velocity as it enters the particle formation vessel, wherein the anti-solvent and the target solution/suspension enter the vessel at différent locations and meet downstreazn (in the direction of anti-solvent flow) of the second fluid inlet, and wherein the outlet of the first fluid inlet has a diameter of less than 0.1 mm.

Description

PROCESS AND DEVICE FOR PARTICLE FORMATION

Field of the invention

This invention relates to methods and apparatus for use in forming particles of a target substance, and to their particulate products.

Background to the invention

It is known to use a compressed fluid, typically a supercritical or near-critical fluid, as an anti- solvent to precipitate particles of a substance of interest (a "target substance") from solution or suspension. The basic technique is known as "GAS" (Gas Anti-Solvent) precipitation [Gallagher et al, "Supercritical Fluid Science and Technology", ACS Symp. Ser., 406, p334 (1989)]. Versions of it have been disclosed for instance in EP-0 322 687 and WO-90/03782.

In one particular version known as the Nektar™ SCF particle formation process (previously known as SEDS™ or "Solution Enhanced Dispersion by Supercritical fluids"), a target substance is dissolved or suspended in an appropriate fluid vehicle, and the resulting "target solution/suspension" then co-introduced into a particle formation vessel with an anti-solvent fluid (usually supercritical) in which the vehicle is soluble. The co-introduction is effected in a particular way, such that:

- the target solution/suspension and the anti-solvent both meet and enter the vessel at substantially the same point; and

- at that point, the mechanical energy of the anti-solvent serves to disperse the target solution/suspension (ie, to break it up into individual fluid elements) at the same time as the anti-solvent extracts the vehicle so as to cause particle formation.

Thus, in the Nektar™ SCF process, the compressed fluid serves not only as an anti-solvent but also as a mechanical dispersing agent. The simultaneity of fluid contact, dispersion and particle formation provides a high degree of control over the physicochemical properties of the particulate product. Versions of this process are described in WO-95/01221, WO-96/00610, WO-98/36825, WO- 99/44733, WO-99/59710, WO-01/03821, WO-01/15664 and WO-02/38127. Other "SEDS™"- based processes are described in WO-99/52507, WO-99/52550, WO-00/30612, WO-00/30613, WO-00/67892 and WO-02/58674.

Another version of the GAS technique is described in WO-97/31691, in which a special form of two-fluid nozzle is used to introduce a "target solution/suspension" and an energising gas into a particle formation vessel containing a supercritical anti-solvent. The energising gas can be the same as the anti-solvent fluid. Within the nozzle, a restriction generates sonic waves in the energising gas/anti-solvent flow and focusses them back (ie, in a direction opposite to that of the energising gas flow) on the outlet of the target solution suspension passage, resulting in mixing of the fluids within the nozzle before they enter the particle formation vessel. It is suggested that where the energising gas is the same as the anti-solvent (typically supercritical carbon dioxide), its flow rate could be sufficiently high to obtain a sonic velocity at the nozzle outlet. However, the authors do not appear ever to have achieved such high velocities in their experimental examples.

Other modifications have been made to the basic GAS process in order to affect atomisation of the target solution suspension at the point of its contact with the compressed fluid anti-solvent. For example, US-5, 770,559 describes a GAS precipitation process in which a target solution is introduced, using a sonicated spray nozzle, into a pressure vessel containing a supercritical or near-critical anti-solvent fluid - see also Randolph et al in Biotechnol. Prog., 1993, 9, 429-435.

Our co-pending PCT patent application published as WO-03/008082 describes a version of the Nektar™ SCF GAS process in which a target solution/suspension and a compressed fluid anti- solvent are introduced separately into a particle formation vessel through first and second fluid inlet means respectively, the anti-solvent having a near-sonic, sonic or supersonic velocity as it enters the vessel. The outlet of the first fluid inlet means is preferably positioned downstream of, and directly in line with, that of the second inlet means, so that the target solution/suspension is introduced directly into the anti-solvent flow. The internal diameter of the first fluid inlet means is suggested to be in the range from 0.1 to 0.2 mm, more preferably from 0.1 to 0.15 mm, such as the 0.125 mm diameter inlet tube used in the examples of the document. It is also stated that the outlet of the first fluid inlet means preferably has a smaller cross sectional area than that of the second fluid inlet means, most preferably less than 70 % or 65 % as large. It would be generally desirable to provide alternative particle formation techniques which combined one or more of the advantages of the prior art methods with a broader applicability (for instance, for a wider range of target substances, vehicles and or anti-solvents) and or a higher degree of control over the product characteristics. In particular it is generally desirable, especially for pharmaceutical substances, to be able to produce small (even sub-micron) particles with narrow size distributions.

Statements of the invention

According to a first aspect of the present invention there is provided a method for preparing a target substance in particulate form, the method comprising introducing into a particle formation vessel, through separate first and second fluid inlets respectively, (a) a solution or suspension of the target substance in a fluid vehicle (the "target solution/suspension") and (b) a compressed fluid anti-solvent for the substance, and allowing the anti-solvent fluid to extract the vehicle from the target solution/suspension so as to form particles of the target substance, the anti- solvent fluid having a sonic, near-sonic or supersonic velocity as it enters the particle formation vessel, wherein the anti-solvent and the target solution/suspension enter the particle formation vessel at different locations and meet downstream (in the direction of anti-solvent flow) of the second fluid inlet, and further wherein the outlet of the first fluid inlet has a diameter of less than 0.1 mm.

Thus, the present invention is a modification of the method disclosed in WO-03/008082, but using a much smaller diameter outlet for the target solution/suspension than is taught for the earlier method. Surprisingly, this has been found to allow production, with good yields and without apparatus blockages, of small particles with narrow size distributions.

The outlet of the first fluid inlet preferably has a diameter of 0.09 or 0.08 mm or less, more preferably of 0.07 or 0.06 mm or less, yet more preferably of 0.05 or 0.04 or 0.03 mm or less. It may for instance be in the range 0.02 to 0.08 mm, or from 0.02 to 0.07 mm. In cases it may be as low as 0.01 or even 0.005 mm.

The outlet of the first fluid inlet preferably has a cross sectional area which is smaller than that of the second fluid inlet, for example less than 30 % as large, more preferably less than 25 % or 20 % as large and most preferably less than 10 % or 8 % or 5 % or 3 % as large. In cases it may be less than 1 % or 0.5 % or 0.1 % as large as that of the second fluid inlet. The first fluid inlet preferably comprises a capillary tube, for example with a capillary internal diameter the same as that of its outlet.

By "sonic velocity" and "supersonic velocity", in the context of the present invention, is meant respectively that the velocity of the anti-solvent fluid as it enters the vessel is the same as or greater than the velocity of sound in that fluid at that point. By "near-sonic velocity" is meant that the anti-solvent velocity on entry into the vessel is slightly lower than, but close to, the velocity of sound in that fluid at that point - for instance its "Mach number" M (the ratio of its actual speed to the speed of sound) is greater than 0.8, preferably greater than 0.9 or 0.95. Generally speaking, in the method of the invention, the Mach number for the anti-solvent fluid on entering the particle formation vessel may be from 0.8 to 1.5, preferably from 0.9 to 1.3.

A near-sonic, sonic or supersonic anti-solvent velocity may be achieved by selecting appropriate operating conditions, in particular the temperature and pressure of the anti-solvent fluid as it enters the particle formation vessel, the temperature and pressure within the vessel (which may be controlled in conventional manner, for instance using an oven and a back pressure regulator) and the geometry (in particular size) of the second fluid inlet.

(References in this specification to a fluid entering a vessel are to the fluid exiting an inlet means (for example, a nozzle) used to introduce the fluid into the vessel. For these purposes, therefore, the inlet means is to be considered as upstream of the vessel in the direction of fluid flow, although parts of it (in particular its outlet) may be located physically within the vessel.)

There needs to be a drop in pressure as the anti-solvent fluid enters the particle formation vessel. This is typically achieved by imparting a relatively high "back pressure" to the anti-solvent, for example by using a high anti-solvent flow rate and forcing it through a restriction such as a nozzle into a vessel maintained at a significantly lower pressure.

However, this pressure reduction can cause undesirable Joule-Thomson cooling of the anti- solvent. Accordingly, the temperature of the anti-solvent upstream of the particle formation vessel needs to be sufficiently high that the fluid remains at an appropriate temperature (typically above its critical temperature T₀), even after expanding into the vessel. The method of the invention thus preferably includes pre-heating the anti-solvent fluid, upstream of the particle formation vessel, to a temperature sufficient to compensate for its Joule-Thomson cooling as it enters the vessel. Thus, in the method of the present invention, preferably (i) the pressure in the particle formation vessel is P] which is preferably greater than the critical pressure P₀ of the anti-solvent, (ii) the anti-solvent is introduced through a restricted inlet so as to have a back pressure of P₂, (iii) the temperature in the particle formation vessel is T] which is preferably greater than the critical temperature T₀ of the anti-solvent, (iv) the anti-solvent is introduced into the vessel at a temperature T₂, where T₂ is greater than Ti, (v) Ti and T₂ are such that Joule-Thomson cooling of the anti-solvent as it enters the vessel does not reduce the anti-solvent temperature to below that required of it at the point of particle formation (and are preferably such that the anti-solvent temperature does not fall below T₀ within the vessel) and (vi) Pi, P₂, Ti and T₂ are such that the anti-solvent fluid has a sonic, near-sonic or supersonic velocity as it enters the particle formation vessel.

Again the anti-solvent and the target solution/suspension must be introduced separately into the particle formation vessel and contact each other downstream of (preferably immediately downstream of) the point of anti-solvent entry into the vessel.

The anti-solvent expansion as it enters the particle formation vessel is isenthalpic. Thus, an appropriate temperature for the anti-solvent upstream of the vessel may be derived from enthalpy charts for the fluid, for instance as illustrated for carbon dioxide in Fig 1. (For C0₂, the critical temperature T_c is 31 °C (304 K) and the critical pressure P₀ is 74 bar.) Fig 1 shows how, when working with a pressure reduction from 300 to 80 bar for the C0₂ on entering a particle formation vessel, the upstream temperature should be at least 360 K (87 °C) to achieve an appropriate temperature of 308 K (35 °C) or greater when the C0₂ enters the vessel.

Thus, a carbon dioxide anti-solvent is preferably introduced with an upstream temperature of 80 °C (353 K) or higher, more preferably from 80 °C to 170 °C (443 K).

The pressures and temperatures needed to ensure a near-sonic, sonic or supersonic velocity depend on the nature of the anti-solvent fluid. In the case of a carbon dioxide anti-solvent, for instance, in order to achieve a sonic or supersonic velocity the operating conditions must satisfy the formula:

k

where p_t is the total C0₂ pressure upstream of entry into the particle formation vessel (ie, the C0₂ back pressure plus the pressure in the vessel) andp₀ is the C0₂ pressure immediately on entry into the vessel, and k is the ratio of the specific heats of C0₂ at constant pressure (C_p) and constant volume (C_v) [see, for instance, International Thermodynamic Tables of the Fluid State, Angus et al, Pergamon Press, 1976, or the standard reference data program of the National Institute of Standards and Technology (NIST), Gaithersburg, USA].

So, for example the C0₂ may be introduced at a temperature of 360 K (87 °C) with an inlet pressure of 300 bar, and the vessel may be at 309 K (36 °C) and 80 bar (ie, the outlet pressure p₀ is 80 bar). At 309 K and 80 bar, A: for C0₂ is 11.41¹. At 360 K and 300 bar, Hs 2.28¹. Taking a geometric average for lc of 5.10, as the C0₂ enters the vessel, then substituting these

values into the above equation gives — = 0.267 and = 0.393, which corifirms that the

P, k + l

C0₂ flow is supersonic irrespective of the C0₂ flow rate into the vessel, so long as there is an appropriate pressure differential between p_{ and p₀. A suitable C0₂ flow might be for instance from 170 to 200 g/min. A suitable pressure drop as the C0 enters the particle formation vessel might be from 170 to 250 bar.

An alternative method for calculating the anti-solvent velocity (again for carbon dioxide, using the same operating conditions as above but with a vessel temperature of 40 °C, and introducing the C0₂ through a nozzle of outlet diameter 0.2 mm) is:

(i) density ofC0₂ at 309 K and 80 bar¹ is 0.355 g/cm³,

(ϋ) therefore, volumetric flow of C0₂ at 200 g/min (Q) is 200/0.355 = 563 cm³/min.

(iii) Surface area (A) of the nozzle = 3.14 x l0^"4 cm²,

(iv) therefore velocity of C0₂ = Q ÷ (A x 60 x 100) = 299 m/s.

(v) Speed of sound in C0₂ at 309 K and 80 bar¹ is 189 m/s.

¹ International thermodynamic tables of the fluid state - 3. Carbon dioxide, Angus et al, Pergamon Press, 1976 [see also the standard reference data program of the National Institute of Standards and Technology (NIST), Gaithersburg, USA]. (vi) Thus, the C0₂ velocity is confirmed as being supersonic under such conditions.

Although we do not wish to be bound by this theory, it is believed that in the method of the invention, a so-called "Mach disk" is generated in the anti-solvent flow downstream of the second fluid inlet. In this region the fluid velocity will change abruptly to sub-sonic thus generating shock waves in the fluids present (in effect a continuous, low volume, supersonic boom). These shock waves are thought to aid mixing and dispersion of the target solution/suspension with the anti-solvent. It is unlikely that the waves will be ultrasonic as in for example the system described in WO-97/31691. Moreover they will propagate in the direction of the anti-solvent flow, rather than in a counter-current sense as in for instance the nozzle described in WO-97/31691 which is said to reflect a sonic wave back towards a source of energising gas.

The arrangement of the first and second fluid inlets will preferably be such that the Mach disk is generated either upstream of (in the direction of anti-solvent flow), or at, the point of entry of the target solution/suspension into the particle formation vessel. It should occur on or close to the main (central) axis of anti-solvent flow, thus typically also in line with the central longitudinal axis of the second fluid inlet. The shock waves should propagate along the main axis of anti-solvent flow, ie, again typically in line with the central longitudinal axis of the second fluid inlet.

The near-sonic, sonic or supersonic anti-solvent velocity is ideally achieved, in the method of the present invention, simply by the use of appropriate anti-solvent flow rates, back pressures and/or operating temperatures, and without the aid of mechanical, electrical and/or magnetic input such as for example from impellers, impinging surfaces especially within the anti-solvent inlet, electrical transducers and the like. . Introducing the anti-solvent via a convergent nozzle, or via a convergent-divergent nozzle, ideally as a single fluid stream, may also help in the achievement of appropriate fluid velocities. Further "energising" fluid streams, such as those required in the method of WO-97/31691, are not then needed in order to achieve the desired level of control over the contact between the target solution/suspension and the anti-solvent fluid.

Not all designs of fluid inlet may permit an anti-solvent velocity which is truly faster than the speed of sound. A perfectly cylindrical nozzle will for instance, according to theory, not permit a supersonic velocity in a fluid flowing from it. Nevertheless, even in such a case, it is possible according to the present invention to use a combination of temperature, pressure, back pressure and flow rate which give rise, in theory (using the above types of calculations), to a supersomc velocity, and in practice to generate an anti-solvent flow which on entering the particle formation vessel is either sonic or near-sonic. Moreover, a nozzle which has a nominally cylindrical section may not in practice be truly cylindrical, again allowing deviations from the theoretical maximum velocity.

The use of near-sonic, sonic or supersonic anti-solvent velocities, together with an extremely small outlet for the target solution/suspension, can allow achievement of smaller particle sizes and narrower size distributions in GAS-based particle formation processes. In particular it can^' allow the formation of small micro- or even nano-particles, for instance of volume mean diameter less than 10 urn, preferably 5 um or less, more preferably 2 μ or less, yet more preferably 1 μm or 900 nm or 600 nm or 500 nm or less. Such particulate products preferably have narrow size distributions, such as with a particle size spread of 5 or less, such as from 1.5 to 3, preferably from 1.5 to 2.5, such as 2.2 or less. (Particle size "spread" is defined as (D₉₀ - Dio) D₅₀ where D is the volume mean diameter of the relevant particle population.)

Particle sizes may be measured for instance using (a) an Aerosizer™ time-of-flight instrument (which gives an aerodynamic equivalent particle diameter, MMAD) or (b) a laser diffraction sensor such as the Helos™ system available from Sympatec GmbH, Germany (which provides a geometric projection equivalent MMD). Volume mean diameters may be obtained in both cases using commercially available software packages.

It appears that the combination of a near-sonic, sonic or supersonic anti-solvent velocity with a small target solution/suspension outlet leads to highly efficient dispersion of the target solution/suspension, and a high degree of control over the physicochemical properties of the product particles. It also appears to facilitate more efficient vehicle extraction, thus potentially yielding particles which have not only a more controlled size and size distribution but also lower residual solvent levels and generally lower levels of impurities. A particulate product prepared according to the invention will typically contain less than 2000 ppm of residual solvent. It preferably contains less than 1000 or 500 ppm, more preferably less than 200 ppm, most preferably less than 150 or 100 or even 50 ppm residual solvent, by which is meant solvents) which were present at the point of particle formation, for instance in the target solution/suspension and or the anti-solvent fluid. Still more preferably the product contains no detectable residual solvent, or at least only levels below the relevant quantification limit(s). Generally such a product will preferably contain 2.5 % w/w or less, more preferably 2 or 1.5 or 1 % w/w or less of impurities, by which is meant substances (either solid or liquid phase) other than the target substance(s) intended to be formed into particles.

The method of the invention can also generate particles which exhibit less agglomeration and generally improved handling properties. Its products tend to have smooth and relatively low energy surfaces, typically less adhesive than those of corresponding products made by prior art techniques (particularly techniques other than the Nektar™ SCF technique); they are typically in the form of free flowing powders, preferably non- or only loosely agglomerated.

When practising the method of the invention, the anti-solvent fluid must be in a compressed state, by which is meant that, at the relevant operating temperature, it is above its vapour pressure, preferably above atmospheric pressure, more preferably from 70 to 150 bar or from 75 to 120 bar. In cases the anti-solvent may be introduced at a pressure (ie, its "back pressure") of from 70 to 300 bar, from 100 to 250 bar, from 150 to 250 bar or from 180 to 220 bar. The anti- solvent fluid is preferably a fluid which is a gas at atmospheric pressure and ambient temperature. In other words, it should have a vapour pressure above 1 bar at ambient temperature (eg, at 18 to 25 °C, such as at 22 °C).

More preferably "compressed" means close to, at or yet more preferably above the critical pressure P₀ for the fluid concerned. Thus, the anti-solvent is preferably a supercritical or near- critical fluid, although it may alternatively be a compressed Hquid such as for instance liquid C0₂. In practice, the pressure is likely to be in the range (1.01 - 9.0)P_o, preferably (1.01 - 7.0)P_C for a supercritical or near-critical fluid anti-solvent, or for example (0.7 - 3.0)P_C, preferably (0.7 - 1.7)P_C, for a compressed liquid anti-solvent such as liquid C0₂.

As used herein, the term "supercritical fluid" means a fluid at or above its critical pressure (P_c) and critical temperature (T_c) simultaneously. In practice, the pressure of the fluid is likely to be in the range (1.01 - 9.0)P_C, preferably (1.01 - 7.0)P_C, and its temperature in the range (1.01 -

4.0)T_o (measured in Kelvin). However, some fluids (eg, helium and neon) have particularly low critical pressures and temperatures, arid may need to be used under operating conditions well in excess of (such as up to 200 times) those critical values.

"Near-critical fluid" is here used to refer to a fluid which is either (a) above its T_c but sHghtly below its P₀, (b) above its P_c but slightly below its T₀ or (c) slightly below both its T_c and its P₀. The term "near-critical fluid" thus encompasses both high pressure liquids, which are fluids at or above their critical pressure but below (although preferably close to) their critical temperature, and dense vapours, which are fluids at or above their critical temperature but below (although preferably close to) their critical pressure.

By way of example, a high pressure liquid might have a pressure from about 1.01 to 9 times its P₀, and a temperature from about 0.5 to 0.99 times its T_c. A dense vapour might, correspondingly, have a pressure from about 0.5 to 0.99 times its P_c, and a temperature from about 1.01 to 4 times its T_c.

The terms "compressed fluid", "supercritical fluid" and "near-critical fluid" each encompass a mixture of fluid types, so long as the overall mixture is in the compressed, supercritical or near- critical state respectively.

In the method of the present invention, it may be preferred that the operating temperature (ie, the temperature in the particle formation vessel) be close to the critical temperature T_c of the mixture of anti-solvent and vehicle formed at the point of fluid contact. For example, the temperature might be from 0.9 to 1.1 times T₀ (in Kelvin), preferably from 0.95 to 1.05 times T_c, more preferably from 0.97 to 1.03 or from 0.98 to 1.02 times T₀, or perhaps from 1 to 1.05 or 1 to 1.03 or 1 to 1.02 times T_c. This is because at T_c the velocity of sound in a fluid is theoretically zero; near-sonic, sonic and supersonic velocities can thus more readily be achieved, using lower anti-solvent flow rates, as T_c is approached.

The anti-solvent should be a compressed (preferably supercritical or near-critical, more preferably supercritical) fluid at its point of entry into the particle formation vessel and preferably also within the vessel and throughout the particle formation process. Thus, for a carbon dioxide anti-solvent the temperature in the particle formation vessel is ideally greater than 31 °C, for example from 31 to 100 °C, preferably from 31 to 70 °C, and the pressure greater than 74 bar, for example from 75 to 350 bar, preferably from 75 to 200 bar, more preferably from 75 to 150 or 120 bar or from 80 to 100 bar.

Carbon dioxide is a highly suitable anti-solvent, but others include nitrogen, nitrous oxide, sulphur hexafluori.de, xenon, ethylene, chlorotrifluoromethane and other chlorofluorocarbons, ethane, trifluoromethane and other hydrofluorocarbons, and noble gases such as helium or neon.

The anti-solvent must be miscible or substantially miscible with the fluid vehicle at the point of their contact, so that the anti-solvent can extract the vehicle from the target solution/suspension. By "miscible" is meant that the two fluids are miscible (ie, they can form a single phase mixture) in all proportions, and "substantially miscible" encompasses the situation where the fluids can rnix sufficiently well, under the operating conditions used, as to achieve the same or a similar effect, ie, dissolution of the fluids in one another and precipitation of the target substance. However the anti-solvent must not, at the point of particle formation, extract or dissolve the target substance. In other words, it must be chosen so that the target substance is for all practical purposes (in particular, under the chosen operating conditions and taking into account any fluid modifiers present) insoluble or substantially insoluble in it. Preferably the target substance is less than 10^"3 mole %, more preferably less than 10^"5 mole %, soluble in the anti-solvent fluid.

The anti-solvent fluid may optionally contain one or more modifiers, for example water, methanol, ethanol, isopropanol or acetone. A modifier (or co-solvent) may be described as a chemical which, when added to a compressed fluid such as a supercritical or near-critical fluid, changes the ability of that fluid to dissolve other materials. When used, a modifier preferably constitutes not more than 40 mole %, more preferably not more than 20 mole %, and most preferably from 1 to 10 mole %, of the anti-solvent fluid.

The vehicle is a fluid which is able to carry the target substance in solution or suspension. It may be composed of one or more component fluids, eg, it may be a mixture of two or more solvents. It must be soluble (or substantially soluble) in the chosen anti-solvent fluid at their point of contact. It may contain, in solution or suspension, other materials apart from the target substance.

The target solution/suspension may in particular comprise two or more fluids which are mixed in situ at or immediately before their point of contact with the anti-solvent. Such systems are described, eg, in WO-96/00610 and WO-01/03821. The two or more fluids may carry two or more target substances, to be combined in some way (for instance, co-precipitated as a matrix, or one precipitated as a coating around the other, or precipitated as the product of an in situ reaction between the substances) at the point of particle formation. Target substance(s) may also be carried in the anti-solvent fluid as well as in the target solution(s)/suspension(s).

A target substance may be any substance which needs to be produced in particulate form. Examples include pharmaceuticals; nutraceuticals; pharmaceutical or nutraceutical excipients such as carriers; dyestuffs; cosmetics; foodstuffs; coatings; agrochemicals; products of use in the ceramics, explosives or photographic industries; etc... It may be organic or inorganic, monomeric or polymeric. It is preferably soluble or substantially soluble in the relevant fluid vehicle, preferably having a solubility in it of 10^"4 mole % or greater under the conditions under which the target solution is prepared (ie, upstream of the point of particle formation).

In a preferred embodiment of the invention, the target substance is for use in or as a pharmaceutical or pharmaceutical excipient. It may in particular comprise a pharmaceutically active substance, especially one for which a small particle size and/or narrow particle size distribution is important, for instance a drug intended for use in inhalation therapy or one for which rapid and/or efficient in vivo dissolution is desirable. The present invention is also highly suitable for producing target substances for which a high degree of purity (including polymorphic purity and/or reduced residual solvent levels) is desired.

The target substance may be in a single or multi-component form (eg, it could comprise an mtimate mixture of two materials, or one material in a matrix of another, or one material coated onto a substrate of another, or other similar mixtures). The particulate product, formed from the target substance(s) using the method of the invention, may also be in such a multi-component form - examples include two pharmaceuticals intended for co-administration, or a pharmaceutical together with a polymer carrier matrix. Such products may be made, as described above, from solutions/suspensions containing only single component starting materials, provided the solutions suspensions are contacted with the anti-solvent fluid in the correct manner. The particulate product may comprise a substance formed from an in situ reaction (ie, immediately prior to, or on, contact with the anti-solvent) between two or more reactant substances each carried by an appropriate fluid.

Particular examples of coated multi-component products include where one target substance is an active (eg, pharmaceutically active) substance, and another an excipient to be deposited as a coating around the first one (for example to provide a controlled release and or taste-masked drug formulation). Alternatively one target substance may comprise a core of an excipient onto which an active substance is to be coated. A yet further alternative is that both target substances are active substances, for instance pharmaceutically active materials intended for co- administration.

In the method of the invention, the anti-solvent and the target solution/suspension are introduced separately into the particle formation vessel (which is preferably the vessel in which the formed particles are collected) and contact each other after (preferably immediately after) the point of anti-solvent entry into the vessel. Their contact ideally takes place at the same or substantially the same point as the target solution/suspension enters the vessel, eg, as a consequence of the solution/suspension being introduced directly into the anti-solvent flow. In these ways, particle formation can be made to occur at a point where there is a high degree of control over conditions such as the temperatures, pressures and flow rates of the fluids.

The fluids are ideally introduced in such a way that the mechanical (kinetic) energy of the anti- solvent fluid can act to disperse the target solution/suspension at the same time as it extracts the vehicle; this again allows a high degree of control over the physicochemical characteristics of the particulate product, in particular the size and size distribution of the particles and their solid state properties. "Disperse" in this context refers generally to the transfer of kinetic energy from one fluid to another, usually implying the formation of droplets, or of other analogous fluid elements, of the fluid to which the kinetic energy is transferred. Thus, the fluid inlet means used to introduce the fluids should allow the mechanical energy (typically the shearing action) of the anti-solvent flow to facilitate intimate mixing of the fluids and to disperse them, at the point where the fluids meet.

Introducing the two fluids separately can help prevent apparatus blockages at their points of entry (in particular at the anti-solvent inlet), due for example to the highly efficient extraction of the vehicle into the anti-solvent under the operating conditions used. At the same time a high degree of control can be retained over the mechanism for fluid contact, and this control may be achieved for example at least partly by introducing the anti-solvent fluid with a sonic, near- sonic or supersonic velocity. Other ways in which such control may be achieved or improved upon include providing controlled agitation within the particle formation vessel, and/or within one or more of the fluid inlets, in particular in the region of fluid contact immediately downstream of the respective target solution/suspension and anti-solvent inlets. For example, the target solution/suspension may be dispersed onto a sonicating surface at or immediately prior to its contact with the anti-solvent fluid. Agitation may alternatively be achieved for instance by stirring, such as with a turbine, propeller, paddle, impeller or the like.

That said, the present invention may if necessary be practised in the absence of such additional agitation means, particularly within the particle formation vessel.

Generally it is unnecessary in the method of the present invention to use more than one anti- solvent flow stream in order to disperse, and extract the vehicle from, the target solution suspension. Thus, an impinging flow of a second anti-solvent fluid, such as is used to aid dispersion in the Nektar™ SCF process described in WO-98/36825, is typically not present when practising the method of the present invention.

The target solution/suspension may be introduced into the vessel through any suitable fluid inlet so long as it has the requisite outlet diameter, including one which effects, or assists in effecting, controlled atomisation of the solution/suspension. The anti-solvent fluid is preferably introduced through a nozzle, more preferably a convergent nozzle which focuses a flowing fluid stream through a smaller area outlet, or a nozzle of the convergent-divergent type.

The target solution/suspension is preferably introduced with a back pressure, for instance from 5 to 250 bar or from 50 to 200 bar or from 50 to 150 bar. This can generally be achieved by manipulation of the solution/suspension flow rate, the pressure in the particle formation vessel and the size and geometry of the outlet through which it is introduced into the vessel. In particular, the outlet may present a restriction in the solution/suspension flow as it enters the vessel, as for example in a nozzle or other similar reduced area outlet.

Preferably the target solution/suspension and the anti-solvent meet immediately downstream of the point of anti-solvent entry. "Immediately" in this context imphes a sufficiently small time interval (between the anti-solvent entering the particle formation vessel and its contact with the target solution/suspension) as preferably still to allow transfer of mechanical energy from the anti-solvent to the solution/suspension so as to achieve dispersion. Nevertheless, there is still preferably a short interval of time between anti-solvent entry and fluid contact so as to eliminate, or substantially eliminate or at least reduce, the risk of apparatus blockage due to particle formation at the points of fluid (in particular anti-solvent) entry. The timing of the fluid contact will depend on the natures of the fluids, the target substance and the desired end product, as well as on the size and geometry of the particle formation vessel and the fluid inlets and on the fluid flow rates. The contact may occur within 0 or 0.001 to 25 or 50 milliseconds, preferably within 0.001 to 10 milliseconds, more preferably within 0.01 to 5 or 10 milliseconds, of the anti-solvent entering the particle formation vessel. Generally it will occur within 0.1 milliseconds, preferably within 0.05 or 0.02 milliseconds, more preferably within 0.01 milliseconds, still more preferably within 0.005 or even 0.001 rnilliseconds, of the anti-solvent entering the vessel.

The target solution/suspension is typically introduced directly into the anti-solvent flow, and thus meets with the anti-solvent flow at the point where the target solution/suspension enters the vessel. Thus, where for instance the anti-solvent inlet generates a conical fluid stream, the outlet of the first fluid inlet may be located, in use, within the emerging anti-solvent cone - the dimensions of this cone depend, inter alia, on the geometry of the anti-solvent outlet, on the anti-solvent velocity and also on the operating conditions (eg, temperature, pressure and anti- solvent back pressure). The diameter of the cone will also increase with distance from the anti- solvent outlet.

The outlet of the first fluid inlet is preferably located on or close to the main (central) axis of anti-solvent flow, suitably within 2 mm, more preferably within 1 mm and most preferably within 0.5 or 0.3 mm of that axis (these distances being measured in a plane perpendicular to the axis itself). Typically this means that the solution/suspension outlet is in line with, or close to being in line with, the central longitudinal axis of the second fluid inlet (for instance a nozzle).

Again the degree of separation which is tolerable between the target solution/suspension outlet and the axis of anti-solvent flow may depend on factors such as those listed above which determine the geometry of the anti-solvent flow stream, it being generally desirable for the target solution/suspension to be introduced directly into the anti-solvent flow and also at a location where the anti-solvent has sufficient kinetic energy to achieve efficient dispersion of the target solution suspension.

It may be suitable for the separation between the target solution/suspension outlet and the main axis of anti-solvent flow (measured in a plane perpendicular to that axis) to be no more than 10 times, preferably no more than 8 times, more preferably no more than 5 times or 3 times the diameter of the anti-solvent outlet.

Preferably the outlet of the first fluid inlet is located vertically below that of the second fluid inlet, and the anti-solvent fluid flows into the particle formation vessel in a vertically downwards direction. "Vertical" for these purposes includes directions which are no more than 30 or preferably 20 or 10 ° from the vertical.

It may be preferred for the target solution/suspension to enter the anti-solvent flow at the same or a similar distance (from the point of anti-solvent entry) as the Mach disk which is generated in the anti-solvent flow stream due to its near-sonic, sonic or supersonic velocity. If not coincident with the Mach disk, the point of entry of the target solution suspension is preferably downstream, in the direction of anti-solvent flow, rather than upstream of the Mach disk position. The position, or approximate position, of the Mach disk (being the region in which the anti- solvent velocity changes abruptly from near-sonic, sonic or supersonic to sub-sonic) may be calculated for instance using computational fluid dynamics models, with reference to the velocity and or density gradients in the fluid flow streams emerging from the first and in particular the second fluid inlet. Alternatively it may be observed, either visually or using other appropriate forms of imagery, through for example a view cell in the particle formation vessel wall - Schlieren imaging, for instance, in the region downstream of the second fluid inlet, allows density gradients (and therefore shock waves) to be captured as an index of refraction gradients, using optical imaging equipment; shadowgraphy can also allow observation of acoustic waves in the anti-solvent flow stream.

At the point where the target solution/suspension and the anti-solvent meet, the angle between their axes of flow may be from 0° (ie, the two fluids are flowing in parallel directions) to 180° (ie, oppositely-directed flows), more typically from 45 to 135°. However, they preferably meet at a point where they are flowing in approximately perpendicular directions, ie, the angle between their axes of flow is from 70 to 110°, more preferably from 80 to 100°, such as 90°.

Suitable fluid inlet means, which may be used to achieve the form of fluid contact required by the first aspect of the invention, are described below in connection with the second aspect.

Use of such a fluid inlet system can allow Nektar™ SCF and other GAS-based particle formation techniques to be practised in cases where the vehicle for the target solution/suspension is a relatively high boiling fluid (eg, boiling point greater than about 150 °C, or even greater than 180 °C) such as dimethyl formamide (DMF), dimethyl sulphoxide (DMSO), dimethyl acetamide (DMA), diethyl acetamide (DEA) or N-methyl pyrollidinone (NMP), or where the target substance is temperature sensitive. Since the anti-solvent and the target solution/suspension enter the vessel separately, the latter can be maintained at a desired lower temperature despite the use of a relatively high temperature for the mcoming anti-solvent. Moreover, the use of a sonic, near-sonic or supersonic anti-solvent velocity can be sufficient to disperse the target solution/suspension at relatively low operating temperatures (ie, vessel temperatures) - again this assists in the processing of temperature sensitive target substances and vehicles.

When carrying out the present invention, the particle formation vessel temperature and pressure are ideally controlled so as to allow particle formation to occur at or substantially at the point where the target solution/suspension meets the anti-solvent fluid (which is generally the point at which the target solution enters the vessel). The conditions in the vessel must generally be such that the anti-solvent fluid, and the solution which is formed when it extracts the vehicle, both remain in the compressed (preferably supercritical or near-critical, more preferably supercritical) form whilst in the vessel. For the supercritical, near-critical or compressed solution, this means that at least one of its constituent fluids (usually the anti-solvent fluid, which in general will be the major constituent of the mixture) should be in a supercritical, near- critical or compressed state, as the case may be, at the time of particle formation. There should at that time be a single-phase mixture of the vehicle and the anti-solvent fluid, otherwise the particulate product might be distributed between two or more fluid phases, in some of which it might be able to redissolve. This is why the anti-solvent fluid needs to be miscible or substantially miscible with the vehicle.

The terms "supercritical solution", "near-critical solution" and "compressed solution" mean respectively a supercritical, near-critical or compressed fluid together with a fluid vehicle which it has extracted and dissolved. The solution should itself still be in the supercritical, near- critical or compressed state, as the case may be, and exist as a single phase, at least within the particle formation vessel.

Selection of appropriate operating conditions will be influenced by the natures of the fluids involved (in particular, their P₀ and T_c values and their solubility and miscibility characteristics) and also by the characteristics desired of the particulate end product, for instance yield, particle size and size distribution, purity, morphology or crystalline, polymorphic or isomeric form.

Variables include the flow rates of the anti-solvent fluid and the target solution/suspension, the concentration of the target substance in the vehicle, the temperature and pressure inside the particle formation vessel, the anti-solvent temperature upstream of the vessel and the construction and relative positioning of the fluid inlets into the vessel, in particular the sizes of the target solution/suspension and anti-solvent outlets and the distance between them. The method of the invention preferably involves controlling one or more of these variables so as to influence the physicochemical characteristics of the particles formed.

The flow rate of the anti-solvent fluid relative to that of the target solution suspension, and its pressure and temperature, should be sufficient to allow it to accommodate the vehicle, so that it can extract the vehicle and hence cause particle formation. The anti-solvent flow rate will generally be higher than that of the target solution/suspension - typically, the volumetric ratio of the target solution/suspension flow rate to the anti-solvent flow rate (both measured at or immediately prior to the two fluids coming into contact with one another) will be 0.001 or greater, preferably from 0.002 to 0.1 or from 0.002 to 0.06, more preferably from 0.004 to 0.05, such as from 0.005 to 0.02.

The anti-solvent flow rate will also generally be chosen to ensure an excess of the anti-solvent over the vehicle when the fluids come into contact, to minimise the risk of the vehicle re- dissolving and/or agglomerating the particles formed. At the point of its extraction into the anti- solvent, the vehicle may constitute from 0.5 or 1 to 80 mole %, preferably 50 mole % or less or 30 mole % or less, more preferably from 1 to 20 mole % and most preferably from 1 to 10 or from 1 to 5 mole %, of the compressed fluid mixture formed.

Both the anti-solvent and the target solution/suspension are ideally introduced into the particle formation vessel with a smooth, continuous and preferably pulse-less or substantially pulse-less flow. Conventional apparatus may be used to ensure such fluid flows.

The method of the invention preferably additionally involves collecting the particles following their formation, more preferably in the particle formation vessel itself.

According to a second aspect of the present invention, there is provided apparatus for use in preparing a target substance in particulate form, and in particular for use in a method according to the first aspect of the invention, the apparatus comprising:

(i) a particle formation vessel;

(ii) a first fluid inlet for introducing into the vessel a solution or suspension of the target substance in a fluid vehicle (the "target solution/suspension"); and

(iii) a second fluid inlet, separate from the first, for introducing a compressed fluid anti- solvent into the particle formation vessel;

wherein the first and second fluid inlets are so arranged that, in use, a target solution/suspension introduced through the first and an anti-solvent introduced through the second enter the particle formation vessel at different locations and meet downstream, preferably immediately downstream (in the direction of anti-solvent flow), of the second fluid inlet,

and further wherein the outlet of the first fluid inlet has a diameter of less than 0.1 mm. The first fluid inlet suitably comprises a fluid inlet tube, for instance of stainless steel or fused silica, which might typically have an internal diameter the same as that of its outlet to the particle formation vessel but may instead have a tapered outlet section. The first fluid inlet may comprise an outlet tube section, for example a length of capillary tubing, having an outlet diameter of less than 0.1 mm, mounted in fluid communication with a wider diameter tube section through which fluid may be directed from its source towards the outlet tube section and thence to the particle formation vessel. The resultant reduction in tube diameter may be used to induce a back pressure in the target solution/suspension flow, the magnitude of which may be varied by altering for example the length and/or outlet diameter of the outlet tube section.

Preferably the outlet of the first fluid inlet has a diameter of 0.09 or 0.08 mm or less, more preferably of 0.07 or 0.06 mm or less, yet more preferably of 0.05 or 0.04 or 0.03 mm or less. It may for instance be in the range 0.02 to 0.08 mm, or from 0.02 to 0.07 mm. In cases it may be as low as 0.01 or even 0.005 mm. Suitably its cross sectional area is smaller than that of the second fluid inlet, for example less than 50 % as large, more preferably less than 30 % or 25 % or 20 % as large and most preferably less than 10 % or 8 % or 5 % or 3 % as large. In cases it may be less than 2 % or 1 % or 0.5 % or 0.1 % as large as that of the second fluid inlet.

The second fluid inlet preferably provides a restriction at the point of fluid entry into the particle formation vessel: for instance, the second fluid inlet may comprise a nozzle. Again it may suitably be made from stainless steel. It preferably has at least one passage of internal diameter from for instance 1 to 2 mm, more preferably from 1.3 to 1.9 mm, such as 1.6 mm. Again, it may have a tapered outlet section (ie, be a "convergenf'-type nozzle), with an angle of taper (with respect to the central longitudinal axis of the nozzle) typically in the range 10 ° to 70 °, such as from 20 ° to 40 ° or from 50 to 70 °. Alternatively it may have a divergent outlet, with the same typical angle of taper as for the convergent version. A nozzle of the convergent- divergent type may also be suitable for use as the second fluid inlet.

The opening at the outlet end (tip) of the second fluid inlet will preferably have a diameter in the range of 0.005 to 5 mm, more preferably 0.05 to 2 mm, most preferably from 0.1 to 0.5 mm, for instance about 0.1, 0.2, 0.3 or 0.35 mm. ϊ cases a smaller diameter outlet may be preferred as it may contribute to higher yields; an outlet diameter of from 0.1 to 0.3 mm or from 0.15 to 0.25 mm may therefore be suitable for the second fluid inlet. The dimensions of the fluid inlets will naturally depend on the scale on which the particle formation is to be carried out; for commercial scale manufacture, for example, the above nozzle dimensions may be up to ten times larger.

A nozzle of the above type may comprise more than one fluid passage; for instance it may comprise two or more coaxial passages such as in the nozzles described in WO-95/01221, WO- 96/00610 and WO-98/36825, particularly if additional fluids are to be introduced into the system. One or more of the passages may be used to introduce two or more fluids at the same time, and the inlets to such passages may be modified accordingly.

The outlet of the first fluid inlet (into the particle formation vessel) is preferably immediately downstream, in the direction of anti-solvent flow in use, of that of the second fluid inlet. A suitable separation for the two outlets is a short distance such as from 0 or 0.1 to 50 times, preferably from 10 to 40 times, more preferably from 10 to 30 or from 15 to 25, such as about 20, times the diameter of the outlet of the second fluid inlet. In some cases the preferred separation might be from 15 to 20 times the diameter of the outlet of the second fluid inlet, in others from 18 to 27 or from 20 to 25 times. Suitable distances might lie from 0 to 10 mm or from 0.1 or 0.5 to 10 mm, preferably from 2 to 8 mm or from 2 to 6 mm, for instance about 4 or 5 mm, in particular for an anti-solvent outlet diameter of 0.2 mm or thereabouts. For an anti- solvent outlet diameter of 0.4 mm or thereabouts, a suitable distance between the two fluid outlets might be from 4 to 10 mm or from 6 to 8 mm, such as about 7 mm. In some cases smaller separations may be appropriate, such as from 0 to 2 mm, preferably from 0 or 0.1 mm to 1.5 or 1 mm.

What constitutes a separation of "0" may depend on practical constraints such as the thickness of the walls of the inlets and the assembly in which they are mounted; generally it will correspond to the two outlets being as close to coincident as possible. Again, the separation between outlets may depend on the scale of the process which the inlets are to be used for.

It is believed, although we do not wish to be bound by this theory, that there may be an optimum separation between the two outlets which represents a balance between avoiding undue agglomeration of the particles as they form whilst also maximising the efficiency of fluid mixing and vehicle extraction. If the target solution/suspension is introduced into the anti- solvent flow close to the outlet of the second fluid inlet, then fluid mixing will be highly efficient and particle formation rapid, but there may also be an increased tendency for agglomeration of the particles as they form, resulting ultimately in a larger diameter product. Conversely, if the two fluids meet at too great a distance from the outlet of the second fluid inlet, then fluid mixing and vehicle extraction may be less efficient, reducing control over the product characteristics (including particle size and morphology), potentially allowing more particle growth and higher residual solvent levels and possibly also reducing yields.

Such distances are suitably measured between the centres of the relevant fluid outlets, or alternatively from the external wall of the fluid inlet, for instance from that point on the external wall which is closest to the anti-solvent outlet.

As described above in connection with the first aspect of the invention, the outlet of the first fluid inlet is preferably located downstream, in the direction of anti-solvent flow, of the Mach disk which is generated in the anti-solvent flow stream. This outlet may be located at the same or a similar distance (from the outlet of the second fluid inlet, measured along the main axis of anti-solvent flow) as the Mach disk.

Preferably the outlet of the first fluid inlet is positioned such that, in use, it is within the flow of anti-solvent fluid exiting the second fluid inlet. More preferably it is positioned on or close to the main axis of anti-solvent flow, thus typically in line with the central longitudinal axis of the second fluid inlet. Most preferred is an arrangement in which the centre of the outlet of the first fluid inlet corresponds to the centre of the outlet of the second fluid inlet, ie, the centres of the two outlets are both positioned on the central longitudinal axis of the second fluid inlet and/or along the main axis of anti-solvent flow.

The first and second fluid inlets are preferably arranged so that at the point where the target solution/suspension and the anti-solvent meet, the angle between their axes of flow is from 70 to 110°, more preferably from 80 to 100°, most preferably about 90°.

The first and second fluid inlets may for convenience be provided as part of a single fluid inlet assembly which may be placed in fluid communication with the particle formation vessel and with sources of the anti-solvent fluid and the target solution/suspension.

Thus, according to a third aspect, the present invention provides a fluid inlet assembly for use as part of apparatus according to the second aspect of the invention, and/or in a method according to the first aspect. In apparatus according to the second aspect of the invention, the particle formation vessel preferably contains particle collection means, such as a filter, by which particles of the target substance may be collected in the vessel in which they form, downstream of the point of contact between the target solution/suspension and the anti-solvent fluid.

The apparatus may additionally comprise a source of a compressed (preferably supercritical or near-critical) fluid and/or a source of a target solution or suspension. The former may itself comprise means for altering the temperature and/or pressure of a fluid so as to bring it into a compressed (preferably supercritical or near-critical) state. The apparatus conveniently includes means for controlling the pressure in the particle formation vessel, for example a back pressure regulator downstream of the vessel, and/or means (such as an oven) for controlling the temperature in the vessel. The vessel is conveniently a pressure vessel and should be capable of withstanding the pressures necessary to maintain compressed (preferably supercritical or near- critical) conditions during the particle formation process, as described above in connection with the method of the invention.

A fourth aspect of the present invention provides a particulate product formed using a method according to the first aspect and/or apparatus according to the second.

Because embodiments of the present invention are modified versions of the inventions disclosed in WO-95/01221, WO-96/00610, WO-98/36825, WO-99/44733, WO-99/59710, WO-01/03821, WO-01/15664, WO-02/38127 and WO-03/008082, technical features described in those documents, for instance regarding the selection of appropriate reagents and operating conditions, can apply also to the present invention. The nine earlier documents are therefore intended to be read together with the present application.

In this specification the term "substantially", when applied to a condition, is meant to encompass the exact condition (eg, exact simultaneity) as well as conditions which are (for practical purposes, taking into account the degree of precision with which such conditions can be measured and achieved) close to that exact condition, and/or which are similar enough to that exact condition as to achieve, in context, the same or a very similar effect.

References to solubilities and miscibilities, unless otherwise stated, are to the relevant fluid characteristics under the operating conditions used, ie, under the chosen conditions of temperature and pressure and taking into account any modifiers present in the fluids. The present invention will now be illustrated with reference to the following non-limiting examples and the accompanying figures, of which:

Fig 1 is a plot of the enthalpy variation of C0₂ with temperature and pressure, illustrating the change in C0₂ temperature during its isenthalpic expansion;

Fig 2 illustrates schematically apparatus suitable for use in carrying out a method according to the present invention;

Figs 3 to 5 are schematic longitudinal cross sections and an under plan view respectively of parts of a fluid inlet assembly useable with the Fig 2 apparatus;

Figs 6 and 7 are schematic longitadinal cross sections through parts of an alternative fluid inlet assembly useable with the Fig 2 apparatus; and

Figs 8 and 9 are SEMs (scarining electron micrographs) of the respective products of Examples Al and A2 below.

Detailed description

Fig 2 shows apparatus suitable for carrying out methods in accordance with the present invention. Item 1 is a particle formation vessel, within which the temperature and pressure can be controlled by means of the heating jacket 2 and back pressure regulator 3. The vessel 1 contains a particle collection device (not shown) such as a filter, filter basket or filter bag. A fluid inlet assembly 4 allows introduction of a compressed (typically supercritical or near- critical) fluid anti-solvent from source 5 and one or more target solutions/suspensions (or additional fluid v ehicles if desired) from sources such as 6 and 7. The items labelled 8 are pumps, and 9 is a cooler. A recycling system 11 allows vehicle recovery.

The fluid inlet assembly 4 may for example take the form shown in Figs 3 to 5. Fig 3 shows the assembly schematically, in use with the particle formation vessel 1 of the Fig 2 apparatus. Nozzle 21 is for introduction of the anti-solvent fluid. It has only a single passage of circular cross section, with a circular outlet 22. Alternatively, a multi-component nozzle may be used, with anti-solvent introduced through one or more of its passages and the remaining passages either closed off or else used to introduce additional reagents. (For example, a multi-passage nozzle of the type described in WO-95/01221 or WO-96/00610 may be used. Such nozzles have two or more concentric (coaxial) passages, the outlets of which are typically separated by a short distance to allow a small degree of internal mixing to take place between fluids introduced through the respective passages before they exit the nozzle. The anti-solvent could for instance be introduced through the inner passage of such a nozzle, traversing a small "mixing" zone as it exits that inner passage and then passing through the main nozzle outlet into the particle formation vessel.)

Although this is not shown in Fig 3, the nozzle may have a tapered (typically convergent) end, with an outlet of smaller diameter than that of the main nozzle passage.

Inlet tube 23 is for introduction of the target solution/suspension, and is so shaped and located that the direction of flow of the solution/suspension at its outlet 24 (see Fig 5) will be perpendicular to that of the anti-solvent exiting nozzle 21. Again the tube is of circular cross section.

Fig 4 shows how tube 23 is mounted, by means of the supporting and locking pieces 25, on a collar 26 which is itself mounted around the lower portion of the nozzle 21. The arrangement is such as to allow adjustment of the distance "d" between the outlets of nozzle 21 and tube 23. It can be seen that the outlet of tube 23 is positioned in line with the central longitudinal axis of the nozzle 21.

Both the nozzle 21 and the tube 23 are preferably made from stainless steel.

The assembly of Figs 3 to 5 may be less likely to suffer blockages (at the nozzle and tube outlets) than when a multi-component nozzle of the type described in WO-95/01221 is used to co-introduce the anti-solvent and target solution suspension together, particularly when the operating conditions are such as to allow a very rapid and efficient removal of the solvent vehicle, from the target solution/suspension, by the anti-solvent.

An assembly such as that of Figs 3 to 5 may be used to generate acoustic waves when the velocity of an anti-solvent fluid introduced through the nozzle 21 approaches or exceeds sonic. These waves, in the form of fluid ripples propagating in the direction of anti-solvent flow, can be viewed optically using focused shadowgraphy. For example, using a convergent nozzle with a 0.2 mm diameter outlet, and supercritical carbon dioxide as the anti-solvent with a flow rate of 200 g/min, an acoustic wave structure is weakly visible in the anti-solvent flow downstream of the nozzle outlet, at vessel-to-nozzle pressure ratios of approximately 0.6 and below (this is also the approximate pressure ratio above which the anti-solvent flow transitions from sonic to subsonic), and more clearly visible at pressure ratios of about 0.3 and below, for instance of about 0.25 or 0.23 or below. Lower vessel-to-nozzle pressure ratios may be achieved by increasing the anti-solvent flow rate such as to 275 or 520 g/min. The waves also become clearer when using a 0.3 mm diameter nozzle outlet.

A target solution tube 23 positioned 4 mm vertically below the nozzle outlet is in such cases downstream of the point from which these sonic waves propagate, ie, downstream of any "Mach disk" generated in the anti-solvent flow stream.

Schlieren techniques may be used for higher sensitivity viewing of such acoustic wave patterns.

An alternative fluid inlet assembly 4, for use in the Fig 2 apparatus, is illustrated in Figs 6 and 7. Again a nozzle 21, as in Figs 3 to 5, is used to introduce the anti-solvent via its outlet 22, which again is preferably tapered. A tube 30, similar to tube 23 in Figs 3 to 5, introduces the target solution suspension.

A length of thin capillary tubing 31 is mounted, preferably although not necessarily centrally, within the outlet of tube 30, for instance with a suitable adhesive 32. This gives a much smaller (eg, of the order of 0.05 mm) effective diameter for the solution outlet 33. The length of the capillary 31, and its cross-sectional area relative to that of the tube 30, determine the degree of back pressure generated in the target solution flow on entering the vessel 1.

Other ways of achieving a small solution outlet are of course possible, for instance using an alternative form of connection between the main solution inlet tube 30 and a smaller diameter outlet tube section.

The tube 30 and capillary 31 are preferably fixed in position relative to one another. They are mounted in a support (shown schematically at 34) which allows their horizontal (x) and vertical (y) separations from the anti-solvent nozzle outlet 22 to be varied, preferably continuously. Fig 6 for instance shows the solution outlet 33 directly in line with the central longitudinal axis of the nozzle 21 (ie, with the main axis of anti-solvent flow) and Fig 7 shows the outlet 33 displaced from that axis by a distance x, shown exaggerated for clarity.

The relative positions of the anti-solvent and solution outlets are preferably similarly variable in the fluid inlet assembly of Figs 3 to 5. Examples A

Apparatus as shown in Fig 2, incorporating a fluid inlet assembly as shown in Figs 6 and 7, was used to carry out particle formation methods in accordance with the invention. The nozzle 21 comprised a fluid inlet tube of internal diameter 0.75 mm, a convergent tip with a 60 ° half angle taper (with respect to the central longitudinal nozzle axis) and an outlet of diameter 0.2 mm. According to theory, this generates a fluid jet with a cone angle of approximately 20 °.

The target solution inlet comprised a fused silica capillary of length 20 mm and internal diameter 50 μm, glued into a standard 1.59 mm (1/16") internal diameter stainless steel tube. Its outlet, into the particle formation vessel 1, was therefore 50 μm in diameter, and its cross sectional area only 6 % of that of the outlet of nozzle 21. A two-component epoxy resin was used to secure the capillary in place, under elevated temperatures (180 °C) to enhance the mechanical strength of the bond. Due to the viscous flow of the uncured resin, it was not possible to centre the capillary within the stainless steel tube.

The vertical separation "y" between the nozzle outlet 21 and the solution tube outlet 33 was 4 mm. For convenience, y was measured from the top external wall of the capillary tube.

The target solution contained 3 % w/v salmeterol xinafoate in methanol, and was introduced at a flow rate of either 1 rnVmin or 4 ml min. In the former case, a back pressure of 12 bar was measured across the solution inlet and in the latter, a back pressure of 85 bar.

Supercritical carbon dioxide was used as the anti-solvent. It was pumped at a flow rate (of hquid C0₂, prior to passing through a heater) of 200 ml/min. Its temperature on entry into the nozzle 21 was 356 K (83 °C).

The pressure in the particle formation vessel 1 (capacity 2 litres) was maintained at 80 bar and 309 K (36 °C). The C0₂ back pressure was between 170 and 220 bar. These conditions created a supersonic C0₂ velocity at the nozzle outlet 22.

Particle formation was allowed to occur by the action of the C0₂ anti-solvent, and the products collected in the vessel 1. The products were assessed by scariring electron microscopy (SEM) and their particle sizes analysed using a Sympatec™ apparatus at 2 bar shear pressure.

The results are shown in Table 1. Table 1

*Particle size spread is defined as (D₉₀ - Dio) / D₅₀ where D is the volume mean diameter of the relevant particle population.

Figs 8 and 9 show SEMs of the products of experiments Al and A2 respectively.

These data illustrate that fine particles can be successfully produced using the method of the present invention. No pressure fluctuations occurred during the experiments, indicating no significant blockages in the fluid inlets.

The data also show that increasing the target solution flow rate (and hence also the back pressure across the solution inlet) can lead to a significant reduction in particle size and a narrowing of particle size distribution, as well as improved yield.

Comparative Examples B

The results of Examples A, carried out in accordance with the present invention, were compared with that obtained from Example B, in which a two-component coaxial nozzle, of the type shown in Fig 3 of WO-95/01221, was used to co-introduce a 3 % w/v salmeterol xinafoate in methanol solution and a supercritical C0₂ anti-solvent.

The operating temperature and pressure, within the particle formation vessel, were 60 °C and 200 bar. The C0₂ flow rate was 200 ml/min, thus under these conditions a sub-sonic velocity. The target solution flow rate 4 riij/min. The nozzle used had a convergent tip (60 ° half angle) with a 0.2 mm outlet diameter. The target solution was introduced through the outer nozzle passage (internal diameter 2.3 mm) and the anti-solvent through the inner passage (internal diameter 0.75 mm). The particle formation vessel had a capacity of 2 litres. The product yield was 73 % w/w. The particle size (volume mean diameter, measured using a Sympatec™ apparatus at 2 bar shear pressure and representing the average of two analyses) was 9.9 μm, with a spread of 2.15.

Thus, the method of the present invention can give improved yields and particle sizes compared to those achieved using (with sub-sonic anti-solvent velocities) the two-component coaxial nozzle of WO-95/01221.

Claims

1. A method for preparing a target substance in particulate form, the method comprising introducing into a particle formation vessel, through separate first and second fluid inlets respectively, (a) a solution or suspension of the target substance in a fluid vehicle (the "target solution/suspension") and (b) a compressed fluid anti-solvent for the substance, and allowing the anti-solvent fluid to extract the vehicle from the target solution/suspension so as to form particles of the target substance, the anti-solvent fluid having a sonic, near-sonic or supersonic velocity as it enters the particle formation vessel, wherein the anti-solvent and the target solution/suspension enter the particle formation vessel at different locations and meet downstream (in the direction of anti- solvent flow) of the second fluid inlet, and further wherein the outlet of the first fluid inlet has a diameter of less than 0.1 mm.

2. A method according to claim 1, wherein the outlet of the first fluid inlet has a diameter ofO.Oό mm or less.

3. A method according to any one of the preceding claims, wherein the Mach number of the anti-solvent as it enters the particle formation vessel (ie, the ratio of the anti-solvent velocity to the velocity of sound in that fluid at that point) is from 0.8 to 1.5.

4. A method according to any one of the preceding claims, wherein the anti-solvent is preheated, upstream of the particle formation vessel, to a temperature sufficient to compensate for its Joule-Thomson cooling as it enters the vessel.

5. A method according to any one of the preceding claims, wherein (i) the pressure in the particle formation vessel is P_l5 (ii) the anti-solvent is introduced through a restricted inlet so as to have a back pressure of P₂, (iii) the temperature in the particle formation vessel is Ti, (iv) the anti-solvent is introduced into the vessel at a temperature T₂, where T₂ is greater than Ti, (v) Ti and T₂ are such that Joule-Thomson cooling of the anti- solvent as it enters the vessel does not reduce the anti-solvent temperature to below that required of it at the point of particle formation and (vi) Pi, P₂, Ti and T₂ are such that the anti-solvent fluid has a sonic, near-sonic or supersonic velocity as it enters the particle formation vessel.

6. A method according to any one of the preceding claims, wherein the anti-solvent and the target solution/suspension meet immediately downstream of the point of anti-solvent entry into the particle formation vessel.

7. A method according to any one of the preceding claims, wherein the anti-solvent and the target solution/suspension meet within 0.001 to 0.1 milliseconds of the anti-solvent entering the particle formation vessel.

8. A method according to any one of the preceding claims, wherein a Mach disk is generated in the anti-solvent flow downstream of the second fluid inlet, thus generating shock waves which propagate in the direction of the anti-solvent flow.

9. A method according to claim 8, wherein the arrangement of the first and second fluid inlets is such that the Mach disk is generated either upstream of (in the direction of anti- solvent flow), or at, the point of entry of the target solution/suspension into the particle formation vessel, and/or at a similar distance (from the point of anti-solvent entry, measured along the main axis of anti-solvent flow) as the point of entry of the target solution/suspension.

10. A method according to any one of the preceding claims, wherein the anti-solvent is introduced into the particle formation vessel with a back pressure of from 100 to 250 bar.

11. A method according to any one of the preceding claims, wherein the anti-solvent is a supercritical or near-critical fluid.

12. A method according to any one of the preceding claims, wherein the anti-solvent is carbon dioxide.

13. A method according to any one of the preceding claims, wherein the target substance comprises a pharmaceutical or pharmaceutical excipient.

14. A method according to any one of the preceding claims, wherein the fluids are introduced in such a way that the mechanical (kinetic) energy of the anti-solvent fluid can act to disperse the target solution/suspension at the same time as it extracts the vehicle.

15. A method according to any one of the preceding claims, wherein the target solution/suspension is introduced into the particle formation vessel with a back pressure.

16. A method according to any one of the preceding claims, wherein the target solution/suspension is introduced directly into the anti-solvent flow, and meets with the anti-solvent flow at the point where the target solution/suspension enters the vessel.

17. A method according to any one of the preceding claims, wherein the outlet of the first fluid inlet is located vertically below that of the second fluid inlet, and the anti-solvent fluid flows into the particle formation vessel in a vertically downwards direction.

18. A method according to any one of the preceding claims, wherein the volumetric ratio of the target solution/suspension flow rate to the anti-solvent flow rate (both measured at or immediately prior to the two fluids corning into contact with one another) is from 0.002 to 0.06.

19. A method according to any one of the preceding claims, which additionally involves collecting the particles following their formation, within the particle formation vessel.

20. A method for preparing a target substance in particulate form, the method being substantially as herein described with reference to the accompanying illustrative drawings.

21. Apparatus for use in preparing a target substance in particulate form, the apparatus comprising:

(i) a particle formation vessel;

(ii) a first fluid inlet for introducing into the vessel a solution or suspension of the target substance in a fluid vehicle (the "target solution suspension"); and

(iii) a second fluid inlet, separate from the first, for introducing a compressed fluid anti-solvent into the particle formation vessel; wherein the first and second fluid inlets are so arranged that, in use, a target solution/suspension introduced through the first and an anti-solvent introduced through the second enter the particle formation vessel at different locations and meet downstream (in the direction of anti-solvent flow) of the second fluid inlet,

and further wherein the outlet of the first fluid inlet has a diameter of less than 0.1 mm.

22. Apparatus according to claim 21, wherein the outlet of the first fluid inlet has a diameter of0.06 mm or less.

23. Apparatus according to claim 21 or claim 22, wherein the outlet of the first fluid inlet has a cross sectional area which is smaller than that of the second fluid inlet.

24. Apparatus according to claim 23, wherein the outlet of the first fluid inlet has a cross sectional area which is less than 10 % as large as that of the second fluid inlet.

25. Apparatus according to any one of claims 21 to 24, wherein the first fluid inlet comprises an outlet tube section having an outlet diameter of less than 0.1 mm, mounted in fluid communication with a wider diameter tube section through which the target solution/suspension may be directed from its source towards the outlet tube section and thence to the particle formation vessel.

26. Apparatus according to any one of claims 21 to 25, wherein the second fluid inlet comprises a convergent nozzle which can focus a flowing fluid stream through a smaller area outlet.

27. Apparatus according to any one of claims 21 to 26, wherein the outlet of the first fluid inlet is positioned such that, in use, it is within the flow of anti-solvent fluid exiting the second fluid inlet.

28. Apparatus according to claim 27, wherein the centres of the outlets of the first and second fluid inlets are both positioned on the central longitudinal axis of the second fluid inlet and/or along the main axis of anti-solvent flow.

29. Apparatus according to any one of claims 21 to 28, wherein the separation between (a) the outlet of the first fluid inlet and (b) the main axis of anti-solvent flow (measured in a plane perpendicular to that axis) is no more than 10 times the diameter of the outlet of the second fluid inlet.

30. Apparatus according to any one of claims 21 to 29, wherein the fluid inlets are arranged such that at the point where the target solution/suspension and the anti-solvent meet, the angle between their axes of flow is from 70 to 110 °.

31. Apparatus according to any one of claims 21 to 30, wherein the outlet of the first fluid inlet (into the particle formation vessel) is immediately downstream, in the direction of anti-solvent flow in use, of that of the second fluid inlet.

32. Apparatus according to any one of claims 21 to 31, wherein the separation between the outlets of the first and second fluid inlets is from 10 to 30 times the diameter of the outlet of the second fluid inlet.

33. Apparatus according to claim 32, wherein the separation between the outlets of the first and second fluid inlets is from 15 to 25 times the diameter of the outlet of the second fluid inlet.

34. Apparatus according to any one of claims 21 to 33, wherein the first and second fluid inlets are provided as part of a single fluid inlet assembly which may be placed in fluid communication with the particle formation vessel and with sources of the anti-solvent fluid and the target solution/suspension.

35. Apparatus according to any one of claims 21 to 34, wherein the particle formation vessel contains particle collection means by which particles of the target substance may be collected in the vessel in which they form, downstream of the point of contact between the target solution/suspension and the anti-solvent fluid.

36. Apparatus according to any one of claims 21 to 35, which additionally comprises a source of a compressed fluid.

37. Apparatus for use in preparing a target substance in particulate form, the apparatus being substantially as herein described with reference to the accompanying illustrative drawings.

8. A fluid inlet assembly for use as part of apparatus according to any one of claims 21 to 37, and/or in a method according to any one of claims 1 to 20.