A process for producing high-density jet fuel from a poor-quality catalytic diesel enriched in aromatics

Abstract

This invention provides a method for producing high-density jet fuel from low-grade catalytic diesel oil rich in aromatics. The method includes: (1) deep hydrodesulfurizing the low-grade catalytic diesel oil rich in aromatics under the action of an unsupported hydrodesulfurization catalyst; (2) selectively cracking the hydrodesulfurized oil to remove alkanes under the action of an HZSM-5 molecular sieve catalyst; (3) distilling the above reaction effluent to separate a jet fuel fraction; and (4) deep aromatics hydrogenation saturation of the above jet fuel fraction using an unsupported nickel catalyst. The unsupported hydrodesulfurization catalyst and the unsupported nickel catalyst are catalysts with high metal content and relatively low carrier or binder content. This method uses low-grade catalytic diesel oil rich in aromatics, especially polycyclic aromatic hydrocarbons, as raw material, and the reaction conditions are mild, producing fuel with a density of not less than 0.87 g / cm³. 3 It is a high-density jet fuel with a simple and practical process route, mild reaction conditions, and easy industrial application.

Description

Technical Field

[0001] This invention relates to a method for producing high-density jet fuel from low-quality catalytic diesel fuel that is rich in aromatics and difficult to process. Background Technology

[0002] Supersonic aircraft, due to mass limitations and the resulting higher heat loads, require jet fuels with higher density and superior high-temperature thermal stability. High-density jet fuels are a type of jet fuel with high density and high volumetric calorific value, such as the high-density jet fuel in my country's GJB1603-93 standard and the US JP-900 fuel. Increasing fuel density is the most effective way to increase its volumetric calorific value; compared to ordinary jet fuels, high-density jet fuels have a higher volumetric calorific value. When the fuel tank volume is fixed, using high-density jet fuel can effectively meet the requirements of high speed and long range for aircraft.

[0003] Literature reports the use of petroleum fractions with high aromatic content, or the production of high-density jet fuel from coal tar or direct coal liquefaction oil. Coal tar has a complex chemical composition and high oxygen content, making processing difficult and generally cumbersome. Conventional supported metal sulfide catalysts are typically used for hydrorefining, while precious metal catalysts are used for aromatic hydrogenation saturation. Conventional supported metal sulfide catalysts have low activity, leading to demanding operating conditions, while precious metal catalysts increase operating costs.

[0004] JP-900, for example, is a synthetic fuel developed in the United States. It uses a 1:1 volume ratio mixture of refined coal tar and petroleum-based light cycle oil as raw materials, produced via a two-step hydrogenation process: the first step uses a nickel-molybdenum or cobalt-molybdenum catalyst, and the second step uses a platinum / palladium catalyst. After hydrogenation, the fuel undergoes distillation to separate a fraction at 180-270°C, which is then used as jet fuel. JP-900 fuel has a density of 0.87 g / cm³. 3 It has a high flash point, low viscosity, high pour point and high volumetric calorific value. It can remain stable for a long time at 900℉ (482℃) without decomposition or carbon buildup.

[0005] Currently, the annual processing capacity of catalytic cracking units in my country exceeds 100 million tons. Simultaneously, as these units strive to improve gasoline quality or increase low-carbon olefin production, operational stringency has generally increased, making the quality of catalytic diesel increasingly unsuitable for use as a diesel blending component. Inferior catalytic diesel components have high aromatic content, particularly rich in bicyclic and tricyclic polycyclic aromatic hydrocarbons, with densities typically reaching 0.94 g / cm³. 3 As mentioned above, it is quite difficult to produce automotive diesel through conventional hydrorefining, and it is difficult to meet the requirements of the China VI standard for the content of polycyclic aromatic hydrocarbons (mass fraction ≤ 7).

[0006] If the aromatics in low-quality catalytic diesel are converted into cycloalkanes, they can be used to produce high-density jet fuel with high density, high bulk calorific value, and low freezing point. However, the conversion of aromatics into cycloalkanes will cause a significant decrease in the density of the fuel, and due to the presence of alkanes in the fuel, it will be difficult to achieve a density similar to 0.87 g / cm³ of US JP-900 fuel. 3 The density level. If high-density jet fuel is produced using low-quality catalytic diesel rich in aromatics, it is necessary to address the problems of low activity and harsh reaction conditions of conventional supported metal sulfide catalysts, and to avoid using precious metal catalysts, in order to facilitate industrial application. Simultaneously, it is necessary to selectively remove alkanes from the oil to obtain high-density jet fuel with higher density. Summary of the Invention

[0007] To address the problems existing in the prior art, the present invention aims to provide a method for producing high-density jet fuel using low-quality catalytic diesel rich in aromatics as feedstock. The present invention employs a highly active unsupported hydrodesulfurization catalyst for deep hydrodesulfurization of low-quality catalytic diesel, and uses an unsupported nickel catalyst for deep aromatics hydrogenation saturation of the jet fuel fraction separated by distillation. This solves the technical problems of low activity and harsh reaction conditions associated with conventional supported metal sulfide catalysts, while avoiding the use of precious metal catalysts. The unsupported hydrodesulfurization catalyst and the unsupported nickel catalyst have high metal content and relatively low support or binder content. Due to the high content of active metals in the catalyst, it has high overall catalyst activity, allowing for more moderate process operating conditions such as reaction temperature and hydrogen pressure. Furthermore, since the active metals are all conventional transition metals, it is beneficial to control the catalyst price. To further improve the density of jet fuel, the deep hydrodesulfurized oil undergoes selective cracking using an HZSM-5 molecular sieve catalyst to remove alkanes. The cracking products of the alkanes can be used as gasoline blending components after subsequent distillation. The distilled jet fuel fraction is then saturated with aromatics through deep hydrogenation to convert it into cycloalkanes, achieving a density similar to that of US JP-900, not less than 0.87 g / cm³. 3 High-density jet fuel.

[0008] The objective of this invention is achieved through the following measures:

[0009] First, a non-supported hydrodesulfurization catalyst was used to perform deep hydrodesulfurization on low-quality catalytic diesel oil rich in aromatics. The density of the low-quality catalytic diesel oil was 0.94 g / cm³. 3The total aromatic hydrocarbon and cycloalkanes have a combined mass percentage of over 70%, of which the combined mass percentage of polycyclic aromatic hydrocarbons and polycyclic cycloalkanes has a combined mass percentage of over 50%; the sulfur content in the deep hydrodesulfurized oil is reduced to below 20 μg / g, the total aromatic hydrocarbon mass percentage is reduced to below 50%, and the polycyclic aromatic hydrocarbon mass percentage is reduced to below 10%.

[0010] The unsupported hydrodesulfurization catalyst, based on the mass percentage of oxides, contains 15-30% nickel oxide, 10-25% molybdenum oxide, 25-40% tungsten oxide, and the balance is alumina as a binder.

[0011] The aforementioned deep hydrodesulfurization reaction conditions for inferior catalytic diesel are: temperature 340-380℃, hydrogen pressure 8-12MPa, and feed space velocity 0.5-2h. -1 Hydrogen / oil volume ratio 500:1-1000:1.

[0012] The hydrodesulfurized oil obtained above undergoes selective cracking to remove alkanes under the action of HZSM-5 molecular sieve catalyst. The HZSM-5 molecular sieve has a silica-to-alumina ratio of 80-180. The preparation process of the HZSM-5 molecular sieve catalyst includes the following steps: 40-90% HZSM-5 molecular sieve and 10-60% alumina are mixed into a homogeneous mixture by mass percentage; guar gum powder is added or not added and mixed evenly, with the guar gum powder addition ratio being 2-5% of the total mass of the mixture; then, a 3-5% nitric acid solution is added, with the nitric acid solution addition ratio being 2% of the total mass of the mixture. 5-70%, thoroughly mixed into a sticky dough; or weigh HZSM-5 molecular sieve and alumina according to the above mass percentages, first add or not add guar gum powder to the alumina to form a uniform mixture, add 3-5% dilute nitric acid solution and mix evenly, then add HZSM-5 molecular sieve and mix thoroughly into a sticky dough; extrude the dough into cylindrical strips with a diameter of 1.0-2.0 mm, air dry naturally, dry at 120℃ for 3 hours, calcine at 500-600℃ for 2-8 hours, and then take it out to form 2-3 mm long shaped particles, which are the HZSM-5 molecular sieve catalysts.

[0013] The selective cracking reaction conditions for the hydrodesulfurized oil are: temperature 280-400℃, carrier gas pressure: atmospheric pressure - 1.0 MPa, and feed space velocity 0.5-2 h⁻¹. -1 The volume ratio of carrier gas to oil is 300:1-1000:1.

[0014] The selective cracking effluent is distilled to separate a jet fuel fraction, which is then subjected to deep aromatic hydrogenation saturation using an unsupported nickel catalyst. The jet fuel fraction has a boiling point range of 180-300°C and contains less than 5% alkane by mass. After deep aromatic hydrogenation saturation, the total aromatic content of the jet fuel fraction is reduced to less than 5% by mass.

[0015] The unsupported nickel catalyst, by mass percentage of oxides, contains 40-90% nickel oxide, with the balance being alumina as a binder.

[0016] The deep aromatics hydrogenation saturation reaction conditions for the jet fuel fraction separated by distillation are: temperature 160-240℃, hydrogen pressure 4-8 MPa, and feed space velocity 0.2-1.5 h⁻¹. -1 Hydrogen / oil volume ratio 500:1-1000:1.

[0017] The beneficial effects of this invention are as follows:

[0018] (1) The process route of the present invention can convert inferior catalytic diesel oil rich in aromatics, especially polycyclic aromatics, into diesel oil with a density of not less than 0.87 g / cm³, similar to US JP-900, under relatively mild reaction conditions. 3 High-density jet fuel; the method is simple, practical, and easy to implement industrially.

[0019] (2) Using an unsupported catalyst with high overall activity can effectively reduce process conditions such as reaction temperature and hydrogen pressure. Furthermore, by using conventional transition metals as the active component, catalyst price and operating costs can be effectively controlled.

[0020] (3) Using HZSM-5 molecular sieve catalyst with appropriate silicon-aluminum ratio to selectively crack and remove alkanes from hydrodesulfurized oil can effectively improve the density of the obtained jet fuel. Detailed Implementation

[0021] The present invention will be further described below with reference to specific embodiments. The scope of protection of the present invention is not limited by the following embodiments.

[0022] Basic Implementation Example:

[0023] The process for producing high-density jet fuel from low-quality catalytic diesel oil rich in aromatics used in this invention is as follows:

[0024] (1) Deep hydrodesulfurization of inferior catalytic diesel

[0025] Deep hydrodesulfurization of inferior catalytic diesel was carried out using a Ni-Mo-W unsupported hydrodesulfurization catalyst in a 100mL fixed-bed hydrotreating unit, and compared with a conventional supported Ni-Mo-P / Al2O3 catalyst.

[0026] Before the reaction, the catalyst is pre-sulfurized. After the reactor is loaded with catalyst, hydrogen is introduced and the hydrogen pressure is adjusted to be the same as that of the hydrodesulfurization reaction. The hydrogen flow rate is controlled to achieve a hydrogen / catalyst volume ratio of 600:1. First, the temperature is raised to 120℃ and stabilized for 1 hour for dehydration. Then, jet fuel containing 2% CS2 by mass is pumped in as pre-sulfurized oil. The feed space velocity of the pre-sulfurized oil is 1.0 h⁻¹. -1 The temperature was increased at a rate of 1℃ / min to 200℃, 240℃, 280℃, and 320℃, and stabilized for 1 hour each time. Finally, the temperature was increased to 340℃ and stabilized for 8 hours. After pre-sulfurization, the reactor temperature was reduced to 300℃, and the feed was switched to low-quality catalytic diesel. The hydrodesulfurization reaction temperature, hydrogen pressure, and feed space velocity were adjusted to meet the predetermined reaction conditions. After stabilizing the feed for 8 hours, the reaction products were collected. The collected hydrodesulfurized oil was immediately subjected to alkaline washing to remove dissolved hydrogen sulfide. The density, sulfur content, and hydrocarbon composition (alkanes, cycloalkanes, and aromatics) of the low-quality catalytic diesel and hydrodesulfurized oil were determined.

[0027] (2) Selective cracking of hydrodesulfurized oil to remove alkanes

[0028] The selective cracking of hydrodesulfurized oil to remove alkanes was carried out using HZSM-5 molecular sieve catalyst with a high silicon-to-aluminum ratio in a 10 mL fixed-bed hydrotreating unit. After the reactor was loaded with catalyst, nitrogen or hydrogen was introduced as the carrier gas, and the carrier gas pressure and flow rate were adjusted to the predetermined reaction pressure and flow rate. The reactor temperature was increased to 280°C at a rate of 1°C / min, and the aforementioned hydrodesulfurized oil was pumped in. The reaction temperature and feed space velocity were adjusted to achieve the predetermined selective cracking reaction conditions. After stabilizing the feed for 8 hours, the reaction products were collected.

[0029] (3) Separate jet fuel fraction from hydrodesulfurized oil by distillation.

[0030] A jet fuel fraction with a boiling point range of 180-300°C was separated from the above selective cracking reaction products using a true boiling point distillation apparatus. The distillation was carried out under reduced pressure of 10 Pa.

[0031] (4) Jet fuel fraction depth aromatics hydrogen saturation

[0032] Deep aromatics hydrogenation saturation of jet fuel fractions was performed using an unsupported nickel catalyst in a 10 mL fixed-bed hydrogenation unit, and compared with conventional supported nickel catalysts.

[0033] Before the reaction, a catalyst pre-reduction was performed. After the reactor was loaded with catalyst, hydrogen was introduced and the hydrogen pressure was adjusted to be the same as that of the aromatic hydrogenation saturation reaction. The hydrogen flow rate was controlled to achieve a hydrogen / catalyst volume ratio of 600:1, and the temperature was increased to 400℃ at a rate of 1℃ / min for 8 hours of reduction. After the reduction, the reactor temperature was cooled to 200℃, and the above-mentioned jet fuel fraction was pumped in. The reaction temperature, hydrogen pressure, feed space velocity, etc., were adjusted to achieve the predetermined aromatic hydrogenation saturation reaction conditions. After stabilizing the feed for 8 hours, the reaction products were collected. The jet fuel fraction and the deep aromatic hydrogenation reaction products were measured for distillation range, density, sulfur content, hydrocarbon type composition (alkanes, cycloalkanes, and aromatics), and other relevant indicators.

[0034] Examples 1-2

[0035] 100 mL of Ni-Mo-W unsupported hydrodesulfurization catalyst was measured and loaded into a 100 mL fixed-bed reactor. After pre-sulfurization according to the method in the basic example, a deep hydrodesulfurization reaction of inferior catalytic diesel was carried out. The chemical composition of Ni-Mo-W unsupported hydrodesulfurization catalyst, hydrodesulfurization conditions and property analysis results of hydrodesulfurized oil are shown in Table 1.

[0036] Comparative Example 1

[0037] 100 mL of conventional supported Ni-Mo-P / Al2O3 catalyst was measured and loaded into a 100 mL fixed-bed reactor. After pre-sulfurization according to the method in the basic example, a deep hydrodesulfurization reaction of inferior catalytic diesel was carried out. The chemical composition of Ni-Mo-P / Al2O3 catalyst, hydrodesulfurization conditions and property analysis results of hydrodesulfurized oil are shown in Table 1.

[0038] Example 3

[0039] 140g of HZSM-5 molecular sieve (silicon-to-alumina ratio 160), 60g of alumina powder, and 5.0g of guar gum powder were weighed and mixed evenly. 100g of 4.0% dilute nitric acid solution was weighed and added dropwise to the mixture while stirring evenly. The mixture was first extruded and kneaded twice in an extruder, and then extruded into strips with a diameter of 1.6mm. After natural air drying, it was dried at 120℃ for 3 hours and calcined at 550℃ for 4 hours. The resulting granules were then formed into 2-3mm long particles, thus obtaining the HZSM-5 molecular sieve catalyst. 10mL of the above HZSM-5 molecular sieve catalyst was measured and loaded into a 10mL fixed-bed reactor. The selective cracking of alkane hydrocarbons from hydrodesulfurized oil was carried out according to the method in the basic example. A jet fuel fraction with a boiling point range of 180-300℃ was distilled and separated from the selective cracking reaction products. The cracking reaction conditions and the property analysis results of the 180-300℃ jet fuel fraction are shown in Table 2.

[0040] Example 4

[0041] The HZSM-5 molecular sieve catalyst was prepared according to the method in Example 3, except that an HZSM-5 molecular sieve with a silicon-to-aluminum ratio of 130 was used. Then, the selective cracking of alkanes from hydrodesulfurized oil and the distillation separation of jet fuel fractions at 180-300℃ were carried out according to the method in Example 3. The cracking reaction conditions and the property analysis results of the jet fuel fractions at 180-300℃ are shown in Table 2.

[0042] Example 5

[0043] Weigh 100g of alumina powder, add 6.0g of guar gum powder and mix well. Weigh 125g of 4.5% dilute nitric acid solution and add it dropwise to the mixture while stirring evenly. Add 100g of HZSM-5 molecular sieve with a silicon-to-aluminum ratio of 160 and continue stirring evenly. Extrude and knead twice in an extruder, then extrude into strips with a diameter of 1.6mm. After natural drying, dry at 120℃ for 3h, calcine at 550℃ for 4h, and then remove and form 2-3mm long shaped particles to obtain the HZSM-5 molecular sieve catalyst. Selective cracking of alkanes from hydrodesulfurized oil and distillation separation of jet fuel fractions at 180-300℃ were carried out according to the method in Example 3. The cracking reaction conditions and the property analysis results of the 180-300℃ jet fuel fraction are shown in Table 2.

[0044] Comparative Example 2

[0045] Hydrodesulfurized oil is directly distilled to separate jet fuel fractions with boiling points ranging from 180 to 300°C without undergoing selective cracking of alkanes. The results of the property analysis are shown in Table 2.

[0046] Examples 6-8

[0047] In a 10 mL fixed-bed reactor, a non-supported nickel catalyst was used to carry out the deep aromatics hydrogenation saturation reaction of the 180-300℃ jet fuel fraction obtained in Example 3. The amount of non-supported nickel catalyst loaded in the reactor was 10 mL. The catalyst pre-reduction and aromatics hydrogenation saturation reaction were carried out according to the method in the basic example. The chemical composition of the non-supported nickel catalyst, the deep aromatics hydrogenation reaction conditions, and the property analysis results of the product oil are shown in Table 3.

[0048] Comparative Example 3:

[0049] Using the hydrodesulfurized oil from Comparative Example 2 without selective cracking, jet fuel fractions at 180-300℃ were directly distilled and separated as feedstock. In a 10mL fixed-bed reactor, a non-supported nickel catalyst was used for deep aromatic hydrogenation saturation of the jet fuel fraction. The amount of non-supported nickel catalyst in the reactor was 10mL. Catalyst pre-reduction and aromatic hydrogenation saturation reactions were carried out according to the method in the basic example. The chemical composition of the non-supported nickel catalyst, the deep aromatic hydrogenation reaction conditions, and the property analysis results of the product oil are shown in Table 3.

[0050] Table 1 lists the property analysis results of inferior catalytic diesel feedstock, the chemical composition, hydrodesulfurization conditions, and property analysis results of the Ni-Mo-W unsupported hydrodesulfurization catalyst of Examples 1-2 and the conventional supported Ni-Mo-P / Al2O3 catalyst of Comparative Example 1. It can be seen that Examples 1-2 used the unsupported hydrodesulfurization catalyst of this invention, with a density of 0.9563 g / cm³. 3 Using low-quality catalytic diesel oil with a sulfur content of 4832 μg / g, a total aromatic hydrocarbon (TH) content of 83.23%, and a polycyclic aromatic hydrocarbon (PAH) content of 66.70% as feedstock, the sulfur content in the hydrodesulfurized oil can be reduced to below 20 μg / g, the TH content to below 50%, and the PAH content to below 10% under relatively low hydrogen pressure. This demonstrates that the Ni-Mo-W unsupported catalyst of this invention exhibits relatively high hydrodesulfurization activity. In contrast, Comparative Example 1, using a conventional supported Ni-Mo-P / Al2O3 catalyst, still exhibits a sulfur content of 60.13 μg / g in the hydrodesulfurized oil even under relatively high hydrogen pressure. If a reduced nickel catalyst is used for subsequent aromatic hydrocarbon hydrogenation saturation, the catalyst will rapidly deactivate due to sulfur poisoning.

[0051] Table 1 Results of hydrodesulfurization reaction of inferior catalytic diesel fuel

[0052]

[0053] Table 2 lists the selective cracking reaction conditions of the hydrodesulfurized oil and the property analysis results of the 180-300℃ jet fuel fraction separated from the cracking products by distillation. It can be seen that after the hydrodesulfurized oil of Examples 3-5 undergoes selective cracking of alkanes according to this invention, the alkanes content in the 180-300℃ jet fuel fraction separated by distillation is significantly lower than that of Comparative Example 2 without selective cracking. The mass percentage of alkanes can be reduced to below 5%, indicating that the HZSM-5 molecular sieve catalyst used in this invention has good selectivity for cracking alkanes. Due to the reduced alkanes content, the density of the 180-300℃ fraction is significantly increased.

[0054] Table 2. Properties analysis results of the jet fuel fraction separated by distillation (180-300℃).

[0055]

[0056] Table 3 lists the results of deep aromatics hydrogenation saturation reaction of the 180-300℃ jet fuel fraction separated by distillation under the action of an unsupported nickel catalyst. It can be seen that, in Examples 6-8, using the method of the present invention, with the 180-300℃ jet fuel fraction after selective cracking to remove alkanes as feedstock, and undergoing aromatics hydrogenation saturation reaction under the action of an unsupported nickel catalyst, the resulting product oil, under relatively low hydrogenation temperature and hydrogen pressure conditions, basically meets the requirements of US JP-900 high-density fuel in terms of various properties, except for a slightly higher total aromatics content; the density can reach 0.87 g / cm³. 3 In all cases, the total aromatic hydrocarbon content can be reduced to below 5%. However, after aromatic hydrocarbon hydrogenation saturation of the 180-300℃ fraction obtained by direct distillation without cracking in Comparative Example 3, the density of the product oil is significantly lower due to the higher alkane content.

[0057] Table 3. Results of deep aromatic hydrogenation saturation reaction of jet fuel fractions at 180-300℃

[0058]

[0059] The above results demonstrate that, using the method of this invention, it is possible to produce diesel fuel with a density of not less than 0.87 g / cm³, similar to US JP-900, from low-quality catalytic diesel fuel rich in aromatics under relatively mild conditions. 3 High-density jet fuel. Highly active unsupported hydrodesulfurization catalysts and unsupported nickel catalysts can effectively reduce process operating conditions, while HZSM-5 molecular sieve catalysts selectively crack and remove alkanes, effectively increasing the density of jet fuel products.

Claims

1. A method for producing high-density jet fuel from low-quality catalytic diesel fuel rich in aromatics, characterized in that: The method includes the following steps: (1) Deep hydrodesulfurization of low-quality catalytic diesel oil rich in aromatics under the action of a non-supported hydrodesulfurization catalyst is carried out to obtain deep hydrodesulfurized oil. (2) The above-mentioned deep hydrodesulfurized oil is selectively cracked to remove alkanes under the action of HZSM-5 molecular sieve catalyst; (3) The jet fuel fraction is separated by distillation of the above selective cracking reaction effluent for the removal of alkanes; (4) Deep aromatic hydrogenation saturation of the above-mentioned jet fuel fraction was carried out using an unsupported nickel catalyst; The density of the inferior catalytic diesel oil is 0.94 g / cm³. 3 The total aromatic hydrocarbon and cycloalkanes content is above 70% by mass, of which the total polycyclic aromatic hydrocarbon and polycyclic cycloalkanes content is above 50% by mass; the sulfur content in the deep hydrodesulfurized oil is below 20 μg / g, the total aromatic hydrocarbon content is below 50% by mass, of which the polycyclic aromatic hydrocarbon content is below 10% by mass; the boiling point range of the jet fuel fraction separated by distillation is 180-300℃, of which the alkanes content is below 5% by mass; after deep aromatic hydrocarbon hydrogenation saturation, the total aromatic hydrocarbon content of the jet fuel fraction is below 5% by mass. The unsupported hydrodesulfurization catalyst, based on the mass percentage of oxides, contains 15-30% nickel oxide, 10-25% molybdenum oxide, and 25-40% tungsten oxide, with the balance being alumina as a binder; the unsupported hydrodesulfurization catalyst needs to be pre-sulfurized before deep hydrodesulfurization of inferior catalytic diesel. The unsupported nickel catalyst, by mass percentage of oxides, contains 40-90% nickel oxide and the balance is alumina as a binder; the unsupported nickel catalyst needs to be pre-reduced before deep aromatic hydrogenation saturation of jet fuel fractions.

2. The method according to claim 1, characterized in that: The HZSM-5 molecular sieve has a silica-to-alumina ratio of 80-180. The preparation process of the HZSM-5 molecular sieve catalyst includes the following steps: by mass percentage, 40-90% HZSM-5 molecular sieve and 10-60% alumina are made into a uniform mixture, guar gum powder is added and mixed evenly, the proportion of guar gum powder added is 2-5% of the total mass of the above mixture, and then a nitric acid solution with a mass concentration of 3-5% is added, the proportion of nitric acid solution added is 25-70% of the total mass of the above mixture, and the mixture is thoroughly stirred into a sticky dough. Alternatively, weigh out 40-90% of HZSM-5 molecular sieve and 10-60% of alumina by mass percentage. First, add guar gum powder to the alumina to make a uniform mixture. Then, add a 3-5% dilute nitric acid solution and stir evenly. Finally, add the HZSM-5 molecular sieve and stir thoroughly to form a sticky dough. The dough obtained by any of the above methods is extruded into cylindrical strips with a diameter of 1.0-2.0 mm, air-dried naturally, dried at 120℃ for 3 hours, and calcined at 500-600℃ for 2-8 hours. After being removed, it is made into shaped particles with a length of 2-3 mm, which is the HZSM-5 type molecular sieve catalyst.

3. The method according to claim 1, characterized in that: The aforementioned deep hydrodesulfurization reaction conditions for inferior catalytic diesel are: temperature 340-380℃, hydrogen pressure 8-12MPa, and feed space velocity 0.5-2h. -1 Hydrogen / oil volume ratio 500:1-1000:

1.

4. The method according to claim 1, characterized in that: The selective cracking reaction conditions for the hydrodesulfurized oil are: temperature 280-400℃, carrier gas pressure: atmospheric pressure - 1.0 MPa, and feed space velocity 0.5-2 h⁻¹. -1 The volume ratio of carrier gas to oil is 300:1-1000:

1.

5. The method according to claim 1, characterized in that: The deep aromatics hydrogenation saturation reaction conditions for the jet fuel fraction separated by distillation are: temperature 160-240℃, hydrogen pressure 4-8 MPa, and feed space velocity 0.2-1.5 h⁻¹. -1 Hydrogen / oil volume ratio 500:1-1000:1.

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