CN114181737B

CN114181737B - Method for producing light aromatic hydrocarbon and clean gasoline component from inferior gasoline

Info

Publication number: CN114181737B
Application number: CN202010964363.2A
Authority: CN
Inventors: 尹晓莹; 尤百玲; 郭振东; 赵乐平; 房莹
Original assignee: China Petroleum and Chemical Corp; Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Current assignee: Sinopec Dalian Petrochemical Research Institute Co ltd; China Petroleum and Chemical Corp
Priority date: 2020-09-15
Filing date: 2020-09-15
Publication date: 2023-07-28
Anticipated expiration: 2040-09-15
Also published as: CN114181737A

Abstract

The invention discloses a method for producing light aromatic hydrocarbon and clean gasoline components from poor gasoline. The method comprises the following steps: (1) The inferior gasoline raw material is subjected to hydrodesulfurization and deep light aromatization reactions through a fluidization reactor to obtain hydrogenation products; (2) Fractionating the hydrogenation product to obtain a light gasoline product, an aromatic hydrocarbon product and a heavy gasoline product; (3) And (3) carrying out solvent extraction and rectification on the aromatic hydrocarbon product to obtain a BTX product and a medium gasoline product. The method of the invention can produce the BTX product with high added value and can also produce clean gasoline blending components with high octane number.

Description

Method for producing light aromatic hydrocarbon and clean gasoline component from inferior gasoline

Technical Field

The invention relates to a method for producing aromatic hydrocarbon and clean gasoline components from inferior gasoline, in particular to a method for converting low-value gasoline into high-value light aromatic hydrocarbon benzene, toluene and para-xylene (BTX) chemical products and low-sulfur and low-olefin clean gasoline components.

Background

Along with the rapid increase of Chinese economy into a high-quality increase period, the problem of excessive productivity in the oil refining industry in China is prominent at present and in the future, the demand of finished oil (gasoline, diesel) is greatly slowed down, the demand of diesel is reduced from 2010, the diesel ratio is reduced from 2.17 in 2010 to about 1.1 in 2020, the gasoline demand of about 2025 is expected to enter a platform period, the distillate oil such as diesel, gasoline and the like is seriously excessive, and the fuel is converted into olefin (C ₂ ⁼ ~C ₄ ⁼ ) And light aromatic hydrocarbon benzene, toluene, paraxylene (BTX) and other basic organic chemical raw materials are continuously in shortage, and the method has great market economic value. The oil refining enterprises change from fuel type to energy chemical type, so that the oil is suitable for oil, the alkene is suitable for alkene, and the aromatic is suitable for aromatic, and the oil refining enterprises become the necessary development trend of clean oil refining.

China is a large country of catalytic cracking (FCC), more than 150 sets of FCC units of different types are built and put into production, and the total processing capacity of the FCC units reaches approximately 150Mt/a. The gasoline component produced by the FCC unit accounts for about 80% of the total gasoline product. The sulfur content in FCC gasoline is generally 200-1000 mug/g, and the olefin content is generally 20.0-45.0 v%. The sulfur and olefin content in FCC gasoline are high, on one hand, the reduction of the sulfur content and olefin content in FCC gasoline is the key to meet the increasingly strict clean gasoline standard, and on the other hand, the research on how to convert inferior (high sulfur and high olefin content) and low value FCC gasoline into high added value light aromatic hydrocarbon (BTX) and other chemical raw materials is an economic and effective scheme for solving the problems of quality upgrading and surplus energy production of gasoline in China.

CN100526430C discloses a process for producing clean gasoline. The method takes a modified ZSM-5 molecular sieve as a catalyst, and adopts a fluidized bed process to carry out hydrodesulfurization and olefin aromatization on the poor FCC gasoline with high sulfur and high olefin content into clean gasoline with low sulfur and low olefin. However, the method has the disadvantage that in order to meet the limit of the vehicle clean gasoline on the total content of aromatic hydrocarbon not more than 35.0v%, the aromatization rate is low, and the aromatic hydrocarbon is generally increased from about 22.0v% to 31.5v%.

CN108452846a discloses a gasoline hydrofining catalyst and a preparation method thereof. The method comprises the steps of uniformly mixing alumina powder and a TS-1 molecular sieve, adding graphene, kneading, forming, drying and roasting to obtain a carrier, preparing an impregnating solution by using heteropolyacid containing active metal components, and drying and roasting to obtain the catalyst. The catalyst can improve the hydrodesulfurization activity, but does not relate to the problem of converting olefins into aromatic hydrocarbons.

CN101492610B discloses a method for deep desulfurization and olefin reduction of gasoline, which comprises contacting gasoline raw material and hydrogen with hydrogenation adsorption desulfurization catalyst and olefin aromatization catalyst in sequence, removing sulfur in gasoline and reducing olefin content of the product. The method increases side reactions such as aromatization reaction, cracking, polymerization and the like of the full-fraction gasoline, so that the catalyst is easy to accumulate and deactivate, and the operation period is influenced; the liquid yield of the gasoline product is reduced, and the indexes such as vapor pressure, benzene content and the like are also affected; the octane number loss is large, and the defect is more remarkable if the content of olefin is required to meet the requirement of no more than 15.0 v%.

CN110184089a discloses a low sulfur catalytic cracking gasoline treatment method. The method is to cut low sulfur catalytic cracking gasoline into light fraction, middle fraction and heavy fraction; wherein the sulfur content in the low-sulfur catalytic cracking gasoline is not more than 10 mg/kg; the aromatic potential content in the middle distillate is not less than 35% by weight, and the C9 aromatic hydrocarbon content is not more than 8% by volume; the benzene content in the light fraction is not higher than 0.8% by volume. The method can realize the production increase of industrial materials and the production of national VI gasoline and national VI ethanol gasoline blending components, but has strict requirements on raw materials, too high dependence and can not produce more light aromatic hydrocarbons, the content of the aromatic hydrocarbons in the raw materials directly determines the amount of the industrial materials such as the light aromatic hydrocarbons and the like, and the applicability range is narrow. CN108315049a discloses a process for producing aromatic hydrocarbon by using catalytically cracked gasoline, which is characterized by comprising the steps of: pre-hydrogenating the catalytic cracking gasoline to obtain pre-hydrogenated catalytic cracking gasoline; cutting the pre-hydrocracked gasoline into a light fraction and a heavy fraction; extracting the light fraction by using a solvent to obtain raffinate oil rich in olefin and extract oil rich in aromatic hydrocarbon; carrying out mild aromatization on the raffinate oil to obtain an aromatization product; recovering light olefins from the extracted oil to obtain light olefins and sulfur-rich oil; returning a portion of said light olefins to said solvent extraction and said mild aromatization of another portion of said light olefins; carrying out selective hydrodesulfurization on the heavy fraction and sulfur-rich oil to obtain a desulfurization heavy fraction; and carrying out aromatic extraction or extractive distillation on the aromatization product and the desulfurization heavy fraction. The method has complex process flow and higher energy consumption, and the obtained gasoline blending component has high olefin content and can not meet the national VI clean gasoline standard.

In the prior art of desulfurizing inferior gasoline, the aromatization reaction of gasoline components is mainly used for reducing octane number loss caused by olefin saturation, and the depth of the aromatization reaction in the prior art is low based on the limitation of aromatic hydrocarbon content in clean gasoline standards, and the selectivity of light aromatic hydrocarbon in reaction products is not deeply studied, so that the prior art cannot be directly utilized to produce clean gasoline components, and simultaneously, more high-value chemical products such as light aromatic hydrocarbon (BTX) and the like are produced. In the existing scheme for producing aromatic hydrocarbon based on catalytic cracking gasoline, the problems that the process flow is too complex, the reduction range of olefin content is limited, and the requirement of simultaneously producing gasoline components meeting VI clean gasoline standards cannot be met exist. Therefore, development of a process method which has simple process flow and can desulfurize and deeply aromatize inferior gasoline to produce high-value light aromatic hydrocarbon and clean gasoline components in a high yield is needed.

Disclosure of Invention

Aiming at the defects in the prior art, the invention provides a production method for producing light aromatic hydrocarbon and clean gasoline components from inferior gasoline.

The invention relates to a production method for producing light aromatic hydrocarbon and clean gasoline components from inferior gasoline, which comprises the following steps:

(1) The inferior gasoline raw material undergoes hydrodesulfurization and deep light aromatization reactions on a hydrodesulfurization/aromatization catalyst through a fluidization reactor to obtain a hydrogenation product;

(2) Fractionating and cutting the hydrogenation product obtained in the step (1) to obtain a light gasoline product, an aromatic hydrocarbon product and a heavy gasoline product;

(3) And (3) performing solvent extraction and rectification on the aromatic hydrocarbon product in the step (2) to obtain a BTX product and a medium gasoline product.

In the invention, the poor-quality gasoline raw materials in the step (1) comprise Fluid Catalytic Cracking (FCC) gasoline, coker gasoline, pyrolysis gasoline and the like, wherein the sulfur content is generally 100-500 mug/g, the aromatic hydrocarbon content is generally 15.0-40.0 v%, the olefin content is generally 15.0-50 v%, and the research octane number RON is generally 90-95.0.

In the invention, the deep light aromatization reaction in the step (1) refers to the aromatization reaction of the inferior gasoline component under the conditions of high temperature and low space velocity aromatization, and the aromatization product is mainly composed of BTX aromatic hydrocarbon of C6-C8.

In the invention, the hydrodesulfurization and deep light aromatization reactions in step (1) are carried out under the following conditions: the reaction pressure is 1.0 MPa-2.5 MPa, the reaction temperature is 400-600 ℃, and the total liquid hourly space velocity is 0.1h ^-1 ~3.0h ^-1 Hydrogen oilThe volume ratio is 50:1-300:1; preferred reaction conditions are as follows: the reaction pressure is 1.5 MPa-2.5 MPa, the reaction temperature is 450-550 ℃, and the total liquid hourly space velocity is 0.5 h ^-1 ~1.5h ^-1 The volume ratio of the hydrogen oil is 50-150:1.

The hydrodesulfurization/aromatization catalyst used in step (1) of the present invention is particularly preferably the following catalyst, in particular: the catalyst comprises zeolite molecular sieve, metal oxide, active metal component, auxiliary agent and binder.

The hydrodesulfurization/aromatization catalyst comprises 30.0wt% -50.0wt%, preferably 35.0wt% -45.0wt%, metal oxide 10.0wt% -20.0wt%, preferably 12.0wt% -18.0wt%, active metal component 10.0wt% -30.0wt%, preferably 15.0wt% -25.0wt%, and auxiliary agent 1.0wt% -5.0wt%, preferably 3.0wt% -5.0wt%.

In the hydrodesulfurization/aromatization catalyst, the zeolite molecular sieve is preferably a ZSM-5 molecular sieve, more preferably a zinc isomorphous substituted nano ZSM-5 molecular sieve, the molar ratio of silicon oxide to aluminum oxide is 50-200, preferably 100-200, and the particle size is 10-100 nm. In the zinc isomorphous substituted nano ZSM-5 molecular sieve, zinc accounts for 0.5 to 4.0 weight percent, preferably 1.0 to 3.8 weight percent of the weight of the zinc isomorphous substituted nano ZSM-5 molecular sieve. The metal oxide component is at least one selected from IIB metal oxide, IVB metal oxide and VB metal oxide, preferably at least one selected from zinc oxide, zirconium oxide and vanadium oxide. The active metal component is a first component active metal and a second component active metal, wherein the first component metal is a group VIII metal, preferably Ni, and the second component active metal is a metal group IIIB metal, preferably La. The weight of the catalyst is taken as a reference, the content of the VIII group metal in terms of oxide is 5.0-27.0 wt%, and the content of the IIIB group metal in terms of oxide is 0.5-5.0 wt%. The auxiliary agent is potassium and titanium, the molar ratio of the auxiliary agent K/Ti in the catalyst is 2:1 based on the molar content of elements, and the precursor of the auxiliary agent titanium and potassium is preferably potassium titanium oxalate. The binder is a binder adopted in the conventional catalyst preparation process, and alumina is generally adopted.

The above hydrodesulfurization/aromatization catalyst may be prepared by the following method: uniformly mixing zeolite molecular sieve, metal oxide, binder and auxiliary agent, spray drying and roasting the obtained slurry to obtain catalyst carrier, loading active metal on the carrier, drying and roasting to obtain the catalyst.

The above hydrodesulfurization/aromatization catalyst is preferably prepared by the following method comprising:

a) Dissolving auxiliary potassium and titanium precursors in an organic acid solution to obtain a solution A;

b) Uniformly mixing a zeolite molecular sieve, a metal oxide, a binder and a forming additive, and then adding the solution A in a spray mode to obtain a mixed material B;

c) Kneading, extruding, drying and roasting the mixed material B to obtain a strip-shaped carrier C;

d) Ball milling and sieving the strip-shaped carrier C in a planetary ball mill to obtain a material D;

e) Mixing and pulping the material D obtained in the step D) in a solution containing active metal components to obtain slurry E with the solid content of 10-60 wt%;

f) And E) performing spray drying on the slurry E obtained in the step E), and roasting to prepare the hydrodesulfurization/aromatization catalyst.

In the preparation method of the hydrodesulfurization/aromatization microspherical catalyst, the organic acid in the step a) is preferably one or more of citric acid, malic acid, tartaric acid, succinic acid, glutaric acid, adipic acid, benzoic acid, salicylic acid, malonic acid and succinic acid; wherein the molar ratio of the addition amount of the organic acid to the auxiliary agent K is 1-30, preferably 5-15, based on the carbon content. The addition of the organic acid can improve the solubility of the auxiliary agent precursor, and meanwhile, the complexation of the titanium potassium oxalate and the organic acid is beneficial to the uniform distribution of the auxiliary agent K, ti on the carrier and the adjustment of the acid property of the surface of the carrier, so that the content of B acid is reduced, the content of L acid is improved, the generation of dehydrogenation active centers is promoted, the selectivity of low-carbon aromatic hydrocarbon is improved, and the aromatization reaction performance of the catalyst is improved.

The forming auxiliary agent in the step b) refers to substances which are favorable for extrusion forming, such as one or more of sesbania powder, carbon black, graphite powder and the like, and the dosage of the forming auxiliary agent is 1.0-5.0 wt% of the total material dry basis.

And c), drying at 100-150 ℃ for 2-10 hours, and roasting at 400-600 ℃ for 3-10 hours.

The ball milling time in the step d) is generally 30-60 min, and the mesh number of the sieving is 150-250 mesh.

In the step e), dispersing agents are preferably added, wherein the dispersing agents are one or more of polyvinyl alcohol, polyvinylpyrrolidone and polyethylene glycol, preferably the polyvinyl alcohol, and the dosage of the dispersing agents is 1.0-10.0 wt% of the total material dry basis. And adding a dispersing agent under the stirring condition, heating to 45-80 ℃, keeping the temperature for 30-90 min, and cooling to room temperature to obtain slurry.

And f) the spray pressure of the spray drying is 4-10 MPa, the preferable range of the inlet temperature is 150-380 ℃, the preferable range of the outlet temperature is 100-230 ℃, the roasting is 400-600 ℃ and the roasting is 3-10 h, and the particle size of the catalyst is 60-100 mu m.

In the invention, in the hydrogenated product obtained in the step (1), the sulfur content is not more than 10 mu g/g, the aromatic hydrocarbon content is not less than 45.0v percent, and the olefin content is not more than 5.0v percent.

In the invention, in the fractional cutting of the hydrogenation product in the step (2), the cutting temperature of the light gasoline and the aromatic hydrocarbon product is 60-80 ℃, preferably 65-80 ℃, and the cutting temperature of the aromatic hydrocarbon product and the heavy gasoline product is 130-150 ℃, preferably 135-145 ℃.

In the invention, the light gasoline product obtained in the step (2) can be used as an ethylene cracking raw material to produce ethylene, and can also be directly used as a blending component (sulfur content not more than 10 mug/g and olefin content not more than 5.0 v%) of low-sulfur and low-olefin clean gasoline together with a medium gasoline product and a heavy gasoline product, so that the clean gasoline standard of state VI and above is satisfied.

In the invention, the BTX product obtained by solvent extraction and rectification in the step (3) generally accounts for 40.0% -60.0% of the aromatic hydrocarbon product by mass, and the medium gasoline product generally accounts for 40.0% -60.0% of the aromatic hydrocarbon product.

In the invention, the BTX product in the step (3) can be used as chemical raw materials such as PX.

In the invention, the light gasoline has a distillation range of 35-80 ℃, the medium gasoline has a distillation range of 60-150 ℃, and the heavy gasoline has a distillation range of 130-205 ℃.

In the hydrodesulfurization/aromatization catalyst prepared by the invention, the carrier components are combined in the modes of extruding strips, drying and roasting to ensure that the carrier obtains a certain carrier pore canal, higher mechanical strength and abrasion resistance; secondly, carrying out ball milling and sieving on the carrier to obtain a plurality of micron-sized reaction unit particles which retain the original pore channels and specific surface properties and are equivalent to a plurality of micro-reaction unit precursors; and immersing the plurality of micron-sized reaction unit particles in an active metal solution containing a dispersing agent to enable the active metal to be fully dispersed on the micron-sized reaction unit particles, and performing spray forming to obtain the catalyst with uniform particle size and high desulfurization activity and aromatization activity.

The hydrodesulfurization/aromatization catalyst prepared by the invention has high desulfurization activity and deep light aromatic aromatization reaction activity, and simultaneously has higher carbon deposit resistance, mechanical strength and abrasion resistance, thereby being beneficial to maintaining the catalyst activity when the catalyst is circularly regenerated in a fluidization reactor. The hydrodesulfurization/aromatization microspheric catalyst and the high-temperature low-space-velocity aromatization reaction conditions are adopted to easily realize the hydrodesulfurization and deep light aromatization reaction, the sulfur content in the hydrogenation product is extremely low, the olefin content is low, the aromatic hydrocarbon content is high, the selectivity of light aromatic hydrocarbon (BTX) in the generated aromatic hydrocarbon is high, and the subsequent separation process is utilized to realize the high-value chemical raw materials and clean gasoline blending components which are produced in high yield of the inferior gasoline, thereby being an economic and effective scheme for solving the problems of quality upgrading and surplus productivity of the gasoline in China.

Compared with the prior art, the invention has the following advantages:

1. according to the method, inferior gasoline is used as a reaction raw material, hydrodesulfurization and deep light aromatization are carried out in a fluidization reactor, desulfurization and aromatization of gasoline components are realized in one step, while the sulfur content in the gasoline is reduced, alkane and alkene in the raw material are subjected to aromatization, so that the alkene content in the gasoline is effectively reduced, the light aromatic hydrocarbon (BTX) component with high added value is increased, and the clean gasoline component with low sulfur and low alkene content, especially with the sulfur content of less than 10 mug/g and the alkene content of less than 5.0v%, can be produced.

2. The method combines the characteristics of the inferior gasoline, and preferably adopts a hydrodesulfurization/aromatization catalyst with a specific preparation method, wherein the catalyst has high desulfurization activity and deep light aromatic aromatization reaction activity, the sulfur content in a hydrogenation product is extremely low, the olefin content is low, the aromatic hydrocarbon content is high, and the selectivity of light aromatic hydrocarbon (BTX) in the generated aromatic hydrocarbon is high under the high-temperature and low-airspeed aromatization reaction conditions, so that the oriented conversion from the inferior gasoline to clean components and high-added-value chemical raw materials is realized. Meanwhile, the catalyst has higher carbon deposition resistance, mechanical strength and abrasion resistance, and can realize long-period operation in the fluidization reactor.

3. The invention realizes the high-efficiency separation of clean gasoline components and high added value light aromatic hydrocarbons (BTX) in the hydrogenated product through the subsequent fractional distillation, cutting and rectifying extraction processes, and the light gasoline product can be used as clean gasoline blending components and also can be used as ethylene cracking raw materials when the gasoline demand is obviously reduced, and the process flow is simple, the scheme is flexible, and the invention has obvious economic benefit.

4. According to the invention, the low-sulfur low-olefin gasoline component meeting national VI standard is produced, and meanwhile, part of the gasoline component is increased in yield and high-added-value light aromatic hydrocarbon (BTX), so that not only can the problem of upgrading the gasoline quality in China be solved, but also the economic and effective technical scheme for solving the problem of excessive oil refining capacity in the future in China can be solved, and the conversion upgrading from fuel type to energy chemical type in oil refining enterprises is promoted.

Drawings

FIG. 1 is a schematic flow chart of the method of the present invention, wherein:

a-fluidization reactor, B-fractionating tower, C-extraction rectifying tower, 1-inferior gasoline, 2-hydrogen, 3-hydrogenation product, 4-light gasoline product, 5-aromatic hydrocarbon product, 6-heavy gasoline product, 7-medium gasoline product, 8-light aromatic hydrocarbon (BTX) product and 9-clean gasoline blending component.

FIG. 2 is another schematic flow chart of the method of the present invention, wherein:

Detailed Description

The poor gasoline raw material in the method is one or more of Fluid Catalytic Cracking (FCC) gasoline, catalytic pyrolysis gasoline, coker gasoline, thermal cracking gasoline and the like. The preferred feedstock for this invention is FCC gasoline. The poor gasoline raw material can be full-fraction FCC gasoline, wherein the initial distillation point is 35-40 ℃, preferably 35-38 ℃, the final distillation point is 180-205 ℃, preferably 190-205 ℃; the sulfur content is not more than 500 mu g/g, preferably 100 mu g/g-500 mu g/g; the olefin content is generally 15.0 to 50.0% by volume, in particular 25.0 to 40.0% by volume; the aromatic hydrocarbon content is generally 15.0 to 40.0% by volume, particularly 20.0 to 30.0% by volume.

The fluidization reactor is a riser reactor or a fluidized bed reactor.

The fluidized bed reactor can be one or more selected from a fixed fluidized bed, a bulk fluidized bed, a bubbling bed, a turbulent bed, a fast bed, a conveying bed and a dense-phase fluidized bed; the riser reactor may be one or more selected from the group consisting of an equal diameter riser, an equal linear velocity riser, and various variable diameter risers.

The solvent extraction and rectification of the aromatic hydrocarbon product is mainly used for realizing the precise separation of aromatic hydrocarbon, olefin, alkane and naphthene so as to meet the production requirements of high-added-value chemical products such as PX and the like. The method adopted by the solvent extraction and rectification is not strictly limited, and can be used as long as the method can realize the accurate separation of aromatic hydrocarbon and non-aromatic hydrocarbon, for example, one or a combination of a plurality of diethylene glycol, sulfolane, N-formylmorpholine, N-formylpyrrolidone and the like can be adopted by an industrially mature method.

The process and effects of the method of the present invention are further described below with reference to the drawings and examples. The logistics and the unit operations are sequentially carried out along the arrow direction.

The method of the present invention will be described in detail with reference to fig. 1.

The inferior gasoline 1 and the hydrogen 2 are subjected to hydrodesulfurization and deep light aromatization reactions in a fluidization reactor A to obtain a hydrogenation product 3; the hydrogenation product 3 enters a fractionating tower B, and a light gasoline product 4, an aromatic hydrocarbon product 5 and a heavy gasoline product 6 are respectively obtained at the top, the side line and the bottom of the fractionating tower; the aromatic hydrocarbon product 5 is fed into a solvent extraction rectifying tower C, and a middle gasoline product 7 and a BTX product 8 are respectively obtained at the top and the bottom of the tower; the light gasoline product 4, the medium gasoline product 7 and the heavy gasoline product 6 are mixed to obtain a clean gasoline blending component 9.

The method of the present invention will be described in detail with reference to fig. 2.

The inferior gasoline 1 and the hydrogen 2 are subjected to hydrodesulfurization and deep light aromatization reactions in a fluidization reactor A to obtain a hydrogenation product 3; the hydrogenation product 3 enters a fractionating tower B, and a light gasoline product 4, an aromatic hydrocarbon product 5 and a heavy gasoline product 6 are respectively obtained at the top, the side line and the bottom of the fractionating tower; the aromatic hydrocarbon product 5 is fed into a solvent extraction rectifying tower C, and a middle gasoline product 7 and a BTX product 8 are respectively obtained at the top and the bottom of the tower; light gasoline product 4 is used as ethylene cracking raw material; the medium gasoline product 7 and the heavy gasoline product 6 are mixed to obtain a clean gasoline blending component 9.

The following examples further illustrate the aspects and effects of the present invention, but are not intended to limit the invention.

Example 1

This example prepares a hydrodesulfurization/aromatization catalyst Z-1 from 35.0wt% Zn-ZSM molecular sieve (SiO ₂ /Al ₂ O ₃ The molar ratio is 100, the grain size is 20 nm-80 nm, the Zn content is 2.0wt%, 10.0wt% ZnO, 5.0wt% (K+Ti), 18.0wt% NiO, 2.0wt% La ₂ O ₃ The balance of alumina.

The preparation method of the Z-1 catalyst comprises the following steps:

14.1g of potassium titanium oxalate was dissolved in 100mL of a citric acid solution having a concentration of 152 g/L; uniformly mixing 35.0g of Zn-ZSM-5 molecular sieve, 10.0g of ZnO, 38.5g of pseudo-boehmite and 3g of sesbania powder in a mortar, adding a potassium titanium oxalate citric acid solution into the mortar in a spray mode, and rolling and mixing to obtain plastic powder. Extruding plastic powder into cylindrical strips with the diameter of 1.5mm by using a strip extruder, drying at 120 ℃ for 5 hours, and roasting at 500 ℃ for 5 hours to prepare strip-shaped carriers; putting the strip-shaped carrier into a planetary ball mill for ball milling for 30min, and sieving the carrier with a 150-250 mesh sieve; taking 30g of powder passing through a 150-250 mesh sieve, adding the powder into 100mL of solution containing nickel nitrate and lanthanum nitrate, mixing and pulping, adding polyvinyl alcohol with the total material dry basis of 2.0wt% into the mixed slurry, heating to 60 ℃ and keeping the temperature for 60min, cooling to room temperature, performing spray drying on the obtained slurry, wherein the spray drying pressure is 6.0MPa, the inlet temperature is 220 ℃, the outlet temperature is about 120 ℃, and roasting for 4h at 400 ℃ to obtain the hydrodesulfurization/aromatization catalyst Z-1.

Example 2

This example prepares hydrodesulfurization/aromatization catalyst Z-2 from 45.0wt% Zn-ZSM molecular sieve (SiO ₂ /Al ₂ O ₃ The molar ratio is 100, the grain size is 20 nm-80 nm, the Zn content is 2.0wt%, 15.0wt% ZnO, 5.0wt% (K+Ti), 22.0 wt% NiO, 1.0wt% La ₂ O ₃ The balance of alumina.

The preparation method of the Z-2 catalyst comprises the following steps:

14.1g of potassium titanium oxalate was dissolved in 100mL of a citric acid solution having a concentration of 152 g/L; uniformly mixing 45.0g of Zn-ZSM-5 molecular sieve, 15.0g of ZnO, 13.8g of pseudo-boehmite and 3g of sesbania powder in a mortar, adding a potassium titanium oxalate citric acid solution into the mortar in a spray mode, and rolling and mixing to obtain plastic powder. Extruding plastic powder into cylindrical strips with the diameter of 1.5mm by using a strip extruder, drying at 120 ℃ for 5 hours, and roasting at 500 ℃ for 5 hours to prepare strip-shaped carriers; putting the strip-shaped carrier into a planetary ball mill for ball milling for 30min, and sieving the carrier with a 150-250 mesh sieve; taking 30g of powder passing through a 150-250 mesh sieve, adding the powder into 100mL of solution containing nickel nitrate and lanthanum nitrate, mixing and pulping, adding polyvinyl alcohol with the total material dry basis of 2.0wt% into the mixed slurry, heating to 60 ℃ and keeping the temperature for 60min, cooling to room temperature, performing spray drying on the obtained slurry, wherein the spray drying pressure is 6.0MPa, the inlet temperature is 220 ℃, the outlet temperature is about 120 ℃, and roasting for 4h at 400 ℃ to obtain the hydrodesulfurization/aromatization catalyst Z-2.

Example 3

This example prepares a hydrodesulfurization/aromatization catalyst Z-3, the composition of which is the same as example 1.

The Z-3 catalyst is prepared according to a conventional preparation method, and the process is as follows:

35.0g of Zn-ZSM-5 molecular sieve, 10.0g of ZnO, 14.1g of potassium titanium oxalate, 38.5g of pseudo-boehmite and 400mL of deionized water are mixed and pulped, the slurry is spray-dried, the spray-drying pressure is 6.0MPa, the inlet temperature is 220 ℃, the outlet temperature is about 120 ℃, and the catalyst carrier is obtained by roasting for 4 hours at 400 ℃. The carrier is put into a spray dipping tank, solution containing lanthanum nitrate and nickel nitrate is sprayed on the carrier within 30 minutes, and after the solution is dried at room temperature, the solution is dried for 10 hours at 120 ℃, and is roasted for 8 hours at 450 ℃ to prepare the hydrodesulfurization/aromatization catalyst Z-3.

Example 4

This example is an examination of the attrition resistance of the Z-1 catalyst. The abrasion resistance of the catalyst is evaluated by adopting a straight pipe abrasion method, the method refers to RIPP29-90 in petrochemical analysis method (RIPP) experimental method, and the smaller the value obtained by testing, the higher the abrasion resistance is, and the evaluation result is shown in Table 1. The abrasion index in Table 1 corresponds to the percentage of fines generated when abraded under certain conditions.

Example 5

In this example, the abrasion resistance of the Z-2 catalyst was examined, and the evaluation method was the same as in example 4, and the evaluation results are shown in Table 1.

Example 6

In this example, the abrasion resistance of the Z-3 catalyst was examined, and the evaluation method was the same as in example 4, and the evaluation results are shown in Table 1.

Example 7

The embodiment is a process method for producing light aromatic hydrocarbon (BTX) and clean gasoline components by using catalytic cracking gasoline, which comprises the following specific steps:

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-1 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to hydrodesulfurization and deep light aromatization reaction in the fluidized bed, wherein the reaction process conditions are as follows: the reaction pressure is 1.6MPa,the reaction temperature is 480 ℃, and the liquid hourly space velocity is 1.0h ^-1 The hydrogen oil volume ratio is 100:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 70 ℃ and 140 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 21.5wt%, 51.8wt% and 26.7wt%, the distillation range of the light gasoline product is 35-70 ℃, the distillation range of the aromatic hydrocarbon product is 70-140 ℃, and the distillation range of the heavy gasoline product is 140-198 ℃.

(3) And (3) extracting and rectifying the aromatic hydrocarbon product, wherein the extracting agent adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extracting agent is 8:1, and the BTX product and the middle gasoline product are respectively 51.1wt% and 48.9wt% of the aromatic hydrocarbon product.

(4) Mixing the light gasoline product, the medium gasoline product and the heavy gasoline product to obtain the clean gasoline blending component.

The properties of the BTX product and clean gasoline blending components obtained by the above process are shown in table 3.

Example 8

The embodiment is a process method for producing light aromatic hydrocarbon (BTX), ethylene cracking material and clean gasoline components by using catalytic cracking gasoline, which comprises the following specific steps:

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-1 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to desulfurization and aromatization reaction in a fluidized bed, and the reaction process conditions are as follows: the reaction pressure is 2.0MPa, the reaction temperature is 500 ℃, and the liquid hourly space velocity is 1.5h ^-1 The hydrogen oil volume ratio is 150:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 65 ℃ and 135 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 18.5wt percent, 51.6wt percent and 29.9wt percent respectively, the distillation range of the light gasoline product is 35 ℃ to 65 ℃, the distillation range of the aromatic hydrocarbon product is 65 ℃ to 135 ℃, and the distillation range of the heavy gasoline product is 135 ℃ to 198 ℃.

(3) And (3) carrying out extractive distillation on the aromatic hydrocarbon product, wherein the extractant adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extractant is 7:1, and the BTX product and the middle gasoline product are obtained, wherein the BTX product and the middle gasoline product respectively account for 52.7wt% and 47.3wt% of the aromatic hydrocarbon product.

(4) The light gasoline product is used as ethylene cracking raw material, and the medium gasoline product and the heavy gasoline product are mixed to be used as clean gasoline blending components.

Properties of the BTX product, clean gasoline blending components, and ethylene pyrolysis stock obtained by the above process are shown in table 3.

Example 9

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-2 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to desulfurization and aromatization reaction in a fluidized bed, and the reaction process conditions are as follows: the reaction pressure is 2.4MPa, the reaction temperature is 450 ℃, and the liquid hourly space velocity is 0.8h ^-1 The hydrogen oil volume ratio is 80:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 75 ℃, the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 23.7wt%, 49.1wt% and 27.2wt%, the distillation range of the light gasoline product is 35-75 ℃, the distillation range of the aromatic hydrocarbon product is 75-140 ℃, and the distillation range of the heavy gasoline product is 140-198 ℃.

(3) And (3) extracting and rectifying the aromatic hydrocarbon product, wherein an extracting agent adopts a mixed solvent of sulfolane and N-formylpyrrolidone, the volume content ratio of the sulfolane to the N-formylpyrrolidone in the mixed extracting agent is 9:1, and the BTX product and the middle gasoline product are obtained, wherein the BTX product and the middle gasoline product respectively account for 54.3wt% and 45.7wt% of the aromatic hydrocarbon product.

Properties of the BTX product, clean gasoline blending component obtained by the above process are shown in table 3.

Example 10

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-2 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to desulfurization and aromatization reaction in a fluidized bed, and the reaction process conditions are as follows: the reaction pressure is 1.5MPa, the reaction temperature is 550 ℃, and the liquid hourly space velocity is 1.2h ^-1 The hydrogen oil volume ratio is 120:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 65 ℃ and 145 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 17.9wt percent, 57.3wt percent and 24.8wt percent respectively, the distillation range of the light gasoline product is 35-65 ℃, the distillation range of the aromatic hydrocarbon product is 65-145 ℃, and the distillation range of the heavy gasoline product is 145-195 ℃.

(3) And (3) extracting and rectifying the aromatic hydrocarbon product, wherein an extracting agent adopts a mixed solvent of sulfolane and N-formylpyrrolidone, the volume content ratio of the sulfolane to the N-formylpyrrolidone in the mixed extracting agent is 8:1, and the BTX product and the middle gasoline product are respectively 49.8wt% and 50.2wt% of the aromatic hydrocarbon product.

Example 11

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-3 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to desulfurization and aromatization reaction in the fluidized bed under the reaction process conditions: the reaction pressure is 1.8MPa, the reaction temperature is 500 ℃, and the liquid hourly space velocity is 1.0h ^-1 The hydrogen oil volume ratio is 150:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 70 ℃ and 135 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 22.8wt percent, 46.7wt percent and 30.5wt percent respectively, the distillation range of the light gasoline product is 35-70 ℃, the distillation range of the aromatic hydrocarbon product is 70-135 ℃, and the distillation range of the heavy gasoline product is 135-198 ℃.

(3) And (3) carrying out extractive distillation on the aromatic hydrocarbon product, wherein the extractant adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extractant is 8:1, and the BTX product and the middle gasoline product are respectively 43.3wt% and 56.7wt% of the aromatic hydrocarbon product.

Example 12

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-3 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to desulfurization and aromatization reaction in a fluidized bed, and the reaction process conditions are as follows: the reaction pressure is 2.2MPa, the reaction temperature is 500 ℃, and the liquid hourly space velocity is 1.2h ^-1 The hydrogen oil volume ratio is 100:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 65 ℃ and 140 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 19.1wt%, 52.3wt% and 28.6wt%, the distillation range of the light gasoline product is 35-65 ℃, the distillation range of the aromatic hydrocarbon product is 65-140 ℃, and the distillation range of the heavy gasoline product is 140-198 ℃.

(3) And (3) carrying out extractive distillation on the aromatic hydrocarbon product, wherein the extractant adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extractant is 7:1, and the BTX product and the middle gasoline product are obtained, wherein the BTX product and the middle gasoline product respectively account for 41.2wt% and 58.8wt% of the aromatic hydrocarbon product.

Comparative example 1

This comparative example is a comparison to example 7, except that the catalyst used in step (1) is a commercial FCAS adsorption desulfurization catalyst, and the specific steps are as follows:

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of FCAS catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials react in the fluidized bed, and the reaction process conditions are as follows: the reaction pressure is 1.6MPa, the reaction temperature is 480 ℃, and the liquid hourly space velocity is 1.0h ^-1 The hydrogen oil volume ratio is 100:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 70 ℃ and 140 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 35.1wt percent, 34.1wt percent and 30.8wt percent respectively, the distillation range of the light gasoline product is 35-70 ℃, the distillation range of the aromatic hydrocarbon product is 70-140 ℃, and the distillation range of the heavy gasoline product is 140-198 ℃.

(3) And (3) carrying out extractive distillation on the aromatic hydrocarbon product, wherein the extractant adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extractant is 8:1, and the BTX product and the middle gasoline product are obtained, wherein the BTX product and the middle gasoline product respectively account for 27.4wt% and 72.6wt% of the aromatic hydrocarbon product.

The properties of the BTX product and clean gasoline blending components obtained by the above process are shown in table 4.

Comparative example 2

This comparative example is a comparison with example 7, except that the catalyst used in step (1) is an aromatization catalyst a prepared according to example 1 in patent CN108479846B, the specific steps are as follows:

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of aromatization catalyst A is filled into a small continuous fluidized bed reactor, and the aromatization reaction is carried out on the reaction raw materials in the fluidized bed, and the reaction process conditions are as follows: the reaction pressure is 1.6MPa, the reaction temperature is 480 ℃, and the liquid hourly space velocity is 1.0h ^-1 The hydrogen oil volume ratio is 100:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 70 ℃ and 140 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 25.4wt%, 40.1wt% and 34.5wt%, the distillation range of the light gasoline product is 35-70 ℃, the distillation range of the aromatic hydrocarbon product is 70-140 ℃, and the distillation range of the heavy gasoline product is 140-198 ℃.

(3) And (3) extracting and rectifying the aromatic hydrocarbon product, wherein the extracting agent adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extracting agent is 8:1, and the BTX product and the middle gasoline product are respectively 30.1wt% and 69.9wt% of the aromatic hydrocarbon product.

Comparative example 3

This comparative example is different from example 7 in that the desulfurization and aromatization reaction conditions used in step (1) are different, and the specific steps are as follows:

(1) The reaction raw material is catalytic cracking gasoline, and the raw material properties are shown in table 2. 40mL of Z-1 catalyst is filled into a small continuous fluidized bed reactor, and the reaction raw materials are subjected to hydrodesulfurization and deep light aromatization reaction in the fluidized bed to reactThe process conditions are as follows: the reaction pressure is 1.6MPa, the reaction temperature is 350 ℃, and the liquid hourly space velocity is 5.0h ^-1 The hydrogen oil volume ratio is 350:1.

(2) The hydrogenation product is subjected to fractional cutting, the fractional cutting temperature is 70 ℃ and 140 ℃, and the yields of the light gasoline product, the aromatic hydrocarbon product and the heavy gasoline product are 24.3wt percent, 45.2wt percent and 30.5wt percent respectively, the distillation range of the light gasoline product is 35-70 ℃, the distillation range of the aromatic hydrocarbon product is 70-140 ℃, and the distillation range of the heavy gasoline product is 140-198 ℃.

(3) And (3) carrying out extractive distillation on the aromatic hydrocarbon product, wherein the extractant adopts a mixed solvent of sulfolane and N-formylmorpholine, the volume content ratio of the sulfolane to the N-formylmorpholine in the mixed extractant is 8:1, and the BTX product and the middle gasoline product are obtained, wherein the BTX product and the middle gasoline product respectively account for 34.8wt% and 65.2wt% of the aromatic hydrocarbon product.

TABLE 1 attrition resistance of catalysts

Table 2 raw gasoline properties

TABLE 3 example reaction product Properties

Table 4 comparative example reaction product properties

From the results of the reaction products, the catalyst prepared by the invention has better abrasion resistance strength, so that the service life of the catalyst can be prolonged. The invention can realize the production of high added value BTX products and low sulfur and low olefin clean gasoline blending components by using the inferior gasoline, has high BTX yield, simple process flow and flexible scheme, and is an economic and effective technical scheme for solving the problems of upgrading gasoline quality in China and excessive oil refining productivity in future.

Claims

1. The production method for producing light aromatic hydrocarbon and clean gasoline components from inferior gasoline is characterized by comprising the following steps: (1) In a fluidization reactor, the inferior gasoline raw material undergoes hydrodesulfurization and deep light aromatization reactions on a hydrodesulfurization/aromatization catalyst to obtain a hydrogenation product; (2) Fractionating and cutting the hydrogenation product obtained in the step (1) to obtain a light gasoline product, an aromatic hydrocarbon product and a heavy gasoline product; (3) Performing solvent extraction and rectification on the aromatic hydrocarbon product in the step (2) to obtain light aromatic hydrocarbon and medium gasoline products;

the step (1) adopts a hydrodesulfurization/aromatization catalyst, and takes the weight of the catalyst as a reference,

the content of the zeolite molecular sieve is 30.0 to 50.0 weight percent,

the content of the metal oxide is 10.0wt% to 20.0wt%,

the content of the active metal component calculated by oxide is 10.0wt percent to 30.0wt percent,

the content of the auxiliary agent is 1.0-5.0 wt% calculated by elements;

the zeolite molecular sieve is ZSM-5 molecular sieve;

the metal oxide component is one or more of zinc oxide, zirconium oxide and vanadium oxide;

the active metal component comprises a first component active metal and a second component active metal, wherein the first component active metal is Ni, and the second component active metal is La;

the auxiliary agent is potassium or titanium.

2. The production method according to claim 1, characterized in that: the sulfur content of the poor-quality gasoline raw material in the step (1) is 100-500 mug/g, the aromatic hydrocarbon content is 15.0-40.0 v%, the olefin content is 15.0-50 v%, and the research octane number RON is 90-95.0.

3. The production method according to claim 1, characterized in that: the deep light aromatization reaction in the step (1) refers to an aromatization reaction of poor gasoline components under the conditions of high-temperature and low-airspeed aromatization reaction, and the aromatization product is mainly composed of C6-C8 light aromatic hydrocarbons.

4. The production method according to claim 1, characterized in that: the hydrodesulfurization and deep light aromatization reaction conditions in the step (1) are as follows: the reaction pressure is 1.0-2.5 MPa, the reaction temperature is 400-600 ℃, and the total liquid hourly space velocity is 0.1-3.0 h ^-1 The volume ratio of the hydrogen to the oil is 50:1-300:1.

5. The production method according to claim 1, characterized in that: the hydrodesulfurization and deep light aromatization reaction conditions described in step (1) are as follows: the reaction pressure is 1.5-2.5 MPa, the reaction temperature is 450-550 ℃, and the total liquid hourly space velocity is 0.5-1.5 h ^-1 The volume ratio of the hydrogen oil is 50-150:1.

6. The production method according to claim 1, characterized in that: zinc isomorphous substituted nano ZSM-5 molecular sieve, the mol ratio of silicon oxide to aluminum oxide is 50-200, and the grain diameter is 10-100 nm; the auxiliary agent is potassium and titanium, and the ratio of the auxiliary agent K to the Ti is 2:1 based on the molar content of elements.

7. The production method according to claim 6, wherein: in the zinc isomorphous substituted nano ZSM-5 molecular sieve, zinc accounts for 0.5 to 4.0 weight percent of the weight of the zinc isomorphous substituted nano ZSM-5 molecular sieve based on elements.

8. The production method according to claim 1, characterized in that: the content of Ni is 5.0-27.0 wt% based on oxide, and the content of La is 0.5-5.0 wt% based on oxide.

9. The production method according to claim 1, characterized in that: the preparation method of the hydrodesulfurization/aromatization catalyst comprises the following steps: a) Dissolving precursors of auxiliary agents titanium and potassium in an organic acid solution to obtain a solution A; b) Uniformly mixing a zeolite molecular sieve, a metal oxide, a binder and a forming additive, and then adding the solution A in a spray mode to obtain a mixed material B; c) Kneading, extruding, drying and roasting the mixed material B to obtain a strip-shaped carrier C; d) Ball milling and sieving are carried out on the strip-shaped carrier C to obtain a material D; e) Mixing and pulping the material D obtained in the step D) in a solution containing active metal components, and adding a dispersing agent under the stirring condition to obtain slurry E; f) And E) performing spray forming on the slurry E obtained in the step E), and roasting to prepare the hydrodesulfurization/aromatization catalyst.

10. The production method according to claim 9, characterized in that: the precursor of the auxiliary agent titanium and potassium is potassium titanium oxalate.

11. The production method according to claim 9, characterized in that: the organic acid in the step a) is one or more of citric acid, malic acid, tartaric acid, succinic acid, glutaric acid, adipic acid, benzoic acid, salicylic acid, malonic acid and succinic acid; the molar ratio of the addition amount of the organic acid to the auxiliary agent potassium is 1-30 based on the carbon content.

12. The production method according to claim 9, characterized in that: the forming auxiliary agent in the step b) is one or more of sesbania powder, carbon black or graphite powder, and the dosage of the forming auxiliary agent is 1.0-5.0 wt% of the total material dry basis.

13. The production method according to claim 9, characterized in that: and c), drying at 100-150 ℃ for 2-10 hours, and roasting at 400-600 ℃ for 3-10 hours.

14. The production method according to claim 9, characterized in that: the ball milling time in the step d) is 30-60 minutes, and the mesh number of the screen is 150-250 meshes.

15. The production method according to claim 9, characterized in that: the dispersing agent in the step e) is one or more of polyvinyl alcohol, polyvinylpyrrolidone or polyethylene glycol, and the dosage of the dispersing agent is 1.0-10.0 wt% of the total material dry basis.

16. The production method according to claim 9, characterized in that: the solid content of the slurry in the step e) is 10-60 wt%.

17. The production method according to claim 9, characterized in that: the spray pressure of the spray forming in the step f) is 4-10 MPa, the inlet temperature is 150-380 ℃, and the outlet temperature is 100-230 ℃.

18. The production method according to claim 9, characterized in that: the particle size of the hydrodesulfurization/aromatization catalyst is 60-100 mu m.

19. The production method according to claim 9, characterized in that: in the hydrogenated product obtained in the step (1), the sulfur content is no more than 10 mug/g, the aromatic hydrocarbon content is no less than 45.0v percent, and the olefin content is no more than 5.0v percent.

20. The production method according to claim 9, characterized in that: in the step (2), the cutting temperature of the light gasoline and the aromatic hydrocarbon product is 60-80 ℃ and the cutting temperature of the aromatic hydrocarbon product and the heavy gasoline product is 130-150 ℃.

21. The production method according to claim 9, characterized in that: the light gasoline product obtained in the step (2) can be used as an ethylene cracking raw material to produce ethylene, or the medium gasoline product and the heavy gasoline product are used as blending components of low-sulfur and low-olefin clean gasoline.

22. The production method according to claim 9, characterized in that: and (3) extracting and rectifying the light aromatic hydrocarbon product by the solvent in the step (3), wherein the light aromatic hydrocarbon product accounts for 40.0-60.0% of the aromatic hydrocarbon product by mass.