CN117654598A - Aromatization catalyst for catalyzing gasoline to reduce olefin, and preparation method and application thereof - Google Patents

Abstract

The invention relates to the technical field of olefin aromatization catalysts, in particular to a catalytic gasoline olefin aromatization catalyst and a preparation method and application thereof. The invention has simple synthesis process, low cost and environmental protection, has the double functions of sulfur resistance and aromatization when being used for catalyzing the aromatization reaction of gasoline, has high aromatization degree of olefin reduction, and can be used as a heavy raw material to realize the purpose of increasing aromatic hydrocarbon of chemical products.

Description

Aromatization catalyst for catalyzing gasoline to reduce olefin, and preparation method and application thereof

Technical Field

The invention relates to the technical field of olefin aromatization catalysts, in particular to a catalyst for catalyzing gasoline to reduce olefin aromatization, a preparation method and application thereof.

Background

With the increasing importance of people on environmental protection, china quickens the upgrading step of the quality of vehicle fuels, and the national standard GB17930-2016 requires that the sulfur content in the national VIb gasoline is not more than 10 mu g/g and the olefin volume content is not more than 15% [ M1 ].

The catalytic cracking gasoline is a main component of automotive gasoline in China, and accounts for about 75% in a gasoline pool, and is characterized by higher olefin and sulfur content, and a method for desulfurizing and reducing olefin is generally adopted, wherein the catalytic gasoline is firstly subjected to fractional distillation and cutting into light and heavy gasoline, the light gasoline is etherified to obtain etherified gasoline, the heavy gasoline is subjected to selective hydrodesulfurization or adsorption desulfurization, then the recovery of olefin and octane number is realized through modification processes such as aromatization, isomerization and the like, the aromatization of the gasoline can convert a large amount of olefin in FCC gasoline into aromatic hydrocarbon, and an aromatization product can be used as a high-octane gasoline blending component and also can be used as a reforming raw material. In the present stage, the desulfurization and aromatization modification of the catalytic gasoline are usually carried out separately, so that the damage of sulfur to the aromatization catalyst can be reduced, but the process is prolonged, more olefin is saturated, and the development of a catalyst with sulfur resistance and olefin aromatization becomes the direction of research at present.

In olefin aromatization catalysts, ZSM-5 molecular sieves are more applied, ZSM-5 molecular sieves are solid acid catalysts with excellent performances, and unique pore channel structures provide excellent shape selection functions for desulfurization and olefin aromatization reactions, but because the ten-membered ring pore size of the ZSM-5 molecular sieves is smaller, the diffusion mass transfer of reaction intermediates and products in pore channels is limited, and the carbon deposition is particularly obvious when the carbon deposition is high, so that the olefin conversion rate is low, and the sulfur tolerance and the stability are poor. In addition, in the synthesis process of the ZSM-5 molecular sieve, an organic template agent is usually required to be introduced for guided synthesis, the organic template agent has high price and large dosage, the cost of the catalyst is greatly increased, and amine recovery and waste liquid treatment are required, the process is complicated and the environment is polluted, so that the addition of the organic template agent is avoided in the synthesis process, the organic template agent can be replaced by the guided synthesis of a seed crystal, the cost and the environmental pollution of the molecular sieve are reduced, the pore channel structure and the acidity of the molecular sieve are improved by combining crystallization, post-treatment modification and the like, the molecular sieve with a step pore structure is obtained, and the desulfurization and aromatization performances of gasoline are improved.

The Chinese patent publication No. CN104030314A discloses a preparation method of ZSM-5 molecular sieve with a hierarchical pore structure, which is prepared by taking tetrapropylammonium bromide as a template agent and adopting cheap raw materials in one step. The method has low cost and simple operation, and the obtained hierarchical porous material has good physicochemical properties and catalytic properties.

The Chinese patent publication No. CN104649295A discloses a preparation and application of a hierarchical ZSM-5 molecular sieve aggregate, which is characterized in that a hierarchical ZSM-5 molecular sieve with open pore channels is synthesized by a one-step method by adopting a seed crystal prepared by adding tetrapropylammonium into silica-alumina sol gel obtained by synthesizing an inorganic aluminum source and an inorganic silicon source as a guiding agent.

The research on the hydrodesulfurization and olefin aromatization reactions of ZSM-5 catalyst, such as Kong Feifei of the university of Liaoning petrochemical industry, adopts Na2CO3 solution andthe mixed alkali solution of Na2CO3 and TPAOH is used for treating ZSM-5 molecular sieves with different silicon-aluminum ratios, and the specific surface area and the mesoporous volume of the molecular sieves are increased after the mixed alkali treatment. FCC gasoline is used as a raw material, and Co-Mo/ZSM-5 catalyst after alkali treatment is subjected to hydrodesulfurization and olefin aromatization performance evaluation. The results show that the volume ratio of hydrogen to oil is 300:1 and the reaction space velocity is 1.5h at 400 ℃ and 2.5MPa ^-1 Under the conditions of (2) the desulfurization rate was 94.2% and the aromatic hydrocarbon yield was 30.82%.

The aromatization of catalytic cracking light gasoline on a nano HZSM-5 zeolite catalyst such as Wang Jincheng is researched, an organic template agent is adopted to synthesize a nano HZSM-5 zeolite molecular sieve, and FCC light gasoline is aromatized. At a reaction temperature of 360 ℃ to 400 ℃ and a reaction pressure of 1.0MPa to 3.0MPa, WHSV for 1.0h ^-1 To 4.0h ^-1 Under the condition of C5 ⁺ The conversion rate of olefin is 39.11% to 97.92%, the net increment of arene in the product is 2.59% to 19.05%, and the low gasoline yield and the quick deactivation of the catalyst are the main problems of aromatization reaction of FCC light gasoline on a nano HZSM-5 zeolite catalyst.

The Chinese patent with the publication number of CN104399518B provides a preparation method of a catalytic cracking light gasoline aromatization catalyst, which mainly comprises modification of a nano ZSM-5 molecular sieve, preparation of a carrier, preparation of the catalyst and the like. The nano ZSM-5 molecular sieve has shorter pore canal and high mass transfer efficiency, and can furthest reduce the low-carbon olefin in the catalytic cracking light gasoline and keep the octane number not to be reduced or even improved after being subjected to surface modification by one or two metals of rare earth or cobalt molybdenum nickel gallium zinc.

The Chinese patent with the publication number of CN1235682C provides a catalyst for catalyzing the aromatization of gasoline and an application process thereof, and the catalyst comprises the following components in percentage by weight: the noble metal content is 0.1 to 1.0m%; the K-type zeolite content is 50.0-90.0 m%; wherein the K2O content is 1.0m% to 5.0m%; the balance being binder. The catalyst can be used for aromatizing the hydrogenated and desulfurized catalytic gasoline, so that the purposes of reducing the olefin content and octane number loss can be achieved, but noble metals such as platinum, palladium and the like are contained, so that the cost of the catalyst is increased, and sulfur poisoning is easy to occur.

The Chinese patent with the publication number of CN108659883BX discloses a method and a system for desulfurizing and aromatizing gasoline, wherein the method comprises (1) cutting a gasoline raw material to obtain a first light gasoline fraction and a first heavy gasoline fraction; (2) Feeding the first heavy gasoline fraction into a first fluidized reactor to contact with a mixed catalyst to carry out desulfurization and aromatization reactions in a hydrogen-contacting state; feeding the first light gasoline fraction into a second fluidized reactor to contact with an adsorption desulfurization catalyst for desulfurization reaction; (3) Cutting the desulfurization and aromatization products of the first heavy gasoline fraction to obtain a second light gasoline fraction and a second heavy gasoline fraction; (4) The light gasoline obtained by twice cutting desulfurization is etherified to obtain etherified oil, and the etherified oil and the second heavy gasoline fraction are sent into a gasoline pool to be blended, so that the sulfur and olefin in the gasoline are reduced, the octane number is kept, and the high gasoline yield is realized. Wherein the mixed catalyst of step (2) is the core of the reaction system, which is a mixture of an adsorption desulfurization catalyst and an olefin aromatization catalyst, the adsorption desulfurization catalyst comprising 5% to 85% silica, 5% to 30% alumina, 10% to 90% zinc oxide, and 5% to 30% desulfurization active metal; the olefin aromatization catalyst is a catalyst comprising 10% to 30% molecular sieve, 0.1% to 20% aromatization active metal oxide, and 50% to 89% support.

The method can reduce the sulfur and olefin content in the gasoline, but needs to pass through two fluidized reactors and two cutting processes, and has long reaction flow; the catalyst is two different types of catalysts, the desulfurization performance and the olefin aromatization performance are difficult to match, the active component molecular sieve of the aromatization catalyst is a microporous molecular sieve, the process is complex through a plurality of acid and alkali treatment procedures in the molecular sieve synthesis process, the cost is high, the catalyst is not environment-friendly, the olefin aromatization degree of the catalyst is low, the olefin content in the product is 17-19%, and the aromatic hydrocarbon content is only 18-20%, and the catalyst can only be used as a gasoline blending component.

Disclosure of Invention

The invention provides a catalyst for catalyzing gasoline to reduce olefin aromatization, a preparation method and application thereof, overcomes the defects of the prior art, and can effectively solve the problems of complex process, high cost, environmental protection and low catalyst olefin aromatization degree existing in the preparation of the catalyst for reducing olefin aromatization.

One of the technical schemes of the invention is realized by the following measures: the catalyst for catalyzing the olefin reduction aromatization of the gasoline comprises 30 to 85 percent of carrier, 10 to 50 percent of ZSM-5 molecular sieve and 0.1 to 20 percent of active metal oxide according to weight percentage, wherein the carrier is alumina, the ZSM-5 molecular sieve is an industrial modified ZSM-5 molecular sieve or a self-made molecular sieve, and the active metal oxide is more than one of nickel oxide, molybdenum oxide, cobalt oxide, zinc oxide, lanthanum oxide and gallium oxide.

The following are further optimizations and/or improvements to one of the above-described inventive solutions:

the industrial modified ZSM-5 molecular sieve is prepared by the following method: firstly, industrial ZSM-5 seed crystal and modified solution are mixed according to a solid-to-liquid ratio of 1: mixing uniformly in a proportion of 10 to 40, and stirring for 2 to 50 hours at a temperature of 20 to 100 ℃; and then washing with deionized water, drying at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain the industrial modified ZSM-5 molecular sieve, wherein the modified solution is alkaline solution or acidic solution with the concentration of 0.10-5.0 mol/L.

The alkaline solution is one or more of sodium hydroxide solution, sodium carbonate solution and sodium acetate solution, and the acidic solution is one or more of hydrochloric acid solution, nitric acid solution and sulfuric acid solution.

The preparation method comprises the following steps: firstly, an aluminum source, a silicon source and an alkali source are mixed according to a mole ratio of 1 to 10:100 to 1000: uniformly mixing 10 to 50, adding a ZSM-5 molecular sieve, and stirring for 2 to 40 hours at the temperature of 10 to 40 ℃ to obtain a first gel mixture, wherein the weight of the ZSM-5 molecular sieve accounts for 2 to 15 percent of the weight of silicon dioxide in the added silicon source; secondly, after the first gel mixture is filled into a closed container, carrying out a first-stage hydrothermal crystallization reaction for 6 to 72 hours at the temperature of 100 to 150 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out a second-stage hydrothermal crystallization reaction on the first-stage hydrothermal crystallization product at 130-200 ℃ for 12-72 h to obtain a second-stage hydrothermal crystallization product; fourthly, cooling the product of the second stage of hydrothermal crystallization, washing with deionized water, drying for 2 to 20 hours at the temperature of 80 to 150 ℃, and roasting for 2 to 10 hours at the temperature of 400 to 700 ℃ to obtain the sodium ZSM-5 molecular sieve with the step pore structure; fifthly, a sodium ZSM-5 molecular sieve with a step hole structure is prepared according to the solid-to-liquid ratio of 1:5 to 20, adding the mixture into an ammonium solution, exchanging for 2 to 6 hours at the temperature of 40 to 90 ℃, and carrying out suction filtration, washing, drying and roasting after the exchange is finished to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing the hydrogen ZSM-5 molecular sieve with a step hole structure with the required amount of alumina, adding dilute acid, kneading to bond the mixture, extruding and molding, drying the molded product at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain a roasted product; seventh, crushing and screening the roasted product, preparing an active component impregnating solution according to the weight percentage of the active metal oxide of 0.1-20%, slowly dripping the active component impregnating solution onto the screened catalyst carrier, impregnating for 2-40 h at the temperature of 0-40 ℃, drying for 2-20 h at the temperature of 80-150 ℃, and roasting for 2-10 h at the temperature of 400-700 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst.

In the first step, the aluminum source is more than one of sodium metaaluminate, gamma aluminum oxide, pseudo-boehmite, aluminum isopropoxide and aluminum hydroxide, the silicon source is more than one of silica sol, silica gel, tetraethoxysilane and white carbon black, and the alkali source is more than one of sodium hydroxide, potassium hydroxide, sodium carbonate and sodium acetate.

In the fifth step, the ammonium solution is one or more of ammonium nitrate solution, ammonium chloride solution and ammonium sulfate solution with concentration of 0.2mol/L to 1 mol/L.

In the sixth step, the alumina is one or more of gamma alumina, pseudo-boehmite and aluminum hydroxide, and the dilute acid is one or more of dilute hydrochloric acid, dilute nitric acid, dilute citric acid and dilute acetic acid with the mass percentage of 0.5-10%.

In the seventh step, the active component in the active component impregnation liquid is at least one of nickel nitrate, nickel sulfate, ammonium molybdate, molybdenum trioxide, cobalt chloride, cobalt sulfate, cobalt nitrate, zinc chloride, zinc nitrate, zinc oxide, zinc sulfate, lanthanum nitrate, gallium sulfate and gallium chloride.

The second technical scheme of the invention is realized by the following measures: the preparation method of the aromatization catalyst for reducing olefin in the catalytic gasoline comprises the following steps: firstly, an aluminum source, a silicon source and an alkali source are mixed according to a mole ratio of 1 to 10:100 to 1000: uniformly mixing 10 to 50, adding a ZSM-5 molecular sieve, and stirring for 2 to 40 hours at the temperature of 10 to 40 ℃ to obtain a first gel mixture, wherein the weight of the ZSM-5 molecular sieve accounts for 2 to 15 percent of the weight of silicon dioxide in the added silicon source; secondly, after the first gel mixture is filled into a closed container, carrying out a first-stage hydrothermal crystallization reaction for 6 to 72 hours at the temperature of 100 to 150 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out a second-stage hydrothermal crystallization reaction on the first-stage hydrothermal crystallization product at 130-200 ℃ for 12-72 h to obtain a second-stage hydrothermal crystallization product; fourthly, cooling the product of the second stage of hydrothermal crystallization, washing with deionized water, drying for 2 to 20 hours at the temperature of 80 to 150 ℃, and roasting for 2 to 10 hours at the temperature of 400 to 700 ℃ to obtain the sodium ZSM-5 molecular sieve with the step pore structure; fifthly, a sodium ZSM-5 molecular sieve with a step hole structure is prepared according to the solid-to-liquid ratio of 1:5 to 20, adding the mixture into an ammonium solution, exchanging for 2 to 6 hours at the temperature of 40 to 90 ℃, and carrying out suction filtration, washing, drying and roasting after the exchange is finished to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing the hydrogen ZSM-5 molecular sieve with a step hole structure with the required amount of alumina, adding dilute acid, kneading to bond the mixture, extruding and molding, drying the molded product at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain a roasted product; seventh, crushing and screening the roasted product, preparing an active component impregnating solution according to the weight percentage of the active metal oxide of 0.1-20%, slowly dripping the active component impregnating solution onto the screened catalyst carrier, impregnating for 2-40 h at the temperature of 0-40 ℃, drying for 2-20 h at the temperature of 80-150 ℃, and roasting for 2-10 h at the temperature of 400-700 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst.

The third technical scheme of the invention is realized by the following measures: the application of the catalyst in catalyzing the aromatization reaction of reducing olefin in gasoline.

The preparation process of the step hole molecular sieve is simple, the production cost is low, and the environmental pollution is small; the prepared catalyst for aromatization of the catalytic gasoline to reduce olefin has the double functions of sulfur resistance and aromatization, can be carried out in one reactor without cutting, shortens the reaction flow, is used for reducing the olefin in the aromatization of the catalytic gasoline, has high aromatization degree, has the olefin content of <16 percent and the aromatic hydrocarbon content of >40 percent, and can be used as reforming raw materials, thereby realizing the purpose of increasing the aromatic hydrocarbon of chemical products.

Detailed Description

The present invention is not limited by the following examples, and specific embodiments can be determined according to the technical scheme and practical situations of the present invention. The various chemical reagents and chemical supplies mentioned in the invention are all commonly known and used in the prior art unless specified otherwise; the percentages in the invention are mass percentages unless specified otherwise; the solutions in the invention are aqueous solutions in which the solvent is water unless otherwise specified, for example, the hydrochloric acid solution is hydrochloric acid aqueous solution; the room temperature and the room temperature in the present invention generally refer to temperatures ranging from 15 ℃ to 25 ℃, and are generally defined as 25 ℃.

The invention is further described below with reference to examples:

example 1: the catalyst for the olefin reduction aromatization of the catalytic gasoline comprises 30 to 85 weight percent of carrier, 10 to 50 weight percent of ZSM-5 molecular sieve and 0.1 to 20 weight percent of active metal oxide, wherein the carrier is alumina, the ZSM-5 molecular sieve is an industrial modified ZSM-5 molecular sieve or a self-made molecular sieve, and the active metal oxide is more than one of nickel oxide, molybdenum oxide, cobalt oxide, zinc oxide, lanthanum oxide and gallium oxide.

In the invention, when the ZSM-5 molecular sieve is a self-made molecular sieve (commercially available), the self-made molecular sieve can be directly added, or can be added after being modified by a modifying solution to obtain the industrial modified ZSM-5 molecular sieve.

Example 2: as an optimization of the above examples, an industrially modified ZSM-5 molecular sieve was prepared as follows: firstly, industrial ZSM-5 seed crystal and modified solution are mixed according to a solid-to-liquid ratio of 1: mixing uniformly in a proportion of 10 to 40, and stirring for 2 to 50 hours at a temperature of 20 to 100 ℃; and then washing with deionized water, drying at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain the industrial modified ZSM-5 molecular sieve, wherein the modified solution is alkaline solution or acidic solution with the concentration of 0.10-5.0 mol/L.

Example 3: as an optimization of the above embodiment, the alkaline solution is one or more of sodium hydroxide solution, sodium carbonate solution and sodium acetate solution, and the acidic solution is one or more of hydrochloric acid solution, nitric acid solution and sulfuric acid solution.

Example 4: as an optimization of the above examples, the following procedure was followed: firstly, an aluminum source, a silicon source and an alkali source are mixed according to a mole ratio of 1 to 10:100 to 1000: uniformly mixing 10 to 50, adding a ZSM-5 molecular sieve, and stirring for 2 to 40 hours at the temperature of 10 to 40 ℃ to obtain a first gel mixture, wherein the weight of the ZSM-5 molecular sieve accounts for 2 to 15 percent of the weight of silicon dioxide in the added silicon source; secondly, after the first gel mixture is filled into a closed container, carrying out a first-stage hydrothermal crystallization reaction for 6 to 72 hours at the temperature of 100 to 150 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out a second-stage hydrothermal crystallization reaction on the first-stage hydrothermal crystallization product at 130-200 ℃ for 12-72 h to obtain a second-stage hydrothermal crystallization product; fourthly, cooling the product of the second stage of hydrothermal crystallization, washing with deionized water, drying for 2 to 20 hours at the temperature of 80 to 150 ℃, and roasting for 2 to 10 hours at the temperature of 400 to 700 ℃ to obtain the sodium ZSM-5 molecular sieve with the step pore structure; fifthly, a sodium ZSM-5 molecular sieve with a step hole structure is prepared according to the solid-to-liquid ratio of 1:5 to 20, adding the mixture into an ammonium solution, exchanging for 2 to 6 hours at the temperature of 40 to 90 ℃, and carrying out suction filtration, washing, drying and roasting after the exchange is finished to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing the hydrogen ZSM-5 molecular sieve with a step hole structure with the required amount of alumina, adding dilute acid, kneading to bond the mixture, extruding and molding, drying the molded product at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain a roasted product; seventh, crushing and screening the roasted product, preparing an active component impregnating solution according to the weight percentage of the active metal oxide of 0.1-20%, slowly dripping the active component impregnating solution onto the screened catalyst carrier, impregnating for 2-40 h at the temperature of 0-40 ℃, drying for 2-20 h at the temperature of 80-150 ℃, and roasting for 2-10 h at the temperature of 400-700 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst.

In the present invention, the closed vessel into which the first gel mixture is charged may be a stainless steel autoclave lined with polytetrafluoroethylene.

Example 5: as the optimization of the above embodiment, in the first step, the aluminum source is one or more of sodium metaaluminate, gamma alumina, pseudo-boehmite, aluminum isopropoxide and aluminum hydroxide, the silicon source is one or more of silica sol, silica gel, tetraethyl orthosilicate and white carbon black, and the alkali source is one or more of sodium hydroxide, potassium hydroxide, sodium carbonate and sodium acetate.

Example 6: as an optimization of the above embodiment, in the fifth step, the ammonium solution is one or more of an ammonium nitrate solution, an ammonium chloride solution and an ammonium sulfate solution having a concentration of 0.2mol/L to 1 mol/L.

Example 7: as an optimization of the above embodiment, in the sixth step, the alumina is one or more of gamma alumina, pseudo-boehmite and aluminum hydroxide, and the dilute acid is one or more of dilute hydrochloric acid, dilute nitric acid, dilute citric acid and dilute acetic acid with a mass percentage of 0.5% to 10%.

Example 8: as an optimization of the above embodiment, in the seventh step, the active component in the active component impregnation liquid is one or more of nickel nitrate, nickel sulfate, ammonium molybdate, molybdenum trioxide, cobalt chloride, cobalt sulfate, cobalt nitrate, zinc chloride, zinc nitrate, zinc oxide, zinc sulfate, lanthanum nitrate, gallium sulfate, and gallium chloride.

Example 9: the preparation method of the catalyst for reducing olefin aromatization of the catalytic gasoline comprises the following steps: firstly, an aluminum source, a silicon source and an alkali source are mixed according to a mole ratio of 1 to 10:100 to 1000: uniformly mixing 10 to 50, adding a ZSM-5 molecular sieve, and stirring for 2 to 40 hours at the temperature of 10 to 40 ℃ to obtain a first gel mixture, wherein the weight of the ZSM-5 molecular sieve accounts for 2 to 15 percent of the weight of silicon dioxide in the added silicon source; secondly, after the first gel mixture is filled into a closed container, carrying out a first-stage hydrothermal crystallization reaction for 6 to 72 hours at the temperature of 100 to 150 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out a second-stage hydrothermal crystallization reaction on the first-stage hydrothermal crystallization product at 130-200 ℃ for 12-72 h to obtain a second-stage hydrothermal crystallization product; fourthly, cooling the product of the second stage of hydrothermal crystallization, washing with deionized water, drying for 2 to 20 hours at the temperature of 80 to 150 ℃, and roasting for 2 to 10 hours at the temperature of 400 to 700 ℃ to obtain the sodium ZSM-5 molecular sieve with the step pore structure; fifthly, a sodium ZSM-5 molecular sieve with a step hole structure is prepared according to the solid-to-liquid ratio of 1:5 to 20, adding the mixture into an ammonium solution, exchanging for 2 to 6 hours at the temperature of 40 to 90 ℃, and carrying out suction filtration, washing, drying and roasting after the exchange is finished to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing the hydrogen ZSM-5 molecular sieve with a step hole structure with the required amount of alumina, adding dilute acid, kneading to bond the mixture, extruding and molding, drying the molded product at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain a roasted product; seventh, crushing and screening the roasted product, preparing an active component impregnating solution according to the weight percentage of the active metal oxide of 0.1-20%, slowly dripping the active component impregnating solution onto the screened catalyst carrier, impregnating for 2-40 h at the temperature of 0-40 ℃, drying for 2-20 h at the temperature of 80-150 ℃, and roasting for 2-10 h at the temperature of 400-700 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst.

Example 10: the application of the catalyst in catalyzing the aromatization reaction of reducing olefin in gasoline.

Example 11: uniformly mixing 10g of industrial ZSM-5 molecular sieve (wherein the mass percent of silicon and aluminum is 120) with 100g of 0.1mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃ and roasting for 2 hours at 500 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium metaaluminate, tetraethoxysilane and sodium acetate are mixed according to the molar ratio of 1:120:10, adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve accounts for 10 percent of the weight of the added silicon dioxide; stirring at 20deg.C for 6 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 12 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 48 hours at 160 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 3 hours at 80 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with pseudo-boehmite according to the mass percentage of 60%: uniformly mixing the materials in a proportion of 40%, dropwise adding 3% dilute nitric acid for kneading, extruding into strips, drying at 120 ℃ for 15 hours, and roasting at 500 ℃ for 6 hours to obtain a roasting product; seventh, crushing and screening the roasting product to 10-20 meshes, preparing zinc nitrate solution according to the proportion of 5% zinc oxide, slowly dripping the zinc nitrate solution onto the roasting product of 10-20 meshes, soaking the roasting product for 24 hours at room temperature, drying the roasting product for 15 hours at 120 ℃ after the soaking is finished, and roasting the roasting product for 6 hours at 500 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst, wherein the product is marked as A-1.

Example 12: uniformly mixing 10g of industrial ZSM-5 molecular sieve (the mass percent of silicon and aluminum is 90) with 120g of 0.15mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃, and roasting for 2 hours at 520 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium metaaluminate, silica sol and sodium hydroxide are mixed according to the mole ratio of 1:90:10, adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve accounts for 10 percent of the weight of the added silicon dioxide; stirring at 20deg.C for 6 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 24 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 60 hours at 160 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 3 hours at 90 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with pseudo-boehmite according to the mass percentage of 50 percent: mixing the materials in a proportion of 50% uniformly, dripping 53% dilute nitric acid into the mixture for kneading, extruding the mixture into strips, drying the strips at 120 ℃ for 15 hours, and roasting the strips at 500 ℃ for 6 hours to obtain a roasted product; seventh, crushing and screening the roasting product to 10-20 meshes, preparing zinc nitrate-nickel nitrate solution according to the proportion of 5% zinc oxide and 8% nickel oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, soaking the solution at room temperature for 24 hours, drying the solution at 120 ℃ for 15 hours after the soaking is finished, and roasting the solution at 500 ℃ for 6 hours to obtain the catalytic gasoline olefin-reducing aromatization catalyst, wherein the product is marked as A-2.

Example 13: uniformly mixing 10g of industrial ZSM-5 molecular sieve (the mass percent of silicon and aluminum is 90) with 120g of 0.15mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃, and roasting for 2 hours at 520 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium metaaluminate, industrial silica gel and sodium hydroxide are mixed according to the mole ratio of 1:90:15, adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve is 5% of the added weight of the silicon dioxide; stirring at 20deg.C for 12 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 36 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 24 hours at 170 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:12, exchanging for 2 hours at 85 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with pseudo-boehmite according to the mass percentage of 50 percent: mixing the materials in a proportion of 50% uniformly, dripping 5% dilute nitric acid into the mixture for kneading, extruding the mixture into strips, drying the strips at 120 ℃ for 15 hours, and roasting the strips at 500 ℃ for 6 hours to obtain a roasted product; seventhly, crushing and screening the roasting product to 10-20 meshes, preparing an ammonium molybdate-zinc nitrate solution according to the proportion of 10% molybdenum oxide and 10% zinc oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, soaking the solution at room temperature for 48 hours, drying the solution at 120 ℃ for 15 hours after the soaking is finished, and roasting the solution at 500 ℃ for 6 hours to obtain the catalytic gasoline olefin-reducing aromatization catalyst, wherein the product is marked as A-3.

Example 14: uniformly mixing 10g of industrial ZSM-5 molecular sieve (wherein the mass percent of silicon aluminum is 120) with 120g of 0.15mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃, and roasting for 2 hours at 520 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, alumina, silica sol and sodium acetate are mixed according to the mole ratio of 1:120:15, and adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve accounts for 4% of the added weight of the silicon dioxide; stirring at 20deg.C for 12 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 24 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 36 hours at 170 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 4 hours at 85 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with pseudo-boehmite according to the mass percentage of 70%: mixing the materials in a proportion of 30% uniformly, dripping 5% dilute nitric acid into the mixture for kneading, extruding the mixture into strips, drying the strips at 120 ℃ for 15 hours, and roasting the strips at 500 ℃ for 6 hours to obtain a roasted product; seventhly, crushing and screening the roasting product to 10-20 meshes, preparing an ammonium molybdate-cobalt nitrate solution according to the proportion of 8% molybdenum oxide and 5% cobalt oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, soaking the solution at room temperature for 48 hours, drying the solution at 120 ℃ for 15 hours after the soaking is finished, and roasting the solution at 500 ℃ for 6 hours to obtain the catalytic gasoline olefin-reducing aromatization catalyst, wherein the product is marked as A-4.

Example 15: uniformly mixing 10g of industrial ZSM-5 molecular sieve (the mass percent of silicon and aluminum is 60) with 100g of 0.10mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃ and roasting for 2 hours at 520 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium aluminate, ethyl silicate and sodium hydroxide are mixed according to the mole ratio of 1:60:10, adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve accounts for 70% of the weight of the added silicon dioxide; stirring at 20deg.C for 12 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 24 hours at 120 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 48 hours at 160 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 4 hours at 80 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with alumina powder according to the mass percentage of 40%: mixing the materials in a proportion of 60% uniformly, dripping 5% dilute nitric acid into the mixture for kneading, extruding the mixture into strips, drying the strips at 120 ℃ for 15 hours, and roasting the strips at 500 ℃ for 6 hours to obtain a roasted product; seventh, crushing and screening the roasting product to 10-20 meshes, preparing zinc nitrate-nickel nitrate-cobalt nitrate solution according to the proportion of impregnating 12% zinc oxide, 5% nickel oxide and 3% cobalt oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, impregnating the solution for 24 hours at room temperature, drying the solution for 15 hours at 120 ℃ after the impregnation is finished, roasting the solution for 6 hours at 500 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst, wherein the product is marked as A-5.

Example 16: uniformly mixing 10g of industrial ZSM-5 molecular sieve (the mass percent of silicon and aluminum is 90) with 120g of 0.15mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃, and roasting for 2 hours at 520 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium metaaluminate, industrial silica gel and sodium hydroxide are mixed according to the mole ratio of 1:90:9, adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve accounts for 6% of the added weight of the silicon dioxide; stirring at 20deg.C for 6 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 30 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 48 hours at 180 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 4 hours at 85 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with alumina powder and silicon dioxide powder according to the mass percentage of 40 percent: 40%: uniformly mixing 20% of the components, dropwise adding 5% of dilute nitric acid for kneading, extruding into strips, drying at 120 ℃ for 15 hours, and roasting at 500 ℃ for 6 hours to obtain a roasting product; seventh, crushing and screening the roasting product to 10-20 meshes, preparing zinc nitrate-ammonium molybdate-lanthanum nitrate solution according to the proportion of 8% zinc oxide, 5% molybdenum oxide and 1% lanthanum oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, soaking the solution for 24 hours at room temperature, drying the solution for 15 hours at 120 ℃ after the soaking is finished, roasting the solution for 6 hours at 500 ℃ to obtain the catalytic gasoline olefin reduction aromatization catalyst, wherein the product is marked as A-6.

Example 17: uniformly mixing 10g of industrial ZSM-5 molecular sieve (the mass percent of silicon and aluminum is 60) with 120g of 0.15mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃, and roasting for 2 hours at 520 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium metaaluminate, industrial silica gel and sodium hydroxide are mixed according to the mole ratio of 1:60:8, uniformly mixing the materials in proportion, and adding an industrial modified ZSM-5 molecular sieve, wherein the adding weight of the industrial modified ZSM-5 molecular sieve accounts for 5% of the weight of the added silicon dioxide; stirring at 20deg.C for 12 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 36 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 36 hours at 160 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 4 hours at 85 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with pseudo-boehmite according to the mass percentage of 40%: mixing the materials in a proportion of 60% uniformly, dripping 5% dilute nitric acid into the mixture for kneading, extruding the mixture into strips, drying the strips at 120 ℃ for 15 hours, and roasting the strips at 500 ℃ for 6 hours to obtain a roasted product; seventh, crushing and screening the roasting product to 10-20 meshes, preparing zinc nitrate-nickel nitrate-ammonium molybdate solution according to the proportion of 8% zinc oxide, 5% nickel oxide and 3% molybdenum oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, soaking the solution for 24 hours at room temperature, drying the solution for 15 hours at 120 ℃ after the soaking is finished, roasting the solution for 6 hours at 500 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst, wherein the product is marked as A-7.

Example 18: uniformly mixing 10g of industrial ZSM-5 molecular sieve (wherein the mass percent of silicon and aluminum is 90) with 100g of 0.1mol/L NaOH solution, stirring for 4 hours at 60 ℃, washing with deionized water, drying for 10 hours at 80 ℃ and roasting for 2 hours at 500 ℃ to obtain the industrial modified ZSM-5 molecular sieve;

the catalyst for catalyzing the olefin reduction aromatization of the gasoline is prepared by the following steps: firstly, sodium metaaluminate, silica sol and sodium hydroxide are mixed according to a mole ratio of 1:100:10, adding an industrial modified ZSM-5 molecular sieve, wherein the added weight of the industrial modified ZSM-5 molecular sieve accounts for 10 percent of the weight of the added silicon dioxide; stirring at 20deg.C for 6 hr to obtain a first gel mixture; secondly, filling the first gel mixture into a reaction kettle with a lining of polytetrafluoroethylene, and placing the reaction kettle in an oven to perform hydrothermal crystallization for 24 hours at 100 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out hydrothermal crystallization for 36 hours at 180 ℃ to obtain a second-stage hydrothermal crystallization product; fourth, cooling and washing after crystallization, drying for 12 hours at 120 ℃, and roasting for 4 hours at 520 ℃ to obtain the sodium ZSM-5 molecular sieve with a step hole structure; fifthly, placing the sodium ZSM-5 molecular sieve with the step hole structure into an ammonium chloride solution with the weight ratio of 1:10, exchanging for 4 hours at 85 ℃, and then washing, drying and roasting to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing hydrogen type ZSM-5 molecular sieve dry powder with a step hole structure with alumina powder and silicon dioxide powder according to the mass percentage of 50 percent: 20%: mixing the materials in a proportion of 30% uniformly, dripping 5% dilute nitric acid into the mixture for kneading, extruding the mixture into strips, drying the strips at 120 ℃ for 15 hours, and roasting the strips at 500 ℃ for 6 hours to obtain a roasted product; seventhly, crushing and screening the roasting product to 10-20 meshes, preparing an ammonium molybdate-cobalt nitrate-gallium nitrate solution according to the proportion of 8% molybdenum oxide, 3% cobalt oxide and 1% gallium oxide, slowly dripping the solution onto the roasting product of 10-20 meshes, soaking the solution for 24 hours at room temperature, drying the solution for 15 hours at 120 ℃ after the soaking is finished, roasting the solution for 6 hours at 500 ℃ to obtain the catalytic gasoline olefin reduction aromatization catalyst, wherein the product is marked as A-8.

The catalytic gasoline olefin-reducing aromatization catalyst prepared in examples 11 to 18 of the present invention was used in catalytic gasoline desulfurization aromatization reaction, 100g of catalyst was loaded in a fixed bed mode evaluation device, the raw material was catalytic gasoline, and the raw material properties of the catalytic gasoline are shown in table 1. The catalyst and the catalytic gasoline raw materials are adopted to carry out catalytic gasoline desulfurization and aromatization reaction evaluation in a fixed bed mode evaluation device, the catalyst loading is 100g, the reaction temperature is 300 ℃ to 360 ℃, the reaction pressure is 0MPa to 2MPa, and the airspeed WHSV is 0.5 h ^-1 To 2 h ^-1 The reaction results are shown in Table 2. As can be seen from Table 2, the catalyst for aromatization of the catalytic gasoline to reduce olefin prepared by the inventionSamples A-1 to A-8 have the double functions of sulfur resistance and aromatization, and have good sulfur resistance and aromatization performance in catalyzing the aromatization reaction of reducing olefin in gasoline, and the olefin content<16%, the aromatic hydrocarbon content of the product is more than 40%, and the aromatized product can be used as reforming raw material.

In conclusion, the method has the advantages of simple synthesis process, low cost and environmental protection, has the double functions of sulfur resistance and aromatization when being used for catalyzing the aromatization reaction of gasoline, has high aromatization degree of olefin reduction, and can be used as a reforming raw material to realize the purpose of increasing aromatic hydrocarbon of chemical products.

The technical characteristics form the embodiment of the invention, have stronger adaptability and implementation effect, and can increase or decrease unnecessary technical characteristics according to actual needs so as to meet the requirements of different situations.

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Claims (10)

1. The catalyst for catalyzing the olefin reduction aromatization of the gasoline is characterized by comprising 30 to 85 weight percent of carrier, 10 to 50 weight percent of ZSM-5 molecular sieve and 0.1 to 20 weight percent of active metal oxide, wherein the carrier is alumina, the ZSM-5 molecular sieve is an industrial modified ZSM-5 molecular sieve or a self-made molecular sieve, and the active metal oxide is more than one of nickel oxide, molybdenum oxide, cobalt oxide, zinc oxide, lanthanum oxide and gallium oxide.

2. The catalytic gasoline olefin reduction aromatization catalyst of claim 1, wherein the industrially modified ZSM-5 molecular sieve is prepared according to the following method: firstly, industrial ZSM-5 seed crystal and modified solution are mixed according to a solid-to-liquid ratio of 1: mixing uniformly in a proportion of 10 to 40, and stirring for 2 to 50 hours at a temperature of 20 to 100 ℃; and then washing with deionized water, drying at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain the industrial modified ZSM-5 molecular sieve, wherein the modified solution is alkaline solution or acidic solution with the concentration of 0.10-5.0 mol/L.

3. The catalyst for aromatization of olefin in catalytic gasoline according to claim 2, wherein the alkaline solution is one or more of sodium hydroxide solution, sodium carbonate solution and sodium acetate solution, and the acidic solution is one or more of hydrochloric acid solution, nitric acid solution and sulfuric acid solution.

4. A catalytic gasoline olefin aromatization catalyst according to claim 1 or 2 or 3, characterized by being prepared according to the following method: firstly, an aluminum source, a silicon source and an alkali source are mixed according to a mole ratio of 1 to 10:100 to 1000: uniformly mixing 10 to 50, adding a ZSM-5 molecular sieve, and stirring for 2 to 40 hours at the temperature of 10 to 40 ℃ to obtain a first gel mixture, wherein the weight of the ZSM-5 molecular sieve accounts for 2 to 15 percent of the weight of silicon dioxide in the added silicon source; secondly, after the first gel mixture is filled into a closed container, carrying out a first-stage hydrothermal crystallization reaction for 6 to 72 hours at the temperature of 100 to 150 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out a second-stage hydrothermal crystallization reaction on the first-stage hydrothermal crystallization product at 130-200 ℃ for 12-72 h to obtain a second-stage hydrothermal crystallization product; fourthly, cooling the product of the second stage of hydrothermal crystallization, washing with deionized water, drying for 2 to 20 hours at the temperature of 80 to 150 ℃, and roasting for 2 to 10 hours at the temperature of 400 to 700 ℃ to obtain the sodium ZSM-5 molecular sieve with the step pore structure; fifthly, a sodium ZSM-5 molecular sieve with a step hole structure is prepared according to the solid-to-liquid ratio of 1:5 to 20, adding the mixture into an ammonium solution, exchanging for 2 to 6 hours at the temperature of 40 to 90 ℃, and carrying out suction filtration, washing, drying and roasting after the exchange is finished to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing the hydrogen ZSM-5 molecular sieve with a step hole structure with the required amount of alumina, adding dilute acid, kneading to bond the mixture, extruding and molding, drying the molded product at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain a roasted product; seventh, crushing and screening the roasted product, preparing an active component impregnating solution according to the weight percentage of the active metal oxide being 0.1-20%, slowly dripping the active component impregnating solution onto the screened roasted product, impregnating for 2-40 h at the temperature of 0-40 ℃, drying for 2-20 h at the temperature of 80-150 ℃, and roasting for 2-10 h at the temperature of 400-700 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst.

5. The catalyst for aromatization of olefin in catalytic gasoline as set forth in claim 4, wherein in the first step, the aluminum source is one or more of sodium metaaluminate, gamma alumina, pseudo-boehmite, aluminum isopropoxide and aluminum hydroxide, the silicon source is one or more of silica sol, silica gel, ethyl orthosilicate and white carbon black, and the alkali source is one or more of sodium hydroxide, potassium hydroxide, sodium carbonate and sodium acetate.

6. The catalyst for aromatization of olefin in catalytic gasoline according to claim 4 or 5, wherein in the fifth step, the ammonium solution is one or more of ammonium nitrate solution, ammonium chloride solution and ammonium sulfate solution having a concentration of 0.2mol/L to 1 mol/L.

7. The catalyst for aromatization of olefin in catalytic gasoline as set forth in claim 4, 5 or 6, wherein in the sixth step, the alumina is one or more of gamma alumina, pseudo-boehmite and aluminum hydroxide, and the dilute acid is one or more of dilute hydrochloric acid, dilute nitric acid, dilute citric acid and dilute acetic acid with a mass percentage of 0.5% to 10%.

8. The catalyst for aromatization of olefin reduction in catalytic gasoline according to claim 4, 5, 6 or 7, wherein in the seventh step, the active component in the active component impregnation liquid is one or more of nickel nitrate, nickel sulfate, ammonium molybdate, molybdenum trioxide, cobalt chloride, cobalt sulfate, cobalt nitrate, zinc chloride, zinc nitrate, zinc oxide, zinc sulfate, lanthanum nitrate, gallium sulfate and gallium chloride.

9. A process for the preparation of a catalytic gasoline olefin reduction aromatization catalyst according to claim 1 or 2 or 3 or 5 or 6 or 7 or 8, characterized by the steps of: firstly, an aluminum source, a silicon source and an alkali source are mixed according to a mole ratio of 1 to 10:100 to 1000: uniformly mixing 10 to 50, adding a ZSM-5 molecular sieve, and stirring for 2 to 40 hours at the temperature of 10 to 40 ℃ to obtain a first gel mixture, wherein the weight of the ZSM-5 molecular sieve accounts for 2 to 15 percent of the weight of silicon dioxide in the added silicon source; secondly, after the first gel mixture is filled into a closed container, carrying out a first-stage hydrothermal crystallization reaction for 6 to 72 hours at the temperature of 100 to 150 ℃ to obtain a first-stage hydrothermal crystallization product; thirdly, carrying out a second-stage hydrothermal crystallization reaction on the first-stage hydrothermal crystallization product at 130-200 ℃ for 12-72 h to obtain a second-stage hydrothermal crystallization product; fourthly, cooling the product of the second stage of hydrothermal crystallization, washing with deionized water, drying for 2 to 20 hours at the temperature of 80 to 150 ℃, and roasting for 2 to 10 hours at the temperature of 400 to 700 ℃ to obtain the sodium ZSM-5 molecular sieve with the step pore structure; fifthly, a sodium ZSM-5 molecular sieve with a step hole structure is prepared according to the solid-to-liquid ratio of 1:5 to 20, adding the mixture into an ammonium solution, exchanging for 2 to 6 hours at the temperature of 40 to 90 ℃, and carrying out suction filtration, washing, drying and roasting after the exchange is finished to obtain the hydrogen ZSM-5 molecular sieve with a step pore structure; sixthly, mixing the hydrogen ZSM-5 molecular sieve with a step hole structure with the required amount of alumina, adding dilute acid, kneading to bond the mixture, extruding and molding, drying the molded product at 80-150 ℃ for 2-20 h, and roasting at 400-700 ℃ for 2-10 h to obtain a roasted product; seventh, crushing and screening the roasted product, preparing an active component impregnating solution according to the weight percentage of the active metal oxide being 0.1-20%, slowly dripping the active component impregnating solution onto the screened roasted product, impregnating for 2-40 h at the temperature of 0-40 ℃, drying for 2-20 h at the temperature of 80-150 ℃, and roasting for 2-10 h at the temperature of 400-700 ℃ to obtain the catalytic gasoline olefin-reducing aromatization catalyst.

10. Use of a catalytic gasoline-to-olefin aromatization catalyst according to any one of claims 1 to 8 for catalyzing a gasoline-to-olefin aromatization reaction.