An aviation kerosene, a preparation method thereof, and a system for producing aviation kerosene

Abstract

The application discloses aviation kerosene and a preparation method and system thereof. The preparation method comprises the following steps: distilling coal-derived oil to obtain a first light oil fraction, a first aviation kerosene fraction, a first diesel oil fraction and a heavy oil fraction; performing hydrocracking treatment on the heavy oil fraction to obtain a second light oil fraction, a second aviation kerosene fraction and a second diesel oil fraction; mixing the first diesel oil fraction and the second diesel oil fraction and performing hydro-upgrading treatment to obtain a third light oil fraction and a third aviation kerosene fraction; mixing the first light oil fraction, the second light oil fraction and the third light oil fraction and performing alkylation reaction and hydrogenation reaction to obtain a fourth aviation kerosene fraction; and mixing the first aviation kerosene fraction, the second aviation kerosene fraction, the third aviation kerosene fraction and the fourth aviation kerosene fraction and performing hydrofining treatment to obtain aviation kerosene. The method realizes maximization of production of aviation kerosene from coal-derived oil, improves the aviation kerosene yield and reduces the production cost.

Description

Technical Field

[0001] This invention relates to the field of coal chemical industry, and more specifically, to an aviation kerosene, its preparation method, and a system for producing aviation kerosene. Background Technology

[0002] Liquid fuels are the power source for aircraft, and fuel energy determines flight performance. The low energy content of conventional liquid fuels is a major problem restricting the performance of existing aircraft and the development of new aircraft. The energy of a fuel (energy = density * calorific value) depends on its molecular structure. Petroleum-refined fuels are mainly composed of chain and monocyclic structures with lower density and volumetric calorific value, while Fischer-Tropsch synthesis fuels have an even higher content of chain structures. Coal-derived oils are rich in polycyclic aromatic hydrocarbons and have a unique molecular structure, fully retaining the high-density polycyclic structure unique to coal. They are a high-quality raw material for producing high-density, high-heat-sinking, and high-heat-stability aviation kerosene.

[0003] The preparation of aerospace fuel from coal-derived oil generally involves processes such as phenol removal, hydrogenation and impurity removal, hydrogenation saturation, and fractionation to obtain a mixture of cycloalkanes with a boiling range of 150–300℃. Current methods for preparing aviation kerosene from coal-derived oil result in low fraction yields and poor product performance, such as low volumetric calorific value, carbon buildup, and impurities, highlighting the need for improved economic efficiency. Summary of the Invention

[0004] This invention is based on the inventor's discovery and understanding of the following facts and problems: current methods for preparing aviation kerosene from coal-derived oil have low jet kerosene fraction yields, poor product performance, and need to be improved in terms of economic efficiency.

[0005] This invention aims to at least partially solve one of the technical problems in related technologies. To this end, embodiments of this invention propose an aviation kerosene and its preparation method, as well as a system for producing aviation kerosene, which maximizes the production of aviation kerosene from coal-derived oil, increases aviation kerosene yield, and achieves high-value utilization of coal-derived oil while reducing production costs.

[0006] This invention provides a method for preparing aviation kerosene, comprising the following steps:

[0007] (1) Distill the coal-derived oil to obtain a first light oil fraction, a first aviation kerosene fraction, a first diesel oil fraction and a heavy oil fraction;

[0008] (2) The heavy oil fraction is subjected to hydrocracking to obtain a second light oil fraction, a second aviation kerosene fraction, and a second diesel fraction;

[0009] (3) The first diesel fraction and the second diesel fraction are mixed and subjected to hydrogenation and upgrading treatment to obtain the third light oil fraction and the third aviation kerosene fraction.

[0010] (4) The first light oil fraction, the second light oil fraction and the third light oil fraction are mixed and subjected to alkylation and hydrogenation reactions to obtain the fourth jet fuel fraction;

[0011] (5) The first aviation kerosene fraction, the second aviation kerosene fraction, the third aviation kerosene fraction and the fourth aviation kerosene fraction are mixed and subjected to hydrorefining treatment to obtain aviation kerosene.

[0012] The advantages and technical effects of the aviation kerosene preparation method of this invention are as follows: Coal-derived oil is distilled to obtain a first light oil fraction, a first aviation kerosene fraction, a first diesel fraction, and a heavy oil fraction. The heavy oil fraction undergoes hydrocracking to further obtain light oil and aviation kerosene fractions, maximizing the conversion of the heavy oil fraction into aviation kerosene. The diesel fraction undergoes hydrotreating to further obtain light oil and aviation kerosene fractions. The mixed light oil fraction undergoes alkylation and hydrogenation reactions, efficiently performing hydrodeoxygenation under hydrogen conditions, converting the phenolic substances abundant in the mixed light oil fraction into aromatics or alkylbenzenes. Aromatics and alkylbenzenes are components of the target product, aviation kerosene, maximizing the production of aviation kerosene. Simultaneously, the mixed light oil fraction is converted into aviation kerosene fraction through alkylation and carbon enrichment reactions, improving the utilization rate of coal-derived oil and increasing the yield of aviation kerosene components. Hydrorefining of jet fuel fractions significantly removes heteroatoms such as sulfur and nitrogen, producing high-quality, high-performance jet fuel. The jet fuel preparation method maximizes the conversion of heavy oil fractions into jet fuel, while alkylating light oil fractions to increase carbon content and produce jet fuel. This improves the conversion efficiency of coal-derived oil to jet fuel, maximizing the production of jet fuel from coal-derived oil, increasing jet fuel yield and fuel performance. The preparation method is simple and economical, achieving high-value utilization of coal-derived oil while reducing production costs.

[0013] In some embodiments, the coal-derived oil includes at least one of low-temperature coal tar, medium-low temperature coal tar, medium-temperature coal tar, high-temperature coal tar, and shale oil;

[0014] And / or, the cut temperature of the first light oil fraction, the second light oil fraction, or the third light oil fraction is independently 170-230°C;

[0015] And / or, the cutting temperature of the first jet fuel fraction, the second jet fuel fraction, the third jet fuel fraction, or the fourth jet fuel fraction is independently 280-300℃;

[0016] And / or, the cutting temperature of the first diesel fraction or the second diesel fraction is independently 340-370°C.

[0017] In some embodiments, in step (2), the hydrocracking process is carried out using a slurry bed reactor;

[0018] And / or, the hydrocracking treatment is carried out at a reaction temperature of 320-470℃, a reaction pressure of 8-30MPa, and a volume hourly space velocity (VHSV) of 0.2-2.0h for the heavy oil fraction. -1 The hydrogen-to-oil volume ratio is 500-2000;

[0019] And / or, the hydrocracking process employs a hydrocracking catalyst; the active component of the hydrocracking catalyst includes at least one of molybdenum, nickel, or iron; optionally, the particle diameter of the hydrocracking catalyst is 0.5-50 μm; optionally, the weight ratio of the active component of the hydrocracking catalyst to the heavy oil fraction is 0.2-5:100.

[0020] In some embodiments, in step (3), the hydrogenation and upgrading process is carried out using a fixed-bed reactor;

[0021] And / or, the hydrotreating process is carried out at a reaction temperature of 300-450℃, a reaction pressure of 5-25MPa, and a volume hourly space velocity (VHSV) of 0.2-2.0h for the mixed diesel fraction. -1 The hydrogen-to-oil volume ratio is 500-2000;

[0022] And / or, the hydrotreating process employs a hydrotreating catalyst; the hydrotreating catalyst comprises an active component and a support; the active component comprises at least one of group VIB and group VIII metal elements; optionally, the active component in the hydrotreating catalyst has a weight content of 0.2% to 20% based on the metal element; optionally, the support comprises at least one of inorganic oxides or molecular sieves.

[0023] In some embodiments, in step (4), the first light oil fraction, the second light oil fraction, and the third light oil fraction are mixed and subjected to alkylation and hydrogenation reactions with methanol and hydrogen to obtain the fourth jet fuel fraction; optionally, the molar ratio of methanol to the mixed light oil fraction is (0.5-2):3.

[0024] And / or, the alkylation and hydrogenation reactions are carried out in a fixed-bed reactor;

[0025] And / or, the alkylation and hydrogenation reactions are carried out at temperatures of 200–460°C, and the volume hourly space velocity (VHSV) of the mixed light oil fraction is 5–15 h⁻¹. -1 The reaction pressure is 4-20 MPa, and the hydrogen-to-oil volume ratio is 5-20.

[0026] In some embodiments, in step (4), the hydrogenation reaction is carried out using a hydrogenation catalyst; the hydrogenation catalyst includes an active component and a support; the active component of the hydrogenation catalyst includes Cu element; optionally, the active component in the hydrogenation catalyst has a weight content of 0.1% to 8% based on the metal element; optionally, the support includes at least one of inorganic oxides or molecular sieves.

[0027] In some embodiments, in step (4), the alkylation reaction is carried out using an alkylation catalyst; the alkylation catalyst includes an active component and a support; the active component includes at least one of Mo and Ni elements; optionally, the active component in the alkylation catalyst has a weight content of 0.1% to 5% based on the metal element; optionally, the support includes at least one of molecular sieves; optionally, the molecular sieve includes at least one of ZSM-11 or MCM-22.

[0028] In some embodiments, in step (5), the hydrorefining process is carried out using a fixed-bed reactor;

[0029] And / or, the reaction temperature for the hydrorefining treatment is 260-400℃, the reaction pressure is 6-17MPa, and the volume hourly space velocity (VHSV) of the mixed jet fuel fraction is 0.2-2.0 h⁻¹. -1 The hydrogen-to-oil ratio is 500-2000;

[0030] And / or, the hydrorefining process employs a hydrorefining catalyst; the hydrorefining catalyst comprises an active component and a support; the active component comprises at least one of group VIB and group VIII metal elements; optionally, the active component in the hydrorefining catalyst has a weight content of 0.1% to 8% based on the metal element; optionally, the support comprises at least one of inorganic oxides or molecular sieves.

[0031] This invention provides an aviation kerosene prepared by the method described in this invention. This invention achieves high yield and excellent fuel performance of the aviation kerosene, realizing the high-value utilization of coal-derived oil while reducing the production cost of aviation kerosene.

[0032] This invention provides a system for producing aviation kerosene, comprising:

[0033] The distillation separation unit is provided with a coal-derived oil inlet, a first light oil fraction outlet, a first aviation kerosene fraction outlet, a first diesel oil fraction outlet, and a heavy oil fraction outlet;

[0034] The hydrocracking unit is provided with a heavy oil fraction inlet, a second light oil fraction outlet, a second jet fuel fraction outlet, and a second diesel fraction outlet, wherein the heavy oil fraction inlet is connected to the heavy oil fraction outlet.

[0035] The hydrotreating unit is provided with a first diesel fraction inlet, a second diesel fraction inlet, a third light oil fraction outlet and a third aviation kerosene fraction outlet. The first diesel fraction inlet is connected to the first diesel fraction outlet, and the second diesel fraction inlet is connected to the second diesel fraction outlet.

[0036] An alkylation and hydrogenation unit is provided with a first light oil fraction inlet, a second light oil fraction inlet, a third light oil fraction inlet, and a fourth jet fuel fraction outlet. The first light oil fraction inlet is connected to the first light oil fraction outlet, the second light oil fraction inlet is connected to the second light oil fraction outlet, and the third light oil fraction inlet is connected to the third light oil fraction outlet.

[0037] The hydrorefining unit is provided with a first aviation kerosene inlet, a second aviation kerosene inlet, a third aviation kerosene inlet, a fourth aviation kerosene inlet, and an aviation kerosene outlet. The first aviation kerosene inlet is connected to the first aviation kerosene outlet, the second aviation kerosene inlet is connected to the second aviation kerosene outlet, the third aviation kerosene inlet is connected to the third aviation kerosene outlet, and the fourth aviation kerosene inlet is connected to the fourth aviation kerosene outlet.

[0038] In this embodiment of the invention, the system for producing aviation kerosene is used to implement the aviation kerosene preparation method described in this embodiment of the invention or to prepare the aviation kerosene described in this embodiment of the invention. The system for producing aviation kerosene can improve the conversion efficiency of coal-derived oil to aviation kerosene, maximize the production of aviation kerosene from coal-derived oil, improve the yield and fuel performance of aviation kerosene, and realize the high-value utilization of coal-derived oil while reducing production costs. Attached Figure Description

[0039] Figure 1 This is a system for producing aviation kerosene according to an embodiment of the present invention.

[0040] Figure label:

[0041] Distillation and separation unit 100, hydrocracking unit 200, hydrotreating unit 300, alkylation and hydrotreating unit 400, hydrorefining unit 500;

[0042] Coal-derived oil 1, first light oil fraction 2, first aviation kerosene fraction 3, first diesel fraction 4, heavy oil fraction 5, second light oil fraction 6, second aviation kerosene fraction 7, second diesel fraction 8, third light oil fraction 9, third aviation kerosene fraction 10, methanol 11, fourth aviation kerosene fraction 12, gaseous products 13, aviation kerosene 14. Detailed Implementation

[0043] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0044] An embodiment of the present invention provides a method for preparing aviation kerosene, comprising the following steps:

[0045] (1) Distill the coal-derived oil to obtain a first light oil fraction, a first aviation kerosene fraction, a first diesel oil fraction and a heavy oil fraction;

[0046] (2) The heavy oil fraction is subjected to hydrocracking to obtain a second light oil fraction, a second aviation kerosene fraction, and a second diesel fraction;

[0047] (3) The first diesel fraction and the second diesel fraction are mixed and subjected to hydrogenation and upgrading treatment to obtain the third light oil fraction and the third aviation kerosene fraction.

[0048] (4) The first light oil fraction, the second light oil fraction and the third light oil fraction are mixed and subjected to alkylation and hydrogenation reactions to obtain the fourth jet fuel fraction;

[0049] (5) The first aviation kerosene fraction, the second aviation kerosene fraction, the third aviation kerosene fraction and the fourth aviation kerosene fraction are mixed and subjected to hydrorefining treatment to obtain aviation kerosene.

[0050] The method for preparing aviation kerosene according to this invention involves distilling coal-derived oil to obtain a first light oil fraction, a first aviation kerosene fraction, a first diesel fraction, and a heavy oil fraction. The heavy oil fraction undergoes hydrocracking to further obtain light oil and aviation kerosene fractions, maximizing the conversion of the heavy oil fraction into aviation kerosene. The diesel fraction undergoes hydrotreating to further obtain light oil and aviation kerosene fractions. The mixed light oil fraction undergoes alkylation and hydrogenation reactions, with efficient hydrodeoxygenation under hydrogen conditions, converting the phenolic substances abundant in the mixed light oil fraction into aromatics or alkylbenzenes. Aromatics and alkylbenzenes are components of the target product, aviation kerosene, maximizing aviation kerosene production. Simultaneously, the mixed light oil fraction undergoes alkylation and carbon enrichment reactions to convert the light oil fraction into aviation kerosene fraction, improving the utilization rate of coal-derived oil and increasing the yield of aviation kerosene components. Hydrorefining of the mixed aviation kerosene fractions significantly removes heteroatoms such as S and N, producing high-quality, high-performance aviation kerosene. The method for preparing aviation kerosene maximizes the conversion of heavy oil fractions into aviation kerosene and achieves carbon enrichment of light oil fractions through alkylation reaction to produce aviation kerosene. This method can improve the conversion efficiency of coal-derived oil to aviation kerosene, maximize the production of aviation kerosene from coal-derived oil, improve the yield and fuel performance of aviation kerosene, and is simple and economical. It realizes the high-value utilization of coal-derived oil while reducing production costs.

[0051] In some embodiments, in step (1), the coal-derived oil includes at least one of low-temperature coal tar, medium-low-temperature coal tar, medium-temperature coal tar, high-temperature coal tar, and shale oil; wherein, the low-temperature coal tar refers to coal tar obtained at a final distillation temperature of 500–700°C, the medium-low-temperature coal tar refers to coal tar obtained at a final distillation temperature of 600–800°C, the medium-temperature coal tar refers to coal tar obtained at a final distillation temperature of 800–1000°C, and the high-temperature coal tar refers to coal tar obtained at a final distillation temperature above 1000°C. In these embodiments, the high-value utilization of various coal-derived oils can be achieved, maximizing the production of aviation kerosene.

[0052] In some embodiments, the cut temperature of the first light oil fraction, the second light oil fraction, or the third light oil fraction is independently 170-230°C, that is, the light oil fraction is a fraction with a cut temperature of no more than 170-230°C. Specifically, the cut temperature can be 170°C, 180°C, 190°C, 200°C, 210°C, 220°C, or 230°C.

[0053] And / or, the cutting temperatures of the first aviation kerosene fraction, the second aviation kerosene fraction, the third aviation kerosene fraction, the fourth aviation kerosene fraction, and aviation kerosene are each independently 280-300℃. Specifically, the cutting temperatures can be 280℃, 290℃, and 300℃, that is, the aviation kerosene fraction is a fraction with a cutting temperature not lower than 170-230℃ and / or not higher than 280-300℃, or the aviation kerosene fraction is a fraction with a cutting temperature not lower than the light oil fraction and / or not higher than the aviation kerosene fraction cutting temperature; in a specific embodiment, the aviation kerosene fraction can be a fraction with a cutting temperature of 170-300℃;

[0054] And / or, the cut temperature of the first diesel fraction or the second diesel fraction is independently 340-370°C. Specifically, the cut temperature can be 340°C, 350°C, 360°C, or 370°C, that is, the diesel fraction is a fraction with a cut temperature not lower than 280-300°C and / or not higher than 340°C-370°C, or the diesel fraction is a fraction with a cut temperature not lower than the jet fuel fraction and / or not higher than the diesel fraction cut temperature.

[0055] And / or, the heavy oil fraction is a fraction with a cutting temperature of not less than 340℃-370℃. Specifically, the cutting temperature can be 340℃, 350℃, 360℃, or 370℃, that is, the heavy oil fraction is a fraction with a cutting temperature of not less than that of the diesel fraction.

[0056] In some embodiments, in step (2), the hydrocracking process employs a slurry bed reactor; optionally, the hydrocracking process employs two slurry bed reactors.

[0057] In some embodiments, in step (2), the heavy oil fraction undergoes slurry preparation, hydrocracking reaction and gas-liquid separation to obtain hydrogen-rich gas and liquid oil; the liquid oil is then distilled to obtain a second light oil fraction, a second jet fuel fraction and a second diesel fraction.

[0058] In some embodiments, in step (2), the reaction temperature of the hydrocracking treatment is 320-470°C, specifically, for example, 320°C, 400°C, 445°C, 450°C, 455°C, or 470°C; the reaction pressure is 8-30 MPa, specifically, for example, 8 MPa, 10 MPa, 16 MPa, 17 MPa, 20 MPa, or 30 MPa; and the volume hourly space velocity (VHSV) of the heavy oil fraction is 0.2-2.0 h⁻¹. -1 Specifically, for example, 0.2h -1 0.8h -1 1.0h -1 1.5h -1 2.0h -1The hydrogen-to-oil volume ratio is 500-2000, specifically, for example, 500, 1000, 1100, 1200, 1500, 2000.

[0059] In some embodiments, in step (2), the hydrocracking process employs a hydrocracking catalyst; the hydrocracking catalyst comprises an active component; the active component of the hydrocracking catalyst comprises at least one of molybdenum, nickel, or iron metal elements;

[0060] Optionally, the active component is a sulfide of a metal element; optionally, the hydrocracking catalyst is unsupported; optionally, the hydrocracking catalyst is a powdered particle containing a single metal active component or a composite multi-metal active component containing molybdenum, nickel, or iron; the particle diameter of the hydrocracking catalyst is 0.5-50 μm; the weight ratio of the active component of the hydrocracking catalyst to the heavy oil fraction is 0.2-5:100, specifically, for example, 0.2:100, 1:100, 2:100, 3:100, 4:100, 5:100.

[0061] In this embodiment of the invention, hydrocracking of heavy oil fractions can further yield light oil fractions and aviation kerosene fractions, thereby increasing the production of aviation kerosene from coal-derived oil and improving the aviation kerosene yield.

[0062] In some embodiments, in step (3), the hydrogenation and upgrading process is carried out using a fixed-bed reactor.

[0063] In some embodiments, in step (3), the first diesel fraction and the second diesel fraction are mixed and subjected to a hydrotreating reaction and gas-liquid separation to obtain hydrogen-rich gas and liquid oil; the liquid oil is then distilled to obtain a third light oil fraction and a third jet fuel fraction.

[0064] In some embodiments, in step (3), the reaction temperature of the hydrotreating process is 300-450℃, specifically, for example, 320℃, 345℃, 360℃, 370℃, 400℃, 450℃; the reaction pressure is 5-25MPa, specifically, for example, 5MPa, 12MPa, 13MPa, 15MPa, 20MPa, 25MPa; and the volume hourly space velocity (VHSV) of the mixed diesel fraction is 0.2-2.0 h⁻¹. -1 Specifically, for example, 0.2h -1 0.6h -1 0.8h -1 1.0h -1 1.5h -1 2.0h -1 The hydrogen-to-oil volume ratio is 500-2000, specifically, for example, 500, 1000, 1100, 1200, 1500, 2000.

[0065] In some embodiments, in step (3), the hydrotreating process employs a hydrotreating catalyst; the hydrotreating catalyst comprises an active component and a support; the active component comprises at least one of group VIB and group VIII metal elements;

[0066] Optionally, the active component includes at least one of the metal elements Ni, Mo, Co, and W; optionally, the active component is a sulfide of a metal element; optionally, the active component in the hydrotreating catalyst has a weight content of 0.2% to 20% based on the metal element, specifically, for example, 0.2%, 5%, 10%, 15%, or 20%; the support includes at least one of inorganic oxides or molecular sieves; optionally, the inorganic oxide includes at least one of alumina and silicon oxide.

[0067] In this embodiment of the invention, hydrotreating the diesel fraction can further yield light oil fraction and aviation kerosene fraction, thereby increasing the production of aviation kerosene from coal-derived oil and improving the aviation kerosene yield.

[0068] In some embodiments, in step (4), the first light oil fraction, the second light oil fraction, and the third light oil fraction are mixed and subjected to alkylation and hydrogenation reactions with methanol and hydrogen to obtain a fourth jet fuel fraction. Optionally, the molar ratio of methanol to the mixed light oil fraction is (0.5-2):3, specifically, for example, 0.5:3, 1:3, 2:3.

[0069] In this embodiment of the invention, the alkylation reaction adopts a hydrogenation process. In the presence of an alkylation catalyst, the mixed light oil fraction of coal-derived oil undergoes an alkylation reaction with methanol to generate aviation kerosene fraction oil at 170-300℃. The light oil fraction is carbonized and produced into aviation kerosene through the alkylation reaction, which can improve the conversion efficiency of coal-derived oil to aviation kerosene, maximize the production of aviation kerosene from coal-derived oil, improve the yield and fuel performance of aviation kerosene, make full use of the abundant and inexpensive methanol resources, and reduce production costs while realizing the high-value utilization of methanol.

[0070] In some embodiments, in step (4), the alkylation reaction is carried out using a hydrogenation process.

[0071] In some embodiments, in step (4), the alkylation reaction and the hydrogenation reaction are carried out in a fixed-bed reactor.

[0072] In some embodiments, the alkylation and hydrogenation reactions are carried out at temperatures ranging from 200 to 460°C, specifically, for example, 200°C, 300°C, 420°C, 430°C, 435°C, and 460°C; the volume hourly space velocity (VHSV) of the mixed light oil fraction is 5 to 15 h⁻¹. -1Specifically, for example, 5h -1 8h -1 9h -1 10h -1 12h -1 15h -1 The reaction pressure is 4–20 MPa, specifically, for example, 4 MPa, 5 MPa, 6 MPa, 10 MPa, 15 MPa, 20 MPa; the hydrogen-to-oil volume ratio is 5–20, specifically, for example, 5, 6, 8, 10, 15, 20.

[0073] In some embodiments, in step (4), the hydrogenation reaction uses a hydrogenation catalyst; the hydrogenation catalyst includes an active component and a support; the active component of the hydrogenation catalyst includes Cu element;

[0074] Optionally, the active component is a sulfide of a metal element; the active component in the hydrogenation catalyst has a weight content of 0.1% to 8% based on the metal element, specifically, for example, 0.1%, 5%, 6%, 7%, or 8%; the support includes at least one of inorganic oxides or molecular sieves; the inorganic oxide includes at least one of alumina and silicon oxide.

[0075] In this embodiment of the invention, in the presence of a hydrogenation catalyst, phenolic substances in a mixed light oil fraction undergo a hydrodeoxygenation reaction with hydrogen, thereby reducing the oxygen content in the feedstock and yielding aromatics and alkylbenzenes, thus increasing the yield of aviation kerosene components. Hydrogen-enriched conditions and a Cu-containing hydrogenation catalyst can efficiently carry out the hydrodeoxygenation reaction, converting the abundant phenolic substances in the feedstock into aromatics or alkylbenzenes, improving the aviation kerosene yield, and maximizing the production of aviation kerosene from coal-derived oil.

[0076] In some embodiments, in step (4), the alkylation reaction is carried out using an alkylation catalyst; the alkylation catalyst includes an active component and a support; the active component includes at least one of Mo and Ni elements;

[0077] Optionally, the active component is a sulfide of a metal element; the active component in the alkylation catalyst has a weight content of 0.1% to 5% based on the metal, specifically, for example, 0.1%, 1%, 2%, 3%, 4%, or 5%; the support includes at least one molecular sieve; optionally, the molecular sieve includes at least one of ZSM-11 or MCM-22; the silicon-to-aluminum ratio, i.e., the silicon-to-aluminum molar ratio, of the molecular sieve is 20 to 200.

[0078] In this embodiment of the invention, the alkylation reaction employs a hydrogen-based process. In the presence of an alkylation catalyst, the mixed light oil fraction of coal-derived oil undergoes an alkylation reaction with methanol to generate aviation kerosene fraction oil at 170–300°C. This fully utilizes the abundant and inexpensive methanol resources, achieving high-value utilization of methanol while reducing production costs. The hydrogen-based process significantly slows down the carbon deposition rate of the alkylation catalyst, extending its service life and reducing catalyst costs. Mo and Ni-modified ZSM-11 or MCM-22 molecular sieve catalysts can significantly remove heteroatoms such as S and N, improving the quality of aviation kerosene. Simultaneously, through the alkylation carbonization reaction, the light fraction can be converted into aviation kerosene fraction oil at 170–300°C, increasing the utilization rate of coal-derived oil and methanol, and increasing the yield of aviation kerosene components.

[0079] In some embodiments, in step (4), the hydrogenation catalyst and the alkylation catalyst are mixed together.

[0080] In some embodiments, in step (4), the mass ratio of alkylation catalyst to hydrogenation catalyst is 1-2:1-2, specifically, 1-2 (e.g., 1, 1.1, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, 1.9, 2) : 1-2 (e.g., 1, 1.1, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, 1.9, 2).

[0081] In some embodiments, in step (5), the hydrorefining process is carried out using a fixed-bed reactor.

[0082] In some embodiments, in step (5), the first jet fuel fraction, the second jet fuel fraction, the third jet fuel fraction and the fourth jet fuel fraction are mixed and then subjected to a hydrorefining reaction and gas-liquid separation to obtain hydrogen-rich gas and liquid oil; the liquid oil is fractionated to obtain aviation kerosene.

[0083] In some embodiments, in step (5), the reaction temperature of the hydrorefining treatment is 260-400℃, specifically, for example, 260℃, 300℃, 345℃, 350℃, 355℃, 400℃; the reaction pressure is 6-17MPa, specifically, for example, 6MPa, 8MPa, 10MPa, 12MPa, 13MPa, 17MPa; and the volume hourly space velocity of the mixed jet fuel fraction is 0.2-2.0 h⁻¹. -1 Specifically, for example, 0.2h -1 0.6h -1 0.8h -1 1.0h -1 1.5h -1 2.0h -1The hydrogen-to-oil ratio is 500-2000, specifically, for example, 500, 800, 900, 1000, 2000.

[0084] In some embodiments, in step (5), the hydrorefining process employs a hydrorefining catalyst; the hydrorefining catalyst comprises an active component and a support; the active component comprises at least one of group VIB and group VIII metal elements;

[0085] Optionally, the active component includes at least one of the metal elements Ni, Mo, Co, and W; optionally, the active component is a sulfide of a metal element; the weight content of the active component in the hydrorefining catalyst, calculated as a metal element, is 0.1% to 8%, specifically, for example, 0.1%, 1%, 2%, 5%, 6%, or 8%; the support includes at least one of inorganic oxides or molecular sieves; the inorganic oxide includes at least one of alumina and silicon oxide.

[0086] In this embodiment of the invention, hydrogenation refining of aviation kerosene fractions significantly removes heteroatoms such as S and N, producing high-quality aviation kerosene with excellent performance.

[0087] This invention discloses an aviation kerosene prepared by the method described in this invention. In this embodiment, the aviation kerosene exhibits high yield and excellent fuel performance, achieving high-value utilization of coal-derived oil while reducing production costs.

[0088] In some embodiments, the density of the aviation kerosene is ≥0.89 g / cm³. 3 Net calorific value ≥43.0MJ / kg.

[0089] An embodiment of the present invention provides a system for producing aviation kerosene, comprising: a distillation and separation unit 100, a hydrocracking unit 200, a hydrotreating unit 300, an alkylation and hydrotreating unit 400, and a hydrorefining unit 500.

[0090] The distillation separation unit 100 is equipped with a coal-derived oil inlet, a first light oil fraction outlet, a first aviation kerosene fraction outlet, a first diesel fraction outlet, and a heavy oil fraction outlet;

[0091] The hydrocracking unit 200 is provided with a heavy oil fraction inlet, a second light oil fraction outlet, a second jet fuel fraction outlet, and a second diesel fraction outlet, with the heavy oil fraction inlet connected to the heavy oil fraction outlet.

[0092] The hydrotreating and upgrading unit 300 is provided with a first diesel fraction inlet, a second diesel fraction inlet, a third light oil fraction outlet and a third aviation kerosene fraction outlet. The first diesel fraction inlet is connected to the first diesel fraction outlet, and the second diesel fraction inlet is connected to the second diesel fraction outlet.

[0093] The alkylation and hydrogenation unit 400 is provided with a first light oil fraction inlet, a second light oil fraction inlet, a third light oil fraction inlet, and a fourth jet fuel fraction outlet. The first light oil fraction inlet is connected to the first light oil fraction outlet, the second light oil fraction inlet is connected to the second light oil fraction outlet, and the third light oil fraction inlet is connected to the third light oil fraction outlet.

[0094] The hydrorefining unit 500 is equipped with a first aviation kerosene fraction inlet, a second aviation kerosene fraction inlet, a third aviation kerosene fraction inlet, a fourth aviation kerosene fraction inlet, and an aviation kerosene outlet. The first aviation kerosene fraction inlet is connected to the first aviation kerosene fraction outlet, the second aviation kerosene fraction inlet is connected to the second aviation kerosene fraction outlet, the third aviation kerosene fraction inlet is connected to the third aviation kerosene fraction outlet, and the fourth aviation kerosene fraction inlet is connected to the fourth aviation kerosene fraction outlet.

[0095] In this embodiment of the invention, the system for producing aviation kerosene is used to implement the aviation kerosene preparation method of this embodiment or to prepare aviation kerosene according to this embodiment. The system for producing aviation kerosene can improve the conversion efficiency of coal-derived oil to aviation kerosene, maximize the production of aviation kerosene from coal-derived oil, improve the yield and fuel performance of aviation kerosene, and realize the high-value utilization of coal-derived oil while reducing production costs.

[0096] like Figure 1 As shown, the method for preparing aviation kerosene according to an embodiment of the present invention uses the system for producing aviation kerosene according to an embodiment of the present invention, including:

[0097] (1) The coal-derived oil 1 is fed into the distillation separation unit 100, and the first light oil fraction 2, the first aviation kerosene fraction 3, the first diesel fraction 4 and the heavy oil fraction 5 are obtained by distillation and cutting.

[0098] (2) The heavy oil fraction 5 and hydrogen are fed into the hydrocracking unit 200. After oil slurry preparation, hydrocracking reaction and gas-liquid separation, hydrogen-rich gas and liquid oil are obtained. The liquid oil is distilled to obtain the second light oil fraction 6, the second jet fuel fraction 7 and the second diesel fraction 8. Optionally, they are fed into the hydrocracking unit 200 via a high-pressure pump.

[0099] (3) The first diesel fraction 4, the second diesel fraction 8 and hydrogen are mixed and fed into the hydrotreating unit 300. After hydrotreating reaction and gas-liquid separation, hydrogen-rich gas and liquid oil are obtained. The liquid oil is distilled to obtain the third light oil fraction 9 and the third aviation kerosene fraction 10. Optionally, the oil is fed into the hydrotreating unit 300 via a high-pressure pump.

[0100] (4) The first light oil fraction 2, the second light oil fraction 6 and the third light oil fraction 9 are mixed and sent to the alkylation and hydrogenation unit 400 to undergo alkylation and hydrogenation reactions with methanol 11 and hydrogen. After gas-liquid separation and fractionation, the fourth aviation kerosene fraction 12 and gaseous product 13 are obtained. Optionally, the gaseous product 13 includes water.

[0101] (5) The first aviation kerosene fraction 3, the second aviation kerosene fraction 7, the third aviation kerosene fraction 10 and the fourth aviation kerosene fraction 12 are mixed and sent to the hydrorefining unit 500 for hydrorefining reaction and gas-liquid separation to obtain hydrogen-rich gas and liquid oil; the liquid oil is fractionated to obtain aviation kerosene 14.

[0102] The present invention will now be described with reference to specific embodiments. It should be noted that these embodiments are merely descriptive and do not limit the present invention in any way.

[0103] Example 1

[0104] A method for preparing aviation kerosene from coal-derived oil according to the present invention includes:

[0105] (1) Using high-temperature coal tar as raw material, the first light oil fraction at <210℃, the first aviation kerosene fraction at 210~280℃, the first diesel oil fraction at 280℃~350℃ and the heavy oil fraction at >350℃ are obtained by distillation separation; the properties of the raw material are shown in Table 1.

[0106] (2) The heavy oil fraction and hydrogen are mixed, and after oil slurry preparation, hydrocracking reaction and gas-liquid separation, hydrogen-rich gas and liquid oil are obtained; the liquid oil is distilled to obtain a second light oil fraction with a temperature <170℃, a second aviation kerosene fraction with a temperature of 170-300℃ and a second diesel fraction with a temperature of 300-370℃. The hydrocracking uses two slurry bed reactors.

[0107] (3) The first diesel fraction and the second diesel fraction are mixed and then hydrotreated to obtain a third light oil fraction with a temperature of <170℃ and a third aviation kerosene fraction with a temperature of 170-300℃. The hydrotreatment is carried out in a fixed-bed reactor.

[0108] (4) The first, second, and third light oil fractions are mixed, and the mixed light oil fractions, methanol, and hydrogen are subjected to alkylation, hydrodeoxygenation, desulfurization, and denitrification reactions. Gas-liquid separation and fractionation are then performed to obtain the fourth jet fuel fraction at 170–300°C. The alkylation and hydrodeionization reactions are carried out in a fixed-bed reactor.

[0109] (5) The first, second, third, and fourth aviation kerosene fractions are mixed and then subjected to hydrorefining to remove heteroatoms such as S and N, to obtain aviation kerosene at 170–300°C. Hydrorefining is carried out using a fixed-bed reactor.

[0110] The specific parameters for hydrocracking, hydrotreating, alkylation, hydrogenation, and hydrorefining are shown in Table 2. The main properties of the aviation kerosene obtained in Example 1 are shown in Table 3.

[0111] Example 2

[0112] A method for preparing aviation kerosene from coal-derived oil according to the present invention includes:

[0113] (1) Using medium-temperature coal tar as raw material, the first light oil fraction at <220℃, the first aviation kerosene fraction at 220~290℃, the first diesel oil fraction at 290℃~360℃ and the heavy oil fraction at >360℃ are obtained by distillation separation; the properties of the raw material are shown in Table 1.

[0114] (2) The heavy oil fraction and hydrogen are mixed, and after oil slurry preparation, hydrocracking reaction and gas-liquid separation, hydrogen-rich gas and liquid oil are obtained; the liquid oil is distilled to obtain a second light oil fraction with a temperature <170℃, a second aviation kerosene fraction with a temperature of 170-300℃ and a second diesel fraction with a temperature of 300-370℃. The hydrocracking uses two slurry bed reactors.

[0115] (3) The first diesel fraction and the second diesel fraction are mixed and then hydrotreated to obtain a third light oil fraction with a temperature of <170℃ and a third aviation kerosene fraction with a temperature of 170-300℃. The hydrotreatment is carried out in a fixed-bed reactor.

[0116] (4) The first, second, and third light oil fractions are mixed, and the mixed light oil fractions, methanol, and hydrogen are subjected to alkylation, hydrodeoxygenation, desulfurization, and denitrification reactions. Gas-liquid separation and fractionation are then performed to obtain the fourth jet fuel fraction at 170–300°C. The alkylation and hydrodeionization reactions are carried out in a fixed-bed reactor.

[0117] (5) The first, second, third, and fourth aviation kerosene fractions are mixed and then subjected to hydrorefining to remove heteroatoms such as S and N, to obtain aviation kerosene at 170–300°C. Hydrorefining is carried out using a fixed-bed reactor.

[0118] The specific parameters for hydrocracking, hydrotreating, alkylation, hydrogenation, and hydrorefining are shown in Table 2. The main properties of the aviation kerosene obtained in Example 2 are shown in Table 3.

[0119] Example 3

[0120] A method for preparing aviation kerosene from coal-derived oil according to the present invention includes:

[0121] (1) Using low-temperature coal tar as raw material, the first light oil fraction at <230℃, the first aviation kerosene fraction at 230~300℃, the first diesel oil fraction at 300℃~370℃ and the heavy oil fraction at >370℃ are obtained by distillation separation; the properties of the raw material are shown in Table 1.

[0122] (2) The heavy oil fraction and hydrogen are mixed, and after oil slurry preparation, hydrocracking reaction and gas-liquid separation, hydrogen-rich gas and liquid oil are obtained; the liquid oil is distilled to obtain a second light oil fraction with a temperature <170℃, a second aviation kerosene fraction with a temperature of 170-300℃ and a second diesel fraction with a temperature of 300-370℃. The hydrocracking uses two slurry bed reactors.

[0123] (3) The first diesel fraction and the second diesel fraction are mixed and then hydrotreated to obtain a third light oil fraction with a temperature of <170℃ and a third aviation kerosene fraction with a temperature of 170-300℃. The hydrotreatment is carried out in a fixed-bed reactor.

[0124] (4) The first, second, and third light oil fractions are mixed, and the mixed light oil fractions, methanol, and hydrogen are subjected to alkylation, hydrodeoxygenation, desulfurization, and denitrification reactions. Gas-liquid separation and fractionation are then performed to obtain the fourth jet fuel fraction at 170–300°C. The alkylation and hydrodeionization reactions are carried out in a fixed-bed reactor.

[0125] (5) The first, second, third, and fourth aviation kerosene fractions are mixed and then subjected to hydrorefining to remove heteroatoms such as S and N, to obtain aviation kerosene at 170–300°C. Hydrorefining is carried out using a fixed-bed reactor.

[0126] The specific parameters for hydrocracking, hydrotreating, alkylation, hydrogenation, and hydrorefining are shown in Table 2. The main properties of the aviation kerosene obtained in Example 3 are shown in Table 3.

[0127] Comparative Example 1

[0128] A method for preparing aviation kerosene from coal-derived oil includes:

[0129] (1) Using the high-temperature coal tar in Example 1 as the raw material, the first light oil fraction at <210℃, the first aviation kerosene fraction at 210~280℃, the first diesel oil fraction at 280℃~350℃ and the heavy oil fraction at >350℃ were obtained by distillation separation; the properties of the raw material are shown in Table 1.

[0130] (2) The heavy oil fraction and hydrogen are mixed, and after oil slurry preparation, hydrocracking reaction and gas-liquid separation, hydrogen-rich gas and liquid oil are obtained; the liquid oil is distilled to obtain a second light oil fraction with a temperature <170℃, a second aviation kerosene fraction with a temperature of 170-300℃ and a second diesel fraction with a temperature of 300-370℃. The hydrocracking uses two slurry bed reactors.

[0131] (3) The first and second aviation kerosene fractions are mixed and then subjected to hydrorefining to remove heteroatoms such as S and N, to obtain aviation kerosene at 170–300°C. Hydrorefining is carried out using a fixed-bed reactor.

[0132] The specific parameters for hydrocracking, hydrotreating, alkylation, hydrogenation, and hydrorefining are shown in Table 2. The main properties of the aviation kerosene prepared in Comparative Example 1 are shown in Table 3.

[0133] Table 1 Properties of coal-derived oils in Examples 1-3

[0134]

[0135] Table 2 Main process conditions of Examples 1-3 and Comparative Example 1

[0136]

[0137]

[0138] Table 3. Main properties of each aviation kerosene product in Examples 1-3 and Comparative Example 1

[0139]

[0140] As can be seen from Tables 2 and 3, the preparation method of this embodiment of the invention prepares aviation kerosene from coal-derived oil through processes such as hydrogenation and methanol alkylation. The aviation kerosene has a high density value, exceeding 0.90 g / cm³. 3 Aviation kerosene has a high yield, reaching over 80%, and based on the high-value utilization of coal-derived oil, maximizing aviation kerosene production, and reducing costs, aviation kerosene has a high quality net calorific value, exceeding 43 MJ / kg.

[0141] Compared to Example 1, Comparative Example 1 had a lower aviation kerosene yield because it failed to fully utilize the diesel fraction, light oil fraction, and light oil fraction generated from the hydrocracking of heavy oil fractions in coal-derived oil. The hydrogenation conditions and Cu-containing single-metal active component hydrogenation catalyst provided by this invention can efficiently perform hydrodeoxygenation reactions, converting the phenolic substances abundant in the feedstock into aromatics or alkylbenzenes, i.e., aviation kerosene fractions. The Mo and Ni-modified MCM-22 or ZSM-11 molecular sieve catalysts provided by this invention can significantly remove heteroatoms such as S and N, while simultaneously converting light fractions into aviation kerosene fractions at 170–300°C through alkylation and carbon enrichment reactions, improving the utilization rate of coal-derived oil and methanol, and maximizing the yield of aviation kerosene components. In Table 3, the aviation kerosene of the embodiments of this invention has sulfur content below 3 mg / L and nitrogen content below 5 mg / L, indicating that sulfur and nitrogen are effectively removed. By significantly removing heteroatoms such as S and N through processes such as alkylation, hydrogenation, and hydrorefining, the quality of aviation kerosene is improved, resulting in high-quality aviation kerosene with excellent performance.

[0142] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0143] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between them; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0144] In this invention, the terms "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to a specific feature, structure, material, or characteristic described in connection with that embodiment or example, which is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0145] Although the above embodiments have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Any changes, modifications, substitutions and variations made to the above embodiments by those skilled in the art are within the protection scope of the present invention.

Claims

1. A method for preparing aviation kerosene, characterized in that, Includes the following steps: (1) Distill coal-derived oil or shale oil to obtain a first light oil fraction, a first aviation kerosene fraction, a first diesel oil fraction and a heavy oil fraction; (2) The heavy oil fraction is subjected to hydrocracking to obtain a second light oil fraction, a second jet fuel fraction, and a second diesel fraction; (3) The first diesel fraction and the second diesel fraction are mixed and subjected to hydrotreating to obtain the third light oil fraction and the third aviation kerosene fraction; (4) The first light oil fraction, the second light oil fraction and the third light oil fraction are mixed and subjected to alkylation and hydrogenation reactions with methanol and hydrogen to obtain the fourth jet fuel fraction; (5) The first aviation kerosene fraction, the second aviation kerosene fraction, the third aviation kerosene fraction and the fourth aviation kerosene fraction are mixed and subjected to hydrorefining treatment to obtain aviation kerosene; In step (4), the hydrogenation reaction uses a hydrogenation catalyst; the hydrogenation catalyst includes an active component and a support; the active component of the hydrogenation catalyst includes Cu element; In step (4), the alkylation reaction is carried out using an alkylation catalyst; the alkylation catalyst includes an active component and a support; the active component of the alkylation catalyst includes at least one of Mo and Ni elements.

2. The method for preparing aviation kerosene according to claim 1, characterized in that, The coal-derived oil includes at least one of low-temperature coal tar, medium-low temperature coal tar, medium-temperature coal tar, and high-temperature coal tar; And / or, the cut temperature of the first light oil fraction, the second light oil fraction, or the third light oil fraction is independently 170-230°C; And / or, the cutting temperature of the first jet fuel fraction, the second jet fuel fraction, the third jet fuel fraction, or the fourth jet fuel fraction is independently 280-300℃; And / or, the cutting temperature of the first diesel fraction or the second diesel fraction is independently 340-370°C.

3. The method for preparing aviation kerosene according to claim 1 or 2, characterized in that, In step (2), the hydrocracking process is carried out using a slurry bed reactor; and / or, the reaction temperature of the hydrocracking treatment is 320-470℃, the reaction pressure is 8-30 MPa, the volume space velocity of the heavy oil fraction is 0.2-2.0h -1 , the hydrogen-oil volume ratio is 500-2000; And / or, the hydrocracking process uses a hydrocracking catalyst; the active component of the hydrocracking catalyst includes at least one of molybdenum, nickel or iron; the particle diameter of the hydrocracking catalyst is 0.5-50 μm; the weight ratio of the active component of the hydrocracking catalyst to the heavy oil fraction is 0.2-5:

100.

4. The method for preparing aviation kerosene according to claim 1 or 2, characterized in that, In step (3), the hydrogenation and upgrading process is carried out using a fixed-bed reactor; And / or, the reaction temperature of the hydrotreating process is 300-450℃, the reaction pressure is 5-25 MPa, and the volume hourly space velocity of the mixed diesel fraction is 0.2-2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 500-2000; And / or, the hydrotreating process employs a hydrotreating catalyst; the hydrotreating catalyst comprises an active component and a support; the active component comprises at least one metal element from Group VIB and Group VIII; the active component in the hydrotreating catalyst has a weight content of 0.2% to 20% based on the metal element; the support comprises at least one inorganic oxide or molecular sieve.

5. The method for preparing aviation kerosene according to claim 1 or 2, characterized in that, In step (4), the molar ratio of methanol to mixed light oil fraction is (0.5-2):3; And / or, the alkylation and hydrogenation reactions are carried out in a fixed-bed reactor; And / or, the alkylation and hydrogenation reactions are carried out at temperatures of 200–460 °C, and the volume hourly space velocity (VHSV) of the mixed light oil fraction is 5–15 h⁻¹. -1 The reaction pressure is 4–20 MPa, and the hydrogen-to-oil volume ratio is 5–20.

6. The method for preparing aviation kerosene according to claim 1 or 2, characterized in that, In step (4), the active component in the hydrogenation catalyst has a weight content of 0.1% to 8% based on metal elements; the support in the hydrogenation catalyst includes at least one of inorganic oxides or molecular sieves.

7. The method for preparing aviation kerosene according to claim 1 or 2, characterized in that, In step (4), the active component in the alkylation catalyst has a weight content of 0.1% to 5% based on metal elements; the support in the alkylation catalyst includes at least one molecular sieve; the molecular sieve includes at least one of ZSM-11 or MCM-22.

8. The method for preparing aviation kerosene according to claim 1 or 2, characterized in that, In step (5), the hydrorefining process is carried out using a fixed-bed reactor; And / or, the hydrorefining treatment is carried out at a reaction temperature of 260-400 °C, a reaction pressure of 6-17 MPa, and a volume hourly space velocity (VHSV) of 0.2-2.0 h⁻¹ for the mixed jet fuel fraction. -1 The hydrogen-to-oil ratio is 500-2000; And / or, the hydrorefining process employs a hydrorefining catalyst; the hydrorefining catalyst comprises an active component and a support; the active component comprises at least one metal element from Group VIB and Group VIII; the active component in the hydrorefining catalyst has a weight content of 0.1% to 8% based on the metal element; the support comprises at least one inorganic oxide or molecular sieve.

9. A system for producing aviation kerosene using the method for preparing aviation kerosene according to any one of claims 1-8, characterized in that, include: The distillation separation unit is provided with a coal-derived oil or shale oil inlet, a first light oil fraction outlet, a first aviation kerosene fraction outlet, a first diesel fraction outlet, and a heavy oil fraction outlet; The hydrocracking unit is provided with a heavy oil fraction inlet, a second light oil fraction outlet, a second jet fuel fraction outlet, and a second diesel fraction outlet, wherein the heavy oil fraction inlet is connected to the heavy oil fraction outlet. The hydrotreating unit is provided with a first diesel fraction inlet, a second diesel fraction inlet, a third light oil fraction outlet and a third aviation kerosene fraction outlet. The first diesel fraction inlet is connected to the first diesel fraction outlet, and the second diesel fraction inlet is connected to the second diesel fraction outlet. An alkylation and hydrogenation unit is provided with a first light oil fraction inlet, a second light oil fraction inlet, a third light oil fraction inlet, and a fourth jet fuel fraction outlet. The first light oil fraction inlet is connected to the first light oil fraction outlet, the second light oil fraction inlet is connected to the second light oil fraction outlet, and the third light oil fraction inlet is connected to the third light oil fraction outlet. The hydrorefining unit is provided with a first aviation kerosene inlet, a second aviation kerosene inlet, a third aviation kerosene inlet, a fourth aviation kerosene inlet, and an aviation kerosene outlet. The first aviation kerosene inlet is connected to the first aviation kerosene outlet, the second aviation kerosene inlet is connected to the second aviation kerosene outlet, the third aviation kerosene inlet is connected to the third aviation kerosene outlet, and the fourth aviation kerosene inlet is connected to the fourth aviation kerosene outlet.

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