Patent Grant
7192467
The invention generally pertains to molybdenum, and more specifically, to molybdenum metal and production thereof.
Molybdenum (Mo) is a silvery or platinum colored metallic chemical element that is hard, malleable, ductile, and has a high melting point, among other desirable properties. Thus, molybdenum is commonly used as an additive for metal alloys to impart various properties thereto, and hence to enhance the properties of the metal alloy. For example, molybdenum may be used as a hardening agent, especially for high-temperature applications. However, molybdenum does not naturally occur in pure form. Instead, molybdenum occurs in a combined state. For example, molybdenum ore typically exists as molybdenite (molybdenum disulfide, MoS2). The molybdenum ore may then be processed by roasting it to form molybdic oxide, MoO3.
Molybdic oxide may be directly combined with other metals, such as steel and iron, to form alloys thereof, or molybdic oxide may be further processed to form pure molybdenum. In its pure state, molybdenum metal is tough and ductile and is characterized by moderate hardness, high thermal conductivity, high resistance to corrosion, and a low expansion coefficient. Therefore, molybdenum metal may be used for electrodes in electrically heated glass furnaces, nuclear energy applications, and for casting parts used in missiles, rockets, and aircraft. Molybdenum metal may also be used as a filament material in various electrical applications that are subject to high temperatures, such as X-ray tubes, electronic tubes, and electric furnaces. In addition, molybdenum metal is often used as a catalyst (e.g., in petroleum refining), among other uses or applications.
Processes have been developed for producing molybdenum metal in its pure state. Such a process involves a two-step process. In the first step, a mixture of molybdenum tri-oxide and ammonium di-molybdate is introduced to a first furnace (e.g., a rotary kiln or fluidized bed furnace) to yield molybdenum dioxide, as expressed by the following formula:
2(NH4)MoO4+2MoO3→3MoO2+4H2O+N2(g) (1)
In the second step, the molybdenum dioxide is transferred to a second furnace (e.g., a pusher furnace) and reacted with hydrogen to form molybdenum powder, for example, as expressed by the following formula:
MoO2+2H2(g)→Mo+2H2O (2)
However, this process for producing molybdenum metal requires multiple batch steps, which is labor intensive, slows production, and increases production costs. In addition, this process requires separate processing equipment (e.g., furnaces) for each step, which increases capital costs and maintenance costs. Furthermore, these processes only produce molybdenum metal having a surface area of about 0.8 square meters per gram (m2/g), or less, and may vary widely in size.
Novel forms of molybdenum metal may be characterized by a surface area of substantially about 2.1 m2/g to substantially about 4.1 m2/g according to BET analysis. Other novel forms of molybdenum metal may be characterized by a substantially uniform size as detected by scanning electron microscopy.
Illustrative and presently preferred embodiments of the invention are illustrated in the drawings, in which:
Apparatus 10 (
According to the teachings of the invention, novel forms of molybdenum metal 12 may be characterized as having a surface area to mass ratio of substantially 2.5 m2/g according to BET analysis. Also according to the teachings of the invention, novel forms of molybdenum metal 12 may be characterized as substantially uniform in size (see
Novel forms of molybdenum metal characterized according to embodiments of the invention are advantageous in and of themselves for various uses or applications. For example, molybdenum metal that is characterized by a relatively high surface area to mass ratio is particularly advantageous when used as a catalyst. That is, less molybdenum metal is required on a mass basis when used as a catalyst to achieve similar or even better results than when molybdenum metal characterized by a smaller surface area to mass ratio is used as a catalyst in the same reactions. Also for example, molybdenum metal characterized by a relatively large surface area to mass ratio and/or a relatively uniform size may be advantageous for use as a sintering agent. That is, the molybdenum-sintering agent has a higher bonding area than conventional molybdenum sintering agents, thereby enhancing the resulting sinter. These novel forms of molybdenum metal may also be particularly advantageous for other uses or applications not specifically called out herein.
Also according to the teachings of the invention, embodiments of apparatus 10 for producing molybdenum metal 12 are disclosed. Apparatus 10 may comprise a furnace 16 having at least two, and preferably three heating zones 20, 21, and 22. A process tube 34 preferably extends through the furnace 16 so that a precursor material 14 (e.g., MoO3) may be introduced into the process tube 34 and moved through the heating zones of the furnace 16, such as is illustrated by arrow 26 shown in
Apparatus 10 may be operated as follows for producing molybdenum metal 12 from a precursor material 14 (e.g., molybdic oxide (MoO3)). As one step in the process, the precursor material is heated to a first temperature (e.g., in Heating Zone 1 of furnace 16) in the presence of a reducing gas 64. The first temperature is increased at least once (e.g., in Heating Zone 3, and also preferably in Heating Zone 2) to reduce the precursor material 14 and form the molybdenum metal 12.
Accordingly, molybdenum metal 12 may be produced in a continuous manner. Preferably, no intermediate handling is required during production of the molybdenum metal product 12. That is, the precursor material 14 is preferably fed into a product inlet end 15 of furnace 16, and the molybdenum metal product 12 is removed from a product discharge end 17 of furnace 16. Thus, for example, the intermediate product 30 (
Having generally described novel forms of molybdenum metal and apparatus and methods for production thereof, as well as some of the more significant features and advantages of the invention, the various embodiments of the invention will now be described in further detail.
A preferred embodiment of apparatus 10 is shown in
Before beginning a more detailed description of preferred embodiments of apparatus 10, however, it should be clear that other embodiments of the furnace 16 and the transfer system 32 are contemplated as being within the scope of the invention. The furnace may comprise any suitable furnace or design thereof, and is not limited to the rotating tube furnace 16, shown in
Turning now to a detailed description of preferred embodiments of apparatus 10, a feed system 36 may be operatively associated with the process tube 34. The feed system 36 may continuously introduce the precursor material 14 into the furnace 16. In addition, the feed system 36 may also introduce the precursor material 14 into the furnace 16 at a constant rate. For example, the feed system 36 may comprise a loss-in-weight feed system for continuously introducing the precursor material 14 into one end of the process tube 34 at a constant rate.
It is understood that according to other embodiments of the invention, the precursor material 14 may be otherwise introduced into the furnace 16. For example, the feed system 36 may feed the precursor material 14 into the furnace 16 on an intermittent basis or in batch. Other designs for the feed system 36 are also contemplated as being within the scope of the invention and may differ depending upon design considerations and process parameters, such as the desired rate of production of the molybdenum metal product 12.
In any event, the precursor material 14 is preferably introduced into the furnace 16 by feeding it into the process tube 34. The process tube 34 preferably extends through a chamber 44 that is formed within the furnace 16. The process tube 34 may be positioned within the chamber 44 so as to extend substantially through each of the heating zones 20, 21, and 22 of the furnace 16. Preferably, the process tube 34 extends in approximately equal portions through each of the heating zones 20, although this is not required. In addition, the process tube 34 may further extend beyond the heating zones 20, 21, and 22 of the furnace 16 and through a cooling zone 23.
According to preferred embodiments of the invention, the process tube 34 is a gas-tight, high temperature (HT) alloy process tube. The process tube 34 also preferably has a nominal external diameter of about 16.5 centimeters (cm) (about 6.5 inches (in)), a nominal internal diameter of about 15.2 cm (about 6 in), and is about 305 cm (about 120 in) long. Preferably, about 50.8 cm (about 20 in) segments of the process tube 34 each extend through each of the three heating zones 20, 21, and 22 of the furnace 16, and the remaining approximately 152.4 cm (60 in) of the process tube 34 extend through the cooling zone 23.
In other embodiments of the invention, however, the process tube 34 may be manufactured from any suitable material. In addition, the process tube 34 need not extend equally through each of the heating zones 20, 21, and 22 and/or the cooling zone 23. Likewise, the process tube 34 may be any suitable length and diameter. The precise design of the process tube 34 will depend instead on design considerations, such as the feed rate of the precursor material 14, the desired production rate of the molybdenum metal product 12, the temperature for each heating zone 20, 21, and 22, among other design considerations readily apparent to one skilled in the art based on the teachings of the invention.
The process tube 34 is preferably rotated within the chamber 44 of the furnace 16. For example, the transfer system 32 may comprise a suitable drive assembly operatively associated with the process tube 34. The drive assembly may be operated to rotate the process tube 34 in either a clockwise or counter-clockwise direction, as illustrated by arrow 42 in
The rotation 42 of the process tube 34 may facilitate movement of the precursor material 14 and the intermediate material 30 (
In addition, the process tube 34 is preferably positioned at an incline 40 within the chamber 44 of the furnace 16. One embodiment for inclining the process tube 34 is illustrated in
Although preferred embodiments for adjusting the incline 40 of the process tube 34 are shown and described herein with respect to apparatus 10 in
In any event, the incline 40 of the process tube 34 may also facilitate movement of the precursor material 14 and intermediate material 30 through the heating zones 20, 21, and 22 of the furnace 16, and through the cooling zone 23. In addition, the incline 40 of the process tube 34 may facilitate mixing of the precursor material 14 and intermediate material 30 within the process tube 34, and expose the same for contact with the process gas 62 to enhance the reactions between the precursor material 14 and/or the intermediate material 30 and the process gas 62. Indeed, the combination of the rotation 42 and the incline 40 of the process tube 34 may further enhance the reactions for forming molybdenum metal product 12.
As previously discussed, the furnace 16 preferably comprises a chamber 44 formed therein. The chamber 44 defines a number of controlled temperature zones surrounding the process tube 34 within the furnace 16. In one embodiment, three temperature zones 20, 21, and 22 are defined by refractory dams 46 and 47. The refractory dams 46 and 47 are preferably closely spaced to the process tube 34 so as to discourage the formation of convection currents between the temperature zones. In one embodiment, for example, the refractory dams 46 and 47 come to within approximately 1.3 to 1.9 cm (0.5 to 0.75 in) from the process tube 34 to define three heating zones 20, 21, and 22 in the furnace 16. In any event, each of the three heating zones are preferably respectively maintained at the desired temperatures within the chamber 44 of the furnace 16. And hence, each segment of the process tube 34 is also maintained at the desired temperature, as shown in more detail in
Preferably, the chamber 44 of the furnace 16 defines the three heating zones 20, 21, and 22 shown and described herein with respect to
It is understood that the heating zones 20, 21, and 22 may be defined in any suitable manner. For example, the heating zones 20, 21, and 22 may be defined by baffles (not shown), by a number of separate chambers (not shown), etc. Indeed, the heating zones 20, 21, and 22 need not necessarily be defined by refractory dams 46, 47, or the like. As an example, the process tube 34 may extend through separate, consecutive furnaces (not shown). As another example, the chamber 44 of the furnace 16 may be open and a temperature gradient may be generated within the chamber 44 to extend from one end of the chamber 44 to the opposite end of the chamber 44 using separate heating elements spaced along the length thereof.
It is also understood that more than three heating zones (not shown) may be defined within the furnace 16. According to yet other embodiments of the invention, fewer than three heating zones (also not shown) may be defined in the furnace 16. Still other embodiments will occur to those skilled in the art based on the teachings of the invention and are also contemplated as being within the scope of the invention.
The furnace 16 may be maintained at the desired temperatures using suitable temperature control means. In preferred embodiments, each of the heating zones 20, 21, and 22 of the furnace 16 are respectively maintained at the desired temperatures using suitable heat sources, temperature control, and over-temperature protection. For example, the heat source may comprise independently controlled heating elements 50, 51, and 52 positioned within each of the heating zones 20, 21, and 22 of the furnace 16, and linked to suitable control circuitry.
In one preferred embodiment, the temperature is regulated within the three heating zones 20, 21, and 22 of the furnace 16 by twenty-eight silicon-carbide, electrical-resistance heating elements. The heating elements are linked to three Honeywell UDC3000 Microprocessor Temperature Controllers (i.e., one controller for each of the three heating zones 20, 21, and 22) for setting and controlling the temperature thereof. In addition, three Honeywell UDC2000 Microprocessor Temperature Limiters (i.e., also one controller for each of the three heating zones 20, 21, and 22) are provided for over-temperature protection. It is understood, however, that any suitable temperature regulating means may be used to set and maintain the desired temperature within the furnace 16. For example, the heating elements need not necessarily be electronically controlled and may instead be manually controlled.
Although each of the heating zones are preferably maintained at relatively uniform temperatures, respectively, it is apparent that conduction and convection of heat may cause a temperature gradient to be established within one or more of the heating zones 20, 21, and 22. For example, although the refractory dams 46, 47 are spaced approximately 1.3 to 1.9 cm (0.5 to 0.75 in) from the process tube 34 to reduce or minimize the transfer or exchange of heat between the heating zones 20, 21, and 22, some heat exchange may still occur therebetween. Also for example, the process tube 34 and/or the precursor material and/or intermediate material may also conduct heat between the heating zones 20, 21, and 22. Therefore, the temperature measured at various points within each of the heating zones 20, 21, and 22 may be several degrees cooler or several degrees warmer (e.g., by about 50 to 100° C.) than the center of the heating zones 20, 21, and 22. Other designs are also contemplated to further reduce the occurrence of these temperature gradients, such as sealing the refractory dams 46, 47 about the process tube 34. In any event, the temperature settings for each of the heating zones 20, 21, and 22 are preferably measured in the center of each of the heating zones 20, 21, and 22 to more accurately maintain the desired temperature therein.
Preferably, the cooling zone (illustrated by outline 23 in
The process gas 62 is preferably introduced into the furnace 16 for reaction with the precursor material 14 and the intermediate product 30. According to preferred embodiments of the invention, the process gas 62 may comprise a reducing gas 64 and an inert carrier gas 65. The reducing gas 64 and the inert carrier gas 65 may be stored in separate gas cylinders near the far end of the process tube 34, as shown in
According to embodiments of the invention, the reducing gas 64 may be hydrogen gas, and the inert carrier gas 65 may be nitrogen gas. However, it is understood that any suitable reducing gas 64, or mixture thereof, may be used according to the teachings of the invention. Likewise, the inert carrier gas 65 may be any suitable inert gas or mixture of gases. The composition of the process gas 62 will depend on design considerations, such as the cost and availability of the gases, safety issues, and desired rate of production, among other considerations.
Preferably, the process gas 62 is introduced into the process tube 34 and directed through the cooling zone 23 and through each of the heating zones 20, 21, and 22, in a direction opposite (i.e., counter-current, as illustrated by arrow 28) to the direction 26 that the precursor material 14 is moved through each of the heating zones 20, 21, and 22 of the furnace 16, and through the cooling zone 23. Directing the process gas 62 through the furnace 16 in a direction that is opposite or counter-current 28 to the direction 26 that the precursor material 14 is moving through the furnace 16 may increase the rate of the reaction of the precursor material 14 and the intermediate material 30 (
The unreacted process gas 62 that flows upstream toward the entry of the process tube 34 thus comprises a lower concentration of the reducing gas 64. However, presumably a larger surface area of unreacted precursor material 14 is available at or near the entry of the process tube 34. As such, smaller concentrations of reducing gas 64 may be required to react with the precursor material 14 at or near the entry of the process tube 34. In addition, introducing the process gas 62 in such a manner may enhance the efficiency with which the reducing gas 64 is consumed by the reaction therebetween, for reasons similar to those just explained.
It is understood that in other embodiments of the invention the process gas 62 may be introduced in any other suitable manner. For example, the process gas 62 may be introduced through multiple injection sites (not shown) along the length of the process tube 34. Or for example, the process gas 62 may be premixed and stored in its combined state in one or more gas cylinders for introduction into the furnace 16. These are merely exemplary embodiments, and still other embodiments are also contemplated as being within the scope of the invention.
The process gas 62 may also be used to maintain the internal or reaction portion of the process tube 34 at a substantially constant pressure, as is desired according to preferred embodiments of the invention. Indeed, according to one preferred embodiment of the invention, the process tube 34 is maintained at about 8.9 to 14 cm (about 3.5 to 5.5 in) of water pressure (gauge). The process tube 34 may be maintained at a constant pressure, according to one embodiment of the invention, by introducing the process gas 62 at a predetermined rate, or pressure, into the process tube 34, and discharging the unreacted process gas 62 at a predetermined rate, or pressure, therefrom to establish the desired equilibrium pressure within the process tube 34.
Preferably, the process gas 62 (i.e., the inert carrier gas 65 and the unreacted reducing gas 64) is discharged from the process tube 34 through a scrubber 66 at or near the entry of the process tube 34 to maintain the process tube 34 at a substantially constant pressure. The scrubber 66 may comprise a dry pot 67, a wet pot 68, and a flare 69. The dry pot 67 is preferably provided upstream of the wet pot 68 for collecting any dry material that may be discharged from the process tube 34 to minimize contamination of the wet pot 68. The process gas 62 is discharged through the dry pot 67 and into water contained in the wet pot 68. The depth of the water that the process gas 62 is discharged into within the wet pot 68 controls the pressure of the process tube 34. Any excess gas may be burned at the flare 69.
Other embodiments for maintaining the process tube 34 at a substantially constant pressure are also contemplated as being within the scope of the invention. For example, a discharge aperture (not shown) may be formed within a wall 74 (
The various components of apparatus 10, such as are shown in
The Harper Rotating Tube Furnace features a high-heat chamber with a maximum temperature rating of 1450° C. A number of refractory dams divide the high-heat chamber into three independent temperature control zones. The three temperature control zones feature discrete temperature control using twenty-eight silicon-carbide electrical resistance heating elements. Thermocouplers are provided at the center of each control zone along the centerline of the roof of the furnace. The temperature control zones are regulated by three Honeywell UDC3000 Microprocessor Temperature Controllers, and by three Honeywell UDC2000 Microprocessor Temperature Limiters, each commercially available from Honeywell International, Inc. (Morristown, N.J.).
The Harper Rotating Tube Furnace also features a gas-tight, high temperature alloy process tube, having a maximum rating of 1100° C. The process tube has a nominal internal diameter of 15.2 cm (6.0 in), nominal external ends diameter of 16.5 cm (6.5 in), and an overall length of 305 cm (120 in). The process tube extends in equal segments (each having a length of 50.8 cm (20 in)) through each of the temperature control zones, leaving 152 cm (60 in) extending through the cooling zone.
The process tube provided with the Harper Rotating Tube Furnace may be inclined within a range of 0 to 5°. In addition, the Harper Rotating Tube Furnace may be provided with a variable direct current (DC) drive with digital speed control for rotating the process tube at rotational speeds of one to five revolutions per minute (rpm).
The Harper Rotating Tube Furnace also features a 316-liter, stainless steel, gas-tight with inert gas purge, discharge hopper. The Harper Rotating Tube Furnace also features an atmosphere process gas control system for maintaining a constant pressure within the process tube. In addition, a 45-kilowatt (kW) power supply may be provided, for heating the furnace and driving the process tube. In addition, the Harper Rotating Tube Furnace may be fitted with a Brabender Loss-In-Weight Feed System (Model No. H31-FW33/50), commercially available from C.W. Brabender Instruments, Inc. (South Hackensack, N.J.).
Although preferred embodiments of apparatus 10 are shown in
Having described apparatus 10, and preferred embodiments thereof, that may be used to produce molybdenum metal product 12 according to the invention, attention is now directed to embodiments of a method for producing molybdenum metal product 12. As an overview, and still with reference to
According to preferred embodiments, the precursor material 14 comprises nano-particles of molybdic oxide (MoO3). The nano-particles of molybdic oxide preferably have a typical surface area to mass ratio of about 25 to 35 m2g. When these nano-particles of molybdic oxide are used as the precursor material 14, the molybdenum metal product 12 produced according to embodiments of the method of the invention may be characterized as having a surface area to mass ratio of about 2.5 m2/g. In addition, the molybdenum metal product 12 may be characterized as being uniform in size.
The nano-particles of molybdic oxide described above may be produced according to embodiments of the invention disclosed in co-owned, U.S. Pat. No. 6,468,497 issued on Oct. 22, 2002 for “METHOD FOR PRODUCING NANO-PARTICLES OF MOLYBDENUM OXIDE” of Khan, et al., which is incorporated herein for all that it discloses. The nano-particles of molybdic oxide are produced by, and are commercially available from the Climax Molybdenum Company (Fort Madison, Iowa).
According to other embodiments of the invention, however, it is understood that the precursor material 14 may comprise any suitable grade or form of molybdic oxide (MoO3). For example, the precursor material 14 may range in size from 0.5 to 80 m2/g. Selection of the precursor material 14 may depend on various design considerations, including but not limited to, the desired characteristics of the molybdenum metal product 12 (e.g., surface area to mass ratio, size, purity, etc.). In general, the surface area to mass ratio of the molybdenum metal product 12 is proportionate to the surface area to mass ratio of the precursor material 14, and typically ranges from 1.5 to 4.5 m2/g.
Turning now to
As the precursor material 14 moves through the first heating zone 20, it is mixed with the process gas 62 and reacts therewith to form the intermediate product 30. The reaction is illustrated by arrows 70 in heating zone 20 (Heating Zone 1) of
MoO3(s)+H2(g)→MoO2(s)+H2O(v)
The temperature in the first heating zone 20 is preferably maintained below the vaporization temperature of the precursor material 14, and that of any intermediate material 30 that is formed in the first heating zone 20 (Heating Zone 1), relative to the pressure within the process tube 34. Overheating the precursor material 14 and/or the intermediate material 30 may cause a reaction only on the surface thereof. The resulting surface reaction may cause beads of molybdenum metal to form, sealing unreacted precursor material 14 and/or intermediate material 30 therein. These beads may require longer processing times and/or higher processing temperatures to convert to pure molybdenum metal product 12, thus reducing the efficiency and increasing the cost of production.
The temperature of the first heating zone 20 is preferably maintained at a lower temperature than the other two heating zones 21, and 22 because the reaction between the precursor material 14 and the reducing gas 64 in the first heating zone 20 (Heating Zone 1) is an exothermic reaction. That is, heat is released during the reaction in the first heating zone 20.
The second heating zone 21 (Heating Zone 2) is preferably provided as a transition zone between the first heating zone 20 (Heating Zone 1) and the third heating zone 22 (Heating Zone 3). That is, the temperature in the second heating zone 21 is maintained at a higher temperature than the first heating zone 20, but preferably maintained at a lower temperature than the third heating zone 22. As such, the temperature of the intermediate material 30 and the unreacted precursor material 14 is gradually ramped up for introduction into the third heating zone 22. Without the second heating zone 22, an immediate transfer of the intermediate material 30 and the unreacted precursor material 14 from the lower temperatures of the first heating zone 20 (Heating Zone 1) to the higher temperatures of the third heating zone 22 (Heating Zone 3) may cause beads of unreacted material to form. The disadvantages of these beads are discussed above. In addition, the molybdenum metal product 12 may agglomerate and produce undesirable product “chunks”.
As the intermediate material 30 moves into the third heating zone 22 (Heating Zone 3), it continues to be mixed with the process gas 62 and reacts therewith to form the molybdenum metal product 12, as illustrated by arrows 72 in
MoO2(s)+2H2(g)→Mo(s)+2H2O(v)
The reaction between the intermediate material 30 and the reducing gas 64 in the third heating zone 22 (Heating Zone 3) is an endothermic reaction. That is, heat is consumed during this reaction. Therefore, the energy input of the third heating zone 22 is preferably adjusted accordingly to provide the additional heat required by the endothermic reaction in the third heating zone 22.
When the molybdenum metal 12 produced by the reactions described above is immediately introduced to an atmospheric environment while still hot (e.g., upon exiting the third heating zone 22), it may react with one or more constituents of the atmosphere. For example, the hot molybdenum metal 12 may reoxidize when it is exposed to an oxygen environment. Therefore, the molybdenum metal product 12 is preferably moved through a cooling zone 23. Also preferably, the process gas 62 flows through the cooling zone so that the hot molybdenum metal product 12 may be cooled in a reducing environment, thus lessening or eliminating the occurrence of reoxidation of the molybdenum metal product 12 (e.g., to form MoO2 and/or MoO3). The cooling zone 23 may also be provided to cool the molybdenum metal product 12 for handling purposes.
As explained above, the reactions in the first heating zone 20 (Heating Zone 1) are primarily the precursor material 14 being reduced to form intermediate material 30. Also as explained above, the second heating zone 21 (Heating Zone 2) is primarily provided as a transition zone for the intermediate material 30 produced in the first heating zone 20 before it is introduced to the third heating zone 22 (Heating Zone 3). And also as explained above, the reactions in the third heating zone 22 are primarily the intermediate material 30 being further reduced to form the molybdenum metal product 12. However, the preceding discussion of the reactions in each of the heating zones 20, 21, and 22 shown in
As will be readily apparent to one skilled in the art, it is understood that these reactions may occur in each of the three heating zones 20, 21, and 22, as illustrated by arrows 70, 71, and 72. That is, some molybdenum metal product 12 may be formed in the first heating zone 20 and/or the second heating zone 21. Likewise, some unreacted precursor material 16 may be introduced into the second heating zone 21 and/or the third heating zone 22. In addition, some reactions may still occur even in the cooling zone 23.
Also as will be readily apparent to one skilled in the art, any unreacted reducing gas 64 and the inert gas 65 is also discharged in the effluent. Likewise, where a reducing gas 64 other than hydrogen is used, the reducing agent combined with oxygen stripped from the molybdic oxide, is also released in the effluent.
Having discussed the reactions in the various portions of the furnace 16 illustrated in
It is understood that molybdenum metal product 12 may also be produced when the process parameters are adjusted outside of the ranges given above in Table 1, as may be readily determined by one skilled in the art based on the teachings of the invention.
According to preferred embodiments of the invention, it is not necessary to screen the molybdenum metal product 12 to remove precursor material 14, intermediate material 30, and/or other contaminating material (not shown) from the product. That is, preferably, 100% of the precursor material 14 is fully converted to pure molybdenum metal product 12. However, according to embodiments of the invention, the molybdenum metal product 12 may be screened to remove oversize particles from the product that may have agglomerated during the process. Whether the molybdenum metal product 12 is screened will depend on design considerations such as, but not limited to, the ultimate use for the molybdenum metal product 12, the purity and/or particle size of the precursor material 14, etc.
An embodiment of a method for producing molybdenum metal 12 according to the teachings of the invention is illustrated as steps in the flow chart shown in
It is understood that the steps shown and described with respect to
Still other embodiments are also contemplated as being within the scope of the invention. Indeed, it is expected that yet other embodiments of the method for producing molybdenum metal product will become readily apparent to one skilled in the art based on the teachings of the invention.
Having described methods and apparatus 10 for producing molybdenum metal according to the invention, characteristics of molybdenum metal will now be shown and described in further detail.
Measurements of particle surface area per unit weight may be obtained by BET analysis. As is well known, BET analysis involves an extension of the Langmuir isotherm equation using multi-molecular layer absorption developed by Brunauer, Emmett, and Teller (hence, BET). BET analysis is an established analytical technique that provides highly accurate and definitive results.
The molybdenum metal, as shown in
Again, although the size of the molybdenum metal product 12 can be expressed in terms of the mean length or the mean diameter of the particles (e.g., as detected by scanning electron microscopy), it is generally more useful to express the size of molybdenum metal in terms of surface area per unit mass due to the correlation between size and surface area.
The molybdenum metal product 12 shown and described with respect to
In this Example 1, the precursor material comprised nano-particles of molybdic oxide (MoO3) having a typical size of about 25 to 35 m2/g. Such nano-particles of molybdic oxide may be produced according to embodiments of the invention disclosed in co-owned, U.S. Pat. No. 6,468,497 issued on Oct. 22, 2002 for “METHOD FOR PRODUCING NANO-PARTICLES OF MOLYBDENUM OXIDE”. The nano-particles of molybdic oxide used as precursor material in this example are produced by and are commercially available from the Climax Molybdenum Company (Fort Madison, Iowa).
The following equipment was used for this example: a Brabender Loss-In-Weight Feed System (Model No. H31-FW33/50), commercially available from C.W. Brabender Instruments, Inc. (South Hackensack, N.J.); and a Harper Rotating Tube Furnace (Model No. HOU-6D60-RTA-28-F), commercially available from Harper International Corporation (Lancaster, N.Y.). The Harper Rotating Tube Furnace comprised three independently controlled 50.8 cm (20 in) long heating zones with a 305 cm (120 in) HT alloy tube extending through each of the heating zones thereof. Accordingly, a total of 152 cm (60 in) of heating and 152 cm (60 in) of cooling were provided in this example.
In this example, the precursor material was fed, using the Brabender Loss-In-Weight Feed System, into the HT alloy tube of the Harper Rotating Tube Furnace. The HT alloy tube was rotated and inclined (see Table 2, below) to facilitate movement of the precursor material through the Harper Rotating Tube Furnace, and to facilitate mixing of the precursor material with a process gas. The process gas was introduced through the HT alloy tube in a direction opposite or counter-current to the direction that the precursor material was moving through the HT alloy tube. In this example, the process gas comprised hydrogen gas as the reducing gas, and nitrogen gas as the inert carrier gas. The discharge gas was bubbled through a water scrubber to maintain the interior of the furnace at approximately 11.4 cm (4.5 in) of water pressure (gauge).
Optimum conversion of the precursor material to the molybdenum metal product occurred when the parameters were set to the values shown in Table 2.
Molybdenum metal 12 produced according to this example is shown in
In this Example 2, the precursor material comprised nano-particles of molybdic oxide (MoO3) having a typical size of about 30–50 m2/g. Such nano-particles of molybdic oxide may be produced according to embodiments of the invention disclosed in co-owned, U.S. Pat. No. 6,468,497 issued on Oct. 22, 2002 for “METHOD FOR PRODUCING NANO-PARTICLES OF MOLYBDENUM OXIDE”. The nano-particles of molybdic oxide used as precursor material in this example are produced by and are commercially available from the Climax Molybdenum Company (Fort Madison, Iowa).
The following equipment was used for this example: a Brabender Loss-In-Weight Feed System (Model No. H31-FW33/50), commercially available from C.W. Brabender Instruments, Inc. (South Hackensack, N.J.); and a Harper Rotating Tube Furnace (Model No. HOU-6D60-RTA-28-F), commercially available from Harper International Corporation (Lancaster, N.Y.). The Harper Rotating Tube Furnace comprised three independently controlled 50.8 cm (20 in) long heating zones with a 305 cm (120 in) HT alloy tube extending through each of the heating zones thereof. Accordingly, a total of 152 cm (60 in) of heating and 152 cm (60 in) of cooling were provided in this example.
In this example, the precursor material was fed, using the Brabender Loss-In-Weight Feed System, into the HT alloy tube of the Harper Rotating Tube Furnace. The HT alloy tube was rotated at 20 seconds per revolution and inclined to 0.3° (see Table 3, below) to facilitate movement of the precursor material through the Harper Rotating Tube Furnace, and to facilitate mixing of the precursor material with a process gas. However, satisfactory results can be obtained with other tube inclinations (e.g., in a range of about 0.2° to about 0.4°). The process gas was introduced through the HT alloy tube in a direction opposite or counter-current to the direction that the precursor material was moving through the HT alloy tube. In this example, the process gas comprised hydrogen gas as the reducing gas, and nitrogen gas as the inert carrier gas. The discharge gas was bubbled through a water scrubber to maintain the interior of the furnace at approximately 11.4 cm (4.5 in) of water pressure (gauge).
Optimum conversion of the precursor material to the molybdenum metal product occurred when the parameters were set to the values shown in Table 3.
The molybdenum metal product 12 produced according to this Example 2 is characterized by a surface area to mass ratio of 2.0837 m2/g (BET). After grinding to break up agglomerations of the product 12, the non-screened molybdenum product 12 had an overall mean size of 1.598 μm, as measured by a Horiba laser scattering analyzer.
In this Example 3, the precursor material comprised nano-particles of molybdic oxide (MoO3) having a typical size of about 30–50 m2/g. Such nano-particles of molybdic oxide may be produced according to embodiments of the invention disclosed in co-owned, U.S. Pat. No. 6,468,497 issued on Oct. 22, 2002 for “METHOD FOR PRODUCING NANO-PARTICLES OF MOLYBDENUM OXIDE”. The nano-particles of molybdic oxide used as precursor material in this example are produced by and are commercially available from the Climax Molybdenum Company (Fort Madison, Iowa).
The following equipment was used for this example: a Brabender Loss-In-Weight Feed System (Model No. H31-FW33/50), commercially available from C.W. Brabender Instruments, Inc. (South Hackensack, N.J.); and a Harper Rotating Tube Furnace (Model No. HOU-6D60-RTA-28-F), commercially available from Harper International Corporation (Lancaster, N.Y.). The Harper Rotating Tube Furnace comprised three independently controlled 50.8 cm (20 in) long heating zones with a 305 cm (120 in) HT alloy tube extending through each of the heating zones thereof. Accordingly, a total of 152 cm (60 in) of heating and 152 cm (60 in) of cooling were provided in this example.
In this example, the precursor material was fed, using the Brabender Loss-In-Weight Feed System, into the HT alloy tube of the Harper Rotating Tube Furnace. The HT alloy tube was rotated at 20 seconds per revolution and inclined to 0.3° (see Table 4, below) to facilitate movement of the precursor material through the Harper Rotating Tube Furnace, and to facilitate mixing of the precursor material with a process gas. However, satisfactory results can be obtained with other tube inclinations (e.g., in a range of about 0.2° to about 0.4°). The process gas was introduced through the HT alloy tube in a direction opposite or counter-current to the direction that the precursor material was moving through the HT alloy tube. In this example, the process gas comprised hydrogen gas as the reducing gas, and nitrogen gas as the inert carrier gas. The discharge gas was bubbled through a water scrubber to maintain the interior of the furnace at approximately 11.4 cm (4.5 in) of water pressure (gauge).
Optimum conversion of the precursor material to the molybdenum metal product occurred when the parameters were set to the values shown in Table 4.
The molybdenum metal product 12 produced according to this example is characterized by a surface area to mass ratio of 3.412 m2/g (BET). After grinding to break up agglomerations of the product 12, the non-screened molybdenum metal product 12 had an overall mean size of 1.019 μm, as measured by a Horiba laser scattering analyzer.
In this Example 4, the precursor material comprised nano-particles of molybdic oxide (MoO3) having a typical size of about 30–50 m2/g. Such nano-particles of molybdic oxide may be produced according to embodiments of the invention disclosed in co-owned, U.S. Pat. No. 6,468,497 issued on Oct. 22, 2002 for “METHOD FOR PRODUCING NANO-PARTICLES OF MOLYBDENUM OXIDE”. The nano-particles of molybdic oxide used as precursor material in this example are produced by and are commercially available from the Climax Molybdenum Company (Fort Madison, Iowa).
The following equipment was used for this example: a Brabender Loss-In-Weight Feed System (Model No. H31-FW33/50), commercially available from C.W. Brabender Instruments, Inc. (South Hackensack, N.J.); and a Harper Rotating Tube Furnace (Model No. HOU-6D60-RTA-28-F), commercially available from Harper International Corporation (Lancaster, N.Y.). The Harper Rotating Tube Furnace comprised three independently controlled 50.8 cm (20 in) long heating zones with a 305 cm (120 in) HT alloy tube extending through each of the heating zones thereof. Accordingly, a total of 152 cm (60 in) of heating and 152 cm (60 in) of cooling were provided in this example.
In this example, the precursor material was fed, using the Brabender Loss-In-Weight Feed System, into the HT alloy tube of the Harper Rotating Tube Furnace. The HT alloy tube was rotated at 20 seconds per revolution and inclined to 0.3° (see Table 5, below) to facilitate movement of the precursor material through the Harper Rotating Tube Furnace, and to facilitate mixing of the precursor material with a process gas. However, satisfactory results can be obtained with other tube inclinations (e.g., in a range of about 0.2° to about 0.4°). The process gas was introduced through the HT alloy tube in a direction opposite or counter-current to the direction that the precursor material was moving through the HT alloy tube. In this example, the process gas comprised hydrogen gas as the reducing gas, and nitrogen gas as the inert carrier gas. The discharge gas was bubbled through a water scrubber to maintain the interior of the furnace at approximately 11.4 cm (4.5 in) of water pressure (gauge).
Optimum conversion of the precursor material to the molybdenum metal product occurred when the parameters were set to the values shown in Table 5.
The molybdenum metal product 12 produced according to this example is characterized by a surface area to mass ratio of 4.106 m2/g (BET). After grinding to break up agglomerations of the product 12, the non-screened molybdenum metal product 12 had an overall mean size of 1.005 μm, as measured by a Horiba laser scattering analyzer.
It is readily apparent that novel forms of molybdenum metal as discussed herein have a relatively larger surface area to mass ratio and are relatively uniform in size. Likewise, it is apparent that apparatus and methods for production of molybdenum metal discussed herein may be used to produce molybdenum metal in a continuous, single stage manner. Consequently, the claimed invention represents an important development in molybdenum metal technology. Having herein set forth various and preferred embodiments of the invention, it is expected that suitable modifications will be made thereto which will nonetheless remain within the scope of the invention. Accordingly, the invention should not be regarded as limited to the embodiments shown and described herein, and it is intended that the appended claims be construed to include yet other embodiments of the invention, except insofar as limited by the prior art.
This is a continuation-in-part of U.S. patent application Ser. No. 10/464,324 filed on Jun. 18, 2003, now U.S. Pat. No. 7,132,005 which is a divisional of application Ser. No. 10/045,637 filed on Nov. 6, 2001 application of U.S. Pat. No. 6,626,976, which are hereby incorporated herein by reference for all that they disclose.
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| Number | Date | Country | |
|---|---|---|---|
| 20040112176 A1 | Jun 2004 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 10045637 | Nov 2001 | US |
| Child | 10464324 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 10464324 | Jun 2003 | US |
| Child | 10719234 | US |
