RU2244589C1 - Catalyst, method of preparation thereof, and a synthesis gas generation method - Google Patents

Abstract

FIELD: hydrocarbon conversion catalysts.

SUBSTANCE: catalyst for generation of synthesis gas via catalytic conversion of hydrocarbons is a complex composite composed of ceramic matrix and, dispersed throughout the matrix, coarse particles of a material and their aggregates in amounts from 0.5 to 70% by weight. Catalyst comprises system of parallel and/or crossing channels. Dispersed material is selected from rare-earth and transition metal oxides, and mixtures thereof, metals and alloys thereof, period 4 metal carbides, and mixtures thereof, which differ from the matrix in what concerns both composition and structure. Preparation procedure comprises providing homogenous mass containing caking-able ceramic matrix material and material to be dispersed, appropriately shaping the mass, and heat treatment. Material to be dispersed are powders containing metallic aluminum. Homogenous mass is used for impregnation of fibrous and/or woven materials forming on caking system of parallel and/or perpendicularly crossing channels. Before heat treatment, shaped mass is preliminarily treated under hydrothermal conditions.

EFFECT: increased resistance of catalyst to thermal impacts with sufficiently high specific surface and activity retained.

4 cl, 1 tbl, 8 ex

Description

The invention relates to a process for producing synthesis gas by catalytic conversion of hydrocarbons in the presence of oxygen-containing gases and / or water vapor at short contact times and to catalysts for this process.

Synthesis gas (a mixture of hydrogen and carbon monoxide) is widely used in large-capacity chemical processes, such as the synthesis of ammonia, methanol, higher alcohols and aldehydes, in the Fischer-Tropsch process and others. Synthesis gas is used as a reducing gas in ferrous and non-ferrous metallurgy , metalworking, used in environmental installations for the neutralization of gas emissions. Promising and extremely rapidly developing new areas for the use of synthesis gas and the hydrogen produced from it are motor vehicles and small-scale energy. In the automotive industry, synthesis gas or hydrogen can be used as an additive to the main fuel in internal combustion engines or as fuel for an engine based on fuel cells. In the energy sector, synthesis gas and hydrogen can be used in combination with fuel cells or gas turbines to produce environmentally friendly heat and energy.

The traditional method of producing synthesis gas is the endothermic process of steam conversion of natural gas on nickel catalysts [J.R. Rostrup-Nielsen, Production of synthesis gas, Catalysis Today, 1993, v. 18, 305-324; B.C. Arutyunov, O.V. Krylov // Oxidative transformations of methane. Moscow, Science, 1998]. This process is characterized by extremely high capital intensity, high operating costs and significant emissions of nitrogen oxides during torch heating of tubular reformers.

An alternative method for producing synthesis gas is the selective catalytic oxidation of hydrocarbons by oxygen (RMS) [S.C. Tsang, J. B. Claridge and M. L. H. Green, Recent advances in the conversion of methane to synthesis gas, Catalysis Today, 1995, v. 23, 3-15]. In contrast to steam reforming of natural gas, SKO has a high selectivity, is an exothermic process, and proceeds efficiently at short contact times, which makes it possible to conduct it in an autothermal mode and reduce the reactor size [DAHickman, LDSchmidt, Synthesis gas formation by direct oxidation of methane , in "Catalytic Selective Oxidation", ACS Symposium series, 1993, p. 416-426; PMTorniainen, X. Chu and LDSchmidt, Comparison of monolith-supported metals for the direct oxidation of methane to syngas, J.CataL, 1994, v.146, 1-10] and thereby reduce both energy costs and capital investments .

The selectivity of the RMS reaction in relation to the target products (carbon monoxide and hydrogen) depends on various factors, however, the chemical composition of the active component is most important. To obtain maximum yields of the target product — synthesis gas — the catalyst should contain an active component that provides high activity and selectivity at short contact times in the conversion reactions and the standard deviation of hydrocarbons. In addition, for the implementation of this process, catalysts with low hydraulic resistance, resistant to thermal shock and carbonization, are required.

The known method of standard deviation of methane to produce synthesis gas [US Pat. US 5149464, C 01 B 3/26, 1992] at a temperature of 650-900 ° C and a space velocity of 40,000-80000 h ^-1 (0.05-0.09 sec) in the presence of a catalyst, which is either a transition metal or oxide deposited on a thermostable oxide of one of the elements (M): Mg, B, Al, Ln, Ga, Si, Ti, Zr, Hf, or a perovskite-like mixed oxide of the general formula MxM'yOz with a pyrochlore structure, where M 'is a transition metal , including elements of 8 groups. The atomic ratio of the element of group 8 to the sum of the base elements in these compounds is 1: 1 or 3: 1, and the content of noble metals is 32.9-48 wt.%. The methane conversion in the presence of mixed oxides Pr ₂ Ru ₂ O ₇ , Eu ₂ Ir ₂ O ₇ , La ₂ MgPtO ₆ at a space velocity of 40,000 h ^-1 and 777 ° C does not exceed 94%, and an increase in the space velocity to 80,000 h ^-1 leads reduction of methane conversion to 73% and selectivity for CO and hydrogen to 82 and 90%, respectively.

In the patent [EP 303438, C 01 B 3/38, 02/15/1989] to obtain a mixture of hydrogen and carbon monoxide, a method of RMS of hydrocarbons is proposed by contacting a reaction mixture containing a hydrocarbon, oxygen or an oxygen-containing gas and optionally water vapor with a catalyst in a selective zone catalytic oxidation. The SKO zone contains a block catalyst with a geometric surface / volume ratio of at least 5 cm ² / cm ³ . The catalyst may contain noble metals, nickel, cobalt, chromium, cerium, lanthanum and a mixture thereof deposited on a heat-resistant oxide carrier, including cordierite, mullite, aluminum titanate, zirconium spinel, aluminum oxide. At the same time, in patent EP 303438 it is stated that the partial oxidation reaction rate is limited by the mass transfer rate and does not depend on the chemical nature of the catalyst, which makes it possible in this case to use materials that do not exhibit catalytic activity, but provide the necessary geometric surface / volume ratio. The process is carried out at temperatures in the range of 760-1090 ° C and a space velocity from 20,000 to 500,000 h ^-1 .

In the patents [RU 2115617, C 01 B 3/38, 07/20/98; RU 2136581, C 01 B 3/38, 09/10/99; RU 2137702, C 01 B 3/38, 09/20/99; RU 2123471, C 01 B 3/38, 12.20.98; US 5486313, C 07 C 1/02, 01/23/1996, and US 5639401, C 07 C 1/02, 06/17/97] propose a method of standard deviation of hydrocarbons, including sulfur containing (0.05-100 ppm) [RU 2132299, C 01 B 3/38, 06/27/99; US 5720901, C 07 C 1/02, 04.24.98], into synthesis gas using catalysts containing noble metals (up to 10 wt.% Pt, Pd, Rh, Os) supported on a heat-resistant carrier. As carriers, for example, α-Al ₂ O ₃ , barium hexaaluminate (grain size ~ 1 mm) or ZrO ₂ , thermostabilized by oxides of elements of groups III B or P A of the Periodic Table (porous blocks in the form of ceramic foam, resistant to thermal shock) are used. The process is carried out in a reactor with a fixed catalyst bed having a large tortuosity - the ratio of the gas path length when passing through the block to its length is in the range 1.1-10 at temperatures of 950-1300 ° C and the gas mixture flow rate is 2-10 ⁴ -10 ⁸ l / kg · hour. The disadvantages of this method are the high hydraulic resistance of the catalyst layer with high tortuosity and the high cost of the catalysts due to the high content of precious metals and the use of expensive zirconium-based ceramic foam, which limits their practical application.

Thus, the literature describes catalysts based on block ceramic supports with different compositions of the active component for the process of selective oxidation of hydrocarbons into synthesis gas at short contact times. Basically, these are carriers that are foam ceramics, however, such blocks at short contact times of the reaction mixture have high hydraulic resistance due to the large tortuosity of the channels. With an increase in the size of macropores in order to reduce hydraulic resistance, the mechanical strength and efficiency of such catalysts decreases due to a decrease in the geometric surface.

It is known that the use of blocks with direct channels (cellular blocks) can reduce the hydraulic resistance. In the patent [US 5648582, C 07 C 004/02, 11/30/1995] for carrying out the RMS process for hydrocarbons at space velocities 800000-12000000 h ^-1 use Pt, Rh or Ni deposited on non-porous ceramic blocks with direct channels. However, these catalysts contain up to 10 wt.% Noble metals and are very expensive, in addition, ablation of metals is observed due to high temperatures developing in the block catalyst layer.

A common disadvantage of non-porous cellular support catalysts is their low specific surface area [GB 1375830, B 01 J 11/06, 1973; US Pat. EP 0197681, B 01 J 37/00, 03/18/1986], which does not provide their sufficient activity.

To increase the geometric surface of the catalysts, the wall thickness of the cell blocks is reduced and the number of channels per unit section of the block is increased. To increase the overall surface, a porous substrate with a high specific surface of aluminum oxides, silicon, rare earth elements is additionally applied to cellular carriers. The latter technique requires special preparation of the materials from which the substrate is made, the introduction of additional stages in the technological process of manufacturing catalysts [US 3824196, B 01 J 11/06, 07/16/1974]. In addition, due to the difference in the coefficients of thermal expansion, peeling of the porous layer during thermal shocks is possible, which is typical for any exothermic catalytic processes. Catalysts prepared on the basis of such carriers have an insufficient resource and are less resistant to catalytic poisons.

A fundamentally different approach is focused on the manufacture of a monolithic honeycomb catalyst having a high specific surface area and incorporating the active component directly into the honeycomb structure. In the applications [WO 0134517, C 01 B 3/40, 05.17.2001; WO 0160740, 08.23.2001; WO 0160515, B 01 J 37/00, 08/23/2001; WO 0160742, C 01 B 3/40, 08/23/2001] synthesis gas is obtained by contacting a reaction mixture containing C ₁ -C ₅ hydrocarbons and an oxygen-containing gas with a catalyst mainly in the form of ceramic foam blocks based on transition metal oxides (Cr, Co , Ni, Mn), alkaline and rare-earth elements with a specific surface area of 5-250 m ² . The proposed catalysts are not destroyed at a temperature of ~ 1120-1160 ° C, however, they have a high ignition temperature of the reaction. In addition, blocks in the form of foam ceramics, as mentioned above, have a large hydraulic resistance.

Known honeycomb block media with a high specific surface of alumina [US 4294806, B 01 D 53/36, 10/13/1981] or a mixture of aluminum oxides and silicon [US Pat. RF 2093249, B 01 D 53/06, 12/22/1992]. However, such media have insufficient mechanical strength and resistance to thermal shock. This does not allow the use of these media for the manufacture of catalysts for the burning of fuels or partial oxidation of methane to synthesis gas, which require thermal stability at higher temperatures.

To increase the thermal stability of the catalyst [US 4637995, B 01 J 23/75, 01/20/1987] use a honeycomb block containing 50-90 wt.% Sintered ceramic matrix material and 10-50 wt.% Material with a high specific surface dispersed throughout matrix. The material of the ceramic matrix consisted of cordierite, mullite, alpha-alumina, or mixtures thereof. The particle size of the matrix material did not exceed 70 μm (200 mesh). The dispersed material had a specific surface area of at least 40 m ² / g and a crystallite size of not more than 0.5 μm and consisted of transition metal sulfides or mixtures thereof, porous oxides based on aluminum oxides, zirconium, spinel based on magnesium aluminate, silicon oxide, zeolite titanium oxide or mixtures thereof, as well as mixtures thereof with metal sulfides.

A disadvantage of the known catalysts and carriers is the use of silicon-containing compounds, which significantly reduce the resistance of monoliths to sintering due to the relatively low melting point, compared with aluminum oxide [Quick reference chemist, L .: Chemistry, 1978]. During high-temperature sintering, metal sulfides are oxidized, which significantly reduces the contact strength between particles. For many processes occurring at high temperatures, the reaction is carried out in the diffusion region, so a very high specific surface area is not required. It is much more important that the catalyst data are resistant to thermal shock and, if possible, have increased thermal conductivity to reduce the likelihood of local overheating. Composite materials have such properties.

The closest to the claimed technical essence and the achieved effect is a block honeycomb catalyst for producing synthesis gas by selective catalytic oxidation of hydrocarbons based on mixed oxides with perovskite structure M ¹ B _1-y M _y O _z and / or fluorite M $\genfrac{}{}{0ex}{}{\text{one}}{\text{x}}$ M $\genfrac{}{}{0ex}{}{\text{2}}{\text{1 x}}$ O _z , where M is an element of group 8 (Pt, Rh, Ir), M ¹ is a rare earth element (La, Ce, Nd) or alkaline earth (Ca, Sr), M ² is an element of group IV b of a group (Zr, Hf), B is a transition element (Ni, Co), which is a complex composite containing components with an ultra-low coefficient of thermal expansion [Pat. RF 2204434, B 01 J 23/40, C 01 B 3/26, 05.20.2003]. At a temperature of 600-800 ° C and a contact time of 0.1-0.4 seconds, high methane conversions and synthesis gas selectivity are achieved. However, the catalyst is a ceramic composite in which the active component does not directly enter the matrix forming a honeycomb structure. In addition, the composite is obtained by extrusion, which leads to the presence of mechanical stresses and a decrease in the thermal and mechanical stability of the catalyst.

The invention solves the problem of creating a thermostable porous block catalyst of a honeycomb structure having a sufficiently high specific and geometric surface, resistant to local overheating and thermal shock to produce synthesis gas, effective for short contact times both in the reactions of selective catalytic oxidation of hydrocarbons with oxygen and in steam and carbon dioxide conversion of hydrocarbons, and the process of producing synthesis gas using this catalyst.

The problem is solved by a catalyst for producing synthesis gas by catalytic conversion of a mixture containing a hydrocarbon or a mixture of hydrocarbons and an oxygen-containing component, which is a composite composite containing aluminum oxide and oxides of rare-earth and / or transition metals, the composite composite is a ceramic matrix and a material consisting of coarse particles particles or aggregates of particles dispersed throughout the matrix, while the catalyst has a system of parallel and / or intersecting channels, dispersion The material is metal oxides, and / or their mixtures, and / or metals, or their alloys, and / or metal carbides, and / or their mixture, different in composition and structure from the matrix, the content of the dispersed material is 0.5-70 wt.%. The dispersed material may have a particle size of from 1 to 250 microns. The catalyst may have a hole in the center that differs from the channels in size and shape.

The use of a matrix that does not contain low melting compounds allows one to maintain high porosity even after overheating. The presence of coarse dispersed material, including metals or metal carbides, can reduce mechanical and thermal stresses during local overheating by increasing the heat capacity of the composite and the reinforcing properties of the coarse fraction. The system of intersecting channels increases the geometric surface of the catalyst and contributes to an increase in its activity. In addition, to firmly fix the catalyst in the housing, it is possible to use a block with a hole in the center with a larger diameter than the cellular channels, sufficient to firmly fix the resulting catalyst in the housing.

The structural features of the proposed catalyst determine the features of the method of its preparation.

The problem is also solved by the method of preparing a catalyst for producing synthesis gas by catalytic conversion of a mixture containing a hydrocarbon or a mixture of hydrocarbons and an oxygen-containing component, including obtaining a homogeneous mass containing sintered ceramic matrix material and dispersed material, molding the mass into the desired shape, heat treatment of the molded mass at a temperature sufficient for sintering the matrix material, powders containing metallic aluminum, impregnated with a homogeneous mass of fibrous and / or fabric materials, forming in the monolithic body during sintering a system of parallel and / or intersecting channels, before heat treatment the molded mass is pre-treated under hydrothermal conditions. As the dispersed material, powdered metal oxides and / or powdered metals and / or their alloys and / or metal carbides and / or their mixture are used, and the content of the dispersed material is 0.5-70 wt.%.

A method of preparing a catalyst of a honeycomb structure according to the invention includes:

1) the use as a material for a ceramic matrix of powdered aluminum or powders based on aluminum oxides or hydroxides with the addition of powdered aluminum;

2) the use as an additional material of powder particles of large size 1-250 microns, which perform reinforcing functions, and the use of metals and carbides improves the thermophysical properties of the carriers;

3) obtaining a homogeneous mass by mixing and impregnating this homogeneous mass of fibrous or fabric materials that burn out during high-temperature processing in air;

4) loading a homogeneous mass with burnable materials into a mold permeable to gaseous substances;

5) processing a homogeneous mass in hydrothermal conditions before calcining in air.

Aluminum powder, interacting with water, oxidizes with the formation of hydroxides, which leads to an increase in the volume of the solid and self-pressing of a homogeneous mass into a mechanically strong monolith. During calcination, thermal decomposition of aluminum hydroxides occurs with the formation of a highly porous matrix of aluminum oxide, as well as the oxidation of aluminum metal with the formation of elongated oxide particles, which along with large particles (1-250 μm) reinforce the porous matrix and increase its resistance to thermal shock. In addition, burnable fibers after heat treatment in air form through parallel channels in the body of a monolith with rough walls. Burning materials after heat treatment in air form a system of channels.

It should be noted that the method of preparation of the catalyst, including the use of powdered aluminum mixed with powdered non-volatile components, followed by steam treatment is known [Pat. RF 2059427, B 01 J 23 // 75, 01/06/1993; US Pat. RF 21322231, B 01 J 37/02, 10/14/1998]. However, this method does not involve the use of additives that burn in the air. This does not allow the manufacture of honeycomb structures.

As the oxides in the present invention can be used simple and / or mixed oxides of transition and rare earth elements. As metals, alloys and carbides, mainly metals of 4 periods are used. The average particle size of metals, alloys and metal carbides is determined from data on the specific surface and the true density of the powders. The average aggregate size of the oxide particles is determined by the Coulter method. In some cases, the particle size is determined by sieving. The specific surface is determined by the BET method [A.P. Karnaukhov. Adsorption. Texture, dispersion and porosity of materials. Novosibirsk, Science, 1999].

The problem is also solved by the method of producing synthesis gas by catalytic conversion of a mixture containing a hydrocarbon or a mixture of hydrocarbons and an oxygen-containing component using the catalyst described above, which is a composite composite containing aluminum oxide, rare earth and / or transition metal oxides. The composite is a ceramic matrix and a material consisting of coarse particles or particle aggregates dispersed throughout the matrix, the catalyst comprising a system of parallel and / or intersecting channels, the dispersed material is an oxide of rare earth and / or transition metals, and / or mixtures thereof, and / or metals, or their alloys, and / or carbides of metals of the 4th period of the Periodic table, and / or their mixture are different in composition and structure from the matrix, the content of the dispersed material is makes up 0.5-70 wt.%. The dispersed material may have a particle size of from 1 to 250 microns. The catalyst may have a hole in the center that differs from the channels in size and shape.

The synthesis gas production process is carried out in a flow reactor in an autothermal mode at a temperature of 550-1100 ° C, variation of the contact time and the composition of the reaction mixture. The reaction mixture containing natural gas or liquid hydrocarbon vapors such as octane, gasoline and, in some examples, water vapors in the air are heated before entering the reactor. At the inlet and outlet of the reactor to prevent heat loss are placed screens - blocks of corundum. During the start-up and operation of the catalyst, the gas temperature at the inlet to the reactor, the temperature of the catalytic unit at the inlet, and the temperature at the outlet of the unit are controlled. The reaction products are analyzed chromatographically. The efficiency of the catalyst is characterized by the reaction start temperature, the degree of methane conversion and the amount of synthesis gas obtained, expressed in volume percent and characterizing the synthesis gas selectivity. The composition of the initial reaction mixture and reaction products are analyzed chromatographically.

The invention is illustrated, but not limited to the following examples.

Example 1. Aluminum powder is mixed with a dispersed material — mixed LaNiО _{3 + x} oxide with a perovskite structure having an average particle aggregate size of about 15 μm, but with a wide size distribution range from 1 to 25 μm. The resulting powder is mixed with a solution of glycerol in water. The resulting suspension is wetted with a cotton cloth in the form of a tape, on top of which cotton threads 1 mm thick are placed parallel to each other and perpendicular to the length of the tape. Then the tape is rolled into a cylindrical body, which is laid in a molding device and placed in an autoclave. In an autoclave, the molding device is steamed, as a result of which part of the aluminum powder is oxidized, and the powder sets in a monolith. After autoclaving, the molding device is dried and calcined to a temperature of at least 1000 ° C, as a result of which the remaining part of aluminum is oxidized, and organic materials burn out with the formation of channels. The resulting honeycomb structure product has a specific surface area of 5 m ² / g. The number of parallel channels per unit of the geometric surface of the end plane is 56 cm ^-2 . The distance between the intersecting channels is 0.5 mm. The content of the dispersed material is 22 wt.%. The resulting catalyst is tested in a reaction of selective oxidation of natural gas to synthesis gas. Activity is shown in the table.

Example 2. Similar to example 1. It is characterized in that a CeO ₂ powder with a C-sesquioxide structure having an average particle aggregate size of 7 μm is used as a dispersed material. The resulting honeycomb structure product has a specific surface area of 10 m ² / g. The number of channels per unit of the geometric surface of the end plane is 40 cm ^-2 . The distance between the intersecting channels is 5 mm. The content of the dispersed material is 26 wt.%.

Example 3. Similar to example 1. It is characterized in that powdered nickel (fraction 100-250 μm) is used as the dispersed material, and powdered aluminum hydroxide is added to the aluminum powder. The resulting honeycomb structure product has a specific surface area of 3 m ² / g. The number of channels per unit of the geometric surface of the end plane is 40 cm ^-2 . The content of the dispersed material is 0.5 wt.%. The resulting catalyst is tested as in example 1.

Example 4. Similar to example 3. It is characterized in that a powdered Fe-Cr-Al alloy having an average particle size of 5 μm is used as a dispersed material. The resulting honeycomb structure product has a specific surface area. The number of parallel channels per unit of the geometric surface of the end plane is 35 cm ^-2 . The content of the dispersed material is 70 wt.%.

Example 5. Similar to example 1. It is characterized in that as a dispersed material, a solid solution powder based on La, Ce, Zr oxides having an average particle aggregate size of 8 μm and a Ni-Cr powder alloy having an average particle size of 60 μm are used . The resulting honeycomb structure product has a specific surface area of 12 m ² / g. The number of channels per unit of the geometric surface of the end plane is 230 cm ^-2 . The content of the dispersed material is 26 wt.% Solid solution based on oxides of La, Ce, Zr and 9 wt.% Alloy Ni-Cr. The resulting catalyst is tested as in example 1.

Example 6. Similar to example 3. It is characterized in that TiC powder having an average particle size of 3 μm is used as a dispersed material. The resulting honeycomb structure product has a specific surface area of 2 m ² / g. The number of channels per unit of the geometric surface of the end plane is 40 cm ^-2 . The content of the dispersed material is 20 wt.%. The resulting catalyst is tested as in example 1.

Example 7. Similar to example 5. It is characterized in that TiC powder is used as a dispersed material as in Example 6 and CeO ₂ powder is as in Example 2. The resulting honeycomb structure product has a specific surface area of 9 m ² / g. The number of channels per unit of the geometric surface of the end plane is 40 cm ^-2 . The content of the dispersed material is, wt.%: 12 TiC and 8 CeO ₂ .

Example 8. Similar to example 7. It is characterized in that as a dispersed material, a powdery NiCr alloy with an average particle size of 60 μm is additionally used. The resulting honeycomb structure product has a specific surface area of 4 m ² / g. The number of channels per unit of the geometric surface of the end plane is 230 cm ^-2 . The content of the dispersed material is, wt.%: 12 TiC; 8 CeO ₂ ; 6 NiCr.

The obtained monolithic catalysts show high efficiency in the synthesis gas production reaction and high resistance to thermal shock.

Thus, as can be seen from the above examples, the present invention solves a certain technical problem of resistance to thermal shock at a sufficiently high specific surface area and activity of the catalysts.

Table. Example Ignition Temperature ° C Contact time, sec. X methane,% The content of CO + H ₂ , vol.% 1 530 0.08 88 46 3 700 0.11 80 45 5 720 0.131 78 35 6 670 0.085 54 thirty

Claims (4)

1. The catalyst for producing synthesis gas by catalytic conversion of a mixture containing a hydrocarbon or a mixture of hydrocarbons and an oxygen-containing component, which is a composite composite containing aluminum oxide, rare earth and / or transition metal oxides, characterized in that the composite composite includes a ceramic matrix based on alumina and material dispersed throughout the matrix, the dispersed material contains rare earth and / or transition metal oxides, and / or a mixture thereof, and / or metals, or floats and / or carbides of metals of the 4th period of the Periodic Table, and / or their mixture in the form of particles or particle aggregates with a size of 1-250 microns, with a content of dispersed material of 0.5-70.0 wt.%, while the catalyst has a system of parallel and / or intersecting channels, 2. The catalyst according to claim 1, characterized in that it can have a hole in the center that differs from the channels in size and shape. 3. A method of preparing a catalyst for producing synthesis gas by catalytic conversion of a mixture containing a hydrocarbon or a mixture of hydrocarbons and an oxygen-containing component, including obtaining a homogeneous mass containing sintered ceramic matrix material and dispersed material, molding the mass into the desired shape, heat treatment of the molded mass at a temperature sufficient for sintering the matrix material, characterized in that as the material of the ceramic matrix using a powder containing metal aluminum or a powder based on oxides or hydroxides of aluminum and metallic aluminum impregnate fibrous and / or fabric materials with a homogeneous mass, forming a system of parallel and / or intersecting channels in the monolithic body during sintering; before heat treatment, the molded mass is pre-treated under hydrothermal conditions as dispersed of the material, oxides of rare-earth and / or transition metals, and / or their mixture, and / or metals, or their alloys, and / or carbides of metals of the 4th period are used Periodically th table, and / or a mixture thereof in the form of particles or aggregates of particles with a size of 1-250 micrometers, the content of the dispersed material is 0,5-70,0 wt.%. 4. A method of producing synthesis gas by catalytic conversion of a mixture containing a hydrocarbon or a mixture of hydrocarbons and an oxygen-containing component using a catalyst, which is a composite composite containing aluminum oxide, rare earth and / or transition metal oxides, characterized in that the process is carried out in the presence of catalyst according to any one of claims 1 to 3.