A method for producing BTX by hydrogenating catalytic cracking diesel

Abstract

The present invention discloses a method for producing BTX by hydrogenating catalytically cracked diesel. The method comprises the following steps: (1) catalytically cracked diesel enters a hydrogenation pretreatment reaction zone, wherein the hydrogenation pretreatment reaction zone is sequentially loaded with a catalyst bed A and a catalyst bed B along the direction of the flow, wherein the catalyst loaded in the catalyst bed A is a hydrorefining catalyst, and the catalyst loaded in the catalyst bed B contains an acidic cracking component; (2) the hydrogenation pretreatment product oil obtained in step (1) enters a hydroconversion reaction zone for a hydrocracking reaction, wherein the hydroconversion reaction zone is loaded with a hydrocracking catalyst; (3) the hydroconversion product oil obtained in step (2) enters a separation system for gas-liquid separation, wherein the separated gas can be recycled as supplementary hydrogen, and the liquid phase product enters a fractionation tower for separation, wherein the fractionation tower is fractionated to obtain light naphtha, heavy naphtha, and tail oil, and the heavy naphtha is subjected to aromatics extraction to obtain BTX. The method can effectively improve the BTX yield in the hydrogenation product and reduce the aromatics loss during the hydrogenation process.

Description

Technical Field

[0001] The present invention relates to a method for producing BTX by hydrogenating catalytic cracking diesel, in particular to a hydrogenation method which uses catalytic cracking diesel as raw material and improves the BTX yield in the hydrogenation product by grading and filling. Background Art

[0002] Light aromatics such as benzene, toluene, and xylene are important basic chemical raw materials. With industrial development and improvements in living standards, the synthetic fiber, synthetic plastic, and synthetic rubber industries have grown rapidly, leading to an annual increase in demand for BTX, which is now in short supply. Hydrocracking, which converts dicyclic aromatics in catalytic diesel into light aromatics such as BTX, is an ideal solution for addressing diesel oversupply and the shortage of low-carbon aromatics. During hydrocracking, dicyclic aromatics are first partially hydrogenated to tetralin compounds, which then undergo ring opening and side chain cleavage to produce short-chain BTX aromatics.

[0003] CN201510761954.9 discloses a hydrocracking catalyst grading method and a catalytic diesel hydroconversion process. This grading method includes the following steps: dividing a hydrocracking reactor into 2 to 8 reaction zones along the direction of material flow, loading each reaction zone with a hydrocracking catalyst containing a regeneration agent. The regeneration agent content in the hydrocracking catalyst is 10% to 90% by weight, based on the weight of the hydrocracking catalyst, with the regeneration agent content gradually increasing in each reaction zone along the direction of material flow. This method also provides a catalytic diesel hydroconversion process that incorporates this hydrocracking catalyst grading method. By grading catalysts of varying reactivity within the cracking reactor, this method improves the hydrogenation selectivity of the diesel / gasoline component during the conversion process and increases the yield of high-octane gasoline products.

[0004] CN201711118958.0 discloses a method for producing high-quality gasoline and diesel from catalytic diesel, comprising the following steps: (1) mixing high-aromatic catalytic diesel with circulating hydrogen and entering a hydrorefining reaction zone I for reaction; (2) mixing the generated oil obtained in step (1) with circulating hydrogen and entering a hydrorefining reaction zone II for reaction, wherein the reaction temperature is 30-120°C higher than that in the hydrorefining reaction zone I; (3) cutting the generated oil obtained in step (2) into a light component and a heavy component; (4) mixing the light component obtained in step (3) with circulating hydrogen and entering a hydroreforming reaction zone, and separating the generated oil to obtain a gasoline fraction and a diesel fraction; (5) mixing the heavy component obtained in step (3) with circulating hydrogen and entering a hydroconversion reaction zone, and passing the generated oil through a separation system to obtain gas, gasoline, and diesel fractions; (6) mixing the gasoline obtained in step (4) with the gasoline obtained in step (5) to obtain a qualified gasoline product, and mixing the diesel obtained in step (4) with the diesel obtained in step (5) to obtain a qualified diesel product. This method can produce high-quality fuel oil products. Compared with other technologies, it has the characteristics of low chemical hydrogen consumption and flexible product structure adjustment.

[0005] CN201711118979.2 discloses a method for catalytic diesel hydroconversion, comprising the following steps: (1) mixing high aromatic catalytic diesel with circulating hydrogen and entering hydrorefining reaction zone I for reaction; (2) mixing the product oil obtained in step (1) with circulating hydrogen and entering hydrorefining reaction zone II for further reaction, wherein the reaction temperature is 30-120°C higher than that in hydrorefining reaction zone I, and the liquid hourly volume space velocity is 0.2-1.5h-1 lower than that in hydrorefining reaction zone I; (3) mixing the product oil obtained in step (2) with circulating hydrogen and entering hydrocracking reaction zone for hydrocarbon hydroconversion reaction; (4) the product oil obtained in step (3) is separated and fractionated in a system to obtain gas, light naphtha, heavy naphtha, and diesel fractions, with part of the diesel recycled back to hydrorefining reaction zone II, and part of the diesel discharged from the device. The catalytic diesel hydroconversion method provided by the method can effectively increase the production of aromatics.

[0006] CN201811264072.1 The present invention discloses a method for producing high-quality gasoline by catalytic diesel hydroconversion, comprising the following steps: (1) mixing high-aromatic catalytic diesel with circulating hydrogen and entering a hydrorefining reaction zone for reaction, wherein the hydrorefining reaction zone is provided with at least two catalyst beds, and the sulfidation degree of the catalyst tends to decrease along the logistics direction; (2) the generated oil obtained in step (1) enters a hydrocracking reaction zone and contacts with at least two sulfided hydrocracking catalysts to carry out a ring-opening conversion reaction of polycyclic aromatic hydrocarbons; (3) the generated oil obtained in step (2) passes through a separation system to obtain gas, gasoline, and diesel fractions. The method solves the problem of a long initial adjustment period in the production process and a long-term low octane number of the main target product, the gasoline fraction.

[0007] CN201611045476.2 discloses a catalytic diesel processing method. The catalytic diesel feedstock is divided into a light component and a heavy component; the light component undergoes hydrorefining and hydro-reforming reactions to produce gasoline and diesel components; the heavy component undergoes hydrorefining and hydroconversion to produce gasoline and diesel components; the two gasoline and diesel components are mixed to produce a gasoline product, and the two diesel components are mixed to produce a diesel product. Through rational separation and processing, this method allows for selective processing of different feedstock types, thereby enabling the rational use of low-quality catalytically cracked diesel to produce qualified gasoline and diesel products.

[0008] CN201310540464.7 discloses a method for hydroconversion of catalytically cracked diesel. After mixing catalytic diesel with hydrogen, it first enters a hydrorefining reactor for a hydrorefining reaction. The effluent from the hydrorefining reaction then enters the hydrocracking reactor, where it undergoes a contact reaction with a graded catalyst bed within the reactor. The hydrocracking reactor contains at least two beds of cracking catalyst, and the hydrogenation activity of the hydrocracking catalyst decreases with the flow of the reactants. The hydrocracking effluent is then separated and fractionated to produce naphtha and diesel. This method ensures diesel hydrocracking efficiency while reducing over-hydrogenation and secondary cracking of the cracked naphtha, lowering chemical hydrogen consumption and thereby increasing the octane number and liquid yield of the naphtha.

[0009] CN201811264066.6 discloses a method for maximizing the production of aromatics by catalytic diesel hydroconversion, comprising the following steps: (1) mixing high-aromatic catalytic diesel with circulating hydrogen and entering a hydrofining reaction zone for reaction, wherein the hydrofining reaction zone is provided with at least two catalyst beds, and the sulfidation degree of the catalyst tends to decrease along the direction of the flow; (2) the generated oil obtained in step (1) enters a hydrocracking reaction zone and contacts at least two sulfided hydrocracking catalysts to carry out a ring-opening conversion reaction of polycyclic aromatic hydrocarbons; (3) the generated oil obtained in step (2) is passed through a separation system to obtain gas, gasoline, and diesel fractions, and the diesel fraction is entirely recycled to the hydrofining reaction zone; (4) the naphtha obtained in step (3) enters an aromatics extraction unit and is extracted with a solvent to obtain a BTX product. This method balances the initial activity of the catalyst by using hydrofining catalysts with different sulfidation degrees in a graded manner, thereby solving the problem of a long initial adjustment period and a long-term low octane number of the gasoline fraction, the main target product, during the application of the technology.

[0010] In the prior art, the catalytic diesel hydroconversion process generally suffers from the problem of low BTX product yield. Summary of the Invention

[0011] Through in-depth research, the inventors discovered that the catalytic diesel hydroconversion process first involves hydrogenation saturation of polycyclic aromatic hydrocarbons (PAHs), followed by hydrocracking. During the hydrocracking reaction, PAHs, due to their high molecular polarity, preferentially adsorb on the catalyst's acidic centers for reaction. However, the alkylbenzenes in the catalytic diesel have low molecular polarity, making effective conversion difficult. To address the shortcomings of the prior art, the present invention provides a hydrogenation method for producing BTX by hydrogenating catalytically cracked diesel. This method can effectively increase the BTX yield in the hydrogenated product while reducing aromatic losses during the hydrogenation process.

[0012] A method for producing BTX by hydrogenating catalytically cracked diesel, comprising the following steps:

[0013] (1) Catalytic cracking diesel enters the hydrogenation pretreatment reaction zone, and the hydrogenation pretreatment reaction zone is sequentially filled with catalyst bed A and catalyst bed B along the flow direction. The catalyst loaded in the catalyst bed A is a hydrorefining catalyst, and the catalyst loaded in the catalyst bed B contains an acidic cracking component (such as beta and / or Y molecular sieve), a hydrogenation active metal component, and a ZSM-5 molecular sieve;

[0014] (2) The hydropretreatment oil obtained in step (1) enters the hydroconversion reaction zone for hydrocracking reaction, and the hydroconversion reaction zone is loaded with a hydrocracking catalyst;

[0015] (3) The oil generated by hydrogenation conversion in step (2) enters the separation system for gas-liquid separation. The separated gas can be recycled as supplementary hydrogen. The liquid product enters the distillation tower for separation. The light naphtha, heavy naphtha and tail oil are fractionated in the distillation tower. The heavy naphtha is subjected to aromatic extraction to obtain BTX.

[0016] In step (1) of the above method, the initial boiling point of the catalytic cracking diesel is generally 60°C to 220°C, preferably 170°C to 210°C; the density is generally 0.90 g / cm -3 ~0.99 g / cm -3 ; The nitrogen content is generally 0.03m%~0.2m%; the aromatic hydrocarbon content is generally 50m%~90m%, preferably 65m%~85m%.

[0017] In step (1) of the above method, the hydrorefining catalyst comprises a support and a hydrogenation-active metal; wherein the support is an inorganic refractory oxide, generally selected from one or more of alumina, amorphous silica-alumina, silica, or titanium oxide; and the hydrogenation-active metal comprises a Group VIB and / or Group VIII metal component. In the hydrorefining catalyst, the Group VIB metal is selected from tungsten and / or molybdenum, and its content in the catalyst is 5% to 30% by weight of the oxide, preferably 10% to 20%. The Group VIII metal is selected from nickel and / or cobalt, and its content in the catalyst is 1% to 6% by weight of the oxide, preferably 1.5% to 5%.

[0018] In step (1) of the above method, the catalyst loaded in the catalyst bed B contains a hydrogenation active metal component and a carrier, and the carrier is composed of ZSM-5 molecular sieve, beta and / or Y molecular sieve, and alumina.

[0019] In step (1) of the above method, the catalyst loaded in the catalyst bed B is based on the weight of its carrier, and the mass content of ZSM-5 molecular sieve is 20% to 80%, preferably 40% to 60%, the mass content of acidic cracking components (such as beta and / or Y molecular sieve) is 5% to 15%, preferably 8% to 12%, and the balance is alumina.

[0020] In step (1) of the above method, the hydrogenation active metal components in the catalyst loaded in the catalyst bed B are metals of Group VIB and Group VIII, the Group VIB metals are preferably molybdenum and / or tungsten, and the Group VIII metals are preferably cobalt and / or nickel.

[0021] In step (1) of the above method, the hydrogenation active metal component in the catalyst loaded in the catalyst bed B is, based on the weight of the catalyst loaded in the catalyst bed B, a content of Group VIB metal calculated as oxide of 5.0% to 15.0%, and a content of Group VIII metal calculated as oxide of 2.0% to 5.0%.

[0022] In step (1) of the above method, the specific surface area of ​​the catalyst loaded in the catalyst bed B is 200~400m 2 / g, pore volume 0.25~0.45mL / g.

[0023] A method for preparing a catalyst loaded with an unrestricted B catalyst bed comprises preparing a carrier and loading a hydrogenation-active metal component. The carrier preparation process is as follows: ZSM-5 molecular sieve, Beta molecular sieve and / or Y molecular sieve, and alumina are mechanically mixed, shaped, and then dried and calcined to prepare the catalyst carrier. The drying and calcining can be carried out under conventional conditions, generally drying at 100°C to 150°C for 1 to 12 hours, and then calcining at 450°C to 550°C for 2.5 to 6.0 hours.

[0024] In the above-mentioned non-limiting method for preparing the catalyst loaded with the catalyst bed B, the hydrogenation-active metal component can be loaded by conventional methods, such as kneading, impregnation, etc. The hydrogenation-active metal component is a Group VIB and / or Group VIII metal component, for example, one or more of Co, Ni, Mo, and W.

[0025] In the above-mentioned non-limiting method for preparing a catalyst loaded with a catalyst bed B, the hydrogenation-active metal component is loaded by impregnation, followed by drying and calcination to obtain the catalyst loaded with the catalyst bed B. The impregnation method can be saturation impregnation, excess impregnation, or complex impregnation, i.e., the support is impregnated with a solution containing the desired active component. The impregnated support is then dried at 100°C to 150°C for 1 to 12 hours and calcined at 450°C to 550°C for 2.5 to 6.0 hours.

[0026] In step (1) of the above method, the reaction conditions of the hydrogenation pretreatment reaction zone are generally as follows: reaction pressure 3.0-15.0 MPa, preferably 5.0-12.0 MPa; liquid hourly volume space velocity 0.1-15.0 h -1 , preferably 0.2 to 3.0 hours -1 .

[0027] In step (1) of the above method, the average reaction temperature of catalyst bed A is 350°C to 390°C, preferably 360°C to 380°C; the average reaction temperature of catalyst bed B is 10°C to 60°C higher than the average reaction temperature of catalyst bed A, preferably 20°C to 50°C higher.

[0028] In step (1) of the above method, the volume ratio of the catalyst loaded in the catalyst bed B to the catalyst loaded in the catalyst bed A is 1:2 to 1:10, preferably 1:4 to 1:8.

[0029] In step (2) of the above method, the hydrocracking catalyst loaded in the hydroconversion reaction zone generally comprises a cracking component, a hydrogenation component, and a binder. The hydrocracking catalyst can be a commercially available product or prepared according to existing techniques. The cracking component is a Y-type molecular sieve, and the binder is generally alumina or silica. The hydrogenation component is a Group VIB and Group VIII metal component such as Co, Ni, Mo, W, etc. Based on the weight of the hydrocracking catalyst, the mass content of the hydrogenation component as oxide is generally 3% to 20% by weight, and the mass content of the cracking component is 30% to 80% by weight, preferably 40% to 70% by weight.

[0030] In step (2) of the above method, the reaction conditions of the hydroconversion reaction zone are generally as follows: reaction pressure 3.0-15.0 MPa, preferably 5.0-12.0 MPa; liquid hourly volume space velocity 0.1-15.0 h -1, preferably 0.2 to 3.0 hours -1 The average reaction temperature in the hydroconversion reaction zone is 300°C to 450°C, preferably 380°C to 420°C.

[0031] In step (3) of the above method, the aromatics extraction can be carried out using existing technologies. Conventional aromatics extraction methods mainly include liquid-liquid extraction or extractive distillation. The present invention uses liquid-liquid extraction, and the extraction solvent is one or more of diethylene glycol (ethylene glycol), tetraethylene glycol, cyclopentane, N-methylpyrrolidone, and dimethyl sulfoxide. The extraction temperature is 20°C to 200°C, preferably 50°C to 150°C; the mass ratio of solvent to heavy naphtha is 1:1 to 8:1, preferably 3:1 to 5:1; and the pressure is 0 MPa to 2 MPa, preferably 0.1 to 0.5 MPa.

[0032] Compared with the prior art, the present invention loads catalyst B in a graded manner at the bottom of a hydrorefining reactor, a high-temperature zone during the hydroconversion reaction. The catalyst contains beta and / or Y molecular sieves, a hydrogenation-active metal component, and a ZSM-5 molecular sieve. This catalyst can achieve the cleavage of aromatic side chains and the retention of aromatic rings, effectively converting alkylbenzenes in catalytic diesel and improving the BTX yield in the product. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] Figure 1 The figure is a schematic flow chart of the principle of a method for producing BTX by hydrogenating catalytic cracking diesel adopted in an embodiment of the present invention.

[0034] Among them, 1 is catalytic diesel, 2 is hydrogen, 3 is hydrogenation pretreatment reaction zone, 4 is hydrogenation pretreatment generated oil, 5 is hydrogenation conversion reaction zone, 6 is hydrogenation conversion generated oil, 7 is separator, 8 is the separated gas phase component, 9 is the separated liquid phase component, 10 is distillation tower, 11 is gas, 12 is light naphtha, 13 is heavy naphtha, 14 is tail oil, 15 is aromatic extraction zone, 16 is BTX component, and 17 is raffinate oil. DETAILED DESCRIPTION

[0035] The effects and benefits of the present invention are further illustrated below by way of examples. However, the following examples do not limit the method of the present invention. Unless otherwise specified, % in this application are percentages by mass.

[0036] Catalytic diesel 1 is mixed with hydrogen 2 and enters into hydrogenation pretreatment reaction zone 3. Oil 4 generated by hydrogenation pretreatment enters into hydrogenation conversion reaction zone 5. Oil 6 generated by hydrogenation conversion reaction zone enters into separator 7 for separation and the obtained gas phase 8 is recycled. Liquid phase 9 enters into fractionation tower 10 for separation and obtains gas 11, light naphtha 12, heavy naphtha 13 and tail oil 14. Heavy naphtha 13 enters into aromatic extraction zone 15 for separation and obtains BTX component 16 and raffinate 17.

[0037] In the embodiment of the present invention, the hydrorefining catalyst used in the hydropretreatment reaction zone is FF-66, which has a composition of 22wt% MoO3, 5wt% NiO, and the balance is alumina; the hydrocracking catalyst used in the hydroconversion reaction zone is FC-70A, which has a composition of 12wt% MoO3, 3wt% NiO, 60wt% Y-type molecular sieve, and the balance is alumina; the manufacturers of the catalysts are all Sinopec Catalyst Co., Ltd. The B catalyst used in the hydropretreatment reaction zone is the DCP-1 catalyst prepared by the method of the present invention, which has a composition of 10wt% MoO3, 3wt% NiO, 50wt% ZSM-5 molecular sieve, 10wt% Beta molecular sieve, and the balance is alumina, with a specific surface area of ​​300m 2 / g, pore volume 0.35mL / g.

[0038] In the examples and comparative examples of the present invention, sulfolane was used as the extraction solvent, and the process conditions were as follows: extraction temperature 80° C.; solvent: heavy naphtha mass ratio 4:1; pressure 0.3 MPa.

[0039] Table 1 shows the properties of the feedstock oil, Table 2 shows the operating conditions and reaction results of the embodiment, and Table 3 shows the reaction conditions and reaction results of the comparative example.

[0040] Table 1

[0041]

[0042] Table 2

[0043]

[0044] Comparative Example 1

[0045] The same process flow as in the embodiment was adopted. The catalytic diesel first entered the hydrogenation pretreatment reaction zone for hydrogenation saturation reaction. The hydrogenation pretreatment zone was completely filled with FF-66 hydrorefining catalyst. The oil generated by the hydrogenation pretreatment entered the hydroconversion reaction zone for hydrocracking reaction. The hydrocracking reaction zone was filled with FC-70A hydrocracking catalyst.

[0046] Table 3

[0047]

[0048] It can be seen from the above examples that the catalytic diesel oil production method of the present invention can effectively increase the BTX yield in the product.

Claims

1. A method for producing BTX by hydrogenating catalytic cracking diesel, characterized in that: The method comprises the following steps: (1) Catalytic cracking diesel enters the hydrogenation pretreatment reaction zone, and the hydrogenation pretreatment reaction zone is sequentially filled with catalyst bed A and catalyst bed B along the direction of the flow. The catalyst loaded in the catalyst bed A is a hydrorefining catalyst; (2) The hydropretreatment oil obtained in step (1) enters the hydroconversion reaction zone for hydrocracking reaction, and the hydroconversion reaction zone is loaded with a hydrocracking catalyst; (3) The oil generated by hydrogenation conversion in step (2) enters the separation system for gas-liquid separation. The separated gas is recycled as supplementary hydrogen. The liquid product enters the fractionation tower for separation. The fractionation tower is fractionated to obtain light naphtha, heavy naphtha and tail oil. The heavy naphtha is subjected to aromatics extraction to obtain BTX; The catalyst loaded in the catalyst bed B contains a hydrogenation active metal component and a carrier, wherein the carrier is composed of a ZSM-5 molecular sieve, an acidic cracking component, and alumina; based on the weight of the carrier, the mass content of the ZSM-5 molecular sieve is 20% to 80%, the mass content of the acidic cracking component is 5% to 15%, and the balance is alumina; wherein the acidic cracking component is beta and / or Y molecular sieve; In step (1), the hydrogenation active metal components in the catalyst loaded in the catalyst bed B are metals of Group VIB and Group VIII; In step (1), the catalyst loaded in the catalyst bed B contains molybdenum and / or tungsten as the Group VIB metal, and cobalt and / or nickel as the Group VIII metal; In step (1), the hydrogenation active metal component in the catalyst loaded in the catalyst bed B is based on the weight of the catalyst loaded in the catalyst bed B, and the content of the Group VIB metal calculated as oxide is 5.0% to 15.0%, and the content of the Group VIII metal calculated as oxide is 2.0% to 5.0%; In step (1), the specific surface area of ​​the catalyst loaded in the catalyst bed B is 200~400m 2 / g, pore volume 0.25~0.45mL / g; In step (1), the average reaction temperature of catalyst bed A is 350°C to 390°C; the average reaction temperature of catalyst bed B is 10°C to 60°C higher than the average reaction temperature of catalyst bed A.

2. The method according to claim 1, wherein: The initial boiling point of the catalytic cracking diesel is 60°C to 220°C; the density is 0.90g / cm -3 ~0.99 g / cm -3 ; Nitrogen content is 0.03m%~0.2m%; Aromatic hydrocarbon content is 50m%~90m%.

3. The method according to claim 2, wherein: The catalytic cracking diesel has an initial boiling point of 170° C. to 210° C. and an aromatics content of 65% to 85% by mass.

4. The method according to claim 1, wherein: In step (1), the hydrorefining catalyst comprises a carrier and a hydrogenation active metal; the carrier is an inorganic refractory oxide; and the hydrogenation active metal comprises a Group VIB and / or Group VIII metal component.

5. The method according to claim 1, wherein: In step (1), the catalyst loaded in the catalyst bed B is based on the weight of its carrier, with 40% to 60% of ZSM-5 molecular sieve, 8% to 12% by mass of acidic cracking component, and the balance being alumina.

6. The method according to claim 1, wherein: In step (1), the reaction conditions of the hydrogenation pretreatment reaction zone are: reaction pressure 3.0-15.0 MPa; liquid hourly volume space velocity 0.1-15.0 h -1 .

7. The method according to claim 6, characterized in that: In step (1), the reaction conditions of the hydrogenation pretreatment reaction zone are: reaction pressure 5.0-12.0 MPa; liquid hourly volume space velocity 0.2-3.0 h -1 .

8. The method according to claim 1, wherein: In step (1), the average reaction temperature of catalyst bed A is 360°C to 380°C; the average reaction temperature of catalyst bed B is 20°C to 50°C higher than the average reaction temperature of catalyst bed A.

9. The method according to claim 1, wherein: In step (1), the volume ratio of the catalyst loaded in the B catalyst bed to the catalyst loaded in the A catalyst bed is 1:2 to 1:

10.

10. The method according to claim 9, characterized in that: In step (1), the volume ratio of the catalyst loaded in the B catalyst bed to the catalyst loaded in the A catalyst bed is 1:4 to 1:

8.

11. The method according to claim 1, wherein: In step (2), the reaction conditions of the hydroconversion reaction zone are: reaction pressure 3.0-15.0 MPa; liquid hourly volume space velocity 0.1-15.0 h -1 The average reaction temperature in the hydroconversion reaction zone is 300℃~450℃.

12. The method according to claim 11, wherein: In step (2), the reaction conditions of the hydroconversion reaction zone are: reaction pressure 5.0-12.0 MPa; liquid hourly volume space velocity 0.2-3.0 h -1 The average reaction temperature in the hydroconversion reaction zone is 380℃~420℃.

Images