Hydrodesulfurization and denitrification method of high-nitrogen aviation kerosene

Abstract

The invention relates to the field of chemical engineering, and discloses a hydrodesulfurization and denitrification method for high-nitrogen aviation kerosene. The method comprises the following steps: (1) in the presence of hydrogen, carrying out a gas-phase desulfurization reaction on an aviation kerosene raw material in a first hydrogenation reactor to obtain a gas-phase desulfurization reaction product; (2) carrying out gas-liquid separation on the gas-phase desulfurization reaction product to obtain a gas-phase component and a liquid-phase component; (3) pressurizing the liquid-phase component, and then carrying out liquid-phase denitrification reaction in a second hydrogenation reactor to obtain a liquid-phase denitrification reaction product; wherein the content of N in the aviation kerosene raw material is not less than 10 [mu] g / g. The method has the advantages that the high-nitrogen aviation kerosene is used as the raw material to produce the qualified aviation kerosene product under the relatively mild process condition, the chemical reaction efficiency is improved, and the energy consumption and the hydrogen consumption are reduced.

Description

Technical Field

[0001] The present invention relates to the field of chemical industry, and in particular to a method for hydrodesulfurization and denitrification of high-nitrogen aviation fuel. Background Art

[0002] Jet fuel is currently the primary fuel source for both civil and military aircraft. In 2021, despite the severe impact of the COVID-19 pandemic, domestic civil aviation consumption reached 27.02 million tons, a year-on-year increase of 5.8%. Jet fuel is generally produced by hydrogenation. By adapting appropriate hydrogenation catalysts and process technologies, mercaptans are removed from the raw material and stability is improved. While the quality standards for jet fuel do not clearly limit nitrogen content, 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 4 MPa or above is generally required to effectively remove nitrogen compounds.

[0003] However, increasing the reaction pressure not only increases unit energy consumption but also leads to excessive sulfide removal, impairing the lubricity of refined jet fuel and requiring the addition of anti-wear additives, which increases factory costs. Furthermore, at higher reaction pressures, aromatic thiophene sulfides undergo both hydrogenation and hydrogenolysis pathways, with the hydrogenation pathway consuming more hydrogen. Consequently, increasing the unit pressure to remove nitrides results in high energy and hydrogen consumption.

[0004] Patent application CN107233927A discloses a medium-oil hydrocracking catalyst and its preparation method. The modified beta molecular sieve produced by this method exhibits relatively balanced cracking performance, enabling the production of middle distillates with a high smoke point comparable to jet fuel. However, the catalyst is used in conventional fixed-bed hydrogenation technology for jet fuel production, which suffers from 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 to obtain a jet fuel light fraction rich in aromatics, which is recycled back to the hydrocracking unit. The resulting fraction, rich in paraffins, is used as the jet fuel product. However, this method produces a low jet fuel yield, consumes a lot of energy during production, and contains a high paraffin content, which can easily lead to substandard products. Summary of the Invention

[0006] The purpose of the present invention is to overcome the technical problem in the prior art that the removal of sulfides and nitrides in the aviation fuel fraction is placed in the same reaction system, which requires a high reaction pressure and leads to excessive hydrogenation. The present invention provides a method for hydrodesulfurization and denitrification of high-nitrogen aviation fuel. The method uses high-nitrogen aviation fuel as raw material under more moderate process conditions to produce qualified aviation fuel products, while also improving the chemical reaction efficiency and reducing energy consumption and hydrogen consumption.

[0007] In order to achieve the above object, the present invention provides a method for hydrodesulfurization and denitrification of high-nitrogen aviation fuel, wherein the method comprises the following steps: (1) In the presence of hydrogen, the jet fuel raw material is subjected to a gas phase desulfurization reaction in a first hydrogenation reactor to obtain a gas phase desulfurization reaction product; (2) performing gas-liquid separation on the gas-phase desulfurization reaction product to obtain a gas phase component and a liquid phase component; (3) pressurizing the liquid phase component, and then performing a liquid phase denitrogenation reaction in a second hydrogenation reactor to obtain a liquid phase denitrogenation reaction product; Wherein, the nitrogen content in the aviation kerosene raw material is ≮10 μg / g.

[0008] Compared with the prior art, the method of the present invention has the following advantages: The method provided by the present invention realizes desulfurization and denitrification using high-nitrogen aviation kerosene as raw material under milder operating conditions and a simpler process flow, thereby reducing reaction hydrogen consumption.

[0009] In the first hydrogenation reactor, the gas-phase desulfurization reaction can only undergo low-hydrogen consumption desulfurization reaction under low pressure conditions, reducing the hydrogen consumption of the reaction. The liquid phase component after gas-liquid separation is pressurized and undergoes nitride hydrogenation saturation reaction.

[0010] The method provided by the present invention does not require a hydrogen compressor in a fixed-bed reaction system and a circulating oil pump in a liquid-phase hydrogenation reaction system for the entire reaction system, thereby reducing investment costs, simplifying the process flow, improving reaction efficiency, and reducing reaction severity.

[0011] Optimally, by using a high-desulfurization activity catalyst in the first hydrogenation reactor, the desulfurization reaction is controlled to follow a low-hydrogen consumption reaction path, reducing chemical hydrogen consumption. This also reduces the hydrogen-to-oil volume ratio in the first hydrogenation reactor, lowering the reaction severity. Furthermore, controlling the reaction conditions in the first hydrogenation reactor not only facilitates gas-phase desulfurization but also, more importantly, facilitates better coordination with the second hydrogenation reactor, thereby facilitating subsequent denitrification.

[0012] The hydrogen of the present invention does not need to be recycled, thus eliminating the need for a circulating hydrogen compressor and significantly reducing the investment in device construction. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] Figure 1 It is a schematic diagram of the process of the present invention.

[0014] Reference numerals DETAILED DESCRIPTION The endpoints of the ranges and any values ​​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 endpoints of each range, the endpoints of each range and individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered to be specifically disclosed herein.

[0015] The description of the exemplary embodiments is intended to be read in conjunction with the accompanying drawings, which are to be considered a part of the entire written description. In the specification, relative terms such as "lower," "upper," "horizontal," "vertical," "above," "below," "upward," "downward," "top," and "bottom," and their derivatives (e.g., "horizontally," "downwardly," "upwardly," etc.) are to be interpreted as referring to the directions shown in the accompanying drawings being described at the time. These relative terms are for convenience of description and do not require that the device be constructed or operated in a particular orientation. Unless otherwise specified, "connected" as used herein refers to a relationship whereby structures are affixed or connected to each other, directly or indirectly, through intermediate structures.

[0016] In the present invention, the symbol “≯” indicates not greater than, and the symbol “≮” indicates not less than.

[0017] The present invention provides a method for hydrodesulfurization and denitrification of high-nitrogen aviation fuel, wherein the method comprises the following steps: (1) In the presence of hydrogen, the jet fuel raw material is subjected to a gas phase desulfurization reaction in a first hydrogenation reactor to obtain a gas phase desulfurization reaction product; (2) performing gas-liquid separation on the gas-phase desulfurization reaction product to obtain a gas phase component and a liquid phase component; (3) pressurizing the liquid phase component, and then performing a liquid phase denitrogenation reaction in a second hydrogenation reactor to obtain a liquid phase denitrogenation reaction product; Wherein, the nitrogen content in the aviation kerosene raw material is ≮10 μg / g.

[0018] In the present invention, the hydrogen in step (1) can be any hydrogen-containing gas that can provide hydrogen, and can be fresh hydrogen, recycled hydrogen, or hydrogen-rich gas. Those skilled in the art will clearly understand the hydrogen-containing gas described in the present invention after understanding the technical solution of the present invention.

[0019] In the present invention, there is no particular limitation on the properties of the aviation kerosene raw material. The method of the present invention is applicable to the desulfurization and denitrification treatment of aviation kerosene raw materials as conventionally defined in the art. Preferably, in step (1), the initial boiling point of the aviation kerosene raw material is 80-180°C, the final boiling point is 220-300°C, 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 raw material can be exemplified by, but not limited to, 1000μg / g, 2000μg / g, 2500μg / g, etc., and the N content of the aviation kerosene raw material can be exemplified by, but not limited to, 11μg / g, 20μg / g, 30μg / g, etc.

[0020] In the present invention, the inventors have found that by controlling the reaction conditions of the gas-phase desulfurization reaction, only a shallow removal reaction of sulfide occurs, thereby achieving the separation of the desulfurization and denitrification reactions, improving the efficiency of each reaction, and the gas-phase desulfurization reaction is carried out under the bottom pressure, which can greatly save energy consumption. Preferably, in step (1), the conditions of the gas-phase desulfurization reaction include: a temperature of 220-400°C, preferably 230-340°C, for example, 230°C, 240°C, 250°C, 260°C, 270°C, 280°C, 290°C, 300°C, 310°C, 320°C, 330°C, 340°C and values ​​between any two groups, 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 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 the sulfur in the jet fuel raw material is removed, but also some small molecular nitrogen compounds (such as fatty amines) therein are removed.

[0021] In the present 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 aviation kerosene feedstock, more preferably 20-60 wt%, for example, 20 wt%, 25 wt%, 30 wt%, 35 wt%, 40 wt%, 45 wt%, 50 wt%, 55 wt%, 60 wt%, and any values ​​between two groups. By controlling the gas-phase desulfurization reaction so that the sulfur content in the gas-phase desulfurization reaction product is within the above range, the depth of the desulfurization reaction can be controlled, thereby preventing deep desulfurization from affecting the lubricity of the refined aviation kerosene product.

[0022] In the present invention, preferably, the method further comprises, before performing the gas-liquid separation, subjecting the gas-phase desulfurization reaction product to heat exchange and cooling. The present invention achieves energy savings by subjecting the gas-phase desulfurization reaction product in step (1) to a small amount of heat exchange at high temperature, retaining a large amount of reaction heat while ensuring liquefaction of macromolecules, thereby satisfying the feed conditions for the liquid-phase hydrodenitrogenation reaction. In the present invention, the heat exchange can be performed in a heat exchange unit (preferably a heat exchanger). The present invention does not particularly limit the specific type of heat exchanger, and for example, it can be a conventional commercial heat exchanger, such as a tubular heat exchanger.

[0023] The present invention has no particular limitation on the heat exchange conditions, and preferably only needs to ensure that the macromolecular heavy substances in the gas phase desulfurization reaction product are liquefied. The present invention has no particular limitation on the specific operation of the heat exchange, and any heat exchange medium commonly used in the art can be used.

[0024] The present invention has no 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 equilibrium of the effluent after heat exchange, so that the gas phase component flows out upward and the liquid phase component flows out downward. The present invention has a wide range of conditions for selecting the gas-liquid separation. Preferably, based on the total amount of the gas-phase desulfurization reaction product, the mass percentage of the liquid phase component is 1-70%, and more preferably 10-35%. Through the above preferred embodiment, the liquefaction ratio can be accurately controlled so that the macromolecular substances that need further reaction enter the liquid phase component.

[0025] In the present invention, there is no particular limitation on the specific operating conditions and methods of the pressurization. Preferably, a booster pump is used as a boosting unit to pressurize the liquid phase component so that the liquid phase component meets the conditions for the liquid phase denitrogenation reaction. The present invention does not specifically limit the pressurization range.

[0026] In the present invention, the range of selection for the liquid phase denitrification reaction conditions is relatively wide. Preferably, in step (3), the liquid phase denitrification reaction conditions include: a pressure of 1-6 MPa, preferably 2-4 MPa, a temperature of 150-300°C, preferably 220-270°C, and a volume space velocity of 0.1-4 h -1 , preferably 0.5-1.5h -1 .

[0027] In the present 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, preferably 1.5-3 MPa higher. In this preferred embodiment, the reaction is carried out at low to medium pressure, which greatly reduces the severity of the reaction and saves energy.

[0028] In the present invention, the temperature of the liquid-phase denitrification reaction is preferably at least 5° C. lower than that of the gas-phase desulfurization reaction, preferably 10-70° C. lower, and more preferably 10-50° C. lower. In this preferred embodiment, macromolecules requiring further reaction can be liquefied while retaining the heat of reaction.

[0029] In the present invention, the first hydrogenation reactor and the second hydrogenation reactor can be selected from a wide range of types. Preferably, the first hydrogenation reactor and the second hydrogenation reactor are each independently a fixed bed reactor.

[0030] In the present invention, there are no particular limitations on the specific types of catalysts used in the gas-phase desulfurization reaction and the liquid-phase denitrification reaction. Preferably, the gas-phase desulfurization reaction is carried out in the presence of a first hydrorefining catalyst comprising 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 comprising a second support and an active component.

[0031] In the present invention, a wide range of specific types of the first and second supports can be selected. Preferably, the first and second supports are each independently an inorganic refractory oxide, more preferably at least one selected from alumina, amorphous silica-alumina, silica, and titania. In the present invention, the first and second supports may be the same or different, but are preferably the same.

[0032] In the present invention, a wide range of choices is available for the hydrogenation-active metal in the first hydrorefining catalyst. 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.

[0033] In the present invention, preferably, based on the total amount of the first hydrorefining catalyst, the content of the Group VIB metal element calculated as oxide is 10-20 wt%, and the content of the Group VIII metal element calculated as oxide is 1-9 wt%.

[0034] In the present invention, there is no particular limitation on the source of the first hydrorefining catalyst. For example, a commercial hydrorefining catalyst may be used, such as the FH-40 series catalysts developed by Sinopec Fushun Research Institute of Petrochemical (FRIPP): FH-40A and FH-40B catalysts.

[0035] In the present invention, there is no particular limitation on the type of active component in the second hydrotreating catalyst. Preferably, the active component is selected from at least one noble metal element and / or at least one non-noble metal element.

[0036] In the present 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 Group metal elements. Further preferably, the VIB Group metal element is tungsten and / or molybdenum, and the VIII Group metal element is nickel and / or cobalt.

[0037] In the present invention, there are no specific limitations on the content of the components in the second hydrorefining catalyst. Preferably, the content of the Group VIB metal element, calculated as oxide, is 10-20 wt%, and the content of the Group VIII metal element, calculated as oxide, is 1-9 wt%, based on the total amount of the second hydrorefining catalyst. In the present invention, there are no specific limitations on the source of the second hydrorefining catalyst. For example, commercial hydrorefining catalysts such as the FH-40 series catalysts developed by Sinopec Fushun Research Institute of Petrochemicals (FRIPP), including FH-40A and FH-40B, can be used.

[0038] In the present invention, when the active component is a precious metal element, the precious metal element is preferably Pt and / or Pd. In the present invention, the source of the second hydrorefining catalyst is not particularly limited; for example, it can be prepared by any method or commercially available, such as the FHDA-10 catalyst developed by Sinopec Fushun Research Institute of Petrochemicals (FRIPP).

[0039] In the present invention, there is no particular limitation on the application of the gas phase component (also referred to as the hydrogenated light component) and the liquid phase denitrogenation reaction product obtained by gas-liquid separation. They can be adaptively treated according to the specific needs of the product. For example, the gas phase component and the liquid phase denitrogenation reaction product can be treated separately or together, preferably together. Preferably, the method further comprises mixing the gas phase component of step (2) and the liquid phase denitrogenation reaction product of step (3) and then performing a dehydrogenation treatment to obtain a refined aviation fuel product. The present invention does not particularly limit the specific operation and conditions of the dehydrogenation treatment, and it can be carried out according to conventional technical means 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 fuel product is less than 6 μg / g, and the S content is less than 2000 μg / g.

[0040] According to a specific embodiment of the present invention, the aforementioned method of the present invention is as follows Figure 1In the system shown, the aviation kerosene feedstock and hydrogen 1 enter the first hydrogenation reactor 2 for gas-phase desulfurization reaction to obtain a gas-phase desulfurization reaction product 3. The gas-phase desulfurization reaction product 3 enters the heat exchange unit 4 for heat exchange and cooling, and then enters the gas-liquid separation unit 5 for gas-liquid separation to obtain a gas phase component 7 and a liquid phase component 6. The liquid phase component 6 is pressurized by the booster unit 8 and enters the second hydrogenation reactor 9 for liquid-phase denitrogenation reaction to obtain a liquid-phase denitrogenation reaction product 10. The gas phase component 7 and the liquid-phase denitrogenation reaction product 10 are mixed and then stripped in the stripping unit 11 to obtain a refined aviation kerosene product 12.

[0041] The present invention will be further described below with reference to the examples, but it should be understood that the scope of the present invention is not limited by the examples. In the present invention, unless otherwise explicitly stated, percentages and percentage contents are all based on mass.

[0042] The following combination Figure 1 The process flow of the present invention is described in detail.

[0043] The aviation kerosene feedstock and hydrogen 1 enter the first hydrogenation reactor 2, where a gas-phase desulfurization reaction occurs to obtain a gas-phase desulfurization reaction product 3; the gas-phase desulfurization reaction product 3 enters the heat exchange unit 4 (heat exchanger), is cooled by the heat exchanger, and then enters the gas-liquid separation unit 5 (gas-liquid separator) for gas-liquid separation to obtain a gas phase component 7 and a liquid phase component 6. The gas phase component 7 is discharged upward from the gas-liquid separator, and the liquid phase component 6 is discharged downward from the gas-liquid separator, and then passes through the boosting unit 8 (boosting pump) to enter the second hydrogenation reactor 9 to obtain a liquid phase denitrogenation reaction product 10. The gas phase component 7 and the liquid phase denitrogenation reaction product 10 are mixed and enter the stripping unit 11 (stripping tower) to finally obtain a refined aviation kerosene product 12.

[0044] In the following examples and comparative examples, chemical hydrogen consumption refers to the mass percentage of hydrogen consumed per unit mass of raw material.

[0045] The wear scar diameter of refined jet fuel products is measured according to the petrochemical standard SH / T 0687-2017.

[0046] Examples 1-3 Use Figure 1 Schematic diagram of the process. Two 100mL fixed-bed hydrogenation reactors are connected in series: the first and second hydrogenation reactors. A heat exchanger, gas-liquid separator, and booster pump are installed between the reactors. The first hydrogenation reactor is loaded with 20mL of Mo-Co hydrogenation catalyst A, and the second hydrogenation reactor is loaded with 80mL of Mo-Ni hydrogenation catalyst B. A gaseous component outlet is located above the gas-liquid separator. The gaseous component is connected to the bottom effluent of the second hydrogenation reactor (liquid denitrogenation reaction product) and then enters the stripping tower together to obtain the refined jet fuel product.

[0047] High-nitrogen jet fuel was used as the raw material. Catalyst properties are shown in Table 1, raw oil properties are shown in Table 2, and reaction process conditions and results are shown in Table 3.

[0048] Example 4 The same process flow as in Example 1-3 was used, except that the hydrogen-to-oil volume ratio at the gas phase reactor inlet was increased. Catalyst properties are shown in Table 1, feed oil properties are shown in Table 2, and reaction process conditions and results are shown in Table 3.

[0049] Example 5 The same process flow as in Example 1-3 was used, except that the separation conditions for gas-liquid separation were changed. The catalyst properties are shown in Table 1, the feed oil properties are shown in Table 2, and the reaction process conditions and results are shown in Table 3.

[0050] Example 6 The same process flow as in Example 1-3 was used, except that the hydrogen-to-oil volume ratio at the inlet of the first hydrogenation reactor was reduced, and the boosting system (boosting pump) before the liquid phase hydrogenation reactor was changed to a boosting and hydrogen mixing system. 3 The liquid phase component, the hydrogen replenishment amount is 30Nm 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 raw materials and catalyst properties were the same as those in Examples 1-3. The reaction process conditions and results are shown in Table 3.

[0051] Comparative Example 1 A conventional fixed-bed jet fuel hydrogenation process was used, with a hydrogenation reactor installed. The reactor was loaded with 100 mL of Mo-Co hydrogenation catalyst A. Conventional processes, including low-pressure fractionation and stripping, were set up after the reactor to produce the jet fuel product. After hydrogen sulfide removal, the hydrogen was compressed and recycled using a circulating hydrogen compressor. The raw materials and catalyst properties were identical to those in Examples 1-3. The reaction conditions and results are shown in Table 3.

[0052] Table 1 Table 2 Table 3 As can be seen from Table 3, the hydrogen-to-oil volume ratio at the inlet of the first hydrogenation reactor in Example 4 is too large, resulting in difficulty in liquefaction during the gas-liquid separation process. Most of the nitrides enter the gas phase components without hydrogenation reaction, and the product nitrogen content is high. The heat exchange during the gas-liquid separation process of Example 5 is large, and the liquefaction ratio is high, but reheating is required to meet the reaction conditions during the liquid phase reaction, and the energy consumption is relatively high. Example 6 Since the hydrogen consumption of the first hydrogenation reactor is relatively low, the hydrogen-to-oil volume ratio of the gas phase hydrogenation reaction is reduced. However, after the hydrogen partial pressure is reduced, the difficulty of gasifying the raw material becomes larger, and a higher reaction temperature is required, resulting in excessive removal of sulfides and increased energy consumption and hydrogen consumption. At the same time, in order to provide enough hydrogen sources for liquid phase hydrogenation reaction denitrification again, it is necessary to add a hydrogen mixer, resulting in increased investment costs.

[0053] Comparative Example 1 uses conventional fixed-bed hydrogenation technology and a traditional catalyst loading system. The high pressure in the first hydrogenation reactor causes desulfurization and denitrification to occur simultaneously and affect each other. The reaction conditions cannot be optimized for a specific reaction. Sulfide removal is deep under high pressure, affecting product lubricity and increasing hydrogen consumption. Hydrogen recycling also results in high energy consumption. However, the reaction system of the present invention significantly reduces the pressure in the first hydrogenation reactor. By separating desulfurization and denitrification into two reaction systems, the reaction conditions are optimized in a targeted manner, better retaining jet fuel sulfides, improving lubricity, and achieving better denitrification results. Sulfides are removed via hydrogenolysis, reducing hydrogen consumption. Hydrogen does not need to be recycled, reducing energy consumption.

[0054] The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, various simple variations of the technical solution of the present invention may be made, including combining the various technical features in any other appropriate manner. These simple variations and combinations should also be regarded as disclosed in the present invention and fall within the scope of protection of the present invention.

Claims

1. A method for hydrodesulfurization and denitrification of high-nitrogen aviation fuel, characterized in that: The method comprises the following steps: (1) in the presence of hydrogen, subjecting the jet fuel raw material to a gas phase desulfurization reaction in a first hydrogenation reactor to obtain a gas phase desulfurization reaction product; (2) separating the gas-phase desulfurization reaction product into gas-liquid components to obtain a gas-phase component and a liquid-phase component; (3) pressurizing the liquid phase component, and then performing a liquid phase denitrogenation reaction in a second hydrogenation reactor to obtain a liquid phase denitrogenation reaction product; Wherein, the N content in the aviation fuel raw material is ≮10 μg / g.

2. The method according to claim 1, wherein: In step (1), the initial distillation point of the jet fuel raw material is 80-180°C, the final distillation point is 220-300°C, the S content is ≯5000 μg / g, preferably ≯3000 μg / g, and the N content is 11-30 μg / g.

3. The method according to claim 1 or 2, wherein: In step (1), the conditions of the gas phase desulfurization reaction include: temperature of 220-400°C, preferably 230-340°C, hydrogen-to-oil volume ratio of 5-200, preferably 20-100, pressure of 0.1-2MPa, preferably 0.5-1.5MPa, volume space velocity of 0.5-20h -1 , preferably 8-16h -1 ; Preferably, in step (1), the sulfur content in the gas phase desulfurization reaction product is 10-90 wt % of the sulfur content in the aviation kerosene feedstock, more preferably 20-60 wt %.

4. The method according to any one of claims 1 to 3, wherein: The method further comprises, before performing the gas-liquid separation, subjecting the gas-phase desulfurization reaction product to heat exchange and cooling; Preferably, based on the total amount of the gas phase desulfurization reaction product, the mass percentage of the liquid phase component is 1-70%, and more preferably 10-35%.

5. The method according to any one of claims 1 to 4, wherein: In step (3), the conditions of the liquid phase denitrification reaction include: pressure of 1-6 MPa, preferably 2-4 MPa, temperature of 150-300°C, preferably 220-270°C, volume space velocity of 0.1-4 h -1 , preferably 0.5-1.5h -1 .

6. The method according to any one of claims 1 to 5, wherein: The pressure of the liquid phase denitrification reaction is at least 1 MPa higher than the pressure of the gas phase desulfurization reaction, and preferably 1.5-3 MPa higher.

7. The method according to any one of claims 1 to 6, wherein: The temperature of the liquid phase denitrification reaction is at least 5°C lower than the temperature of the gas phase desulfurization reaction, and preferably 10-70°C lower.

8. The method according to any one of claims 1 to 7, wherein: The first hydrogenation reactor and the second hydrogenation reactor are each independently a fixed bed reactor.

9. The method according to any one of claims 1 to 8, wherein: The gas phase desulfurization reaction is carried out in the presence of a first hydrofining catalyst, wherein the first hydrofining catalyst comprises a first carrier and a hydrogenation active metal; Preferably, the liquid phase denitrogenation reaction is carried out in the presence of a second hydrotreating catalyst, wherein the second hydrotreating catalyst comprises a second carrier and an active component; Preferably, the first carrier and the second carrier are each independently an inorganic refractory oxide, further preferably at least one selected from alumina, amorphous silica-alumina, silica and titania; Preferably, the hydrogenation active metal is selected from at least one of the metal elements of Group VIB and / or at least one of the metal elements of Group VIII; Preferably, the active component is selected from at least one of the noble metal elements and / or at least one of the non-noble metal elements.

10. The method according to any one of claims 1 to 9, wherein: The method further comprises mixing the gas phase component of step (2) with the liquid phase denitrification reaction product of step (3) and then performing a hydrogen sulfide removal treatment to obtain a refined jet fuel product; Preferably, the N content in the refined jet fuel product is below 6 μg / g, and the S content is below 2000 μg / g.

Images