Patent Application
20180344747
This disclosure relates generally to systems and methods for the preparation and stabilization of particulate materials. More specifically, this disclosure relates to systems and methods for conditioning particulate materials to improve the physicochemical stability of the materials as well as compositions incorporating such particles.
Particulate crystalline materials, including micronized crystalline particulates, are useful in a variety of contexts. For example, certain industrially useful compounds are conveniently stored in bulk as dry, particulate powders. Additionally, certain compounds can be better utilized or incorporated into commercial products when provided as micronized crystalline particulates. This can be seen with pharmaceutically active compounds that exhibit improved formulation, delivery, or therapeutic attributes when provided in micronized crystalline form.
However, processes used to produce certain crystalline materials can result in material characteristics that introduce an undesired level of physiochemical instability. Techniques for micronization of crystalline material often utilize energy-intensive milling, grinding, shearing or particle-to-particle collisions to reduce particle size. An example of one such technique is air jet milling, which uses high velocity air or gas to cause particle-to-particle collisions and to generate micronized material, including particles ranging from about 0.5 to about 30 μm in diameter. The exertion of thermal or mechanical energy during energy-intensive micronization processes can cause the formation of non-crystalline, amorphous material that can lead to significant physicochemical instability of the resulting micronized particles. Such amorphous material may be present in the form of amorphous regions on otherwise crystalline particles or as substantially amorphous particles.
The presence of amorphous material within micronized crystalline material can result in a propensity for the particles to fuse, aggregate, and/or agglomerate. In certain cases, the instability appears particularly acute when the micronized material is exposed, even for very short periods of time, to an environment that includes a solvent capable of solubilizing or plasticizing the amorphous material. In such instances, exposure of the micronized material often leads to recrystallization of amorphous material contained therein or sorbed, vapor-driven conversion of amorphous phase to crystalline phase, which can be accompanied by fusing and agglomeration of the micronized particles. The fusing, aggregation and/or agglomeration of the micronized particles can cause significant changes in particle size and the overall particle size distribution of the micronized material, which is problematic for applications requiring the long-term physical stability of the micronized material.
In addition, processes used in the manufacture and purification of crystalline materials can leave undesired contaminants. For example, solvents, including various organic solvents, play an important role in the manufacture of pharmaceutically active compounds and excipients used in the production of drug products. Solvents are often used during the synthesis of pharmaceutically active compounds and drug product excipients to increase yields or aid in crystallization. In many manufacturing processes, the final purification step involves crystallization or re-crystallization of the desired compound, and the crystalline material formed in such processes can entrap solvent present in the solution from which the material is crystallized. Even after subjecting the material to a drying step, such as a freeze-drying or a high-temperature drying process, solvent entrapped in a crystalline material is often difficult to completely remove, and some amount of residual solvent can remain. The presence of residual solvent, even in small amount can have undesirable effects. Organic solvents, in particular, can present health and safety hazards and can influence product efficacy, safety and stability.
Systems and methods for conditioning particulate crystalline material are described herein. Conditioning a particulate crystalline material according to the present description generally involves (i) providing a particulate material to be conditioned, (ii) delivering the material to be conditioned to a mixing zone where it is combined with a conditioning gas, (iii) maintaining the material in contact with the conditioning gas within a conditioning zone for a desired residence time, (iv) separating the conditioned material from the conditioning gas, and (v) collecting the conditioned material. In carrying out a conditioning process according to the present description, the material to be conditioned is typically entrained or aerosolized within a delivery gas that is blended with the conditioning gas, and the particulate material remains entrained, suspended or aerosolized in the conditioning gas as it travels through the conditioning zone. The nature of the conditioning gas and the residence time of the particulate material within the conditioning zone are controlled to accomplish annealing or phase transformation of the material.
In certain embodiments, the systems and methods described herein may be adapted for conditioning a single crystalline material. In alternative embodiments, the systems and methods described herein may be adapted to simultaneously condition two or more crystalline materials. For example, where two or more materials are to be conditioned simultaneously, the materials may be introduced into a conditioning zone as a blended material or as individual materials delivered via independent material inputs.
Additionally, the systems and methods described herein can be configured and adapted to provide one or more conditioning steps. For example, in certain embodiments, systems and methods may be adapted to provide a conditioning gas and conditioning zone that subject the particulate material to annealing conditions whereby amorphous material is converted into a more stable crystalline structure, and the amorphous content of the of the crystalline material is measurably reduced or eliminated. In other embodiments, the systems and methods described herein may be adapted to anneal particulate crystalline material by reducing the presence of residual solvent(s). In such embodiments, the systems and methods may be adapted to provide a conditioning gas and conditioning zone that subject the particulate material to annealing conditions whereby residual solvent within the crystalline material is reduced, removed, or replaced by, for example, vaporization or by solvent exchange. In still other embodiments, the methods and systems described herein can be adapted to both reduce or eliminate amorphous content and reduce or eliminate the presence of residual solvent(s). In such embodiments, the different annealing processes may be conducted simultaneously (e.g., using a conditioning gas and conditioning zone that serves to reduce both amorphous content and the presence of one or more solvent within the crystalline material) or sequentially using primary and secondary conditioning environments.
Where the systems and methods described herein are adapted to reduce amorphous content, without being bound by a particular theory, it is presently believed that amorphous material present in the crystalline particulate material undergoes an amorphous to crystalline phase transformation preceded by the plasticization or localized dissolution followed by crystallization of the amorphous material. Annealing of particulate material, including micronized material, as described herein works to reduce the amount of amorphous material and preserve the desired particle size distribution of the particulate material by inhibiting fusing, aggregation, and/or agglomeration of the micronized particles as a result of the plasticization or localized dissolution that can occur in unannealed materials. In specific embodiments, the methods described herein provide a reduction in amorphous content relative to unconditioned material of at least 50%. For example, in such embodiments, the methods described herein provide a reduction in amorphous content relative to unconditioned material selected from of at least 75% and at least 90%.
The systems and methods described herein are suited to conditioning a wide variety of particulate crystalline materials that include, for example, amorphous material (e.g., particles formed of amorphous material or crystalline particles that include one or more regions of amorphous material) and/or residual solvent. For example, the systems and methods described herein are suitable for application to materials exhibiting different physical and chemical characteristics (e.g., water soluble materials and materials soluble in organic solvents), and the methods and systems described herein are applicable to materials prepared for and useful in a wide range of products and processes, including, for example, industrial chemicals and processes, food products and additives, cosmetic products, nutritional products and formulations, such as nutritional supplement products, nutraceutical products and formulations, pharmaceutically active agents, and pharmaceutical excipients. In the context of food additives and nutritional products, for example, among many others, the systems and methods described herein may be utilized to improve the physiochemical stability of one or more of the following: aspartame; cyclamate; saccharin; stevia; sucralose; amino acids; vitamins; minerals for nutritional supplements; creatine; and ascorbic acid.
Though not limited to such applications, for convenience of description and exemplification, the disclosure and experimental examples provided herein describe the present systems and methods in the context of micronized crystalline materials for use in pharmaceutical products. Micronization of crystalline active agent and pharmaceutical excipient material is often employed and can be useful in formulation of pharmaceutical compositions for a variety of reasons. For example, for a given active agent or excipient, a crystalline morphology is the most physically and chemically stable morphology, yet it is often beneficial to reduce the particle size distribution of crystalline materials to facilitate delivery (e.g., micronization to allow respiratory or pulmonary delivery or to provide improved formulation characteristics, delivery performance, dissolution performance, and/or bioavailability). Where micronized material is utilized, however, preserving the physiochemical stability of micronized particulates is also generally important to maintaining the efficacy and shelf-life of pharmaceutical products incorporating such materials. Though they are described in the context of micronized pharmaceutical materials, the systems and methods according to the present description can be utilized to condition a variety of crystalline materials exhibiting any particle size distribution that allows the material to be entrained, suspended, or aerosolized within a conditioning gas contained within a conditioning zone for a residence time sufficient to anneal the selected material.
Active agents that can be delivered or formulated as a crystalline material can be processed using the systems and methods described herein. Systems and methods according to the present description are adaptable to water soluble active agents as well as to active agents soluble in organic solvents. Examples of active agents that may be processed according to the present methods include, but are not limited to, beta agonists, muscarinic antagonists, corticosteroids, PDE4 inhibitors, anti-infectives, diuretics, beta blockers, statins, anti-inflammatories, including non-steroidal anti-inflammatory actives, analgesics, and active agents exhibiting a combination of one or more of the preceding pharmacological effects (e.g., bi- or multifunctional molecules, such as, for example, a bi-functional muscarinic antagonist and beta agonist).
More specific examples of active agents suitable for processing using the systems and methods described herein include steroids, muscarinic antagonists, ß-agonists, and bi-functional compounds exhibiting, for example, muscarinic antagonist and ß-agonists activity suited for respiratory or pulmonary delivery. Such actives include, for example, short-acting beta agonists, e.g., bitolterol, carbuterol, fenoterol, hexoprenaline, isoprenaline (isoproterenol), levosalbutamol, orciprenaline (metaproterenol), pirbuterol, procaterol, rimiterol, salbutamol (albuterol), terbutaline, tulobuterol, reproterol, ipratropium and epinephrine; long-acting β2 adrenergic receptor agonist, e.g., bambuterol, clenbuterol, formoterol, and salmeterol; ultra-long-acting β2 adrenergic receptor agonists, e.g., carmoterol, milveterol, indacaterol, and saligenin- or indole-containing and adamantyl-derived β2 agonists; corticosteroids, e.g., beclomethasone, budesonide, ciclesonide, flunisolide, fluticasone, methyl-prednisolone, mometasone, prednisone and trimacinolone; anti-inflammatories, e.g., fluticasone propionate, beclomethasone dipropionate, flunisolide, budesonide, tripedane, cortisone, prednisone, prednisilone, dexamethasone, betamethasone, or triamcinolone acetonide; antitussives, e.g., noscapine; bronchodilators, e.g., ephedrine, adrenaline, fenoterol, formoterol, isoprenaline, metaproterenol, salbutamol, albuterol, salmeterol, terbutaline; and muscarinic antagonists, including long-acting muscarinic antagonists, e.g., glycopyrronium, dexipirronium, scopolamine, tropicamide, pirenzepine, dimenhydrinate, tiotropium, darotropium, aclidinium, trospium, ipatropium, atropine, benzatropin, or oxitropium.
Where appropriate, the active agents conditioned using the systems and methods described herein may be provided as salts (e.g., alkali metal or amine salts or as acid addition salts), esters, solvates (hydrates), derivatives, or a free base. Additionally, the active agents may be in any isomeric form or mixture of isomeric forms, for example, as pure enantiomers, a mixture of enantiomers, as racemates or as mixtures thereof. In this regard, the form of the active agent may be selected to optimize the activity and/or stability.
The systems and methods described herein are also applicable to excipients, adjuvants, carriers, etc. used in pharmaceutical formulations. Such materials can be processed according to the methods described herein either individually or in mixtures suitable for formulation. Though not limited to these specific examples, the systems and methods described herein can be utilized to improve the physiochemical stability of sucrose, a-lactose monohydrate, mannitol, citric acid, glucose, maltose, arabinose, xylose, ribose, fructose, mannose, galactose, sorbose, trehalose, sorbitol, xylitiol, maltodextrin, and isomaltol.
Where a micronized crystalline material is conditioned using the methods or systems described herein, the material can be prepared to exhibit a wide range of desired particle size distributions using any suitable micronization technique. In the context of the present description, the term “micronized” refers to materials exhibiting a median size as large as, for example, 500 microns, and “micronization” processes refer to any suitable process by which a micronized crystalline material is produced. The desired particle size or size distribution of crystalline material conditioned according to the present description will depend on, among other factors, the nature of the material and its desired use or application of the material. Techniques suitable for preparing and providing micronized crystalline material include, for example, milling or grinding processes, including wet-milling and jet milling processes, precipitation from supercritical or near-supercritical solvents, high pressure homogenization, spray drying, spray freeze drying, or lyophilization. Examples of patent references teaching suitable methods for obtaining micronized crystalline particles include, for example, in U.S. Pat. No. 6,063,138, U.S. Pat. No. 5,858,410, U.S. Pat. No. 5,851,453, U.S. Pat. No. 5,833,891, U.S. Pat. No. 5,707,634, and International Patent Publication No. WO 2007/009164, the contents of each of which are incorporated herein by reference.
Though the median size of a micronized material may be as large as 500 μm, often where a micronized material is needed, the particle size distribution of the material will be significantly smaller. For example, in many contexts requiring micronized material, the material will exhibit a median particle size of 100 μm or less. In the context of pharmaceutically active agents or materials prepared for use in pharmaceutical formulations, the median particle size of the micronized material may be below 50 μm or even 10 μm. Where the micronized material conditioned according to the methods described herein is an excipient or active agent to be used in a pharmaceutical product for pulmonary delivery, the micronized material is prepared to exhibit a particle size distribution that facilitates pulmonary delivery. In such embodiments, for example, the micronized material may exhibit a particle size distribution wherein at least 90% of the active agent particles by volume exhibit an optical diameter of about 10 μm or less. In other such embodiments, the micronized material may exhibit a particle size distribution wherein at least 90% of the active agent particles by volume exhibit an optical diameter selected from a range of about 10 μm to about 1 μm, about 9 μm to about 1 μm, about 8 μm to about 1 μm, about 7 μm to about 1 μm, about 5 μm to about 2 μm, and about 3 μm to about 2 μm. In still further embodiments where the micronized material is prepared for use in a pharmaceutical product for pulmonary delivery, the micronized material may exhibit a particle size distribution wherein at least 90% of the active agent particles by volume exhibit an optical diameter selected from 10 μm or less, 9 μm or less, 8 μm or less, 7 μm or less, 6 μm or less, 5 μm or less, 4 μm or less, 3 μm or less, 2 μm or less, or 1 μm or less.
It will be readily understood that the embodiments, as generally described herein, are exemplary. The more detailed description of the systems and methods provided herein is not intended to limit the scope of the present disclosure, but is merely representative of various embodiments.
Unless specifically defined otherwise, the terms used herein have their normal meaning as understood in the art. The following terms are specifically defined for the sake of clarity.
The term “active agent” as used herein includes any agent, drug, compound, composition or other substance that may be used on, or administered to a human or animal for any purpose, including any agent, drug, compound, composition or other substance that provides a nutritional, therapeutic, pharmaceutical, pharmacological, diagnostic, cosmetic, prophylactic agents and/or immunomodulating effect. The term “active agent” may be used interchangeably with the terms, “drug,” “pharmaceutical,” “medicament,” “drug substance,” “active pharmaceutical ingredient,” “pharmaceutically active agent,” or “therapeutic.” As used herein the “active agent” may also encompass natural or homeopathic products that are not generally considered therapeutic.
The term “annealing” refers to a physiochemical change or phase transformation in a material that results in improved physiochemical stability. In certain embodiments, the term “annealing” refers to a process whereby amorphous content within a crystalline particulate material is reduced or eliminated. In other embodiments, the term “annealing” refers to a process whereby residual solvent contained within a crystalline particulate material is reduced or eliminated by, for example, solvent vaporization and/or exchange. In still further embodiments, the methods and systems described herein may anneal a crystalline particulate material by both reducing amorphous content and reducing the presence of a residual solvent.
The term “conditioning,” as used herein, generally refers to methods and processes that may be used to improve the physiochemical stability of a particulate crystalline material. In specific embodiments, the term “conditioning” refers to methods that cause a controlled annealing of the particulate material.
The term “phase transformation” refers to a change in the bulk of the crystals present in a particulate crystalline material. In particular embodiments, annealing of a material using the conditioning systems or methods described herein results in a phase transformation selected from, for example, removal of a solvent of crystallization, replacement of a solvent of crystallization, an amorphous to crystalline phase change, or a change in physical structure beyond just an amorphous to crystalline phase change.
As used herein, “physiochemical” refers to one or both of the physical and chemical stability of a material.
As used herein, the term “inhibit” refers to a reduction, prevention, or slowing of any given process, event, or characteristic.
When used to refer to the conditioned particulate material described herein, the terms “physical stability” and “physically stable” refer to a composition that is resistant to one or more of particle fusing, aggregation, agglomeration, and particle size changes. In certain embodiments, physical stability may be evaluated through exposing the particulate material to accelerated degradation conditions, such as increased temperature and/or humidity as described herein.
When referred to herein, the term “optical diameter” indicates the size of a particle as measured using a laser diffraction particle size analyzer equipped with a dry powder dispenser (e.g., Sympatec GmbH, Clausthal-Zellerfeld, Germany).
The nature of and extent to which annealing of the particulate material takes place can be controlled by the residence time of the material within the conditioning zone and by the properties of the conditioning gas, including, for example the presence and concentration of one or more solvents, and the temperature, flow rate, and direction or turbulence of flow of the conditioning gas. In some embodiments of the systems disclosed herein, the residence time of the micronized active agent particles in the conditioning zone 140 may be controlled by the geometry of the conditioning zone 140 or by the flow rate of the conditioning gas through the conditioning zone 140.
The material to be conditioned may be provided to the delivery zone 110 in a form that is appropriate for the chosen material and the conditioning process. Where a particulate material exhibiting a desired particle size distribution is desired, the material may be prepared to exhibit the targeted particle size distribution prior to introduction into the delivery zone 110. In such an embodiment, the particulate material can be fed from the delivery zone 110 into the mixing zone 130 using any suitable device or system for controlled feeding of a powder or particulate material at a desired feed rate. Controlled feeding of the particulate material will typically include entraining the particulate material in a dispersion component, such as, for example a delivery gas suitable for dispersion and delivery of the particulate material into the mixing zone 130 and/or the conditioning zone 140.
In certain embodiments, particulate material may be subjected to a micronization process within the delivery zone 110. In such embodiments, the delivery zone 110 may include a device or system that processes the crystalline material to provide a micronized particulate material that exhibits a desired particle size distribution. Where the delivery zone 110 includes a device or system suitable for carrying out micronization of the selected crystalline material, the delivery zone 110 may incorporate any one of a number of known devices or systems for micronization. For example, the crystalline material may be micronized in the delivery zone 110 using known milling or grinding processes, known crystallization or recrystallization processes, or known micronization processes utilizing precipitation from supercritical or near-supercritical solvents, spray drying, spray freeze drying, or lyophilization.
In embodiments where the delivery zone 110 includes a micronizer, the mixing zone 130 and/or conditioning zone 140 may be operably linked to the micronizer. In such embodiments, the crystalline material may be processed to exhibit the targeted particle size distribution within the delivery zone 110 and, prior to collection, immediately delivered to the mixing zone 130 while the particles remain airborne as they exit from the micronizer. Therefore, the systems and methods described herein allow for conditioning of micronized material as a sequential but integrated step in a process of producing and collecting a micronized crystalline material. Such “in-line” or “in-process” conditioning of micronized crystalline material provides the benefits associated with the annealing achieved by the conditioning process, while also eliminating the need to conduct a first process for producing micronized (or size comminuted) material followed by a second, separate conditioning process for annealing the micronized material.
The mixing zone 130 illustrated in
The conditioning zone 140 may be formed within a conditioning chamber, which can be provided by any structure, such as a column, tank, tube, funnel, coil, or the like, suitable for maintaining a controlled atmosphere and receiving the particulate material and conditioning gas. The characteristics of the controlled atmosphere within the conditioning zone 140 can be adjusted to achieve a desired conditioning of one or more selected particulate materials. In particular embodiments, the conditioning gas is delivered at a specified rate and mixes with the delivery gas at a selected ratio. For example, the conditioning gas may be supplied to the conditioning zone 140 (e.g., through a dispersion head assembly) at a targeted gas flow rate. The gas flow rate will depend on, among other factors, the amount of micronized material being processed and the angle at which the gas is introduced into the conditioning zone 140. In certain embodiments, the conditioning gas is introduced into the conditioning zone 140 at a rate ranging from about 20 SCFM up to about 500 SCFM, and the delivery gas having the particulate material to be conditioned entrained therein may be supplied at a gas flow rate ranging from about 20 SCFM up to about 75 SCFM. However, depending on the angle at which the conditioning and delivery gases are introduced into the conditioning zone 140 and the nature of the material being processed, the gas flow rate of both the conditioning gas and the delivery gas may be increased as high as 3,300 SCFM. In other embodiments, the conditioning gas may be supplied at a flow rate of 30 SCFM up to about 100 SCFM and the delivery gas containing the micronized material to be conditioned may be supplied at a gas flow rate ranging from about 30 SCFM up to about 60 SCFM. In addition to, or as an alternative to, controlling the rate at which the conditioning gas is introduced into the controlled atmosphere, the ratio of the conditioning gas to the delivery gas may be selected to facilitate conditioning of the micronized material. In particular embodiments, the conditioning gas is mixed with the delivery gas at a ratio selected from 1:1, 1.2:1, 1.4:1, 1.6:1, 1.8:1, 2.0:1, 2.2:1, 2.4:1, 2.6:1, 2.8:1, 3:1, 3.2:1, 3.4:1, 3.6:1, 3.8:1, and 4:1.
The temperature of the conditioning gas may also be controlled. Annealing of particulate material can be significantly affected by temperature. In certain embodiments, the temperature of the conditioning gas is selected from between about 10° C. and 100° C. In specific examples of such embodiments, the temperature of the conditioning gas may be selected from one of the following ranges, between about 10° C. and 70° C., between about 20° C. and 50° C., between about 10° C. and 50° C., and between about 20° C. and 30° C., depending on the nature of the particulate material being processed.
The conditioning gas may also include one or more solvent vapors. In such embodiments, the conditioning gas includes a carrier gas having one or more solvent vapors dispersed therein. The inclusion of a solvent vapor within the conditioning gas can be particularly useful in conditioning processes adapted to reduce or eliminate amorphous content and to conditioning process adapted to reduce or eliminate the presence of residual solvent(s) by solvent exchange.
Where a solvent is included in the conditioning gas, the solvent will typically be selected according to the material to be conditioned. For example, in embodiments where the material to be conditioned is water soluble, the conditioning gas may include water vapor carried within an inert gas. In certain embodiments, the solvent vapor may be a combination of water and water miscible organic solvents (e.g., alcohols, ketones, esters, etc.) Alternatively, in embodiments where the material to be conditioned is not water soluble, but exhibits solubility in one or more organic solvents, the solvent vapor included in the conditioning gas may simply include an organic solvent vapor, such as an alcohol (e.g., ethanol, methanol, isopropyl alcohol, etc.), ketone (e.g., acetone, methyl ketone, ethyl ketone, etc.), ester (e.g., ethyl acetate, etc.), aliphatic alcohol (e.g., octanol, etc.), or alkane (e.g., octane, nonane, etc.) vapor, carried within an inert gas. As used herein, “inert” refers to a carrier gas that is non-reactive with the micronized material being conditioned and preferably the solvent vapor. Examples of inert gases include, without limitation, compressed dry air, nitrogen, inert gas (e.g., argon, helium, etc.), carbon dioxide, and the carrier gas included in the conditioning gas can be selected according to the solvent vapor or combination of solvent vapors to be used in the conditioning gas or conditioning zone. In embodiments where the conditioning of the particulate material includes solvent exchange, the solvent(s) included in the conditioning gas may be selected to provide improved safety and/or physiochemical stability of the particulate material.
Where a solvent is included in the conditioning gas, the conditioning gas can be prepared and maintained at a specified temperature or temperature range in order to maintain the solvent as a vapor. As already mentioned, controlling the temperature of the conditioning gas can also serve to facilitate the conditioning process, with the temperature being selected to facilitate a desired level of annealing over a selected residence time.
The relative concentration of solvent vapor included in a conditioning gas can also be adjusted to accomplish a desired level of conditioning for different material characteristics. For example, the concentration of solvent vapor within the conditioning gas may be adjusted based on the chemical or physical properties of the crystalline material to be processed. In specific embodiments, the relative humidity (RH) or relative saturation (RS) and temperature conditions of the conditioning gas are selected to provide RH or RS and temperature conditions that exceed the glass transition temperature (Tg) of the amorphous content of the material being processed. For example, for each of the solvents included within the conditioning gas, the vapor pressure of the solvent may be maintained at a vapor pressure of about 0.05 to 0.95 of the saturation vapor pressure for the solvent.
Crystallization of an amorphous phase typically occurs rapidly when the amorphous material is exposed to conditions that exceed its glass transition temperature, usually twenty degrees Celsius above the glass transition temperature (Lechuga-Ballesteros, D.; Miller, D. P.; Zhang, J., Residual water in amorphous solids, measurement and effects on stability. In Progress in Amorphous Food and Pharmaceutical Systems, Levine, H., Ed. The Royal Society of Chemistry: London, 2002; pp 275-316). Exposure of amorphous material to temperature in excess of the glass transition can be achieved in the absence of any solvent by exposing the amorphous material to a stream of hot air above its glass transition temperature. However, the glass transition temperature is also a function of the fraction of solvent present in the amorphous material, an effect known as plasticization. Plasticization is typically represented by a plasticization curve, such as the one shown in
In addition, the solvent content held in an amorphous material is a function of the vapor concentration of the solvent surrounding the amorphous solid. This can be illustrated by the sorption isotherm provided in
The glass transition plasticization curve and the sorption isotherm can be combined to construct a stability diagram as the one shown in
The nature and extent of annealing that takes place within the conditioning zone can also be adjusted by altering the residence time of the particulate material within the conditioning zone 140. The residence time is the average time particulate material spends within the conditioning zone 140. The residence time of the particulate material within the conditioning zone 140 can be adjusted by changes to one or more of a variety of process variables. For example, the volume and dimensions of the conditioning chamber can be altered, to provide longer or shorter residence times, with, for example, relatively higher volume or larger physical dimensions generally resulting in relatively longer residence times. The flow rates and temperatures of one or both of the conditioning gas and the delivery gas can also be adjusted to affect residence time. In addition, the manner by which the conditioning gas or delivery gas is introduced into the conditioning chamber can affect particle residence time. As an example, introduction of the conditioning gas and/or delivery gas in a manner that creates a generally linear flow through the conditioning chamber may create a relatively shorter residence time compared to introduction of the same gas(es) in a manner that creates a more turbulent recirculating dispersion of the gas(es).
In general, the residence time of the particulate material within the conditioning chamber can be selected from about 0.5 seconds to several minutes. In particular embodiments, the residence time may be up to about 10 minutes or 600 seconds. In particular embodiments, the residence time may be selected from about 0.5 to about 10 seconds, 0.5 to about 20 seconds, 0.5 to about 30 seconds, 0.5 to about 40 seconds, and 0.5 to about 50 seconds. In certain such embodiments, the particulate material may be conditioned by the conditioning gas for a residence time selected from about 0.5 seconds, 1 second, 1.5 seconds, 2 seconds, 2.5 seconds, 3 seconds, 3.5 seconds, 4 seconds, 5 seconds, 6 seconds, 7 seconds, 8 seconds, 9 seconds, and 10 seconds.
After the particulate material has been annealed in the conditioning zone 140, the conditioned material is separated from the conditioning gas and collected in the separation and collection zone 150. The micronized material may be separated and collected from the conditioning gas using known particle collection techniques and equipment. In certain embodiments of the systems disclosed herein, the micronized material may continue to anneal while in the separation and collection zone 150. The collection zone 150 can be formed by or include a cyclone collector. Cyclone collectors for collection of particulate materials, including micronized materials, and separation of such materials from a conditioning gas. Cyclone collectors are commercially available and suitable for use as the collection zone 150 of the systems described herein.
In addition to a collection device, such as a cyclone collector, the collection zone 150 may be configured to facilitate direct collection of the processed material. Where a collection zone 150 is configured to allow direct collection of the conditioned material, the collector included in the collection zone may simply deliver the conditioned product to a container from which the conditioned material can be collected or removed. Such a container may include a collection bag that can be removed from the collection device, as is often used in conjunction with a cyclone collector. The collection bag may be sealable and formed using a material that enables efficient collection of the conditioned material, while also being permeable to a gas used in the collection system. In another embodiment, the collector included in the collection zone 150 may be configured as a holding chamber. In such an embodiment, the collector, such as a cyclone collector, may be used to separate the conditioned material from a conditioning gas and collect the conditioned material into a holding chamber where the conditioned material can be maintained in a fluidized state for a desired period of time. Annealing of the crystalline material processed according to the present description is not always complete as the material exits the conditioning zone 140, and may continue as the material is collected. Depending on the material being processed and the annealing conditions, it may be beneficial to maintain the conditioned material in a fluidized state within a collection chamber for a period of time sufficient to allow additional progress of the annealing process.
In still other embodiments, the collection zone 150 may be configured to allow further processing of the conditioned material. In such embodiments, the collection zone 150 may be operably linked to one or more additional systems, including an additional conditioning system as described herein, for further processing of the conditioned material. In such embodiments, the collector included in the collection zone 150 may be configured to deliver the conditioned material directly for continued processing or the collection zone 150 may be configured to include or be in operable communication with a holding chamber as described and illustrated herein, such as, for example, in association with the systems illustrated in
In some embodiments, the systems and methods described herein may be utilized to simultaneously process and condition more than one particulate material. For example, two or more micronized materials may be simultaneously introduced into a conditioning zone. The materials may be combined prior to introduction into the conditioning zone or they may be introduced independently into the conditioning zone. In some embodiments, the materials may be combined prior to micronization and introduced into the conditioning zone as a particulate material including a combination of two or more chemical entities. Even further, where two or more different particulate materials are introduced into the conditioning zone (whether as a combined product stream or as two or more independently introduced materials), the materials may exhibit similar solubility characteristics (e.g., each of the different materials exhibit solubility in water or each of the materials exhibit solubility in a given organic solvent). However, the methods described herein are also suited to simultaneously conditioning two or more materials in the same conditioning zone where at least two of the two or more different materials exhibit different solubility characteristics (e.g., at least one is water soluble, while another is soluble only in an organic solvent, or one is soluble in a first organic solvent, while a second is soluble in a second organic solvent).
Certain embodiments of a system for the in-process conditioning of a micronized material according to the present description can be represented by the system illustrated in
The micronized crystalline material is supplied to the mixing zone 230 as a micronized material with a desired particle size distribution. In certain embodiments, for example, at least 90% of the micronized particles by volume exhibit an optical diameter of about 10 μm or less. In other embodiments, at least 90% of the micronized crystalline particles by volume exhibit an optical diameter selected from a range of about 10 μm to about 1 μm, about 9 μm to about 1 μm, about 8 μm to about 1 μm, about 7 μm to about 1 μm, about 5 μm to about 2 μm, and about 3 μm to about 2 μm. In further embodiments, at least 90% of the micronized crystalline particles by volume exhibit an optical diameter selected from 10 μm or less, 9 μm or less, 8 μm or less, 7 μm or less, 6 μm or less, 5 μm or less, 4 μm or less, 3 μm or less, 2 μm or less, or 1 μm or less.
The micronizing zone 210 may be separated from an external environment or contained within a safety barrier or enclosure (not shown). Such a design can be particularly advantageous where the micronized material is an active agent or is otherwise biologically active. The safety barrier may be used in order to prevent unwanted contact with any micronized material produced in the micronizing zone 210. Where included in the systems described herein, a safety barrier may be constructed of any suitable material such as metal, glass, plastic, composites, etc., that are sufficient to contain micronized particles.
With reference to
The conditioning gas supply zone 220 may further comprise a liquid evaporation chamber 225. The solvent used to produce the solvent vapor disbursed within the carrier gas 222 can be generated within or provided from the evaporation chamber 225, and the evaporation chamber can be configured to provide the carrier gas 222 with a desired concentration of solvent vapor within the conditioning gas 226. Where the micronized crystalline material is water soluble, the solvent can be an aqueous solvent, such as purified or distilled water, and in such embodiments, the evaporation chamber 225 is configured to create a conditioning gas 226 having a desired relative humidity. In other embodiments, particularly where the micronized crystalline material to be conditioned is not water soluble, the solvent for use with the systems disclosed herein may be a non-aqueous liquid, such as an organic solvent described herein.
A liquid atomizer 223 may be used to deliver liquid solvent to the carrier gas 222 in the form of atomized liquid droplets 224 suspended within the carrier gas 222. Atomization of the liquid solvent facilitates conversion of the liquid solvent into a solvent vapor within the evaporation chamber 225. In more specific embodiments, a liquid atomizer used in the systems described herein provides control over the size of the atomized droplets delivered to the carrier gas 222 as well as the rate and volume of liquid solvent atomized. Where used, a liquid atomizer 223 can be selected from, for example, pressure nozzles, pneumatic atomizers, impinging jet atomizers. In one such embodiment, the carrier gas 222 is heated in the heating chamber 221, a liquid atomizer 223 delivers liquid solvent to the carrier gas within the conditioning gas supply zone 220, and the carrier gas 222 and atomized liquid solvent 224 are supplied to the liquid evaporation chamber 225. As the carrier gas 222 and atomized liquid solvent 224 pass through the liquid evaporation chamber, the liquid solvent vaporizes and the carrier gas becomes a conditioning gas 226 having a desired solvent vapor concentration.
In certain embodiments, where the solvent vapor is formed from an aqueous solvent, the conditioning gas 226 may be supplied at a temperature ranging from about 20° C. to about 100° C., and with a relative humidity ranging from about 0.05% to about 75%. In more specific embodiments where the solvent used to form the solvent vapor is an aqueous solvent, the conditioning gas 226 may be supplied having a temperature selected from at least about 20° C., 21° C., 22° C., 23° C., 24° C., 25° C., 26° C., 27° C., 28° C., 29° C., and 30° C. and having a relative humidity selected from at least about 50%, 51%, 52%, 53%, 54%, 55%, 56%, 57%, 58%, 59%, 60%, 61%, 62%, 63%, 64%, 65%, 66%, 67%, 68%, 69%, 70%, 71%, 72%, 73%, 74% and 75%. In particular embodiments, however, the temperature may be as high as 22° C. and the relative humidity as low as 0.05%.
With continued reference to
Where a mixing head is included in a system according to the present description, as shown in
In certain embodiments, the dispersion head assembly and/or mixing head may be configured to mix the conditioning gas and the micronized crystalline material upon entry into the conditioning zone 240. Alternatively, the dispersion head assembly and/or mixing head may be configured to mix the conditioning gas and micronized crystalline material before the mixture leaves the mixing zone 230 and is delivered to the conditioning zone 240. For example,
The systems disclosed herein can include a mixing zone 230 configured to mix the conditioning gas 226 with the delivery gas 216 in a desired ratio, such as a ratio of gas volumes (volume/volume) or a mass flow rate ratio (SCFM/SCFM). For example, in particular embodiments, the mixing zone, including, for example, a dispersion head assembly, may be configured to mix the conditioning gas 226 and delivery gas 216 in a ratio of about 1 to 4 parts conditioning gas 226 with about 1 part of the delivery gas 216. In certain such embodiments, the conditioning gas 226 may be mixed with the delivery gas 216 in a ratio selected from any of about 1:1, 1.2:1, 1.4:1, 1.6:1, 1.8:1, 2.0:1, 2.2:1, 2.4:1, 2.6:1, 2.8:1, 3:1, 3.2:1, 3.4:1, 3.6:1, 3.8:1, and 4:1.
With continued reference to
In certain embodiments, after the conditioning gas 226 and the delivery gas 216, comprising micronized active agent particles, are mixed together in the mixing zone 230, the micronized particles 235 enter the conditioning chamber 240 together with the conditioning gas 226. While in the conditioning chamber 240, the micronized particles 235 are exposed for a desired time period to the conditioning gas 226, and during their residence time within the conditioning chamber 240, the amorphous material included in the micronized particles 235 anneals. The residence time of the micronized particles 235 in the conditioning chamber 240 may be controlled by one or more of the following: the dimension and geometry of the conditioning chamber 240; the rate at which the mixture of the conditioning gas 226 and the delivery gas 216 are delivered into the conditioning chamber 240; the flow pattern of the mixture of the conditioning gas 226 and the delivery gas 216 within the conditioning chamber 240; the amount of micronized material carried by the mixture of delivery gas 216 and conditioning gas 226; and the system used for collection of the conditioned micronized material. In particular embodiments, the residence time of the micronized active agent particles 235 within the conditioning chamber 240 may be for a period of time ranging from about 0.5 to 10 seconds. In certain such embodiments, the residence time of the micronized particles 235 within the conditioning chamber 240 may be selected from one the residence times detailed herein.
A conditioning chamber 240 suitable for use in the systems described may be configured as for example, a tank, a column, a funnel, a tube, or other appropriate devices or structures. In further embodiments, the conditioning chamber 240 may further include heaters, inlets, outlets, and other means and devices for controlling the conditions and gas flow within the conditioning chamber 240. The geometry of the conditioning chamber 240 may be modified by adjusting, for example, the length, width, height, volume, and shape of the conditioning chamber 240.
Conditioned micronized active agent particles 246 are separated from the conditioning gas 226 in a separating zone 250. The separating zone 250 may comprise elements or devices designed to separate conditioned micronized active agent particles 246 from the carrier gas 216 and conditioning gas 226, such as, for example, a cyclone separator, bag collector or other separation equipment, as known by those of skill in the art. In particular embodiments, the separating zone 250 may comprise an exhaust outlet 255 whereby, for example, the exhaust gas and other materials may exit from the separating zone 250. Though micronized material will have been conditioned within the conditioning zone 240, in certain embodiments, the process of annealing is does not end immediately upon collection of the micronized material from the conditioning zone 240. For example, in certain embodiments, although the controlled atmosphere of the conditioning zone 240 initiates or even substantially completes the annealing process, annealing of amorphous material continues as the micronized material exits the conditioning zone 240 and is separated and collected. In addition to a system or device of separating the conditioned micronized material from the delivery and conditioning gases, the separating zone 250 may further included one or more filters and collectors. Filters may be placed, for example, at the exhaust outlet 255 to capture or prevent unwanted escape of fines. Additionally, a collector 260 is included within the separating zone 250 to facilitate capture and containment of the conditioned material. Once collected the, conditioned crystalline material can be stored or further processed, as desired.
Though
As shown in
Once delivered to the product holding chamber 660, the conditioned product may be maintained in a fluidized state and the cut-off valve 670 closed. At that point, the system can re-equilibrate to supply a secondary conditioning gas. In such an embodiment, the upstream components of the conditioning system 600 (e.g., the delivery zone 610, conditioning gas supply zone 620, mixing zone 630, conditioning zone 640, and collection zone 650) may be purged of the primary conditioning gas used to condition the material present in the product holding chamber 660, and a secondary conditioning gas can be supplied from and/or generated in the gas supply zone 620. Once the system is re-equilibrated with the secondary conditioning gas, the cut-off valve 670 may be opened to expose the conditioned product contained within the product holding chamber 660 to the secondary conditioning gas. The product can be maintained in a continuously fluidized state within the product holding chamber 660 as it is exposed to the secondary conditioning gas for a period of time sufficient to accomplish a secondary annealing. The nature and content of the secondary conditioning gas, including the presence and concentration of one or more solvents, and the temperature, flow rate, and direction or turbulence of flow of the secondary conditioning gas may be adjusted to accomplish a desired secondary annealing for a wide range of selected materials using process conditions described herein. By adjusting the characteristics of the secondary conditioning gas and the residence time of the particulate material within the product holding chamber 660, the system illustrated in
The residence time of the conditioned product within the holding chamber 660 can be easily adjusted based on the material itself, the conditioning gas(es), and the nature or extent of annealing desired. For example, as is true of particles conditioned within a conditioning zone, the residence time of a conditioned product within a holding chamber 660 may be a matter of seconds or minutes. For example the residence time of the conditioned material within the holding chamber 660 may be selected from those residence times detailed above in relation to the conditioning zone. However, the conditioned product can also be maintained within the holding chamber 660 indefinitely. In certain embodiments, the conditioned product is maintained within a holding chamber 660 for a time selected from up to 5 minutes, up to 10 minutes, up to 30 minutes, up to 1 hour, up to 1.5 hours, up to 2 hours, up to 5 hours, up to 10 hours, up to 12 hours, up to 18 hours, and up to 24 hours. Such flexibility enables the conditioned product to be exposed to a secondary conditioning gas for any amount of time needed to accomplish secondary conditioning. A relatively longer residence time affords exposure to a secondary conditioning gas over a long period of time and may be particularly useful for a secondary conditioning process that requires more time than might be practically achieved within a given system's conditioning zone.
As shown in
As material is processed in the primary conditioning system 701 a primary annealing of the material takes place and the primary annealed material is collected in the primary collection zone 750 and delivered to the primary holding chamber 760. While the product is processed in the primary conditioning system 701 and collected in the primary holding chamber 760, the cut-off valve 770 will typically remain closed. Once the first conditioning process is complete and the primary annealed material is collected in the primary holding chamber 760, the cut-off valve 770 may be opened and the primary annealed material delivered into the secondary mixing zone 830. The primary annealed material may be dispersed within a delivery gas as it is delivered to or within the secondary mixing zone 830. The delivery gas can be any suitable delivery gas as described herein, and by dispersing the primary annealed product in a delivery gas, the primary annealed product is suspended or entrained within the delivery gas. A secondary conditioning gas is delivered and/or generated within the secondary conditioning gas supply zone 820, and the secondary conditioning gas is mixed with the primary annealed product (and any delivery gas used to disperse the primary annealed product) in the secondary mixing zone 830.
The primary annealed product remains entrained, suspended or aerosolized in the secondary conditioning gas within the secondary conditioning zone 840. The primary annealed product is maintained within the secondary conditioning zone 840 for a period of time sufficient to accomplish a secondary annealing. As is true of the conditioning gas utilized in each embodiment of the systems described herein, the nature and content of the secondary conditioning gas, including the presence and concentration of one or more solvents, and the temperature, flow rate, and direction or turbulence of flow of the secondary conditioning gas may be adjusted to accomplish a desired secondary annealing for a wide range of selected materials using process conditions described herein. By adjusting the characteristics of the secondary conditioning gas and the residence time of the particulate material within the secondary conditioning zone 840, the system illustrated in
Though described in relation to embodiments illustrated in the figures provided herein, conditioning systems according to the present description are not limited to the specific, illustrated embodiments. The systems for conditioning crystalline particulate materials described herein are scalable and adaptable for areas of various size. In particular embodiments, the systems disclosed herein may be scaled-up or scaled-down with regard to, for example, gas flow rates, active agent mass, material output, desired particle residence time, etc., according the desired output rate and the available space and equipment. In certain embodiments, the systems disclosed herein may be assembled as a modular unit and incorporated or built into established processes and systems for the manufacture of conditioned particulate material, and are well-suited for efficient production of conditioned, micronized particulates. For example, the systems as disclosed here may be incorporated into commercial milling and micronization processes or a built into a spray drying system. In further embodiments, the systems described herein may be operated as part of a batch process where one or more micronized materials are conditioned and then collected in separate batches. In alternative embodiments, the systems described herein may be operated as part of a continuous feed process whereby one or more micronized materials are continuously delivered to the system and continuously conditioned and collected.
Methods for conditioning particulate crystalline material are also provided herein. Methods according to the present description can be carried out using the conditioning systems provided herein. In general, the methods described herein include: (1) generating and/or providing a crystalline particulate material; (2) introducing the particulate material in an atmosphere where it is blended with a conditioning gas; (3) maintaining the particulate material in contact with the conditioning gas for a desired residence time; and (4) collecting the conditioned particulate material. In specific embodiments, the particulate material is a micronized crystalline material. Examples of materials that may be conditioned using the methods described herein include those materials already described. In particular embodiments of methods according to the present description, the material to be conditioned is typically entrained or aerosolized within a delivery gas that is blended with the conditioning gas, and the particulate material remains entrained, suspended or aerosolized in the conditioning gas as it travels through the conditioning zone. The nature of the conditioning gas and the residence time of the particulate material within the conditioning zone are controlled to accomplish annealing of the material.
In specific embodiments, the methods include a continuous process for micronizing, conditioning, and collecting a crystalline material. In such embodiments, generating the crystalline material includes subjecting the material to a micronization process and conditioning of the micronized material may be conducted in-line with particle collection. Where, the methods described herein provide in-line or in-process conditioning of micronized material (or, more generally, any size comminuted material), the particulate material may be blended with a conditioning gas and retained within a conditioning zone to anneal the particulate prior to particle collection.
In other embodiments, methods according to the present description include primary and secondary conditioning steps. In such embodiments, the crystalline particulate material can be introduced into (e.g., entrained, suspended, or aerosolized within) a first conditioning gas to carry out a primary annealing and subsequently introduced into (e.g., entrained, suspended, or aerosolized within) a second conditioning gas to carry out a secondary annealing. Alternatively, for certain materials, a conditioning gas may be selected that provides substantially simultaneous primary and secondary annealing of the particulate material. For example, in methods where primary and secondary annealing are carried out using a single conditioning gas, the conditioning gas may anneal the particulate material through both reduction of amorphous content and removal of an undesired residual solvent by vaporization or solvent replacement.
The methods provided can be tailored to specific materials to be processed. For example, glycopyrronium is an active agent that can be conditioning using the systems and methods described herein. Micronization of crystalline glycopyrronium can lead to a micronized material that includes significant amorphous content, and in particular embodiments, the present methods can be adapted to reduce or eliminate amorphous material from crystalline glycopyrronium particulates. Glycopyrronium conditioned according to the present description may be in any crystalline form, isomeric form or mixture of isomeric forms. In this regard, the form of glycopyrronium may be selected to optimize the activity and/or stability of glycopyrronium. Where appropriate, glycopyrronium may be provided as a salt (e.g. alkali metal or amine salts, or as acid addition salts), esters or solvate (hydrates). Suitable counter ions include, for example, fluoride, chloride, bromide, iodide, nitrate, sulfate, phosphate, formate, acetate, trifluoroacetate, propionate, butyrate, lactate, citrate, tartrate, malate, maleate, succinate, benzoate, p-chlorobenzoate, diphenyl-acetate or triphenylacetate, o-hydroxybenzoate, p-hydroxybenzoate, 1-hydroxynaphthalene-2-carboxylate, 3-hydroxynaphthalene-2-carboxylate, methanesulfonate and benzenesulfonate. In particular embodiments of the methods described herein, the bromide salt of glycopyrronium is used, namely (3-[(cyclopentylhydroxyphenylacetyl)oxy]-1, 1-dimethyl-, bromide). The bromide salt of glycopyrronium is commonly referred to as glycopyrrolate. Glycopyrrolate is commercially available and can be prepared according to the procedures set out in U.S. Pat. No. 2,956,062, the contents of which are incorporated herein by reference.
Where crystalline glycopyrronium, such as crystalline glycopyrrolate, is the material processed by the methods described herein, the glycopyrronium material can be micronized to exhibit particle size characteristics as described herein, such as, for example, a particle size distribution suitable for pulmonary delivery. Moreover, the micronized glycopyrronium can be prepared and provided using any suitable micronization technique and delivered into the conditioning chamber via a delivery gas suitable to the chosen micronization technique. In one such embodiment, the glycopyrronium is micronized via a jet mill and the delivery gas may be typical gas flow exiting the jet mill, which would include aerosolized, micronized particles of glycopyrronium.
In specific embodiments, the bromide salt of glycopyrronium (glycopyrrolate) may be processed according to the present methods. Where glycopyrrolate is the material being conditioned, a conditioning gas may be mixed with a delivery gas (e.g., a jet mill gas flow) in a ratio of about 1 to 4 parts conditioning gas flow with about 1 part of the delivery gas. In certain such embodiments, the conditioning gas flow may be mixed with the jet mill gas flow in a ratio selected from about 1:1, 1.2:1, 1.4:1, 1.6:1, 1.8:1, 2.0:1, 2.2:1, 2.4:1, 2.6:1, 2.8:1, 3:1, 3.2:1, 3.4:1, 3.6:1, 3.8:1, and 4:1. In specific embodiments, the conditioning gas may be supplied at a gas flow rate ranging from about 150 SCFM up to about 500 SCFM, and the delivery gas may be supplied at a gas flow rate of ranging from about 20 SCFM up to about 75 SCFM. However, in some embodiments, depending on the desired conditions for the conditioning zone and the nature of the material being processed, the gas flow rate of both the conditioning gas and the delivery gas may be increased as high as 3,300 SCFM.
When conditioning glycopyrrolate, the conditioning gas may be delivered at a temperature ranging from about 20° C. to about 30° C. and include water vapor as a solvent. In particular embodiments of methods for conditioning glycopyrrolate, the temperature of the conditioning gas may be selected from at least 20° C., 21° C., 22° C., 23° C., 24° C., 25° C., 26° C., 27° C., 28° C., 29° C., and 30° C. Moreover, where included in the conditioning gas for annealing glycopyrrolate according to the methods described herein, water vapor may be provided at a concentration that results in a relative humidity ranging from about 50% to about 80%. In particular embodiments of methods for conditioning glycopyrrolate, the conditioning gas may be supplied at a temperature described herein with a relative humidity selected from at least about 50%, 51%, 52%, 53%, 54%, 55%, 56%, 57%, 58%, 59%, 60%, 61%, 62%, 63%, 64%, 65%, 66%, 67%, 68%, 69%, 70%, 71%, 72%, 73%, 74% and 75%. At the temperatures and relative humidity described herein, the residence time of the micronized glycopyrrolate material within the conditioning chamber may be from about 0.5 to about 10 seconds. In certain such embodiments, the micronized glycopyrrolate material is present within the conditioning chamber for a residence time selected from about 0.5 seconds, about 1 second, about 1.5 seconds, about 2 seconds, about 2.5 seconds, about 3 seconds, about 3.5 seconds, about 4 seconds, about 5 seconds, about 6 seconds, about 7 seconds, about 8 seconds, about 9 seconds, and about 10 seconds. However, the residence time can be adjusted as needed to achieve the desired reduction of amorphous content.
In other embodiments, the methods provided can be tailored to for the annealing of materials soluble in organic solvents. For example, the methods described herein can be tailored to the conditioning of corticosteroid active agents soluble in organic solvents. In certain such embodiments, the methods described herein can be tailored for the conditioning of a corticosteroid selected from fluticasone and budesonide. Fluticasone, pharmaceutically acceptable salts of fluticasone, such as fluticasone propionate, and preparation of such materials are known, and described, for example, in U.S. Pat. Nos. 4,335,121, 4,187,301, and U.S. Patent Publication No. US2008/125407, the contents of which are incorporated herein by reference. Budesonide is also well known and described, for example, in U.S. Pat. No. 3,929,768, the contents of which are incorporated herein by reference.
Micronization of crystalline corticosteroids, such as budesonide and fluticasone, can lead to a micronized material that includes significant amorphous content, and in particular embodiments, the present methods can be adapted to reduce or eliminate amorphous material from particulate crystalline corticosteroid material. A corticosteroid conditioned according to the present description may be in any crystalline form, isomeric form or mixture of isomeric forms. In this regard, the form of the corticosteroid may be selected to optimize the activity and/or stability of corticosteroid. Where appropriate, the corticosteroid may be provided as a salt (e.g. alkali metal or amine salts, or as acid addition salts), esters or solvate (hydrates).
Where a crystalline corticosteroid material, such as crystalline fluticasone or budesonide, is the material processed by the methods described herein, the corticosteroid material can be micronized to exhibit particle size characteristics as described herein, such as a particle size distribution suitable for pulmonary delivery. Moreover, the micronized corticosteroid can be prepared and provided using any suitable micronization technique and delivered into the conditioning chamber via a delivery gas suitable to the chosen micronization technique. In one such embodiment, the selected corticosteroid is micronized via a jet mill and the delivery gas may be typical gas flow exiting the jet mill, which would include aerosolized, micronized particles of the corticosteroid.
In specific embodiments, the corticosteroid to be processed according to the present methods is selected from fluticasone propionate and budesonide. In such embodiments, a conditioning gas may be mixed with a delivery gas (e.g., a jet mill gas flow) in a ratio of about 1 to 4 parts conditioning gas flow with about 1 part of the delivery gas. In certain such embodiments, the conditioning gas flow may be mixed with the jet mill gas flow in a ratio selected from about 1:1, 1.2:1, 1.4:1, 1.6:1, 1.8:1, 2.0:1, 2.2:1, 2.4:1, 2.6:1, 2.8:1, 3:1, 3.2:1, 3.4:1, 3.6:1, 3.8:1, and 4:1. In specific embodiments, the conditioning gas may be supplied at a gas flow rate ranging from about 150 SCFM up to about 500 SCFM and the delivery gas may be supplied at a gas flow rate of ranging from about 20 SCFM up to about 75 SCFM. However, in some embodiments, depending on the desired conditions for the conditioning zone and the nature of the material being processed, the gas flow rate of both the conditioning gas and the delivery gas may be increased as high as 3,300 SCFM.
When conditioning a corticosteroid exhibiting solubility in an organic solvent, such as fluticasone propionate or budesonide, the conditioning gas may be delivered at a temperature ranging from about 20° C. to about 30° C. and include an organic solvent vapor as a solvent. In particular embodiments of methods for conditioning a corticosteroid, including a corticosteroid selected from fluticasone propionate and budesonide, the temperature of the conditioning gas may be selected from at least 20° C., 21° C., 22° C., 23° C., 24° C., 25° C., 26° C., 27° C., 28° C., 29° C., and 30° C.
Moreover, where included in the conditioning gas, the organic solvent vapor may be provided within the conditioning gas to provide a relative saturation of the solvent in the conditioning zone ranging from about 10% to about 95%. Suitable organic solvents include an alcohol (e.g., ethanol, methanol, isopropyl alcohol, etc.), ketone (e.g., acetone, methyl ketone, ethyl ketone, etc.), ester (e.g., ethyl acetate, etc.), aliphatic alcohol (e.g., octanol, etc.), or alkane (e.g., octane, nonane, etc.). In specific embodiments for the conditioning of corticosteroid materials, including corticosteroids selected from fluticasone propionate and budesonide, the organic solvent vapor may be provided within the conditioning gas to provide a relative saturation of the solvent in the conditioning zone ranging from about 50% to about 80%. For example, in embodiments of methods for conditioning corticosteroid materials, including corticosteroids selected from fluticasone propionate and budesonide, the conditioning gas may be supplied at a temperature described herein with a relative solvent saturation selected from at least about 50%, 51%, 52%, 53%, 54%, 55%, 56%, 57%, 58%, 59%, 60%, 61%, 62%, 63%, 64%, 65%, 66%, 67%, 68%, 69%, 70%, 71%, 72%, 73%, 74% and 75%. At the temperatures and relative solvent saturation described herein, the residence time of the micronized corticosteroid material within the conditioning chamber may be from about 0.5 to about 10 seconds. In certain such embodiments, the micronized corticosteroid material is present within the conditioning chamber for a residence time selected from about 0.5 seconds, about 1 second, about 1.5 seconds, about 2 seconds, about 2.5 seconds, about 3 seconds, about 3.5 seconds, about 4 seconds, about 5 seconds, about 6 seconds, about 7 seconds, about 8 seconds, about 9 seconds, and about 10 seconds. However, the residence time can be adjusted as needed to achieve the desired conditioning.
As is further evidenced by the experimental examples that follow, methods according to the present description can be adapted to accomplish conditioning of varying materials exhibiting divergent physical and chemical properties.
In specific embodiments, methods for conditioning a particulate crystalline material (e.g., micronized crystalline material) according to the present description include: providing aerosolized micronized crystalline particles, wherein said micronized crystalline particles contain one or both of an amorphous material and a residual solvent; continuously mixing the micronized crystalline particles with a conditioning gas comprising a carrier gas and a conditioning vapor in a chamber connected directly to the exit of a micronization apparatus; maintaining the micronized crystalline particles in contact with the conditioning gas for sufficient time to result in annealing of said micronized crystalline particles, wherein said annealing results in a phase transformation; and separating the micronized crystalline particles from the conditioning gas. As detailed herein, such a phase transformation refers to a change in the bulk of the crystals present in a particulate crystalline material. In such embodiments, the phase transformation may be selected from removal of a solvent of crystallization, replacement of a solvent of crystallization, an amorphous to crystalline phase change, or a change in physical structure beyond just an amorphous to crystalline phase change.
The material (e.g., micronized crystalline material) processed according to any method described herein may be mixed with the conditioning gas for between about 0.1 to 600 seconds before the micronized crystalline material exits the conditioning zone.
The material (e.g., micronized crystalline material) processed according to any method described herein may be mixed with the conditioning gas for between about 2 to 6 seconds before the material exits the conditioning zone.
The material (e.g., micronized crystalline material) processed according to any method described herein may be mixed with the conditioning gas for about 3 seconds before the micronized crystalline material exits the conditioning zone.
The material (e.g., micronized crystalline material) processed according to methods described herein may be water soluble. Where the material to be processed according to a method described herein is water soluble, the conditioning gas may include a solvent vapor that is an aqueous solvent vapor, and the conditioning gas may be provided at a temperature ranging from about 20° C. to 100° C. and at a relative humidity ranging from about 0.05% to 95%.
The material (e.g., micronized crystalline material) processed according methods described herein may not be water soluble (e.g., soluble in one or more organic solvents). Where the material to be processed according to a method described herein is not water soluble the conditioning gas may include a solvent vapor that is an organic solvent vapor, and the conditioning gas may be provided at a temperature ranging from about 20° C. to 100° C. and at a vapor pressure of a non-aqueous solvent in the range of about 0.05% to 95%.
The material (e.g., micronized crystalline material) processed according to methods described herein may be an admixture of water soluble and non-water soluble materials. In such instances, the conditioning gas may include a solvent vapor that includes an aqueous solvent vapor and an organic solvent vapor, and the conditioning gas may be supplied at a temperature ranging from about 10° C. to 100° C. and at a relative humidity of the aqueous solvent in the range of about 0.05% to 95% and a vapor pressure of the non-aqueous solvent in the range of about 0.05% to 95%.
In any of the methods described herein, the material (e.g., micronized crystalline material) to be processed may be entrained, suspended, or aerosolized within a delivery gas before mixing with a conditioning gas. In such embodiments, the material may be produced using a jet mill and aerosolized in the jet mill gas flow.
In any of the embodiments of the methods and systems described herein, the conditioning gas may be mixed with the particulate material (e.g., an aerosolized micronized crystalline material) in a ratio of about 1 to 10 parts conditioning gas with about 1 part of the aerosolized micronized crystalline material. In such embodiments, the aerosolized micronized crystalline material may be entrained, suspended or aerosolized within a delivery gas.
In any of the embodiments of the systems and methods described herein, the conditioning gas may be supplied at a flow rate ranging from about 25 standard cubic feet per minute (SCFM) up to about 300 SCFM while mixing with the particulate crystalline material.
In any of the embodiments of the systems and methods described herein, the particulate material (e.g., micronized crystalline material) may be entrained, suspended or aerosolized within a delivery gas and the aerosolized particulate material supplied at a flow rate ranging from about 25 standard cubic feet per minute (SCFM) up to about 200 SCFM while mixing with a conditioning gas.
In any of the embodiments of the systems and methods described herein, the conditioning gas may comprise nitrogen gas.
In any of the embodiments of the systems and methods described herein, the particulate material (e.g., micronized crystalline material) may be mixed with the conditioning gas in a closed chamber.
In any of the embodiments of the systems and methods described herein, the particulate material (e.g., micronized crystalline material) may be one of glycopyrronium, including glycopyrrolate, dexipirronium, scopolamine, tropicamide, pirenzepine, dimenhydrinate, tiotropium, darotropium, aclidinium, umeclidinium, trospium, ipatropium, atropine, benzatropin, oxitropium, ephedrine, adrenaline, fenoterol, formoterol, isoprenaline, metaproterenol, salbutamol, albuterol, salmeterol, terbutaline, fluticasone, including fluticasone propionate, budesonide, mometasone, ciclesonide, and Compound A.
In specific embodiments, systems for conditioning a particulate crystalline material (e.g., micronized crystalline material) according to the present description include: a delivery zone for delivering the particulate material; a mixing zone in fluid communication with the delivery zone, wherein the particulate crystalline material is delivered from the micronizing zone to the mixing zone and therein mixed with a conditioning gas; a conditioning gas supply zone in fluid communication with the mixing zone, the conditioning gas supply zone providing the conditioning gas at a desired temperature and solvent vapor concentration to the mixing zone to be mixed with the particulate crystalline material; a conditioning zone in fluid communication with the mixing zone, wherein the mixture of the particulate crystalline material and the conditioning gas is delivered and remains in the conditioning zone for a desired residence time; and a separation and collection zone, wherein the conditioned particulate crystalline material is separated from the conditioning gas and the conditioned material is collected. In certain such embodiments, the delivery zone may be a micronizing zone comprising a device for micronizing the particulate crystalline material.
In particular embodiments, the systems described herein are configured to process a particulate crystalline material (e.g., micronized crystalline material) that is water soluble and the conditioning gas supply zone is configured to provide a conditioning gas that includes a water vapor at a temperature ranging from about 20° C. to 100° C. and at a humidity ranging from about 0.05% to 90% relative humidity.
In particular embodiments, the systems described herein are configured to process a particulate crystalline material (e.g., micronized crystalline material) that is not water soluble and the conditioning gas supply zone is configured to provide a conditioning gas that includes an non-aqueous (e.g. an organic solvent as described herein) vapor at a temperature ranging from about 20° C. to 100° C. and at a vapor pressure of a non-aqueous solvent in the range of about 0.05% to 90%.
In particular embodiments, the systems described herein are configured to process a particulate crystalline material (e.g., micronized crystalline material) that is an admixture of water soluble and non-water soluble materials, and the conditioning gas supply zone is configured to provide the conditioning gas at a temperature ranging from about 20° C. to 30° C. and at a relative humidity of 50 to 75% and vapor pressure of a non-aqueous solvent in the range of about 50% to 75%.
In any of the embodiments described herein, the system for conditioning particulate material may include a conditioning gas supply zone configured to provide a conditioning gas at a temperature of about 25° C. and with a humidity of about 65% relative humidity
In any of the embodiments described herein, the system for conditioning particulate material may include a conditioning zone configured to maintain the mixture of the particulate material (e.g., micronized crystalline material) and the conditioning gas within the conditioning zone for a residence time of between about 0.5 to 60 seconds. For example, the systems for conditioning particulate material described herein may include a conditioning zone configured to maintain a mixture of the particulate crystalline material and the conditioning gas within the conditioning zone for a residence time of between about 1 to about 10 seconds. In even more specific embodiments, the systems for conditioning particulate material described herein may include a conditioning zone configured to maintain a mixture of the particulate crystalline material and the conditioning gas within the conditioning zone for a residence time of about 3 seconds.
In any of the embodiments described herein including a delivery zone that comprises a device for micronizing the particulate crystalline material (i.e., a micronizing zone), the device for micronizing the particulate crystalline material may be a jet mill or any other suitable system or device as described herein.
In any of the embodiments described herein, the systems for conditioning a particulate material may be configured for conditioning a material selected from a particulate crystalline material (e.g., micronized crystalline material) selected from at least one of glycopyrronium, including glycopyrrolate, dexipirronium, scopolamine, tropicamide, pirenzepine, dimenhydrinate, tiotropium, darotropium, aclidinium, umeclidinium, trospium, ipatropium, atropine, benzatropin, oxitropium, ephedrine, adrenaline, fenoterol, formoterol, isoprenaline, metaproterenol, salbutamol, albuterol, salmeterol, terbutaline, fluticasone, including fluticasone propionate, budesonide, mometasone, ciclesonide, and Compound A.
In particular embodiments of the systems described herein, the systems may be configured for conditioning a particulate glycopyrrolate material using any of the process conditions detailed herein. In certain such embodiments, the systems described herein can be configured for micronizing a crystalline glycopyrrolate material. In such embodiments, the systems may include a micronizing zone with a jet mill for micronizing glycopyrrolate. In certain such embodiments, the jet mill gas may be a delivery gas and mixed with a conditioning gas within the mixing zone at a ratio of from about 1 to 4 parts conditioning gas mixed with about 1 part of the jet mill gas.
In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material) may include a conditioning gas supply zone configured to provide the conditioning gas to the mixing zone at a flow rate ranging from about 150 standard cubic feet per minute (SCFM) up to about 300 SCFM.
In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material) may be configured to entrain, suspend, or aerosolize the particulate material within a delivery gas before the material is introduced to a mixing zone or blended with a conditioning gas. In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material) may be configured to deliver the particulate material in a delivery gas at a flow rate ranging from about 35 standard cubic feet per minute (SCFM) up to about 200 SCFM.
In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material) may be configured to include a mixing zone that comprises a dispersion head assembly wherein the conditioning gas and the micronized crystalline material are mixed. In such embodiments, the dispersion head assembly may include a mixing head configured to control the mixing of the conditioning gas and the particulate crystalline material. Where a system as described herein includes a mixing head, the mixing head may be configured to include an injection nozzle inlet configured to deliver the conditioning gas to an injection nozzle and a delivery gas inlet configured to deliver the micronized crystalline material to the injection nozzle.
In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material) the collection zone may include a cyclone collector.
In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material), the system may be configured to process micronized crystalline material having a particle size ranging from about 0.1 μm to about 10 μm.
In any of the embodiments described herein, the systems for conditioning a particulate crystalline material (e.g., micronized crystalline material), the system may include a holding chamber for collecting the conditioned particles. In certain such embodiments, the system may be configured to prepare and/or deliver a secondary conditioning gas to the holding chamber and mix the secondary conditioning gas with the conditioned crystalline particles within in the holding chamber for a period of time sufficient to provide a secondary conditioning of the crystalline particles. Alternatively, in embodiments of a system for conditioning a particulate crystalline material that include a holding chamber, the holding chamber may be configured simply to receive the conditioned material or to facilitate transition of the conditioned material from a primary conditioning system to a secondary conditioning system. In any of the embodiments of the systems described herein that include a holding chamber, the holding chamber may be configured to maintain the conditioned material in a continuously fluidized state.
Glycopyrrolate (3-[(cyclopentylhydroxyphenylacetyl)oxy]-1, 1-dimethyl-, bromide) was received as coarse crystalline active agent from the manufacturer (Boehringer Ingelheim Chemicals, Inc., Petersburg, Va. 23805). The glycopyrrolate (GP) was then micronized by jet milling to achieve a reduction in particle size distribution.
A portion of the micronized GP was also conditioned using an in-process conditioning system wherein nitrogen conditioning gas was supplied to the in-process conditioning system and was controlled for flow rate, temperature and humidity. The conditioning gas was humidified through a droplet evaporation chamber after which it was directed to a mixing zone. In the mixing zone, the conditioning gas was mixed with the jet-milled aerosol comprising the micronized GP. The aerosol then entered a conditioning zone where annealing of the micronized GP occurred. The particle residence time through the conditioning zone was adjusted by means of the conditioning zone chamber geometry and/or the gas flow rate through the conditioning zone chamber. After passing through the conditioning zone, the micronized GP particles reached the cyclone-collection zone where the solid particles were separated from the gas phase and transported to a collection vessel. Upon completion of the batch processing, the collector was disengaged and transferred to a glove box for sampling. The sampling occurred in a <5% relative humidity environment. Samples were then analyzed for particle size distribution and amorphous content.
The particle size distribution of the standard jet milled micronized GP particles and the micronized GP particles after in-process conditioning were sampled and are shown in Table 1. The particle size distributions in Table 1 reflect the GP particle sizes sampled immediately after processing. As is shown in Table 1, the in-process conditioning does not affect the particle size distribution of the micronized GP particles.
Experimental batches of micronized GP particles were prepared according to the in-process conditioning system as described herein. The jet milling parameters and the conditioning parameters used for the in-process conditioning for each of the experimental batches are shown in Table 2. Batch 1A was a control batch of standard micronized GP and was not conditioned but was processed using dry nitrogen gas at ambient temperature. The powder feed rate for all batches were set nominally at 66 g/hr.
Table 3 lists the particle size distribution for the experimental batches as was determined by laser diffraction immediately after processing and again after 1-day of exposure to 25° C. and 60% relative humidity.
As shown in
In contrast, analysis of the 2D batch that was conditioned according to the in-process conditioning parameters as listed in Table 2, showed particle size stability. As shown in
Electron micrographs of the in-process conditioned sample 2E show improved stability of conditioned micronized GP particles. As shown in
Examples 2 and 3 provide examples of in-process conditioning of water insoluble molecules using a conditioning gas containing a vaporized organic solvent (ethanol) to promote annealing. Budesonide and fluticasone propionate were selected as representative compounds. The annealing conditions were determined by selecting conditions that would promote crystallization of the amorphous fraction under an ethanol atmosphere by determining the corresponding ethanol sorption isotherms.
Budesonide (16,17-(butylidenebis(oxy))-11,21-dihydroxy-, (11-β, 16-α)-pregna-1,4-diene-3,20-dione16, 17-(butylidenebis(oxy))-11,21-dihydroxy-, (11-β, 16-α)-pregna-1,4-diene-3,20-dione) was micronized using a laboratory scale jet mill set at 75 psig grinding pressure and 80 psig injection pressure. The crystalline budesonide was fed into the jet mill at a powder feed rate of approximately 25±10% g/hr. Two batches of micronized budesonide were produced. One was not subjected to further processing, while the second was conditioned to remove amorphous content according to the present description.
Batch 1 (unannealed/not conditioned) did not undergo any thermal or vapor conditioning. The nitrogen gas was supplied dry to the system (i.e., no organic solvents were used), and the micronized material was collected under at ambient temperature. Batch 1 was collected and transferred into a purged isolator for sampling.
Batch 2 (annealed/conditioned) was conditioned according to the present description using a conditioning gas that included an ethanol vapor, with a target of 75% relative saturation in the conditioning zone. To form the conditioning gas, ethanol (95% w/w) was atomized in nitrogen gas using a 0.21″ atomizer nozzle with a set atomizer gas flow rate of 30 std. L/min (SLPM) and a liquid flow rate of 32 g/min. The conditioning gas flow rate was set to 205 SLPM with a humidifier inlet temperature of 185° C. and conditioning zone outlet of 30° C. The jet mill grind pressure was delivered at 75 psig with an injection pressure of 80 psig, resulting in a nominal micronizer gas flow rate of 122 SLPM, along with a total conditioning gas flow rate (including the atomizer gas flow) of 235 SLPM. The conditioning gas to micronizing gas (also referred to as a delivery gas) ratio (CMR) for this process configuration was 1.9:1, with a nominal total system gas flow rate of 357 SLPM. Batch 2 was collected in a 0.5 L stainless steel collector, transferred to a purged (<5% RH) isolator and sampled for analysis.
Both batches of micronized budesonide were analyzed for particle size distribution by Sympatec laser diffraction, with the results provided in Table 4. As can be seen in Table 4, Batch 2 (annealed) demonstrated good physical stability after micronization, whereas Batch 1 (unannealed) demonstrated potential agglomeration marked by a significant shift in size distribution.
The amorphous content by vapor sorption and particle morphology for both batches were also assessed.
Fluticasone propionate (S-(fluoromethyl)-6α,9-difluoro-11β, 17-dihydroxy-16α-methyl-3-oxoandrosta-1, 4-diene-17β-carbothioate, 17-propanoate) was micronized using a laboratory scale jet mill set at 65 psig grinding pressure and 74 psig injection pressure. The crystalline fluticasone was fed into the jet mill at a powder feed rate of approximately 25±10% g/hr. Two batches of micronized fluticasone were produced. One was not subjected to further processing, while the second was conditioned to remove amorphous content according to the present description.
Batch 1 (unannealed/not conditioned) did not undergo any thermal or vapor conditioning. The nitrogen gas was supplied dry to the system (i.e., no organic solvents were used), and the micronized material was collected under at ambient temperature. Batch 1 was collected and transferred into a purged isolator for sampling.
Batch 2 (annealed/conditioned) was conditioned according to the present description using a conditioning gas that included an ethanol vapor, with a target of 75% relative saturation in the conditioning zone. To form the conditioning gas, ethanol (95% w/w) was atomized in nitrogen gas using a 0.21″ atomizer nozzle with a set atomizer gas flow rate of 30 std. L/min (SLPM) and a liquid flow rate of 32 g/min. The conditioning gas flow rate was set to 205 SLPM with a humidifier inlet temperature of 185° C. and conditioning zone outlet of 30° C. At the given grind and injection pressures delivered to the system, the resulting micronizer gas flow was nominally 108 SLPM, along with a total conditioning gas flow rate (including the atomizer gas flow) of 235 SLPM. The conditioning gas to micronizing gas (also referred to as a delivery gas) ratio (CMR) for this process was 2.2:1, with a total gas flow of 343 SLPM. Batch 2 was collected in a 0.5 L stainless steel collector, transferred to a purged (<5% RH) isolator and sampled for analysis.
Both batches of micronized fluticasone were analyzed for particle size distribution by Sympatec laser diffraction, with the results provided in Table 5. As can be seen in Table 5, Batch 2 (annealed) demonstrated good physical stability after micronization, whereas Batch 1 (unannealed) demonstrated agglomeration marked by a shift in size distribution.
The amorphous content by vapor sorption and particle morphology for both batches were also assessed.
Three scale-up batches of micronized glycopyrrolate (GP) were produced via a large-scale in-process micronization and conditioning system according to the present description that utilized a two-collector process at approximately 1 kg per batch. The first two lots were manufactured using a single, raw crystalline API lot, while the third used a different lot from the same vendor. All batches were produced on different dates using the same process configuration that utilized the same 4″ jet mill, and the same conditioning environment (i.e., a target of 55% RH at 40° C. conditioning zone outlet temperature).
The system was brought to steady-state equilibrium, with the jet mill operating at 68 psig injection pressure and 48 psig grind pressure for a micronizer gas flow of approximately 36 SCFM. Again, the micronizer gas also served as the delivery gas for the micronized material. The conditioning gas flow rate was supplied at approximately 78 SCFM with a humidifier outlet temperature of 57° C. Water was delivered to the 0.21″ atomizer nozzle at a liquid flow rate of 75.1 ml/min. The conditioning to micronization gas ratio (CMR) was set at 2.2:1. Product was collected in 8 L stainless steel collectors, which were heated using a thermal jacket to prevent the collector environment from falling below the dew-point temperature.
Once the system reached steady-state, powder was fed into the jet mill at a nominal rate of 1 kg/hr. A collector change-out was performed half way through each run with a collector purging step before each change-out to obviate the risk of any post-process affects due to residual vapor. The collectors were transferred to a purged isolator (<5% RH) for sampling and packaging to prevent any post-process affects due to ambient moisture.
All batches were analyzed for particle size distribution by Sympatec laser diffraction, with the results provided in Table 6. n=3 replicates per collector were assessed (mean values are shown). As can be seen in Table 6, the particle size distribution achieved in each batch exhibited good batch to batch reproducibility.
All batches were also analyzed for amorphous content by dynamic vapor sorption using n=2 replicates per collector. The results are provided in Table 7, which reflects that the amorphous content achieved in each batch also exhibited good batch to batch reproducibility.
Sucrose (saccharose; α-D-glucopyranosyl-(1→2)-β-D-fructofuranoside) was micronized and conditioned using the large scale micronization/annealing system utilized in Example 4. Particulate sucrose was delivered to the 4″ jet mill at a nominal powder feed rate of 0.5 kg/hr. Two batches of micronized sucrose were produced. For the first, the 4″ jet mill was set at an 80 psig injection pressure and a grind pressure of 70 psig. For the second, the 4″ jet mill was set at an 80 psig injection pressure and a grind pressure of 76 psig. Identical lots of the raw input material were used for dispensing both batches. Process conditions for each batch are provided in Table 8.
Sucrose A (unannealed/not conditioned) did not undergo any thermal or vapor conditioning. The nitrogen gas was supplied dry to the system, and the system was run at ambient temperature. The jet mill was operated at 80 psig injection pressure and 70 psig grind pressure for a nominal micronizer gas flow of approximately 45.0 SCFM. The conditioning gas flow rate (ambient temperature, 0% RH) was supplied at approximately 61.0 SCFM. The conditioning to micronizing gas Ratio (CMR) was set at 1.4:1. Product was collected in 8 L stainless steel collectors, without the use of a thermal jacket.
Powder was fed into the jet mill at a nominal feed rate of 0.5 kg/hr. A collector change-out was performed half way through each run. The collectors were transferred to a purged isolator (<5% RH) for sampling and packaging to prevent any post-process affects due to ambient moisture.
Sucrose B (annealed/conditioned) was conditioned at a target 55% relative humidity at 40° C. conditioning zone outlet temperature. The system was brought to steady-state equilibrium, with the jet mill operating at 80 psig injection pressure and 76 psig grind pressure for a nominal micronizer gas flow of approximately 49.4 SCFM. The conditioning gas flow rate was supplied at approximately 61.8 SCFM with a humidifier outlet temperature of 157.2° C. Water was delivered to a 0.21″ atomizer nozzle at a liquid flow rate of 76.2 ml/min. The conditioning to micronizing gas Ratio (CMR) was set at 1.4:1. Product was collected in 8 L stainless steel collectors, which were heated using a thermal jacket to prevent the collector environment from falling below the dew-point temperature.
Once the system reached steady state, powder was fed into the jet mill at a rate of 0.5 kg/hr. A collector change-out was performed half way through each run, including a system purge-out step prior to each change-out to obviate the risk of any post-process affects due to residual vapor. The collectors were transferred to a purged isolator (<5% RH) for sampling and packaging to prevent any post-process affects due to ambient moisture.
Both micronized sucrose batches were analyzed for particle size distribution by Sympatec laser diffraction. The results of the analysis are provided in Table 9 and
The amorphous content by vapor sorption and particle morphology for both batches of micronized sucrose were also assessed.
Compound A, a novel bi-functional muscarinic antagonist and beta2 agonist (IUPAC: 7-[(1R)-2-[2-[2-fluoro-5-[[4-(2-isopropylthiazole-4-carbonyl)-1-oxa-4,9-diazaspiro[5.5]undecan-9-yl]methyl]phenyl]ethylamino]-1-hydroxy-ethyl]-4-hydroxy-3H-1,3-benzothiazol-2-one; di[[(1S,4R)-7,7-dimethyl-2-oxo-norbornan-1-yl]methanesulfonic acid] salt), was selected for micronization and subsequent solvent removal using primary and secondary conditioning steps. Compound A retained ˜5% residual isopropyl alcohol solvent after manufacture. Compound A was micronized and conditioned using an in-process conditioning system according to the present description that included a 1″ jet mill. Process conditions were selected to promote solvent exchange to reduce or remove residual isopropyl alcohol and replace the isopropyl alcohol either directly with water or with ethanol and secondarily with water. Three batches of micronized Compound A were produced as described in Table 10 below. Identical lots of the raw input material were used for dispensing all three batches.
Batch 1 (unannealed) did not undergo any thermal or vapor conditioning. The nitrogen gas was supplied dry to the system and ran at ambient temperature (i.e., no heat or solvent vapor was used). The total conditioning gas flow rate was 255 SLPM. The micronization gas flow rate was about 110 SLPM at the given milling pressures, giving a conditioning to micronization gas Ratio (CMR) of 2.3:1 and total gas flow of 365 SLPM. Batch 1 was collected and transferred into a purged isolator for sampling.
Batch 2 (conditioned with water vapor at 29° C./69% RH) was conditioned using a conditioning gas that provided water vapor at 69% relative humidity (RH) in the conditioning zone. The conditioning gas was formed by atomizing water in nitrogen gas using a 0.21″ atomizer nozzle, with a set atomizer gas flow rate of 35 std. L/min (SLPM) and a liquid flow rate of 7 g/min. The conditioning gas flow rate was set to 220 SLPM with a humidifier inlet temperature of 100° C. and conditioning zone outlet of 29° C. The total conditioning gas flow rate including the atomizer was 255 SLPM. The micronization gas flow rate was about 110 SLPM at the given milling pressures, giving a conditioning to micronization gas Ratio (CMR) of 2.3:1 and total gas flow of 365 SLPM. Batch 2 was collected in a 0.5 L stainless steel collector, transferred to a purged (<5% RH) isolator and sampled for analysis.
Batch 3 (primary conditioning with ethanol at 30° C./53% RS; secondary conditioning with water at 30° C./67% RH) was conditioned using a conditioning gas including ethanol vapor, with a target of 75% relative saturation in the conditioning zone. The conditioning gas was formed by atomizing ethanol (95% w/w) in nitrogen gas using a 0.21″ atomizer nozzle, with a set atomizer gas flow rate of 35 std. L/min (SLPM) and a liquid flow rate of 28 g/min. The conditioning gas flow rate was set to 220 SLPM with a humidifier inlet temperature of 150° C. and conditioning zone outlet of 30° C. The micronization gas flow rate was about 110 SLPM at the given milling pressures, giving a conditioning to micronization gas Ratio (CMR) of 2.3:1 and total gas flow of 365 SLPM. Upon completion of conditioning with ethanol, ethanol liquid flow was stopped, and the process was adjusted to provide a conditioning gas containing water vapor. The humidifier inlet temperature of 100° C. was set and water was then fed into the system at a flow rate of 7 g/min at a CZ outlet temperature and collector temperature of 30° C. The material was secondarily conditioned in the collector with a conditioning gas containing water vapor at 67% RH. Batch 3 was collected in a 0.5 L stainless steel collector, transferred to a purged (<5% RH) isolator and sampled for analysis.
All three batches were analyzed for particle size distribution by Sympatec laser diffraction, with the results shown in Table 11. Particle Size Distribution of conditioned Compound A demonstrates good reproducibility, and the particle size distribution of the conditioned Compound A is consistent with the unannealed micronized material.
Residual solvent content of the material from different batches was also analyzed. Table 12 shows the residual solvent content of materials from each batch as assessed by GC analysis. Residual solvent is partially removed using primary (ethanol) and secondary (water) conditioning. Material that was treated using a secondary conditioning process exhibited increased replacement of the IPA.
Compound A (IUPAC: 7-[(1R)-2-[2-[2-fluoro-5-[[4-(2-isopropylthiazole-4-carbonyl)-1-oxa-4,9-diazaspiro[5.5]undecan-9-yl]methyl]phenyl]ethylamino]-1-hydroxy-ethyl]-4-hydroxy-3H-1,3-benzothiazol-2-one; di[[(1S,4R)-7,7-dimethyl-2-oxo-norbornan-1-yl]methanesulfonic acid] salt) was received with a 3.8% ethanol residual content. This material had been previously micronized and conditioned according to the present description to reduce the presence of isopropyl (IPA) and ethanol (EtOH) by solvent exchange/removal. The material was exposed to another conditioning gas that included water vapor, and was mixed with the conditioning gas in a conditioning zone for approximately 1.5 hours. As shown in Table 13, residual IPA and EtOH was nearly completely removed and water content of the material increased.
The various embodiments described above can be combined to provide further embodiments. All of the U.S. patents, U.S. patent application publications, U.S. patent applications, foreign patents, foreign patent applications and non-patent publications referred to in this specification and/or listed in the Application Data Sheet, including but not limited to U.S. Provisional Application No. 61/799,956, filed Mar. 15, 2013, are incorporated herein by reference, in their entirety. Aspects of the embodiments can be modified, if necessary to employ concepts of the various patents, applications and publications to provide yet further embodiments.
| Number | Date | Country | |
|---|---|---|---|
| 61799956 | Mar 2013 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 14213834 | Mar 2014 | US |
| Child | 15873779 | US |
