Patent Grant
6916389
The present application relates to a process of forming particulate mixtures, and to an apparatus for performing the process.
Traditional processes for mixing particulates use organic solvents as a medium to mix and carry the particulates. These processes have the disadvantage that, once the particulates are mixed, the organic solvent must be removed from the mixed particulates. Where the particulates are energetic, as in the case of thermites, the process of solvent removal increases the risk of an undesirable or uncontrolled reaction. The use of organic solvents also increases the cost to capture, remove, and/or dispose of organic solvent, and the residue from an organic solvent can be undesirable for some applications. The removal of an organic solvent also requires an additional process step in large scale formulation and delivery schemes. Additional handling of energetic mixtures may increase the risk of an explosion. A process is needed for mixing ultrafine materials which avoids these problems while producing a well-mixed end product.
The present application provides a process for producing a mixture of particulates comprising: forming a dispersion comprising at least a first particulate material and a second particulate material dispersed in compressed gas under mixing conditions comprising a temperature and a pressure effective to maintain at least a portion of said compressed gas in liquid phase and comprising agitation conditions effective to produce substantially no agglomeration, said agitation conditions comprising sonication; and, separating said compressed gas from said mixed dispersion, producing said mixture of particulates.
The present application provides a process for producing mixtures of particulates. The process avoids the need to use an organic solvent. At least one dispersion is formed comprising at least two particulates dispersed in compressed gas. In a preferred embodiment, at least two separate dispersions are formed comprising different particulates.
The process is especially useful in processing reactive particulates, defined as particulates which react with one another exothermically. Where the particulates are reactive particulates, it is preferred to form a separate dispersion for each reactive particulate.
Where two or more dispersions are formed, the dispersion(s) are carried to a mixing zone. In a preferred embodiment, agglomeration is prevented using sonication. When the mixed particulates are exposed to reduced pressure, preferably slightly above atmospheric pressure, the compressed gas flashes off, leaving a dry, substantially uniform particulate product mixture.
The Particulates
The particulates processed using the method generally may have substantially any composition. Examples of suitable particulates include, but are not necessarily limited to reactive particulates, metals, ceramics, polymeric materials, oxides, nitrides, borides, silicides, phosphites, sulfides, oxynitrides, carbides, carbonitrides, intermetallic compounds, organometallic compounds, and nanocomposite materials. Cosolvents may be used to offer increased solubililty or desirable powder properties.
In a preferred embodiment, the particulates comprise reactive particulates. The reactive particulates comprise at least a first reactive particulate and a second reactive particulate which, when exposed to one another, react exothermically. In a preferred embodiment, the first reactive particulate comprises at least a primary component, preferably a metal, and the second reactive particulate comprises a reaction product between at least a major component, preferably a different metal, and at least one reactive element. The reaction product of the major component and the reactive element has a higher heat of formation than the reaction product of the primary component and the reactive element. Hence, the exothermic reaction. Suitable reactive particulates have a thermodynamic energy density of from about 10 kJ/cc to about 20 kJ/cc, preferably about 17 kJ/cc, and most preferably 17.1 kJ/cc.
Preferred reactive particulates undergo redox reactions. Preferred reactive particulates comprise a first metal particulate and an electron donating particulate. The electron donating particulate comprises a second metal and an electron carrying group, preferably an oxidizing agent. Upon mixing of the reactive particulates, the electron carrying group of the electron donating particulate reacts exothermically with the first metal to produce a particulate comprising the first metal and the electron carrying group, preferably an oxide of the first metal. In a preferred embodiment, as explained above, the reaction is exothermic, or produces heat.
In this preferred embodiment, suitable first metals include, but are not necessarily limited to, calcium, magnesium, sodium, lithium, aluminum, boron zirconium, titanium, yttrium, silicon, and zinc. Silicon is not a metal, but it is capable of acting like the other metals in this group, and is included as a “first metal” for convenience in terminology. A preferred first metal is aluminum, most preferably a nanoaluminum.
Suitable second metals include, but are not necessarily limited to copper, and molybdenum, titanium, iron, and magnesium. Preferably, the second metal is selected from the group consisting of copper and molybdenum, most preferably molybdenum.
Suitable electron donating particulates comprise an electron carrying group which forms stable products with both the first metal and with the second metal, but which reacts more readily at a lower heat of formation with the first metal. Examples of suitable electron carrying groups include, but are not necessarily limited to oxygen, halogens, and sulfur, preferably oxygen and halogens. More preferred electron carrying groups are selected from the group consisting of oxygen, chlorine, bromine and fluorine. A most preferred electron carrying group is oxygen.
Table 1 lists examples of reactive particulate pairs that are useful in the present application, as well as the products of their reactions and the estimated heats of each reaction per gram of reactant. The heats of the following reactions were calculated by subtracting the heats of formation of the reactants from those of the products.
As shown in Table 1, suitable reactive particulate pairs include, but are not necessarily limited to: CuClO4 and Al; Cu(NO3)2 and Al; CuO and Al; Fe2O3 and Al; S and Ca; CuO and Mg; TiF4 and Ca; S and Na; S and Mg; TiF4 and Li; MnO and Al; and, MoO3 and Al.
Preferred reactive pairs are superthermites, most preferably nanoaluminum and molybdenum trioxide (MoO3). Nanoaluminum has a thermodynamic energy density of 84 kJ/cc to complete oxidation with molecular oxygen. The superthermites have a thermodynamic energy density of from about 10 kJ/cc to about 20 kJ/cc, most preferably about 17.1 kJ/cc. Al/MoO3 typically has a flame temperature of about 3850° C. Methods of making such particulates are known in the art. Preferred particulates are commercially available from a number of sources, including but not necessarily limited to Nanophase Technologies, Inc., Argonide Corporation, Aveka, Inc., Technanogy, LLC, Climax Molybdenum GmbH, S, and Shepherd Chemical Company.
Generally, the electrical, chemical, mechanical, optical, and magnetic properties of the particulates are selectively controlled by engineering the size, morphology, and composition of the particulates using known techniques.
Suitable particulates have substantially any morphology. Suitable morphologies include, but are not necessarily limited to spherical, round, flat, dendritic, laminar, fibrous or branched shapes, while the term may also refer to an individual material or mixtures of materials. Typically, nanoaluminum is a spherical particulate and MoO3 is a rod-shaped particulate.
Suitable particulates have substantially any size as long as the size is sufficiently small to be dispersed in the compressed gas under the conditions of operation. In a preferred embodiment, the particulates have a maximum outer diameter of from about 5 nanometers (nm) to about 20 microns. In general, nanoscale particulates are preferred. Nanoscale particulates have a maximum outer diameter of 100 nm or less, preferably less than 100 nm. Most preferred nanoscale particulates have a maximum outer diameter of from about 40 nm to about 60 mm.
Where the reactive particulates are metals, the particulates sometimes tend to form oxide coatings. At least some oxide coating is desirable for some metals because an oxide coating tends to prevent agglomeration of the particulate mixture when collected and stored. The thickness of the oxide coating may be varied using known conditions. Typically, the oxide coating thickness is from about 1.5 nm to about 4.0 nm. Preferably, the oxide coating thickness on nanoaluminum particulates is from about 2.0 nm to about 2.5 nm. Thinner oxide coatings may be used, but they are not preferred because the resulting powder tends to be sensitive to shock, friction and exposure to air and water.
The surface area of the particulates will vary depending on their composition and intended use. Where the particulates are reactive particulates, the surface area of the first metal particulate is from about 15 m2/g to about 150 m2/g. The surface area of the electron donating particulate is from about 20 m2/g to about 60 m2/g. In superthermites, the specific surface area of the superthermite particulate product is from about 35 m2/g to about 49 m2/g. The aluminum content of superthermite mixtures ranges from about 40% to about 75% of the total mass.
Compressed Gas
The particulates are mixed using a solventless medium, preferably a compressed gas. Suitable compressed gases include, but are not necessarily limited to inert gases, hydrocarbons, fluorocarbons and carbon dioxide. A suitable inert gas is xenon. Preferred hydrocarbons have from about 1 to about 10 carbon atoms. A preferred compressed gas is carbon dioxide. The compressed gas need not be completely inert to the particulates as long as any interaction between the gas and the particulates does not affect the final composition of the product mixture.
Suitable compressed gases are effective to disperse the particulates in the gas and to form a dispersion of the particulates in the compressed gas. The dispersion preferably has fluid-like properties at temperatures and pressures of operation. The fluid-like properties permit the dispersion to flow from one location to another in the system.
Preferably, the compressed gas is maintained at a pressure above the vapor pressure of the gas to ensure a liquid phase throughout the entire volume. Suitable temperatures and pressures will vary with the particular gas and with the conditions of operation. Generally, the temperature required to maintain a liquid phase decreases as the pressure increases. Hence, at least one of the temperature or the pressure is sufficient to maintain the compressed gas in a liquid phase. In some instances, it may be desirable to maintain the compressed gas in the supercritical phase. Typically, supercritical conditions are not required where solubility is not an issue, such as when the particulates are inorganic. However, where the particulates are organic, supercritical conditions typically are desirable.
Compressed CO2 is a preferred compressed gas, especially for mixing energetic particulates, because (a) CO2 has a relatively low surface tension, which allows for favorable wetting of the particulates and thus for dispersion of the particulates in the CO2, and (b) CO2 provides for adequate absorption and discharge of the heat generated from the energy input for mixing energetic particulates. CO2 is not completely inert to the molybdenum oxide and aluminum particulates. In principle, CO2 can react with Al and aluminum nanopowder does burn in a CO2 atomosphere. However, the thermal buffering of the liquid CO2 is relied upon to prevent a sustained reaction.
Compressed CO2 provides fluid like properties, but is sufficiently nonflammable to maintain the combustion stability of energetic particulates under conditions of operation. For example, compressed CO2 does not tend to oxidize or reduce the energetic material under typical conditions of operation. Compressed CO2 also provides for thermal buffering of the energetic materials. Where the compressed gas is carbon dioxide, suitable temperatures for conducting the process are from about 0° C. to about 150° C., preferably from about 10° C. to about 32° C., more preferably about 31.1° C. or less, most preferably about 20° C. Suitable pressures are from about 70 bar to about 170 bar, preferably about 120 bar. At the conditions of operation, the compressed gas preferably has a density between that of a gas and that of a liquid, or from about 0.5 g/cm2 to about 1.1. g/cm, preferably about 1.0 g/cm2. At the conditions of operation, the fluid preferably has a viscosity of at least about 1.2×10−4 Pa-s.
Apparatus
In one embodiment, which is suitable for mixing non-reactive particulates, the apparatus comprises a source of compressed gas, at least one mixing zone, and a collector. This embodiment may use any suitable pressure vessel. The particulates are supplied to the pressure vessel and compressed gas is fed to the vessel with mixing, and preferably with sonication.
In a preferred embodiment, preferably for mixing reactive particulates, the apparatus comprises a source of compressed gas, at least two dispersion vessels, a mixing zone, and a collector.
Source of Compressed Gas
The source of compressed gas 1 preferably is a pressurized cylinder of a suitable gas. In
A chiller 4 is provided for the efficient pumping of carbon dioxide. Carbon dioxide from the pump 5 and/or the chiller 4 flows to a high pressure heat exchanger 5 and from there through pneumatic ball valves 6 and into the mixing vessels 7, 7a.
Dispersion Vessel
Suitable dispersion vessels provide for temperature and pressure control within the vessel. As seen in the apparatus of
The actual dispersion vessels may have substantially any configuration as long as the vessel(s) define an enclosure adapted to retain the dispersion at the pressures and temperatures of operation. In a preferred embodiment, the vessel is substantially cylindrical with minimal “dead spots.” Dead spots may be avoided by using substantially rounded bottoms. Persons of ordinary skill in the art will be able to adapt the size of the dispersion vessel depending upon the quantity of product to be produced over a particular time period.
For production on the scale of about 200 g/hr superthermites, effective dispersion vessels comprises a volume of from about 2 liters to about 10 liters, most preferably about 5 liters, with a depth to diameter ratio of about 0.5 to 1.5. At five liters, the dispersion vessels 7, 7a can be operated at lower solids loadings (i.e., more dilute), preferably at a solids loading of about 5% or less, most preferably about 2 wt. % or less. In a preferred embodiment, the dispersion vessels 7, 7a preferably are self-sealing having a “c” cup seal made of graphite reinforced Teflon®. and all tubing is preferably ⅛″ to ¼″ stainless steel tubing.
The pressure and temperature in the dispersion vessels are preferably maintained by sensors. A preferred material of construction for a dispersions vessels is 304 stainless steel. Preferably, the dispersion vessels are self-sealing having a “c” cup seal made of graphite reinforced Teflon®.
A preferred dispersion vessel comprises a source of agitation and a source of sonication. Mixing performed in high-pressure closed mixing vessels is commonly accomplished in one of two ways: (1) using mechanically driven stirring elements, or (2) using magnetically coupled stirring elements. Where the particulates are not reactive particulates, such as thermites, the source of agitation may include substantially any mechanical agitation device, including but not necessarily limited to high-speed impellers (turbine agitators and propeller agitators), paddle agitators, and homogenizers. Mechanical mixers are very powerful but have the liability of relying on seals and gaskets with limited lifetimes. Also, mechanical stirrers are subject to the buildup of significant static in the mixing vessel. The unacceptable risk associated with static buildup precludes the use of a mechanical stirrer when mixing thermites.
Preferred stirrers for use in mixing reactive particulates are magnetically coupled stirrers, which rely on a magnetic coupling between the motor 8 and impeller shaft 29 to produce the stirring motion. In the preferred embodiment shown in
The source of sonication may be substantially any sonochemical apparatus effective to assist in forming a dispersion and reducing agglomeration of the particulates. A preferred sonochemical apparatus includes an ultrasonic probe 9 having ultrasonic energy in the range of from about 100 Watts to about 750 Watts, most preferably about 200 Watts. Preferably, the probe is mounted on the lid of the mixing vessel and sealed using an o-ring.
In order to form effective dispersions, the particulates must be properly wetted, physically separated, and stabilized. When the particulates are wetted while sonicating, air is released from the bulk packing of the particulates. Once the air is released, the agitator separates and distributes the particulates throughout the compressed gas. Once an effective dispersion is formed, the ultrasonic energy prevents reagglomeration of the particulates.
The tubing used to feed the dispersions from the dispersion vessels 7,7a to the mixing zone preferably is fitted to maintain a pressure of from about 90 bar to about 440 bar, most preferably about 330 bar. A preferred tubing is ¼″ stainless steel having a wall thickness of about 0.049″.
Mixing Zone
Each mixing vessel 7, 7a is in fluid communication with a mixing zone 14, preferably via suitable chemically resistant high performance tubing, most preferably ¼″ stainless steel tubing 19. To maintain the rate of mixing and to control unwanted or surplus mixing of the dispersions, a preferred apparatus incorporates three levels of control: (1) high torque ball valves 12a effective to control the rate of delivery of dispersions from the mixing vessels 7, 7a to the mixing zone 14 at pressures of from about 1 to about 3000, preferably about 2500; (2) check valves 12b, located downstream from the ball valves 12a, effective to minimize plugging of the high torque ball valves 12a by preventing flow of dispersions in reverse direction (backflow) back past the ball valves 12a; and (3) a “pressure bridge” 11 that connects and equalizes the pressure between the mixing vessels 7, 7a by allowing CO2 to pass between the bridge. In the embodiment shown in
Where the particulates are not reactive particulates, the mixing zone 14 may comprise a mixing vessel comprising substantially any configuration as long as the mixing vessel defines an enclosure which retains the dispersion at the pressures and temperatures of operation and which permits adequate mixing of the dispersions. Suitable mixing vessels include, but are not necessarily limited to, pan mixers, horizontal trough mixers, shearing devices, and in-line mixers. Preferred mixing vessels include static or motionless mixers, preferably comprising ¼″ stainless steel tubing. Suitable static mixers are of cylindrical length and incorporate mixing elements, preferably fins, obstructions, or channels mounted in the mixing vessel. Suitable mixing of the dispersions is achieved by producing multiple flow patterns of the particulates in the compressed gas. Preferably, mixing is accomplished by the displacement and distortion, cutting and twisting, acceleration and retardation, and separation and reuniting of the nanoscale particulates in the compressed gas. The volume of the mixing vessel will vary depending upon the particulates mixed, the compressed gas, and the temperatures and pressures of operation, among other things. The contact interval, the mechanical intensity inside the mixer, the composition of particulates, the size of particulates, and viscosity of the compressed gas, also will vary and influence the quality of the resulting mixture.
Where the particulates are reactive, the mixing vessel preferably minimizes the contact interval and, when combined with the buffering effect of the solvent, prevents redox reactions between the reactive particulates. A preferred mixing vessel for reactive particulates is an unobstructed Y-type fitting 13. A Y-type fitting 13 also minimizes plugging compared to that found using right angle fittings. A most preferred mixing vessel for reactive particulates is a Y-type fitting having opposed angles of from about 100° to about 150°; most preferably about 120°.
A needle valve, preferably a low impedance needle valve and a control valve 15, preferably a manual control valve for controlling the outlet flow rate of the mixture are provided between the mixing zone 14 and a collection vessel 22. The control valve 15 serves as the backpressure regulator. Preferred control valves comprise high strength SS seats, preferably SS 316, and pistons capable of controlling mixtures with flow rates of from about 50 g/min to about 350 g/min, preferably 200 g/min. Preferred valves 15 are bellows valves and are effective at temperatures of from about −10° C. to about 300° C., preferably about 20° C.; and at the pressures described.
The collection vessel 22 preferably comprises a nozzle 16 for feeding product to the collection vessel 22. The apparatus also preferably comprises a shield 34, preferably a polycarbonate shield on all four sides and top of the apparatus; and an automated control system 21 located outside of the shield.
Collection Vessel
The particulates exiting the system achieve a very high velocity and are difficult to control. A preferred collection vessel is designed to capture these high-pressure particulate product streams as they are delivered through the nozzle 16. Prior to being fed to a collection vessel 22, the liquid CO2 preferably is heated with a vaporizer 32 at about 50° C. to about 150° C., preferably about 110° C., to insure that all of the liquid CO2 is converted to gas during depressurization. A preferred vaporizer can effectively heat the liquid CO2 at flow rates from about 100 g/min to about 350 g/min, preferably about 200 g/min, and at the pressures previously described.
Referring to
The delivery of fine particulates from a high pressure CO2 stream can cause a sizeable static charge to accumulate. Where the product is superthermites, which requires a static free environment, proper grounding, static control and static monitoring are required throughout the system.
In a first embodiment, ultrafine particulates, preferably superthermites, most preferably nanoaluminum powder and MoO3 powder are added to individual mixing vessels in a ratio of about 1.5 to 2 parts MoO3 to 1 part nanoaluminum powder. The nanoaluminum powder is dispersed in a first mixing vessel with compressed CO2. The MoO3 powder is dispersed in a second mixing vessel with compressed CO2. Suitable stirring and sonication produces dispersions with substantially no agglomeration of the nanoscale particulates. By “substantially no agglomeration” is meant that discrete particle sizes are achieved down to the minimum base particle/hard aggregate level, i.e., no bonds weaker than covalent or ionic bonds hold individual particles together.
Once an effective dispersion of each reactive particulate is formed, the dispersions flow to the mixing zone, preferably at a pressure of from about 120 bar to about 170 bar, more preferably about 120 bar. The dispersions enter the mixing zone, preferably a Y-shaped fitting, at a steady state velocity of from about 7 m/s to about 700 m/s, preferably about 70 m/s.
Upon entering the mixing zone, the streams preferably contact each other and split, recombine and split again continuously to achieve adequate mixing. Preferably, the contact time lasts less than about 2 seconds. At dispersion levels of about 20 g/l, the amount of particulates being mixed is relatively small compared to the amount of compressed CO2 being fed through the mixer. The short contact interval provided by a preferred static mixer maximizes mixing efficiency while also maintaining the combustion stability of energetic particulates, such as superthermites. Resulting particulate sizes in the superthermite mixtures are substantially the same as the original particle sizes. Once the dispersions are properly mixed, the mixture is collected and brought to atmospheric pressure wherein the compressed CO2 flashes off, leaving a relatively dry, well-mixed product.
Venting directly from the operating pressure of about 1000 psi to ambient conditions causes CO2 expansion and may form dry ice, which may condense on the product after collection. Preferably, collection of the high-pressure mixture comprises a two-stage pressure drop which allows the product to be collected at an intermediate pressure of 25 bar, down from the operating pressure of 1000 psi. Depressurization from 25 bar allows for venting off of the CO2 without dry ice formation at the collection source. Eliminating dry ice formation helps insure the collection of a well-mixed dry end product. Suitably, the mixing process is a continuous or semi-continuous operation producing a powder product on the scale of up to about 25 bar.
In a second embodiment, which is used to mix substantially non-reactive particulates, at least two particulates are added to a single dispersion vessel (not shown) to form a mixed dispersion under stirring and sonication conditions. The particulates may be added to the dispersion vessel in any preferred amount and in any preferred ratio. A compressed gas, preferably compressed CO2, is added to the dispersion vessel in an amount effective for desired mixing and/or dispersion of the particulates. The compressed CO2 has the effect of minimizing the agglomerating ability of particulates under sonication. At temperatures ranging from about 10° C. to about 40° C., compressed CO2 will comprise a density of about 1 g/mL. The rate of dispersion is directly correlated to the density of the compressed CO2, wherein the density of the compressed CO2 decreases with increasing temperature at a given pressure. Preferably, the compressed CO2 is in the liquid state for effective dispersion of the nanoscale particulates. In the above temperature range, the heat generated through sonication of the nanoscale particulates is absorbed or discharged by the compressed CO2. Sonication at about 200 Watts allows for adequate wetting of the nanoscale particulates in the compressed CO2.
Once wet, the particulates disperse throughout the entire mixing vessel under turbulent flow. Sonication allows for the production of a powder mixture comprising a level of mechanical rearrangement not obtained by turbulent flow alone. Once mixing is completed, the mixture is exposed to reduced atmospheric pressure to permit the compressed gas to flash off, leaving a well-mixed, dry product. The system is flushed with CO2 to remove any remaining particulates from the system.
The invention will be better understood with reference to the following example, which is illustrative only and not intended to limit the present invention to a particular embodiment.
An experiment was run in a mixing vessel to test the effect of dense phase CO2 on aluminum nanopowder. The reductive potential of aluminum is well known and is sufficient to reduce water into hydrogen gas and oxygen or carbon dioxide into carbon and oxygen. Control experiments were run to verify that no reaction would occur between aluminum nanopowder and CO2 at normal operating conditions. A small powder (35 nm) with a thin oxide shell (2.0 nm), 61.0% aluminum content, was selected to represent an extreme test of the reaction. Typically, powders of this quality are the most reactive and have been shown to reduce water the most readily in previous experiments.
Standard mixing conditions were simulated in a single mixing vessel by adding 2.5 grams of aluminum powder from Lot # Al1A to the bottom of the vessel and sealing the material inside. The vessel was pressurized to 70 bar and stirring began at a rate corresponding to 1.4 bar inlet pressure on the pneumatic stirrer. Sonication was performed throughout the entire mixing experiment at 22% output. The vessel held pressure for the duration of the four hours mixing experiment and the contents were then vented through the manual relief valve (⅛″ stainless steel tubing with a HiP valve as the outlet).
The results in
The performance of the mixer was tested by mixing aluminum nanopowder with nanometer sized Al2O3 (alumina). The nano-alumina (purchased from Nanophase Inc.) acted as a surrogate for MoO3 in all mixing experiments. The advantages of nano-alumina as a surrogate for molybdenum trioxide included: the lack of reactivity between Al and Al2O3; the availability and low cost of high quality nanometer-sized alumina; alumina's inert properties (TGA, in CO2, reactivity with Al etc.); and the contrast in color between Al2O3 (white) and aluminum nanopowder (black). Shortcomings of alumina as a surrogate for nanoscale MoO3 include: the inability to measure performance data for the mixtures; the inability to distinguish Al and Al2O3 by electron microscopy; and the difference in shape between alumina (spherical particles) and MoO3 (rod like particles).
The powder was delivered to the collection chamber and analyzed. The TGA and BET are shown in the following Table:
This example illustrates the mixing of nanoaluminum powder and molybdenum trioxide powder. In a continuous operation at a collection rate of 200 g/hr, a first five-liter stainless steel mixing vessel is pre-filled with 140 g of nanoaluminum powder and a second five-liter stainless steel mixing vessel is pre-filled with 260 g of molybdenum trioxide powder. Each mixing vessel is sealed and a high-pressure piston pump delivers compressed CO2 from a storage cylinder to each mixing vessel at a pressure of 1000 psi. Once pressurized, each powder solution is vigorously mixed with a magnetically coupled mechanical stirrer within each pressure vessel. Each powder solution is simultaneously exposed to ultrasonic energy at 200 Watts to disperse and wet the particulates within the compressed CO2. Once the solutions are thoroughly dispersed, each solution is fed to a static mixer through ⅛″ stainless steel tubing. The dispersions are subjected to multiple flow patterns within the static mixer resulting in a short contact interval between the two dispersions forming superthermites. Once mixed, the superthermites are fed to a collection vessel. The collection vessel is depressurized to atmospheric conditions wherein the high vapor pressure CO2 flashes off resulting in a dry, well-mixed powder product. The resulting superthermite powder includes a molybdenum metal and aluminum oxide formulation generating over 17 kJ/cm3 of heat. The resulting particle size is approximately 50 nm with an outer oxide shell of approximately 2.0 nm.
This example illustrates the mixing of nanoaluminum powder and copper oxide powder. In a continuous operation at a collection rate of 200 g/hr, a first five-liter stainless steel mixing vessel is pre-filled with 140 g of nanoaluminum powder and a second five-liter stainless steel mixing vessel is pre-filled with 260 g of copper oxide powder. Following the procedure of Example 3, the resulting powder includes a copper and aluminum oxide formulation generating over 21 kJ/cm3 of heat. The resulting particle size is approximately 50 nm with an outer oxide shell of approximately 2.0 nm.
Persons of ordinary skill in the art will recognize that many modifications may be made to the present invention without departing from the spirit and scope of the present invention. The embodiment described herein is meant to be illustrative only and should not be taken as limiting the invention, which is defined in the following claims.
The U.S. government has certain rights in this invention pursuant to contract number DAAE30-01-1098 from the U.S. Army (TACOM-ARDEC), Picatinny Arsenal, N.J.
| Number | Name | Date | Kind |
|---|---|---|---|
| 4151075 | Othmer | Apr 1979 | A |
| 4483276 | Lomas et al. | Nov 1984 | A |
| 4734227 | Smith | Mar 1988 | A |
| 5884138 | Chalasani et al. | Mar 1999 | A |
| 5935514 | Ford, Jr. et al. | Aug 1999 | A |
| 6113795 | Subramaniam et al. | Sep 2000 | A |
| Number | Date | Country |
|---|---|---|
| 0105980 | Apr 1984 | EP |
| 0105980 | Apr 1984 | EP |
| 0920921 | Jun 1999 | EP |
| WO0029096 | May 2000 | WO |
| Number | Date | Country | |
|---|---|---|---|
| 20040031754 A1 | Feb 2004 | US |
