JP2009029771A - Method for producing aromatic compound - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To increase the production amount of aromatic compounds of useful components such as benzene, toluene, etc., by improving an active life span stability of methane conversion rate, benzene production rate, naphthalene production rate and BTX production rate (the total production rate of the benzene, toluene and xylene). <P>SOLUTION: This method for producing the aromatic compound comprises reacting a lower hydrocarbon and carbon dioxide gas with a catalyst prepared by loading molybdenum and silver on a metallosilicate carrier, to produce aromatic compounds. In the method for producing the aromatic compound, the amount of the carbon dioxide gas to be added is preferably set to 0.5 to 6% range based on the whole reaction gases. It is also preferable to load the metals by setting the loaded concentration of the molybdenum after calcining so as to become 2 to 12 wt.% based on the carrier, and also setting the rate X in the silver to molybdenum molar ratio in the formula (Ag:Mo)=(X:1) so as to become 0.01 to 0.3. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to advanced utilization of natural gas, biogas, and methane hydrate mainly composed of methane. Natural gas, biogas, and methane hydrate are considered to be the most effective energy resources as a countermeasure against global warming, and there is an increasing interest in their utilization technologies. Methane resources are attracting attention as the next generation of new organic resources and hydrogen resources for fuel cells, taking advantage of cleanliness. In particular, the present invention relates to catalytic chemical conversion technology for efficiently producing aromatic compounds mainly composed of benzene and naphthalene, which are raw materials for chemical products such as plastics, and high-purity hydrogen gas from methane, and catalyst production technology thereof. About.

  As a method of producing an aromatic compound such as benzene and hydrogen from methane, a method of reacting methane in the presence of a catalyst is known. As the catalyst at this time, molybdenum supported on ZSM-5-based zeolite is effective (Non-patent Document 1). However, even when these catalysts are used, there are problems that carbon deposition is large and methane conversion is low. In order to solve this problem, a catalyst in which a catalyst material such as Mo (molybdenum) is supported on a porous metallosilicate has been proposed (Patent Document 1, Patent Document 2, etc.).

In Patent Document 1 and Patent Document 2, lower hydrocarbons are efficiently converted into aromatic compounds by using a catalyst in which a metal component is supported on a porous metallosilicate having a 7 angstrom pore diameter as a carrier. Accompanyingly, it has been confirmed that high purity hydrogen can be obtained. According to the patent document, molybdenum, cobalt, iron or the like is supported on the carrier as the metal component.
JOURNAL OF CATALYSIS, 1997, pp. 165, pp. 150-161 JP 10-272366 A Japanese Patent Laid-Open No. 11-60514

  As a method for producing an aromatic compound such as benzene and hydrogen from methane, a catalyst in which molybdenum is supported on ZSM-5 is effective as a method for reacting methane in the presence of a catalyst.

  However, the methane conversion rate (utilization rate of methane used for producing aromatic compounds and hydrogen) is low.

  In order to improve this problem, a catalyst in which molybdenum and another second metal are supported on a porous metallosilicate has been proposed as in Patent Document 1 and Patent Document 2, but the methane conversion rate is further improved. In order to increase the production efficiency of the aromatic compound, development of a more excellent catalyst is desired.

  Therefore, in the method for producing an aromatic compound for solving the above-mentioned problem, an aromatic compound is produced by reacting a lower hydrocarbon and carbon dioxide gas with a catalyst in which molybdenum and silver are supported on a metallosilicate as a carrier.

  According to this method for producing an aromatic compound, the active life stability of the methane conversion rate, the benzene production rate, the naphthalene production rate and the BTX production rate (total production rate of benzene, toluene and xylene) is improved.

  Examples of the metallosilicate include ZSM-5 and MCM-22. In addition, the supported concentration of the molybdenum after the baking is 2 to 12% by weight with respect to the support, and the silver has a molar ratio Ag: Mo = X: 1 of molybdenum to the ratio X of 0.01 to 0. .3 should be supported. The improvement of the active life stability is ensured. The firing temperature after molybdenum and silver are supported on the metallosilicate may be set in the range of 400 to 700 ° C. The strength and properties of the catalyst are maintained.

  In the method for producing an aromatic compound, the amount of carbon dioxide added may be set in the range of 0.5 to 6% with respect to the entire reaction gas. The production amount of aromatic compounds which are useful components such as benzene and toluene is stabilized.

  According to the above invention, active life stability of methane conversion rate, benzene formation rate, naphthalene formation rate and BTX formation rate (total formation rate of benzene, toluene and xylene) is improved, so useful components such as benzene and toluene The production amount of the aromatic compound is increased.

  The lower hydrocarbon aromatization catalyst according to the present invention contains at least one selected from molybdenum and its compounds as a catalyst material. When the aromatic compound is produced, the lower hydrocarbon aromatization catalyst is reacted with carbon dioxide gas (carbon dioxide) in addition to the lower hydrocarbon.

  The carrier carrying the metal component substantially includes a porous metallosilicate having pores with a diameter of 4.5 to 6.5 angstroms. This metallosilicate carries molybdenum as the first metal component and silver as the second metal component other than molybdenum. The molybdenum component and silver component may be dried and fired after the metallosilicate is added to an aqueous impregnation solution prepared with silver acetate or silver nitrate and ammonium molybdate to impregnate the metallosilicate with the molybdenum component and the silver component. Supported on the metallosilicate. Thus, the stability of the catalyst can be obtained by supporting not only MoC (molybdenum carbide), that is, a molybdenum component, but also silver as a second metal component in addition to the molybdenum component in the porous metallosilicate. In particular, the active life stability of methane conversion rate, benzene production rate, naphthalene production rate and BTX production rate (total production rate of benzene, toluene and xylene) is improved.

  The lower hydrocarbon aromatization catalyst used in the production method according to the invention will be described with reference to the following comparative examples and examples.

1. Production of lower hydrocarbon aromatization catalyst (hereinafter abbreviated as catalyst) (Comparative Example 1)
The catalyst of Comparative Example 1 employs ammonium type ZSM-5 (SiO ₂ / Al ₂ O ₃ = 25-60) as a metasilicate, and only molybdenum is supported thereon.

(1) Blending Blending of inorganic components: ZSM-5 (82.5 wt%), clay (12.5 wt%), glass fiber (5 wt%)
Total formulation: inorganic component (76.5 wt%), organic binder (17.3 wt%), moisture (24.3 wt%)
(2) Molding The inorganic component, organic binder, and moisture were blended at the blending ratio, and mixed and kneaded by a kneading means (kneader). Next, this mixture was molded into a rod shape (diameter 5 mm × length 10 mm) with a vacuum extrusion molding machine. The extrusion pressure at the time of molding at this time was set to 2 to 8 MPa.

  Usually, the catalyst support used for reforming hydrocarbons is used as a fluidized bed catalyst using particles having a particle size of several μm to several hundred μm. In this case, the catalyst carrier is produced by mixing a catalyst carrier material, an organic binder, an inorganic binder (usually using clay) and water, forming a slurry and granulating it with a spray dryer (no molding pressure), followed by firing. . In this case, since there was no molding pressure, the amount of clay added as a firing aid to ensure the firing rate was about 40 to 60% by weight. Here, the amount of the additive such as clay added as a firing aid can be reduced to 15 to 25% by weight by molding the catalyst at a high pressure using a vacuum extrusion molding machine. Therefore, the catalytic activity can also be improved.

(3) Impregnation of molybdenum The molded body obtained in the molding step was added to the stirred ammonium molybdate aqueous solution to impregnate the molded body with the molybdenum component, and then subjected to the following drying and firing steps. The molded body was added so that the weight ratio of molybdenum to ZSM-5 was 6% by weight.

(4) Drying and calcination Drying was carried out at 70 ° C. for 12 hours and then at 90 ° C. for about 36 hours in order to remove moisture added during molding. Firing was performed at 90 to 100 ° C./hour for both the heating rate and the cooling rate. In order to prevent the organic binder added at the time of molding from burning instantaneously, the temperature was held twice in the temperature range of 250 to 500 ° C. for about 2 to 6 hours to remove the binder. This is because the rate of temperature increase and the rate of temperature decrease are higher than this, and when the keep time for removing the binder is not secured, the binder burns instantaneously and the strength of the fired body decreases. The firing temperature was in the range of 550 to 800 ° C. This is because the strength of the carrier is lowered at 550 ° C. or lower, and the properties are lowered at 800 ° C. or higher. In addition, it baked here at 550 degreeC for 5 hours in the air.

(5) Carbonization treatment The fired body is heated to 700 ° C. in 2 hours under a flow of a mixed gas of CH ₄ and H ₂ (mixed molar ratio of methane / hydrogen = 1/4), and this state is maintained for 3 hours. did. Thereafter, this atmosphere was switched to a reaction gas of CH _{4 and} the temperature was raised to 780 ° C. to obtain a catalyst according to Comparative Example 1.

(Comparative Example 2)
The catalyst of Comparative Example 2 supported molybdenum and cobalt, and was produced by the same method as the steps of compounding, molding, drying, firing and carbonizing treatment of the catalyst of Comparative Example 1 except for the impregnation step.

  In the impregnation step, the molded body obtained in the molding step is added while stirring the aqueous impregnated solution prepared with cobalt acetate and ammonium molybdate to impregnate the molded body with the molybdenum component and the cobalt component, followed by drying and evaporation to dryness. Solidified. And this was calcined in the air at 550 degreeC for 5 hours, and the catalyst which carry | supported molybdenum and cobalt was obtained. The supported amount of molybdenum was set to 6 wt% with respect to ZSM-5, and the supported amount of cobalt was set to be cobalt: molybdenum = 0.3: 1.0 in terms of molar ratio with molybdenum.

(Comparative Example 3)
The catalyst of Comparative Example 3 supported molybdenum and iron, and was produced by the same method as the steps of compounding, molding, drying, firing and carbonizing treatment of the catalyst of Comparative Example 1 except for the impregnation step.

  In the impregnation step, the impregnated aqueous solution prepared with iron acetate and ammonium molybdate is stirred and the shaped product obtained in the forming step is added to impregnate the shaped product with the molybdenum component and the iron component, followed by drying and evaporation to dryness. Solidified. And this was baked in the air at 550 degreeC for 5 hours, and the catalyst which carry | supported molybdenum and iron was obtained. The supported amount of molybdenum was set to 6% by weight with respect to ZSM-5, and the supported amount of iron was set to iron: molybdenum = 0.3: 1.0 in terms of molar ratio with molybdenum.

Example 1
The catalyst of Example 1 supported molybdenum and silver, and was produced by the same method as the steps of compounding, molding, drying, firing and carbonization treatment of Comparative Example 1 except for the impregnation step.

  In the impregnation step, the molded product obtained in the molding step is added while stirring the aqueous impregnation solution prepared with silver acetate and ammonium molybdate, and the molded product is impregnated with the molybdenum component and the silver component, and then dried and evaporated to dryness. Solidified. And this was calcined in air at 550 ° C. for 5 hours to obtain a catalyst carrying molybdenum and silver. The supported amount of molybdenum was set to 6% by weight with respect to ZSM-5, and the supported amount of silver was set such that silver: molybdenum = 0.3: 1.0 in terms of molar ratio with molybdenum.

(Example 2)
The catalyst of Example 2 carries silver and molybdenum at a molar ratio of silver: molybdenum = 0.6: 1.0, and the catalyst production process of Comparative Example 1 (molding, molding, (Drying, baking and carbonization treatment).

  In the molding step, the mixture of the inorganic component, the organic binder, and moisture according to Comparative Example 1 was molded into a rod shape (diameter 2.4 mm × length 5 mm) with a vacuum extrusion molding machine at an extrusion pressure of 2 to 8 MPa. In the impregnation step, an aqueous impregnation solution prepared with silver acetate and ammonium molybdate is stirred, and a molded body containing ZSM-5 that has undergone the molding step is added to the stirred aqueous impregnation solution, so that a molybdenum component and a silver component are added. Were impregnated into the molded body. Then, after drying this, it baked in the air at 550 degreeC for 5 hours, and obtained the ZSM-5 support | carrier which carry | supported molybdenum and silver. In preparation of the aqueous impregnation solution, the supported amount of molybdenum is 6% by weight with respect to the total amount of the catalyst after calcination, and the supported amount of silver is silver: molybdenum = 0.6: It was set to 1.0.

(Example 3)
The catalyst of Example 3 carries silver and molybdenum in a molar ratio of silver: molybdenum = 0.8: 1.0, and the production process of the catalyst of Comparative Example 1 (molding, molding, (Drying, baking and carbonization treatment).

  In the molding step, the mixture of the inorganic component, the organic binder, and moisture according to Comparative Example 1 was molded into a rod shape (diameter 2.4 mm × length 5 mm) with a vacuum extrusion molding machine at an extrusion pressure of 2 to 8 MPa. In the impregnation step, an aqueous impregnation solution prepared with silver acetate and ammonium molybdate is stirred, and a molded body containing ZSM-5 that has undergone the molding step is added to the stirred aqueous impregnation solution, so that a molybdenum component and a silver component are added. Were impregnated into the molded body. Then, after drying this, it baked in the air at 550 degreeC for 5 hours, and obtained the ZSM-5 support | carrier which carry | supported molybdenum and silver. In the preparation of the aqueous impregnation solution, the supported amount of silver is 6% by weight based on the total amount of the catalyst after calcination, and the supported amount of silver is silver: molybdenum = 0.8: It was set to 1.0.

Example 4
The catalyst of Example 4 carries silver and molybdenum at a molar ratio of silver: molybdenum = 0.1: 1.0, and the production process of the catalyst of Comparative Example 1 (molding, molding, (Drying, baking and carbonization treatment).

  In the molding step, the mixture of the inorganic component, the organic binder, and moisture according to Comparative Example 1 was molded into a rod shape (diameter 2.4 mm × length 5 mm) with a vacuum extrusion molding machine at an extrusion pressure of 2 to 8 MPa. In the impregnation step, an aqueous impregnation solution prepared with silver acetate and ammonium molybdate is stirred, and a molded body containing ZSM-5 that has undergone the molding step is added to the stirred aqueous impregnation solution, so that a molybdenum component and a silver component are added. Were impregnated into the molded body. Then, after drying this, it baked in the air at 550 degreeC for 5 hours, and obtained the ZSM-5 support | carrier which carry | supported molybdenum and silver. In the preparation of the aqueous impregnation solution, the supported amount of silver is 6% by weight based on the total amount of the catalyst after calcination, and the supported amount of silver is silver: molybdenum = 0.1: It was set to 1.0.

(Example 5)
The catalyst of Example 5 carries silver and molybdenum at a molar ratio of silver: molybdenum = 0.3: 1.0, and the catalyst production process (molding, molding, (Drying, baking and carbonization treatment).

  In the molding step, the mixture of the inorganic component, the organic binder, and moisture according to Comparative Example 1 was molded into a rod shape (diameter 2.4 mm × length 5 mm) with a vacuum extrusion molding machine at an extrusion pressure of 2 to 8 MPa. In the impregnation step, an aqueous impregnation solution prepared with silver acetate and ammonium molybdate is stirred, and a molded body containing ZSM-5 that has undergone the molding step is added to the stirred aqueous impregnation solution, so that a molybdenum component and a silver component are added. Were impregnated into the molded body. Then, after drying this, it baked in the air at 550 degreeC for 5 hours, and obtained the ZSM-5 support | carrier which carry | supported molybdenum and silver. In preparation of the aqueous impregnation solution, the supported amount of silver was 6% by weight based on the total amount of the catalyst after calcination, and the supported amount of silver was silver: molybdenum = 0.3: It was set to 1.0.

2. Evaluation of Catalysts of Comparative Examples and Examples Evaluation methods of the catalysts of Comparative Examples and Examples will be described. As shown in FIG. 9, 14 g of the catalyst to be evaluated (zeolite ratio 82.50%) was filled in the reaction tube (inner diameter: 18 mm) of the inconel 800H gas contact part calorizing treatment of the fixed bed flow type reactor 1. And based on the conditions shown in Table 1, the reaction gas was supplied to the said reaction tube. That is, under conditions of reaction space velocity = 3000 ml / g-MFI / h (CH ₄ gas flow base), reaction temperature 780 ° C., reaction time 24 hours, reaction pressure 0.3 MPa, catalyst and reaction gas (100 methane (CH ₄ ) +3 carbon dioxide gas (CO ₂ )). At this time, the product was analyzed, and the methane conversion rate, benzene production rate, naphthalene production rate, and BTX production rate were examined over time. The product was analyzed using TCD-GC and FID-GC.

Methane conversion rate, benzene production rate, naphthalene production rate and BTX production rate are defined as follows.
“Methane conversion rate (%)” = [(“Raw material methane flow rate” − “Unreacted methane flow rate”) / “Raw material methane flow rate”] × 100
“Benzene production rate” = “nmol number of benzene produced per second per 1 g of catalyst”.
“Naphthalene production rate” = “nmol number of naphthalene produced per second per 1 g of catalyst”.
“BTX production rate” = “total number of nmols of benzene, toluene and xylene produced per second per gram of catalyst”.

  FIG. 1 shows changes over time in the methane conversion rate when each of the catalysts according to Comparative Examples 1 to 3 and Example 1 is reacted with methane gas and carbon dioxide gas. As is clear from the time-dependent change in the methane conversion rate shown in this characteristic diagram, the catalyst of Example 1 (a catalyst supporting molybdenum and silver (Ag / Mo)) was used in Comparative Example 1 according to the prior art. Catalyst (catalyst (Mo) carrying only molybdenum (Mo)) catalyst of Comparative Example 2 (catalyst carrying molybdenum and cobalt (Co / Mo)), catalyst of Comparative Example 3 (catalyst carrying molybdenum and iron (Fe / Mo)) Compared with Mo)), the stability of the active lifetime of the methane conversion is improved.

  FIG. 2 shows changes over time in the benzene production rate when each of the catalysts according to Comparative Examples 1 to 3 and Example 1 was reacted with methane gas and carbon dioxide gas. As is apparent from this characteristic diagram, according to the catalyst (Ag / Mo) of Example 1, the catalyst of Comparative Example 1 (Mo), the catalyst of Comparative Example 2 (Co / Mo), and the catalyst of Comparative Example 3 according to the prior art Compared with (Fe / Mo), the stability of the active lifetime of the benzene formation rate is improved.

  FIG. 3 shows changes over time in the naphthalene production rate when each of the catalysts according to Comparative Examples 1 to 3 and Example 1 is reacted with methane gas and carbon dioxide gas. As is apparent from this characteristic diagram, according to the catalyst (Ag / Mo) of Example 1, the catalyst of Comparative Example 1 (Mo), the catalyst of Comparative Example 2 (Co / Mo), and the catalyst of Comparative Example 3 according to the prior art Compared with (Fe / Mo), the stability of the active lifetime of the naphthalene production rate is improved.

  FIG. 4 shows the change over time of the BTX production rate when each of the catalysts according to Comparative Examples 1 to 3 and Example 1 is reacted with methane gas and carbon dioxide gas. As is apparent from this characteristic diagram, according to the catalyst (Ag / Mo) of Example 1, the catalyst of Comparative Example 1 (Mo), the catalyst of Comparative Example 2 (Co / Mo), and the catalyst of Comparative Example 3 according to the prior art Compared with (Fe / Mo), the stability of the active lifetime of the BTX generation rate is improved.

  Table 2 shows the methane conversion rate, benzene production rate, and BTX production after a reaction time of 3 to 24 hours when each of the catalysts according to Examples 2 to 5 was reacted with methane gas and carbon dioxide gas based on the evaluation method. It is a list of rate of change of speed. In particular, it can be confirmed that the catalysts according to Example 4 and Example 5 are more effective than the catalysts according to Example 2 and Example 3 from the viewpoint of the rate of change in methane conversion rate, benzene production rate, and BTX production rate.

  FIG. 5 shows changes over time in the methane conversion rate when each of the catalysts according to Example 4 and Example 5 was reacted with methane gas and carbon dioxide gas. As is clear from this characteristic diagram, according to the catalysts according to Example 4 and Example 5, the stability of the active life of the methane conversion rate is improved.

  FIG. 6 shows changes with time in the benzene production rate when each of the catalysts according to Example 4 and Example 5 was reacted with methane gas and carbon dioxide gas. As is clear from this characteristic diagram, according to the catalysts according to Example 4 and Example 5, the stability of the active lifetime of the benzene production rate is improved.

  FIG. 7 shows changes over time in the naphthalene production rate when each of the catalysts according to Example 4 and Example 5 is reacted with methane gas and carbon dioxide gas. As is clear from this characteristic diagram, according to the catalysts according to Example 4 and Example 5, the stability of the active lifetime of the naphthalene production rate is improved.

  FIG. 8 shows the change with time of the BTX generation rate when each of the catalysts according to Example 4 and Example 5 was reacted with methane gas and carbon dioxide gas. As is clear from this characteristic diagram, according to the catalysts according to Example 4 and Example 5, the stability of the active life of the BTX generation rate is improved.

  As is apparent from the results of the above examples, the metallosilicate is supported with silver as a second metal component in addition to molybdenum to form a lower hydrocarbon aromatization catalyst, and this catalyst is used as a lower hydrocarbon and carbon dioxide gas. It was shown that the activity lifetime stability of methane conversion rate, benzene formation rate and naphthalene formation rate was improved by reacting with. Furthermore, it has been shown that the production rate of BTX, which is a useful component such as benzene and toluene, is stable. In particular, when the molar ratio Ag: Mo = X: 1 of the silver to molybdenum ratio X is in the range of 0.01 to 0.3, the methane conversion is further stabilized, and the active life stability of the catalyst is ensured. It has been shown to improve.

The catalyst of Comparative Example 1 (at the time of Mo single loading), Comparative Example 2 (at the same time of Co / Mo loading), Comparative Example 3 (at the same time of Fe / Mo loading), and Example 1 (at the same time of Ag / Mo loading) Change with time of methane conversion rate when each is reacted with methane gas and carbon dioxide gas. The catalyst of Comparative Example 1 (at the time of Mo single loading), Comparative Example 2 (at the same time of Co / Mo loading), Comparative Example 3 (at the same time of Fe / Mo loading), and Example 1 (at the same time of Ag / Mo loading) Changes in benzene production rate over time when each is reacted with methane gas and carbon dioxide gas. The catalyst of Comparative Example 1 (at the time of Mo single loading), Comparative Example 2 (at the same time of Co / Mo loading), Comparative Example 3 (at the same time of Fe / Mo loading), and Example 1 (at the same time of Ag / Mo loading) Changes in the naphthalene production rate over time when each was reacted with methane gas and carbon dioxide gas. The catalyst of Comparative Example 1 (at the time of Mo single loading), Comparative Example 2 (at the same time of Co / Mo loading), Comparative Example 3 (at the same time of Fe / Mo loading), and Example 1 (at the same time of Ag / Mo loading) The time-dependent change of the BTX production | generation rate at the time of making each react with methane gas and a carbon dioxide gas. Each of the catalysts according to Example 4 (Ag / Mo molar ratio Ag / Mo = 0.1) and Example 5 (Ag / Mo molar ratio Ag / Mo = 0.3) was reacted with methane gas and carbon dioxide gas. Change in methane conversion rate over time. Each of the catalysts according to Example 4 (Ag / Mo molar ratio Ag / Mo = 0.1) and Example 5 (Ag / Mo molar ratio Ag / Mo = 0.3) was reacted with methane gas and carbon dioxide gas. Change in benzene production rate with time. Each of the catalysts according to Example 4 (Ag / Mo molar ratio Ag / Mo = 0.1) and Example 5 (Ag / Mo molar ratio Ag / Mo = 0.3) was reacted with methane gas and carbon dioxide gas. Change of naphthalene formation rate with time. Each of the catalysts according to Example 4 (Ag / Mo molar ratio Ag / Mo = 0.1) and Example 5 (Ag / Mo molar ratio Ag / Mo = 0.3) was reacted with methane gas and carbon dioxide gas. Change in BTX generation rate with time. The schematic of the fixed bed flow-type reaction apparatus used for the aromatization reaction of a lower hydrocarbon.

Claims (5)

A method for producing an aromatic compound, characterized in that an aromatic compound is produced by reacting a lower hydrocarbon and carbon dioxide with a catalyst obtained by supporting molybdenum and silver on a metallosilicate as a carrier. The method for producing an aromatic compound according to claim 1, wherein the amount of carbon dioxide added is in the range of 0.5 to 6% with respect to the entire reaction gas. The method for producing an aromatic compound according to claim 1 or 2, wherein the metallosilicate is ZSM-5 or MCM-22. The supported concentration of the molybdenum after firing is 2 to 12% by weight with respect to the support, and the silver has a molar ratio Ag: Mo = X: 1 of molybdenum to the ratio X of 0.01 to 0.3. The method for producing an aromatic compound according to any one of claims 1 to 3, wherein the aromatic compound is supported so as to become. The method for producing an aromatic compound according to any one of claims 1 to 4, wherein a firing temperature after molybdenum and silver are supported on the metallosilicate is 400 to 700 ° C.

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