Patent Grant
7575761
The present invention relates generally to systems and methods for manufacturing dry powder formulations. More specifically, the present invention provides systems and methods for the production of spray dried powders suitable for pharmaceutical applications, preferably for dry powders to be administered by inhalation. According to the invention, the drying kinetics of a spray drying process may be controlled, for example, to facilitate surface diffusion of surface active components or to facilitate amorphous-to-crystalline transformations during the manufacture of dry powder formulations.
Over the years, certain drugs have been sold in compositions suitable for pulmonary delivery to treat various conditions in humans. Such pulmonary drug delivery compositions include an aerosolized drug formulation that is inhaled by the patient so that the active agent can reach the alveolar region of the lungs.
Pulmonary drug delivery can be achieved by, for example, delivery of dry powder formulations to the deep lung. These powders have been prepared by spray drying as described in WO 96/32149, WO 99/16419 and U.S. Pat. Nos. 5,976,574, 5,985,248, 6,001,336, and 6,051,256, the disclosures of which are incorporated herein in their entirety. Preparing pharmaceutical compositions as stable dry powders by spray drying, however, poses many challenges. In order to scale up the spray drying process, it is desirable to increase the total solids content of the feed stream. It was found, however, that the emitted dose of powders prepared from higher total solids content feed streams, that is above about 1% (w/v), declined significantly.
In addition, the ability to deliver pharmaceutical compositions as dry powders poses many challenges. For example, particles containing both crystalline and amorphous phases may exhibit physical or chemical instability. Transformations of the materials during storage from amorphous to crystalline may result in such instability as a result of particle fusion and other physical changes. Further, crystallization tends to increase the water content in the remaining amorphous phase and thereby decrease the glass transition temperature (Tg) of the materials. Increased water content of the amorphous region increases molecular mobility and may increase chemical degradation reaction rates (i.e., hydrolysis, aggregation, etc.). Formulations having a higher percentage of crystallinity are less likely to degrade during storage.
It is known to provide spray dryers with drying zones which are maintained at different temperatures in order to provide some control of the drying kinetics. For example, U.S. Pat. No. 4,257,799 discloses a method for producing small hollow glass spheres having an outer diameter from about 100 to 500 microns wherein the method involves introducing aqueous droplets of a glass-forming solution into a long vertical drop oven or furnace having varying temperature regions.
U.S. Pat. Nos. 5,632,100, 5,924,216 and 4,281,024 also disclose spray drying with multiple drying zones, in which larger particles are typically subjected to a secondary drying in order to achieve desired moisture content.
U.S. Pat. No. 6,051,257 discloses structurally modifying particles after they are formed by a spray drying process in order to impart desired physical properties to the particles. The particle modifier is typically a furnace having temperature control independent of the spray dryer furnace and is positioned to receive the formed particles after they exit the spray dryer furnace.
U.S. Pat. No. 5,874,063 to Briggner et al. describes a method for increasing the crystallinity of conventional fine particles by treating the already manufactured fine particles with a solvent in the vapor phase and then removing the excess solvent. The solvent may be an organic solvent or it may be water.
WO 00/64552 discloses a method of spray drying and a plant therefore whereby spray drying is performed at increased pressure. The invention is directed to spray drying where an amorphous product is desired and/or where a high bulk density powder is desired. Spray drying according to this disclosure is conducted in a pressurized environment not below 1.25 bar absolute.
There remains a need to provide control of drying kinetics of spray drying processes in order to produce particles of desired physical properties for pharmaceutical applications such as the preparation of dry powders for inhalation. It is desirable to provide systems and methods which provide for dry powders with acceptable pulmonary delivery characteristics. The present invention overcomes the above shortcomings in the prior art.
The present invention provides exemplary systems and methods for producing dry powder formulations which in one aspect encourage surface diffusion of surface active components during the formation of dry powder medicaments, and therefore have improved emitted doses for pulmonary delivery. In another aspect of this invention, we have found that it is possible to provide improved control of the drying kinetics of spray drying methods in order to encourage amorphous-to-crystalline transformations during drying without exposing the finished fine particles to added water, solvent or thermal processing. We are thus able to reduce or minimize the potential instability of a fine particle formulation throughout its shelf life.
One embodiment of the present invention is directed to spray drying of pharmaceutical formulations containing surface active components. A system is provided for producing dry powders wherein the system includes an atomizer and at least one conditioning zone coupled to the atomizer to suspend an atomized formulation for a residence time where the atomized formulation remains in the liquid state. A dryer is coupled to the conditioning zone to dry the formulation exiting the conditioning zone. Further, a collector collects the dried formulation in powder form. In this manner, by controlling the residence time, temperature and relative humidity in the conditioning zone, the atomized formulation is suspended in a manner which allows the droplets to reach thermodynamic equilibrium, wherein the surface active component diffuses to the surface of the droplets to reach its equilibrium orientation. According to this aspect of the invention, the temperature and relative humidity in the conditioning zone is maintained at levels to minimize droplet drying in the conditioning zone during the period immediately following atomization, preferably at levels which prevent solvent evaporation all together.
The present invention further provides methods for producing a powdered formulation having a high concentration of surface active components on the surface of the particles. In one method of the present invention, an atomized formulation of liquid droplets is introduced into a conditioning zone. The atomized formulation is suspended within the conditioning zone for a residence time, during which the formulation remains in the liquid state to allow the droplets to reach thermodynamic equilibrium and allow diffusion of surface active components to the surface of the droplets. The method includes transferring the conditioned formulation to a dryer, introducing a heated gas into the drier to dry the conditioned formulation and form dry particles, and collecting the dry particles.
In another aspect, the present invention provides exemplary systems and methods for producing dry powder formulations which encourage amorphous-to-crystalline transformations of such formulations during manufacture to result in increased stability during storage. The present invention is based at least in part on the unexpected observation that storage stability of powdered formulations is greatly effected by the manufacturing conditions of the powders. According to this aspect of the invention, a multi-zonal spray dryer system and method of use are provided for producing dry powders. The system includes at least one conditioning zone having an inlet to introduce an atomized formulation into the conditioning zone. Air flow into the conditioning zone is controlled to control temperature and relative humidity.
The atomized formulation remains in the conditioning zone for a residence time at a predetermined temperature and relative humidity to allow equilibration of the water activity in the atomized droplet with the environment of the conditioning zone. This equilibration of water activity, or water content, results in partial drying of the droplet and promotes amorphous-to-crystalline transformations in the atomized formulation. A dryer is coupled to the conditioning zone to dry the atomized formulation into the final dried particles. Further, a collector collects the dried particles. In this manner, by controlling temperature and relative humidity in the conditioning zone and by controlling the residence time, the atomized formulation is conditioned and dried in a manner that promotes amorphous-to-crystalline transformation. According to this aspect of the invention, partially dried particles leave the conditioning zone wherein the particles retain a sufficiently high moisture content so as to require further drying. This excess moisture in the partially dried particles acts as a plasticizer to allow crystallization. The partially dried particles are then exposed to temperatures and relative humidity levels that allow crystallization to occur at a rate to convert amorphous material within a residence time of a few seconds.
According to another aspect of the invention, the pressure is controlled in order to provide elevated pressures of up to 75 atmospheres within the conditioning zones and/or within the dryer.
“Active agent” as described herein includes an agent, drug, compound, composition of matter or mixture thereof which provides some pharmacologic, often beneficial, effect. This includes feeds, feed supplements, nutrients, drugs, vaccines, vitamins, and other beneficial agents. As used herein, the terms further include any physiologically or pharmacologically active substance that produces a localized or systemic effect in a patient. The active agent that can be delivered includes antibiotics, antiviral agents, anepileptics, analgesics, anti-inflammatory agents and bronchodilators, and viruses and may be inorganic and organic compounds, including, without limitation, drugs which act on the peripheral nerves, adrenergic receptors, cholinergic receptors, the skeletal muscles, the cardiovascular system, smooth muscles, the blood circulatory system, synaptic sites, neuroeffector junctional sites, endocrine and hormone systems, the immunological system, the reproductive system, the skeletal system, autacoid systems, the alimentary and excretory systems, the histamine system and the central nervous system. Suitable agents may be selected from, for example, polysaccharides, steroids, hypnotics and sedatives, psychic energizers, tranquilizers, anticonvulsants, muscle relaxants, antiparkinson agents, analgesics, anti-inflammatories, muscle contractants, antimicrobials, antimalarials, hormonal agents including contraceptives, sympathomimetics, polypeptides, and proteins capable of eliciting physiological effects, diuretics, lipid regulating agents, antiandrogenic agents, antiparasitics, neoplastics, antineoplastics, hypoglycemics, nutritional agents and supplements, growth supplements, fats, antienteritis agents, electrolytes, vaccines and diagnostic agents.
Examples of active agents useful in this invention include but are not limited to insulin, calcitonin, erythropoietin (EPO), Factor VIII, Factor IX, ceredase, cerezyme, cyclosporine, granulocyte colony stimulating factor (GCSF), alpha-1 proteinase inhibitor, elcatonin, granulocyte macrophage colony stimulating factor (GMCSF), growth hormone, human growth hormone (HGH), growth hormone releasing hormone (GHRH), heparin, low molecular weight heparin (LMWH), interferon alpha, interferon beta, interferon gamma, interleukin-2, luteinizing hormone releasing hormone (LHRH), somatostatin, somatostatin analogs including octreotide, vasopressin analog, follicle stimulating hormone (FSH), insulin-like growth factor, insulintropin, interleukin-1 receptor antagonist, interleukin-3, interleukin-4, interleukin-6, macrophage colony stimulating factor (M-CSF), nerve growth factor, parathyroid hormone (PTH), thymosin alpha 1, IIb/IIIa inhibitor, alpha-1 antitrypsin, respiratory syncytial virus antibody, cystic fibrosis transmembrane regulator (CFTR) gene, deoxyribonuclease (Dnase), bactericidal/permeability increasing protein (BPI), anti-CMV antibody, interleukin-1 receptor, 13-cis retinoic acid, pentamidine isethionate, natural or synthetic lung surfactant, nicotine, albuterol sulfate, metaproterenol sulfate, beclomethasone dipropionate, triamcinolone acetamide, budesonide acetonide, ipratropium bromide, flunisolide, fluticasone, cromolyn sodium, ergotamine tartrate and the analogues, agonists and antagonists of the above, ciprofloxacin, tobramicin, gentamicin, and azithromicycin. Active agents may further comprise nucleic acids, present as bare nucleic acid molecules, viral vectors, associated viral particles, nucleic acids associated or incorporated within lipids or a lipid-containing material, plasmid DNA or RNA or other nucleic acid construction of a type suitable for transfection or transformation of cells, particularly cells of the alveolar regions of the lungs. The active agents may be in various forms, such as soluble and insoluble charged or uncharged molecules, components of molecular complexes or pharmacologically acceptable salts. The active agents may be naturally occurring molecules or they may be recombinantly produced, or they may be analogs of the naturally occurring or recombinantly produced active agents with one or more amino acids added or deleted. Further, the active agent may comprise live attenuated or killed viruses suitable for use as vaccines.
The active agent of the present invention may optionally be combined with pharmaceutical carriers or excipients which are suitable for respiratory and pulmonary administration. Such carriers or excipients may serve simply as bulking agents when it is desired to reduce the active agent concentration in the powder which is being delivered to a patient, or may be added to the active agent prior to processing to improve the stability and/or dispersability of the powder within a powder dispersion device. In other embodiments, the excipients may be delivered via the pulmonary route without an active agent, for example in clinical trials as a placebo. Such excipients include but are not limited to (a) carbohydrates, e.g., monosaccharides such as fructose, galactose, glucose, D-mannose, sorbose, and the like; disaccharides, such as lactose, trehalose, cellobiose, and the like; cyclodextrins, such as 2-hydroxypropyl-β-cyclodextrin; and polysaccharides, such as raffinose, maltodextrins, dextrans, and the like; (b) amino acids, such as glycine, arginine, aspartic acid, glutamic acid, cysteine, lysine, and the like; (c) organic salts prepared from organic acids and bases, such as sodium citrate, sodium ascorbate, magnesium gluconate, sodium gluconate, tromethamin hydrochloride, and the like; (d) peptides and proteins such as aspartame, human serum albumin, gelatin, and the like; and (e) alditols, such as mannitol, xylitol, and the like. A preferred group of carriers includes lactose, trehalose, raffinose, maltodextrins, glycine, sodium citrate, human serum albumin and mannitol.
“Dry powder” refers to a composition that consists of finely dispersed solid particles that are free flowing and capable of (i) being readily dispersed in an inhalation device and (ii) inhaled by a subject so that a portion of the particles reach the lungs to permit penetration into the alveoli. Such a powder is considered to by “respirable” or suitable for pulmonary delivery. The term dry, in reference to the powder, means that the composition has a moisture content which allows the particles to be readily dispersed in an inhalation device to form an aerosol. A dry powder will typically contain less than about 10 percent moisture, preferably less than 5% moisture, and more preferably will contain less than about 3 percent moisture.
“Emitted dose” or “ED” refers to an indication of the delivery of dry powder from a suitable a suitable inhaler device after a firing or dispersion event from a powder unit or reservoir. ED is defined as the ratio of the delivered dose to the nominal dose (i.e. the mass of the powder per unit dose placed into a suitable inhaler device prior to firing). The ED is an experimentally-determined amount, and is typically determined using an in-vitro device set up which mimics patient dosing. To determine an ED value, a nominal dose of dry powder (as defined above) is placed into a suitable inhaler device, which is then actuated, dispersing the powder. The resulting aerosol cloud is then drawn by vacuum from the device, where it is captured on a tared filter attached to the device mouthpiece. The amount of powder that reaches the filter constitutes the delivered dose. For example, for a 5 mg, dry powder-containing blister pack placed into an inhalation device, if dispersion of the powder results in the recovery of 4 mg powder on a tared filter as described above, then the ED for the dry powder composition is 4 mg (delivered dose)/5 mg (nominal dose)=80%.
“Mass median diameter” or “MMD” is a measure of median particle size, since the powders of the invention are generally polydisperse (i.e., consist of a range of particle sizes). MMD values as reported herein are determined by centrifugal sedimentation, although any number of commonly employed techniques can be used for measuring median particle size.
“Mass median aerodynamic diameter” or “MMAD” is a measure of the aerodynamic size of a dispersed particle. The aerodynamic diameter is used to describe an aerosolized powder in terms of its settling behavior, and is the diameter of a unit density sphere having the same settling velocity, generally in air, as the particle. The aerodynamic diameter encompasses particle shape, density and physical size of a particle. As used herein, MMAD refers to the midpoint or median of the aerodynamic particle size distribution of an aerosolized powder determined by cascade impaction.
“Powdered formulation” means the active agent as defined above in a formulation that is suitable for pulmonary delivery or the excipient that is suitable for pulmonary delivery or a combination of the active agent and the excipient. The powdered formulation may be delivered in the dry powder form or it may be in a mixture with a suitable low boiling point, highly volatile propellant. It is to be understood that more than one active agent or excipient may be incorporated into the powdered formulation and that the use of the term “agent” or “excipient” in no way excludes the use of two or more such agents or excipients.
“Surface active components” refers to any component of a formulation used with the systems and methods of the present invention which acts to decrease the surface tension of the droplets and may be the active agent including surface active proteins such as insulin, or may be an excipient added to the formulation.
According to a first aspect of the present invention directed to systems and methods for producing dry powders comprising increased surface concentration of surface active components, the active agent, excipient or active agent/excipient combination is dissolved or suspended in feed stock 18 at a concentration from 0.01% (w/v) to 10% (w/v), usually from 0.1% to 5.0% (w/v) and often from 1.0% to 3.0% (w/v). The formulation is atomized and then enters into conditioning zone 12. The atomized formulation remains in the conditioning zone at relative humidity and temperature levels controlled in order to minimize evaporation and allow the droplet to reach thermodynamic equilibrium wherein the surface active component reaches its equilibrium orientation at the droplet surface. According to this aspect of the invention, droplets leaving the conditioning zone maintain a majority of the solvent and thus remain in liquid state as discussed in detail below.
According to this aspect of the present invention, the conditioning zone 12 is operated to minimize slow drying rates in order to facilitate increased diffusion of surface active components, such as proteins including insulin, to the droplet surface prior to formation of a dried particle “skin” as discussed above. Preferably, the temperature in conditioning zone 12 is lowered to minimize droplet drying in the period immediately following atomization. Initial droplet drying is limited by maintaining a high relative humidity environment within conditioning zone 12 at moderate temperatures. Temperatures in conditioning zone 12 are less than 60° C., preferably less than 50° C., and most preferably 25-50° C., and relative humidities of greater than 10%, preferably greater than 20%, and most preferably greater than 25% up to 100%, are maintained in conditioning zone 12. Droplet residence time in conditioning zone 12 according to this aspect of the invention is preferably from about 0.1 second to about 20 seconds, and more preferably is from about 2 seconds to about 5 seconds. However, the specific residence time may vary depending upon the particular formulation of feed stock 18. During the residence time, atomized formulation 18 preferably remains as liquid droplets. The residence time and conditions in the conditioning zone are maintained such that the atomized formulation exiting the conditioning zone 12 remains in liquid form.
The control of temperature, relative humidity of the air added to the conditioning zone 12 and control of the residence time within conditioning zone 12 facilitates the production of exemplary dry powders by suspending the atomized feed stock 18 in liquid form for a sufficient duration to encourage increased surface enrichment of surface active components. Conditioning of the liquid droplets at minimized drying rates compared to standard spray drying systems, such as those manufactured by Buchi, Niro, APV, Yamato Chemical Company, Okawara Kakoki Company and others, facilitates the droplets reaching thermodynamic equilibrium and diffusion of the surface active components to the droplet surface. In this manner, increased solids content in the atomized feed stock 18 can be processed while enriching the surface of the dry powders produced with surface active components. Accordingly, the dry powders so produced will have a higher emitted dose as compared to those produced in a standard Buchi or Niro spray drier (see
According to another aspect of the present invention directed to promoting amorphous to crystalline transformation of a spray dried formulation, the present invention provides for systems and methods for producing dry powders that are more stable than previously produced spray dried powders. Dry powders are preferably prepared by spray drying under conditions which often result in a mixed amorphous and crystalline powder. Bulk active agent, usually in crystalline form, is dissolved in a physiologically acceptable aqueous buffer, typically a citrate buffer having a pH range from about 2 to 9. Excipients may be added to the solution either in combination with the active agent or, where no active agents to be delivered, by themselves. The active agent is dissolved or suspended in a feed stock at a concentration typically from 0.01% (w/v) to 3% (w/v), usually from 0.2%-2.0% (w/v). It is to be understood that higher concentrations of active agent in the feed stock are within the scope of this invention. According to this aspect of the invention, the atomized formulation passes through at least one conditioning zone where temperature and relative humidity are controlled to provide amorphous to crystalline transformation of the formulation. According to this aspect of the invention, a majority of the liquid phase is evaporated from the atomized formulation prior to the final drying process such that the droplets entering the conditioning zone leave as partially dried particles. The partially dried particles retain sufficient moisture to act as a plasticizer and allow crystallization.
According to this aspect of the present invention, the partially dried particles are exposed to significantly increased relative humidities for prolonged residence times. According to this aspect of the invention, the temperature in conditioning zone 12 is within 35-120° C. the relative humidity in conditioning zone 12 is from 10-99% and the residence times are sufficient to allow amorphous-to-crystalline transformation to the extent where substantially no further crystallization occurs. Residence times are preferably from about one second to about 60 seconds, and more preferably is from about 2 seconds to about 20 seconds. However, the specific residence time may vary depending upon the particular formulation of feed stock 18. According to this aspect of the invention, partially dried particles exit conditioning zone 12 for further conditioning and/or final drying prior to collection. A majority of the liquid has been evaporated from the atomized formulation exiting the conditioning zone (or the last conditioning zone if multiple conditioning zones are used) prior to entering the final drying stage.
Referring back to FIG. 1., atomizer 20 operates as an inlet to conditioning zone 12. More specifically, feed stock formulation 18 is atomized by atomizer 20 and injected into conditioning zone 12, where it remains for a residence time as discussed above. For preparation of dry powders intended for inhalation, atomizer 20 produces droplets of less then 50μm, preferably less then 30μm, and most preferably less than 20μm in diameter. The time that atomized formulation 18 remains in conditioning zone 12 will vary according to the size, type and number of conditioning zone(s) 12. Preferably, conditioning zone 12 is configured to provide prolonged residence times of formulation 18 within conditioning zone 12 as compared to more rapid drying environments as discussed above.
System 10 can be used with a variety of feed stock 18 to form a dry powder 30. For example, feed stock 18 may include the active agents described above alone or in combination with any of the excipients described above or the feed stock 18 may include the excipients in the absence of active agents. One or more active agents and one or more excipients may be included in the feed stock formulation. The feed stock formulation may also include a solvent or cosolvent system. The solvents may be but are not limited to water, ethanol, acetone, isopropanaol, and methanol or combinations thereof.
In one embodiment, conditioning zone 12 comprises a plug flow conditioning zone 12, i.e. a first-in-first-out (FIFO) conditioning zone. Alternatively, conditioning zone 12 may be a back mixing conditioning zone 12, i.e. a recirculation conditioning zone. Further, more than one conditioning zone 12 may be used, including combinations of FIFO and recirculation (continuous stirred tank reactors) configurations. In this manner, the residence time can be controlled by controlling the time feed stock 18 spends in the desired temperature/relative humidity environment within conditioning zone 12. In one embodiment, conditioning zone 12 comprises an elongate insulated tube (such as a glass tube) having a length of about 2 meters to about 6 meters.
For embodiments using relative humidity controller 14, controller 14 allows enough humid air into the conditioning zone 12 to control its relative humidity to be at least 10%, preferably between about 20% and about 99%.
During operation, it is preferable to monitor the temperature within system 10. Estimates of effective temperature in relative humidity environments may be extimated from a differential scanning calorimetry (DSC) thermoactivity monitor (TAM), moisture sorption and x-ray powder diffraction. In one embodiment, temperatures in conditioning zone 12 range from between about 35° C. and about 110° C. depending upon the temperature/relative humidity combination selected for an individual run.
In one embodiment, feed stock formulations of known composition and solids content are pumped through a twin fluid atomizer 20 at liquid rates of between about 2.5 to about 100.0 milliliters per minute (ml/min), often between about 2.5 and 7.0 ml/min for a laboratory scale process and about 10.0 to 100.0 ml/min for a pilot commercial scale process. Atomizer 20 gas pressures and flow rates are between about 30 pounds per square inch (psig) to about 100 psi and about 0.5 to 1.3 scfm, respectively for a laboratory scale process and about 30-130 psig and 5-20 scfm for a pilot commercial scale process.
As depicted in
Dryer 24 can have a variety of configurations within the scope of the present invention. For example, in one embodiment dryer 24 is an insulated glass chamber or tube about 2 meters to about 6 meters in length. In one embodiment, drying zone 24 is an insulated glass chamber or tube about 1 meter to about 3 meters in length. In one particular embodiment for promoting crystallinity, particle residence time in drying zone 24 is about 0.4 seconds.
Total airflow through system 10 will vary depending upon system 10 configuration, collection device, and feed stock 18 being processed. In one example, total airflow is from about 19 scfm to about 23 scfm, taking into account atomizer air, feed stock 18 and air injected into conditioning zone 12 and heated air injected into dryer 24.
The dried formulation comprises dry powder 30 that is collected in a collector 28. Collector 28 may comprise, for example, a cyclone or baghouse collector. It will be appreciated by those skilled in the art that other collectors also may be used within the scope of the present invention. Dry powder 30 preferably has a mass median diameter (MMD) from between about 0.5 microns to about 10.0 microns and a mass median aerodynamic diameter (MMAD) between about 1 and 5 microns.
The present invention further provides exemplary methods of producing powdered formulations using system 10. As shown in
In one aspect, the conditioning zone is configured to suspend the atomized droplets for a residence time in the range from about 0.1 second to about 20 seconds. In another aspect, the conditioning zone includes an elongate insulated tube having a length of at least about 1 meter. By controlling, inter alia, the conditioning zone size and the feed stock formulation flow rate through the conditioning zone, the residence time can be controlled. In one aspect, the conditioning zone includes a tank capable of suspending the feed stock formulation. In one aspect, a humidifier is coupled to the conditioning zone to control the relative humidity therein. Similarly, in another aspect the system includes a temperature controller to control the temperature of the feed stock formulation upon entry into the conditioning zone. Controlling the formulation temperature and conditioning zone relative humidity assists in the diffusion of surface active particles, in part by maintaining the atomized formulation in the liquid state in the conditioning zone.
In one aspect, the formulation is suspended in conditioning zone 12 by passing the formulation through an elongate tube of the conditioning zone. Alternatively, the formulation is suspended by circulating the formulation in a tank of the conditioning zone. Hence, a variety of conditioning zones may be used within the scope of the present invention.
Turning now to
The use of multiple conditioning zones 52, 62-64 further enables the introduction of a variety of constituents into the flow of system 50 at appropriate locations. For example, in certain circumstances it may be desirable to introduce additional material such as solvents and solvent vapors into system 50. The introduction of such materials can occur at appropriate locations within system 50 and, more specifically, within desired conditioning zones 52, 62-64. As shown in
For example, multiple conditioning zones enable the sequential transformation and drying of constituents within formulation 58 by using cosolvents having different vapor pressures. In one embodiment, formulation 58 comprises an active agent and an excipient in a ethanol/water cosolvent. The evaporation of one cosolvent, for example the ethanol, causes solidification of components that were dissolved therein and results in the composition of the drying surface of the droplet to be enriched by those components. Next, evaporation of the remaining solvent, for example the water, results in the solidification of the ethanol soluble components. It will be appreciated by those skilled in the art that the use of water and ethanol is but one example of many cosolvents and multi-solvents that may be processed in system 50. For example, to the active agent ethanol/water cosolvent formulation 58 described above, a first material 70, comprising excess ethanol, and a second material 72, comprising heated dry air may be added. As previously described, the ethanol will evaporate first, and then the water will evaporate. However, since ethanol has been added in excess, the ethanol dissolved component will remain dissolved until after the second material 72 is added. The first solvent to evaporate will determine the surface of the drying particle since the components dissolved in that solvent will solidify first. The remaining solvent(s) evaporate through that drying skin and their dissolved components solidify on the inside of the drying skin.
In one embodiment, second material 72 or Nth material 74 comprise reagents capable of reacting with the surface components of the dispersed particles forming part of formulation 58. Such reagents could provide, for example, a coating of formulation 58. Such reagents may include, but are not limited to phospholipids, saccharin, leucine and cholesterol. Materials 70-74 further may include the heated gas streams containing sublimed materials. When added to the flow of gas and formulation 58 through conditioning zones 52, 62-64 sublimed material may be deposited as a solid coating around the particle.
As shown in
Turning now to
Similarly, as shown in
According to another embodiment of the present invention, any of the conditioning zones or dryers discussed above are operated at elevated pressure up to about 75 atmospheres, preferably up to 15 atmospheres, and most preferably up to about 10 atm. (150 psig). Operation at such elevated pressures provides the ability to de-couple absolute and relative humidity effects to modulate the drying kinetics and augment crystalline growth rate. Operation at elevated pressure also provides the ability to reduce the initial droplet size from the atomizer, reduce secondary atomization caused by internal droplet expansion due to dissolved gasses in the liquid, and increase the drying gas mass flow and hence powder throughput by an order of magnitude. It further provides an expanded range of gas mixing rates by the manipulation of gas jet density ratios.
For example, for a given temperature and absolute humidity, the relative humidity increases in proportion to the absolute pressure. Therefore, the relative humidity increases as the dryer system pressure increases for any given set of flow rates and temperature. The residual moisture in a dried powder is a function of formulation and the relative humidity it is in equilibrium with. This causes a significant increase in the moisture content of a powder in the dryer or collector or conditioning zone at several atmospheres pressure. Thus, decoupling of the absolute and relative humidities can be manipulated to increase the rate of crystallization for some formulations including those containing polyols such as mannitol.
The conditioning zones and/or dryer are pressurized by providing a source of pressurized gas such as air or nitrogen in communication with the conditioning zone and/or dryer. According to the invention, the pressure source is capable of providing a pressure of up to about 75 atmospheres within the conditioning zone and/or dryer, and preferably provides a pressure of up to about 15 and most preferably 10 atmospheres. The dryer may also be pressurized by providing the hot drying gas to the chamber under pressure.
In one particular aspect, the formulation includes at least about 1 percent solids content, and the dry particles have an emitted dose of at least about 60 percent. The present invention further includes dry powdered formulations produced according to the claimed methods.
The amount of active agent in the powdered formulation will be that amount necessary to deliver a therapeutically effective amount of the active agent to achieve the desired result. In practice, this will vary widely depending upon the particular agent, the severity of the condition, and the desired therapeutic effect. However, pulmonary delivery is generally practical for active agents that must be delivered in doses of from 0.001 mg/day to 100 mg/day, preferably 0.01 mg/day to 50 mg/day.
Powdered formulations suitable for use in the present invention include dry powders and particles suspended or dissolved within a propellant. The powdered formulations have a particle size selected to permit penetration into the alveoli of the lungs, that is, preferably less than 10 μm mass median diameter (MMD), preferably less than 7.5 μm, and most preferably less than 5 μm, and usually being in the range of 0.1 μm to 5 μm in diameter. The emitted dose (ED) of these powders is >30%, usually >40%, preferably >50% and often >60% and the aerosol particle size distribution is about 1.0-5.0 μm mass median aerodynamic diameter (MMAD), usually 1.5-4.5 μm MMAD and preferably 1.5-4.0 μm MMAD. These dry powders have a moisture content below about 10% by weight, usually below about 5% by weight, and preferably below about 3% by weight. Such powders are described in WO 95/24183, WO 96/32149, and WO 99/16419 which are incorporated by reference herein.
Dry powders are preferably prepared by spray drying. The active agent, excipient, or combination of active agent and excipient, is dissolved or suspended in a physiologically acceptable aqueous buffer, typically a citrate buffer having a pH range from about 2 to 9.
The dry powders may be delivered using Inhale Therapeutic Systems' dry powder inhaler as described in U.S. Pat. Nos. 5,740,794, 5,785,049, WO 96/09085 and in U.S. patent application Ser. Nos. 60/136,418 and 60/141,793 which are incorporated herein by reference. The dry powders may also be delivered using a metered dose inhaler as described by Laube et al in U.S. Pat. No. 5,320,094, which is incorporated by reference herein.
Other features and advantages of the invention will appear from the following description in which the preferred embodiment has been set forth in detail in conjunction with the accompanying drawings.
A multi-zonal spray dryer (MZD) in accordance with
The 60 percent insulin formulation was prepared by dissolving human zinc insulin, mannitol, sodium citrate, sodium hydroxide and glycine in deoinized water for a total solids concentration as listed in Table 1. The residence time was between 3.6 and 3.8 seconds and was designed to be of sufficient length to encourage surface diffusion of insulin protein molecules. The success of the example was determined by comparing emitted dose (ED) as a function of total solids. Results and operating conditions for four test runs using solutions containing 3% solids are provided in Table 1 below. The values are plotted as triangles on the graph shown in
The conditioning zone was an insulated glass tube about 2.1 meters in length and the drying zone was an insulated glass chamber about 0.6 meters in length. The conditioning zone temperature was monitored at a position immediately prior to the hot dry air inlet position. Temperature was nearly constant along the length of the conditioning zone (plus or minus about 2° C.). Monitored temperatures were used to calculate system relative humidity.
As shown above in Table 1, in one run (lot #97322) a 60 percent insulin formulation having about three percent solids was pumped into the conditioning zone at a rate of 5 ml/min. The conditioning zone was operated at about 50 degrees Celsius and about 45 percent relative humidity. The formulation remained in the conditioning zone for about 3.8 seconds before proceeding into the dryer. The now partially dried particles passed through the dryer in about 0.4 seconds, with the dryer operating at about 63 degrees Celsius and about 19 percent relative humidity. Dried particles were collected by a cyclone collector operating at about 60 degrees Celsius and about 19 percent relative humidity. An 85% yield was produced having an MMD of about 2.20 microns. The moisture content in the dry powder on a weight-to-weight percentage was about 2.8 percent.
As shown in
A multi-zonal spray dryer (MZD) in accordance with
Aqueous solutions containing 1.5% PTH (1-34 parathyroid hormone) and mannitol were dried in the MZD according to the following procedure and in the concentrations shown in Table 2. Water was pumped into Buchi 1 at a rate of between about 9 mL/min and about 22.5 mL/min. The inlet temperature of Buchi 1 was set between about 200 and 215° C. The drying airflow rate was about 10 standard cubic feet per min (scfm) to about 14 scfm. Atomizer gas pressure and flow rate were set to 35 psi and 0.7-1.0 scfm. The outlet temperature of the humid air from Buchi 1 ranged from about 52° C. to about 72° C.
The humid air from Buchi 1 was fed into Buchi 2. The active agent formulation feed solution was further atomized into Buchi 2 at a rate of about 2.5-7 mL/min. Atomizer pressure and flow rate were set to 80-100 psi and 1.0-1.3 scfm, respectively. The temperature of the atomized formulation that reached the conditioning zone was controlled by the volume and temperature of humid air added. The conditioning zone temperature was monitored at a position immediately after formulation atomization and the hot dry air inlet position. Temperature was nearly constant along the length of the conditioning zone (plus or minus about 2° C.). Monitored temperatures were used to calculate system relative humidity. Relative humidity calculations were based on the total amount of water entering the system, conditioning zone temperature, and assumed no leaks in the system.
From the conditioning zone, the formulations entered the drying zone and remained there from between about 0.4 and 0.5 seconds. The temperature of the drying zone was measured just before the cyclone collector and was between 40 and 80° C. The temperature of the dry air was between 90 and 180° C. A cyclone collector was used for powder collection. Table 1 shows the operating conditions and product characteristics of PTH/mannitol compositions prepared according to the invention. Table 3 shows emitted dose of the formulations.
The amount of crystallizable components were estimated by comparison of enthalpies of crystallization (ΔHc) obtained by differential scanning calorimetry (DSC) for particles prepared according to the invention (MZD) and those prepared by conventional spray drying systems.
Compared to a similar formulation processed through a Buchi or Niro system, the multi-zonal dryer of the present invention produced a much lower ΔHc (see Table 4). This indicates that a much higher level of crystallization occurred as a result of processing through the present invention. With increased crystallinity observed as a result of the present invention system and method, the resultant particles had a higher rate of amorphous-to-crystalline transformation during processing and thus will show a much greater storage stability than those processed in conventional manners.
ΔHc1
MZD of Example 5 was used to spray dry a 1.5% solution of 85% mannitol and 15% citrate. Operating conditions and product characteristics are shown in Table 5. Particle sizes (mass median diameter, MMD) were determined by centrifugal sedimentation (Horiba) and moisture contents were determined by Karl Fisher titration.
1particle fusion observed for these lots; n.d. = not determined
The emitted dose of the first lot stored for 5 months in a dry box showed less than a 10% drop as compared to greater than 25% drop for powders produced by conventional spray drying. This further indicates the stability of powders produced in the multizonal dryer.
The invention has now been described in detail. However, it will be appreciated that certain changes and modifications may be made. Therefore, the scope and content of this invention are not limited by the foregoing description rather the scope and content are to be defined by the following claims.
This application is a continuation-in-part of U.S. patent application Ser. No. 09/607,975, filed Jun. 30, 2000 now abandoned.
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| Child | 09733269 | US |
