COBALT-BASED CATALYSTS AND PROCESS FOR PRODUCING SYNTHESIS GAS

Abstract: A process is disclosed for the catalytic partial oxidation of light hydrocarbons such as methane. The process involves the conversion of a hydrocarbon feedstock by contacting a feed stream comprising the hydrocarbon feedstock and an oxygen-containing gas with a catalyst in a reaction zone maintained at conversion-promoting conditions in a millisecond contact time reactor effective to produce an effluent stream containing primarily carbon monoxide and hydrogen. Certain preferred catalysts of the invention comprise cobalt metal and/or cobalt containing compound(s), a promoter, and a refractory support are capable of efficiently producing syngas at high selectivities for CO and H2 products.

Description: COBALT-BASED CATALYSTS AND PROCESS FOR PRODUCING SYNTHESIS GAS CROSS-REFERENCE TO RELATED APPLICATIONS This application claims the benefit of U.S. Provisional Patent Application No. 60/165,981 filed November 17, 1999. BACKGROUND OF THE INVENTION Field of the Invention The present invention generally relates to catalysts and processes for converting a light hydrocarbon (e.g., natural gas) and oxygen to a product containing a mixture of carbon monoxide and hydrogen, also referred to as synthesis gas or syngas. More particularly, the invention relates to supported cobalt-containing catalysts and syngas production processes employing them. Description of Related Art Large quantities of methane, the main component of natural gas, are available in many areas of the world, and natural gas is predicted to outlast oil reserves by a significant margin. However, most natural gas is situated in areas that are geographically remote from population and industrial centers. The costs of compression, transportation, and storage make its use economically unattractive. To improve the economics of natural gas use, much research has focused on methane as a starting material for the production of higher hydrocarbons and hydrocarbon liquids. The conversion of methane to hydrocarbons is typically carried out in two steps. In the first step, methane is reformed with water to produce carbon monoxide and hydrogen (i.e., synthesis gas or syngas). In a second step, the syngas is converted to hydrocarbons, for example, using the Fischer-Tropsch process to provide fuels that boil in the middle distillate range, such as kerosene and diesel fuel, and hydrocarbon waxes. Current industrial use of methane as a chemical feedstock proceeds by the initial conversion of methane to carbon monoxide and hydrogen by either steam reforming, which is the most widespread process, or by dry reforming. Steam reforming is the major process used commercially for the conversion of methane to synthesis gas, the conversion proceeding by the strongly endothermic reaction shown in Equation 1. CH 4 + H 2 O => CO + 3H 2 (1) This process requires the input of appreciable quantities of thermal energy to initiate and maintain the reaction. Although steam reforming has been widely practiced for over five decades, efforts to improve the energy efficiency and reduce the capital investment required for this technology continue. In contrast, the partial oxidation of methane and other light hydrocarbons is exothermic, and under ideal conditions can proceed according to the stoichiometry of Equation 2 to yield a syngas mixture with a H :CO ratio of 2: 1. This ratio is more useful than the H 2 :CO ratio from steam reforming for such downstream operations as the conversion of the syngas to chemicals such as methanol and to fuels. CH 4 + l/2O 2 CO + 2H 2 (2) Another advantage of utilizing partial oxidation processes for syngas production is that oxidation reactions are typically much faster than reforming reactions, and therefore, allow the use of much smaller reactors. The non-catalytic partial oxidation of methane carried out at high temperatures (>1300°C) and high pressures (150 atm) can produce syngas at high selectivities for CO and H 2 products (Chang et al. 1993 Catalysis Letters 21:215-224). While currently limited as an industrial process due to the technical difficulties of obtaining the desired stoichiometry, partial oxidation offers an additional advantage over conventional steam reforming of methane in that significant heat is released by the oxidation reaction, thereby eliminating the need for a fuel gas. Depending on the relative proportions of hydrocarbon and oxygen and other reaction conditions, other, more highly exothermic partial oxidation reaction stoichiometries, can occur instead of or in addition to the reaction stoichiometry shown in Equation 2. However, the greater amounts of heat produced by those reactions, if excessive, can damage the reactor or its components. In order to avoid such extreme conditions, various metal-containing catalysts have been employed to catalyze the partial oxidation of hydrocarbons such as methane. In a typical catalytic partial oxidation process, the light hydrocarbon is mixed with air, oxygen-enriched air, or oxygen, and introduced to a catalyst at elevated temperature and pressure. The selectivities of catalytic partial oxidation to the desired products (i.e., carbon monoxide and hydrogen) are controlled by several factors. One of the most important of these factors is the choice of catalyst composition. Choosing an economical catalyst that is efficient and provides excellent selectivities for CO and H is a problem. Typically, catalyst compositions have included precious metals and/or rare earths. The large volumes of expensive catalysts required in most conventional catalytic partial oxidation processes have placed these processes generally outside the limits of economic justification. For successful operation at commercial scale, the catalytic partial oxidation process must be able to achieve a high conversion of the methane feedstock at high gas hourly space velocities, and the selectivity of the process to the desired products of carbon monoxide and hydrogen must be high. Such high conversion and selectivity must be achieved without detrimental effects to the catalyst, such as the formation of carbon deposits ("coke") on the catalyst, which severely reduces catalyst performance. Accordingly, substantial effort has also been devoted in the art to the development of catalysts allowing sustainable commercial performance without coke formation. A number of process regimes have been proposed for the production of syngas via catalyzed partial oxidation reactions, and a number of catalyst formulations have been examined. For example, European Pat. No. EP303438 describes one method for the catalytic partial oxidation of methane using a high temperature, high pressure mixture of methane and oxygen at GHSV (gas hourly space velocity) of up to 5 x 10 5 . U.S. Pat. No. 5,149,464 discloses a method for selectively converting methane to syngas at 650°C to 950°C by contacting the methane/oxygen mixture with a solid catalyst comprising a supported d-Block transition metal, transition metal oxide, or a compound of the formula M x M' y O z wherein M' is a d-Block transition metal and M is Mg, B, Al, Ga, Si, Ti, Xr, Hf or a lanthanide. U.S. Pat. No. 5,500,149 discloses various transition metals that can act as catalysts in the reaction CO 2 + CH 4 -» 2CO + 2H , and demonstrates how reaction conditions can affect the product yield. The partial oxidation of methane to synthesis gas using various transition metal catalysts under a range of conditions has been described by Vernon, D.F. et al. (Catalysis letters 6:181-186 (1990)). European Pat. App. Pub. No. 640561 discloses a catalyst for the catalytic partial oxidation of hydrocarbons comprising a Group VIII metal on a refractory oxide having at least two cations. U.S. Pat. No. 5,149,516 discloses a process for partial oxidation of methane to produce a product including carbon monoxide and hydrogen employing a type of perovskite catalyst, such as LaCoO 3 . U.S. Pat. No. 5,447,705 discloses another catalyst having a perovskite crystalline structure and the general composition: Ln x Aι_ y B y O 3 , wherein Ln is a lanthanide and A and B are different metals chosen from Group IVb, Vb, VIb, Vllb or VIII of the Periodic Table of the Elements. Lago et al. (1997 J Catalysis 167:198-209; and in Grasselli, et al. (eds.) 3 rd World Congress on Oxidation Catalysis, Elsevier Science B.V., 1997, pp. 721-730) also describe certain perovskite catalyst precursors containing cobalt and lanthanide oxides for the partial oxidation of methane to synthesis gas. U.S. Pat. No. 5,338,488 describes a process for the production of synthesis gas by oxidative conversion of methane using composite catalysts containing certain transitional and alkaline earth metal oxides. The transition metals include Ni, Co, Pd, Ru, Rh, Ir and mixtures thereof; and the alkaline earth metals include Mg, Ca, Ba, Sr and mixtures thereof. U.S. Pat. No. 5,368,835, U.S. Pat. No. 5,411, 927 and U.S. Pat. No. 5,756,421 describe the oxidative conversion of methane to synthesis gas using catalysts containing certain transition and non- transition metal oxides. Some investigators have examined certain cobalt-containing catalysts, many of which also include nickel or a Group VIII metal. For example, U.S. Pat. No. 5,752,995 describes a cobalt promoted nickel catalyst for the production of gases rich in H from methane with decreased carbon deposition. The catalyst may include certain refractory materials as supports for the catalyst. Xianjun et al. (1998 "Microwave Effect on Partial Oxidation of Methane to Syngas over Co/La 2 O 3 " Chinese Journal of Chemical Physics 11 :193-196) describe a Co/La 2 O 3 catalyst and activation of the reaction by microwave heating. However, Xianjun et al. (1999 "Partial Oxidation of Methane to Syngas by Microwave Initiating" Chinese Journal of Catalysis 20:73-75) found that the activity and selectivity of a Co/La 2 O 3 catalyst decreased markedly with increasing time on-stream. U.S. Pat. No. 5,235,804 suggests that certain cobalt oxide catalysts are capable of partially oxidizing C]. 2 o hydrocarbons and controlling NO x and other pollutant emissions associated with the combustion of hydrocarbon fuels. These catalysts may be supported on alumina or similar substrate, or in the form of granules, extrudates, coating on a metal heat exchanger surface, metal honeycomb or ceramic honeycomb. Chinese Pat. No. 1130150A discloses a cobalt- alkaline earth-lanthanide-containing catalyst used to convert CH 4 to CO and H 2 at 300- 900°C. Japanese Pat. No. 1-52055 describes a cobalt-alumina-magnesia spinel catalyst and a cobalt oxide-barium aluminate catalyst for catalyzing the partial oxidation of hydrocarbons. Others have employed certain cobalt-containing catalysts in hydrocarbon reforming processes. For example, U.S. Pat. No. 4,024,075 (Russ et al.) describes a supported cobalt catalyst for reforming hydrocarbons with steam and carbon dioxide. Wang, et al. (1998 Chinese J. of Catalysis 19:196-200) disclose certain reforming catalysts containing Co/Al O 3 for methane and carbon dioxide reformation to syngas. U.S. Patent No. 5,989,457 describes a process for making synthesis gas by methane reforming with carbon dioxide using a Co, Ni, Pt or Pd catalyst on a thermally stabilized oxidic support containing an oxide of Y, La, Al, Ca, Ce or Si. U.S. Patent No. 6,060,420 describes a catalyst for purifying exhaust gas comprising an alumina or zirconia catalyst carrier substrate and a composite oxide of A-site defect perovskite structure represented by the general formula: A^αBO^ where A is an alkali metal, alkaline earth metal, rare earth element, Y or Pb. B is Mn, Co, Ti, Fe, Ni, Cu and Al and α is from 0.12-0.15 and δ is up to 1. One disadvantage of many of the existing catalytic hydrocarbon conversion methods is the need to include steam in the feed mixture to suppress coke formation on the catalyst. Another drawback of some of the existing processes is that the catalysts that are employed often result in the production of significant quantities of carbon dioxide, steam, and C 2 + hydrocarbons. Also, large volumes of catalyst are sometimes required, necessitating the use of exceptional devices in an attempt to evenly distribute the feed to the top of the catalyst bed. None of the existing processes or catalysts are capable of providing high conversion of reactant gas and high selectivity of CO and H 2 reaction products. Accordingly, there is a continuing need for better processes for the catalytic partial oxidation of light hydrocarbons, in which the catalyst retains a higher level of activity and selectivity to carbon monoxide and hydrogen under conditions of high gas space velocity and elevated pressure. SUMMARY OF THE INVENTION The present invention provides processes for preparing synthesis gas using cobalt- containing catalysts for the catalytic partial oxidation of any gaseous hydrocarbon having a low boiling point (e.g. C]-C 5 hydrocarbons, particularly methane, or methane containing feeds). One advantage of the cobalt catalysts of the process is that they retain a high level of activity and selectivity to carbon monoxide and hydrogen under conditions of high gas space velocity and elevated pressure. Another advantage of the new catalytic processes is that they are economically feasible for use in commercial-scale conditions. Also provided by the present invention are supported cobalt-containing catalysts for catalyzing the partial oxidation of a hydrocarbon, and their methods of making. The supported catalysts contain cobalt metal and/or one or more cobalt containing compound(s) including the various oxides of cobalt, cobalt containing spinels, mixed metal oxides or metals of cobalt with magnesia, nickel, LaZrO 2 , lanthanum oxide, alumina, zirconia, ceria, and calcium oxide. The spinels and mixed metal oxides include CoAl O , MgCo O 4 , Co AlO 4 , LaAl 8 Co 2 O 3 , CaCo 2 O 4 , ZnCo 2 O 4 , and NiCo O 4 . The catalyst may be comprised of a cobalt-containing hydrotalcite, including the hydrotalcite Co 6 Al 2 (OH)ι 6 CO 3 • 4 H 2 O. Preferably, the support structure comprises a spinel, a perovskite, magnesium oxide, a hydrotalcite, LaZrO 2 , lanthanum oxide, a pyrochlore, a brownmillerite, zirconium phosphate, magnesium stabilized zirconia, zirconia stabilized alumina, silicon carbide, yttrium stabilized zirconia, calcium stabilized zirconia, yttrium aluminum garnet, alumina, cordierite, ZrO 2 , ZnO, LaAlO 3 , MgAl 2 O 4 , SiO 2 or TiO 2 . The cobalt metal and/or cobalt containing compound(s) are disposed on or within the support structure. In some of the more preferred embodiments, the catalyst support structure is a hydrotalcite, spinel, a perovskite, a pyrochlore or a brownmillerite, and the cobalt metal and/or cobalt containing compound(s) are incorporated into the support structure. In certain embodiments of the catalysts the support structure comprises a refractory oxide, which may be in the form of a foam structure. Preferably such a foam structure comprises about 12-60 pores per centimeter of structure. Alternatively, in some embodiments the support structure is in the form of a honeycomb monolith structure. In some embodiments, the catalyst comprises the cobalt metal and/or cobalt containing compound(s) on a support structure comprising Al 2 O 3 . Some embodiments comprise a Co containing hydrotalcite. In some embodiments the catalyst comprises mixtures of cobalt metal and/or oxides with magnesia in the form of solid solution. Another catalyst embodiment comprises cobalt spinels and mixed metal oxides including CoAl 2 O 4 , MgCo 2 O 4 , Co AlO 4 , LaAl 8 Co 2 O 3 , CaCo 2 O 4 , ZnCo 2 O 4 , and NiCo 2 O 4 . And others comprise cobalt metal and/or oxides on LaZrO 2 , alumina, lanthanum oxide, and zirconia. In some embodiments a syngas catalyst device is provided that comprises cobalt metal and/or cobalt oxide, a promoter chosen from the group consisting of Mn, Ni, La, Cu, Sm, Yb, Eu, Pr, Ce, Y, Pt, Rh and Re, and a support structure comprising partially stabilized zirconia. In some embodiments the catalyst device comprises cobalt metal and/or cobalt oxide, manganese metal and/or manganese oxide, magnesium oxide and a partially stabilized zirconia support. In some embodiments the catalyst comprises 0.15 wt% Pt, about 6.5 wt% Co and about 6.1 wt% Mg by catalyst weight. In certain embodiments a syngas catalyst is prepared by impregnating a refractory metal oxide support, such as a PSZ foam, with a solution of an oxidizable magnesium salt and then calcining the resulting magnesium impregnated support. The magnesium impregnated support is then re-impregnated with a solution of an oxidizable cobalt salt to provide a cobalt/magnesium oxide intermediate, which is then calcined and reduced. In certain preferred embodiments, this (cobalt/magnesium) oxide loaded support is then coated with a promoter by impregnating with a solution of an oxidizable metal salt, such as a nitrate or an acetate. Suitable promoter metals include Mn, Ni, La, Cu, Sm, Yb, Eu, Pr, Ce, Y, Pt, Rh and Re. The promoter/(cobalt/magnesium) oxide coated support is then calcined and reduced to provide a supported catalyst that is active for catalyzing the net partial oxidation of methane in the presence of O 2 to CO and H under partial oxidation promoting conditions in a short contact time reactor. Also provided by the present invention is a process for the net partial oxidization of a C 1 -C 5 hydrocarbon to form a product gas mixture comprising CO and H . According to certain embodiments, the process comprises passing a reactant gas mixture comprising a Ci- C 5 hydrocarbon and an O 2 -containing gas over a supported catalyst, or catalyst device, as described above, in a millisecond contact time reactor. The contact time of a portion of reactant gas mixture in contact with the catalyst device does not exceed about 10 milliseconds. The process also includes maintaining net catalytic partial oxidation promoting conditions during operation of the reactor. Such reaction-promoting conditions include maintaining a favorable hydrocarbomoxygen molar ratio in the reactant gas mixture, maintaining a favorable catalyst temperature, maintaining a favorable reactant gas preheat temperature and reactant flow rate. In certain preferred embodiments the process includes maintaining the reactant gas mixture and the catalyst at a temperature of about 600-l,200°C during contact. In some embodiments the temperature is maintained at about 700-l,100°C. In certain embodiments of the process, maintaining net catalytic partial oxidation promoting conditions includes mixing a methane-containing feedstock and an oxygen- containing feedstock to provide a reactant gas mixture feedstock having a carbomoxygen molar ratio of about 1.25:1 to about 3.3:1. In some of these embodiments, the mixing step is such that it yields a reactant gas mixture feed having a carbomoxygen ratio of about 1.3:1 to about 2.2:1, or preferably about 1.5:1 to about 2.2:1. In some of the most preferred embodiments the mixing step provides a reactant gas mixture feed having a carbon:oxygen ratio of about 2:1. In some embodiments of the process the oxygen-containing gas that is mixed with the hydrocarbon also contains steam or CO 2 , or both. In some embodiments of the process the Cj-C 5 hydrocarbon comprises at least about 50 % methane by volume, and in some of the preferred embodiments the C]-C 5 hydrocarbon comprises at least about 80 % methane by volume. Some embodiments of the process include preheating the reactant gas mixture, to facilitate catalyst activation for the reaction. Some embodiments of the processes comprise passing the reactant gas mixture over the catalyst at a space velocity of about 20,000 to about 100,000,000 normal liters of gas per kilogram of catalyst per hour (NL/kg/h). In certain of these embodiments, the gas mixture is passed over the catalyst at a space velocity of about 50,000 to about 50,000,000 NL/kg/h. In some embodiments of the reactor is operated at a pressure of about 100-12,500 kPa during the contacting, and in some of the more preferred embodiments the pressure is maintained at about 130-10,000 kPa. These and other embodiments, features and advantages of the present invention will become apparent with reference to the following description. DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS Supported catalysts, or catalyst devices, useful for catalytically converting C]-C 5 hydrocarbons to CO and H contain cobalt metal and/or cobalt-containing compound(s) have been developed which include support materials such as hydrotalcites, spinels, perovskites, magnesium oxide, lanthanum oxide, LaZrO , pyrochlores, brownmillerites, zirconium phosphate, magnesium stabilized zirconia, zirconia stabilized alumina, silicon carbide, yttrium stabilized zirconia, calcium stabilized zirconia, yttrium aluminum garnet, alumina, cordierite, mullite, ZrO 2 , ZnO, LaAlO 3 , MgAl 2 O 4 , SiO 2 or TiO 2 . In some of these catalysts, the cobalt metal and/or cobalt-containing compound(s) are incorporated into the structure of a hydrotalcite, spinel, perovskite, pyrochlore or brownmillerite. As described in the following examples, representative catalysts comprised of cobalt metal and/or one or more cobalt- containing compounds are prepared utilizing conventional techniques such as impregnation, wash coating, adsoφtion, ion exchange, precipitation, co-precipitation, deposition precipitation, sol-gel method, slurry dip-coating, microwave heating, and the like, all of which are well known in the field. Preferred techniques are wash coating, impregnation, sol- gel methods and co-precipitation. As described in more detail below, some of the more active supported catalysts include a promoter and are prepared using a multi-step support loading process and defined calcining and reducing program. In some cases, the catalyst components with or without a ceramic support material are extruded to prepare a three-dimensional form or structure such as a honeycomb, foam, or other suitable tortuous-path structure. The catalyst components may be added to the powdered ceramic composition and then extruded to prepare the foam or honeycomb. A suitable foam catalyst structure has from 30 to 150 pores per inch (12 to 60 pores per centimeter). Alternative forms for the catalyst include refractory oxide honeycomb monolith structures, or other configurations having longitudinal channels or passageways permitting high space velocities with a minimal pressure drop. Such configurations and their manner of making are described, for example, in Structured Catalysts and Reactors, A. Cybulski and J.A. Moulijn (Eds.), Marcel Dekker, Inc., 1998, p. 599-615 (Ch. 21, X. Xu and J.A. Moulijn, "Transformation of a Structured Carrier into Structured Catalyst"). EXAMPLES Catalyst Preparation Exemplary catalysts were prepared as described below, and were tested for their activity in catalyzing the production of synthesis gas in a short contact time, or millisecond contact time reactor similar to that described by L.D. Schmidt and his colleagues at the University of Minnesota in U.S. Pat. No. 5,648,582 and in J. Catalysis 138, 267-282 (1992) for use in the production of synthesis gas by direct oxidation of methane over a catalyst such as platinum or rhodium. The disclosures of those references are incoφorated herein by reference. The samples obtained from the following examples were evaluated at defined high gas hourly space velocities, temperature and pressure and the levels of CH 4 and O conversion and selectivities to CO and H 2 products were determined. Example 1: Co/Mg/O (Co:Mg =1.2) In a 4 L glass beaker was mixed 211.2 g Co(NO 3 ) 2 -6H 2 O and 371.8 g of Mg(NO 3 ) 2 -6H 2 O in 2332.2 g of H 2 O. To this mixture was added 340 mL of 20% NH 4 OH solution. The mixture was stirred for 90 minutes and then allowed to settle overnight. Solids were collected by centrifuge and then washed with deionized water. After drying at 110°C overnight, the solids were then ground to powder and calcined in air at 600°C for 2 hours. This procedure was repeated five times and products were combined. Powder X-ray diffraction analysis indicated spinel-like phase formation and MgO. For the puφoses of the present disclosure the term "spinel-like" refers to a mixed metal oxide that conforms to the molecular formula AB 2 O , where A and B represent the two metals forming the mixed metal oxide. Chemical analysis by inductively coupled plasma spectrometry gave 51.95% Co and 17.2%Mg. Example 2: Co/Mg/O (Co:Mg = 1) In a 4 L glass beaker was mixed 162.37 g Co(NO 3 ) 2 -6H 2 O and 285.97 g of Mg(NO 3 ) 2 -6H 2 O in 1794 g of H 2 O. To this mixture was added 285 mL of 20% NH 4 OH solution. The mixture was stirred for 60 minutes and then allowed to settle overnight. Solids were collected by centrifuge and then washed with deionized water. After drying at 110°C overnight, the solids were then ground to powder and calcined in flowing nitrogen at 550°C for 6 hours. Powder X-ray diffraction analysis indicated spinel-like phase formation and MgO. Chemical analysis by inductively coupled plasma spectrometry gave 32.20% Co and 12.80% Example 3: Co/Al/O (Co:Al = 0.4) In a 2 L Roto-Vap flask was mixed, 145.51 g of Co(NO 3 ) 2 -6H 2 O, 375.10 g of Al(NO 3 ) 3 -9H 2 O and 1000 mL H 2 O. After water removal, the sample was melted out of the flask, poured into a crystallizing dish and then calcined in air at 400°C for two hours. Powder X-ray diffraction analysis indicated spinel-like phase formation. Chemical analysis by inductively coupled plasma spectrometry gave 26.8% Co and 29.0% Al. Example 4: Co/Mg/O (Co:Mg = 2) In a 2 L Roto-Vap flask, 291.04 g of Co(NO 3 ) 2 -6H 2 O, 128.20 g of Mg(NO 3 ) 2 -6H 2 O and 1000 mL H 2 O was mixed together. After water removal, the sample was melted out of the flask, poured into a crystallizing dish and then calcined in air at 400°C for two hours. Powder X-ray diffraction analysis indicated a spinel-like phase formation and MgO. Chemical analysis by inductively coupled plasma spectrometry gave 51.5% Co and 11.4% Mg. Example 5: Co-Al-Substituted hydrotalcite Added a solution containing 10.5 kg Co(NO 3 ) 2 -6H 2 O, 6.77 kg Al(NO 3 ) 3 -9H 2 O and 50.52 kg H 2 O to one containing 10.10 kg NaOH (50%), Na 2 CO 3 and 36.08 kg H 2 O slowly over a 4 hour period maintaining the mixture at 35°C. After the addition, the container was held at 35 °C for 30 minutes, then raised to 65°C and held for 18 hours after which the container was cooled to room temperature. The mixture was filtered, washed and dried at 85°C in a vacuum oven with nitrogen purge. Powder X-ray diffraction analysis showed the presence of Co 6 Al 2 (OH)ι CO 3 4H O. Chemical analysis by inductively coupled plasma spectrometry gave 38.2% Co, 7.48% Al, and 0.72% Na. Example 6: Co/Al/O (Co.Al = 1.7) In a 2 L Roto-Vap flask was mixed, 291.04 g of Co(NO 3 ) 2 -6H 2 O, 187.60 g of Al(NO 3 ) 3 -9H O and 1000 mL H 2 O. After water removal, the sample was melted out of the flask, poured into a crystallizing dish and then calcined in air at 400°C for two hours. Powder X-ray diffraction analysis indicated spinel-like phase formation. Chemical analysis by inductively coupled plasma spectrometry gave 50.0%) Co and 13.7% Al . Example 7: Co/Mg/O (Co:Mg = 3) A solution containing 84.2 g of Mg(NO 3 ) 2 -6H 2 O in 100 mL H2O was added to 92.03 g of Co 3 O (Alfa, Lot Number A24F29). The mixture was heated in air at 60°C/hour to 400°C and held for 2 hours at 400°C. The resulting material was calcined in air at 600°C for 2 hours. Powder X-ray diffraction analysis indicated spinel-like phase formation and MgO. Chemical analysis by inductively coupled plasma spectrometry gave 59.5% Co and 8.01% Mg. Example 8: CoAl 2 O 4 A sample was obtained from Alfa Aesar (Lot Number B05J32). X-ray diffraction analysis showed the presence of CoAl 2 O . Example 9: Co/Ni/Na/Al/O In a 3 L round bottom flask, a mixture containing 140 g NaOH, 50 g Na 2 CO 3 and 500 mL H O was added dropwise over a 4.2 hour period to one containing 145.52 g Ni(NO 3 ) 2 -6H 2 O, 145.52 g Co(NO 3 ) 2 -6H 2 O, 93.75 g Al(NO 3 ) 3 -9H 2 O and 700 mL H 2 O with stirring. The resulting mixture was heated at 65°C for 18 hours. After cooling, solids were recovered by centrifugation, washed with H 2 O, and dried at 110°C overnight. The dried solids were ground and then calcined in air by heating 60°C/h to 550°C, holding at 550°C for 10 hours. . Powder X-ray diffraction analysis indicated spinel-like phase formation as a primary phase. Chemical analysis by inductively coupled plasma spectrometry gave 25.4% Co, 28.4% Ni, 5.84% Al, and 7.02%Na. Example 10: Co/La/Zr/O 31.5 g of Co(NO ) 2 »6H 2 O was dissolved in 500 ml water. 100 g of La-doped zirconium hydroxide (MEI XZO 681/01) was added and stirred for 1 hour. The slurry was filtered without washing. The solid was dried at 135°C, and then pressed into pellets. The pellets were heated 4 hours at 600°C, and then crushed into 6-16 mesh granules. Chemical analysis by inductively coupled plasma spectrometry gave 2.87% Co, 3.06% La, and 59.6% Zr. Example 11: Co/La/Al/O In a Roto-Vap flask was mixed,500 mL 1M La(NO 3 ) 3 -6H 2 O, 200 mL 1M Al(NO 3 ) 3 -9H 2 O, and 100 mL 1 M Co(NO 3 ) 2 -6H 2 O. The mixture was evaporated to 200 mL, poured into a crucible and dried at 1 10°C in a vacuum oven for 6 days. The resulting material was calcined at 325°C for 24 hours, ground to a powder, and then calcined at 1000°C for 96 hours. Example 12: Co/Ca/O In a 2 L Roto-Vap flask was mixed, 291.04 g of Co(NO 3 ) 2 -6H 2 O, 118.08 g of Ca(NO 3 ) 2 -4H 2 O and 1000 mL H 2 O. After water removal, the sample was melted out of the flask, poured into a crystallizing dish and then cacined in air at 400°C for two hours. Powder X-ray diffraction analysis indicated spinel-like phase formation. Chemical analysis by inductively coupled plasma spectrometry gave 30.4% Co and 12.8% Ca. Example 13: Co/La/AVO In a Roto-Vap flask was mixed,500 mL 1M La(NO 3 ) 3 -6H 2 O, 200 mL 1M Al(NO 3 ) 3 -9H 2 O, and 100 mL 1 M Co(NO 3 ) 2 -6H 2 O. The mixture was evaporated to 200 mL, poured into a crucible and dried at 110°C in a vacuum oven for 6 days. The resulting material (123.75 g) was calcined at 325°C for 24 hours, ground to a powder, and then calcined at 900°C for 96 hours. Chemical analysis by inductively coupled plasma spectrometry gave 6.33% Co, 45.0% La, and 5.42% Al. Example 14: 2%Co/Al 2 O 3 8.47 g of CoCl 2 -6H 2 O were dissolved in 184 mL H 2 O. 105 g gamma-alumina (dried at 110°C overnight) were added with stirring to the CoCl 2 solution. The water was evaporated off by heating on a hot plate at approximately 90°C. The catalyst was stirred every 10 to 15 minutes until dry. Example 15: Co/Zn/O In a 2 L Roto-Vap flask was mixed, 291.04 g of Co(NO 3 ) 2 -6H 2 O, 148.74 g of Zn(NO 3 ) -6H 2 O and 1000 mL H 2 O. After water removal, the sample was melted out of the flask, poured into a crystallizing dish and then calcined in air at 400°C for two hours. Powder X-ray diffraction analysis indicated spinel-like phase formation and ZnO. Chemical analysis by inductively coupled plasma spectrometry gave 42.2% Co and 25.6% Zn. Comparative Example A: C0 3 O4 In a 2 L Roto-Vap flask was mixed, 436.6 g of Co(NO 3 ) 2 -6H 2 O and 1000 mL H 2 O. After water removal, the sample was melted out of the flask, poured into a crystallizing dish and calcined in air at 400°C for two hours. Powder X-ray diffraction showed the presence of Co 3 O 4 Chemical analysis by inductively coupled plasma spectrometry gave 67.6% Co. Comparative Example B: CoO A sample of Cobalt(II) oxide was obtained from Alfa (lot number 100377) and granulated to -20/+40 mesh. Powder X-ray diffraction analysis showed the presence of CoO. Test Procedure for Examples 1-15 and Comparative Examples A andB: The catalysts were evaluated in a laboratory scale short contact time reactor, a 25 cm long x 4 mm i.d. quartz tube reactor equipped with a co-axial quartz thermocouple well. The void space within the reactor was packed with quartz chips. The catalyst bed was positioned with quartz wool at about the mid-length of the reactor. The catalyst bed was heated with a 4 inch (10.2 cm) 600 watt band furnace at 90% electrical output. All runs were done at a CH 4 :O 2 molar ratio of 2:1 and at a pressure of 5 psig (136 kPa). The reactor effluent was analyzed using a gas chromatograph equipped with a thermal conductivity detector. The C, H and O mass balance were all between 98% and 102%. The runs were conducted over two operating days with 6 hours of run time each day. The comparative results of these runs are shown in Table 1, wherein gas hourly space velocity is indicated by "GHSV." As shown in Table 1, no evidence of catalyst deactivation occurred after 12 hours. Table 1 Ex. Vol Wt. Temp GHSV %CH_j/O 2 %CO/H 2 H 2 :CO fmL) fe) rø xlO 4 Conv. Sel. Ratio 1 1.2 0.9611 806 10.2 96/100 98/97 1.98 2 2.0 0.9013 780 6.1 95/100 98/97 1.98 3 2.0 1.1711 735 6.1 94/100 99/99 2.00 4 1.5 1.9275 670 8.1 93/100 97/97 2.00 5 2.0 1.2364 791 6.1 93/100 97/97 2.00 6 0.4 0.6065 782 30.4 90/100 95/95 2.00 7 1.4 1.1901 806 8.7 89/100 95/93 1.96 8 2.0 2.7610 782 6.1 89/100 95/93 1.96 9 2.0 2.5467 798 6.1 86/100 94/94 2.00 10 0.8 1.0675 750 15.2 85/100 93/88 1.89 11 0.7 0.9994 583 6.1 85/100 97/93 1.92 12 1.6 1.9054 750 7.6 83/100 92/91 1.98 13 2.0 2.1324 750 6.1 81/100 93/92 1.98 14 1.7 1.2404 641 7.2 81/100 93/90 1.94 15 1.6 2.3868 755 7.6 78/100 91/89 1.96 A 1.0 0.9820 939 12.2 52/100 81/58 1.43 B 1.1 2.1458 774 11.0 32/76 63/44 1.40 Feed: 30% CH 4 , 15% 0 2 , 55% N 2 Comparative Examples A and B serve as comparative examples demonstrating that the Co oxides, themselves, are not as effective in catalyzing the partial oxidation of methane to syngas. As the data entries in Table 1 indicate, methane conversion and syngas selectivity are significantly lower for those runs which were catalyzed by Co 3 O 4 and CoO. Example 18: 12%(Co/Al/O)/PSZ The powder catalyst prepared in Example 3 was first ground to less than 325 mesh, then 1.3909g of H 2 O was added to the powder (0.3173 g) in a glass vial to form a slurry. A PSZ foam (12mm OD x 10mm of 80ppi) from Vesuvius Hi-Tech Inc. was dipped into the slurry and saturated for 5 minutes. The foam was removed from the vial and the slurry remained in the pores of the foam was removed by blowing some compressed air. Finally, the foam was dried at 100°C for 2 hours. Example 19: 9% (Co/Mg/O)/PSZ The powder catalyst prepared in Example 4 was first ground to less than 325 mesh, then 1.2370g of H O was added to the powder (0.3067g) in a glass vial to form a slurry. A PSZ foam (12mm OD x 10mm of 80ppi) from Vesuvius Hi-Tech Inc. was dipped into the slurry and saturated for 5 minutes. The foam was removed from the vial and the slurry remained in the pores of the foam was removed by blowing some compressed air. Finally, the foam was dried at 100°C for 2 hours Example 20: 12%(Co/Al/O), 4%MgO/PSZ A PSZ foam (12mm OD x 10mm of 80ppi) from Vesuvius Hi-Tech Inc. was coated with 4 wt.% MgO by dripping a solution of Mg( NO 3 ) 2 6H 2 O (0.40g) in H 2 O (1.25g) to saturation, evaporating off the solvent at room temperature, drying at 110°C overnight and calcining at 900°C for 2 hours. The powder catalyst prepared in Example 3 was first ground to less than 325 mesh, then 1.3026g of H 2 O was added to the powder (0.2965g) in a glass vial to form a slurry. The MgO coated PSZ foam was dipped into the slurry and saturated for 5 minutes. The foam was removed from the vial and the slurry remained in the pores of the foam was removed by blowing some compressed air. Finally, the foam was dried at 100°C for 2 hours. Example 21: 14%(Co-AI-Substituted hydrotalcite) /PSZ The powder catalyst prepared in Example 5 was first ground to less than 325 mesh, then 1.2271g of H 2 O was added to the powder (0.2800g) in a glass vial to form a slurry. A PSZ foam (12mm OD x 10mm of 80ppi) from Vesuvius Hi-Tech Inc. was dipped into the slurry and saturated for 5 minutes. The foam was removed from the vial and the slurry remained in the pores of the foam was removed by blowing some compressed air. Finally, the foam was dried at 100°C for 2 hours. Test Procedure for Examples 18-21 The partial oxidation reactions were done with a conventional flow apparatus using a 19 mm O.D. x 13 mm I.D. and 12" long quartz reactor. A ceramic foam of 99% Al 2 O 3 (12 mm OD x 5 mm of 45 ppi) were placed before and after the catalyst as radiation shields. The inlet radiation shield also aided in uniform distribution of the feed gases. An Inconel sheathed, single point K-type (Chromel/Alumel) thermocouple (TC) was placed axially inside the reactor touching the top (inlet) face of the radiation shield. A high temperature S- Type (Pt/Pt 10% Rh) bare-wire TC was positioned axially touching the bottom face of the catalyst and was used to indicate the reaction temperature. The catalyst and the two radiation shields were sealed tight against the walls of the quartz reactor by wrapping them radially with a high purity (99.5%) alumina paper. A 600 watt band heater set at 90% electrical output was placed around the quartz tube, providing heat to light off the reaction and to preheat the feed gases. The bottom of the band heater corresponded to the top of the upper radiation shield. In addition to the TCs placed above and below the catalyst, the reactor also contained two axially positioned, triple-point TCs, one before and another after the catalyst. These triple-point thermocouples were used to determine the temperature profiles of reactants and products subjected to preheating and quenching, respectively. All runs were done at a CIr_ :O 2 molar ratio of 2:1 with a combined flow rate of 2.5 standard liters per minute (SLPM) or 134,000/h gas hourly space velocity (GHSV) and at a pressure of 5 psig (136 kPa). The reactor effluent was analyzed using a gas chromatograph equipped with a thermal conductivity detector. The C, H and O mass balance were all between 98% and 102%). TABLE 2 Syngas Production by Cobalt-based Catalysts Example 22. Co-MgO/PSZ A Co-MgO solid solution catalyst supported on PSZ was prepared according to the following procedure (amounts given are for laboratory-scale batches): 4.3024 grams of Mg(NO 3 ) 2 .6H 2 O (Aldrich 23,717-5) was dissolved in 4.1652 grams of distilled and deionized (DDI) water at about 50°C. This solution was added to a PSZ foam 12-mm diameter x 10-mm long, weighing 1.9245 grams. The wet PSZ foam was dried at about 70°C and calcined in air according to the following schedule: 10°C/min ramp up to 500°C; hold at 500°C for 2 hours; 10°C/min ramp down to room temperature. The above procedure was repeated until 13 wt% MgO, based on the weight of PSZ foam, was obtained. 0.75 gram of Co(NO 3 ) 2 .6H 2 O (Aldrich 23,926-7) was dissolved in 1.86 grams of DDI water at about 50°C and added to the MgO-coated PSZ foam at about 70°C. The wet MgO-loaded PSZ foam was dried at about 70°C and calcined in air according to the following schedule: 5°C/min ramp up to 200°C; hold at 200°C for 1 hour; 5°C/min ramp up to 400°C; hold at 400°C for 1 hour; 5°C/min ramp up to 800°C; hold at 800°C for 12 hours; 10°C/min ramp down to room temperature. The resulting material contained a Co oxide loading of 0.1684 gram or 8.75 wt% based on the weight of PSZ foam. The catalyst was reduced with H 2 using 1 : 1 by volume flow of N 2 :H 2 mixture at 0.3 standard liter per minute (SLPM) measured at 0°C and 1 atm pressure, using the following schedule: 5°C/min ramp up to 125°C; hold at 125°C for 0.5 hour; 5°C/min ramp up to 500°C; hold at 500°C for 3 hours; 5°C/min ramp down to room temperature. This catalyst had an estimated loading of 0.0687 g. Mg and 0.0626 g. Co based on the respective oxide weights. Calculated as metal wt% based on the final catalyst weight, the final catalyst had 5.7 wt% Co, 6.4 wt% Mg. Example 23. (Pt/Co/MgO)/PSZ A Co-MgO solid solution catalyst supported on PSZ was prepared according to the following procedure (amounts given are for laboratory-scale batches): 6.0664 grams of Mg(NO 3 ) 2 .6H 2 O (Aldrich 23,717-5) was dissolved in 5.2249 grams of distilled and deionized (DDI) water at about 50°C. One-third of this solution was added to a PSZ foam 12- mm diameter x 10-mm long, weighing 0.8628 gram. The wet PSZ foam was dried at about 70°C and calcined in air according to the following schedule: 5°C/min ramp up to 500°C; hold at 500°C for 2 hours; 10°C/min ramp down to room temperature. The above procedure resulted in 12.33 wt% MgO, based on the weight of PSZ foam. 0.66 gram of Co(NO 3 ) 2 .6H 2 O (Aldrich 23,926-7) was dissolved in 1.5 grams of DDI water at about 50°C and added to the MgO-coated PSZ foam at about 70°C. The wet MgO-loaded PSZ foam was dried at about 70°C and calcined in air according to the following schedule: 5°C/min. ramp up to 200°C; hold at 200°C for 1 hr.; 5°C/min. ramp up to 400°C; hold at 400°C for 1 hr.; 5°C/min. ramp up to 800°C; hold at 800°C for 12 hrs.; 10°C/min. ramp down to room temperature. . The above procedure resulted in 0.0876 gram or 11.15 wt% CoO, based on the weight of PSZ foam.. Addition of platinum was done as follows: 0.16 g. Pt(NH 3 ) 4 (NO 3 ) 2 (Aldrich 27,872- 6) was dissolved in 0.3 g. of distilled and deionized (DDI) water at about 70°C and added to the CoO-MgO-coated PSZ foam, also at about 70°C. The wet foam was dried at about 70°C on a hotplate for about 2 hrs. and then calcined in air according to the following schedule: 5°C/min. ramp up to 110°C; hold at 125°C for 1/2 hr.; 5°C/min. ramp up to 250°C; hold at 250°C for 2 hr.; 10°C/min. ramp down to room temperature. The resulting material contained a Pt oxide loading of 0.0022 g., corresponding to a loading of 0.25% based on the weight of PSZ foam. Based on the total weight of the catalyst after calcination, the composition was: 0.15%) Pt, 6.5 % Co and 6.1%) Mg. The catalyst was reduced with H 2 using a 1 :1 (by volume) flow of N 2 :H 2 mixture at 0.2 standard liters per minute (SLPM) measured at 0°C and 1 atm pressure, using the following schedule: 3°C/min. ramp up to 125°C; hold at 125°C for 0.5 hr; 3°C/min. ramp up to 500°C; hold at 500°C for 3 hrs; 5°C/min. ramp down to room temperature. Other promoters including Ni, Mn, La, Cu, Sm, Yb, Eu, Pr, Ce, Y, Rh, and Re may be substituted for Pt in the procedure to provide additional active syngas catalysts. These catalysts are made as described above, but substituting the corresponding metal salt solution for the Pt(NH 3 ) 4 (NO 3 ) 2 solution. Other refractory catalyst support materials may be substituted for PSZ, such as cordierite honeycomb or alpha-alumina foam having about 40-400 pores per inch (ppi) density. Test Procedure for Examples 22-23 Preferred syngas catalysts comprise catalytically active cobalt-containing components supported on a ceramic monolith porous carrier such as partially stabilized zirconia (PSZ) foam (stabilized with Mg, Y or Ca). PSZ foams have been described in the literature (e.g., U.S. Patent No. 4,835,123 (Bush et al.)) and are commercially available from suppliers such as Vesuvius Hi-Tech Ceramics Inc., Alfred Station, New York. Alternatively the catalyst support may be α-alumina foam (also stabilized with Zr) or "honeycomb" straight channel extrudate made of cordierite or mullite. In the present series of tests, the catalyst support was a laboratory-scale ceramic monolith comprising porous PSZ foam with approximately 6,400 channels per square inch (80 pores per linear inch). The monolith was cylindrical overall, with a diameter corresponding to the inside diameter of the reactor tube and the length varying from 1/8" to 1-1/2". These catalysts were tested substantially as described in the section entitled Test Procedure for Examples 18-21, using a feed containing natural gas or methane and oxygen in the molar ratio of from 1.7:1 to 2.3:1 (CH 4 :O 2 ratio) at a total GHSV of from 61,000 1/h to 1,000,000 1/h in the laboratory-scale reactor (at 5-15 psig) and pilot unit (at 15-400 psig) testing. The laboratory-scale tests used methane and oxygen feed, while the pilot unit tests used natural gas and oxygen feed. Reacted gases were analyzed for content of CFL*, O 2 , CO, H 2 , CO 2 , and, optionally, other components. The results of those tests are shown in Table 3. Table 3 Performance of Co-MgO Supported on PSZ foam Example Composition CH<:0 2 Combined Pressure Preheat Catalyst %CH 4 .%0- %CO/%H 2 H 2 :CO molar feed ratio Flowrate Temp. Temp. Conv. Sel. in GHSV 22 5.7 wt% Co, 6.3 wt% Mg 1.75 192,300 5 psig 150°C 840°C 93/100 96/90 1.7 22 5.7 wt% Co, 6.3 wt% Mg 1.75 391,200 7 psig 150°C 910°C 85/100 96/84 1.6 23 0.15 wt% Pt, 6.5 wt% Co, 6.1 wt% Mg 2.00 1,300,000 45 psig 488°C 1094°C 81/100 93/67 1.7 \D Compared to the performance of the catalyst of Example 19, it can be seen that an unpromoted Co-MgO catalyst prepared by the multi-step loading procedure and having a composition as in Example 22 resulted in higher levels of CH4 conversion and selectivity for CO and H 2 products operating at higher space velocities than in Example 19. Inclusion of very small amounts of Pt in the catalyst, prepared as described in Example 23, has the effect of lowering the light off temperature while not increasing the reaction temperature, at pressures as high as 45 psig and flow rates as high as 1.3 million GHSV. In addition, this catalyst showed excellent resistance to coking and Co metal loss by volatilization over 9 days, normally observed with unpromoted Co-based catalysts at higher flowrates. Excellent levels of conversion of methane and oxygen reactants and selectivities for CO and H 2 products by a predominantly, or net catalytic partial oxidation reaction are achievable by the new catalyst devices in a short contact time reactor. The term "net catalytic partial oxidation" means that the partial oxidation reaction of Equation 2 predominates over reforming reactions, and the molar ratio of the H 2 :CO products is preferably about 2:1. Although not wishing to be bound by a particular theory, the inventors believe that the primary reaction catalyzed by the preferred catalysts described herein is the partial oxidation reaction of Equation 2. Other chemical reactions may also occur, but to a lesser extent, catalyzed by the same catalyst device, to yield an overall or net partial oxidation reaction. For example, in the course of syngas generation, intermediates such as CO 2 + H 2 O may occur as a result of the oxidation of methane, followed by a reforming step to produce CO and H 2 . Also, particularly in the presence of carbon dioxide-containing feedstock or CO 2 intermediate, the reaction shown in Equation 3 CH 4 + CO 2 → 2 CO + 2H 2 (3) may also occur to some extent during the production of syngas, in which case the molar ratio of the H 2 and CO products is somewhat less than the preferred Fischer-Tropsch stoichiometric molar ratio of 2:1 H 2 :CO. Process for Producing Syngas The reactants are contacted with the catalyst in a fixed bed configuration in the reaction zone of a millisecond contact time reactor. Particles of the catalyst or supported catalyst are retained in the reaction zone using fixed bed techniques well known in the art. Alternatively, a catalyst device, or impregnated monolith, prepared as described above, is employed. The catalyst or catalyst device preferably has sufficient permeability or porosity to permit a stream of said reactant gas mixture to pass over it at a gas hourly space velocity of at least about 20,000 NL/kg/hr, when the reactor is operated to produce synthesis gas. A feed stream comprising a hydrocarbon feedstock and an oxygen-containing gas is contacted with one of the above-described catalysts comprised of cobalt metal and or cobalt containing compound(s) in a reaction zone maintained at conversion-promoting conditions effective to produce an effluent stream comprising carbon monoxide and hydrogen. The hydrocarbon feedstock is any gaseous hydrocarbon having a low boiling point, such as methane, natural gas, associated gas, or other sources of light hydrocarbons having from 1 to 5 carbon atoms. For example, the hydrocarbon feedstock may be a gas arising from naturally occurring reserves of methane, and may also contain carbon dioxide. Preferably, the feed comprises at least 50% by volume methane, more preferably at least 75% by volume, and most preferably at least 80% by volume methane. The hydrocarbon feedstock is in the gaseous phase when contacting the catalyst. The hydrocarbon feedstock is contacted with the catalyst as a mixture with an oxygen-containing gas, preferably pure oxygen. The oxygen- containing gas may also comprise steam and or CO 2 in addition to oxygen. Alternatively, the hydrocarbon feedstock is contacted with the catalyst as a mixture with a gas comprising steam and/or CO 2 . The preheated feed gases pass over or through the monolith or catalyst device to heat the catalytic materials to the point at which they ignite and start the reaction. A net partial oxidation reaction ensues, and the reaction conditions are maintained to promote continuation of the autothermal process. For the puφoses of this disclosure, "autothermal" means that after catalyst ignition, no additional heat is supplied to the catalyst in order for the production of synthesis gas to continue. Autothermal reaction conditions are promoted by optimizing the concentrations of hydrocarbon and O in the reactant gas mixture. Preferably the methane-containing feed and the oxygen-containing gas are mixed in such amounts to give a carbon to oxygen (i.e., O 2 ) molar ratio from about 1.25:1 to about 3.3:1, more preferably, from about 1.3:1 to about 2.2:1, and most preferably from about 1.5:1 to about 2.2:1, especially the stoichiometric ratio of 2:1. The hydrocarbomoxygen (i.e., O 2 ) molar ratio of the reactant gas mixture is an important variable for maintaining the partial oxidation reaction and the desired product selectivities. Residence time, amount of feed preheat and amount of nitrogen dilution, if used, also affect the selectivity and yield of reaction products. The dwell time or residence time of the portion of gas mixture in contact with the catalyst is preferably maintained at no more than about 10 milliseconds. This ultra short contact time is accomplished by passing the reactant gas mixture over or through one or more of the above-described cobalt-containing catalyst devices at a space velocity of about 20,000 to about 100,000,000 normal liters of gas per kilogram of catalyst per hour (NL/kg/h). Preferably the space velocity is about 50,000 to about 50,000,000 NL/kg/h. The process is operated at atmospheric or superatmospheric pressures, the latter being preferred. The pressures may be from about 100 kPa to about 12,500 kPa, preferably from about 130 kPa to about 10,000 kPa. The process is preferably operated at temperatures of from about 60°C to about 1,200°C, preferably from about 700°C to about 1,100°C. The hydrocarbon feedstock and the oxygen-containing gas are preferably pre-heated at about 60°C - 700°C, preferably from about 100°C to about 500°C, before contact with the catalyst. The hydrocarbon feedstock and the oxygen-containing gas are passed over the catalyst at any of a variety of space velocities. The product gas mixture emerging from the reactor is collected and may be routed to a syngas-consuming process such as a Fischer-Tropsch operation. While the preferred embodiments of the invention have been shown and described, modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. The embodiments described herein are exemplary only, and are not intended to be limiting. Many variations and modifications of the invention disclosed herein are possible and are within the scope of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims which follow, that scope including all equivalents of the subject matter of the claims. The disclosure of U.S. Provisional Patent Application No. 60/165,981 filed November 17, 1999 and all patents and publications cited herein are incoφorated by reference.

Claims: CLAIMS What is claimed is: 1. A syngas catalyst device comprising cobalt metal and/or at least one oxidizable cobalt containing compound and a support structure comprising a substance chosen from the group consisting of hydrotalcites, spinels, perovskites, magnesium oxide, pyrochlores, brownmillerites, zirconium phosphate, magnesium stabilized zirconia, zirconia stabilized alumina, silicon carbide, yttrium stabilized zirconia, calcium stabilized zirconia, yttrium aluminum garnet, alumina, lanthanum oxide, cordierite, mullite, LaZrO 2 , ZrO 2 , ZnO, LaAlO 3 , MgAl 2 O 4 , SiO 2 and TiO 2 . 2. The catalyst device of claim 1 comprising cobalt metal and/or said at least one cobalt containing compound disposed on said support structure. 3. The catalyst device of claim 1 wherein said support structure comprises a substance chosen from the group consisting of hydrotalcites, spinels, perovskites, magnesia, LaZrO , Al 2 O 3 , and lanthanum oxide, and said cobalt metal and/or said at least one cobalt containing compound is incoφorated into said support structure. 4. The catalyst device of claim 1 wherein said substance comprises at least one refractory metal oxide. 5. The catalyst device of claim 1 wherein said support structure comprises a refractory ceramic foam. 6. The catalyst device of claim 5 wherein said foam structure comprises about 12-60 pores per centimeter of structure. 7. The catalyst device of claim 4 wherein said support structure comprises a honeycomb monolith structure. 8. The catalyst device of claim 1 wherein said cobalt metal and or said at least one cobalt containing compound comprises a mixture of cobalt metal and a metal oxide chosen from the group consisting of cobalt oxide and magnesium oxide, in the form of a solid solution. 9. The catalyst device of claim 1 comprising a spinel chosen from the group consisting of MgCo 2 O 4 and Mg CoO 4 . 10. The catalyst device of claim 1 comprising a spinel-like formation chosen from the group consisting of: Co/Mg/O and MgO, Co/Mg/O, Co/Al/O and Al 2 O 3 , and Co/Al/O. 11. The catalyst device of claim 1 comprising a compound chosen from the group consisting of CoAl 2 O 4 and Co 2 AlO 4 . 12. The catalyst device of claim 1 comprising a mixture of cobalt metal and/or cobalt oxide and Al 2 O 3 . 13. The catalyst device of claim 1 comprising a cobalt-containing hydrotalcite. 14. The catalyst device of claim 1 comprising a cobalt hydrotalcite having the formula Co 6 Al 2 (OH) 16 CO 3 • 4 H 2 O. 15. The catalyst device of claim 1 comprising cobalt metal and/or cobalt oxide supported on LaZrO 2 . 16. The catalyst device of claim 1 comprising cobalt metal and or cobalt oxide supported on lanthanum oxide doped zirconia. 17. The catalyst device of claim 1 comprising LaAl 8 Co 2 O 3 . 18. The catalyst device of claim 1 comprising a mixture of the metals and/or metal oxides of La, Al and Co. 19. The catalyst device of claim 1 comprising cobalt metal and/or cobalt oxide supported on a mixture of alumina and lanthanum oxide. 20. The catalyst device of claim 1 comprising a compound chosen from the group consisting of CaCo O and Ca 2 CoO 4 . 21. The catalyst device of claim 1 comprising a mixed metal oxide chosen from the group consisting of: Co/Ca/O, and Co/Ca/O and CaO. 22. The catalyst device of claim 1 comprising Co metal and/or cobalt oxide supported on CaO. 23. The catalyst device of claim 1 comprising a compound chosen from the group consisting of ZnCo O 4 and Zn 2 CoO 4 . 24. The catalyst device of claim 1 comprising a mixed metal oxide chosen from the group consisting of: Zn Co/O and ZnO, and Zn Co/O. 25. The catalyst device of claim 1 comprising cobalt metal and/or cobalt oxide supported on ZnO. 26. The catalyst device of claim 1 comprising a mixed metal oxide of Co/Ni/Na/Al/O. 27. The catalyst device of claim 1 comprising a mixture of metals and/or metal oxides chosen from the group consisting of Co, Ni, Na and Al, and oxides thereof. 28. A syngas catalyst device comprising cobalt metal and/or cobalt oxide, a promoter chosen from the group consisting of Mn, Ni, La, Cu, Sm, Yb, Eu, Pr, Ce, Y, Pt, Rh and Re, and a support structure chosen from the group consisting of alumina and partially stabilized zirconia. 29. The catalyst device of claim 28 comprising cobalt metal and/or cobalt oxide, magnesium oxide, platinum metal and/or platinum oxide and a partially stabilized zirconia support. 30. The catalyst device of claim 29 comprising about 0.15% Pt, about 6.5% Co and about 6.1% Mg. 31. A syngas catalyst prepared by impregnating a refractory metal oxide support with a solution of an oxidizable magnesium salt; calcining said magnesium impregnated support; impregnating said magnesium impregnated support with a solution of an oxidizable cobalt salt to provide a cobalt/magnesium oxide intermediate; calcining said cobalt/magnesium oxide intermediate; impregnating said cobalt/magnesium intermediate with a solution of an oxidizable promoter salt, said promoter chosen from the group of metals consisting of Mn, Ni, La, Cu, Sm, Yb, Eu, Pr, Ce, Y, Pt, Rh and Re, to provide a promoter/cobalt/magnesium oxide intermediate; calcining said promoter/cobalt/magnesium oxide intermediate; and reducing said calcined promoter/cobalt/magnesium oxide intermediate to provide a supported catalyst having activity for catalyzing the net partial oxidation of methane in the presence of O to CO and H 2 under reaction promoting conditions in a short contact time reactor. 32. A method of producing synthesis gas comprising: in a millisecond contact time reactor, passing a reactant gas mixture comprising a C \ - C 5 hydrocarbon and an O 2 -containing gas over the catalyst device of claim 1 , such that the contact time of a portion of said reactant gas mixture in contact with said catalyst device does not exceed about 10 milliseconds; maintaining net catalytic partial oxidation promoting conditions of hydrocarbon:O 2 molar ratio in said reactant gas mixture, catalyst temperature and reactant gas preheat temperature. 33. The method of claim 32 wherein said step of maintaining said net catalytic partial oxidation promoting conditions includes maintaining a catalyst temperature of about 600- 1,200°C. 34. The method of claim 32 further comprising mixing a methane-containing feedstock and an oxygen-containing feedstock to provide a reactant gas mixture feedstock having a hydrocarbon:O 2 molar ratio of about 1.25:1 to about 3.3:1. 35. The method of claim 34 wherein said mixing provides a reactant gas mixture feed having a hydrocarbon: O 2 molar ratio of about 1.5:1 to about 2.2:1. 36. The method of claim 35 wherein said mixing provides a reactant gas mixture feed having a carbo oxygen ratio of about 2:1. 37. The method of claim 32 wherein said O 2 -containing gas further comprises steam, CO 2 , or both. 38. The method of claim 32 further comprising mixing a hydrocarbon feedstock and a gas comprising steam and/or CO 2 to provide said reactant gas mixture. 39. The method of claim 32 wherein said C 1 -C 5 hydrocarbon comprises at least about 50 % methane by volume. 40. The method of claim 32 further comprising preheating said reactant gas mixture. 41. The method of claim 32 wherein said step of passing said reactant gas mixture over said catalyst device comprises passing said reactant gas mixture over said catalyst device at a space velocity of about 20,000 to about 100,000,000 normal liters of gas per kilogram of catalyst per hour (NL/kg/h). 42. A method of producing synthesis gas comprising: in a millisecond contact time reactor, passing a reactant gas mixture comprising a C]- C 5 hydrocarbon and an O 2 -containing gas over the catalyst device of claim 28, such that the contact time of a portion of said reactant gas mixture in contact with said catalyst device does not exceed about 10 milliseconds; maintaining net catalytic partial oxidation promoting conditions of hydrocarbon:O molar ratio in said reactant gas mixture, catalyst temperature and reactant gas preheat temperature. 43. The method of claim 42 wherein said step of maintaining said reaction promoting conditions includes maintaining a catalyst temperature of about 600-l,200°C. 44. The method of claim 42 wherein said step of maintaining net catalytic partial oxidation promoting conditions comprises mixing a methane-containing feedstock and an O 2 - containing feedstock to provide a reactant gas mixture having a hydrocarbon: O 2 molar ratio of about 1.25:1 to about 3.3:1. 45. The method of claim 44 wherein said mixing provides a reactant gas mixture feed having a hydrocarbon :O 2 molar ratio of about 1.5:1 to about 2.2:1. 46. The method of claim 45 wherein said mixing provides a reactant gas mixture feed having a hydrocarbon :O 2 molar ratio of about 2:1. 47. The method of claim 41 wherein said O 2 -containing gas further comprises steam, CO 2 , or both. 48. The method of claim 41 further comprising mixing a hydrocarbon feedstock and a gas comprising steam and/or CO 2 to provide said reactant gas mixture. 49. The method of claim 41 wherein said C 1 -C 5 hydrocarbon comprises at least about 50 % methane by volume. 50. The method of claim 41 further comprising preheating said reactant gas mixture. 51. The method of claim 41 wherein said step of passing said reactant gas mixture over said catalyst device comprises passing said reactant gas mixture over said catalyst device at a space velocity of about 20,000 to about 100,000,000 normal liters of gas per kilogram of catalyst per hour (NL/kg/h). 52. A method of converting a C1-C5 hydrocarbon comprising at least about 50 vol% methane to a product gas mixture comprising CO and H 2 , the process comprising: mixing a methane-containing feedstock and an O 2 -containing feedstock to provide a reactant gas mixture having a hydrocarbon: O 2 ratio of about 1.25 : 1 to about 3.3:1; passing said reactant gas mixture over a catalyst device comprising cobalt metal and/or cobalt oxide, optionally, a promoter chosen from the group consisting of Mn, Ni, La, Cu, Sm, Yb, Eu, Pr, Ce, Y, Pt, Rh, and Re, and a catalyst support structure comprising a substance chosen from the group consisting of partially stabilized zirconia, hydrotalcites, spinels, perovskites, magnesia, LaZrO 2 , alumina, and lanthanum oxide; passing said reactant gas mixture feedstock over said catalyst at a space velocity of about 20,000 to about 100,000,000 normal liters of gas per kilogram of catalyst per hour (NL/kg/h), such that the contact time of a portion of said reactant gas mixture in contact with said catalyst device is no more than about 10 milliseconds; maintaining the temperature of said catalyst device at about 600-l,200°C; and, optionally, preheating said reactant gas mixture.

Inventors: CORBIN DAVID, GAFFNEY ANNE M, OSWALD ROBERT, SONG ROGER, CORBIN, DAVID, GAFFNEY, ANNE, M., OSWALD, ROBERT, SONG, ROGER
Applicants: CONOCO INC, CONOCO INC.
Application year: 2000
Main classification: C01B3
IPC codes: B01J23, C01B3