A process and apparatus for producing aviation kerosene

Abstract

The present application relates to the technical fields of chemical synthesis, and discloses a kind of aviation kerosene production process and equipment, production process includes: carbon source gas, hydrogen, circulating gas is sent into main reactor reaction and obtains including hydrocarbon, methanol, CO, water and unreacted gas mixed component a;Mixed component a is sent into cascade reactor and is prepared to obtain including aviation kerosene component, light hydrocarbon component and water mixed component b, wherein light hydrocarbon component includes one or more of C2-C7 light hydrocarbon;Mixed component b is fractionally condensed to collect liquid phase and gas phase, and liquid phase is carried out three-phase separation to obtain aviation kerosene component, light hydrocarbon component and water respectively, aviation kerosene component is hydrotreated, fractionation to obtain aviation kerosene.The present application realizes the step-by-step control of reaction path in carbon source hydrogenation process through the synergistic effect of main reactor and cascade reactor, improves the selectivity of aviation kerosene target product, so that the obtained product meets the 3# aviation kerosene standard requirements in key indicators such as distillation range distribution, aromatic content and low temperature performance.

Description

Technical Field

[0001] This invention relates to the field of chemical synthesis technology, specifically to a process and equipment for producing aviation kerosene. Background Technology

[0002] Aviation fuel is an indispensable energy source in the air transport system, and its quality indicators and airworthiness safety requirements are typically regulated by international standards such as ASTM D1655. Currently, aviation kerosene mainly relies on conventional refining processes, obtaining corresponding fractions through crude oil distillation and hydrorefining. This route has advantages in terms of industrial maturity and fuel performance stability, but its carbon source is entirely dependent on fossil resources, inevitably generating large amounts of greenhouse gas emissions throughout its entire life cycle.

[0003] With the continued recovery and growth of global air transport demand, aviation fuel consumption is constantly increasing, highlighting the growing problems of fossil-based aviation kerosene in terms of carbon emissions, resource sustainability, and energy security. On the one hand, fossil resource reserves are limited and prices fluctuate significantly, making long-term stable supply uncertain. On the other hand, under the existing refining system, the emission reduction potential of fossil-based aviation kerosene routes is gradually approaching saturation, and the marginal benefits of further reducing carbon emissions are continuously declining. Developing green aviation fuels based on non-fossil carbon sources, while meeting the airworthiness and safety requirement of "direct deployment," has become an important research direction in this field.

[0004] Existing research has attempted to prepare aviation fuel components via catalytic conversion using syngas or carbon dioxide as carbon sources. For example, patent publication number CN110624483A discloses a multi-stage fluidized bed reactor and reaction circulation system for one-step synthesis of aromatics from syngas. This technology uses syngas as raw material, with aromatic compounds as the main target product. However, this technical route still relies on fossil-derived syngas and cannot directly realize the resource utilization of carbon dioxide, thus contributing limitedly to mitigating carbon dioxide emissions.

[0005] Furthermore, patent publication number CN121135550A discloses a process and system for producing aromatics by carbon dioxide hydrogenation. This technology uses carbon dioxide as a carbon source, which represents a certain advancement in carbon source selection. However, this technology suffers from low selectivity of the target product, with the obtained product being mainly aromatics. It can typically only be used as an additive component in aviation fuel and cannot directly meet the requirements of aviation kerosene for distillation range distribution, aromatic content, and overall performance. Therefore, it cannot be directly used as a full-component aviation kerosene. Additionally, this patent employs a fixed-bed single-stage reactor structure with a high reaction temperature, posing challenges in scale-up design and long-term continuous operation. Furthermore, fixed-bed reactors generally face difficulties in online activation and complex catalyst replacement during industrial operation.

[0006] Although a large number of catalysts and reaction pathways have been studied in recent years in the fields of carbon dioxide hydrogenation and syngas conversion, and there are many related literature and laboratory research reports, most of the existing technologies focus on obtaining some aviation kerosene components or specific types of hydrocarbon products. The products obtained cannot simultaneously meet the requirements of the No. 3 aviation kerosene standard in terms of key indicators such as distillation range distribution, aromatic content, and low temperature performance. The stable preparation of full-component aviation kerosene that meets the current aviation fuel standards has not yet been achieved. Summary of the Invention

[0007] This invention provides a process and equipment for producing aviation kerosene, which solves the problem that the reaction path of existing aviation kerosene is relatively simple, and the target products are mostly aromatics or aviation kerosene component oils, making it difficult to directly obtain full-component aviation kerosene that meets the No. 3 aviation kerosene standard.

[0008] In a first aspect, the present invention provides a jet fuel production process, comprising the following steps: (1) Carbon source gas, hydrogen, and circulating gas are fed into the main reactor to react and obtain a mixed component a including hydrocarbons, methanol, CO, water and unreacted gas; (2) The mixed component a is fed into a cascade reactor to prepare a mixed component b, which includes jet fuel component, light hydrocarbon component and water, wherein the light hydrocarbon component includes one or more of C2-C7 light hydrocarbons; wherein C2-C7 light hydrocarbons refer to hydrocarbon compounds with 2 to 7 carbon atoms, including one or more of alkanes, alkenes, cycloalkanes and aromatic hydrocarbons. (3) The mixed component b is condensed and collected in stages to obtain liquid and gas phases. The liquid phase is then separated into three phases to obtain jet fuel component, light hydrocarbon component and water. The jet fuel component is then hydrogenated, refined and fractionated to obtain jet fuel.

[0009] The aviation kerosene production process provided by this invention first feeds carbon source gas, hydrogen, and recycle gas into the main reactor for hydrogenation reaction, preferentially generating a mixed component a containing intermediate components such as hydrocarbons and methanol. Mixed component a is then fed into a cascade reactor for further conversion, allowing processes such as methanol dehydration, olefin polymerization, and carbon chain growth to proceed stepwise. This helps reduce the uncontrolled product distribution caused by multiple reactions occurring simultaneously in a single reactor, increases the proportion of target components in aviation kerosene within the C8-C18 range, and suppresses the excessive generation of lighter components such as C2-C7 light hydrocarbons. Simultaneously, by performing staged condensation and three-phase separation on mixed component b, the separation and recovery of aviation kerosene components, light hydrocarbon components, and water can be effectively achieved. This ensures that the aviation kerosene components have a relatively stable composition before entering subsequent hydrogenation refining and fractionation, thereby facilitating the acquisition of target products that meet the requirements of aviation kerosene fractions, improving carbon source utilization efficiency, and enhancing the continuity and stability of the entire process.

[0010] In one optional implementation, in step (1), the carbon source gas includes one or two of syngas and carbon dioxide; wherein the syngas is mainly composed of carbon monoxide, carbon dioxide and hydrogen.

[0011] In one optional embodiment, the ratio of the total number of moles of CO2 and CO in the circulating gas to the number of moles of hydrogen is 1:(1.5 to 3); for example, the mole ratio is 1:1.5, 1:2, or 1:3.

[0012] In this invention, the ratio of the total number of moles of CO2 and CO in the circulating gas to the number of moles of hydrogen refers to the ratio between the sum of the moles of CO2 and CO in the circulating gas and the number of moles of hydrogen in the feed gas. The content of CO2 and CO in the circulating gas can be detected using existing gas composition analysis methods, such as gas chromatography to detect the volume fraction or mole fraction of each gas component in the circulating gas, and then calculating the moles of CO2 and CO based on the total flow rate of the circulating gas. The number of moles of hydrogen in the feed gas can be calculated based on the composition of the feed gas and the feed flow rate, or by performing gas chromatography on the feed gas and then calculating based on the total flow rate of the feed gas. Therefore, the ratio of the total number of moles of CO2 and CO in the circulating gas to the number of moles of hydrogen in the feed gas can be further calculated.

[0013] In one optional embodiment, in step (1), the reaction temperature in the main reactor is 270°C to 400°C; for example, the reaction temperature is 270°C, 280°C, 300°C, 350°C, or 400°C.

[0014] In one optional embodiment, in step (1), the reaction pressure in the main reactor is 1.0~8.0 MPa; for example, the reaction pressure is 1.0 MPa, 2.0 MPa, 5.0 MPa, 6.0 MPa, or 8.0 MPa.

[0015] In one optional embodiment, in step (2), the reaction temperature in the cascade reactor is 270°C to 400°C; for example, the reaction temperature is 270°C, 280°C, 300°C, 350°C, or 400°C.

[0016] In one alternative embodiment, in step (2), the reaction pressure in the cascade reactor is 1.0~8.0 MPa. For example, the reaction pressure is 1.0 MPa, 2.0 MPa, 5.0 MPa, 6.0 MPa, or 8.0 MPa.

[0017] In one alternative implementation, in step (3), the mixed component b exchanges heat with the feed to the main reactor and then undergoes staged condensation.

[0018] In one optional embodiment, in step (3), the feed to the main reactor exchanges heat with the mixed component b to 250°C to 350°C; for example: heat exchange to 250°C, 270°C, 290°C, 300°C, 320°C, 350°C.

[0019] In an optional embodiment, in step (3), the staged condensation includes cooling the mixed component b at a temperature of 55°C to 80°C to separate the liquid phase and the gas phase, cooling the gas phase again at a temperature of 30°C to 50°C to separate the liquid phase and the gas phase, and collecting the staged condensed liquid phase for three-phase separation. Preferably, the cooling method for the second cooling includes one or more of the following: condenser cooling and oil washing cooling; Preferably, the oil washing and cooling process adopts a counter-current contact method with air intake at the bottom and oil intake at the top.

[0020] In this invention, the oil washing cooling refers to using liquid oil as the absorption and heat exchange medium, allowing the gas phase to come into countercurrent contact with the liquid oil. The liquid oil absorbs some of the hydrocarbon components in the gas phase and carries away heat, thereby achieving further cooling of the gas phase and component separation. Preferably, the oil washing cooling employs a countercurrent contact method with bottom-inlet air and top-inlet oil.

[0021] In an optional implementation, in step (3), the gas phase obtained by cooling and separation again is split, a portion of which is compressed to 1.0~8.0 MPa and reused as circulating gas in step (1), and the other portion is discharged as release gas. Preferably, the purge gas is fed into a purge gas recovery system, where hydrogen is recovered through membrane separation, and the recovered hydrogen is reused in step (1).

[0022] In one optional embodiment, in step (1), the main reactor is selected from a fluidized bed reactor or a fixed bed reactor; wherein, the fixed bed reactor is provided at least once; preferably, the main reactor is filled with a metal oxide-molecular sieve composite catalyst. The metal oxide-molecular sieve composite catalyst refers to a catalyst formed by combining a metal oxide component and a macroporous molecular sieve component. Specifically, on a dry basis, the catalyst comprises 10%–50% macroporous molecular sieve, 5%–50% Fe₂O₃, 0.10%–15% CoO, 0.10%–10% MnO₂, 0.1%–5% K₂O, 0.10%–25% ZnO, 0.10%–30% Cr₂O₃, 0.10%–5% Ce₂O₃, 0.10%–30% SiO₂, and 0.10%–30% ZrO₂; the macroporous molecular sieve is selected from at least one of Beta molecular sieve, Y-type molecular sieve, MCM-41 molecular sieve, and mordenite.

[0023] The metal oxide-molecular sieve composite catalyst can be prepared by co-precipitation combined with molecular sieve composite. Specifically, a metal salt solution containing iron, cobalt, manganese, zinc and cerium is first mixed with a precipitant solution under stirring conditions. After filtration and washing, a filter cake containing a metal oxide precursor is obtained. Then, Beta molecular sieve and silica sol are added to form a slurry. After spray drying and calcination, the metal oxide-molecular sieve composite catalyst is obtained.

[0024] In one optional embodiment, in step (2), the cascade reactor is a fixed-bed reactor, and the fixed-bed reactor is filled with a molecular sieve catalyst; preferably, the molecular sieve catalyst includes one or more of ZSM-5 molecular sieve, Beta molecular sieve, Y-type molecular sieve and mordenite.

[0025] Secondly, the present invention provides aviation kerosene production equipment, comprising: The main reactor is connected to a temperature control system; A cascade reactor, in which the outlet of the main reactor is connected to the inlet of the cascade reactor; A staged condenser is constructed by connecting the outlet of a cascade reactor to the inlet of the staged condenser. The three-phase separator has its inlet connected to the outlet of the staged condenser. The hydrorefining system connects the jet fuel component outlet of the three-phase separator to the inlet of the hydrorefining system for the purpose of hydrogenating jet fuel. Preferably, the staged condenser includes at least a primary condenser and a secondary condenser, the outlet of the cascade reactor is connected to the inlet of the primary condenser, the exhaust port of the primary condenser is connected to the inlet of the secondary condenser, and the liquid outlets of the primary and secondary condensers are connected to the inlet of the three-phase separator. Alternatively, the staged condenser includes a primary condenser and an oil washing tower, the outlet of the cascade reactor is connected to the inlet of the primary condenser, the exhaust port of the primary condenser is connected to the inlet at the bottom of the oil washing tower, and the liquid outlet of the primary condenser and the liquid outlet at the top of the oil washing tower are connected to the inlet of the three-phase separator.

[0026] In one alternative implementation, the device further includes: The raw material compressor has an inlet for receiving carbon source gas and hydrogen, and its outlet is connected to the main reactor. A circulating gas compressor has its inlet connected to the exhaust port of the staged condenser for receiving circulating gas, and its outlet connected to the main reactor. Preferably, a heat exchanger is provided between the main reactor and the staged condenser. The inlet of the heat exchanger is connected to the outlet of the raw material compressor and the circulating gas compressor, and the outlet of the heat exchanger is connected to the main reactor and the staged condenser. Preferably, the outlet of the cascade reactor is connected to the heat exchange medium inlet of the heat exchanger, and the heat exchange medium outlet of the heat exchanger is connected to the staged condenser. Preferably, the device further includes a purge gas recovery system, wherein the exhaust port of the staged condenser is connected to the purge gas recovery system via a first pipe and to the circulating gas compressor via a second pipe; Preferably, the hydrogen outlet of the purge gas recovery system is connected to the feed inlet of the raw material compressor; Preferably, the device further includes a hydrogen production system, wherein the hydrogen outlet of the hydrogen production system is connected to the inlet of the raw material compressor; Preferably, the equipment further includes a water treatment device, wherein the outlet of the three-phase separator is connected to the inlet of the water treatment device, and the outlet of the water treatment device is connected to the inlet of the hydrogen production system.

[0027] The technical solution of this invention has the following advantages: This invention feeds carbon source gas, hydrogen, and recycled gas into the main reactor for reaction, so that the carbon source gas is preferentially converted into a mixed component a containing intermediate components such as hydrocarbons and methanol. This provides a suitable reaction precursor for the subsequent generation of target components for jet fuel, which is beneficial to improving carbon source utilization efficiency and reducing the excessive generation of light by-products.

[0028] Furthermore, the mixed component a is fed into a cascade reactor for further conversion, allowing processes such as methanol dehydration, olefin polymerization, and carbon chain growth to occur stepwise. This helps to increase the proportion of jet fuel components in the C8-C18 range and avoids the problem of uncontrollable product distribution caused by multiple reactions occurring simultaneously in a single reactor. Simultaneously, by performing staged condensation on the products after the cascade reaction and combining it with three-phase separation, the light hydrocarbon components, water, and jet fuel components are effectively separated. This ensures that the jet fuel components have a relatively stable composition before entering subsequent hydrorefining and fractionation, thus facilitating the acquisition of the target jet fuel product and improving the continuity and stability of the entire process.

[0029] Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. Attached Figure Description

[0030] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0031] Figure 1 This is a schematic diagram of the assembly structure of the aviation kerosene production equipment of the present invention; Figure 2 This is a schematic diagram of the main reactor assembly structure of the present invention.

[0032] In the diagram: 1. Cascade reactor; 2. Main reactor; 21. Buffer tank; 22. Circulating pump; 23. Heater; 24. Waste heat boiler; 3. Heat exchanger; 4. Flare system; 5. Off-gas recovery system; 6. Circulating compressor; 7. Stage condenser; 8. Light hydrocarbon recovery unit; 9. Three-phase separator; 10. Fractionating unit; 11. Hydrogenation refining unit; 12. Water treatment unit; 13. Product jet fuel; 14. Feed compressor; 15. Hydrogen production system; 16. Feed gas. Detailed Implementation

[0033] The following embodiments are provided to better understand the present invention, but the following embodiments do not constitute a limitation on the content and scope of protection of the present invention. Any product that is the same as or similar to the present invention, derived by any person under the guidance of the present invention or by combining the features of the present invention with other prior art, falls within the scope of protection of the present invention.

[0034] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs; the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the application; the terms “comprising” and “having” and any variations thereof in the text of this application are intended to cover non-exclusive inclusion.

[0035] In the description of the embodiments of this application, the technical terms "first", "second", etc. are used only to distinguish different objects and should not be construed as indicating or implying relative importance or implicitly indicating the number, specific order or primary and secondary relationship of the indicated technical features.

[0036] In this document, the term "embodiment" means that a particular feature, structure, or characteristic described in connection with an embodiment may be included in at least one embodiment of this application. The appearance of this phrase in various places throughout the specification does not necessarily refer to the same embodiment, nor is it a separate or alternative embodiment mutually exclusive with other embodiments. It will be explicitly and implicitly understood by those skilled in the art that the embodiments described herein can be combined with other embodiments.

[0037] The "range" disclosed in this application is defined by a lower limit and an upper limit. A given range is defined by selecting a lower limit and an upper limit, which define the boundaries of the specific range. Ranges defined in this way can include or exclude endpoints and can be arbitrarily combined; that is, any lower limit can be combined with any upper limit to form a range. In this application, unless otherwise stated, the numerical range "ab" represents a shortened representation of any combination of real numbers from a to b, where a and b are real numbers. For example, the numerical range "0-5" indicates that all real numbers between "0-5" have been listed herein, and "0-5" is merely a shortened representation of these numerical combinations. Furthermore, when a parameter is described as an integer ≥ 2, it is equivalent to disclosing that the parameter can be, for example, integers 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, etc.

[0038] In the description of the embodiments in this application, the term "and / or" is merely a description of the relationship between related objects, indicating that three relationships can exist. For example, A and / or B can represent: A existing alone, A and B existing simultaneously, and B existing alone. Additionally, the character " / " in this document generally indicates that the preceding and following related objects have an "or" relationship.

[0039] In the description of the embodiments of this application, the term "at least one" refers to one or more (including two).

[0040] Unless otherwise specified, all experimental steps or conditions in the examples were performed according to conventional experimental procedures and conditions in the art. Reagents or instruments whose manufacturers are not specified are all commercially available products.

[0041] The present application will now be described with reference to specific embodiments. It should be noted that these embodiments are merely descriptive and do not limit the present application in any way.

[0042] Unless otherwise specified, all experimental steps or conditions in the examples were performed according to conventional experimental procedures and conditions in the art. Reagents or instruments whose manufacturers are not specified are all commercially available products.

[0043] The method for preparing the molecular sieve composite catalyst used in the embodiments of the present invention is as follows: Take 2200 g of demineralized water and add 2525 g of ferric nitrate hexahydrate, 326 g of cobalt nitrate, 190 g of potassium manganate, 45 g of zinc nitrate, and 100 g of cerium nitrate to prepare solution A. Separately, take 3500 g of demineralized water and add 2370 g of ammonium carbonate and 675 g of sodium carbonate to prepare solution B. Mix solutions A and B in a co-current manner with stirring at 50°C. After mixing, filter the mixture and wash the filter cake once with 5000 g of demineralized water. Then, add 800 g of Beta molecular sieve and 1650 g of silica sol (30% by mass) to the resulting filter cake and stir thoroughly to prepare a slurry. Spray dry the resulting slurry and calcine it at 500°C to obtain the catalyst sample, denoted as oxide molecular sieve catalyst A.

[0044] 1000 g of H-Beta molecular sieve with a silica-to-alumina ratio of 45 was mixed with 565 g of boehmite and 55 g of guar gum powder. After thorough mixing, 108 g of 65% nitric acid was added, along with 260 g of deionized water. The mixture was then kneaded until homogeneous. The resulting material was extruded into strips using a 3 mm perforated plate and then calcined at 500℃ to obtain a strip-shaped catalyst, denoted as molecular sieve catalyst B.

[0045] like Figure 1 and Figure 2 As shown, this invention provides a jet fuel production device, including a cascade reactor 1, a main reactor 2, a heat exchanger 3, a flare system 4, a purge gas recovery system 5, a circulating compressor 6, a staged condenser 7, a light hydrocarbon recovery device 8, a three-phase separator 9, a fractionation unit 10, a hydrorefining device 11, a water treatment device 12, product jet fuel 13, a raw material compressor 14, a hydrogen production system 15, and raw material gas 16. The main reactor 2 is connected to a temperature control system. The outlet of the main reactor 2 is connected to the inlet of the cascade reactor 1. The outlet of the cascade reactor 1 is connected to the inlet of the staged condenser 7. The outlet of the staged condenser 7 is connected to the inlet of the three-phase separator 9. The jet fuel component outlet of the three-phase separator 9 is connected to the inlet of the hydrorefining device 11. The outlet of the hydrorefining device 11 is connected to the inlet of the fractionation unit 10. The jet fuel product outlet of the fractionation unit 10 is used to output product jet fuel 13. Thus, the products from the reactions in the main reactor 2 and the cascade reactor 1 are sequentially subjected to staged condensation, three-phase separation, hydrogenation refining, and fractionation to obtain the target jet fuel product.

[0046] In this invention, the feed inlet of the raw material compressor 14 is used to receive the raw material gas 16 and hydrogen from the hydrogen production system 15, and the discharge port of the raw material compressor 14 is connected to the feed inlet of the heat exchanger 3. The feed inlet of the circulating compressor 6 is connected to the exhaust port of the staged condenser 7 and is used to receive the circulating gas. The discharge port of the circulating compressor 6 is also connected to the feed inlet of the heat exchanger 3. The discharge port of the heat exchanger 3 is connected to the feed inlet of the main reactor 2, the discharge port of the cascade reactor 1 is connected to the heat exchange medium inlet of the heat exchanger 3, and the heat exchange medium outlet of the heat exchanger 3 is connected to the feed inlet of the staged condenser 7. With the above arrangement, after the fresh raw material gas 16 and the circulating gas merge, they first exchange heat with the high-temperature reaction products discharged from the cascade reactor 1 in the heat exchanger 3 to raise their temperature, and then enter the main reactor 2 for reaction; while the reaction products discharged from the cascade reactor 1 are cooled in the heat exchanger 3 and then enter the staged condenser 7, thereby realizing heat recovery and process connection.

[0047] The main reactor 2 is preferably a fluidized bed reactor, with an internal heat exchange structure serving as a temperature control system. This system includes a buffer tank 21, a circulating pump 22, a heater 23, and a waste heat boiler 24. Specifically, the heat transfer oil from the outlet of the main reactor 2 enters the buffer tank 21, is pumped by the circulating pump 22, and then a portion enters the heater 23 for heating, while the other portion enters the waste heat boiler 24 for heat exchange. The regulated heat transfer oil is then returned to the main reactor 2 to regulate its reaction temperature. During start-up, the heater 23 primarily provides heat to raise the main reactor 2 to the set reaction temperature. During normal operation, the waste heat boiler 24 removes residual heat, supplemented by the heater 23 for temperature compensation, thereby maintaining stable operation of the main reactor 2.

[0048] The staged condenser 7 preferably includes a primary condenser and a secondary condenser. The reaction products discharged from the cascade reactor 1 are cooled by the heat exchanger 3 and first enter the primary condenser for initial condensation and separation. The exhaust port of the primary condenser is connected to the feed port of the secondary condenser. The liquid outlets of both the primary and secondary condensers are connected to the feed port of the three-phase separator 9. The liquid phases separated by the primary and secondary condensers enter the three-phase separator 9 together, which separates them into a light hydrocarbon-enriched organic phase, an aqueous phase, and a heavy hydrocarbon-enriched organic phase. The light hydrocarbon-enriched organic phase is sent to the light hydrocarbon recovery unit 8, the heavy hydrocarbon-enriched organic phase is sent to the hydrorefining unit 11, and the aqueous phase is sent to the water treatment unit 12. Alternatively, the staged condenser 7 may also include a primary condenser and an oil washing tower. The exhaust port of the primary condenser is connected to the feed port at the bottom of the oil washing tower, and the liquid outlets of the primary condenser and the top of the oil washing tower are connected to the feed port of the three-phase separator 9 to achieve the same staged condensation and liquid phase collection functions as described above.

[0049] Furthermore, the exhaust port of the staged condenser 7 is connected to the purge gas recovery system 5 via a first pipe and to the circulating compressor 6 via a second pipe. A portion of the gas phase after staged condensation enters the circulating compressor 6 as circulating gas, is compressed, returns to the heat exchanger 3, and further enters the main reactor 2; the remaining gas phase enters the purge gas recovery system 5 as purge gas to recover hydrogen. The dry gas not recovered by the purge gas recovery system 5 is sent to the flare system 4 for processing. Preferably, the hydrogen outlet of the purge gas recovery system 5 is connected to the inlet of the raw material compressor 14, so that the recovered hydrogen is reintegrated into the raw material system.

[0050] The inlet of the water treatment device 12 is connected to the outlet of the three-phase separator 9, and the outlet of the water treatment device 12 is connected to the inlet of the hydrogen production system 15, thereby treating the aqueous phase separated by the three-phase separator 9 and reusing it for use in the hydrogen production system 15. The hydrogen produced by the hydrogen production system 15 is transported to the inlet of the raw material compressor 14 through its hydrogen outlet, forming the raw material source for entering the main reactor 2 together with the raw material gas 16. The hydrorefining device 11 is used to hydrogenate the heavy hydrocarbon-enriched organic phase separated by the three-phase separator 9 to reduce the aromatic hydrocarbon content. Specifically, the heavy hydrocarbon-enriched organic phase enters the hydrorefining device 11 in the presence of hydrogen and undergoes a hydrogenation reaction under the action of a catalyst, converting the unsaturated hydrocarbons and at least some of the aromatic hydrocarbons into hydrocarbon components with a higher degree of saturation, thereby reducing the aromatic hydrocarbon content, improving product quality, and providing conditions for subsequent fractionation to obtain aviation kerosene products. The hydrorefining can be carried out using conventional hydrorefining catalysts and hydrorefining conditions in the art.

[0051] The hydrorefined material enters the fractionation unit 10, where it is separated to obtain the product jet fuel 13 and a light-end fraction. The light-end fraction can be further sent to the light hydrocarbon recovery unit 8 for recycling. Thus, this invention forms a complete process of raw material introduction, reaction conversion, heat exchange recovery, staged condensation, three-phase separation, gas recovery, hydrorefining, and product fractionation.

[0052] Example 1 Combination such as Figure 1 and Figure 2 The aviation kerosene production equipment shown in this embodiment provides a process for producing aviation kerosene through carbon dioxide hydrogenation, and the specific steps are as follows: (1) Carbon dioxide and hydrogen in the raw material gas 16 enter the raw material compressor 14 in proportion. After being pressurized to 5.2 MPa by the raw material compressor 14, they are mixed with the returned circulating gas to form the reaction feed. The ratio of the total molar number of CO2 and CO to the molar number of hydrogen in the circulating gas is controlled to be 1:2. The reaction feed enters the heat exchanger 3 and exchanges heat with the mixed component b at the outlet of the cascade reactor 1. After being preheated to 320 °C, it enters the main reactor 2. Part of the gas phase after separation by the secondary condenser is used as circulating gas. The circulating gas is pressurized to 5.2 MPa by the circulating compressor 6 and returned to be mixed with the raw material gas 16 output by the raw material compressor 14 to form the reaction feed. The ratio of the molar flow rate of the circulating gas to the total molar flow rate of the raw material gas 16, i.e., the circulation ratio, is 8:1.

[0053] The main reactor 2 is a fluidized bed reactor with an internal heat exchange structure forming a temperature control system, preferably using thermal oil as the temperature control medium. During start-up or activation, the thermal oil is heated by heater 23 and then enters the internal heat exchange structure of the main reactor 2 to provide heat to the main reactor 2, raising its temperature to the set reaction temperature. During normal operation, an exothermic reaction occurs in the main reactor 2, with the reaction temperature controlled at 350°C. At this time, the thermal oil is mainly used to remove residual heat from the reaction and regulate the temperature of the main reactor 2. The inlet temperature of the thermal oil is 300°C, and the outlet temperature is 320°C. The thermal oil absorbs heat and heats up within the main reactor 2, then carries the reaction heat out of the reactor.

[0054] The heat transfer oil from the outlet of the main reactor 2 enters the buffer tank 21. After being pumped by the circulating pump 22, part of it enters the heater 23 for heating, and the other part enters the waste heat boiler 24 for heat exchange. The heat transfer oil, after being regulated by the heater 23 and the waste heat boiler 24, is returned to the main reactor 2 to regulate its temperature. During the start-up phase, the heater 23 is the primary heat source to raise the temperature of the main reactor 2 to the reaction temperature. During normal operation, the waste heat boiler 24 removes the residual heat from the reaction, and the heater 23 is used for temperature compensation to stabilize the reaction temperature of the main reactor 2 at 350℃.

[0055] Waste heat boiler 24 is equipped with a water inlet and a steam outlet. After entering the waste heat boiler 24, water indirectly exchanges heat with the heat transfer oil and absorbs heat. At least part of the water is converted into steam and then discharged, thereby realizing the removal and recovery of waste heat from the main reactor 2. The operating pressure of the main reactor 2 is controlled at 5.0 MPa, and the pressure is maintained stable by adjusting the system's venting gas discharge.

[0056] The main reactor 2 is filled with oxide molecular sieve catalyst A. The reaction feed undergoes a hydrogenation conversion reaction in the main reactor 2. The outlet of the main reactor 2 yields a mixed component a containing hydrocarbons, methanol, water, and unreacted gases.

[0057] (2) Mixed component a is fed into cascade reactor 1 at a temperature of 350 °C. Cascade reactor 1 is filled with molecular sieve catalyst B. Methanol dehydration and olefin saturation reaction continue in cascade reactor 1. Mixed component b containing jet fuel component, light hydrocarbon component and water is obtained from the outlet of cascade reactor 1. The temperature of the reaction gas at the outlet of cascade reactor 1 is 350 °C and the operating pressure is controlled at 5.0 MPa.

[0058] (3) After leaving the cascade reactor 1, the mixed component b enters the heat exchanger 3 and exchanges heat with the reaction feed. After the heat exchange and cooling, it enters the staged condensation system.

[0059] The staged condensation system includes a primary condenser and a secondary condenser. After heat exchange, the mixed component b first enters the primary condenser and is cooled to 60°C, separating the first liquid phase. The gaseous phase after primary condensation enters the secondary condenser and is further cooled to 40°C, separating the second liquid phase. A portion of the gaseous phase separated by the secondary condenser is returned to the system as recirculated gas, while the remainder is discharged as purge gas to stabilize system pressure and control the inert component content. The purge gas enters the purge gas recovery system 5 to recover hydrogen and return it to the feedstock system; any unrecovered dry gas is sent to the flare system 4 for processing.

[0060] The liquid phases obtained from the primary and secondary condensers are combined and then sent to the three-phase separator 9 for three-phase separation, resulting in a light hydrocarbon-enriched organic phase, an aqueous phase, and a heavy hydrocarbon-enriched organic phase. The light hydrocarbon-enriched organic phase consists of C2-C7 light hydrocarbons, accounting for 20 wt% of the total organic phase mass; the heavy hydrocarbon-enriched organic phase consists of C8-C18 hydrocarbons, accounting for 80 wt% of the total organic phase mass.

[0061] The light hydrocarbon-enriched organic phase is fed into the light hydrocarbon recovery unit 8; the aqueous phase is treated by the water treatment unit 12 and can be reused in the hydrogen production system 15, and the resulting hydrogen can be reused in the raw material system; the heavy hydrocarbon-enriched organic phase is a crude product of aviation kerosene and is sent to the hydrorefining unit 11 for processing.

[0062] The crude jet fuel is hydrogenated in the hydrorefining unit 11. By controlling the hydrogenation conditions, the aromatic content is reduced to less than 20% molar aromatic content in the hydrogenated material. Subsequently, it is fractionated to obtain jet fuel 13 and a light-end fraction. The molar aromatic content is determined by compositional analysis of the hydrogenated material. The light-end fraction is sent to the light hydrocarbon recovery unit 8. Usable light hydrocarbons in the light hydrocarbon recovery unit 8 can be returned to the hydrorefining unit 11 for further hydrogenation. Gases such as methane are discharged as tail gas and are preferably sent to the purge gas recovery system 5 for further hydrogen recovery.

[0063] Example 2 Combination such as Figure 1 and Figure 2The aviation kerosene production equipment shown in this embodiment provides a process for producing aviation kerosene by hydrogenating syngas, and the specific steps are as follows: (1) Syngas and hydrogen in feed gas 16 enter feed compressor 14 in proportion. After being pressurized to 5.2 MPa by feed compressor 14, they are mixed with the returned recycle gas to form reaction feed. The ratio of the total molar number of CO2 and CO to the molar number of hydrogen in the recycle gas is controlled to be 1:2. The reaction feed enters heat exchanger 3 and exchanges heat with the mixed component b at the outlet of cascade reactor 1. After being preheated to 320 °C, it enters main reactor 2. Part of the gas phase after separation by the secondary condenser is used as recycle gas. The recycle gas is pressurized to 5.2 MPa by recycle compressor 6 and returned to be mixed with feed gas 16 output by feed compressor 14 to form the reaction feed. The ratio of the molar flow rate of the recycle gas to the total molar flow rate of feed gas 16, i.e., the recycle ratio, is 6:1.

[0064] The main reactor 2 is a fluidized bed reactor with an internal heat exchange structure forming a temperature control system, preferably using thermal oil as the temperature control medium. During start-up or activation, the thermal oil is heated by heater 23 and then enters the internal heat exchange structure of the main reactor 2 to provide heat to the main reactor 2, raising its temperature to the set reaction temperature. During normal operation, an exothermic reaction occurs in the main reactor 2, with the reaction temperature controlled at 350°C. At this time, the thermal oil is mainly used to remove residual heat from the reaction and regulate the temperature of the main reactor 2. The inlet temperature of the thermal oil is 300°C, and the outlet temperature is 320°C. The thermal oil absorbs heat and heats up within the main reactor 2, then carries the reaction heat out of the reactor.

[0065] The heat transfer oil from the outlet of the main reactor 2 enters the buffer tank 21. After being pumped by the circulating pump 22, part of it enters the heater 23 for heating, and the other part enters the waste heat boiler 24 for heat exchange. The heat transfer oil, after being regulated by the heater 23 and the waste heat boiler 24, is returned to the main reactor 2 to regulate its temperature. During the start-up phase, the heater 23 is the primary heat source to raise the temperature of the main reactor 2 to the reaction temperature. During normal operation, the waste heat boiler 24 removes the residual heat from the reaction, and the heater 23 is used for temperature compensation to stabilize the reaction temperature of the main reactor 2 at 350℃.

[0066] Waste heat boiler 24 is equipped with a water inlet and a steam outlet. After entering the waste heat boiler 24, water indirectly exchanges heat with the heat transfer oil and absorbs heat. At least part of the water is converted into steam and then discharged, thereby realizing the removal and recovery of waste heat from the main reactor 2. The operating pressure of the main reactor 2 is controlled at 5.0 MPa, and the pressure is maintained stable by adjusting the system's venting gas discharge.

[0067] The main reactor 2 is filled with oxide molecular sieve catalyst A. The reaction feed undergoes a hydrogenation conversion reaction in the main reactor 2. The outlet of the main reactor 2 yields a mixed component a containing hydrocarbons, methanol, water, and unreacted gases.

[0068] (2) Mixed component a is fed into cascade reactor 1 at a temperature of 350 °C. Cascade reactor 1 is filled with molecular sieve catalyst B. Methanol dehydration and olefin saturation reaction continue in cascade reactor 1. Mixed component b containing jet fuel component, light hydrocarbon component and water is obtained from the outlet of cascade reactor 1. The temperature of the reaction gas at the outlet of cascade reactor 1 is 350 °C and the operating pressure is controlled at 5.0 MPa.

[0069] (3) After leaving the cascade reactor 1, the mixed component b enters the heat exchanger 3 and exchanges heat with the reaction feed. After the heat exchange and cooling, it enters the staged condensation system.

[0070] The staged condensation system includes a primary condenser and a secondary condenser. After heat exchange, the mixed component b first enters the primary condenser and is cooled to 60°C, separating the first liquid phase. The gaseous phase after primary condensation enters the secondary condenser and is further cooled to 40°C, separating the second liquid phase. A portion of the gaseous phase separated by the secondary condenser is returned to the system as recirculated gas, while the remainder is discharged as purge gas to stabilize system pressure and control the inert component content. The purge gas enters the purge gas recovery system 5 to recover hydrogen and return it to the feedstock system; any unrecovered dry gas is sent to the flare system 4 for processing.

[0071] The liquid phases obtained from the primary and secondary condensers are combined and then sent to the three-phase separator 9 for three-phase separation, resulting in a light hydrocarbon-enriched organic phase, an aqueous phase, and a heavy hydrocarbon-enriched organic phase. The light hydrocarbon-enriched organic phase consists of C2-C7 light hydrocarbons, accounting for 15 wt% of the total organic phase mass; the heavy hydrocarbon-enriched organic phase consists of C8-C18 hydrocarbons, accounting for 85 wt% of the total organic phase mass.

[0072] The light hydrocarbon-enriched organic phase is fed into the light hydrocarbon recovery unit 8; the aqueous phase is treated by the water treatment unit 12 and can be reused in the hydrogen production system 15, and the resulting hydrogen can be reused in the raw material system; the heavy hydrocarbon-enriched organic phase is a crude product of aviation kerosene and is sent to the hydrorefining unit 11 for processing.

[0073] The crude jet fuel is hydrogenated in the hydrorefining unit 11. By controlling the hydrogenation conditions, the aromatic content is reduced to less than 20% molar aromatic content in the hydrogenated material. Subsequently, it is fractionated to obtain jet fuel 13 and a light-end fraction. The molar aromatic content is determined by compositional analysis of the hydrogenated material. The light-end fraction is sent to the light hydrocarbon recovery unit 8. Usable light hydrocarbons in the light hydrocarbon recovery unit 8 can be returned to the hydrorefining unit 11 for further hydrogenation. Gases such as methane are discharged as tail gas and are preferably sent to the purge gas recovery system 5 for further hydrogen recovery.

[0074] Example 3 Combination such as Figure 1 and Figure 2 The aviation kerosene production equipment shown in this embodiment provides a process for producing aviation kerosene through carbon dioxide hydrogenation, and the specific steps are as follows: (1) Carbon dioxide and hydrogen in the raw material gas 16 enter the raw material compressor 14 in proportion. After being pressurized to 1 MPa by the raw material compressor 14, they are mixed with the returned circulating gas to form the reaction feed. The ratio of the total molar number of CO2 and CO to the molar number of hydrogen in the circulating gas is controlled to be 1:1.5. The reaction feed enters the heat exchanger 3 and exchanges heat with the mixed component b at the outlet of the cascade reactor 1. After being preheated to 250 °C, it enters the main reactor 2. Part of the gas phase after separation by the secondary condenser is used as circulating gas. The circulating gas is pressurized to 1 MPa by the circulating compressor 6 and returned to be mixed with the raw material gas 16 output by the raw material compressor 14 to form the reaction feed. The ratio of the molar flow rate of the circulating gas to the total molar flow rate of the raw material gas 16, i.e., the circulation ratio, is 10:1.

[0075] The main reactor 2 is a fluidized bed reactor with an internal heat exchange structure forming a temperature control system, preferably using thermal oil as the temperature control medium. During start-up or activation, the thermal oil is heated by heater 23 and then enters the internal heat exchange structure of the main reactor 2 to provide heat to the main reactor 2, raising its temperature to the set reaction temperature. During normal operation, an exothermic reaction occurs in the main reactor 2, with the reaction temperature controlled at 270°C. At this time, the thermal oil is mainly used to remove residual heat from the reaction and regulate the temperature of the main reactor 2. The thermal oil absorbs heat within the main reactor 2, raises its temperature, and then carries the reaction heat out of the reactor.

[0076] The heat transfer oil from the outlet of the main reactor 2 enters the buffer tank 21. After being pumped by the circulating pump 22, part of it enters the heater 23 for heating, and the other part enters the waste heat boiler 24 for heat exchange. The heat transfer oil, after being regulated by the heater 23 and the waste heat boiler 24, is returned to the main reactor 2 to regulate its temperature. During the start-up phase, the heater 23 is the primary heat source to raise the temperature of the main reactor 2 to the reaction temperature. During normal operation, the waste heat boiler 24 removes the residual heat from the reaction, and the heater 23 is used for temperature compensation to stabilize the reaction temperature of the main reactor 2 at 270℃.

[0077] Waste heat boiler 24 is equipped with a water inlet and a steam outlet. After entering the waste heat boiler 24, water indirectly exchanges heat with the heat transfer oil and absorbs heat. At least part of the water is converted into steam and discharged, thereby realizing the removal and recovery of waste heat from the main reactor 2. The operating pressure of the main reactor 2 is controlled at 1.0 MPa, and the pressure is maintained stable by adjusting the system's venting gas discharge.

[0078] The main reactor 2 is filled with oxide molecular sieve catalyst A. The reaction feed undergoes a hydrogenation conversion reaction in the main reactor 2. The outlet of the main reactor 2 yields a mixed component a containing hydrocarbons, methanol, water, and unreacted gases.

[0079] (2) Mixed component a is fed into cascade reactor 1 at a temperature of 270 °C. Cascade reactor 1 is filled with molecular sieve catalyst B. Methanol dehydration and olefin saturation reaction continue in cascade reactor 1. Mixed component b containing jet fuel component, light hydrocarbon component and water is obtained from the outlet of cascade reactor 1. The outlet temperature of the reaction gas of cascade reactor 1 is 270 °C and the operating pressure is controlled at 1.0 MPa.

[0080] (3) After leaving the cascade reactor 1, the mixed component b enters the heat exchanger 3 and exchanges heat with the reaction feed. After the heat exchange and cooling, it enters the staged condensation system.

[0081] The staged condensation system includes a primary condenser and a secondary condenser. After heat exchange, the mixed component b first enters the primary condenser and is cooled to 55°C, separating the first liquid phase. The gaseous phase after primary condensation enters the secondary condenser and is further cooled to 30°C, separating the second liquid phase. A portion of the gaseous phase separated by the secondary condenser is returned to the system as recirculated gas, while the remainder is discharged as purge gas to stabilize system pressure and control the inert component content. The purge gas enters the purge gas recovery system 5 to recover hydrogen and return it to the feedstock system; any unrecovered dry gas is sent to the flare system 4 for processing.

[0082] The liquid phases obtained from the primary and secondary condensers are combined and then sent to the three-phase separator 9 for three-phase separation, resulting in a light hydrocarbon-enriched organic phase, an aqueous phase, and a heavy hydrocarbon-enriched organic phase. The light hydrocarbon-enriched organic phase consists of C2-C7 light hydrocarbons, accounting for 30 wt% of the total organic phase mass; the heavy hydrocarbon-enriched organic phase consists of C8-C18 hydrocarbons, accounting for 70 wt% of the total organic phase mass.

[0083] The light hydrocarbon-enriched organic phase is fed into the light hydrocarbon recovery unit 8; the aqueous phase is treated by the water treatment unit 12 and can be reused in the hydrogen production system 15, and the resulting hydrogen can be reused in the raw material system; the heavy hydrocarbon-enriched organic phase is a crude product of aviation kerosene and is sent to the hydrorefining unit 11 for processing.

[0084] The crude jet fuel is hydrogenated in the hydrorefining unit 11. By controlling the hydrogenation conditions, the aromatic content is reduced to less than 20% molar aromatic content in the hydrogenated material. Subsequently, it is fractionated to obtain jet fuel 13 and a light-end fraction. The molar aromatic content is determined by compositional analysis of the hydrogenated material. The light-end fraction is sent to the light hydrocarbon recovery unit 8. Usable light hydrocarbons in the light hydrocarbon recovery unit 8 can be returned to the hydrorefining unit 11 for further hydrogenation. Gases such as methane are discharged as tail gas and are preferably sent to the purge gas recovery system 5 for further hydrogen recovery.

[0085] Example 4 Combination such as Figure 1 and Figure 2 The aviation kerosene production equipment shown in this embodiment provides a process for producing aviation kerosene through carbon dioxide hydrogenation, and the specific steps are as follows: (1) Carbon dioxide and hydrogen in the raw material gas 16 enter the raw material compressor 14 in proportion. After being pressurized to 8 MPa by the raw material compressor 14, they are mixed with the returned circulating gas to form the reaction feed. The ratio of the total molar number of CO2 and CO to the molar number of hydrogen in the circulating gas is controlled to be 1:3. The reaction feed enters the heat exchanger 3 and exchanges heat with the mixed component b at the outlet of the cascade reactor 1. After being preheated to 400 °C, it enters the main reactor 2. Part of the gas phase after separation by the secondary condenser is used as circulating gas. The circulating gas is pressurized to 8 MPa by the circulating compressor 6 and returned to be mixed with the raw material gas 16 output by the raw material compressor 14 to form the reaction feed. The ratio of the molar flow rate of the circulating gas to the total molar flow rate of the raw material gas 16, i.e., the circulation ratio, is 10:1.

[0086] The main reactor 2 is a fluidized bed reactor with an internal heat exchange structure forming a temperature control system, preferably using thermal oil as the temperature control medium. During start-up or activation, the thermal oil is heated by heater 23 and then enters the internal heat exchange structure of the main reactor 2 to provide heat to the main reactor 2, raising its temperature to the set reaction temperature. During normal operation, an exothermic reaction occurs in the main reactor 2, with the reaction temperature controlled at 400℃. At this time, the thermal oil is mainly used to remove residual heat from the reaction and regulate the temperature of the main reactor 2. The thermal oil absorbs heat within the main reactor 2, raises its temperature, and then carries the reaction heat out of the reactor.

[0087] The heat transfer oil from the outlet of the main reactor 2 enters the buffer tank 21. After being pumped by the circulating pump 22, part of it enters the heater 23 for heating, and the other part enters the waste heat boiler 24 for heat exchange. The heat transfer oil, after being regulated by the heater 23 and the waste heat boiler 24, is returned to the main reactor 2 to regulate its temperature. During the start-up phase, the heater 23 is the primary heat source to raise the temperature of the main reactor 2 to the reaction temperature. During normal operation, the waste heat boiler 24 removes the residual heat from the reaction, and the heater 23 is used for temperature compensation to stabilize the reaction temperature of the main reactor 2 at 400℃.

[0088] Waste heat boiler 24 is equipped with a water inlet and a steam outlet. After entering the waste heat boiler 24, water indirectly exchanges heat with the heat transfer oil and absorbs heat. At least part of the water is converted into steam and discharged, thereby realizing the removal and recovery of waste heat from the main reactor 2. The operating pressure of the main reactor 2 is controlled at 8.0 MPa, and the pressure is maintained stable by adjusting the system's venting gas discharge.

[0089] The main reactor 2 is filled with oxide molecular sieve catalyst A. The reaction feed undergoes a hydrogenation conversion reaction in the main reactor 2. The outlet of the main reactor 2 yields a mixed component a containing hydrocarbons, methanol, water, and unreacted gases.

[0090] (2) Mixed component a is fed into cascade reactor 1 at a temperature of 400 °C. Cascade reactor 1 is filled with molecular sieve catalyst B. Methanol dehydration and olefin saturation reaction continue in cascade reactor 1. Mixed component b containing jet fuel component, light hydrocarbon component and water is obtained from the outlet of cascade reactor 1. The outlet temperature of the reaction gas of cascade reactor 1 is 400 °C and the operating pressure is controlled at 8.0 MPa.

[0091] (3) After leaving the cascade reactor 1, the mixed component b enters the heat exchanger 3 and exchanges heat with the reaction feed. After the heat exchange and cooling, it enters the staged condensation system.

[0092] The staged condensation system includes a primary condenser and a secondary condenser. After heat exchange, the mixed component b first enters the primary condenser and is cooled to 80°C, separating the first liquid phase. The gaseous phase after primary condensation enters the secondary condenser and is further cooled to 50°C, separating the second liquid phase. A portion of the gaseous phase separated by the secondary condenser is returned to the system as recirculated gas, while the remainder is discharged as purge gas to stabilize system pressure and control the inert component content. The purge gas enters the purge gas recovery system 5 to recover hydrogen and return it to the feedstock system; any unrecovered dry gas is sent to the flare system 4 for processing.

[0093] The liquid phases obtained from the primary and secondary condensers are combined and then sent to the three-phase separator 9 for three-phase separation, resulting in a light hydrocarbon-enriched organic phase, an aqueous phase, and a heavy hydrocarbon-enriched organic phase. The light hydrocarbon-enriched organic phase consists of C2-C7 light hydrocarbons, accounting for 40 wt% of the total organic phase mass; the heavy hydrocarbon-enriched organic phase consists of C8-C18 hydrocarbons, accounting for 60 wt% of the total organic phase mass.

[0094] The light hydrocarbon-enriched organic phase is fed into the light hydrocarbon recovery unit 8; the aqueous phase is treated by the water treatment unit 12 and can be reused in the hydrogen production system 15, and the resulting hydrogen can be reused in the raw material system; the heavy hydrocarbon-enriched organic phase is a crude product of aviation kerosene and is sent to the hydrorefining unit 11 for processing.

[0095] The crude jet fuel is hydrogenated in the hydrorefining unit 11. By controlling the hydrogenation conditions, the aromatic content is reduced to less than 20% molar aromatic content in the hydrogenated material. Subsequently, it is fractionated to obtain jet fuel 13 and a light-end fraction. The molar aromatic content is determined by compositional analysis of the hydrogenated material. The light-end fraction is sent to the light hydrocarbon recovery unit 8. Usable light hydrocarbons in the light hydrocarbon recovery unit 8 can be returned to the hydrorefining unit 11 for further hydrogenation. Gases such as methane are discharged as tail gas and are preferably sent to the purge gas recovery system 5 for further hydrogen recovery.

[0096] Comparative Example 1 The only difference between this comparative example and Example 1 is that: no cascade reactor 1 is set in this comparative example. The reaction feed that was preheated by heat exchanger 3 and then entered the cascade reactor 1 for pre-reaction in Example 1 is directly entered into the main reactor 2 for reaction in this comparative example after preheating. Specifically, carbon dioxide and hydrogen in the feed gas 16 enter the feed compressor 14 in a certain proportion. After being pressurized by the feed compressor 14, they are mixed with the returned circulating gas to form the reaction feed. The reaction feed is preheated by the heat exchanger 3 and then directly enters the main reactor 2 instead of the cascade reactor 1. In the main reactor 2, it comes into contact with the catalyst and reacts, yielding reaction products containing hydrocarbons, methanol, water, and unreacted gases. Since the cascade reactor 1 is not set up in this comparative example, the mixed component b at the outlet of the cascade reactor 1 in Example 1 does not exist. The heat exchanger 3 is adjusted accordingly to exchange the reaction products at the outlet of the main reactor 2.

[0097] In this comparative example, the liquid phases separated by the primary and secondary condensers are combined and then sent to the three-phase separator 9 for three-phase separation, resulting in a light hydrocarbon-enriched organic phase, an aqueous phase, and a heavy hydrocarbon-enriched organic phase. The light hydrocarbon-enriched organic phase consists of C2-C7 light hydrocarbons, accounting for 45 wt% of the total organic phase mass; the heavy hydrocarbon-enriched organic phase consists of C8-C18 hydrocarbons, accounting for 55 wt% of the total organic phase mass.

[0098] Test Example 1 To verify whether the aviation kerosene products prepared using the processes and systems described in Examples 1 to 4 meet the technical requirements of current No. 3 jet fuel, key physicochemical properties of the aviation kerosene products obtained in each example were tested and compared with the No. 3 jet fuel standard. Specifically, the volume fraction of aromatics, volume fraction of olefins, mass fraction of total sulfur, distillation range, closed-cup flash point, density at 20°C, freezing point, net calorific value, and smoke point were tested to evaluate whether the aviation kerosene products prepared in this application meet the quality requirements of No. 3 jet fuel for all components of aviation kerosene.

[0099] The detection methods for each parameter are as follows: the volume fraction of aromatics and olefins are detected using GB / T 11132; the mass fraction of total sulfur is detected using SH / T 0689; the distillation range is detected using GB / T 6536; the closed-cup flash point is detected using GB / T 21789; the density at 20℃ is detected using GB / T 1884; the freezing point is detected using GB / T 2430; the net calorific value is detected using GB / T 384; and the smoke point is detected using GB / T 382.

[0100] The test results are shown in Table 1. As can be seen from Table 1, the aviation kerosene products obtained in Examples 1 to 4 all meet the technical requirements of No. 3 jet fuel in terms of aromatic volume fraction, olefin volume fraction, total sulfur mass fraction, 10% boiling point, final boiling point, closed-cup flash point, density at 20℃, freezing point, net calorific value, and smoke point. This indicates that the process and system described in this application can produce aviation kerosene products that meet the No. 3 jet fuel standard.

[0101] Table 1: Test Results of Physicochemical Properties of Aviation Fuel Products

[0102] Test Example 2 This test example analyzes the light hydrocarbon-enriched organic phase, aqueous phase, and heavy hydrocarbon-enriched organic phase obtained by separating the combined liquid phases from the primary and secondary condensers in each embodiment and Comparative Example 1 through a three-phase separator. The analysis focuses on detecting the mass percentage of C2-C7 light hydrocarbons and the mass percentage of C8-C18 hydrocarbons in the organic phase.

[0103] During testing, the light hydrocarbon-enriched organic phase and the heavy hydrocarbon-enriched organic phase separated by the three-phase separator were collected and weighed to obtain the mass of each organic phase. Simultaneously, gas chromatography or gas chromatography-mass spectrometry was used to analyze the composition of each organic phase. Based on the detected hydrocarbon components, they were classified and statistically analyzed according to the number of carbon atoms. The mass ratio of C2-C7 light hydrocarbons and C8-C18 hydrocarbons was calculated using the total mass of the separated organic phases as a baseline. The test results are shown in Table 2.

[0104] Table 2: Separation Results of the Three-Phase Separator

[0105] As shown in Table 2, the mass proportion of C8-C18 hydrocarbons in the organic phases obtained in Examples 1 to 4 is higher than that in Comparative Example 1, while the mass proportion of C2-C7 light hydrocarbons is lower than that in Comparative Example 1. This indicates that the process scheme of the present invention, which uses a main reactor and a cascade reactor in combination, is beneficial to promoting the further conversion of intermediate products into target hydrocarbons in the C8-C18 range and suppressing the formation of lighter hydrocarbons. Since C8-C18 hydrocarbons are the main components of the target fraction of jet fuel, the present invention can increase the yield ratio of the target jet fuel components, thereby facilitating the subsequent acquisition of the target product jet fuel with a lower separation load, demonstrating significant process advantages.

[0106] Obviously, the above embodiments are merely illustrative examples for clear explanation and are not intended to limit the implementation. Those skilled in the art will recognize that other variations or modifications can be made based on the above description. It is neither necessary nor possible to exhaustively list all possible implementations here. However, obvious variations or modifications derived therefrom are still within the scope of protection of this invention.

Claims

1. A process for producing aviation kerosene, characterized in that, Includes the following steps: (1) Carbon source gas, hydrogen, and circulating gas are fed into the main reactor to react and obtain a mixed component a including hydrocarbons, methanol, CO, water and unreacted gas; (2) The mixed component a is fed into a cascade reactor to prepare a mixed component b, which includes jet fuel component, light hydrocarbon component and water, wherein the light hydrocarbon component includes one or more of C2-C7 light hydrocarbons; (3) The mixed component b is condensed and collected in stages to obtain liquid and gas phases. The liquid phase is then separated into three phases to obtain jet fuel component, light hydrocarbon component and water. The jet fuel component is then hydrogenated, refined and fractionated to obtain jet fuel.

2. The aviation kerosene production process according to claim 1, characterized in that, In step (1), the carbon source gas includes one or both of syngas and carbon dioxide; And / or, the ratio of the total number of moles of CO2 and CO in the circulating gas to the number of moles of hydrogen is 1:(1.5~3).

3. The aviation kerosene production process according to claim 1 or 2, characterized in that, In step (1), the reaction temperature in the main reactor is 270℃~400℃; And / or, in step (1), the reaction pressure in the main reactor is 1.0 MPa to 8.0 MPa; And / or, in step (2), the reaction temperature in the cascade reactor is 270℃~400℃; And / or, in step (2), the reaction pressure in the cascade reactor is 1.0 MPa to 8.0 MPa.

4. The aviation kerosene production process according to any one of claims 1-3, characterized in that, In step (3), the mixed component b exchanges heat with the feed of the main reactor and then undergoes staged condensation.

5. The aviation kerosene production process according to claim 4, characterized in that, In step (3), the feed to the main reactor exchanges heat with the mixed component b to 250°C~350°C.

6. The aviation kerosene production process according to any one of claims 1-5, characterized in that, In step (3), the staged condensation includes cooling the mixed component b at a temperature of 55℃~80℃ to separate the liquid phase and the gas phase, cooling the gas phase again at a temperature of 30℃~50℃ to separate the liquid phase and the gas phase, and collecting the liquid phase from the staged condensation for three-phase separation. Preferably, the cooling method for the second cooling includes one or more of the following: condenser cooling and oil washing cooling; Preferably, the oil washing and cooling process adopts a counter-current contact method with air intake at the bottom and oil intake at the top.

7. The aviation kerosene production process according to claim 6, characterized in that, In step (3), the gas phase obtained by cooling and separation again is split, a part of which is compressed to 1.0 MPa~8.0 MPa and then recycled as circulating gas for step (1), and the other part is discharged as release gas; Preferably, the purge gas is fed into a purge gas recovery system, where hydrogen is recovered through membrane separation, and the recovered hydrogen is reused in step (1).

8. The aviation kerosene production process according to any one of claims 1-7, characterized in that, In step (1), the main reactor is selected from fluidized bed reactor and fixed bed reactor; preferably, the main reactor is filled with metal oxide-molecular sieve composite catalyst. And / or, in step (2), the cascade reactor is a fixed-bed reactor, and the fixed-bed reactor is filled with a molecular sieve catalyst; preferably, the molecular sieve catalyst includes one or more of ZSM-5 molecular sieve, Beta molecular sieve, Y-type molecular sieve and mordenite.

9. A jet fuel production device, characterized in that, include: The main reactor is connected to a temperature control system; A cascade reactor, in which the outlet of the main reactor is connected to the inlet of the cascade reactor; A staged condenser is constructed by connecting the outlet of a cascade reactor to the inlet of the staged condenser. The three-phase separator has its inlet connected to the outlet of the staged condenser. The hydrorefining system connects the jet fuel component outlet of the three-phase separator to the inlet of the hydrorefining system for the purpose of hydrogenating jet fuel. Preferably, the staged condenser includes at least a primary condenser and a secondary condenser, the outlet of the cascade reactor is connected to the inlet of the primary condenser, the exhaust port of the primary condenser is connected to the inlet of the secondary condenser, and the liquid outlets of the primary and secondary condensers are connected to the inlet of the three-phase separator. Alternatively, the staged condenser includes a primary condenser and an oil washing tower, the outlet of the cascade reactor is connected to the inlet of the primary condenser, the exhaust port of the primary condenser is connected to the inlet at the bottom of the oil washing tower, and the liquid outlet of the primary condenser and the liquid outlet at the top of the oil washing tower are connected to the inlet of the three-phase separator.

10. The aviation kerosene production equipment according to claim 9, characterized in that, The device also includes: The raw material compressor has an inlet for receiving carbon source gas and hydrogen, and its outlet is connected to the main reactor. A circulating gas compressor has its inlet connected to the exhaust port of the staged condenser for receiving circulating gas, and its outlet connected to the main reactor. Preferably, a heat exchanger is provided between the main reactor and the staged condenser. The inlet of the heat exchanger is connected to the outlet of the raw material compressor and the circulating gas compressor, and the outlet of the heat exchanger is connected to the main reactor and the staged condenser. Preferably, the outlet of the cascade reactor is connected to the heat exchange medium inlet of the heat exchanger, and the heat exchange medium outlet of the heat exchanger is connected to the staged condenser. Preferably, the device further includes a purge gas recovery system, wherein the exhaust port of the staged condenser is connected to the purge gas recovery system via a first pipe and to the circulating gas compressor via a second pipe; Preferably, the hydrogen outlet of the purge gas recovery system is connected to the feed inlet of the raw material compressor; Preferably, the device further includes a hydrogen production system, wherein the hydrogen outlet of the hydrogen production system is connected to the inlet of the raw material compressor; Preferably, the equipment further includes a water treatment device, wherein the outlet of the three-phase separator is connected to the inlet of the water treatment device, and the outlet of the water treatment device is connected to the inlet of the hydrogen production system.

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