Hydrodesulfurization and denitrification methods for high-nitrogen jet fuel

Abstract

This invention relates to the chemical industry and discloses a method for hydrodesulfurization and denitrification of high-nitrogen jet fuel. The method includes the following steps: (1) in the presence of hydrogen, the jet fuel raw material undergoes a gas-phase desulfurization reaction in a first hydrotreating reactor to obtain a gas-phase desulfurization reaction product; (2) the gas-phase desulfurization reaction product is subjected to gas-liquid separation to obtain a gas phase component and a liquid phase component; (3) the liquid phase component is pressurized and then subjected to a liquid-phase denitrification reaction in a second hydrotreating reactor to obtain a liquid-phase denitrification reaction product; wherein the nitrogen content in the jet fuel raw material is ≥10 μg / g. This method allows for the production of qualified jet fuel products under more moderate process conditions using high-nitrogen jet fuel as raw material, while also improving chemical reaction efficiency and reducing energy and hydrogen consumption.

Description

Technical Field

[0001] This invention relates to the field of chemical engineering, and specifically to a method for hydrodesulfurization and denitrification of high-nitrogen jet fuel. Background Technology

[0002] Aviation kerosene is currently the primary fuel source for both civilian and military aircraft. In 2021, despite the severe impact of the pandemic, domestic aviation aviation consumption reached 27.02 million tons, a year-on-year increase of 5.8%. Aviation kerosene is generally produced using the hydrogenation process, which involves removing mercaptans from the raw materials and improving stability by using suitable hydrogenation catalysts and technologies. Although there are no explicit restrictions on nitrogen content in aviation kerosene quality standards, indicators such as color stability and operational stability are significantly correlated with nitrogen content. Therefore, when processing high-nitrogen raw materials, a reaction pressure of over 4 MPa is generally required to achieve effective removal of nitrogen oxides.

[0003] However, increasing the reaction pressure not only increases the energy consumption of the unit but also causes excessive removal of sulfides, resulting in poor lubricity of refined jet fuel and requiring the addition of anti-wear agents, thus increasing the cost at the factory. Simultaneously, under higher reaction pressures, thiophene sulfides containing aromatic rings follow both hydrogenation and hydrogenolysis pathways, with the hydrogenation pathway consuming more hydrogen. Therefore, using the method of increasing unit pressure to remove nitrides results in high energy and hydrogen consumption.

[0004] Patent application CN107233927A discloses a medium-oil type hydrocracking catalyst and its preparation method. This method uses a modified β-molecular sieve with relatively balanced cracking performance, resulting in middle distillate oil with the high smoke point characteristic of jet fuel. However, the conventional fixed-bed hydrocracking process used to produce jet fuel with this catalyst suffers from drawbacks such as high hydrogen and energy consumption and low jet fuel yield.

[0005] Patent application CN111088072A discloses a hydrocracking method for reducing the bromine index of heavy naphtha and increasing the smoke point of jet fuel. This method involves fractionating the hydrorefined and hydrocracking oil products, resulting in a light jet fuel component rich in aromatics, which is recycled back to the hydrocracking unit. The component rich in alkanes obtained from the fractionation is used as the jet fuel product. However, this method produces a low jet fuel yield, consumes a large amount of energy during production, and the product contains a high content of alkanes, which can easily lead to product defects. Summary of the Invention

[0006] The purpose of this invention is to overcome the technical problems of existing technologies, such as the removal of sulfides and nitrogen oxides in aviation kerosene fractions being carried out in the same reaction system, requiring high reaction pressure and leading to excessive hydrogenation. This invention provides a method for hydrodesulfurization and denitrification of high-nitrogen aviation kerosene. This method uses high-nitrogen aviation kerosene as raw material under more moderate process conditions to produce qualified aviation kerosene products, while also improving chemical reaction efficiency and reducing energy consumption and hydrogen consumption.

[0007] To achieve the above objectives, the present invention provides a method for hydrodesulfurization and denitrification of high-nitrogen jet fuel, wherein the method includes the following steps:

[0008] (1) In the presence of hydrogen, the jet fuel is subjected to gas-phase desulfurization reaction in the first hydrogenation reactor to obtain gas-phase desulfurization reaction products;

[0009] (2) The gas phase desulfurization reaction products are subjected to gas-liquid separation to obtain gas phase components and liquid phase components;

[0010] (3) The liquid phase component is pressurized and then carried out in the second hydrogenation reactor to obtain the liquid phase denitrification reaction product;

[0011] The nitrogen content in the aviation kerosene raw material is ≥10 μg / g.

[0012] Compared with the prior art, the method of the present invention has the following advantages:

[0013] The method provided by this invention achieves desulfurization and denitrification of high-nitrogen jet fuel under more moderate operating conditions and a simpler process flow, while reducing hydrogen consumption in the reaction.

[0014] In the first hydrogenation reactor, the gas-phase desulfurization reaction can occur under low-pressure conditions with low hydrogen consumption, thus reducing hydrogen consumption. The liquid phase component after gas-liquid separation undergoes a nitride hydrogenation saturation reaction after pressurization.

[0015] The method provided by this invention eliminates the need for a hydrogen compressor in a fixed-bed reaction system and a circulating oil pump in a liquid-phase hydrogenation reaction system, thereby reducing investment costs, simplifying the process flow, improving reaction efficiency, and reducing the severity of the reaction.

[0016] In a preferred embodiment, by using a highly active desulfurization catalyst in the first hydrogenation reactor, the desulfurization reaction is controlled to follow a low-hydrogen-consumption reaction pathway, reducing the chemical hydrogen consumption of the desulfurization reaction. This also lowers the hydrogen-to-oil volume ratio in the first hydrogenation reactor, reducing the severity of the reaction. Furthermore, controlling the reaction conditions in the first hydrogenation reactor is not only for gas-phase desulfurization but also, more importantly, for better coordination with the second hydrogenation reactor, thus facilitating subsequent nitrogen removal.

[0017] The hydrogen produced by this invention does not require recycling, eliminating the need for a circulating hydrogen compressor and significantly reducing investment in equipment construction. Attached Figure Description

[0018] Figure 1 This is a schematic diagram of the process flow of the present invention.

[0019] Figure Labels

[0020] Detailed Implementation

[0021] 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.

[0022] The description of exemplary embodiments is intended to be read in conjunction with the accompanying drawings, which are considered an integral part of the entire written description. In this specification, relative terms such as “lower,” “upper,” “horizontal,” “vertical,” “above,” “below,” “upward,” “downward,” “top,” and “bottom,” and their derivatives (e.g., “horizontally,” “downward,” “upward,” etc.) should be interpreted as referring to the orientation shown in the accompanying drawings as described at the time. These relative terms are for ease of description and do not require the device to be constructed or operated in a particular orientation. Unless otherwise stated, “connection” as used in this invention refers to a relationship in which structures are directly or indirectly fixed or connected to each other via an intermediate structure.

[0023] In this invention, the symbol “≯” indicates not greater than, and the symbol “≮” indicates not less than.

[0024] This invention provides a method for hydrodesulfurization and denitrification of high-nitrogen jet fuel, wherein the method includes the following steps:

[0025] (1) In the presence of hydrogen, the jet fuel is subjected to gas-phase desulfurization reaction in the first hydrogenation reactor to obtain gas-phase desulfurization reaction products;

[0026] (2) The gas phase desulfurization reaction products are subjected to gas-liquid separation to obtain gas phase components and liquid phase components;

[0027] (3) The liquid phase component is pressurized and then carried out in the second hydrogenation reactor to obtain the liquid phase denitrification reaction product;

[0028] The nitrogen content in the aviation kerosene raw material is ≥10 μg / g.

[0029] In this invention, the hydrogen gas mentioned in step (1) can be any hydrogen-containing gas capable of providing hydrogen, including fresh hydrogen, recycled hydrogen, and hydrogen-rich gas. Those skilled in the art, after understanding the technical solution of this invention, can clearly understand the hydrogen-containing gas described in this invention.

[0030] In this invention, the properties of the aviation kerosene feedstock are not particularly limited, and the method of this invention is applicable to the desulfurization and denitrification treatment of aviation kerosene feedstock as conventionally defined in the art. Preferably, in step (1), the initial boiling point of the aviation kerosene feedstock is 80-180℃, the final boiling point is 220-300℃, the S content is ≤5000μg / g, preferably ≤3000μg / g, and the N content is 11-30μg / g. For example, the S content of the aviation kerosene feedstock can be, but is not limited to: 1000μg / g, 2000μg / g, 2500μg / g, etc., and the N content of the aviation kerosene feedstock can be, but is not limited to: 11μg / g, 20μg / g, 30μg / g, etc.

[0031] In this invention, the inventors discovered that by controlling the reaction conditions of the gas-phase desulfurization reaction, only a shallow removal reaction of sulfides occurs, thereby separating the desulfurization and denitrification reactions, improving their respective reaction efficiencies, and the gas-phase desulfurization reaction is carried out under a pressure that can greatly save energy consumption. Preferably, in step (1), the conditions of the gas-phase desulfurization reaction include: a temperature of 220-400℃, preferably 230-340℃, for example, 230℃, 240℃, 250℃, 260℃, 270℃, 280℃, 290℃, 300℃, 310℃, 320℃, 330℃, 340℃ and any two of these values; a hydrogen-to-oil volume ratio of 5-200, preferably 20-100; a pressure of 0.1-2MPa, preferably 0.5-1.5MPa; and a volume hourly space velocity of 0.5-20h. -1 Preferably 8-16h -1 It should be noted that during the gas-phase hydrogenation reaction in step (1), not only will sulfur be removed from the jet fuel, but also some small molecule nitrogen compounds (such as aliphatic amines) will be removed.

[0032] In this invention, preferably, in step (1), the sulfur content in the gas-phase desulfurization reaction product is 10-90 wt% of the sulfur content of the jet fuel raw material, more preferably 20-60 wt%, for example, it can be 20 wt%, 25 wt%, 30 wt%, 35 wt%, 40 wt%, 45 wt%, 50 wt%, 55 wt%, 60 wt%, or any value between any two groups. By controlling the gas-phase desulfurization reaction, the sulfur content in the gas-phase desulfurization reaction product is kept within the above range, thus controlling the depth of the desulfurization reaction and avoiding the impact of deep desulfurization on the lubricity of the refined jet fuel product.

[0033] In this invention, preferably, the method further includes cooling the gas-phase desulfurization reaction product by heat exchange before performing the gas-liquid separation. This invention achieves the feeding conditions for the liquid-phase hydrodenitrification reaction by performing a small amount of heat exchange on the gas-phase desulfurization reaction product in step (1) under high temperature conditions, thus retaining a large amount of reaction heat while ensuring the liquefaction of macromolecules, thereby saving energy. In this invention, the heat exchange can be performed in a heat exchange unit (preferably a heat exchanger). This invention does not particularly limit the specific type of heat exchanger; for example, it can be a conventional commercial heat exchanger, such as a tubular heat exchanger.

[0034] This invention does not impose any particular limitation on the heat exchange conditions, but preferably, conditions sufficient to ensure the liquefaction of large molecular weight heavy substances in the gas-phase desulfurization reaction products are met. This invention also does not impose any particular limitation on the specific operation of the heat exchange; any heat exchange medium conventionally used in the art can be employed.

[0035] This invention does not impose any particular limitation on the gas-liquid separation in step (2), which can be carried out in a gas-liquid separator. The gas-liquid separation is used to establish a gas-liquid balance in the effluent after heat exchange, allowing the gas phase component to flow upwards and the liquid phase component to flow downwards. This invention allows for a wide range of conditions for the gas-liquid separation. Preferably, based on the total amount of the gas-phase desulfurization reaction products, the mass percentage of the liquid phase component is 1-70%, more preferably 10-35%. Through the above preferred embodiments, the liquefaction ratio can be accurately controlled, allowing the macromolecular substances that require further reaction to enter the liquid phase component.

[0036] In this invention, there are no particular limitations on the specific operating conditions and methods of pressurization. In a preferred case, a booster pump is used as a pressurization unit to pressurize the liquid phase component so that the liquid phase component meets the conditions for liquid phase denitrification reaction. In this invention, there are no particular limitations on the pressurization range.

[0037] In this invention, the selection range for liquid-phase denitrification reaction conditions is relatively wide. Preferably, in step (3), the conditions for the liquid-phase denitrification reaction include: a pressure of 1-6 MPa, preferably 2-4 MPa; a temperature of 150-300℃, preferably 220-270℃; and a volume hourly space velocity of 0.1-4 h⁻¹. -1 Preferably, it is 0.5-1.5h. -1 .

[0038] In this invention, preferably, the pressure of the liquid-phase denitrification reaction is at least 1 MPa higher than the pressure of the gas-phase desulfurization reaction, and more preferably 1.5-3 MPa higher. Under this preferred embodiment, the reaction is carried out at medium to low pressure, which greatly reduces the severity of the reaction and saves energy.

[0039] In this invention, preferably, the temperature of the liquid-phase denitrification reaction is at least 5°C lower than the temperature of the gas-phase desulfurization reaction, more preferably 10-70°C lower, and even more preferably 10-50°C lower. Under this preferred embodiment, macromolecules requiring further reaction can be liquefied while retaining the heat of reaction.

[0040] In this invention, a wide range of types can be selected for the first hydrogenation reactor and the second hydrogenation reactor. Preferably, the first hydrogenation reactor and the second hydrogenation reactor are each independently a fixed-bed reactor.

[0041] In this invention, there is no particular limitation on the specific types of catalysts used in the gas-phase desulfurization and liquid-phase denitrification reactions. Preferably, the gas-phase desulfurization reaction is carried out in the presence of a first hydrorefining catalyst, which comprises a first support and a hydrogenation-active metal. Preferably, the liquid-phase denitrification reaction is carried out in the presence of a second hydrorefining catalyst, which comprises a second support and an active component.

[0042] In this invention, the specific types of the first and second carriers can be selected from a wide range. Preferably, the first and second carriers are each independently an inorganic refractory oxide, and more preferably at least one selected from alumina, amorphous aluminum silica, silicon dioxide, and titanium dioxide. In this invention, the first and second carriers can be the same or different, but are preferably the same.

[0043] In this invention, the range of hydrogenation active metals selected for the first hydrogenation refining catalyst is relatively wide. Preferably, the hydrogenation active metal includes at least one group VIB metal element and / or at least one group VIII metal element; more preferably, the group VIB metal element is tungsten and / or molybdenum, and the group VIII metal element is nickel and / or cobalt.

[0044] In this invention, preferably, based on the total amount of the first hydrorefining catalyst, the content of the VIB metal element (calculated as oxide) is 10-20 wt%, and the content of the VIII metal element (calculated as oxide) is 1-9 wt%.

[0045] In this invention, there is no particular limitation on the source of the first hydrorefining catalyst. For example, commercially available hydrorefining catalysts can be used, such as the FH-40 series catalysts developed by the Sinopec Fushun Petrochemical Research Institute (FRIPP): FH-40A and FH-40B catalysts.

[0046] In this invention, there is no particular limitation on the type of active component in the second hydrorefining catalyst. Preferably, the active component is selected from at least one noble metal element and / or at least one non-noble metal element.

[0047] In this invention, preferably, when the active component is a non-precious metal element, the non-precious metal element is selected from at least one of the VIB metal elements and / or at least one of the VIII metal elements. More preferably, the VIB metal element is tungsten and / or molybdenum, and the VIII metal element is nickel and / or cobalt.

[0048] In this invention, the content of each component in the second hydrorefining catalyst is not particularly limited. Preferably, based on the total amount of the second hydrorefining catalyst, the content of the VIB metal element (calculated as oxide) is 10-20 wt%, and the content of the VIII metal element (calculated as oxide) is 1-9 wt%. In this invention, the source of the second hydrorefining catalyst is not particularly limited. For example, commercially available hydrorefining catalysts can be used, such as the FH-40 series catalysts developed by the Fushun Petrochemical Research Institute of Sinopec (FRIPP): FH-40A and FH-40B catalysts.

[0049] In this invention, preferably, when the active component is a noble metal element, the noble metal element is Pt and / or Pd. In this invention, the source of the second hydrorefining catalyst is not particularly limited; for example, it can be prepared by any method or obtained commercially, such as the FHDA-10 catalyst developed by the Fushun Petrochemical Research Institute (FRIPP) of Sinopec.

[0050] In this invention, there are no particular limitations on the application of the gas phase component (also known as the hydrogenated light component) and the liquid phase denitrification reaction product obtained by gas-liquid separation. Adaptive processing can be performed according to the specific needs of the product. For example, the gas phase component and the liquid phase denitrification reaction product can be processed separately or together, preferably together. Preferably, the method further includes mixing the gas phase component from step (2) and the liquid phase denitrification reaction product from step (3) and then performing a hydrogen sulfide removal treatment to obtain refined aviation kerosene. This invention does not particularly limit the specific operation and conditions of the hydrogen sulfide removal treatment; it can be carried out according to conventional techniques in the art, preferably by steam stripping. The steam stripping can be carried out in a stripping unit, such as a stripping tower. Preferably, the N content in the refined aviation kerosene product is below 6 μg / g, and the S content is below 2000 μg / g.

[0051] According to a specific embodiment of the present invention, the aforementioned method of the present invention is carried out as follows: Figure 1The system is as follows: jet fuel and hydrogen 1 enter the first hydrogenation reactor 2 for gas-phase desulfurization reaction to obtain gas-phase desulfurization product 3. The gas-phase desulfurization product 3 enters the heat exchange unit 4 and, after being cooled by heat exchange, enters the gas-liquid separation unit 5 for gas-liquid separation to obtain gas phase component 7 and liquid phase component 6. The liquid phase component 6 is pressurized by the pressurization unit 8 and then enters the second hydrogenation reactor 9 for liquid-phase denitrification reaction to obtain liquid-phase denitrification product 10. The gas phase component 7 and the liquid-phase denitrification product 10 are mixed and then subjected to stripping unit 11. After stripping, refined jet fuel product 12 is obtained.

[0052] The present invention will be further described below with reference to embodiments, but it should be understood that the scope of protection of the present invention is not limited to the embodiments. In the present invention, unless otherwise expressly stated, percentages and contents are all expressed by mass.

[0053] The following is combined Figure 1 The process flow of the present invention will be described in detail.

[0054] The jet fuel and hydrogen 1 enter the first hydrogenation reactor 2, where a gas-phase desulfurization reaction occurs, yielding a gas-phase desulfurization product 3. The gas-phase desulfurization product 3 enters the heat exchange unit 4 (heat exchanger), where it is cooled and then enters the gas-liquid separation unit 5 (gas-liquid separator) for gas-liquid separation, yielding a gas phase component 7 and a liquid phase component 6. The gas phase component 7 is discharged upwards from the gas-liquid separator, while the liquid phase component 6 is discharged downwards. After passing through the pressurization unit 8 (pressurization pump), the mixture enters the second hydrogenation reactor 9, yielding a liquid phase denitrification reaction product 10. The gas phase component 7 and the liquid phase denitrification reaction product 10 are mixed and then enter the stripping unit 11 (stripping tower), ultimately yielding refined jet fuel product 12.

[0055] In the following examples and comparative examples, chemical hydrogen consumption refers to the percentage of hydrogen mass consumed per unit mass of raw material.

[0056]

[0057] The wear mark diameter of refined aviation kerosene products was determined according to the SH / T 0687-2017 petrochemical standard.

[0058] Examples 1-3

[0059] Adopting such Figure 1The process flow diagram is shown below. Two 100mL fixed-bed hydrogenation reactors are connected in series, designated as the first and second hydrogenation reactors. A heat exchanger, a gas-liquid separator, and a booster pump are installed between the reactors. The first hydrogenation reactor is loaded with 20mL of Mo-Co type hydrogenation catalyst A, and the second hydrogenation reactor is loaded with 80mL of Mo-Ni type hydrogenation catalyst B. A gas phase component outlet is located above the gas-liquid separator. The gas phase component is connected to the bottom effluent (liquid phase denitrification reaction product) of the second hydrogenation reactor and then enters the stripping tower together to obtain refined jet fuel.

[0060] High-nitrogen jet fuel was used as the feedstock. Catalyst properties are shown in Table 1, feedstock oil properties are shown in Table 2, and reaction process conditions and results are shown in Table 3.

[0061] Example 4

[0062] The same process flow as in Examples 1-3 was used, except that the hydrogen-to-oil volume ratio at the inlet of the gas-phase reactor was increased. Catalyst properties are shown in Table 1, feedstock properties in Table 2, and reaction process conditions and results in Table 3.

[0063] Example 5

[0064] The same process flow as in Examples 1-3 was used, except that the gas-liquid separation conditions were changed. Catalyst properties are shown in Table 1, feedstock properties are shown in Table 2, and reaction process conditions and results are shown in Table 3.

[0065] Example 6

[0066] The process flow is the same as in Examples 1-3, except that the hydrogen-to-oil volume ratio at the inlet of the first hydrogenation reactor is reduced, and the pressurization system (booster pump) before the liquid-phase hydrogenation reactor is replaced with a pressurization and hydrogen mixing system, relative to 1m 3 The liquid phase component has a hydrogen replenishment amount of 30 Nm. 3 The first hydrogenation reactor was loaded with 20 mL of Mo-Co type hydrogenation catalyst A, and the second hydrogenation reactor was loaded with 80 mL of Mo-Ni type hydrogenation catalyst B. The properties of the raw materials and catalysts were the same as in Examples 1-3, and the reaction process conditions and results are shown in Table 3.

[0067] Comparative Example 1

[0068] A conventional fixed-bed hydrogenation process for aviation kerosene was adopted, with one hydrogenation reactor. The reactor was loaded with 100 mL of Mo-Co type hydrogenation catalyst A. Following the reactor, conventional processes such as low-temperature fractionation and stripping were performed to obtain the aviation kerosene product. Hydrogen gas, after being desulfurized, was pressurized and recycled using a circulating hydrogen compressor. The properties of the raw materials and catalyst were the same as in Examples 1-3, and the reaction process conditions and results are shown in Table 3.

[0069] Table 1

[0070]

[0071] Table 2

[0072]

[0073] Table 3

[0074]

[0075] As shown in Table 3, in Example 4, the hydrogen-to-oil volume ratio at the inlet of the first hydrogenation reactor was too high, leading to difficulties in liquefaction during gas-liquid separation. Most of the nitrogen compounds entered the gas phase without undergoing hydrogenation, resulting in a high nitrogen content in the product. In Example 5, the gas-liquid separation process involved significant heat exchange and a high liquefaction rate, but reheating was required during the liquid phase reaction to meet reaction conditions, resulting in high energy consumption. In Example 6, because the hydrogen consumption of the first hydrogenation reactor was low, the hydrogen-to-oil volume ratio for the gas-phase hydrogenation reaction was reduced. However, the reduced hydrogen partial pressure made the gasification of the feedstock more difficult, requiring a higher reaction temperature, leading to excessive removal of sulfides and increased energy and hydrogen consumption. Furthermore, to provide sufficient hydrogen again for denitrification in the liquid-phase hydrogenation reaction, a hydrogen mixer was needed, increasing investment costs.

[0076] Comparative Example 1 employs conventional fixed-bed hydrogenation technology and a traditional catalyst loading system. The high pressure in the first hydrogenation reactor leads to simultaneous and mutually influential desulfurization and denitrification, making it impossible to optimize reaction conditions for any single reaction. Sulfides are removed to a greater depth under high pressure, affecting product lubricity and resulting in high hydrogen consumption; hydrogen is recycled, leading to high energy consumption. In contrast, the reaction system of this invention, with a significantly reduced pressure in the first hydrogenation reactor, separates desulfurization and denitrification into two reaction systems, allowing for targeted optimization of reaction conditions. This results in better retention of jet fuel sulfides, improved lubricity, and better denitrification; sulfides are removed via hydrogenolysis, reducing hydrogen consumption; and hydrogen does not need to be recycled, further reducing energy consumption.

[0077] 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 hydrodesulfurization and denitrification of high-nitrogen jet fuel, characterized in that, The method includes the following steps: (1) In the presence of hydrogen, the jet fuel is subjected to gas-phase desulfurization reaction in the first hydrogenation reactor to obtain gas-phase desulfurization reaction products; (2) The gas phase desulfurization reaction products are subjected to gas-liquid separation to obtain gas phase components and liquid phase components; (3) The liquid phase component is pressurized and then carried out in the second hydrogenation reactor to obtain the liquid phase denitrification reaction product; The nitrogen content in the aviation kerosene raw material is ≥10 μg / g; The pressure of the liquid-phase denitrification reaction is at least 1 MPa higher than the pressure of the gas-phase desulfurization reaction; In step (3), the conditions for the liquid-phase denitrification reaction include: a pressure of 2-4 MPa, a temperature of 220-270 °C, and a volume hourly space velocity of 0.5-1.5 h⁻¹. -1 ; In step (1), the conditions for the gas-phase desulfurization reaction include: a temperature of 220-340℃, a hydrogen-to-oil volume ratio of 20-100, a pressure of 0.1-2 MPa, and a volume hourly space velocity of 0.5-20 h⁻¹. -1 ; In step (1), the sulfur content in the gas-phase desulfurization reaction products is 10-90 wt% of the sulfur content of the jet fuel. Based on the total amount of the gas-phase desulfurization reaction products, the mass percentage of the liquid phase component is 10-35%; The temperature of the liquid-phase denitrification reaction is at least 5°C lower than the temperature of the gas-phase desulfurization reaction. The method further includes mixing the gas phase component described in step (2) with the liquid phase denitrification reaction product described in step (3) and then performing desulfurization treatment to obtain refined aviation kerosene product.

2. The method according to claim 1, wherein, In step (1), the initial boiling point of the jet fuel is 80-180℃, the final boiling point is 220-300℃, the S content is ≤5000μg / g, and the N content is 11-30μg / g.

3. The method according to claim 2, wherein, S content ≤ 3000 μg / g.

4. The method according to any one of claims 1-3, wherein, In step (1), the conditions for the gas-phase desulfurization reaction include: a temperature of 230-340℃, a hydrogen-to-oil volume ratio of 30-100, a pressure of 0.5-1.5 MPa, and a volume hourly space velocity of 8-16 h⁻¹. -1 .

5. The method according to any one of claims 1-3, wherein, In step (1), the sulfur content in the gas phase desulfurization reaction product is 20-60 wt% of the sulfur content of the jet fuel.

6. The method according to any one of claims 1-3, wherein, The method also includes cooling the gas-phase desulfurization reaction products by heat exchange before performing the gas-liquid separation.

7. The method according to any one of claims 1-3, wherein, Based on the total amount of the gas-phase desulfurization reaction products, the mass percentage of the liquid phase component is 20-35%.

8. The method according to any one of claims 1-3, wherein, The pressure of the liquid-phase denitrification reaction is 1.5-3 MPa higher than that of the gas-phase desulfurization reaction.

9. The method according to any one of claims 1-3, wherein, The temperature of the liquid-phase denitrification reaction is 10-70°C lower than the temperature of the gas-phase desulfurization reaction.

10. The method according to any one of claims 1-3, wherein, The first hydrogenation reactor and the second hydrogenation reactor are each independently a fixed-bed reactor.

11. The method according to any one of claims 1-3, wherein, The gas-phase desulfurization reaction is carried out in the presence of a first hydrorefining catalyst, which includes a first support and a hydrorefining active metal.

12. The method according to claim 11, wherein, The liquid-phase denitrification reaction is carried out in the presence of a second hydrorefining catalyst, which includes a second support and an active component.

13. The method according to claim 12, wherein, The first carrier and the second carrier are each independently inorganic refractory oxides.

14. The method according to claim 13, wherein, The first carrier and the second carrier are each independently selected from at least one of alumina, amorphous aluminum silica, silicon dioxide and titanium oxide.

15. The method according to claim 11, wherein, The hydrogenated active metal is selected from at least one group VIB metal element and / or at least one group VIII metal element.

16. The method according to claim 12, wherein, The active component is selected from at least one of noble metal elements and / or at least one of non-noble metal elements.

17. The method according to any one of claims 1-3, wherein, The refined aviation kerosene product contains less than 6 μg / g of nitrogen and less than 2000 μg / g of sulfur.

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