CATALYTIC PROCESS FOR CONVERTING CARBON MONOXIDE TO A HIGH ENERGY GAS

Abstract: A particulate, freeflowing, fluid-bed catalyst comprising a porous catalyst support having a surface area of greater than 1 to less than 350 m²/gm and a pore volume of 0.4 to 3.0 cc/gm and a Group VIII metal or mixture thereof on the pore surfaces of said support, said Group VIII metal or mixture being present in an amount equivalent to at least one atomic layer. This catalyst is capable of catalyzing carbon deposition and methanation reactions with high catalytic activity and has a combination of physical properties making it suitable for use in a conventional fluid-bed reactor.

Description: TITLE NOVEL CATALYTIC MATERIAL AND USE THEREOF FOR CONVERTING CARBON MONOXIDE TO A IIIGII ENERGY GAS This invention relates to a novel catalytic materials in particular of use in converting carbon monoxide to a high energy gas. Belgian Patent No. 869,185, issued January 22, 1979. (corresponding to U.S.S.N. 817,647, filed July 21, 1977 now abandoned, the disclosure of which is incorporated herein by reference) describes a novel catalytic material comprising carbon fibers containing small nodules of iron or another Group VIII metal. This material is formed by contacting the Group. VIII metal with a mixture of carbon monoxide and hydrogen at elevated temperature to cause deposition of carbon through the disproportionation of carbon monoxide. When the material so formed is contacted with hydrogen at elevated temperature, the carbon in the material reacts with the hydrogen to form methane. Repeated cycling between carbon deposition and methanation causes the catalystiematerialto exhibit high activity, i.e. high carbon deposition rates and high methaiiation rates. In addition to very high catalytic activity, this material exhibits other unusual properties. For example, the material undergoes drastic changes in volume between the carbon deposition and methanation steps. Thus, it has been found that the volume of the material at the end of a carbon deposition step can be as much as 20 times as great as the volume at the end of a methanation step. Also, it has been found that repeated carbon deposition/methanation cycling causes gradual pulverization of the Group VIII metal on which the carbon fiberes are grown. Also, the carbon fibers, especially when grown from pulverized metal produced by repeated cycling can exhibit extremely great expansive forces. For example, in one instance a stainless steel laboratory reactor was actually split open by the carbon fibers groom therein when the volume of the carbon fibers exceeded the internal volume of the reactor. Because of the high catalytic activity of this material, it has been proposed to use this material for the production of high BTU gas from coal. This would be accomplished by gasification of. the coal to produce producer gas and reacting the carbon monoxide in the producer gas in accordance with the above technique to produce methane. Unfortunately, the unusual properties of this material make it difficult or impossible to handle in conventional gasXsolid contacting apparatus such as fixed or fluid-bed reactors wherein a bed of the solid is continously contacted with a gas flowing therethrough. For example, in fixed bed operation, destruction of the reactor by growing too much carbon fiber material is always a possibility. Also, the powdery residue produced by repeated carbon deposition/methanation cycles tends to collect together and on subsequent carbon deposition steps the carbon/metal mass produced agglomerates and plugs the reactor inlets and outlets. In fluid-bed operation, it is necessary that the solid being contacted has a relatively specific particle size distribution and density. The vast changes in volume as well;as density of the material and the fragile nature of the carbon fibers makes the material totally unsuitable for fluid-bed operation. Accordingly, it is an object of the present invention to provide a new catalytic material which is also capable of catalyzing carbon deposition and methanation reactions with high catalytic activity but which also has a combination of physical properties making it amenable for use in a conventional fluid-bed reactor. We have found, surprisingly, that a dimensionally stable attrition resistant particulate material having a density and particle size distribution appropriate for use in a fluid-bed reactor and capable of catalyzing carbon deposition and methanation at high rates can be produced by impregnating a Group VIII metal into a conventional fluidbed catalyst support material having a special combination of properties. The present invention provides a particulate, freeflowing, fluid-bed catalyst comprising a porous catalyst support having a surface area of greater than 1 to less than 350m2/gm and a pore volume of 0.4 to 3.0 cc./gm. and a Group VIII metal on the pore surfaces of the support, the Group VIII metal being present in an amount equivalent to at least one atomic layer. The catalytic material according to the invention is composed of a porous fluid-bed support material having a specific combination of properties which is impregnated with iron or other Group VIII metal so that the metal is present on the inside surfaces of the particulate support, that is on the pore surfaces. Particles composed of a porous particulate material such as silica impregnated with iron are well known. In accordance with the invention, however, the nature of the pores must be precisely selected, that is the particles must exhibit a precise combination of properties due to the pores, in order that the catalytic material according to the invention will exhibit the necessary properties. If the support material does not exhibit the desired combination of properties, the resultant material will be ineffective as a catalyst eitterbecause it cannot catalyze the carbon deposition and/or methanation steps with appropriate catalytic activity or it will be dimensionally unstable. Support Material Porous, particulate, free-flowing catalyst support materials for use in making fluid-bed catalysts are well, known. Examples of such materials are silica, alumina, silica/alumina, zirconia, titania, hafnia, silicon carbide, boron phosphate, diatomaceous earth, pumice and so forth. In accordance with the invention, any such support material can be employed to make the catalytic material according to the invention provided that such support material has a surface area of greater than 1 to less than 2 350 m /gm., a pore volume of 0.4 to 3 cc./gm. and a particle size distribution and density appropriate for use as a fluid-bed material. Preferred are those supports having 2 a surfacedareaof 6 to 250 m /gm and pore volumes of 1 to 2 cc./gm. Even more preferred are supports having a surface area of 30 to 80 mê/gm. and a pore volume of 1 to 2 cc./gm. Especially preferred support materials are those as described above which are further characterized in containing no measurable pores having pore diameters less than 50, preferably less than 80, more preferably less than 100 angstroms when measured by the mercury porousimeter techniques. In accordance with this technique, which is described in H.M. Rootare and C.F. Prenzlow, Surface Area from Mercury Porousimeter Measurements, Journal of Physical Chemistry, 71, 2733 (1967), a mixture of mercury and the porous material to be tested is subjected to increasing pressure whereby mercury is forced into the pores of the material. A decrease in volume of the mixture corresponds to the amount of mercury taken up by the pores of the material. As the diameter of the pores decreases, greater pressure is needed to force mercury into the pores, and this relationship (pressure versus pore diameter) is known. Thus measurement of the pressure at any one point of time as the mixture is being subjected to increasing pressure indicates the diameter of the pores being filled with mercury at that point in time. In accordance with the preferred embodiment of the invention, porous support particles are used which show no measurable pores having a pore- diameter of less than 50 angstroms, preferably 80 and more preferable 100 angstroms. This is reflected by the fact that once the pressure corresponding to 50 (or 80 or 100) angstroms is reached, there is no more volume decrease and hence no more uptake of mercury by the pores of the support even if the pressure is further increased. This does not mean that the particles contain no pores having a pore diameter of 50 angstroms or less, but rather just that the mercury porousimeter technique is unable to measure the presence of such pores. Although not wishing to be bound to any theory, it is believed that the importance of the above surface area and pore volume restrictions relates to the elimination of extremely small pores from the support particles. This is reinforced by the further positive restriction that no measurable pores of the pore sizes indicated above be present. If carbon were allowed to grow in extremely small pores in the support particles, it would soon fill up these pores. Continued growing of the carbon would cause high stresses to be exerted on the particle skeleton which would ultimately lead to fracturing of the particles. Hence, by eliminating the very small pores, the tendency of the particles to break up because of the high compressive stresses developed when the carbon material outgrows its growing space is eliminated. It is not known whether or not particulate support material having the combination of properties set forth above is readily available. These materials, however, can be easily produced by known processing techniques from support materials which are readily available. For example, the preferred support material of the present invention is porous particular silica which is produced by subjecting a commercially available porous particulate silica to a hydrothermal technique to adjust the pores to the desired eonfiguration. The commercially available silica used in this technique has the properties and characteristics as set forth in the following Table I. TABLE I CHEMICAL COMPOSITION: Loss in ignition (1 hr. 1000"C) 4.5 0% wb Al203 0.3 3 % db Na2O 0.07 % db SO4 ouzos % db Fe 0.03 % db PHYSICAL PROPERTIES: Apparent Bulk Density 0.38 g/ml Compacted Bulk Density 0.47 g/ml Surface Area 645 mê/g Pore Volume - H20 (6000 C) 1.07 ml/g PARTICLE SIZE DISTRIBUTION: : (micromesh - square holes) - 149 micron 98.5 % - 105 micron 95.5 % - 90 micron 90.5 % - 45 micron 32 % - 30 micron 10 % - 20 micron 1.5 % This material is processed into the preferred support material of the present invention by the following procedure. 40 gms. of the above material is placed in a 300 cc. glass autoclave liner with 100 cc. of dilute aqueous K2CO3 solution. The autoclave is then brought to 23000 and maintained at that temperature for 30 minutes The pressure at this point is 400 psig. (28 kg/cm2). At 30 minutes, the autoclave is rapidly cooled. The silica is then removed from the reactor, washed three times with 100 ml. aliquots of distilled water and then dried-overnight in air at 11000. The porous, particulate free-flowing silica product made in this manner exhibits a surface area of 53 m2/gm. (N2 adsorption technique), a pore volume (measured by the porousimeter technique) of 1.22 cc./gm. and no measurable pores with pore diameter less than 150 angstroms when measured by the mercury porousimeter technique The above hydrothermal technique serves to reduce the surface area of the silica starting material, presumably through elimination of extremely small pores. Other techniques are known which will reduce surface area and otherwise adjust the pore structure of fluid-bed support materials, and any such technique can be employed in connection with suitable starting materials. For example, it is known that impregnation of a high surface area support material such as silica or alumina with ammonium heptamolybdate will, once the support is calcined in air or other atmospheres, significantly reduce the support surface area of the support material, this presumably being due to blockage of the small pores with molybdenum oxide. Impregnation of silica with phosphoric acid followed by calcination in air is also known to significantly reduce the surface area of porous silica. Any such techniques can be employed in accordance with the present invention to produce particulate support material of ti appropriate properties. As well known to those skilled in the art of fluid-bed reactions, a solid which is to be fluidized must have an appropriate particle size distribution and density. Since the vast majority of the Group VIII metal deposited on the support of the inventive catalytic material will be incorporated into the support interior, the particle size distribution of the support will be similar or essentially the same as the particle size distribution of the catalytic material of the invention itself. The support, therefore, must also exhibit a particle size distribution appropriate for use as a fluidbed material. Normally, this means that at least 80 of the particulate support will have a particle size distribution ranging between 5 to 300, preferably 10 to 200, more preferably 20 to 150 microns. Group VIII Metal Any Group VIII metal of the mixture thereof can be employed as the coating or impregnant for the support pores surfaces of the inventive catalytic material. Iron, cobalt and nickel are preferred, while iron and nickel are especially preferred. The amount of Group VIII metal in the support can vary widely. For convenience, the amount of Group VIII element is normally set forth in terms of single layers of the Grow, VIII element based on the measured surface area of the support to be impregnated. In other words, based on the surface area of the support to be impregnated and the atomic radius of the Group VIII element to be deposited on the pore surfaces of the support, the total number of atoms and hence the total number of moles of Group VIII element needed to completely coat all the surfaces of the particles with a single layer of the Group VIII element one atom thick can be calculated. Referring to the amount of Group VIII element impregnated into the support in terms of multiples or fractions of such layers has been found to be very convenient. For the purposes of this invention, the amount of Group VIII element impregnated into the support particles should be at least about one layer. Metal loadings less than one layer have been found to produce a catalyst of very poor activity and should be avoided. As the metal loading increases above one layer, the performance of the catalyst increases rapidly with catalysts having a metal loading corresponding to two layers exhibiting excellent activity. As the metal loading increases above two layers, no significant advantage is realized. Theoretically, there is no maximum to the amount of metal loading except that too much metal will fill the pores of the support and hence reduce its overall capacity to grow carbon. As a practical matter, therefore, metal loadings in excess of five layers should be avoided. Metal loadings on the order of 1.5 to 3 are preferred with metal loadings on the order of two layers being especially preferred. Incidentally, it should be appreciated that in porous particles having the relatively high surface areas reported herein, the amount of surface area attributable to the external surface of the-particles is essentially negligible. Accordingly, even if the entire external surfaces of the particles also carry deposited iron, the amount of this deposited iron will be negligible or essentially negligible compared with the amount deposited in the body of the support particles. The Group VIII metal can be deposited into the pores of the porous support by any of the well known techniques for accomplishing such impregnations. Normally, this will be accomplished by impregnating the porous support with a liquid containing the Group VIII metal or a compound thereof in solution, drying and, if necessary, heat treating in an appropriate atmosphere or series of atmospheres so as to recover the metal in elemental form. For example, the catalytic material of Example 10 reported below was produced as follows. 46.7 gms. of Fe(NO3)3.9 H20 were dissolved in 20 cc. of water. This solution was added dropwise with stirring to 31.7 gms. of the hydrothermally treated silica described above having a surface area of 53 mê/gm. and a pore volume of 1.22 cc./gm. Addition was done gradually and with enough stirring to maintain a homogeneous appearance of the catalyst. The impregnated catalyst was then dried overnight at 1100 C. In the early stages of drying, the catalyst was stirred every half hour to break-up a soft dark brown crust which formed on the surface. After drying, the catalyst appeared cinnamon in colonr,uniform and freeflowing. The catalyst was then calcined in air at 1500C for 30 minutes and further at 4000C for an additional 6 hours to decompose the iron nitrate and form iron oxide. Next, the catalyst was placed in a 25 mm. inside diameter quartz fluid-bed reactor. After raising the temperature to 55O0C under a nitrogen atmosphere, the gas stream was changed to hydrogen and maintained for 90 minutes. The temperature was then increased to 6500C and maintained there for an additional 30 minutes in the hydrogen atmosphere whereby the oxidized iron was reduced to elemental iron. The catalyst was then cooled in an atmosphere of nitrogen and then removed from the reactor once reaching room temperature. At room temperature, the catalyst was stable to atmospheric oxygen. Other techniques for depositing the Group VIII metal can beremployed. For example, organic compounds such as iron carbonyl or phenyl iron dissolved in a suitable organic solvent such as n-pentane could be employed as the impregnating solution. Or inorganic salts of Group VIII metals dissolved in organic solution (e.g. methanol) could be used, as impregnating solution. The catalytic material according to the invention as described above has many unique features. It catalyzes the deposition of carbon by disproportionation of carbon monoxide at a high rate with the vast majority of the carbon being deposited within its pores. It also shows high activity in the carbon removal step by formation of methane through contract with hydrogen as also shown in the above-noted Belgian patent. Furthermore, it is able to withstand repeated cycling between carbon deposition and removal without significant loss in activity or without significant attrition even though carbon loadings (weight carbon/total particle weight) as high as 20% and higher are realized during carbon deposition. It is also resistant to temperature changes which may occur because the carbon deposition and carbon removal steps in the carbon cycle occur at diffent temperatures. Further it is readily'fluidized in conventional fluidized bed reactors operating with conventional flow rates such as 0.01 to 10, preferably 0.5 to 5, more normally about 1 to 2 ft./sec. (gas velocity). Finally, it exhibits little or no growth or carbon fibers on its surface and hence problems due to the fragility of these fibers and agglomeration through comingling of these fibers is avoided. Because of these properties, the inventive catalytic material is ideally suited for carrying out the carbon deposition/removal procedure described in the above-mentioned Belgian patent in a fluidized bed system. WORKING EXAMPLES A number of different catalytic materials of the present invention were produced by the preferred technique of impregnating a support (usually the preferred hydrothermally processed silica described above) with a solution of a compound of a Group VIII metal,calcining to convert the metal compound to the corresponding metal oxide and then reducing the oxide to the metal. Usually, the calcination reduction procedure was the same as described above in.connection with the preferred embodiment, although in some instances more severe reduction conditions (i.e. higher temperàtures) were employed. Also in some instance additional elements such as potassium and chromium were incorporated into the catalyst. The catalytic materials so'made were subjected to repeated carbon deposition/carbon removal cycles. Normally, carbon was removed by methanation although sometimes carbon was removed by steaming and in other instances carbon was removed by methanation first followed by steaming in the later cycles. Unless otherwise indicated, in each example, 40 cc. of the catalyst were placed in a 25 mm. inside diameter 90 cm. long fluid-bed reactor equipped with a quartz frit supporting the catalyst located 25 cm. from the bottom. Incoming feed gas streams were dispersed by a coarse gray glass sparger inserted 12 cm. up from the bottom of the quartz tube, and at the top of the tube another gas sparger of fine porosity was inserted 4 cm. from the top of filter catalyst fines from the tailgas. In each experiment, 40 cc. of catalyst was placed in the reactor. Next, the catalyst was brought to 500C under nitrogen atmosphere. When the temperature stabilized at 4500 C, 112 and CO flows were added at 46 cc./min. and 195 cc./min respectively. Under these carbon deposition, conditions, the catalyst became black within about a half an-hour. The above donditions were maintained for about one hour and then the temperature was raised to 5500C and kept at this temperature for one hour for the first carbon deposition step. Then the carbon monoxide and nitrogen flows were shut off and the 119 flow increased to 129 cc./min. accomplish methanation. Me'thanation was carried out for about 2 hours to complete the first carbon deposition/methanation step. Thereafter, the carbon deposition/carbon removal cycle was repeated a number of times under the same conditions except that carbon deposition was carried out at 45O0C in the second and subsequent cycles rather than 5500 C. All reactions were carried out at atmospheric pressure. In a number of examples carbon removal was accomplished by steaming. During each carbon deposition and carbon removal step, the gross reaction product was recovered and analyzed. From this analysis, the rate of carbon deposition and rate of carbon removal, both during methanation and steaming, were determined. The identity of the catalyst, including the identity, surface area an pore volume of the support, the overall catalyst composition and average rates of carbon deposition and carbon removal are given in the following Table II. The carbon deposition rate is reported in grams carbon deposited per hour per gram metal on the catalyst and grams carbon removed is similarly reported in grams carbon removed per hour per gram metal of catalyst. During carbon removal by methanation, a slight amount of the carbon occasionally forms carbon dioxide or carbon monoxide. This is excluded from the carbon removal rate. Also, since the first carbon deposition/carbon removal step serves to activate the catalyst, the first cycle is omitted from the reported average rates. TABLE II Support Surf Pore Steam Rates Exam Area Vol Catalyst Temp Carbon Carb Removal No Composition mê/gm cc/gm Composition ( C) Deposit Meth Steam Remarks 1 SiO2 120 1.53 15.0% Fe --- 0.66 0.18 -- 85.0% SiO2 2 SiO2 62 1.29 15.0% Fe --- 0.42 0.11 --- The fines ( < 325 mesh) 85.0% SiO2 were removed. 3 SiO2 62 1.29 15.0% Fe --- 0.74 0.38 --- To the catalyst of Ex. 2 85.0% SiO2 (after 325 removed) inert fines ( < 325) were added. 4 SiO2 61 1.46 15.0% Fe --- 0.66 0.27 -- 85.0% SiO2 5 SiO2 46 1.39 15.0% Fe 550- 0.59 0.31 --- At 750 C good steaming 85.0% SiO2 750 reaction but oxidised catalyst. 6 SiO2 * * 16.9% Fe --- 0.31 0.21 --- Support calcined before 83.1% SiO2 metal addition. 7 SiO2 75 1.39 16.9% Fe --- 0.62 0.23 -- 83.1% SiO2 8 SiO2 129 1.35 16.9% Fe --- 0.59 0.29 -- 83.1% SiO2 9 SiO2 * * 16.9% Fe --- 0.50 0.20 -- 83.1% SiO2 10 SiO2 53 1.22 16.9% Fe --- 0.55 0.25 -- 83.1% SiO2 * Not available. TABLE II (Contd) Support Surf Pore Steam Rates Exam Area Vol Catalyst Temp Carbon Carb Removal No Composition mê/gm cc/gm Composition ( C) Deposit Meth Steam Remarks 11 SiO2 58 1.39 15.0% Ni --- 0.74 0.28 -- 85.0% SiO2 12 SiO2 58 1.39 15.0% Ni 700 after 2.30 Unexpected increase in 85.0% SiO2 650 steam 2.18 deposition rate after 600 1.31 1.97 steaming--20 cc. catalyst 550 1.00 13 SiO2 58 1.39 10.0% Fe --- 1.03 0.42 -- 90.0% SiO2 14 SiO2 45 1.18 15.0% Fe --- 0.55 0.26 -- 85.0% SiO2 15 SiO2 15.0% Fe --- 0.61 0.25 -- 85.0% SiO2 A SiO2 688 0.95 15.0% Fe --- 0.00 --- Less than mono-layer Fe. 85.0% SiO2 B SiO2 688 0.95 30.0% Fe --- 0.00 --- Less than mono-layer Fe. 70.0% SiO2 C SiO2 128 0.32 15.0% Fe --- 0.36 Not --- Catalyst broke-up and 85.0% SiO2 deter- clumped. mined D SiO2 688 0.95 71.0% Fe --- 0.09 0.03 --- Very poor rates, very bad 29.0% SiO2 fluidization--20 cc. catalyst 16 SiO2 64 1.29 15.0% Fe 600- 0.84 0.26 0.75 Catalyst didn't fluizide well 85.0% SiO2 550 0.39 17 SiO2 32 1.89 15.0% Fe --- 0.63 0.29 -- 85.0% SiO2 Support Surf Pore Steam Rates Exam Area Vol Catalyst Temp Carbon Carb Removal No Composition mê/gm cc/gm Composition ( C) Deposit Meth Steam Remarks E Alundum 1.0 0.57 5.0% Fe --- --- Support contianed many 95.0% Alundum < 50A pores. Catalyst was not homogeneous and could not be used. 18 SiO2 58 1.39 15.0% Ni 600 0.80 --- 0.53 Added K did not 85.0% SiO2 550 0.46 improve catalyst. 0.5% K 19 75 SiO2/25 166 0.98 15.0% Fe --- 0.68 0.19 --- Fe reduced with H2 Al2O3 85.0% SiO2/ at 725 C. Very good Al2O3 fluidization. 20 SiO2 58 1.39 24.0% Fe --- 0.42 0.16 -- 76.0% SiO2 21 SiO2 245 1.41 15.0% Fe --- 0.65 0.23 --- Activated at 700 C 85.0% SiO2 in H2. 22 SiO2 58 1.39 10.0% Ni 550 1.07 --- 0.91 Reported rates based 5.0% Cr on Ni content only. 85.0% SiO2 23 Al2O3 61 0.45 15.0% Ni --- 0.45 0.15 -- 85.0% Al2O3 24 SiO2 6 1.24 15.0% Fe --- 0.58 0.27 -- 85.0% SiO2 25 Al2O3 195 0.58 15.0% Ni --- 0.33 0.10 -- 85.0% SiO2 26 SiO2 42 2.45 15.0% Ni --- 1.31 0.49 --- Catalyst broke apart 85.0% SiO2 because of overloading with carbon during carbon deposition. From the above, it can be seen that catalysts produced in accordance with the invention exhibit good rates for carbon deposition and carbon removal. In addition from Comparative Examples A, B,and D it can be seen that catalysts made from supports having surface areas which are too high exhibit essentially no activity. Furthermore, from Comparative Example C it can be seen that catalysts made with a support having an acceptable surface area but a pore volume which is too small also' áre unsuitable. In addition, from Comparative Example E it can be seen that catalysts made from a support having a surface area too lowareaJso ineff- active Thus, it will be appreciated that only by selecting the support to have the properties indicated is it possible to form a dimensionally stable catalyst exhibiting good activity in carbon deposition and removal and which further is suitable for use as a fluid-bed catalyst. Although only a few embodiments of the invention have been described above, many modifications can be made without departing from the spirit and scope of the invention. For example, it should be appreciated that other inventive catalytic material can be formed so as to be useful in entrained bed systems and fast fluid-bed systems as well as conventional fluid-bed systems. All such modifications are intended to be included within the scope of the invention, which is to be limited only by the following claims:

Claims: Claims: 1. A particulate, freeflowing, fluid-bed catalyst comprising a porous catalyst support having a surface area of greater than 1 to less than 350 mê/gm and a pore volume of 0.4 to 3.0 cc/gm and a Group VIII metal or mixture thereof on the pore surface of said support, said Group VIII metal or mixture being present in an amount equivalent to at least one atomic layer. 2. A catalyst as claimed in claim 1 characterised in that said catalyst has a particle size distribution such that 80% of said catalyst is between 5 to 300 microns in size and a density such that said catalyst will form a fluidized bed when contacted with an up flowing gas flowing at a velocity of 0.1 to 10 ft/sec. 3. A catalyst as claimed in claim 1 or claim 2 characterised in that said surface area is 6 to 250 m2 /gm and said pore volume is 1 to 2 cc/gm. 4. A catalyst as claimed in any of claims 1 to 3 characterised in that said support exhibits no measurable pores having a pore diameter of less than 50 angstroms. 5. A catalyst as claimed in any of claims 1 to 4 characterised in that said support is silica. 6. A catalyst as claimed in any of claims 1 to 5 characterised in that the Group VIII metal is iron, cobalt or nickel. 7. A fluid-bed process for converting carbon monoxide to a high energy gas comprising contacting the catalytic material of claim 1 with an flowing gas stream containing carbon monoxide so as to fluid ize said catalytic material and deposit carbon in the pores of said catalytic material and thereafter contacting said catalyst with a carbon removal gas selected from hydrogen and steam so as to fluidize said catalytic material and remove carbon from said catalytic material. 8. A process as claimed in claim 7 characterised in that said carbon removal gas is hydrogen. 9. A process as claimed in claim 7 characterised in that the carbon removal gas is steam. 10. A process as claimed in claim 7 characterised in that the gas flow rates of said methane during carbon deposition and said carbon removal gas during carbon removal are 0.1 to 10 ft/sec. 11. A process as claimed in claim 10 characterised in that the surface area is greater than 1 to less than 350 m2/gm and said pore volume is 0.4 to 3cc/gm.

Inventors: HARDMAN HARLEY FOCH, VELENYI LOUIS JOSEPH, HARDMAN, HARLEY FOCH, VELENYI, LOUIS JOSEPH
Applicants: STANDARD OIL CO OHIO, THE STANDARD OIL COMPANY
Application year: 1981
Main classification: B01J23
IPC codes: B01J35, B01J23, B01J21, C07C1