Aerospace kerosene component oil and preparation method thereof

Abstract

The invention relates to the technical field of coal chemical industry, and discloses aerospace kerosene component oil and a preparation method thereof. The method comprises the following steps: (1) heating coal-based Fischer-Tropsch wax to 60-140 DEG C, conveying the heated coal-based Fischer-Tropsch wax to a reactor loaded with an isomerization catalyst, pressurizing hydrogen to 2.5-10 MPa, injecting the pressurized hydrogen into the reactor, and carrying out hydrocracking; (2) carrying out gas-liquid separation on the hydrocracking product, conveying the separated liquid-phase component into a normal-pressure rectifying tower for normal-pressure rectification, and cutting out an aviation kerosene fraction or an aerospace kerosene fraction from the middle of the tower; (3) heavy components cut out from the bottom of the normal-pressure rectifying tower continue to enter a reduced-pressure rectifying tower to be subjected to reduced-pressure rectifying, and a lubricating oil base oil fraction is cut out from the middle of the tower. The aviation and aerospace kerosene component oil prepared by the method can well meet the requirements of cold regions and high-altitude flight on oil fluidity.

Description

Technical Field

[0001] This invention relates to the field of coal chemical technology, specifically to an aerospace kerosene component oil and its preparation method. Background Technology

[0002] The fuel-to-liquid (FT) synthesis reaction, using coal, natural gas, and biomass as raw materials to convert into liquid fuels, has emerged as a promising technological approach for producing clean alternative fuels. Key characteristics of FT-synthesized fuels include low sulfur, low nitrogen, and low aromatics content, meeting the requirements of clean fuels and increasingly stringent environmental regulations. Another important aspect of alternative fuel research is improving my country's energy structure. As is well known, coal, my country's primary energy source, suffers from low utilization rates and is accompanied by significant CO2 emissions causing environmental pollution. Therefore, developing alternative fuels using coal as a raw material can diversify energy supply and is of strategic importance for ensuring oil security. Developing FT technology using coal as a raw material can fully utilize my country's abundant coal resources to convert them into liquid fuels, initially addressing my country's energy supply shortages, responding to the energy crisis, and safeguarding sustainable economic development.

[0003] In 1999, Sasol, a South African company, introduced a blend of coal-based synthetic fuel produced using its FT process and petroleum-based jet fuel into Johannesburg's O.R. Tambo International Airport. Sasol synthetic fuel comprised up to 50% of the blend. International standards such as the UK Ministry of Defence standard DEF STAN 91-91, the American Society for Testing and Materials standard ASTM D1655, and joint refueling standards all permit the safe use of a blend consisting of 50% FT-produced synthetic fuel and 50% JetA or JetA-1. However, the production of semi-synthetic jet fuel is susceptible to disruptions caused by petroleum-based jet fuel production capacity. To ensure fuel supply, Sasol developed a coal-based fully synthetic jet fuel that meets all international performance requirements for jet fuels, including storage, handling, and flight safety. In 2008, Sasol announced the successful production of its coal-based fully synthetic jet fuel, which received international commercial aviation certification. The first step in the synthesis of coal-based fully synthetic jet fuel is the gasification of raw coal into syngas (H2 and CO). The syngas then undergoes a Fischer-Tropsch synthesis process using an iron-based catalyst for catalytic conversion. Summary of the Invention

[0004] The purpose of this invention is to overcome the problems of complex preparation processes, high production costs and energy consumption, and insufficient utilization of by-products in existing aerospace fuel technologies, and to provide an aerospace kerosene component oil and its preparation method. The aerospace kerosene component oil prepared according to the method of this invention has suitable density, high calorific value, good thermal stability and oxidation stability, and is free of mechanical impurities and harmful substances such as water, thus better meeting the fluidity requirements of fuels used in cold regions and high-altitude flights.

[0005] To achieve the above objectives, the present invention provides a method for preparing aerospace kerosene component oil, the method comprising the following steps:

[0006] (1) The coal-based Fischer-Tropsch wax is heated to 60-140°C and then transported to a reactor loaded with an isomeric catalyst. Hydrogen is pressurized to 2.5-10 MPa and injected into the reactor, and then hydrocracking is carried out.

[0007] (2) The hydrocracking products are subjected to gas-liquid separation, and the separated liquid phase components are then transported to an atmospheric distillation column for atmospheric distillation, and aviation kerosene fraction or aerospace kerosene fraction is cut out from the middle of the column.

[0008] (3) The heavy components cut off from the bottom of the atmospheric distillation column continue to enter the vacuum distillation column for vacuum distillation, and the lubricating oil base oil fraction is cut off from the middle of the column;

[0009] The heterogeneous catalyst is formed by molding mesoporous molecular sieves and macroporous pseudoboehmite, and the silicon-to-aluminum ratio of the heterogeneous catalyst is 90-130:1.

[0010] Preferably, the heterogeneous catalyst is prepared by molding mesoporous molecular sieves and macroporous pseudoboehmite at a mass ratio of 1:0.25-0.8.

[0011] Preferably, the mesoporous molecular sieve is at least one of ZSM-48 molecular sieve, Z-5 molecular sieve, and SAPO-11 molecular sieve.

[0012] Preferably, the coal-based Fischer-Tropsch wax has a sulfur content of <0.01 wt%, a nitrogen content of <0.01 wt%, an aromatic hydrocarbon content of <0.2 wt%, and a melting point of 55-75°C.

[0013] Preferably, in step (1), the conditions for hydrocracking include: a temperature of 300-450°C, a mass hourly space velocity of 0.5-1 h⁻¹, and a reaction pressure of 1-10 MPa.

[0014] Preferably, in step (1), the hydrogen-to-oil volume ratio in the hydrocracking process is 500-700:1.

[0015] Preferably, the temperature of the vacuum distillation is 250-280°C higher than the temperature of the atmospheric distillation.

[0016] Preferably, the temperature of the atmospheric distillation is 60-300℃.

[0017] Preferably, the temperature of the vacuum distillation is 280-600℃.

[0018] Preferably, the method further includes: combining and collecting the light components cut from the top of the atmospheric distillation column with the light components cut from the top of the vacuum distillation column, and collecting the heavy components cut from the bottom of the vacuum distillation column.

[0019] A second aspect of the present invention provides an aerospace kerosene component oil prepared by the method described above.

[0020] According to the preparation method of aerospace kerosene component oil described in this invention, coal-based Fischer-Tropsch wax is used as the initial feedstock. Hydrocracking is carried out in a reactor loaded with an isomeric catalyst. The hydrocracking products are then subjected to gas-liquid separation. The separated liquid phase components are then subjected to ambient temperature distillation and vacuum distillation sequentially. This method enables the efficient preparation of aerospace kerosene component oil from coal-based Fischer-Tropsch wax, offering advantages such as a short process flow, high economic efficiency, and safety and environmental friendliness. Furthermore, the aerospace kerosene component oil prepared according to the method of this invention has suitable density, high calorific value, good thermal stability and oxidation stability, and is free of mechanical impurities and harmful substances such as moisture. It can effectively meet the fluidity requirements of fuels used in cold regions and high-altitude flights. Attached Figure Description

[0021] Figure 1 The present invention provides a process flow diagram for preparing aerospace kerosene component oil from coal-based Fischer-Tropsch wax.

[0022] Explanation of reference numerals in the attached figures

[0023] 1. Raw material tank; 2. Reactor; 3. Atmospheric distillation column; 4. Vacuum distillation column; 5. Light component tank. Detailed Implementation

[0024] The following provides a detailed description of specific embodiments of the present invention. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit the scope of the invention.

[0025] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0026] The preparation method of aerospace kerosene component oil according to the present invention includes the following steps:

[0027] (1) The coal-based Fischer-Tropsch wax is heated to 60-140°C and then transported to a reactor loaded with an isomeric catalyst. Hydrogen is pressurized to 2.5-10 MPa and injected into the reactor, and then hydrocracking is carried out.

[0028] (2) The hydrocracking products are subjected to gas-liquid separation, and the separated liquid phase components are then transported to an atmospheric distillation column for atmospheric distillation, and aviation kerosene fraction or aerospace kerosene fraction is cut out from the middle of the column.

[0029] (3) The heavy components cut off from the bottom of the atmospheric distillation column continue to enter the vacuum distillation column for vacuum distillation, and the lubricating oil base oil fraction is cut off from the middle of the column;

[0030] The heterogeneous catalyst is formed by molding mesoporous molecular sieves and macroporous pseudoboehmite, and the silicon-to-aluminum ratio of the heterogeneous catalyst is 90-130:1.

[0031] In the method described in this invention, preferably, the mesoporous molecular sieve has a pore size of 2.5-4 nm; the macroporous boehmite has a pore size of 5-8 nm. The isomeric catalyst is prepared by molding the mesoporous molecular sieve and macroporous boehmite at a mass ratio of 1:0.25-0.8. More preferably, the isomeric catalyst is prepared by molding the mesoporous molecular sieve and macroporous boehmite at a mass ratio of 1:0.3-0.7. The mesoporous molecular sieve can be at least one of ZSM-48 type molecular sieve, Z-5 type molecular sieve, and SAPO-11 type molecular sieve, preferably ZSM-48 type molecular sieve.

[0032] In the method described in this invention, the silicon-to-aluminum ratio of the heterogeneous catalyst can be 90-130:1, preferably 100-120:1.

[0033] In the method described in this invention, the sulfur content of the coal-based Fischer-Tropsch wax is <0.01 wt%, the nitrogen content is <0.01 wt%, the aromatic content is <0.2 wt%, and the melting point can be 55-75℃. Preferably, the sulfur content of the coal-based Fischer-Tropsch wax is <0.0001 wt%, the nitrogen content is <0.0001 wt%, the aromatic content is <0.002 wt%, and the melting point can be 65-68℃. Specifically, the coal-based Fischer-Tropsch wax can be 56# Fischer-Tropsch wax and / or 59# Fischer-Tropsch wax. The 56# Fischer-Tropsch wax can be purchased from Ningxia Coal Industry Company, Shanxi Lu'an Company, or Inner Mongolia Yitai Group Co., Ltd. The 59# Fischer-Tropsch wax can be purchased from Ningxia Coal Industry Company, Shanxi Lu'an Company, or Inner Mongolia Yitai Group Co., Ltd.

[0034] In step (1), the conditions for hydrocracking may include: a temperature of 300-450°C and a mass hourly space velocity of 0.5-1 h⁻¹. -1 The reaction pressure is 1-10 MPa. Preferably, the reaction conditions include: a temperature of 320-420°C and a mass hourly space velocity (HHSV) of 0.6-0.9 h⁻¹. -1 The reaction pressure is 2-7 MPa. In this invention, the pressure is gauge pressure.

[0035] In step (1), the hydrogen-to-oil volume ratio in the hydrocracking process can be 500-700:1, preferably 550-680:1, and more preferably 570-630:1.

[0036] In the method described in this invention, preferably, the temperature of the vacuum distillation is 250-280°C higher than the temperature of the atmospheric distillation. More preferably, the temperature of the vacuum distillation is 260-270°C higher than the temperature of the atmospheric distillation.

[0037] In the method described in this invention, the temperature of the atmospheric distillation can be 60-300℃, preferably 80-280℃. The pressure of the atmospheric distillation can be 0-0.5MPa, preferably 0-0.2MPa.

[0038] In the method described in this invention, the temperature of the vacuum distillation can be 280-600℃, preferably 300-580℃. The pressure of the vacuum distillation can be 1-100 Torr, preferably 1-10 Torr.

[0039] In a preferred embodiment of the method described in this invention, the method further includes: combining and collecting the light components cut off from the top of the atmospheric distillation column and the light components cut off from the top of the vacuum distillation column, and collecting the heavy components cut off from the bottom of the vacuum distillation column.

[0040] like Figure 1As shown, the apparatus for preparing the aerospace kerosene component oil of the present invention includes: a feed tank 1, a reactor 2, an atmospheric distillation column 3, a vacuum distillation column 4, and a light component tank 5. Coal-based Fischer-Tropsch wax is heated to 60-140°C in the feed tank 1 and then transported to the reactor 2. Hydrogen gas is pressurized to 2.5-10 MPa and injected into the reactor, followed by hydrocracking. The gaseous products from hydrocracking are discharged through the gas phase outlet, while the liquid products enter the atmospheric distillation column 3 for atmospheric distillation. The heavy components cut off from the bottom of the column enter the vacuum distillation column 4 for vacuum distillation. The light component tank 5 is used to collect the light components separated from the atmospheric distillation column 3 and the vacuum distillation column 4.

[0041] In the apparatus described in this invention, the apparatus further includes a residue tank for collecting heavy components separated from the vacuum distillation column 4.

[0042] In the apparatus described in this invention, the raw material tank 1 is used for storing and heating coal-based Fischer-Tropsch wax. A pump is installed on the connecting pipeline between the raw material tank 1 and the reactor 2 to transport the coal-based Fischer-Tropsch wax from the raw material tank 1 to the reactor 2. The flow rate of the coal-based Fischer-Tropsch wax can be 0.3-1.5 h⁻¹. -1 .

[0043] In the apparatus described in this invention, reactor 2 is filled with an isomeric catalyst. Reactor 2 has a gas phase outlet at the top for discharging the gaseous products generated by hydrocracking. Reactor 2 also has a liquid phase outlet at the bottom for conveying the liquid products generated by hydrocracking to the atmospheric distillation column 3.

[0044] In the apparatus described in this invention, naphtha fraction (distillation range <150℃) can be extracted from the top of the atmospheric distillation column 3 and transported to the light component tank 5 for storage. Aviation kerosene fraction (distillation range 150-250℃) or aerospace kerosene fraction (distillation range 180-280℃) can be extracted from the middle of the atmospheric distillation column 3.

[0045] In the apparatus described in this invention, a lubricating oil base oil fraction (distillation range 310-440℃) can be separated from the middle of the vacuum distillation column 4. The lubricating oil base oil fraction can be at least one of base oil #2, base oil #3, base oil #4, and base oil #6. Heavy components are collected at the bottom of the vacuum distillation column 4 and transported to a residue tank for storage. Light components are collected at the top of the vacuum distillation column 4 and transported to a light component tank 5 for storage.

[0046] The present invention also provides an aerospace kerosene component oil prepared by the above method. This aerospace kerosene component oil comprises aerospace kerosene fraction or aviation kerosene fraction prepared by the above method and lubricating oil base oil fraction. Furthermore, this aerospace kerosene component oil has the characteristics of suitable density, high calorific value, good thermal stability and oxidation stability, and is free of mechanical impurities and harmful substances such as water, thus effectively meeting the fluidity requirements of oil products in cold regions and high-altitude flights.

[0047] The following examples further illustrate the aerospace kerosene component oil and its preparation method according to the present invention. These examples are implemented based on the technical solution of the present invention, providing detailed implementation methods and specific operating procedures; however, the scope of protection of the present invention is not limited to the following examples.

[0048] Unless otherwise specified, the experimental methods used in the following embodiments are conventional methods in the art. Unless otherwise specified, the experimental materials used in the following embodiments are commercially available.

[0049] In the following examples and comparative examples, the relevant parameters, test methods, standards, and test instruments for the fractions cut from the distillation column are shown in Table 1 below. The yield (%) of each fraction = (actual output per unit time / actual feed per unit time) × 100%, specifically as follows: Aviation kerosene fraction yield = (aviation kerosene component oil output within 1 hour / atmospheric distillation column feed within 1 hour) × 100%; Aerospace kerosene fraction yield = (aerospace kerosene component oil output within 1 hour / atmospheric distillation column feed within 1 hour) × 100%; Lubricating oil base oil fraction yield = (lubricating oil base oil output within 1 hour / atmospheric distillation column feed within 1 hour) × 100%.

[0050] Table 1

[0051]

[0052]

[0053] Example 1

[0054] This embodiment is in Figure 1 The process is carried out in the apparatus shown. Specifically, 56# Fischer-Tropsch wax (purchased from Ningxia Coal Industry Company, melting point 65℃, the same below) is placed in raw material tank 1 and heated to 100℃. An isomeric catalyst (silicon-aluminum ratio 130:1) prepared by molding mesoporous ZSM-48 molecular sieve and macroporous pseudoboehmite at a mass ratio of 1:0.42 is loaded into reactor 2. 56# Fischer-Tropsch wax is pumped into reactor 2 at a flow rate of 0.7 h⁻¹. -1 Hydrogen gas was pressurized to 4 MPa and injected into reactor 2, with a hydrogen-to-oil volume ratio of 600:1, at a temperature of 325°C and a mass hourly space velocity (HHSV) of 0.7 h⁻¹. -1Hydrocracking is carried out under a pressure of 3.5 MPa. The hydrocracking products are subjected to gas-liquid separation. The separated liquid phase component is sent to an atmospheric distillation column 3 for atmospheric distillation under the following conditions: temperature 200°C and pressure 0.1 MPa. The light component separated from the top of the atmospheric distillation column 3 is stored in a light component tank 5, and the liquid phase component separated from the bottom of the atmospheric distillation column 3 is sent to a vacuum distillation column 4 for vacuum distillation under the following conditions: temperature 350°C and pressure 10 Torr. The light component separated from the top of the vacuum distillation column 4 is stored in a light component tank 5, and the heavy component separated from the bottom of the vacuum distillation column 4 is stored in a residue tank. The fraction cut from the middle of the atmospheric distillation column 3 is condensed to obtain the aviation kerosene fraction A1 of this invention. The fraction cut from the middle of the vacuum distillation column 4 is condensed to obtain the lubricating oil base oil fraction B1 of this invention.

[0055] Table 2 shows the physicochemical parameters of aviation kerosene fraction A1. Table 3 shows the physicochemical parameters of lubricating oil base oil fraction B1.

[0056] Table 2

[0057]

[0058] As shown in Table 2, the freezing point of aviation kerosene fraction A1 is much lower than the target requirement, resulting in better low-temperature fluidity; the flash point is higher than the target requirement, resulting in better ignition performance; the aromatic content is lower than the target requirement, resulting in better cleanliness; and it has low moisture content, no mechanical impurities, and low corrosivity to materials.

[0059] Table 3

[0060]

[0061]

[0062] As shown in Table 3, the various indicators of the lubricating oil base oil fraction B1 meet the requirements.

[0063] Example 2

[0064] This embodiment is in Figure 1 The process is carried out in the apparatus shown. Specifically, 59# Fischer-Tropsch wax is placed in raw material tank 1 and heated to 60°C. An isomeric catalyst (silicon-to-aluminum ratio of 120:1) prepared by molding mesoporous Z-5 molecular sieve and macroporous pseudoboehmite at a mass ratio of 1:0.5 is loaded into reactor 2. 59# Fischer-Tropsch wax is then pumped into reactor 2 at a flow rate of 0.9 h⁻¹. -1 Hydrogen gas was pressurized to 4 MPa and injected into reactor 2, with a hydrogen-to-oil volume ratio of 600:1, at a temperature of 335℃ and a mass hourly space velocity of 0.7 h⁻¹. -1Hydrocracking is carried out under a pressure of 3.5 MPa. The products of the hydrocracking are subjected to gas-liquid separation. The separated liquid phase component is sent to an atmospheric distillation column 3 for atmospheric distillation. The atmospheric distillation conditions include a temperature of 200°C and a pressure of 0.1 MPa. The light component separated from the top of the atmospheric distillation column 3 is stored in a light component tank 5, and the liquid phase component separated from the bottom of the atmospheric distillation column 3 is sent to a vacuum distillation column 4 for vacuum distillation. The vacuum distillation conditions include a temperature of 350°C and a pressure of 10 Torr. The light component separated from the top of the vacuum distillation column 4 is stored in the light component tank 5, and the heavy component separated from the bottom of the vacuum distillation column 4 is stored in a residue tank. The fraction cut from the middle of the atmospheric distillation column 3 is condensed to obtain the aerospace kerosene fraction A2 of this invention. The fraction cut from the middle of the vacuum distillation column 4 is condensed to obtain the lubricating oil base oil fraction B2 of this invention.

[0065] Table 4 shows the physicochemical parameters of aerospace kerosene fraction A2. Table 5 shows the physicochemical parameters of the lubricating oil base oil fraction of aerospace kerosene component oil A2.

[0066] Table 4

[0067]

[0068] As shown in Table 4, the aromatic hydrocarbon content, total sulfur content, and mercaptan sulfur content of aerospace kerosene fraction A2 are far below the required levels, indicating superior cleanliness. It is free of mechanical impurities, has low acidity, and is less corrosive to materials. Its crystallization point temperature is lower than the required level, which can better meet the requirements for oil flowability in cold regions and high-altitude flights.

[0069] Table 5

[0070]

[0071] As shown in Table 5, the various indicators of the lubricating oil base oil fraction B2 meet the requirements.

[0072] Example 3

[0073] This embodiment is in Figure 1 The process is carried out in the apparatus shown. Specifically, 56# Fischer-Tropsch wax is placed in raw material tank 1 and heated to 140°C. An isomeric catalyst (silicon-to-aluminum ratio of 100:1) prepared from mesoporous SAPO-11 molecular sieve and macroporous pseudoboehmite is loaded into reactor 2 at a mass ratio of 1:0.42. 56# Fischer-Tropsch wax is then pumped into reactor 2 at a flow rate of 0.6 h⁻¹. -1 Hydrogen gas was pressurized to 8 MPa and injected into reactor 2, with a hydrogen-to-oil volume ratio of 630:1, at a temperature of 420℃ and a mass hourly space velocity of 0.9 h⁻¹. -1Hydrocracking is carried out under a pressure of 7 MPa. The hydrocracking products are subjected to gas-liquid separation. The separated liquid phase component is sent to an atmospheric distillation column 3 for atmospheric distillation. The atmospheric distillation conditions include a temperature of 200°C and a pressure of 0.1 MPa. The light component separated from the top of the atmospheric distillation column 3 is stored in a light component tank 5, and the liquid phase component separated from the bottom of the atmospheric distillation column 3 is sent to a vacuum distillation column 4 for vacuum distillation. The vacuum distillation conditions include a temperature of 350°C and a pressure of 10 Torr. The light component separated from the top of the vacuum distillation column 4 is stored in the light component tank 5, and the heavy component separated from the bottom of the vacuum distillation column 4 is stored in a residue tank. The fraction cut from the middle of the atmospheric distillation column 3 is condensed to obtain the aviation kerosene fraction A3 of this invention. The fraction cut from the middle of the vacuum distillation column 4 is condensed to obtain the lubricating oil base oil fraction B3 of this invention.

[0074] Example 4

[0075] Aerospace kerosene fractions were prepared according to the method of Example 1, except that mesoporous ZSM-48 molecular sieve and macroporous pseudoboehmite were prepared at a mass ratio of 1:0.67, resulting in the aerospace kerosene fraction A4 and lubricating oil base oil fraction B4 of the present invention.

[0076] Example 5

[0077] Aerospace kerosene component oils were prepared according to the method of Example 1, except that the hydrogen-oil volume ratio of 56# Fischer-Tropsch wax and hydrogen was adjusted to 400:1, resulting in the aerospace kerosene fraction A5 and lubricating oil base oil fraction B5 of the present invention.

[0078] Example 6

[0079] Aerospace kerosene fractions were prepared according to the method of Example 1, except that the temperature of atmospheric distillation was adjusted to 180°C and the temperature of vacuum distillation was adjusted to 330°C, thus obtaining the aerospace kerosene fraction A6 and the lubricating oil base oil fraction B6 of the present invention.

[0080] Comparative Example 1

[0081] Aerospace kerosene fractions were prepared according to the method in Example 1, except that only mesoporous ZSM-48 molecular sieves were used as isomer catalysts to obtain aviation kerosene fraction D1 and lubricating oil base oil fraction E1.

[0082] Comparative Example 2

[0083] Aerospace kerosene fractions were prepared according to the method of Example 1, except that the mass ratio of mesoporous ZSM-48 molecular sieve and macroporous pseudoboehmite was adjusted so that the silicon-aluminum ratio of the prepared isomeric catalyst was 80:1, resulting in aviation kerosene fraction D2 and lubricating oil base oil fraction E2.

[0084] The yield test results of each fraction in the above embodiments and comparative examples are shown in Table 6 below.

[0085] Table 6

[0086]

[0087] The test results of Examples 1-6 and Comparative Examples 1-2 show that the aerospace kerosene component oil prepared according to the method of the present invention has the characteristics of suitable density, high calorific value, good thermal stability and antioxidant stability, and no mechanical impurities or harmful substances such as water. It can better meet the requirements of oil fluidity for cold regions and high-altitude flights.

[0088] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for preparing aerospace kerosene component oil from coal-based Fischer-Tropsch wax, characterized in that, The method includes the following steps: (1) The coal-based Fischer-Tropsch wax is heated to 60-140°C and then transported to a reactor loaded with an isomeric catalyst. Hydrogen is pressurized to 2.5-10 MPa and injected into the reactor, and then hydrocracking is carried out. (2) The hydrocracking products are subjected to gas-liquid separation, and the separated liquid phase components are then transported to an atmospheric distillation column for atmospheric distillation, and aviation kerosene fraction or aerospace kerosene fraction is cut out from the middle of the column. (3) The heavy components cut off from the bottom of the atmospheric distillation column continue to enter the vacuum distillation column for vacuum distillation, and the lubricating oil base oil fraction is cut off from the middle of the column; The heterogeneous catalyst is formed by molding mesoporous molecular sieves and macroporous pseudoboehmite, and the silicon-to-aluminum ratio of the heterogeneous catalyst is 90-130:

1.

2. The method according to claim 1, characterized in that, The heterogeneous catalyst is prepared by molding mesoporous molecular sieves and macroporous pseudoboehmite at a mass ratio of 1:0.25-0.

8. Preferably, the mesoporous molecular sieve is at least one of ZSM-48 molecular sieve, Z-5 molecular sieve, and SAPO-11 molecular sieve.

3. The method according to claim 1 or 2, characterized in that, The coal-based Fischer-Tropsch wax has a sulfur content of <0.01 wt%, a nitrogen content of <0.01 wt%, an aromatic hydrocarbon content of <0.2 wt%, and a melting point of 55-75℃.

4. The method according to any one of claims 1-3, characterized in that, In step (1), the conditions for hydrocracking include: a temperature of 300-450°C and a mass hourly space velocity of 0.5-1 h⁻¹. -1 The reaction pressure is 1-10 MPa.

5. The method according to claim 1 or 4, characterized in that, In step (1), the hydrogen-to-oil volume ratio in the hydrocracking process is 500-700:

1.

6. The method according to any one of claims 1-5, characterized in that, The temperature of the vacuum distillation is 250-280°C higher than that of the atmospheric distillation.

7. The method according to claim 1 or 6, characterized in that, The temperature of the atmospheric distillation is 60-300℃.

8. The method according to claim 1 or 6, characterized in that, The temperature of the vacuum distillation is 280-600℃.

9. The method according to any one of claims 1-8, characterized in that, The method further includes: combining and collecting the light components cut off from the top of the atmospheric distillation column and the light components cut off from the top of the vacuum distillation column, and collecting the heavy components cut off from the bottom of the vacuum distillation column.

10. An aerospace kerosene component oil prepared by the method according to any one of claims 1-9.

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