KR20120077973A - Process for producing aromatics using transition metal phosphide catalyst - Google Patents

Abstract

PURPOSE: A producing method of an aromatic product using a transition metal phosphide catalyst is provided to enable use the catalyst capable of using for a long time compare to a conventional catalyst for the hydro-desulfurization/denitrification. CONSTITUTION: A producing method of an aromatic product using a transition metal phosphide catalyst comprises the following steps: distill-separating coal tar to obtain bottom oil and distilled oil(U1); and performing the hydro-desulfurization/denitrification with the distilled oil under the presence of the transition metal phosphide catalyst for removing sulfur, nitrogen, sulfur compounds, or nitrogen compounds from the distilled oil(U2). The transition metal phosphide catalyst contains more than one compound selected from the group consisting of Ni2P, Co2P, Fe2P, MoP, and WP, and is deposited in more than one carrier selected from silica alumina, alumina, zinc oxide, zirconia, ceria, silica, zeolite, mesoporous silica, clay, USY zeolite, saponite, or titania.

Description

Process for Producing Aromatic Products Using Transition Metal Phosphate Catalysts {PROCESS FOR PRODUCING AROMATICS USING TRANSITION METAL PHOSPHIDE CATALYST}

The present application relates to a method for producing an aromatic product, and more particularly, to a method for producing an aromatic product using a transition metal phosphide catalyst.

When the raw coal is carbonized in a conventional coke oven during the metallurgical coke manufacturing process during the steelmaking process, solid coke is obtained in the carbonization chamber of the coke oven, whereas as a by-product, liquid coal tar and gaseous coke oven gas (COG) are used. ) Is obtained.

Coal tar is a mixture of various aromatic carbon compounds having two or three or more benzene rings and a small amount of sulfur or nitrogen compounds, although there are little differences depending on the composition of the raw coal for producing coke and the conditions for producing coke.

Coke oven gas (COG), which has the largest calorific value among the by-products of the steelmaking process, is recycled as a primary energy source for heating the steelmaking process, and therefore has low added value.In the case of coal tar regeneration process, which reaches 10wt% of COG, Is converted to carbon black, naphthalene, pitch, etc. through energy-intensive pyrolysis process that requires high temperature of 1,200K or more, and is used as low-value raw materials such as tire, cement admixture, aluminum refining, etc. In order to use it, it is required to utilize it in the manufacture of aromatic products such as benzene, toluene or xylene which are high value-added chemicals.

However, coal tar generated as a by-product of the steelmaking process contains a large amount of nitrogen compounds and sulfur compounds, which are not easy to decompose and separate, and thus cannot be used for the production of high value-added chemicals, and gaseous coke oven gas (COG) is also a high value chemical. There was a problem that cannot be used in the manufacture of the product.

Accordingly, the present invention has been made to solve the problems of the prior art as described above and the technical problems that have been requested from the past, the object of the present invention is the durability that can be used for a longer period of time than the existing catalyst used for hydrogenation desulfurization / denitrification reaction The present invention seeks to provide an efficient process for the production of low sulfur, low pollution and high value added aromatic products using a novel transition metal phosphide catalyst.

It is another object of the present invention to provide a method for producing an aromatic product having a high alternative effectiveness with an existing method because of similar operating conditions with existing catalysts.

It is another object of the present invention to provide a method for producing an aromatic product having excellent hydrogenation desulfurization / denitrification efficiency.

The present invention also seeks to provide a process for producing aromatic products which can use coke oven gas as a hydrogen source.

As a technical means for achieving the above-described technical problem, the first aspect of the present invention, the step of distilling coal tar to separate the remaining oil and effluent oil (a); (B) removing sulfur, nitrogen, sulfur compounds or nitrogen compounds contained in the effluent oil by hydrodesulfurization / denitrification reaction of the effluent oil in the presence of a transition metal phosphide catalyst; And converting the effluent oil which has undergone the hydrodesulfurization / denitrification reaction into an aromatic product comprising at least one selected from benzene, toluene and xylene through a catalytic cracking reaction. Can be provided.

According to one embodiment of the present invention, the transition metal phosphide catalyst of step (b) may include at least one metal selected from Group 6, Group 8 to Group 10 metals of the periodic table.

According to another embodiment of the present invention, the transition metal phosphide catalyst of step (b) may include one or more selected from Ni ₂ P, Co ₂ P, Fe ₂ P, MoP and WP.

According to another embodiment of the present invention, the transition metal phosphide catalyst of step (b) is one or more selected from Ni ₂ P, Co ₂ P, Fe ₂ P, MoP and WP silica alumina (SiO ₂ -Al ₂ O ₃ ), alumina (Al ₂ O ₃ ), zinc oxide (ZnO), zirconia (ZrO ₂ ), ceria (CeO ₂ ), silica (SiO ₂ ), zeolite, porous silica (Mesoporous silica), clay (Clay), USY zeolite (zeolite), saponite (Saponite) and titania (TiO ₂ ) may be supported on at least one selected from.

According to another embodiment of the present invention, the step (b) may be operated at a temperature of 200 to 1000 ℃ and a pressure of 10 to 200 atm.

According to another embodiment of the present invention, the step (b) may be a step of using a coke oven gas (coke oven gas) as a hydrogen source of the hydrodesulfurization / denitrification reaction.

According to another embodiment of the present invention, the catalytic cracking reaction process is characterized in that at least one reaction selected from pyrolysis reaction, dealkylation reaction, isomerization reaction, transalkylation reaction and alkylation reaction is carried out.

According to another embodiment of the invention, the method for producing the aromatic product may be carried out in a batch reactor, a continuous fixed bed reactor or a continuous fluidized bed reactor.

Another aspect of the present invention can provide an aromatic product prepared according to the method for producing an aromatic product.

According to the present invention, it is possible to provide a method for producing a high value-added aromatic compound as a product using coal tar as a raw material.

In addition, the present invention can provide a method for producing an aromatic product using a durable transition metal phosphide catalyst that can be used longer than the conventional catalyst.

In addition, the present invention can provide a method for producing an aromatic product having a large alternative effectiveness of the conventional method for producing an aromatic product because the operating method is similar to the production method of an aromatic product using a conventional catalyst.

In another aspect, the present invention can provide a method for producing an aromatic product that can use the coke oven gas as a hydrogen source.

In addition, the present invention can provide a method for producing an aromatic product excellent in hydrogenation desulfurization / denitrification effect.

1 is a process schematic showing one embodiment according to the present invention.

DETAILED DESCRIPTION Hereinafter, embodiments and embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art may easily implement the present invention.

However, the following description is not intended to limit the present invention to specific embodiments, and it should be understood that the present invention covers all the transformations, equivalents, and substitutes included in the spirit and scope of the present invention. In the following description of the present invention, if it is determined that the detailed description of the related known technology may obscure the gist of the present invention, the detailed description thereof will be omitted.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. Singular expressions include plural expressions unless the context clearly indicates otherwise. In this application, the terms "comprise" or "have" are intended to indicate that there is a feature, number, step, operation, component, part, or combination thereof described in the specification, and one or more other features. It is to be understood that the present invention does not exclude the possibility of the presence or the addition of numbers, steps, operations, components, components, or a combination thereof.

In addition, the expression "low temperature-temperature programmed reduction (LT-TPR)" means a method of reducing the catalyst supported on the support at a low temperature (about 500 ℃ or less).

In addition, the expression "ligand stabilization method" means a method capable of ligand stabilization, lowering the reduction temperature of the catalyst and high dispersion on the carrier by using a surfactant and a reducing agent.

As a technical means for achieving the above-described technical problem, the first aspect of the present invention, the step of distilling coal tar to separate the remaining oil and effluent oil (a); (B) removing sulfur, nitrogen, sulfur compounds or nitrogen compounds contained in the effluent oil by hydrodesulfurization / denitrification reaction of the effluent oil in the presence of a transition metal phosphide catalyst; And converting the effluent oil which has undergone the hydrodesulfurization / denitrification reaction into an aromatic product comprising at least one selected from benzene, toluene and xylene through a catalytic cracking reaction. Can be provided.

The distillation separation process of the present invention is to separate the coal tar used as a raw material according to the boiling point range and to use the light fraction to produce aromatic products such as benzene, toluene and xylene, the coal tar fraction is introduced into the distillation separation process The oil is separated into an effluent oil, which is an oil containing a sulfur compound, a nitrogen compound, and an aromatic compound having one or two benzene rings, and separated into a residual oil that is an oil containing an aromatic compound having three or more benzene rings.

In the present invention, the hydrodesulfurization / denitrification reaction process is included in the oil to produce a low pollution aromatic product with very little generation of SOx and NOx and to maintain the activity of the catalyst used in the subsequent catalytic cracking reaction process. As a step for removing sulfur compounds and nitrogen compounds which are impurities, it proceeds by reacting the oil with hydrogen in the presence of the transition metal phosphide catalyst for hydrogenation.

According to one embodiment of the invention, the transition metal phosphide catalyst of the hydrodesulfurization / denitrification reaction step may include one or more metals selected from Group 6, Group 8 to Group 10 metals of the periodic table, more preferably May include at least one selected from Ni ₂ P, Co ₂ P, Fe ₂ P, MoP, and WP, and more preferably 1 selected from Ni ₂ P, Co ₂ P, Fe ₂ P, MoP, and WP. Species more than alumina (Al ₂ O ₃ ), zinc oxide (ZnO), zirconia (ZrO ₂ ), ceria (CeO ₂ ), silica (SiO ₂ ), porous silica (Mesoporous silica), clay (Clay), USY zeolite It may be supported on one or more selected from zeolite, saponite and titania (TiO ₂ ), and more preferably supported on alumina.

According to another embodiment of the present invention, the transition metal phosphide catalyst may be prepared by a temperature reduction method, a ligand stabilization method or a low temperature reduction method.

The low temperature reduction method is a method of producing a metal phosphide catalyst on a carrier by applying a phosphorus (P) precursor having a low oxidation number to 500 ° C. or lower, and is capable of increasing the activity per unit area of the catalyst. It is described in detail in one Korean patent application 10-2009-0067480.

According to the present invention, the transition metal phosphide catalyst comprises the steps of (1) adding a carrier to an aqueous solution of a transition metal precursor and a phosphorus precursor having an oxidation number of phosphorus +1; Drying the mixture obtained in step (1) (2); Firing the dried product obtained in the step (2) under an inert atmosphere (3); And (4) reducing the calcined material obtained in the step (3) in a hydrogen atmosphere at 200 ° C. to 500 ° C. to form a transition metal phosphide catalyst. Can be.

As for the said transition metal precursor used for the transition metal phosphide catalyst manufacturing method of this invention, it is more preferable that it is a precursor of group 6 or group 8 metal on a periodic table.

More specifically, the transition metal precursor may be selected from transition metal halides, transition metal nitrates, transition metal acetates, transition metal hydroxides or transition metal carbonyl complexes.

The phosphorus precursor used in the method for preparing a transition metal phosphide catalyst of the present invention is preferably metal hypophosphite.

More specifically, the metal hypophosphite is red hypophosphite, sodium hypophosphite, ferric hypophosphite, barium hypophosphite, bariumhypophosphite, quinine hypophosphite (quinine hypophosphite), calcium hypophosphite, potassium hypophosphite, magnesium hypophosphite, manganese hypophosphite, thiabendazole hypophosphite hypophosphite), poly (acrylic acid-co-sodium hypophosphite) or 4-ethoxycarbonyl-1- (2-hydroxy-3-phenoxypropyl) 4- Phenylpiperidine hypophosphite may be selected from 4-ethoxycarbonyl-1- (2-hydroxy-3-phenoxypropyl) 4-phenylpiperidine hypophosphite.

In addition, in the method for preparing a transition metal phosphide catalyst, the ligand stabilization method, which is a production method in which the reduction temperature is lowered and the nanocatalyst is highly dispersed on the carrier by using a ligand stabilization method and using a surfactant and a phosphorus reducing agent, is the present applicant. The method of preparing the metal phosphide catalyst described in detail in Korean Patent Application No. 10-2010-0061758 filed here can be used in the present invention.

According to the present invention, the transition metal phosphide catalyst comprises the steps of preparing a compound represented by the transition metal precursor and formula (1) ⓐ; Reacting the transition metal precursor of step ⓐ and the compound represented by Formula 1 with the compound represented by Formula 2; And it can be prepared by the method for producing a nano-transition metal phosphide catalyst using a ligand stabilization method comprising the step ⓒ impregnating the product of step ⓑ to the carrier.

[Formula 1]

R ¹ to R ³ in Formula 1 are each independently hydrogen or an alkyl group having 1 to 12 carbon atoms, more preferably an alkyl group having 6 to 10 carbon atoms.

[Formula 2]

R ⁴ to R ⁶ in Formula 2 are each independently hydrogen or an alkyl group having 1 to 12 carbon atoms, more preferably hydrogen or an alkyl group having 6 to 10 carbon atoms.

In the present invention, the transition metal precursor may be one or more selected from the group consisting of transition metal acetates, transition metal halides, transition metal nitrates, transition metal hydroxides and transition metal carbonyl complexes.

In the present invention, step ⓐ may include a step ⓓ of mixing the transition metal precursor and the compound represented by Formula 1, step ⓑ may be a step ⓔ to react the mixture of step ⓐ with the compound represented by the formula (2).

In the present invention, the step ⓓ of mixing the transition metal precursor and the compound represented by Formula 1 may be performed at 50 to 200 ° C.

According to the invention, step ⓓ of mixing the transition metal precursor and the compound represented by the formula (1) is characterized in that it is carried out for more than 5 minutes, the reaction of step ⓑ is carried out at 250 to 350 ℃, performed for 1 to 3 hours It is characterized by.

In the present invention, the step ⓒ impregnating the product of step ⓑ to the centrifugation of the product of step ⓑ; Adding the centrifuged product of step ⓕ to an organic solvent to disperse it; Contacting the carrier with the organic solvent containing the product of step ⓖ; And drying the carrier of step ⓗ.

In the present invention, the carrier is one selected from the group consisting of alumina (Al ₂ O ₃ ), zinc oxide (ZnO), zirconia (ZrO ₂ ), ceria (CeO ₂ ), silica (SiO ₂ ) and titania (TiO ₂ ). It may be more than, it is more preferable that the alumina (Al ₂ O ₃ ).

Hydrogenation desulfurization / denitrification reaction process of the present invention is the hydrogen partial pressure of 10 ~ 200 kg / cm ^{2, the amount} of hydrogen of 50 ~ 600 Nm ³ / kl, the space velocity (LHSV) of 0.1 ~ 10 h-1, 200 ~ 1,000 ℃ It is preferable to proceed under the conditions of the reaction temperature of. These conditions are suitable for hydrogenating the feed fraction to remove impurities such as sulfur and nitrogen.

According to the present invention, the hydrodesulfurization / denitrification reaction process may be performed after or before the distillation separation process. When the hydrodesulfurization / denitrification reaction process is located at the end of the distillation separation process, the effluent from distillation of coal tar is hydrodesulfurization / denitrification, and when the hydrodesulfurization / denitrification process is located at the front of the distillation separation process. Coalta is directly dehydrogenated / denitrogenated to oil and then separated into light and heavy oil.

According to the present invention, a coke oven gas may be used as a hydrogen source for the hydrodesulfurization / denitrification reaction.

In the present invention, the catalytic cracking reaction process is carried out in the hydrogenation desulfurization / denitrification process of the front end as a feedstock, and reacted with hydrogen in the presence of a catalyst to produce fuel gas, liquefied petroleum gas (LPG) and aromatic products It is a process for obtaining.

The catalyst used in the process is at least one selected from the group consisting of mordenite, beta zeolite and ZSM-5 zeolite, 10 to 95 wt% zeolite having a molar ratio of silica / alumina of 200 or less and inorganic binder 5 to 90 Mix by weight to use as a carrier. And 0.01 to 0.5 parts by weight of platinum based on the total weight of the mixed carrier and tin or lead on the carrier, and 0.1 to 5.0 parts by weight of tin, and 0.02 to 5.0 parts by weight of lead. Support.

The catalyst allows dealkylation, transalkylation, alkylation, isomerization and hydrocracking reactions of the feedstock to occur in at least one reactor in the reaction zone.

In the present invention, the hydrogenated desulfurization / denitrification fraction containing the aromatic component is introduced into the catalytic cracking reactor at a space velocity (WHSV) of 0.5 to 10 h ⁻¹ , and the temperature range of 250 to 600 ° C. and 5 to 50 atmospheres. Reacts under pressure conditions.

In the catalytic cracking reactor, dealkylation, transalkylation, alkylation, isomerization and hydrocracking reactions of aromatic components are carried out in the presence of the above reaction conditions and catalysts. Through such a reaction process, aromatic components such as benzene, toluene and xylene are formed. Obtained.

According to another embodiment of the invention, the method for producing the aromatic product may be carried out in a batch reactor, a continuous fixed bed reactor or a continuous fluidized bed reactor.

Another aspect of the present invention can provide an aromatic product prepared according to the method for producing an aromatic product.

1 is a process diagram schematically showing a specific example of producing an aromatic product from coal tar according to an embodiment of the present invention.

Referring to Figure 1, coal tar oil (S1) produced in the manufacturing process of metallurgical coke during steelmaking process is a sulfur compound, nitrogen compound, aromatic compound having one benzene ring, aromatic compound having two benzene rings, and benzene ring Containing three or more aromatic compounds as a component component, the coal tar fraction (S1) is introduced into the distillation separation process (U1) to include a sulfur compound, a nitrogen compound, and an aromatic compound having one or two benzene rings. The oil is separated into effluent oil (S2), and is separated into residual oil (S3) which is an oil containing an aromatic compound having three or more benzene rings.

The effluent oil (S2) is reacted in the presence of a catalyst with hydrogen (S4) in the hydrogenation desulfurization / denitrification reaction step (U2) to remove the sulfur compound and nitrogen compounds as catalyst poisoning components, the treated oil (S5) After being fed to the catalytic cracking reaction step (U3), it is reacted with hydrogen (S4) in the presence of a catalyst to be converted and separated into an aromatic product (S7) and unconverted fraction (S8) containing benzene, toluene, xylene. The unconverted fraction (S8) is mainly an fraction containing naphthalene.

Hereinafter, the configuration of the present invention will be described in more detail with reference to the following examples, but is not limited thereto.

[Example]

Manufacturing example  One. Ni ₂ P Of Al ₂ O ₃ (γ- phase ) Synthesis (Low Temperature Reduction Method)

1.82 g (1.5 g of Nickel chloride hexahydrate)

mmol Ni loading) and 1.64 g (3 mmol P loading) of sodium hypophosphite were dissolved in 40 ml of distilled water. The alumina carrier (5 g) was added dropwise to the aqueous solution while stirring. Then, the solution containing the alumina carrier was slowly evaporated and stirred at 80 ° C., and then dried at 80 ° C. for 8 hours to remove moisture. Nitrogen was flowed into the dried solid at 100 sccm, and then heated to 5 ° C./min from room temperature to 300 ° C. and maintained for 30 minutes. Thereafter, hydrogen was flowed at 1,000 sccm, the temperature was increased to 2 ° C./min per minute to 500 ° C., and maintained at 500 ° C. for 30 minutes to prepare a catalyst Ni ₂ P / Al ₂ O ₃ .

Manufacturing example  2. Ni ₂ P Of Al ₂ O ₃ - TOP Synthesis of Ligand  Stabilization method)

0.38 g (1.5 mmol Ni loading) of nickel acetylacetate, 7 mL of trioctylphosphine (TOP) used as a surfactant and a phosphorus reducing agent, was mixed at 70 ° C. for 10 minutes, and then trioctylphosphine oxide was stirred at 300 ° C. ( Rapid injection into 5 g solution of trioctylphosphine oxide (TOPO) and maintained at 300 ° C for 2 hours. After the reaction, 50 mL of methanol was added to the solution to form a precipitate, which was separated by centrifugation. The precipitate is washed three times with acetone and centrifuged to remove residual TOP and TOPO. The final precipitate was dispersed in acetone and the dispersed solution was impregnated in 1 g of an alumina support, and then dried at room temperature to prepare a catalyst Ni ₂ P / Al ₂ O ₃ .

Example  One

According to the method of the present invention, as shown in Table 1, coal tar was used as a raw material, and this was subjected to monodistillation under atmospheric pressure to separate an oil belonging to a boiling point up to 250 ° C. to obtain a bicyclic aromatic, which was then applied to the reaction.

Item Raw material (wt%) Spilled Oil (wt%) Monocyclic aromatic 5.0 15.0 Bicyclic aromatic 31.0 <80.0 Tricyclic or more aromatic > 55.0 <5.0 Sulfur compounds 1.0 0.1 Nitrogen compounds 5.0 1.2 Oxygen compound 1.0 0.05

Example  2

The hydrodesulfurization / denitrification reaction was carried out while adding hydrogen in a fixed bed high pressure reactor in the presence of the catalyst of Preparation Example 1 for the effluent oil shown in Table 1 of Example 1, and the experimental conditions and the results are shown in Table 2 below. .

Catalyst Type and Filling Amount Catalyst of Preparation Example 1 / 1.0 g Driving conditions Hydrogen partial pressure (kg / cm ² ) 50 Hydrogen flow rate (cm ³ / min) 500 LHSV (hr ^-1 ) 1.0 Reaction temperature (℃) 370 Result of Analysis Sulfur content (wtppm) 250 Nitrogen content (wtppm) 850 Aromatic content (wt%) 45

Example  3

The hydrodesulfurization / denitrification reaction was carried out while adding hydrogen in a fixed bed high pressure reactor in the presence of the catalyst of Preparation Example 2 for the effluent oil shown in Table 1 of Example 1, and the experimental conditions and the results are shown in Table 3 below. .

Catalyst Type and Filling Amount Catalyst of Preparation Example 2 / 1.0 g Driving conditions Hydrogen partial pressure (kg / cm ² ) 50 Hydrogen flow rate (cm ³ / min) 500 LHSV (hr ^-1 ) 1.0 Reaction temperature (℃) 370 Result of Analysis Sulfur content (wtppm) <50 Nitrogen content (wtppm) <50 Aromatic content (wtppm) 52.0

The foregoing description of the present invention is intended for illustration, and it will be understood by those skilled in the art that the present invention may be easily modified in other specific forms without changing the technical spirit or essential features of the present invention. will be. It is therefore to be understood that the above-described embodiments are illustrative in all aspects and not restrictive. For example, each component described as a single entity may be distributed and implemented, and components described as being distributed may also be implemented in a combined form.

The scope of the present invention is shown by the following claims rather than the above description, and all changes or modifications derived from the meaning and scope of the claims and their equivalents should be construed as being included in the scope of the present invention. do.

U1: Distillation Separation Process
U2: Hydrodesulfurization / Denitrification Reaction Process
U3: catalytic cracking reaction process

Claims (11)

Distilling coal tar to separate the remaining oil and the effluent oil (a);
(B) removing sulfur, nitrogen, sulfur compounds or nitrogen compounds contained in the effluent oil by hydrodesulfurization / denitrification reaction of the effluent oil in the presence of a transition metal phosphide catalyst; And
(C) converting the effluent oil having undergone the hydrodesulfurization / denitrification reaction into an aromatic product including at least one selected from benzene, toluene and xylene through catalytic cracking reaction;
Method for producing an aromatic product comprising. The method of claim 1, wherein the transition metal phosphide catalyst of step (b) comprises at least one metal selected from Group 6, Group 8 and Group 10 metals of the periodic table. The method of claim 2, wherein the transition metal phosphide catalyst of step (b) comprises at least one selected from Ni ₂ P, Co ₂ P, Fe ₂ P, MoP, and WP. The method of claim 3, wherein the transition metal phosphide catalyst of step (b) is at least one selected from Ni ₂ P, Co ₂ P, Fe ₂ P, MoP and WP silica alumina (SiO ₂ -Al ₂ O ₃ ), Alumina (Al ₂ O ₃ ), Zinc Oxide (ZnO), Zirconia (ZrO ₂ ), Ceria (CeO ₂ ), Silica (SiO ₂ ), Zeolite, Mesoporous silica, Clay, USY zeolite (zeolite), saponite (saponite) and titania (TiO ₂₎ method of the aromatic products, characterized in that a bearing on at least one selected from. The method of claim 1, wherein the transition metal phosphide catalyst
Adding an alumina carrier to an aqueous solution of a transition metal precursor and a phosphorus precursor having an oxidation number of phosphorus of +1 (1);
Drying the mixture obtained in step (1) (2);
Firing the dried product obtained in the step (2) under an inert atmosphere (3); And
Characterized in that it was prepared by the method for producing a transition metal phosphide catalyst comprising the step (4) of reducing the calcined material obtained in the step (3) in a hydrogen atmosphere at 200 ℃ to 500 ℃ to form a transition metal phosphide catalyst Method for producing aromatic products. The method of claim 1, wherein the transition metal phosphide catalyst
Preparing a metal precursor and a compound represented by Chemical Formula 1ⓐ;
Reacting the metal precursor of step ⓐ with the compound represented by Formula 1 with the compound represented by Formula 2; And
A method for producing an aromatic product, characterized in that it was prepared by a process for preparing a transition metal phosphide catalyst comprising step © impregnating the product of step ⓑ into a carrier.
[Formula 1]

R ¹ to R ³ in Formula 1 are each independently hydrogen or an alkyl group having 1 to 12 carbon atoms.
(2)

R ⁴ to R ⁶ in Formula 2 are each independently hydrogen or an alkyl group having 1 to 12 carbon atoms. The method of claim 1, wherein step (b) is performed at a temperature of 200 to 1000 ° C. and a pressure of 10 to 200 atm. The method of claim 1, wherein step (b) is a step of using a coke oven gas (coke oven gas) as a hydrogen source of the hydrodesulfurization / denitrification reaction. The method of claim 1, wherein the catalytic cracking reaction is carried out at least one reaction selected from pyrolysis reaction, dealkylation reaction, isomerization reaction, transalkylation reaction and alkylation reaction. The method of claim 1 wherein the aromatic product is produced in a batch reactor, continuous fixed bed reactor or continuous fluidized bed reactor. An aromatic product prepared according to the method of any one of claims 1 to 10.

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