JP2005193111A - Synthetic gas producing catalyst and method for producing synthetic gas by using the same - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a new catalyst for producing synthetic gas, in which the generation of a hot spot can be further restrained, the performance of which can be prevented from being deteriorated with time and which exhibits an excellent conversion rate of a hydrocarbon being a raw material. <P>SOLUTION: This catalyst for producing synthetic gas contains a carrier and first and second components supported on the carrier. The carrier is a molding which is molded out of a heat-resistant material and has ≤10 m<SP>2</SP>/g specific surface area. The first component consists of cobalt or a cobalt-based compound and the amount of the metal to be supported is 5×10<SP>-5</SP>to 1.5×10<SP>-3</SP>mol/g-carrier. The second component consists of at least one metal selected from the group of platinum, rhodium, ruthenium and iridium or its compound and the amount of the metal to be supported is 1×10<SP>-6</SP>to 1×10<SP>-4</SP>mol/g-carrier. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

  The present invention relates to a catalyst for producing a synthesis gas used for producing a synthesis gas by catalytically reforming a hydrocarbon gas having 1 to 5 carbon atoms such as natural gas and a gas containing oxygen in the presence of the catalyst. And a method for producing synthesis gas using the same.

  In recent years, natural gas has attracted attention as a future oil alternative energy source. Since natural gas has clean combustion characteristics compared to other fossil fuels, it can be said that it is extremely beneficial in terms of environmental protection if its use is promoted as a primary energy or secondary energy raw material.

  From this point of view, the development of technologies for chemically converting natural gas to produce methanol, DME, synthetic petroleum, and the like is currently underway. The mainstream of these technologies is an indirect conversion method via a synthesis gas as a synthesis raw material, and the synthesis gas production technology occupies a large weight in the economics of the entire process.

  As a synthesis gas production technique, for example, a steam reforming method, ATR (Auto Thermal Reforming), a catalytic partial oxidation method (CPOX: Catalytic Partial Oxidation), and the like are known.

  In the steam reforming method, since the reaction itself becomes an endothermic reaction, it is necessary to install a reaction tube in a heating furnace and supply heat necessary for the reforming reaction from the outside as an apparatus specification. Therefore, it can be said that the reactor itself becomes large and is not suitable for large-scale production.

  ATR is a method in which part of hydrocarbons in a raw material is burner-burned, and then a high-temperature combustion gas is reformed by a catalyst layer. In this method, it is difficult to operate under economically optimal conditions, such as having to supply excess steam to maintain the life of the burner.

  The catalytic partial oxidation method is a method in which part of the raw material hydrocarbon is catalytically combusted in the catalyst layer, and the generated high-temperature combustion gas is further reformed in the catalyst layer. It can be said that. Although the mechanism is simple and high heat efficiency and production efficiency can be expected, heat generation tends to concentrate near the catalyst layer entrance (so-called hot spot generation), and it is necessary to sufficiently deal with catalyst deterioration due to high heat and reactor loss.

  As prior art, JP-A-6-92603, JP-A-7-10503, JP-A-7-89701, JP-A-196301, JP-T-10-503462 (all of which are Shell International Research Marchippi) Bay et al. Discloses a catalytic partial oxidation method using a catalyst in which a metal element such as Pt, Rh, Ru, Ir, or Pd is supported on a refractory support such as alumina. However, even in the disclosed technique, the reaction gas temperature reaches 1000 to 1200 ° C., and there is a concern that the catalyst is deteriorated due to high heat.

  In addition, Japanese Patent Laid-Open No. 10-245201 (Haldor, Topser, Achzelaurekabet) separates catalyst layers in multiple stages to suppress the temperature of hot spots in contact partial oxidation, and introduces oxygen separately between the catalyst layers. A method is disclosed. Japanese Patent Laid-Open No. 2000-84410 (Idemitsu Kosan) discloses a method of introducing oxygen into the catalyst layer in a divided manner in order to avoid the generation of hot spots in contact partial oxidation. However, even in these two proposals, it is considered that the temperature rise in the oxygen release portion is unavoidable locally, and it can be said that it is not sufficient as a measure for avoiding hot spot generation.

  The reason for the generation of hot spots near the catalyst layer entrance is that ordinary metal catalysts become oxides by contact with oxygen, and the catalyst itself loses the activity of reforming reaction, which is an endothermic reaction, and only the combustion activity, which is an exothermic reaction This is thought to be due to expression. Under such circumstances, Sugiju, the inventor in the present patent application, has already proposed a catalyst in which Pt and Ni are supported on an alumina carrier, and by using this catalyst, in the vicinity of the catalyst layer inlet. Has succeeded in developing both combustion and reforming reactions (Catalyst Letters Vol. 84 No.1-2 (2002)).

JP-A-6-92603 JP 7-10503 A JP 7-89701 A JP 7-196301 A Japanese National Patent Publication No. 10-503462 JP-A-10-245201 JP 2000-84410 A Catalyst Letters Vol. 84 Nos.1-2 (2002))

  However, there is no limit to the improvement in catalyst performance in syngas production, and further improvement in catalyst performance is required. That is, it is desired to propose a new catalyst for production of synthesis gas that can further suppress the generation of hot spots, prevent deterioration of catalyst performance over time, and is excellent in the conversion rate of hydrocarbon as a raw material. ing.

In order to solve such problems, the present invention synthesizes a gas containing a hydrocarbon having 1 to 5 carbon atoms, oxygen, carbon dioxide, and / or steam mainly containing CO and H _2. A synthesis gas production catalyst used for conversion into a gas, the synthesis gas production catalyst comprising a carrier as a base material, a first component supported on the carrier, and a second component The carrier is a molded body having a specific surface area of 10 m ² / g or less molded from a heat-resistant material, and the first component is composed of cobalt or a compound containing cobalt as a main component. Is 5 × 10 ^{−5 to} 1.5 × 10 ⁻³ mol / g-support, and the second component is at least one metal selected from the group consisting of platinum, rhodium, ruthenium, and iridium, or The amount of metal supported by the compound Of 1 × 10 ⁻⁶ to 1 × 10 ⁻⁴ mol / g-carrier.

  As a preferred embodiment of the catalyst for producing synthesis gas of the present invention, the carrier is composed of at least one heat resistant material selected from the group consisting of alumina, calcium alumina, magnesium alumina, and magnesia.

  Moreover, as a preferred embodiment of the catalyst for producing synthesis gas of the present invention, the carrier is composed of α-alumina.

  In a preferred embodiment of the catalyst for producing synthesis gas according to the present invention, the carrier is configured such that the equivalent sphere diameter is 0.5 to 20 mm.

  As a preferred embodiment of the catalyst for producing synthesis gas according to the present invention, the ratio of the total number of moles of metal of the second component to the total number of moles of metal of the first component is 0.005 to 0.5. Configured.

As a preferred embodiment of the synthesis gas production catalyst of the present invention, the carrier is configured such that its specific surface area is 0.2 to 10 m ² / g.

In addition, the present invention mainly comprises CO and H ₂ by bringing a raw material gas containing a hydrocarbon having 1 to 5 carbon atoms, oxygen, carbon dioxide and / or steam into contact with a synthesis gas production catalyst. A method for producing a synthesis gas as a component, wherein a catalyst for producing a synthesis gas used in the method comprises a carrier as a substrate, a first component supported on the carrier, and a second component. The carrier is a molded body having a specific surface area of 10 m ² / g or less molded from a heat-resistant material, and the first component is composed of cobalt or a compound containing cobalt as a main component. Is 5 × 10 ^{−5 to} 1.5 × 10 ⁻³ mol / g-support, and the second component is at least one metal selected from the group consisting of platinum, rhodium, ruthenium, and iridium, or Composed of the compound, the gold The genus loading is configured to be 1 × 10 ⁻⁶ to 1 × 10 ⁻⁴ mol / g-carrier.

Further, as a preferred embodiment of the method for producing the synthesis gas of the present invention, when the number of moles of carbon in the hydrocarbon gas as the raw material is represented by C, O ₂ / C (molar ratio) in the raw material gas is 0.4. in the range of ~1.0, CO ₂ / C (molar ratio) is in the range of 0~1.0, H ₂ O / C (molar ratio) is within the range of 0 to 0.5 The reaction temperature is set in the range of 700 to 1200 ° C. as the product gas temperature, the reaction pressure is set in the range of 0.1 MPa to 10 MPa, the catalyst weight W (g) and the introduced gas total flow rate F are set. W / F, which is a ratio to (mol / hr), is set within a range of 0.15 to 6 (g · hr / mol).

Further, as a preferred embodiment of the method for producing a synthesis gas of the present invention, the carrier is configured such that its specific surface area is 0.2 to 10 m ² / g.

  Compared with the prior art, the generation of hot spots can be further suppressed, and the problems of deterioration in catalyst performance over time, deterioration due to high temperature of the reactor, and damage can be solved. The conversion rate of hydrocarbons as raw materials is also extremely excellent.

  BEST MODE FOR CARRYING OUT THE INVENTION The best mode for carrying out the synthesis gas production catalyst of the present invention and the synthesis gas production method using the same will be described in detail below.

First, the synthesis gas production catalyst will be described.
The catalyst for producing synthesis gas according to the present invention comprises a gas containing 1 to 5 carbon atoms, oxygen, carbon dioxide and / or steam (gas introduced into the reaction vessel), CO and H ₂ . Used when converted to synthesis gas containing the main component.

  The catalyst for producing synthesis gas in the present invention comprises a carrier (carrier) serving as a base material, a first component supported on the carrier, and a second component.

The carrier is a molded body composed of a heat-resistant material, and the specific surface area is 10 m ² / g or less, particularly 0.2 to 10 m ² / g, preferably 0.5 to 10 m ² / g, more preferably. Is set to 2 to 10 m ² / g. When the value of the specific surface area exceeds 10 m ² / g, the temperature near the inlet of the catalyst layer becomes high (generation of hot spots), and the conversion rate of the hydrocarbon as a raw material is improved. There is a tendency for inconvenience that it cannot be achieved. The specific surface area is measured by the “BET” method.

  Here, the carrier is “a molded body” means a granular material formed through a granulation step, and more specifically, for example, raw material powder is pressure-formed into a substantially spherical shape by a mold. Later, it means a granular material formed by firing. Alternatively, it may be a so-called industrial catalyst shape such as a ring, saddle, or multihole, or an irregular shape such as a crushed material.

  The carrier in the present invention needs to be a molded body that satisfies the value of the specific surface area and is composed of a heat-resistant material. Preferable examples include at least one heat resistant material selected from the group consisting of alumina, calcium alumina (having a spinel structure), magnesium alumina (having a spinel structure), and magnesia. Of these, α-alumina is particularly preferred. This is because α-alumina exhibits the most excellent effect in the relationship between the supported first component and the second component.

  α-alumina can be obtained, for example, by firing a bead-shaped alumina molded body at, for example, 1100 to 1300 ° C. That is, by such heat treatment, the beads initially in the state of γ-alumina are crystallized to α-alumina, the primary particle diameter is increased, and the specific surface area is remarkably reduced.

  The carrier in the present invention has a sphere equivalent diameter of 0.5 to 20 mm, preferably 5 to 20 mm. If this value exceeds 20 mm, there is a tendency for the disadvantage that the raw material conversion rate decreases. Moreover, when this value is less than 0.5 mm, there is a tendency that the pressure loss of the reactor increases. The equivalent diameter (average value) of the spheres may be converted to the diameter of the sphere by determining the volume of the carrier and regarding it as the volume of the sphere.

Such a carrier in the present invention carries the first component and the second component.
The first component is made of cobalt (Co) metal or a compound thereof, and the metal loading is 5 × 10 ^{−5 to} 1.5 × 10 ⁻³ mol / g-support, preferably 1 × 10 ^−4. ˜5 × 10 ⁻⁴ mol / g-carrier. When the loading amount of the first component per 1 g of the carrier is less than 5 × 10 ⁻⁵ mol, desired conversion and selectivity cannot be obtained, and the loading amount of the first component per 1 g of the carrier is 1.5. If it exceeds × 10 ⁻³ mol, there is a disadvantage that the conversion rate reaches a peak despite the increase in catalyst cost.

The second component is composed of at least one metal selected from the group consisting of platinum, rhodium, ruthenium and iridium or a compound thereof, and the amount of the metal supported is 1 × 10 ⁻⁶ to 1 × 10 ⁻⁴ mol / The g-carrier is preferably 5 × 10 ^{−6 to} 5 × 10 ⁻⁵ mol / g-carrier. Particularly preferred among the second components is platinum or rhodium. When the loading amount of the second component per 1 g of the support is less than 1 × 10 ^−6, so-called hot spot generation in which the temperature in the vicinity of the catalyst layer inlet is likely to occur, and a desired conversion rate cannot be obtained. When the loading amount of the second component per 1 g of the support exceeds 1.5 × 10 ⁻³ mol, the conversion rate reaches a peak against the increase in the catalyst cost, resulting in a disadvantage that it is not economical.

  The ratio of the total number of moles of the metal of the second component to the total number of moles of the metal of the first component is 0.005 to 0.5, preferably 0.1 to 0.4. If this ratio exceeds 0.5, the conversion rate reaches a peak against the increase in catalyst cost, resulting in inconvenience that it is not economical. On the other hand, when this ratio is less than 0.005, so-called hot spot generation in which the temperature in the vicinity of the inlet of the catalyst layer rises easily occurs, and there is a tendency that a desired conversion rate cannot be obtained.

  The loading of the first component and the second component on the carrier described above may be a loading by the so-called co-impregnation method in which loading on the carrier is performed simultaneously, or the first component is loaded. It may be supported by a so-called sequential impregnation method in which the second component is subsequently supported. For specific methods of the co-impregnation method and the sequential impregnation method, refer to the examples described later.

  Next, a synthesis gas production method using the synthesis gas production catalyst of the present invention will be described.

The synthesis gas production method of the present invention is based on the premise that the above-described synthesis gas production catalyst is used, and a raw material gas containing a hydrocarbon having 1 to 5 carbon atoms, oxygen, carbon dioxide and / or steam. This is a method for producing a synthesis gas mainly composed of CO and H ₂ while being brought into contact with a synthesis gas production catalyst.

  Examples of the hydrocarbon having 1 to 5 carbon atoms in the raw material gas include methane, ethane, propane, and butane. Furthermore, natural gas containing methane as a main component and containing ethane, propane, butane or the like can also be used. This natural gas may contain carbon dioxide, nitrogen and the like.

When the hydrocarbon is methane, the production of synthesis gas mainly composed of CO and H ₂ is represented by the following reaction formulas (1) to (3). All these reactions are carried out on a catalyst.

CH ₄ + 2O ₂ → CO ₂ + 2H ₂ O Formula (1)
CH ₄ + H ₂ O → CO + 3H ₂ O Formula (2)
CH ₄ + CO ₂ → 2CO + 2H ₂ formula (3)

  As the reactor, a fixed bed reactor in which a catalyst is packed in the inside of the reaction tube is usually used. However, the reactor is not limited thereto, and may be a fluidized bed reactor, for example.

In the present invention, when the number of moles of carbon in the hydrocarbon gas as the raw material is represented by C, O ₂ / C (molar ratio) in the raw material gas is 0.4 to 1.0 (preferably 0.4 to 0.7), and CO ₂ / C (molar ratio) is in the range of 0 to 1.0 (preferably 0.05 to 0.7), and H ₂ O / C (molar ratio). ) Is in the range of 0 to 0.5 (preferably 0.1 to 0.4).

  Moreover, reaction temperature is set as the product gas temperature in the range of 700-1200 degreeC (preferably 800-1100 degreeC).

  The reaction pressure is set within the range of 0.1 MPa to 10 MPa (preferably 0.5 to 5 MPa). In addition, W / F, which is a ratio between the catalyst weight W (g) and the total introduced gas flow rate F (mol / hr), is set within a range of 0.15 to 6 (g · hr / mol).

Hereinafter, the present invention will be described in more detail with reference to specific examples.
A catalyst for syngas production was produced as follows.

(Manufacture of carrier)
First, the carrier surface area was prepared and confirmed in the following manner.

  That is, alumina beads (catalyst society reference catalyst JRC-ALO-1 2 to 3 mm in diameter) were fired at 500 ° C., 700 ° C., 900 ° C., 1200 ° C. and 1300 ° C., respectively. The measurement result of the BET specific surface area of the obtained carrier was as follows.

Carrier 1: untreated alumina beads not fired: BET specific surface area = 143 m ² / g
Carrier 2: Alumina beads fired at 500 ° C. BET specific surface area = 117 m ² / g
Carrier 3: Alumina beads calcined at 700 ° C. BET specific surface area = 102 m ² / g
Carrier 4: Alumina beads calcined at 900 ° C. BET specific surface area = 105 m ² / g
Carrier 5: Alumina beads calcined at 1200 ° C. BET specific surface area = 6 m ² / g

  By baking at 1200 ° C. or higher, the specific surface area of the carrier can be greatly reduced.

  The support | carrier used as an Example and a comparative example was selected from the said support | carrier, and various catalysts were produced in the following way, Then, the synthetic gas manufacture experiment was done according to the following reactivity evaluation test method.

(Reactivity evaluation test method)
A quartz reaction tube having an inner diameter of 6 mm, an outer diameter of 8 mm, and a length of 300 mm is filled with about 0.14 g of the catalyst adjusted as described below, and the catalyst layer can be observed from the observation window in the annular electric furnace with the observation window. Was installed.

A thermocouple was installed on the outlet side of the catalyst layer, and the output of the electric furnace was controlled so that the catalyst layer outlet gas temperature was 850 ° C. After filling the catalyst, hydrogen was circulated as a pretreatment, and the catalyst was reduced at 850 ° C. for 30 minutes. Then, the raw material gas composition in the synthesis gas production to be performed is CH ₄ : CO ₂ : H ₂ O: O ₂ = 100: 12: 29: 48 (Vol ratio), W / F (W: catalyst weight (g), F : Introduction gas flow rate (mol / hr)) was 0.6 g · hr / mol and 0.3 g · hr / mol.

  The temperature of the catalyst layer was measured from the observation window using IR thermography. In all tests, the pressure was 0.1 MPa.

(Example 1)
3 g of the carrier 5 (BET specific surface area = 6 m ² / g) weighed in 5 ml of an aqueous solution containing Co (NO ₃ ) ₂ and H ₂ PtCl ₆ (Co concentration = 0.09 mol / l; Pt concentration = 0.018 mol / l) and dried at a temperature of 120 ° C. for 12 hours. Thereafter, the dried product was fired in an air atmosphere at a temperature of 500 ° C. for 3 hours. Thus, a catalyst sample of Example 1 on which 3.0 × 10 ⁻⁵ mol / g-supported Pt and 1.5 × 10 ⁻⁴ mol / g-supported Co was supported was prepared.

  Using this catalyst, a synthesis gas production test was conducted according to the above-described reactivity evaluation test method. W / F was 0.6 g · hr / mol.

(Comparative Example 1)
3 g of the above-mentioned support 5 (BET specific surface area = 6 m ² / g) was impregnated with 5 ml of an aqueous solution containing Co (NO ₃ ) ₂ (Co concentration = 0.27 mol / l), at a temperature of 120 ° C. Dry for 12 hours. Thereafter, the dried product was fired in an air atmosphere at a temperature of 500 ° C. for 3 hours. Thus, a catalyst sample of Comparative Example 1 on which Co of 1.5 × 10 ⁻⁴ mol / g-support was supported was prepared.

  Using this catalyst, a synthesis gas production test was conducted according to the above-described reactivity evaluation test method. W / F was 0.6 g · hr / mol.

(Comparative Example 2)
3 g of the above support 5 (BET specific surface area = 6 m ² / g) was impregnated with 5 ml of an aqueous solution containing H ₂ PtCl ₆ (Pt concentration = 0.018 mol / l), and the temperature was 120 ° C. for 12 hours. Dried. Thereafter, the dried product was fired in an air atmosphere at a temperature of 500 ° C. for 3 hours. Thus, a catalyst sample of Comparative Example 2 on which 3.0 × 10 ⁻⁵ mol / g-support of Pt was supported was prepared.

  Using this catalyst, a synthesis gas production test was conducted according to the above-described reactivity evaluation test method. W / F was 0.6 g · hr / mol.

(Comparative Example 3)
The support 5 (BET specific surface area = 6 m ² / g) used in Example 1 was replaced with the support 4 (BET specific surface area = 105 m ² / g). Other than that, in the same manner as in Example 1, a comparison was made in which Pt of 3.0 × 10 ⁻⁵ mol / g-support and Co of 1.5 × 10 ⁻⁴ mol / g-support were supported. The catalyst sample of Example 3 was prepared.

  Using this catalyst, a synthesis gas production test was conducted according to the above-described reactivity evaluation test method. W / F was set to 0.6 g · hr / mol as in Example 1.

(Example 2)
In Example 1 above, the Pt loading was reduced to 4.5 × 10 ⁻⁶ mol / g-carrier. Otherwise, the catalyst sample of Example 2 was prepared in the same manner as in Example 1.

  Using this catalyst, a synthesis gas production test was conducted according to the above-described reactivity evaluation test method. W / F was set to 0.6 g · hr / mol as in Example 1.

(Example 3)
Using the catalyst in Example 1 above, only the W / F condition was changed. That is, a synthesis gas production test was performed under the same conditions as in Example 1 except that W / F = 0.3 g · hr / mol.

(Comparative Example 4)
The catalyst in Comparative Example 3 was used, and only the W / F condition was changed. That is, a synthesis gas production test was performed under the same conditions as in Comparative Example 3 except that W / F = 0.3 g · hr / mol.

The methane conversion rate, H ₂ / CO (molar ratio), and maximum catalyst layer temperature (° C.), which are the results of the reactivity evaluation test, were determined and shown in Table 1 below.

  From the experimental results of Example 1 and Comparative Example 1, the maximum temperature of the catalyst layer can be kept low by adding Pt to Co.

From the results of Example 1, Example 3, Comparative Example 3, and Comparative Example 4, it can be seen that the reactivity decreases when the specific surface area of the carrier exceeds 10 m ² / g.

  From the results of Example 2, it can be seen that the catalyst metal still shows high activity even when the amount of the noble metal component supported is small. The reason why the maximum temperature of the catalyst layers of Example 3 and Comparative Example 4 is higher than that of the other examples is that the raw material gas flow rate per catalyst is large.

It can be used in a synthesis gas production process for producing a synthesis gas mainly composed of CO and H ₂ using a hydrocarbon gas having 1 to 5 carbon atoms such as natural gas as a raw material.

Claims (9)

Catalyst for producing synthesis gas used when converting a gas containing hydrocarbons having 1 to 5 carbon atoms, oxygen, carbon dioxide and / or steam into synthesis gas mainly composed of CO and H ₂ Because
The catalyst for syngas production includes a carrier serving as a base material, a first component supported on the carrier, and a second component,
The carrier is a molded body having a specific surface area of 10 m ² / g or less molded from a heat-resistant material,
The first component is made of cobalt or a compound containing cobalt as a main component, and the metal loading is 5 × 10 ^{−5 to} 1.5 × 10 ⁻³ mol / g-support,
The second component is composed of at least one metal selected from the group consisting of platinum, rhodium, ruthenium, and iridium or a compound thereof, and the amount of the metal supported is 1 × 10 ⁻⁶ to 1 × 10 ⁻⁴ mol. / G-catalyst for synthesis gas production, characterized by being a carrier.   The catalyst for syngas production according to claim 1, wherein the carrier is composed of at least one heat-resistant material selected from the group consisting of alumina, calcium alumina, magnesium alumina, and magnesia.   The catalyst for syngas production according to claim 1 or 2, wherein the carrier is composed of α-alumina.   The catalyst for syngas production according to any one of claims 1 to 3, wherein the support has a spherical equivalent diameter of 0.5 to 20 mm.   The synthesis gas production according to any one of claims 1 to 4, wherein the ratio of the total number of moles of metal of the second component to the total number of moles of metal of the first component is 0.005 to 0.5. Catalyst. The catalyst for syngas production according to any one of claims 1 to 5, wherein the support has a specific surface area of 0.2 to 10 m ² / g. By bringing a raw material gas containing a hydrocarbon having 1 to 5 carbon atoms, oxygen, carbon dioxide and / or steam into contact with a catalyst for production of synthesis gas, a synthesis gas mainly composed of CO and H ₂ is produced. A method of manufacturing comprising:
The synthesis gas production catalyst used in the method includes a carrier serving as a base material, a first component supported on the carrier, and a second component,
The carrier is a molded body having a specific surface area of 10 m ² / g or less molded from a heat-resistant material,
The first component is made of cobalt or a compound containing cobalt as a main component, and the metal loading is 5 × 10 ^{−5 to} 1.5 × 10 ⁻³ mol / g-support,
The second component is composed of at least one metal selected from the group consisting of platinum, rhodium, ruthenium, and iridium or a compound thereof, and the amount of the metal supported is 1 × 10 ⁻⁶ to 1 × 10 ⁻⁴ mol. / G-a method for producing synthesis gas, which is a carrier. When the number of moles of carbon in the hydrocarbon gas as the raw material is represented by C, O ₂ / C (molar ratio) in the raw material gas is in the range of 0.4 to 1.0, and CO ₂ / C (mol Ratio) is in the range of 0 to 1.0 and H ₂ O / C (molar ratio) is in the range of 0 to 0.5,
The reaction temperature is set as a product gas temperature in a range of 700 to 1200 ° C.
The reaction pressure is set within the range of 0.1 MPa to 10 MPa,
8. The W / F, which is the ratio between the catalyst weight W (g) and the total introduced gas flow rate F (mol / hr), is set within a range of 0.15 to 6 (g · hr / mol). A method for producing the described synthesis gas. The method for producing a synthesis gas according to claim 7 or 8, wherein the carrier has a specific surface area of 0.2 to 10 m ² / g.