A hydrocracking process for jet fuel

Abstract

The present invention discloses a hydrocracking treatment process for jet fuel, wherein the treatment process is to mix jet fuel and hydrogen and then enter a reactor, wherein the reactor includes a hydrocracking reaction zone and a hydrofining reaction zone according to the material flow direction, and the materials are contacted with the catalyst in the reactor for reaction, and the reaction material flow is separated to obtain light naphtha, heavy naphtha and tail oil; wherein the hydrocracking reaction zone is provided with a first hydrocracking catalyst bed, a second hydrocracking catalyst bed and a third hydrocracking catalyst bed; and the hydrofining reaction zone is filled with a hydrofining catalyst. The process solves the problems of low conversion depth, product quality and selectivity when using the existing hydrocracking process and catalyst to treat jet fuel by adjusting the catalyst grading system.

Description

Technical Field

[0001] The invention belongs to the technical field of petrochemical industry and relates to a hydrocracking process, in particular to a hydrocracking process using jet fuel as raw material. Background Art

[0002] With the overcapacity of domestic refining and the vigorous development of the new energy vehicle sector, the current development trend of refining and chemical companies has been adjusted from reducing the diesel-to-gasoline ratio to "oil conversion" and "oil-to-special", that is, the production target has been shifted from fuel products to chemical raw materials and special oil products. The hydrocracking process has become the core device for improving the quality and efficiency, transformation and upgrading of refining and chemical companies due to its advantages such as a wide range of processed raw materials and flexible product structure; currently, the industry has a relatively mature application of wax oil and diesel fraction hydrocracking process, which can efficiently convert wax oil and diesel fraction into catalytic reforming raw materials and steam cracking raw materials.

[0003] Since jet fuel is positioned as a growing demand in the development of the petrochemical industry, it is believed that jet fuel has good economic value. At present, the research on jet fuel is mainly focused on how to further improve the quality of the product. However, when the aviation industry reduces its carrying capacity due to objective reasons, jet fuel will also face the problem of overcapacity. At this time, it is necessary to find a new and efficient processing route for it, so that when the production is in excess, the product structure can be adjusted by adjusting the processing route to improve its economic value, thereby ensuring the benefits of the production enterprise. Combined with the actual situation that the market demand for chemical raw materials is relatively high, if the development of jet fuel to produce chemical raw materials is an economically valuable route, there is no report on the industrial application of research on hydrocracking using jet fuel as raw material.

[0004] CN106520195A discloses a hydrocracking method for improving the quality of aviation kerosene, which adds an aviation kerosene fractionation tower in addition to the conventional fractionation tower to separate the aviation kerosene into a light aviation kerosene fraction, a medium aviation kerosene fraction and a heavy aviation kerosene fraction, and improves the product quality by extracting the medium aviation kerosene fraction.

[0005] CN103773487A discloses a catalytic cracking diesel hydrocracking method, which is characterized in that part of the fraction (190°C to 300°C) is recycled to the inlet of the hydrocracking reactor to improve the feed hydrocarbon composition of the hydrocracking reaction zone, thereby increasing the gasoline fraction yield and its octane number.

[0006] CN100443572C discloses a hydrocracking method for producing diesel from high-nitrogen raw materials, which is characterized by providing two hydrorefining reaction zones, and the first hydrorefining reaction product is subjected to gas-liquid separation in a flash tank to achieve processing of inferior raw materials under mild process conditions. Summary of the invention

[0007] In view of the above problems existing in the prior art, the applicant proposed to use the hydrocracking process to treat jet fuel. However, due to the great difference between the properties of jet fuel and the existing hydrocracking raw materials, the existing mature hydrocracking process cannot be directly applied. After research, the applicant adjusted the catalyst system and realized the conversion of jet fuel into high-value light naphtha, heavy naphtha and tail oil products through the hydrocracking process. It not only broadened the "raw material pool" of hydrocracking, but also conducted high value-added hydrocracking process research on the common first-line fractions that have not entered the hydrocracking processing range. At the same time, high value-added products can be obtained, among which heavy naphtha can be used as catalytic reforming feed, and tail oil and light naphtha can be used as ethylene cracking raw materials. The process solves the problems of low conversion depth, product quality and selectivity when using the existing hydrocracking process and catalyst to treat jet fuel by adjusting the catalyst grading system.

[0008] In view of the deficiencies in the prior art, the present invention aims to provide a hydrocracking process for jet fuel. The main contents of the technical solution are as follows:

[0009] A hydrocracking process for jet fuel, wherein the jet fuel and hydrogen are mixed and then introduced into a reactor, wherein the reactor includes a hydrocracking reaction zone and a hydrofining reaction zone according to the material flow direction, and the jet fuel is contacted with a catalyst in the reactor for reaction, and the reaction material flow is separated to obtain light naphtha, heavy naphtha and tail oil;

[0010] The hydrocracking reaction zone is provided with a first hydrocracking catalyst bed, a second hydrocracking catalyst bed and a third hydrocracking catalyst bed; the hydrorefining reaction zone is filled with a hydrorefining catalyst.

[0011] Furthermore, in the hydrocracking process of the jet fuel, the nitrogen content of the jet fuel is generally not higher than 100 mg / kg, preferably not higher than 30 mg / kg, the sulfur content is not particularly limited, the initial boiling point of the jet fuel is generally 150-200° C., and the final boiling point is generally 250-290° C. Specifically, it can be selected from one or more of straight run jet fuel and secondary processed jet fuel.

[0012] Furthermore, in the above-mentioned jet fuel hydrocracking process, the volume of the hydrocracking reaction zone accounts for 50% to 95%, preferably 60% to 80%, of the total catalyst loading volume of the reactor.

[0013] Furthermore, in the above jet fuel hydrocracking process, the volume of the hydrotreating reaction zone accounts for 5% to 50%, preferably 20% to 40%, of the total catalyst loading volume of the reactor.

[0014] Furthermore, in the above-mentioned hydrocracking treatment process of jet fuel, the carrier of the hydrocracking catalyst HC1 in the first hydrocracking catalyst bed is Y molecular sieve, and the content of Y molecular sieve is F1% of the weight of the catalyst; the carrier of the hydrocracking catalyst HC2 in the second hydrocracking catalyst bed is Y molecular sieve and β molecular sieve, and the content of the carrier is F2% of the weight of the catalyst, and the weight ratio of Y molecular sieve to β molecular sieve is 0.5-5, preferably 0.8-1.2; the carrier of the hydrocracking catalyst HC3 in the third hydrocracking catalyst bed is β molecular sieve, and the content of β molecular sieve is F3% of the weight of the catalyst. In a further preferred case, F1 / F2>1.1, F2 / F3>1.2.

[0015] Furthermore, in the above-mentioned hydrocracking process of jet fuel, the volume ratio of the first hydrocracking catalyst bed, the second hydrocracking catalyst bed, and the third hydrocracking catalyst bed is generally 30% to 80%: 10% to 50%: 10% to 50%, preferably 35% to 55%: 25% to 35%: 20% to 30%.

[0016] Furthermore, in the above-mentioned jet fuel hydrocracking treatment process, the pore volume of the hydrocracking catalyst in the first hydrocracking catalyst bed is 0.20-0.40 mL / g, preferably 0.25-0.37 mL / g, and the active metal component content is 20 wt%-35 wt%, preferably 22 wt%-28 wt%, based on the weight of the catalyst and calculated as metal oxide.

[0017] Furthermore, in the above-mentioned jet fuel hydrocracking treatment process, the pore volume of the hydrocracking catalyst in the second hydrocracking catalyst bed is 0.18 to 0.38 mL / g, preferably 0.23 to 0.35 mL / g, and the active metal component content is 18 wt% to 33 wt%, preferably 20 wt% to 28 wt%, based on the weight of the catalyst and calculated as metal oxide.

[0018] Furthermore, in the above-mentioned jet fuel hydrocracking treatment process, the pore volume of the hydrocracking catalyst in the third hydrocracking catalyst bed is 0.16-0.35 mL / g, preferably 0.20-0.25 mL / g, and the active metal component content is 15wt%-30wt%, preferably 18wt%-22wt%, based on the weight of the catalyst and calculated as metal oxide.

[0019] Furthermore, in the above-mentioned jet fuel hydrocracking treatment process, the pore volume of the hydrotreating catalyst loaded in the hydrotreating reaction zone is 0.15-0.30 mL / g, preferably 0.18-0.25 mL / g, and Co and Mo are used as active metals. The active metal component content is 20 wt%-30 wt%, preferably 22 wt%-25 wt%, calculated as metal oxide, based on the weight of the catalyst.

[0020] Furthermore, in the above-mentioned jet fuel hydrocracking process, the reaction operating conditions are as follows: reaction temperature is 280-400°C, preferably 300-390°C; hydrogen partial pressure is 2-12MPa, preferably 5-8MPa; hydrogen-oil volume ratio is 100-1000, preferably 200-500; volume space velocity is 0.5-3h -1 , preferably 0.1 to 2 hours -1 .

[0021] Furthermore, in the above-mentioned jet fuel hydrocracking process, a hydrogenation pretreatment reaction zone is arranged on the upper part of the hydrocracking reaction zone according to the flow direction of the liquid phase material, and the volume of the hydrogenation pretreatment reaction zone accounts for 0% to 8% of the catalyst loading volume of the reactor. When the nitrogen content of the jet fuel feedstock is not higher than 10 mg / kg, there is no need to set up a hydrogenation pretreatment reaction zone.

[0022] Furthermore, in the above-mentioned jet fuel hydrocracking process, a hydropretreatment catalyst is loaded in the hydropretreatment reaction zone, wherein the hydropretreatment catalyst uses Ni-W and Ni-Mo as active metals, the pore volume of the catalyst is 0.25-0.50 mL / g, preferably 0.28-0.35 mL / g, and the content of the active metal component is 18 wt%-38 wt% based on the weight of the catalyst and calculated as metal oxide, preferably 20 wt%-25 wt%. The hydropretreatment catalyst may also contain an additive, which may be F and / or Mg, and the content of the additive is 0.5 wt%-5 wt%, preferably 1 wt%-2 wt%.

[0023] In summary, the jet fuel hydrocracking process provided by the present invention has the following technical advantages:

[0024] 1. This application originally proposes to use a hydrocracking process to produce chemical raw materials using jet fuel as raw material, and specifically proposes to use a reverse processing flow of "cracking-refining". The jet fuel directly enters the cracking reaction zone for reaction, which can significantly improve the yield and selectivity of the heavy naphtha fraction that can be used as a reforming raw material, and can also improve the aromatic potential content of the heavy naphtha and the liquid product yield of the device. However, the hydrocracking process of refining first and then cracking will inevitably cause the jet fuel to be oversaturated in the refining reaction zone and undergo a partial ring-opening reaction. The fraction obtained after refining will then enter the cracking reaction zone and will undergo excessive cracking, resulting in a decrease in the yield and selectivity of the heavy naphtha, and a corresponding decrease in the aromatic potential content of the heavy naphtha and the liquid yield of the device.

[0025] 2. In the jet fuel hydrocracking process provided by the present invention, hydrocracking catalysts with different acidic functions are loaded by grading, and the reaction path of jet fuel is designed according to the "molecular" oil refining concept. Aromatic hydrocarbons in jet fuel with larger polarity will be preferentially adsorbed on the acidic sites of the catalyst, and the stronger the acidity, the greater the tendency of ring-opening cracking reaction. According to the reaction law of jet fuel in the reactor, hydrocracking catalysts with different acidities are loaded from top to bottom. First, the upper part of the reactor has the largest ring-opening task, so the top part is loaded with a cracking catalyst with a strong ring-opening ability containing a Y molecular sieve, and the aromatic hydrocarbons and polycyclic cycloalkanes are saturated and ring-opened. The polycyclic cycloalkanes obtained with the saturation of aromatic hydrocarbons and the polycyclic cycloalkanes rich in the raw materials will further react on the cracking catalyst containing Y / β molecular sieve with moderate ring-opening ability. Finally, the β molecular sieve with weaker ring-opening function and the alumina in the hydrorefining catalyst will jointly provide acidic sites to prevent excessive acidity from causing further cracking of the monocyclic cyclic hydrocarbons of the target component, thereby significantly increasing the yield of the heavy naphtha fraction.

[0026] 3. In the jet fuel hydrocracking process provided by the present invention, due to the targeted setting of the reaction path, the hydrorefining catalyst is set at the lower part of the reactor, which will reduce the overall required reaction temperature and chemical hydrogen consumption. This is because the activity of the hydrocracking catalyst is higher, and a lower inlet temperature can ensure that it fully reacts. At the same time, due to the reaction heat released by the hydrocracking process, the temperature at the bottom of the reactor where the hydrorefining catalyst is located is relatively high, so that its activity can be exerted, realizing the rational use of heat. In addition, since the reaction temperature of the hydrorefining catalyst at the bottom of the reactor in the technical solution of this application is higher than the temperature of the upper part of the reactor where it is located in the existing process, the higher temperature will inhibit the hydrogenation function of the hydrorefining catalyst and promote it to exert more acidic function, so that hydrogen consumption is reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 The figure is a schematic diagram of the process flow of the jet fuel hydrocracking treatment according to the present invention.

[0028] Among them, 1-jet fuel feedstock; 2-new hydrogen; 3-hydrocracking reactor; 4-hydrogenation pretreatment reaction zone; 5-first hydrocracking catalyst bed; 6-second hydrocracking catalyst bed; 7-third hydrocracking catalyst bed; 8-hydrogenation refining reaction zone; 9-reaction effluent; 10-gas-liquid separator; 11-liquid phase material; 12-fractionation tower; 13-gas; 14-light naphtha; 15-heavy naphtha; 16-tail oil; 17-gas phase material; 18-circulating hydrogen compressor; 19-circulating hydrogen. DETAILED DESCRIPTION

[0029] The technical scheme and technical effects of the present invention are further described below in conjunction with the accompanying drawings and specific implementation methods.

[0030] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.

[0031] In this document, for the convenience of description, spatial relative terms such as "below", "below", "down", "above", "above", "upper", etc. may be used to describe the relationship between one element or feature and another element or feature in the accompanying drawings. It should be understood that the spatial relative terms are intended to include different orientations of the object in use or operation in addition to the orientation depicted in the figure. For example, if the object in the figure is turned over, the element described as being "below" or "below" other elements or features will be oriented "above" the element or feature. Therefore, the exemplary term "below" can include both below and above. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatial relative terms used in this document should be interpreted accordingly.

[0032] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.

[0033]

[0043] All numerical values ​​for parameters (eg, amounts or conditions) herein are to be understood as being modified in all instances by the term "about," whether or not "about" actually appears before the numerical value.

[0034] Combined with Figure 1The specific process of the jet fuel hydrocracking treatment process of the present invention is as follows: the jet fuel raw material 1 and hydrogen (including new hydrogen 1 and recycled hydrogen 19) are mixed and then enter the hydrocracking reactor 3, and the reactor includes an optionally set hydrocracking pretreatment reaction zone 4 according to the material flow direction, and the hydrocracking reaction zone is filled with a hydrocracking catalyst, and the hydrocracking reaction zone is provided with a first hydrocracking catalyst bed HC1 (5), a second hydrocracking catalyst bed HC2 (6), and a third hydrocracking catalyst bed HC1 (5). Cracking catalyst bed HC3 (7), hydrofining reaction zone 8, wherein the hydrofining reaction zone is filled with a hydrofining catalyst, and the jet fuel and hydrogen are contacted with the catalyst in the reactor to react, and the reaction stream 9 first enters the gas-liquid separator 10 for separation to obtain a gas phase material 17 and a liquid phase material 11, and the gas phase stream 17 is compressed by the circulating hydrogen compressor 18 and used as circulating hydrogen 19; the liquid phase stream 11 enters the fractionation tower, and after separation, a gas 13, light naphtha 14, heavy naphtha 15 and tail oil 16 are obtained;

[0035] Example 1

[0036] use Figure 1 The catalyst grading scheme of the jet fuel hydrocracking method is shown in Table 2. The properties of the used catalysts are shown in Table 2. Jet fuel 1 is used as the raw material. The properties of the oil product are shown in Table 1. The process conditions and experimental results are listed in Table 3. The reactor is divided into two catalyst loading areas from top to bottom. The upper middle part is the hydrocracking area, and the volume of this area accounts for 80% of the catalyst loading volume of the reactor; the lower part is the hydrorefining area, and the volume of this area accounts for 20% of the catalyst loading volume of the reactor. The hydrocracking area is loaded with hydrocracking catalyst HC1, hydrocracking catalyst HC2 and hydrocracking catalyst HC3 from top to bottom, and the loading volume percentages are 35%, 35% and 30% respectively. The hydrorefining area is loaded with hydrorefining catalyst HR2.

[0037] Example 2

[0038] use Figure 1 The catalyst grading scheme of the jet fuel hydrocracking method is shown in Table 2. The properties of the used catalysts are shown in Table 2. Jet fuel 2 is used as the raw material. The properties of the oil product are shown in Table 1. The process conditions and experimental results are listed in Table 3. The reactor is divided into three catalyst loading areas from top to bottom. The upper part is the flexible hydrogenation area, and the volume of this area accounts for 3% of the catalyst loading volume of the reactor; the middle part is the hydrocracking area, and the volume of this area accounts for 75% of the catalyst loading volume of the reactor; the lower part is the hydrorefining area, and the volume of this area accounts for 22% of the catalyst loading volume of the reactor. The flexible hydrogenation area is loaded with HR1 catalyst, and the hydrocracking area is loaded with HC1, HC2 and HC3 hydrocracking catalysts from top to bottom, and the loading volume percentages are 55%, 25% and 20% respectively. The hydrorefining area is loaded with HR2 hydrorefining catalyst.

[0039] Comparative Example 1

[0040] The conventional process route of refining first and then cracking was adopted, with jet fuel 1 as the raw material. The properties of the oil are shown in Table 1, and the process conditions and experimental results are listed in Table 3. The refined catalyst used was HR1, and the cracking section was graded from top to bottom with HC1, HC2 and HC3 hydrocracking catalysts, with the filling volume percentages being 35%, 35% and 30% respectively.

[0041] Comparative Example 2

[0042] The conventional refining followed by cracking process was adopted, with aviation kerosene 1 as the raw material. The properties of the oil are shown in Table 1, and the process conditions and experimental results are listed in Table 3. The refining catalyst used was HR1, and the cracking section was loaded with HC2 hydrocracking catalyst.

[0043] Comparative Example 3

[0044] use Figure 1 The catalyst grading scheme of the aviation kerosene hydrocracking method is shown in Table 2. The properties of the catalyst used are shown in Table 2. Aviation kerosene 2 is used as the raw material. The properties of the oil are shown in Table 1. The process conditions and experimental results are listed in Table 3. The reactor is divided into three catalyst loading areas from top to bottom. The upper part is the flexible hydrogenation area, and the volume of this area accounts for 3% of the reactor catalyst loading volume; the middle part is the hydrocracking area, and the volume of this area accounts for 75% of the reactor catalyst loading volume; the lower part is the hydrorefining area, and the volume of this area accounts for 22% of the reactor catalyst loading volume. The flexible hydrogenation area is loaded with HR1 catalyst, and the hydrocracking area is self-loaded with HC1 hydrocracking catalyst. The hydrorefining area is loaded with HR2 hydrorefining catalyst.

[0045] Table 1 Raw oil properties

[0046] project Aviation kerosene raw materials 1 Aviation kerosene raw materials 2 <![CDATA[Density (20 °C), kg / m 3 > 788.0 776.0 S, wt% 66 525 N, mg / kg 3.4 12 Distillation range, ℃ D-86 D-86 HK 155 140 10％ 170 158 50％ 190 178 90％ 220 208 KK 250 260

[0047] Table 2 Physicochemical properties of catalysts

[0048] catalyst HR1 HR2 HC1 HC2 HC3 Chemical composition, wt% <![CDATA[WO3]]> 20.1 --- --- --- --- NiO 3.4 --- 3.5 2.5 1.5 <![CDATA[MoO3]]> --- 19.8 20.5 18.8 16.5 CoO --- 3.8 --- --- --- Mg 1.2 1.8 --- --- --- <![CDATA[Pore volume, m 2 ·g -1 > 0.32 0.20 0.28 0.25 0.22 Y molecular sieve, % --- --- 34 15 --- β molecular sieve, % --- --- --- 15 23

[0049] Table 3 Comparative Example Process Conditions and Reaction Effects

[0050]

[0051] The above embodiments and comparative examples show that the hydrocracking process of aviation kerosene invented by the present invention can significantly increase the yield and selectivity of the target product heavy naphtha, and at the same time, the aromatics potential content of the heavy naphtha and the liquid yield of the device are also significantly increased.

Claims

1. A hydrocracking process for jet fuel, wherein the jet fuel and hydrogen are mixed and then introduced into a reactor, wherein the reactor includes a hydrocracking reaction zone and a hydrofining reaction zone according to the material flow direction, and the jet fuel is contacted with a catalyst in the reactor for reaction, and the reaction material flow is separated to obtain light naphtha, heavy naphtha and tail oil; in, The hydrocracking reaction zone is provided with a first hydrocracking catalyst bed, a second hydrocracking catalyst bed, and a third hydrocracking catalyst bed; the hydrofining reaction zone is filled with a hydrofining catalyst; the carrier of the hydrocracking catalyst HC1 in the first hydrocracking catalyst bed is a Y molecular sieve, the carrier of the hydrocracking catalyst HC2 in the second hydrocracking catalyst bed is a Y molecular sieve and a β molecular sieve, and the carrier of the hydrocracking catalyst HC3 in the third hydrocracking catalyst bed is a β molecular sieve; The Y molecular sieve content in the hydrocracking catalyst HC1 in the first hydrocracking catalyst bed is F1% of the catalyst weight, the carrier content in the hydrocracking catalyst HC2 in the second hydrocracking catalyst bed is F2% of the catalyst weight, and the weight ratio of the Y molecular sieve to the β molecular sieve is 0.5-5; the β molecular sieve content in the hydrocracking catalyst HC3 in the third hydrocracking catalyst bed is F3% of the catalyst weight; F1 / F2>1.1, F2 / F3>1.

2.

2. The hydrocracking process for jet fuel according to claim 1, characterized in that: The nitrogen content of jet fuel shall not exceed 100 mg / kg.

3. The hydrocracking process for jet fuel according to claim 1 or 2, characterized in that: The nitrogen content of jet fuel shall not exceed 30 mg / kg.

4. The hydrocracking process for jet fuel according to claim 1 or 2, characterized in that: The initial distillation point of jet fuel is 150-200°C, and the final distillation point is 250-290°C.

5. The hydrocracking process for jet fuel according to claim 1, characterized in that: The volume of the hydrocracking reaction zone accounts for 50% to 95% of the total catalyst loading volume of the reactor.

6. The hydrocracking process for jet fuel according to claim 1 or 5, characterized in that: The volume of the hydrocracking reaction zone accounts for 60% to 80% of the total catalyst loading volume of the reactor.

7. The hydrocracking process for jet fuel according to claim 1, characterized in that: The volume of the hydrotreating reaction zone accounts for 5% to 50% of the catalyst loading volume of the reactor.

8. The hydrocracking process for jet fuel according to claim 1 or 7, characterized in that: The volume of the hydrotreating reaction zone accounts for 20% to 40% of the catalyst loading volume of the reactor.

9. The hydrocracking process for jet fuel according to claim 1, characterized in that: The carrier content of the hydrocracking catalyst HC2 in the second hydrocracking catalyst bed is F2% of the catalyst weight, and the weight ratio of the Y molecular sieve to the β molecular sieve is 0.8-1.

2.

10. The hydrocracking process for jet fuel according to claim 1, characterized in that: The volume ratio of the first hydrocracking catalyst bed, the second hydrocracking catalyst bed and the third hydrocracking catalyst bed is 30% to 80%: 10% to 50%: 10% to 50%.

11. The hydrocracking process for jet fuel according to claim 1 or 10, characterized in that: The volume ratio of the first hydrocracking catalyst bed, the second hydrocracking catalyst bed and the third hydrocracking catalyst bed is 35% to 55%: 25% to 35%: 20% to 30%.

12. The hydrocracking process for jet fuel according to claim 1, characterized in that: The pore volume of the hydrocracking catalyst HC1 in the first hydrocracking catalyst bed is 0.20-0.40 mL / g, and the active metal component content is 20 wt%-35 wt% in terms of metal oxide based on the catalyst weight.

13. The hydrocracking process for jet fuel according to claim 1 or 12, characterized in that: The pore volume of the hydrocracking catalyst HC1 in the first hydrocracking catalyst bed is 0.25-0.37 mL / g, and the active metal component content is 22 wt%-28 wt% in terms of metal oxides based on the catalyst weight.

14. The hydrocracking process for jet fuel according to claim 1, characterized in that: The pore volume of the hydrocracking catalyst HC2 in the second hydrocracking catalyst bed is 0.18-0.38 mL / g, and the active metal component content is 18 wt%-33 wt% in terms of metal oxides based on the catalyst weight.

15. The hydrocracking process for jet fuel according to claim 1 or 14, characterized in that: The pore volume of the hydrocracking catalyst HC2 in the second hydrocracking catalyst bed is 0.23-0.35 mL / g, and the active metal component content is 20 wt%-28 wt% in terms of metal oxides based on the catalyst weight.

16. The hydrocracking process for jet fuel according to claim 1, characterized in that: The pore volume of the hydrocracking catalyst HC3 in the third hydrocracking catalyst bed is 0.16-0.35 mL / g, and the active metal component content is 15 wt%-30 wt% in terms of metal oxide based on the catalyst weight.

17. The hydrocracking process for jet fuel according to claim 1 or 16, characterized in that: The pore volume of the hydrocracking catalyst HC3 in the third hydrocracking catalyst bed is 0.20-0.25 mL / g, and the active metal component content is 18 wt%-22 wt% in terms of metal oxides based on the weight of the catalyst.

18. The hydrocracking process for jet fuel according to claim 1, characterized in that: The pore volume of the hydrotreating catalyst loaded in the hydrotreating reaction zone is 0.15-0.30 mL / g, Co and Mo are used as active metals, and the content of active metal components is 20 wt%-30 wt% based on the weight of the catalyst and calculated as metal oxides.

19. The hydrocracking process for jet fuel according to claim 1 or 18, characterized in that: The pore volume of the hydrotreating catalyst loaded in the hydrotreating reaction zone is 0.18-0.25 mL / g, Co and Mo are used as active metals, and the content of active metal components is 22 wt%-25 wt% based on the weight of the catalyst and calculated as metal oxides.

20. The hydrocracking process for jet fuel according to claim 1, characterized in that: The reaction operating conditions are as follows: reaction temperature is 280-400°C, hydrogen partial pressure is 2-12 MPa, hydrogen-oil volume ratio is 100-1000, and volume space velocity is 0.5-3 h -1 .

21. The hydrocracking process for jet fuel according to claim 1, characterized in that: The reaction operating conditions are as follows: reaction temperature is 300-390°C, hydrogen partial pressure is 5-8MPa, hydrogen-oil volume ratio is 200-500, and volume space velocity is 0.1-2h -1 .

22. The hydrocracking process for jet fuel according to claim 1, characterized in that: A hydrogenation pretreatment reaction zone is arranged on the upper part of the hydrocracking reaction zone according to the flow direction of the liquid phase material. The volume of the hydrogenation pretreatment reaction zone accounts for 0% to 8% of the catalyst loading volume of the reactor. When the nitrogen content of the jet fuel feedstock is not higher than 10 mg / kg, there is no need to arrange a hydrogenation pretreatment reaction zone.

23. The hydrocracking process for jet fuel according to claim 22, characterized in that: The hydrogenation pretreatment reaction zone is filled with a hydrogenation pretreatment catalyst, wherein the hydrogenation pretreatment catalyst uses Ni-W and Ni-Mo as active metals, the pore volume of the catalyst is 0.25-0.50 mL / g, and the content of the active metal component is 18wt%-38wt% based on the weight of the catalyst and calculated as metal oxide. The hydrogenation pretreatment catalyst optionally contains an additive, which is F and / or Mg, and the content of the additive is 0.5wt%-5wt%.

24. The hydrocracking process for jet fuel according to claim 22 or 23, characterized in that: The hydrogenation pretreatment reaction zone is filled with a hydrogenation pretreatment catalyst, wherein the hydrogenation pretreatment catalyst uses Ni-W and Ni-Mo as active metals, the pore volume of the catalyst is 0.28-0.35 mL / g, and the content of the active metal component is 20wt%-25wt% based on the weight of the catalyst and calculated as metal oxide. The hydrogenation pretreatment catalyst optionally contains an additive, which is F and / or Mg, and the content of the additive is 1wt%-2wt%.

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