Process for the preparation of a catalyst for the production of aviation kerosene from synthesis gas

Abstract

The application provides a preparation method of a catalyst for preparing aviation kerosene from synthesis gas, the catalyst comprising a carrier and an active component, the active component being loaded on the carrier, the preparation method comprising the following steps: step 1, contacting a precursor of the active component with the carrier, and then performing calcination in a mixed gas atmosphere of NO and an inert gas to obtain a precursor of the catalyst; and step 2, performing reduction treatment on the precursor of the catalyst to obtain the catalyst; wherein the precursor of the active component is a soluble salt of the active component, a hydrate of the soluble salt of the active component or an oxide of the active component; and the precursor of the active component at least contains a nitrate of the active component or a hydrate of the nitrate of the active component. By calcining the contact of the carrier and the precursor of the active component in a specific atmosphere, the dispersion of the active phase can be improved, the size of the active phase can be controlled, the conversion rate of carbon monoxide in the synthesis gas can be improved, and the selectivity of long-chain hydrocarbons in the product can be improved. 16 long-chain hydrocarbons.

Description

Technical Field

[0001] This invention relates to the field of syngas-to-aviation kerosene production, and more specifically to a method for preparing a catalyst for syngas-to-aviation kerosene production. Background Technology

[0002] Aviation kerosene is one of the important fuels in the chemical industry. Its sources are mainly fossil fuels and biomass energy. Fossil fuels include oil, natural gas, and coal; biomass energy includes lignocellulose and animal and vegetable oils. Currently, global oil resources are increasingly depleted; bio-aviation kerosene is limited by factors such as high raw material prices, unstable sources, and small-scale production, and therefore lacks market competitiveness. Syngas (CO / H2), as a bridge for energy conversion, can convert natural gas, coal, and biomass into clean liquid fuels, showing great development potential and attracting the attention of many researchers.

[0003] Currently, only Shell and Sasol have achieved commercial production of aviation kerosene from syngas abroad. Shell uses the middle distillate synthesis (SMDS) process, with Co and Ru as the active catalyst components and Al2O3 as the support. The synthesized heavy-chain alkanes are then hydrocracking to obtain naphtha, kerosene, gasoline, and other products. Sasol uses a low-temperature slurry-bed process, with precipitated iron as the catalyst and potassium as the auxiliary agent. Fischer-Tropsch synthesis yields hydrocarbon gases, naphtha, kerosene, and heavier substances, which are then processed through hydrocracking, oligomerization, hydrorefining, aromatization, and alkylation. Therefore, the aviation kerosene production processes of Shell and Sasol are relatively complex.

[0004] To achieve highly selective production of aviation kerosene, bifunctional catalysts have become a research hotspot in the Fischer-Tropsch synthesis field. Bifunctional catalysts possess both metal active sites for CO hydrogenation to long-chain hydrocarbons and acidic sites for the hydrocracking and isomerization of these long-chain hydrocarbons. Bifunctional catalysts exhibit significant structure sensitivity; the size of the active metal, the acid strength of the support, the interaction between the support and the active metal, the diffusion effect of the support pore structure on the products, and the amount of co-catalyst all have a significant impact on the reaction activity and selectivity.

[0005] Patents CN110368983 A and WO 2019 / 196703A1 disclose the preparation of a catalyst for synthesizing aviation kerosene from syngas, as well as the resulting catalyst and its applications. This invention patent includes: (A) 1-50% by weight of elements selected from Ru, Fe, Ni, Co, Pt, and Pd as the catalytically active component; (B) 1-20% by weight of elements different from the catalytically active component, selected from Group I metals, transition elements, and lanthanides of the periodic table as catalytic promoters; and (C) a support. However, this technology suffers from poor dispersion of the catalytically active component and a low CO conversion rate. Summary of the Invention

[0006] The main objective of this invention is to provide a method for preparing a catalyst for the synthesis of aviation kerosene from syngas, thereby overcoming the defects of existing catalysts for the synthesis of aviation kerosene from syngas, such as poor dispersion of active components and low CO conversion rate in syngas.

[0007] To achieve the above objectives, the present invention provides a method for preparing a catalyst for the production of aviation kerosene from syngas. The catalyst comprises a support and an active component, wherein the active component is loaded on the support. The preparation method includes the following steps:

[0008] Step 1: The precursor of the active component is contacted with the support, and then calcined in a mixed atmosphere of NO and inert gas to obtain the precursor of the catalyst;

[0009] Step 2: The precursor of the catalyst is reduced to obtain the catalyst;

[0010] The precursor of the active component is a soluble salt of the active component, a hydrate of the soluble salt of the active component, or an oxide of the active component; and the precursor of the active component contains at least a nitrate of the active component or a hydrate of the nitrate of the active component.

[0011] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the active component is at least one of Co, Fe, and Ru; the content of the active component is 5-30% based on the total weight of the catalyst; and in the precursor of the active component, the nitrate of the active component and the hydrate of the nitrate of the active component account for more than or equal to 50% of the mass of the precursor of the active component.

[0012] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the catalyst further includes an auxiliary agent, which is at least one selected from La, Ce, Mn, and Y, and the content of the auxiliary agent is 2-10% based on the total weight of the catalyst.

[0013] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the precursor of the auxiliary agent and the precursor of the active component are simultaneously or separately contacted with the support, and then calcined; the precursor of the auxiliary agent is a soluble salt of the auxiliary agent, a hydrate of the soluble salt of the auxiliary agent, or an oxide of the auxiliary agent.

[0014] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the mixed atmosphere of NO and inert gas is at least one of NO and helium, NO and argon, and NO and nitrogen, wherein the volume fraction of NO in the mixed atmosphere is 1% to 20%; and the flow rate of the mixed atmosphere of NO and inert gas during calcination is 1 to 50 mL / min.

[0015] In one embodiment of the method for preparing the catalyst for producing aviation kerosene from syngas according to the present invention, the calcination temperature is 400-700℃, the heating rate is 0.5-20℃ / min, and the calcination time is 2-10h.

[0016] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the contact method is one of impregnation, precipitation, melt permeation, and collision contact.

[0017] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the precursor of the catalyst is reduced in an H2 atmosphere with a flow rate of 1-50 mL / min.

[0018] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the support is at least one of oxides, molecular sieves, and carbon materials, and the silicon-aluminum molar ratio of the support is 3 to 200, and the specific surface area is 200 to 1000.

[0019] In one embodiment of the method for preparing a catalyst for producing aviation kerosene from syngas according to the present invention, the molecular sieve undergoes ammonium ion exchange treatment before contacting the precursor of the active component.

[0020] The beneficial effects of this invention are:

[0021] This invention improves the dispersibility and controls the size of the active phase by calcining the contact material between the support and the active component precursor in a specific atmosphere, namely a mixed atmosphere of NO and inert gas. This results in a bifunctional supported catalyst with nanoparticle size, increasing the conversion rate of carbon monoxide in syngas and improving the C8-C content of the products. 16 Selectivity of long-chain hydrocarbons. Attached Figure Description

[0022] Figure 1 This is a scanning electron microscope (SEM) image of the catalyst in Example 3.

[0023] Figure 2 This is the XRD pattern of the catalyst in Example 1.

[0024] Figure 3 This is a chromatogram of the gas phase products of the Fischer-Tropsch synthesis reaction in Example 2, using syngas as a raw material and under appropriate conditions with a catalyst. Detailed Implementation

[0025] The technical solution of the present invention will be described in detail below. The following embodiments are implemented under the premise of the technical solution of the present invention and a detailed implementation process is given. However, the protection scope of the present invention is not limited to the following embodiments. Structures or experimental methods that do not specify specific conditions in the following embodiments are generally performed under conventional conditions.

[0026] This invention provides a method for preparing a catalyst for the production of aviation kerosene from syngas. The catalyst includes a support and an active component, wherein the active component is loaded on the support. The preparation method includes the following steps:

[0027] Step 1: The precursor of the active component is brought into contact with the support, and then calcined in a mixed atmosphere of NO and inert gas to obtain the precursor of the catalyst.

[0028] Step 2: The precursor of the catalyst is reduced to obtain the catalyst;

[0029] The precursor of the active component is a soluble salt of the active component, a hydrate of the soluble salt of the active component, or an oxide of the active component; and the precursor of the active component contains at least a nitrate of the active component or a hydrate of the nitrate of the active component.

[0030] This invention improves the dispersibility and controls the size of the active phase by calcining the contact material between the support and the active component precursor in a specific atmosphere, namely a mixed atmosphere of NO and inert gas. This results in a bifunctional supported catalyst with nanoparticle size, which increases the conversion rate of carbon monoxide in syngas and improves the C8-C content of the product. 16 Selectivity of long-chain hydrocarbons.

[0031] In detail, when the contact material between the carrier and the active component precursor is calcined under NO and inert gas, the active component precursor contains the nitrate of the active component. The nitrate of the active component decomposes to produce active component oxide, NO2 and NO. The NO atmosphere is conducive to shifting the equilibrium of the decomposition reaction in the reverse direction, reducing the decomposition rate of nitrate, resulting in a smaller active phase size, which is more conducive to the dispersion of the active phase.

[0032] In one embodiment, the active component of the present invention is a metal capable of catalytically producing aviation kerosene from syngas, such as at least one of Co, Fe, and Ru. The precursor of the active component is a soluble salt, hydrate, or oxide of Co, Fe, or Ru. The present invention does not particularly limit the type of precursor of the active component, and may include one or more of the soluble salts, hydrates, and oxides of the active component. However, the precursor of the active component of the present invention should include at least one metal nitrate, such as a nitrate or nitrate hydrate of Co, Fe, or Ru, in order to control the decomposition rate of the active component precursor.

[0033] This invention does not specifically limit the type of soluble salt of the active component, such as nitrates, chlorides, etc.

[0034] In another embodiment, the nitrate and nitrate hydrate of the active component constitute 50% or more of the precursor of the active component by mass, more preferably 100%. Thus, by controlling the ratio of nitrate and nitrate hydrate in the precursor of the active component, the decomposition rate of the active component can be better controlled, and the dispersibility of the active component can be improved. (This mass ratio is based on the mass of the active component, i.e., the mass of the metal element in the nitrate relative to the total mass of all metal elements in the precursor of the active component.)

[0035] The carrier of this invention can be an oxide, a molecular sieve, a carbon material, etc. In one embodiment, the carrier of this invention is at least one selected from ZSM-5 molecular sieve, MCM-41 molecular sieve, and silica gel. More specifically, the MCM-41 molecular sieve can be a mesoporous MCM-41 molecular sieve (e.g., pore size range of 2–10 nm, preferably 3–5 nm), the silica gel can be a mesoporous silica gel (e.g., pore size range of 2–50 nm, preferably 5–15 nm), and the ZSM-5 molecular sieve can be a microporous ZSM-5 molecular sieve (e.g., pore size range of 0.1–2 nm, preferably 0.3–1.5 nm). In another embodiment, the silicon-to-aluminum molar ratio of the carrier of this invention is 3–200, preferably 50–100. In yet another embodiment, the specific surface area of ​​the carrier of this invention is 200–1000, preferably 300–400.

[0036] In one embodiment, the molecular sieve of the present invention undergoes ammonium ion exchange treatment before contacting the precursor of the active component. The present invention does not particularly limit the ammonium ion exchange process; for example, the molecular sieve may be mixed with an ammonium salt solution, heated, then subjected to liquid-solid separation, dried, and calcined to obtain the ion-exchanged molecular sieve.

[0037] The present invention does not particularly limit the contact method between the precursor of the active component and the carrier, such as impregnation, precipitation, melt infiltration, collision contact, etc., as long as the precursor of the active component can be loaded onto the carrier.

[0038] Then, the support carrying the active component precursor is calcined in a mixed atmosphere of NO and an inert gas, wherein the inert gas is, for example, helium, argon, or nitrogen, and the mixed atmosphere of NO and inert gas can be one or more of NO and helium, NO and argon, or NO and nitrogen. In one embodiment, the volume fraction of NO in the mixed atmosphere of NO and inert gas is 1-20%, preferably 5-10%.

[0039] In another embodiment, during calcination, the flow rate of the mixed atmosphere of NO and inert gas is 1 to 50 mL / min, preferably 5 to 30 mL / min.

[0040] The calcination temperature of the present invention is, for example, 400-700°C, preferably 500-600°C, the heating rate is, for example, 0.5-20°C / min, preferably 1-10°C / min, and the calcination time is, for example, 2-10h, preferably 5-8h.

[0041] In one embodiment, the catalyst of the present invention further includes an auxiliary agent, such as at least one selected from La, Ce, Mn, and Y. The precursor of the auxiliary agent can be a soluble salt of the auxiliary agent, a hydrate of a soluble salt of the auxiliary agent, or an oxide of the auxiliary agent. The soluble salt of the auxiliary agent is, for example, a nitrate or chloride salt of the auxiliary agent. The precursor of the auxiliary agent is contacted with a support to load the auxiliary agent onto the support. In another embodiment, the precursor of the auxiliary agent and the precursor of the active component are simultaneously contacted with the support. In yet another embodiment, the contact between the precursor of the auxiliary agent and the support, and the contact between the precursor of the active component and the support, are performed separately, followed by calcination. The present invention does not particularly limit the order in which the precursors of the auxiliary agent and the active component are contacted with the support, but contacting the precursor of the auxiliary agent with the support before contacting the precursor of the active component with the support is beneficial for further improving the dispersibility of the active component.

[0042] In one embodiment, based on the total weight of the catalyst of the present invention, the content of the active component is 5-30%, preferably 10-25%, the content of the auxiliary agent is 2-10%, preferably 2-8%, and the content of the support is 60-93%, preferably 75-84%.

[0043] The catalyst precursor of the present invention can be reduced to obtain the catalyst. In one embodiment, the reduction of the catalyst precursor is carried out under an H2 atmosphere with a flow rate of 1-50 mL / min, preferably 10-40 mL / min.

[0044] Thus, the present invention provides a method for preparing a catalyst for the synthesis of aviation kerosene from syngas. The active phase of the catalyst obtained by the method of the present invention has a particle size of 5 to 100 nm, preferably 10 to 50 nm, and has a high degree of dispersion.

[0045] The catalyst obtained by this invention can be used to catalyze the production of aviation kerosene from syngas. In one embodiment, the H2 / CO molar ratio in the syngas-to-aviation kerosene reaction is 1–4, preferably 1–2. The reaction pressure ranges from 1 to 3 MPa, the reaction temperature is 200–280 °C, and the volume hourly space velocity is 100–5000.

[0046] The catalyst prepared using this invention is used to produce aviation kerosene from syngas, achieving a carbon monoxide conversion rate of over 70% and a selectivity of aviation kerosene components in the total product of over 30%, demonstrating good performance. The synthesized aviation kerosene, when blended with existing petroleum-based aviation kerosene, can be used as fuel for jet aircraft, showing broad application prospects.

[0047] The technical solution of the present invention will be further described below through specific embodiments.

[0048] Example 1

[0049] Catalyst preparation

[0050] ZSM-5 molecular sieve (silicon-aluminum molar ratio of 20, specific surface area of ​​350 m²) was used. 2 / g) was ion-exchanged with ammonium nitrate solution, with a molecular sieve to NH4NO3 molar ratio of 1:3, and heated at 60℃ for 2 hours. After the reaction was complete, it was centrifuged at 5000 r / min for 10 minutes. After centrifugation, it was dried at 100℃ for 4 hours, and then calcined at 500℃ for 4 hours.

[0051] Cobalt was loaded onto ZSM-5 molecular sieve at a content of 6 wt%. First, the appropriate amount of cobalt nitrate was accurately measured and dissolved in three times the mass of the molecular sieve in deionized water. After complete dissolution, the prepared cobalt nitrate solution was added dropwise to the ZSM-5 molecular sieve powder. The mixture was allowed to stand at room temperature for 24 hours. Then, it was placed in a vacuum drying oven and dried at 100°C for 6 hours.

[0052] The dried catalyst was calcined in a NO / nitrogen mixed atmosphere with a NO volume fraction of 3%, a flow rate of 10 mL / min, a heating rate of 10 °C / min, a calcination temperature of 500 °C, and a calcination time of 4 h. Finally, Co / ZSM-5 molecular sieve was obtained and named catalyst A. The average diameter of the active phase of the catalyst is shown in Table 2, where the average diameter of the active phase of the catalyst was calculated based on the XRD results.

[0053] Reduction and reaction of catalysts

[0054] Weigh 1.0 g of catalyst A and mix it with 2.0 g of quartz sand, then add the mixture to a reaction tube with an inner diameter of 10 mm. Introduce reducing gas (hydrogen) at a flow rate of 10 mL / min and reduce at 350 °C for 4 hours. Then introduce the reaction gas (synthesis gas) and react at a pressure of 2 MPa, a temperature of 220 °C, and a space velocity of 2000 for 25 hours. Gas samples are collected every hour for chromatographic analysis. The reaction results are shown in Table 1.

[0055] Example 2

[0056] Catalyst preparation

[0057] The preparation of the catalyst in Example 1 was repeated, except that cerium nitrate (2 wt% based on cerium) was loaded onto the cobalt-impregnated Co / ZSM-5 molecular sieve to obtain the Co / Ce / ZSM-5 catalyst, which was named catalyst B.

[0058] Reduction and reaction of catalysts

[0059] The reduction and reaction process of the catalyst in Example 1 was repeated, except that catalyst A was replaced with catalyst B. The reaction results are shown in Table 1.

[0060] Example 3

[0061] Catalyst preparation

[0062] Mesoporous MCM-41 (silicon-aluminum molar ratio 28, specific surface area 850 m²) was used. 2 The molecular sieve ( / g) was used as the carrier. The molar ratio of molecular sieve to NH4NO3 was 1:3, and the mixture was heated at 60℃ for 2 hours. After the reaction was completed, the mixture was centrifuged at 5000 r / min for 10 minutes. After centrifugation, the mixture was dried at 100℃ for 4 hours, and then calcined at 500℃ for 4 hours.

[0063] Cobalt was loaded onto MCM-41 molecular sieve at a content of 6 wt%. The corresponding amount of cobalt nitrate was dissolved in three times the mass of the molecular sieve in deionized water. After complete dissolution, the prepared cobalt nitrate solution was added dropwise to ZSM-5 molecular sieve powder that had undergone ion exchange. After standing, the mixture was placed in a vacuum drying oven and dried at 100°C for 4 hours, followed by calcination at 500°C for 4 hours to obtain catalyst C.

[0064] Reduction and reaction of catalysts

[0065] The reduction and reaction process of the catalyst in Example 1 was repeated, except that catalyst A was replaced with catalyst C. The reaction results are shown in Table 1.

[0066] Example 4

[0067] Catalyst preparation

[0068] Mesoporous silica gel (specific surface area 360m²) was used. 2 / g) and microporous ZSM-5 (silicon-aluminum molar ratio of 28, specific surface area of ​​345m²) 2 A mixture of molecular sieves and NH4NO3 (with a mass ratio of mesoporous silica gel to microporous ZSM-5 of 4) was used as the support. The molar ratio of molecular sieve to NH4NO3 was 1:3 (ammonium nitrate was 1 mol / L), and the mixture was heated at 60 °C for 2 hours. After the reaction was completed, the mixture was centrifuged at 5000 r / min for 10 minutes. After centrifugation, the mixture was dried at 100 °C for 4 hours, and then calcined at 500 °C for 4 hours.

[0069] Cobalt nitrate hexahydrate (6 wt% by mass, cobalt as a whole) was physically mixed with mesoporous silica gel and microporous ZSM5 support in a mortar for 10 min, sealed in a glass bottle, and allowed to melt-permeate at 50 °C for 24 h. Then, it was calcined in a mixed atmosphere of NO and argon (500 °C, flow rate 20 mL / min) for 4 h to obtain catalyst D.

[0070] Reduction and reaction of catalysts

[0071] The reduction and reaction process of the catalyst in Example 1 was repeated, except that catalyst A was replaced with catalyst D. The reaction results are shown in Table 1.

[0072] Example 5

[0073] Catalyst preparation

[0074] Mesoporous silica gel (specific surface area of ​​350 m²) was used. 2 / g) and microporous ZSM-5 (silicon-aluminum molar ratio of 18, specific surface area of ​​350m²) 2 A mixture of molecular sieves and NH4NO3 (mass ratio of mesoporous silica gel to microporous ZSM-5 was 4) was used as the carrier. The molecular sieve and NH4NO3 were in a molar ratio of 1:3, and the mixture was heated at 60°C for 2 hours. After the reaction was completed, the mixture was centrifuged at 5000 r / min for 10 minutes. After centrifugation, the mixture was dried at 100°C for 4 hours, and then calcined at 500°C for 4 hours.

[0075] Cobalt nitrate hexahydrate (6 wt% cobalt), ruthenium chloride (2 wt% ruthenium), and lanthanum nitrate (2 wt% lanthanum) were physically mixed with mesoporous silica gel and microporous ZSM-5 support in a mortar for 10 min. The mixture was then sealed in a glass bottle and allowed to melt-permeate at 50 °C for 24 h. Afterward, it was calcined in a mixed atmosphere of NO and helium (500 °C, flow rate 20 mL / min) for 4 h to obtain catalyst E.

[0076] Reduction and reaction of catalysts

[0077] The reduction and reaction process of the catalyst in Example 1 was repeated, except that catalyst A was replaced with catalyst E. The reaction results are shown in Table 1.

[0078] Example 6

[0079] The preparation of the catalyst in Example 1 was repeated, except that cobalt nitrate was replaced with iron nitrate, and yttrium nitrate (2 wt% yttrium content) was loaded onto iron-impregnated Fe / ZSM-5 molecular sieve to obtain Fe / Y / ZSM-5 catalyst, named catalyst F.

[0080] Reduction and reaction of catalysts

[0081] The reduction and reaction process of the catalyst in Example 1 was repeated, except that catalyst A was replaced with catalyst F. The reaction results are shown in Table 1.

[0082] Comparative Example 1

[0083] Catalyst preparation

[0084] The preparation of the catalyst in Example 5 was repeated, except that the mixed support of mesoporous silica gel and microporous ZSM-5 was replaced with an Al2O3 support (specific surface area of ​​200) to obtain a Co / Al2O3 catalyst, named catalyst G.

[0085] Reduction and reaction of catalysts

[0086] The reduction and reaction process of the catalyst in Example 5 was repeated, except that catalyst E was replaced with catalyst G. The reaction results are shown in Table 1.

[0087] Comparative Example 2

[0088] The preparation of the catalyst in Example 1 was repeated, except that the calcination atmosphere was changed from NO / nitrogen atmosphere to nitrogen atmosphere to obtain catalyst H. The average diameter of the active phase of the catalyst is shown in Table 2.

[0089] Reduction and reaction of catalysts

[0090] The reduction and reaction process of the catalyst in Example 1 was repeated, except that catalyst A was replaced with catalyst H. The reaction results are shown in Table 1.

[0091] Table 1

[0092]

[0093] Table 2

[0094]

[0095] Of course, the present invention may have other various embodiments. Without departing from the spirit and essence of the present invention, those skilled in the art can make various corresponding changes and modifications according to the present invention, but these corresponding changes and modifications should all fall within the protection scope of the claims of the present invention.

Claims

1. A method for preparing a catalyst for the production of aviation kerosene from syngas, the catalyst comprising a support and an active component, wherein the active component is supported on the support, characterized in that, The preparation method includes the following steps: Step 1: The precursor of the active component is contacted with the support, and then calcined in a mixed atmosphere of NO and inert gas to obtain the precursor of the catalyst; Step 2: The precursor of the catalyst is reduced to obtain the catalyst; The precursor of the active component is a soluble salt of the active component, a hydrate of the soluble salt of the active component, or an oxide of the active component; and the precursor of the active component contains at least a nitrate of the active component or a hydrate of the nitrate of the active component. The carrier is at least one of ZSM-5 molecular sieve, MCM-41 molecular sieve, and silica gel, and the silica-alumina molar ratio of the carrier is 3 to 200, and the specific surface area is 200 to 1000.

2. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 1, characterized in that, The active component is at least one of Co, Fe, and Ru; the content of the active component is 5-30% based on the total weight of the catalyst; in the precursor of the active component, the nitrate of the active component and the hydrate of the nitrate of the active component account for more than or equal to 50% of the mass of the precursor of the active component.

3. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 2, characterized in that, The catalyst further includes an auxiliary agent, which is at least one of La, Ce, Mn, and Y, and the content of the auxiliary agent is 2-10% based on the total weight of the catalyst.

4. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 3, characterized in that, The precursor of the auxiliary agent and the precursor of the active component are simultaneously or separately contacted with the carrier, and then calcined; the precursor of the auxiliary agent is a soluble salt of the auxiliary agent, a hydrate of the soluble salt of the auxiliary agent, or an oxide of the auxiliary agent.

5. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 1, characterized in that, The mixed atmosphere of NO and inert gas is at least one of NO and helium, NO and argon, and NO and nitrogen, wherein the volume fraction of NO in the mixed atmosphere is 1% to 20%; the flow rate of the mixed atmosphere of NO and inert gas during calcination is 1 to 50 mL / min.

6. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 1, characterized in that, The calcination temperature is 400~700℃, the heating rate is 0.5~20℃ / min, and the calcination time is 2~10h.

7. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 1, characterized in that, The contact method is one of the following: impregnation, precipitation, melt penetration, or collision contact.

8. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 1, characterized in that, The precursor of the catalyst is reduced in an H2 atmosphere with a flow rate of 1~50 mL / min.

9. The method for preparing the catalyst for producing aviation kerosene from syngas according to claim 1, characterized in that, The molecular sieve undergoes ammonium ion exchange treatment before contacting the precursor of the active component.

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