Catalyst for preparing low-carbon olefins from synthesis gas and method for preparing the same

Abstract

The application provides a preparation method of a catalyst for preparing low-carbon olefins from synthesis gas, which comprises the following steps: mixing a soluble salt solution of a metal component with phosphoric acid, performing a precipitation reaction, and drying the obtained slurry; calcining the dried product at 300-500 DEG C for 1-24h to obtain solid grains with a diameter of 0.5-7nm; immersing the solid grains in a soluble salt solution of an auxiliary agent, reacting for 1-3h, then evaporating the reaction system, and transferring the obtained solid product to a calcination furnace at 350-650 DEG C for 1-8h to obtain a catalyst for preparing olefins from synthesis gas; the preparation method uses phosphoric acid as an essential auxiliary agent, effectively reduces the amount of the auxiliary agent, and saves the preparation cost of the catalyst; the stability of the phosphoric acid salt is high, the catalyst is not deactivated in a long operation, and the replacement cost of the catalyst is saved; the catalyst is used for preparing olefins, the content of C5+ products can be reduced by 50%-90%, and the proportion of C2-C4 olefins can be increased to 75%-88%. The economic efficiency of the product is improved, and the separation cost is reduced.

Description

Technical Field

[0001] This invention relates to the fields of clean coal chemical industry and catalyst technology, and in particular to a catalyst for the preparation of low-carbon olefins from syngas and its preparation method. Background Technology

[0002] Olefins are among the most important chemical raw materials, providing the foundation for the synthesis of various plastics, fibers, and medical devices. China's current ethylene and propylene production both exceed 50 million tons per year, and C4 olefin production exceeds 6 million tons per year. The remaining C5 to C12 high-carbon olefins can be used to prepare various high-performance polyethylene copolymers, detergents, and fine chemical products, forming a vast chemical and materials product network. Currently, most olefins are still obtained through the cracking of petroleum feedstocks. Other developing routes include coal-to-methanol olefin production and ethane dehydrogenation-to-ethylene production. The bottleneck of the petroleum route lies in its resource dependence. The coal-to-methanol olefin production route is lengthy, requires large equipment investments, and has high carbon emissions.

[0003] The direct production of olefins from syngas is an emerging technological route. Since syngas can be derived from coal chemical, natural gas chemical, or biomass chemical processes, this route has strong vitality and market adaptability. Undoubtedly, the catalyst is the most crucial element in the direct production of olefins from syngas. Currently, catalysts using a coupling of metal oxides and molecular sieves are available, which are also metal carbide forms. Catalysts with simple carbide and basic promoter structures often yield large quantities of C5+ and higher olefins, limiting their applications. Catalysts using a coupling of metal oxides and molecular sieves can produce more C2-C4 products, but their catalyst lifetime is short, and even when C2-C4 products are obtained, the proportion of longer carbon chains is very large. Because this process is still in its early stages of development, these problems have not yet been effectively resolved. Summary of the Invention

[0004] In view of the above-mentioned problems in the prior art, the present invention provides a catalyst for the preparation of low-carbon olefins from syngas and a method thereof. The catalyst can precisely control the limit of carbon chain growth during the preparation of olefins from syngas and has the effect of highly selectively producing C2-C4 olefins.

[0005] The specific details of the invention are as follows:

[0006] In a first aspect, the present invention provides a method for preparing a catalyst for the synthesis of low-carbon olefins from syngas, the method comprising:

[0007] Step 1: Mix the soluble salt solution of the metal component with phosphoric acid to carry out a precipitation reaction, and dry the filtered slurry.

[0008] Step 2: Calcine the dried material at 300-500℃ for 1-24 hours to obtain solid grains with a diameter of 0.5-7nm;

[0009] Step 3: Immerse the solid crystals in a soluble salt solution of auxiliary agents and react for 1-3 hours. Then evaporate the reaction system to dryness and transfer the obtained solid material to calcine at 350-650℃ for 1-8 hours to obtain a catalyst for the direct preparation of olefins from syngas.

[0010] The metal component is one or more of iron, cobalt, nickel, palladium, platinum, manganese, chromium and zinc, and the soluble salt solution of the metal component is a sulfate solution, a carbonate solution or a chloride solution.

[0011] The auxiliary agent is one or more of lithium, sodium, calcium, magnesium and strontium, and the soluble salt solution of the auxiliary agent is a sulfate solution, a carbonate solution or a chloride solution.

[0012] In the catalyst, the mass ratio of phosphoric acid to the metal component is 1:50 to 2:1, and the mass ratio of the auxiliary agent to the metal component is 1:100 to 1:10.

[0013] Optionally, the precipitation reaction is carried out at room temperature.

[0014] Optionally, the drying temperature is 100-150℃ and the time is 1-6 hours.

[0015] Optionally, in step 1, after mixing the salt solution containing the metal component with phosphoric acid, the method further includes: adding hydrogen peroxide solution dropwise to carry out a precipitation reaction, and drying the filtered slurry.

[0016] In a second aspect, the present invention provides a catalyst for the direct preparation of olefins from syngas obtained by the preparation method described in the first aspect above.

[0017] Optionally, the catalyst includes a metal component, essential additives, and auxiliary additives;

[0018] The metal component is one or more of iron, cobalt, nickel, palladium, platinum, manganese, chromium and zinc;

[0019] The essential auxiliary agent is phosphoric acid;

[0020] The auxiliary agent is one or more of lithium, sodium, calcium, magnesium and strontium;

[0021] The mass ratio of phosphoric acid to metal component is 1:50 to 2:1, and the mass ratio of auxiliary agent to metal component is 1:100 to 1:10.

[0022] Optionally, the catalyst is used to directly prepare olefins from syngas, and the resulting reaction products contain hydrocarbons with 1-5 carbon atoms, of which C2-C4 olefins account for 75%-88%.

[0023] Optionally, the use of the catalyst for the direct preparation of olefins from syngas includes:

[0024] The catalyst is loaded into the reactor, the temperature is controlled at 380-500℃, and a reducing gas is introduced to reduce the catalyst for 3-8 hours.

[0025] Syngas is introduced into the reactor, and the reactor pressure is controlled at 1-6 MPa and the temperature at 250-380℃, so that the syngas reacts on the catalyst to produce hydrocarbon reaction products.

[0026] The space velocity of the catalyst is 2000-20000 ml / gcat / h.

[0027] Optionally, the reducing gas includes one or more of CH4, CO, and H2.

[0028] Optionally, the reactor includes a fixed bed, a fluidized bed, or a moving bed.

[0029] Compared with the prior art, the present invention has the following advantages:

[0030] The present invention provides a method for preparing a catalyst for the synthesis of low-carbon olefins from syngas, which uses phosphoric acid as an essential auxiliary agent, effectively reducing the content of alkaline auxiliary agents (auxiliary agents) by 30%-80% and saving 25%-30% of the catalyst preparation cost; moreover, phosphate has strong stability, ensuring that the catalyst does not deactivate during long-term operation, and can save catalyst replacement costs.

[0031] Furthermore, using the catalyst provided in this invention for the preparation of low-carbon olefins from syngas can reduce the content of C5+ products by 50%-90% and increase the proportion of C2-C4 olefins to 75%-88%. This results in a 30-50% improvement in product economics and a 30-60% reduction in separation costs. Attached Figure Description

[0032] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0033] Figure 1 A flowchart illustrating the preparation method of the catalyst for the synthesis of low-carbon olefins from syngas provided in an embodiment of the present invention is shown. Detailed Implementation

[0034] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. Based on the embodiments 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 protection scope of the present invention. Furthermore, all other embodiments obtained by those skilled in the art without inventive effort are within the protection scope of the present invention.

[0035] Specific experimental steps or conditions are not specified in the embodiments; they can be performed according to the conventional experimental steps or conditions described in the prior art. Reagents and other instruments used, unless otherwise specified, are all commercially available conventional reagent products. Furthermore, the accompanying drawings are merely illustrative diagrams of the embodiments of the present invention and are not necessarily drawn to scale. The same reference numerals in the drawings denote the same or similar parts, and therefore, repeated descriptions of them will be omitted. Some block diagrams shown in the drawings are functional entities and do not necessarily correspond to physically or logically independent entities.

[0036] Techniques, methods, and devices known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques, methods, and devices should be considered part of this specification.

[0037] In the description of this invention, it should be understood that the use of terms such as "first" and "second" to define components is merely for the purpose of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore should not be construed as limiting the scope of protection of this invention.

[0038] Furthermore, the technical features involved in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.

[0039] In a first aspect, the present invention provides a method for preparing a catalyst for the synthesis of low-carbon olefins from syngas. Figure 1 A flowchart illustrating the preparation method of the catalyst for the synthesis of low-carbon olefins from syngas provided in an embodiment of the present invention is shown, as follows: Figure 1 As shown, the preparation method includes:

[0040] Step 1: Mix the soluble salt solution of the metal component with phosphoric acid to carry out a precipitation reaction, and dry the filtered slurry.

[0041] Step 2: Calcine the dried material at 300-500℃ for 1-24 hours to obtain solid grains with a diameter of 0.5-7nm;

[0042] Step 3: Immerse the solid crystals in a soluble salt solution of auxiliary agents and react for 1-3 hours. Then evaporate the reaction system to dryness and transfer the obtained solid material to calcine at 350-650℃ for 1-8 hours to obtain a catalyst for the direct preparation of olefins from syngas.

[0043] The metal component is one or more of iron, cobalt, nickel, palladium, platinum, manganese, chromium and zinc, and the soluble salt solution of the metal component is a sulfate solution, a carbonate solution or a chloride solution.

[0044] The auxiliary agent is one or more of lithium, sodium, calcium, magnesium and strontium, and the soluble salt solution of the auxiliary agent is a sulfate solution, carbonate solution or chloride solution;

[0045] In the catalyst, the mass ratio of phosphoric acid to metal components is 1:50 to 2:1, and the mass ratio of auxiliary agents to metal components is 1:100 to 1:10.

[0046] In the preparation method of the catalyst for the synthesis of low-carbon olefins from syngas provided by this invention, phosphoric acid is used as an essential auxiliary agent, which is co-precipitated with a soluble salt of a metal component. After filtration, drying, and calcination, nano-sized solid crystals are obtained. The solid crystals are then impregnated in a soluble salt solution of an auxiliary agent, allowing the auxiliary agent to be loaded onto the surface of the solid crystals. After drying and calcination, the finished catalyst is obtained. This preparation process effectively reduces the amount of alkaline auxiliary agent used, saving catalyst preparation costs. Furthermore, phosphate has strong stability, ensuring that the catalyst does not deactivate during long-term operation, thus saving catalyst replacement costs. Using the catalyst for the synthesis of low-carbon olefins from syngas provided by this invention, the content of C5+ products can be reduced by 50%-90%, and the proportion of C2-C4 olefins can be increased to 75%-88%. It can effectively control the carbon number of hydrocarbon products to below 5 or 4, improving product economics by 30-50% and reducing separation costs by 30-60%.

[0047] To enable those skilled in the art to more clearly understand the present invention, the catalyst for the synthesis of low-carbon olefins from syngas and its preparation method described in the present invention are now described in detail through the following examples.

[0048] Example 1

[0049] A precipitation reaction was carried out using 1 ml of a 1 mol / L solution of iron chloride (FeCl2) and 3 ml of phosphoric acid to produce ferric divalent phosphate. After filtration, the slurry was dried at 150°C for 1 hour and calcined at 500°C for 1 hour to obtain a solid with crystals of 0.5-4 nm in diameter. 1 g of the solid was then immersed in 1 ml of a 1 mol / L solution of lithium nitrate (LiNO3) and reacted for 2-3 hours. The solution was then evaporated to dryness and calcined at 650°C for 3 hours to obtain the final product. The mass ratio of phosphoric acid to iron in the catalyst was 2:1. The mass ratio of lithium to iron in the auxiliary agent was 1:100.

[0050] The obtained catalyst was packed into a fixed-bed reactor and reduced with a reducing gas (H2) at 420°C for 8 hours. Then, syngas was introduced, with the pressure controlled at 3.6 MPa, the temperature at 345-350°C, and the space velocity at 2000 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins comprising 80%.

[0051] Example 2

[0052] A precipitation reaction was carried out using 2 ml of a 0.5 mol / L solution of cobalt nitrate and 10 ml of phosphoric acid to produce divalent phosphate. After filtration, the slurry was dried at 100°C for 6 hours and then calcined at 300°C for 24 hours to obtain a solid with crystals of 3-7 nm in diameter. 1 g of the solid was then immersed in 1 ml of a 0.1 mol / L solution of sodium chloride and reacted for 3 hours. The solution was then evaporated to dryness and calcined at 350°C for 8 hours to obtain the final product. The mass ratio of phosphoric acid to cobalt in the catalyst was 1:10. The mass ratio of sodium to cobalt in the auxiliary agent was also 1:10.

[0053] The obtained catalyst was packed into a fluidized bed reactor and reduced with a reducing gas (50% CO, 50% H2) at 450°C for 5 hours. Then, syngas was introduced, with the pressure controlled at 3 MPa, the temperature at 250°C, and the space velocity ranging from 20000 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins comprising 88%.

[0054] Example 3

[0055] A precipitation reaction was carried out using 10 ml of a 5 mol / L cobalt nitrate solution and 50 ml of phosphoric acid to produce divalent phosphate. After filtration, the slurry was dried at 100-150℃ for 1-6 hours and then calcined at 390℃ for 14 hours to obtain a solid with crystals of 5-7 nm in diameter. 1 g of the solid was then immersed in 0.01 ml of a 1 mol / L calcium nitrate solution and reacted for 2.3 hours. The solution was then evaporated to dryness and calcined at 480℃ for 4.5 hours to obtain the final product. The mass ratio of phosphoric acid to cobalt in the catalyst was 1:1. The mass ratio of the auxiliary agent (calcium) to the metal component (cobalt) was 1:50.

[0056] The obtained catalyst was packed into a moving bed reactor and reduced with a reducing gas (40% CH4, 20% CO, 40% H2) at 500℃ for 3 hours. The pressure was 6 MPa, the temperature was 280-300℃, and the space velocity was 2500 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins accounting for 79%.

[0057] Example 4

[0058] A precipitation reaction was carried out using 8 ml of a 1 mol / L nitrate solution of metals (5% iron, 95% nickel) and 20 ml of phosphoric acid to generate divalent phosphate. Hydroxyl peroxide was then used to oxidize the phosphate, producing trivalent phosphate. After filtration, the slurry was dried at 130°C for 3 hours and calcined at 450°C for 12 hours to obtain a solid with crystals of 3-5 nm in diameter. 1.6 g of the solid was then immersed in 0.2 ml of a 1 mol / L nitrate solution of 50% calcium or 50% magnesium, reacted for 2 hours, and then the solution was evaporated to dryness. The catalyst was then calcined at 520°C for 4 hours to obtain the final product. The mass ratio of phosphoric acid to the metal components (iron, nickel) on the catalyst was 1:5. The mass ratio of the auxiliary agents (calcium and magnesium) to the metal components (iron, nickel) was 1:80.

[0059] The obtained catalyst was placed in a fluidized bed reactor and reduced with reducing gases (CH4, CO, H2) at 400℃ for 3.5 hours. Syngas was introduced at a pressure of 1 MPa, a temperature of 250-280℃, and a space velocity (HSV) of 5000 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins comprising 87%.

[0060] Example 5

[0061] A precipitation reaction was carried out using 10 ml of a 0.9 mol / L nitrate solution containing 99.9% iron, 0.05% palladium, and 0.05% platinum, and 5 ml of phosphoric acid to generate divalent phosphate. After filtration, the slurry was dried at 130°C for 4 hours and then calcined at 450°C for 13 hours to obtain a solid with crystals of 2-6 nm in diameter. 1 g of the solid was then immersed in 5 ml of a 0.1 mol / L chloride solution containing 20% ​​strontium and 80% potassium, and reacted for 2-3 hours. The solution was then evaporated to dryness and calcined at 480°C for 3 hours to obtain the final product. The mass ratio of phosphoric acid to the metal components (iron, palladium, platinum) on the catalyst was 1:50. The mass ratio of the auxiliary agents (strontium and potassium) to the metal components (iron, palladium, platinum) was 1:90.

[0062] The obtained catalyst was placed in a fixed-bed reactor and reduced with a reducing gas (60% CO, 40% H2) at 380°C for 6 hours. Syngas was introduced at a pressure of 2 MPa, a temperature of 380°C, and a space velocity (HSV) of 14000 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins comprising 83%.

[0063] Example 6

[0064] A precipitation reaction was carried out using 20 ml of a 2 mol / L solution of metal (85% iron, 15% manganese) nitrate and 50 ml of phosphoric acid to generate divalent phosphate. This divalent phosphate was then oxidized to trivalent phosphate by hydrogen peroxide treatment. After filtration, the slurry was dried at 130°C for 4 hours and calcined at 450°C for 13 hours to obtain a solid with crystals of 1.5-4.5 nm in diameter. 1 g of this solid was then immersed in 8 ml of a 2 mol / L solution of lithium nitrate and reacted for 3 hours. The solution was then evaporated to dryness and calcined at 400°C for 8 hours to obtain the final product. The mass ratio of phosphoric acid to the metal components (iron, manganese) on the catalyst was 1:20. The mass ratio of the auxiliary agent (lithium) to the metal components (iron, manganese) was also 1:20.

[0065] The obtained catalyst was placed in a fixed-bed reactor and reduced with a reducing gas (60% CO, 40% H2) at 460 °C for 4 hours. Syngas was introduced at a pressure of 2 MPa, a temperature of 330 °C, and a space velocity (HSV) of 4000 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins comprising 84%.

[0066] Example 7

[0067] A precipitation reaction was carried out using 20 ml of a 0.5 mol / L solution of nitrates containing 95% iron and 5% chromium, and 10 ml of phosphoric acid, to produce divalent phosphates. After filtration, the slurry was dried at 130°C for 4 hours and then calcined at 450°C for 13 hours to obtain a solid with crystals of 2-6 nm in diameter. 1 g of the solid was then immersed in a 0.5 mol / L solution of calcium chloride and reacted for 1 hour. The solution was then evaporated to dryness and calcined at 600°C for 1 hour to obtain the final product. The mass ratio of phosphoric acid to the metal components (iron and chromium) on the catalyst was 1:2.5. The mass ratio of the auxiliary agent (calcium) to the metal components (iron and chromium) was 1:15.

[0068] The obtained catalyst was placed in a fixed-bed reactor and reduced with a reducing gas (60% CO, 40% H2) at 460°C for 4 hours. Syngas was introduced at a pressure of 2 MPa, a temperature of 360°C, and a space velocity (HSV) of 6000 ml / gcat / h. The resulting hydrocarbons had 1-5 carbon atoms, with C2-C4 olefins comprising 84%.

[0069] Example 8

[0070] A precipitation reaction was carried out using 20 ml of a 1 mol / L solution of metal (50% iron, 50% zinc) nitrate and 10 ml of phosphoric acid to produce divalent phosphate. After filtration, the slurry was dried at 140°C for 3 hours and then calcined at 480°C for 5 hours to obtain a solid with crystals of 2-5 nm in diameter. 1 g of the solid was then immersed in 10 ml of a 0.6 mol / L solution of sodium carbonate and reacted for 2-3 hours. The solution was then evaporated to dryness and calcined at 500°C for 2 hours to obtain the final product. The mass ratio of phosphoric acid to the metal components (iron, zinc) on the catalyst was 1:3. The mass ratio of the auxiliary agent (sodium) to the metal components (iron, zinc) was 1:30.

[0071] The obtained catalyst was placed in a fluidized bed reactor and reduced with a reducing gas (H2) at 430°C for 4 hours. Syngas was introduced at a pressure of 5 MPa, a temperature of 340°C, and a space velocity (HSV) of 8000 ml / gcat / h. The resulting hydrocarbons had 1-4 carbon atoms, with C2-C4 olefins comprising 77%.

[0072] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. In addition, those skilled in the art can combine and integrate the different embodiments or examples described in this specification.

[0073] For the sake of simplicity, the method embodiments are described as a series of actions. However, those skilled in the art should understand that the present invention is not limited to the described order of actions, as some steps can be performed in other orders or simultaneously according to the present invention. Furthermore, those skilled in the art should also understand that the embodiments described in the specification are preferred embodiments, and the actions and components involved are not necessarily essential to the present invention.

[0074] The catalyst for producing low-carbon olefins from syngas and its preparation method provided by the present invention have been described in detail above. Specific examples have been used to illustrate the principle and implementation of the present invention. The description of the above examples is only for the purpose of helping to understand the method and core idea of ​​the present invention. At the same time, for those skilled in the art, there will be changes in the specific implementation and application scope based on the idea of ​​the present invention. Therefore, the content of this specification should not be construed as a limitation of the present invention.

Claims

1. A method for preparing a catalyst for the synthesis of low-carbon olefins from syngas, characterized in that, The preparation method includes: Step 1: Mix the soluble salt solution of the metal component with phosphoric acid to carry out a precipitation reaction, and dry the filtered slurry. Step 2: Calcine the dried material at 300-500 ℃ for 1-24 h to obtain solid grains with a diameter of 0.5-7 nm; Step 3: Immerse the solid crystals in a soluble salt solution of the auxiliary agent and react for 1-3 h. Then evaporate the reaction system to dryness and transfer the obtained solid material to calcine at 350-650 °C for 1-8 h to obtain a catalyst for the direct preparation of olefins from syngas. The metal component is one or more of iron, cobalt, nickel, palladium, platinum, manganese, chromium and zinc, and the soluble salt solution of the metal component is a sulfate solution or a chloride solution. The auxiliary agent is one or more of lithium, sodium, calcium, magnesium and strontium, and the soluble salt solution of the auxiliary agent is a sulfate solution or a chloride solution. In the catalyst, the mass ratio of phosphoric acid to the metal component is 1:50 to 2:1, and the mass ratio of the auxiliary agent to the metal component is 1:100 to 1:

10.

2. The preparation method according to claim 1, characterized in that, The precipitation reaction is carried out at room temperature.

3. The preparation method according to claim 1, characterized in that, The drying temperature is 100-150℃, and the time is 1-6 hours.

4. The preparation method according to claim 1, characterized in that, In step 1, after mixing the salt solution of the metal component with phosphoric acid, the method further includes: adding hydrogen peroxide solution dropwise to carry out a precipitation reaction, and drying the filtered slurry.

5. A catalyst for the direct preparation of olefins from syngas obtained by any of the preparation methods described in claims 1-4.

6. The catalyst according to claim 5, characterized in that, When the catalyst is used to directly prepare olefins from syngas, the resulting reaction products contain hydrocarbons with 1-5 carbon atoms, of which C2-C4 olefins account for 75%-88%.

7. The catalyst according to claim 6, characterized in that, The use of the catalyst for the direct preparation of olefins from syngas includes: The catalyst is loaded into the reactor, the temperature is controlled at 380-500℃, and a reducing gas is introduced to reduce the catalyst for 3-8 hours. Syngas is introduced into the reactor, and the reactor pressure is controlled at 1-6 MPa and the temperature at 250-380℃, so that the syngas reacts on the catalyst to produce hydrocarbon reaction products. The space velocity of the synthesis gas is 2000-20000 mL / gcat / h.

8. The catalyst according to claim 7, characterized in that, The reducing gas includes one or more of CH4, CO, and H2.

9. The catalyst according to claim 7, characterized in that, The reactor includes a fixed bed, a fluidized bed, or a moving bed.

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