Method and system for preparing 1, 1, 3-trichloropropene through gas phase cracking

Abstract

The invention discloses a method and system for preparing 1, 1, 3-trichloropropene through gas phase cracking, and belongs to the technical field of organic synthesis.The method comprises the following steps that 1, 1, 1, 3-tetrachloropropane is preheated to be vaporized and then introduced into a tubular fixed bed reactor provided with a catalyst bed layer to be subjected to a dehydrochlorination reaction, and 1, 1, 3-trichloropropene is obtained; the catalyst bed layer is formed by stacking a self-supporting structured metal catalyst, and the self-supporting structured metal catalyst is made of one or a combination of more of iron, zinc, copper, cobalt and nickel; the self-supporting structured metal catalyst has an open-pore annular structure, the open-pore annular structure is selected from one of a Raschig ring, a Pall ring, a theta ring or a cascade ring, and the catalyst with the corresponding structure can realize high gas flux, carbon deposition blockage resistance and low mass transfer resistance, and is good in catalytic effect, less in carbon deposition and low in maintenance cost. The method provided by the invention has the advantages of high reaction conversion rate and good selectivity on 1, 1, 3-trichloropropene.

Description

Technical Field

[0001] This invention belongs to the field of organic synthesis technology, specifically relating to a method and system for preparing 1,1,3-trichloropropene by gas-phase pyrolysis. Background Technology

[0002] 1,1,3-Trichloropropene (HCC-1240za) is an important chemical intermediate, primarily used in the synthesis of the refrigerant 2,3,3,3-tetrafluoropropene (HFO-1234yf). This refrigerant possesses zero ozone depletion potential (ODP) and extremely low global warming potential (GWP). As a new generation of environmentally friendly refrigerants, it is gradually replacing high-GWP hydrofluorocarbons (HFCs) and is widely used in automotive air conditioning and commercial refrigeration. Furthermore, HCC-1240za is also widely used in pesticide synthesis, pharmaceutical manufacturing, and polymer materials. In pesticide synthesis, it can be used to construct fluorinated active molecules, improving efficacy and stability. In pharmaceutical manufacturing, it is a key monomer for synthesizing certain fluorinated drugs. In polymer materials, it can be used as a modifying monomer or additive, endowing specialty polymers with unique weather resistance and chemical stability.

[0003] Currently, the main raw material for the industrial production of HCC-1240za is 1,1,1,3-tetrachloropropane. HCC-1240za can be prepared from 1,1,1,3-tetrachloropropane through a dehydrochlorination reaction. Several synthetic methods for HCC-1240za have been disclosed in existing technologies. Chinese patent document CN111643917A discloses a continuous production apparatus and method for 1,1,3-trichloropropene. This invention utilizes a continuous reactive distillation unit to separate and couple the reactant 1,1,1,3-tetrachloropropane with the product 1,1,3-trichloropropene, promptly removing the product and preventing it from prolonged heating and deterioration within the reactor, thus improving reaction yield. However, this production apparatus has a complex structure and high investment costs, and its core reaction relies on traditional FeCl3 block / powder catalysts, failing to fundamentally solve the problems of catalytic efficiency and reaction selectivity.

[0004] Chinese patent document CN105121395A discloses a method for preparing 1,1,3-trichloropropene. This method involves adding one or more UV-stabilizing and / or antioxidant compounds to the dehydrochlorination reaction system. These UV-stabilizing and antioxidant compounds can act as inhibitors to suppress the formation of high-boiling substances during the FeCl3-catalyzed dehydrochlorination of 1,1,1,3-tetrachloropropane, thereby improving the selectivity of the target product. However, this increases the complexity of the raw materials and post-processing steps, and remains limited to liquid-phase systems or specific catalyst deactivation issues.

[0005] Chinese patent document CN120058466A discloses a process for the dehydrochlorination of 1,1,1,3-tetrachloropropane. This invention modifies γ-alumina powder with an aminosilane coupling agent to obtain modified γ-alumina powder; a catalyst is obtained by impregnation of the modified γ-alumina powder loaded with a trivalent metal salt; the catalyst is activated; and 1,1,1,3-tetrachloropropane is introduced to carry out the dehydrochlorination reaction at adjusted reaction temperature and pressure to obtain 1,1,3-trichloropropene. This catalyst allows the active component to adhere to a solid matrix, and the catalytic effect is affected by the uniformity and loading rate of the active component.

[0006] Therefore, it is necessary to improve the preparation process of 1,1,3-trichloropropylene in order to improve catalytic efficiency, reduce reaction energy consumption, and avoid problems such as catalyst deactivation due to local overheating or increased side reactions. Summary of the Invention

[0007] To address the shortcomings of existing technologies, this invention provides a method for preparing 1,1,3-trichloropropylene by gas-phase pyrolysis, which uses a self-supporting structured metal catalyst and combines it with a specific gas-phase reaction method, resulting in high reaction conversion and good selectivity for 1,1,3-trichloropropylene.

[0008] The specific technical solution adopted is as follows: A method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis includes the following steps: 1,1,1,3-Tetrachloropropane is preheated to vaporization and then passed into a tubular fixed-bed reactor equipped with a catalyst bed to carry out a dehydrochlorination reaction to obtain 1,1,3-trichloropropene. The catalyst bed is formed by stacking self-supporting structured metal catalysts with a packing density of 0.35~2 g / cm³. 3 The self-supporting structured metal catalyst is made of one or a combination of iron, zinc, copper, cobalt, and nickel; the self-supporting structured metal catalyst has an open-hole annular structure (with axial through holes, annular wall openings, and annular wall window structures), and the open-hole annular structure is selected from Raschig rings, Pall rings, θ rings, or step rings; The tubular fixed-bed reactor is made of Inconel, Hastelloy, or stainless steel.

[0009] The catalyst used in this invention has a "self-supporting structured metal open-cell annular morphology without carrier" (Raschig ring, Pall ring, θ ring, or step ring). Its core advantage lies in its structural characteristics. Through the "regular open-cell structure", it achieves high gas flux, resistance to carbon buildup and blockage, and low mass transfer resistance. It has good catalytic effect, less carbon buildup, and will not cause reactor blockage. After deactivation, it can be directly poured out from the bottom, making it easy to replace and maintain. Moreover, the raw materials for the structured metal catalyst are readily available and inexpensive, which can save production costs and is suitable for industrial production.

[0010] The tubular fixed-bed reactor is preferably made of Inconel 600 nickel alloy tubes, Hastelloy C-276 alloy tubes, or 316L stainless steel tubes.

[0011] In traditional reactors, catalyst particles in the catalyst bed are physically separated from the reactor wall. Inorganic salt or metal oxide supported catalysts differ significantly from the metal reactor wall material, resulting in substantial contact thermal resistance (wall effect). This leads to low radial heat transfer efficiency, hot spots within the bed, catalyst sintering, and side reactions. Furthermore, it enlarges fluid channels near the wall, creating channeling that can cause short-circuiting of some reactants and uneven conversion. The mismatch in thermal expansion coefficients during the thermal cycle also causes catalyst particles to pulverize, increasing bed pressure drop. These factors severely restrict the reactor's operating efficiency and stability. This invention utilizes a self-supporting structured metal catalyst made of pure metal, forming a low-thermal-resistance, close contact with the alloy reactor wall. This creates a continuous, high-thermal-conductivity network within the catalyst bed, achieving efficient radial heat transfer and temperature homogenization control of the reaction bed.

[0012] Preferably, the preheating temperature of 1,1,1,3-tetrachloropropane is 80°C to 200°C, and more preferably 60°C to 180°C.

[0013] Preferably, the dehydrochlorination reaction parameters include: space velocity 1–60 min. -1 The reaction pressure is 50 kPa to 300 kPa, the reaction temperature is 280℃ to 450℃, and the residence time is 1 to 30 seconds.

[0014] Further preferred parameters for the dehydrochlorination reaction include: space velocity 20–30 min. -1 The reaction pressure is 90 kPa to 120 kPa, the reaction temperature is 340℃ to 360℃, and the residence time is 1 to 10 s. If the space velocity is too low or the residence time is too long, the reactants will remain on the catalyst surface for too long, which can easily lead to over-reaction; if the space velocity is too high or the residence time is too short, the reactants will not fully contact the active sites before flowing out, resulting in a decrease in conversion rate.

[0015] Self-supporting structured metal catalysts do not require the assistance of supports such as alumina and activated carbon. Due to their own open-pore ring structure, their geometric specific surface area can reach 100 to 1000 times that of conventional solid catalysts (such as iron wire, iron filings, and powder).

[0016] Further preferably, the self-supporting structured metal catalyst is made of a mixture of iron and zinc (iron to zinc mass ratio of 1:0.05~0.3) or a mixture of iron and copper (iron to copper mass ratio of 1:0.05~0.3). In the reaction of 1,1,1,3-tetrachloropropane cracking and deHClation to prepare 1,1,3-trichloropropene, it is susceptible to chlorine poisoning and coking deactivation. In the Fe-Zn combination, Zn acts as a selective chlorine trapping agent and structural isolator, which significantly improves the chlorine resistance stability of the catalyst. In the Fe-Cu combination, Cu acts as a highly efficient hydrogen activation and transfer center, forming a tandem catalytic pathway with Fe, which effectively suppresses deep dehydrogenation side reactions and improves the selectivity of the target product.

[0017] The aforementioned self-supporting structured metal catalyst can be obtained commercially or through custom manufacturing. The size is selected according to the diameter of the reaction tube and is not particularly limited. The general size is 3mm-5mm×3mm-5mm×3mm (length×width×height). Specifically, the sidewall of the Pall ring has multiple rectangular openings, and the blades at the edge of the openings are bent towards the center of the ring. The θ ring is made of metal wire mesh and has a θ-shaped cross section.

[0018] Specifically, the self-supporting structured metal catalyst undergoes pretreatment before use: the self-supporting structured metal catalyst is loaded into a tubular fixed-bed reactor, and under an inert gas (nitrogen) atmosphere, the temperature is programmed to rise to 300-500°C at a certain heating rate (2-5°C / min), and held at that temperature for 2-4 hours to remove possible oil and oxides from the surface, eliminate stress, reduce oxidation, induce slight nitriding, improve catalyst activity and stability, and extend service life.

[0019] In a further preferred embodiment, vaporized 1,1,1,3-tetrachloropropane is introduced into one end of the tubular fixed-bed reactor for dehydrochlorination reaction, and the reaction products are collected at the other end of the tubular fixed-bed reactor. After condensation and gas-liquid separation, the non-condensable gases (mainly HCl and a small amount of carrier gas) enter the subsequent processing system, and the condensed products are separated by distillation to obtain 1,1,3-trichloropropene.

[0020] Preferably, the conversion rate of 1,1,1,3-tetrachloropropane is 60% to 90%, and the selectivity of 1,1,3-trichloropropene is 90% to 99%.

[0021] The present invention also provides a system for producing 1,1,3-trichloropropene, the structure of which includes: Vaporization device: used to preheat 1,1,1,3-tetrachloropropane to vaporize it; Tubular fixed-bed reactor: The feed inlet of the tubular fixed-bed reactor is connected to the discharge outlet of the gasification device. It is filled with a self-supporting structured metal catalyst. The self-supporting structured metal catalyst has an open-pore annular structure, which is selected from Raschig rings, Pall rings, θ rings or step rings. Heating and temperature control device: used for heating and temperature control of tubular fixed-bed reactors; Condensation recovery unit: The inlet of the condensation recovery unit is connected to the outlet of the tubular fixed-bed reactor; Gas-liquid separation device: The outlet of the condensation recovery device is connected to the inlet of the gas-liquid separation device to achieve the separation of condensate and non-condensable gas; Exhaust gas treatment device: The exhaust gas treatment device is used for the absorption and treatment of non-condensable gases.

[0022] Furthermore, the exhaust gas treatment device includes a connected exhaust gas buffer tank, an acid washing tower, and a blower.

[0023] The system of this invention can realize the continuous production of 1,1,3-trichloropropylene, and the by-product HCl can be recovered, which is environmentally friendly and economical.

[0024] Compared with the prior art, the beneficial effects of the present invention are as follows: (1) The present invention uses a self-supporting structured metal catalyst to catalyze the gas-phase cracking reaction of 1,1,1,3-tetrachloropropane in a tubular fixed-bed reactor of a specific alloy material. It has good catalytic effect, good catalyst stability, high catalytic efficiency, high gas flux, high specific surface area, and high reaction contact area, which helps to improve conversion rate and selectivity, improve heat transfer efficiency, and reduce side reactions (such as the formation of high-boiling substances). The self-supporting structured metal catalyst has a longer service life than the supported catalyst, and the active components will not be lost, nor will carbon buildup cause deactivation.

[0025] (2) The self-supporting structured metal catalyst has an open-pore ring structure with uniform pore size, which allows the reaction gas to flow in a directional manner along the channel, avoiding the "dead volume" and diffusion resistance caused by the accumulation of supported catalyst particles. It has high contact efficiency, no "dilution" effect of the carrier, high density of active sites per unit volume, stronger industrial adaptability, and small scale-up effect. It overcomes the problem that the reaction performance of supported catalysts will drop significantly during scale-up production due to uneven particle packing density and bed pressure drop fluctuations.

[0026] (3) Temperature is the core driving factor for the dehydrochlorination reaction. The self-supported structured metal catalyst has a high thermal conductivity (far superior to that of inert support), which can quickly and uniformly transfer the heat of reaction and avoid local overheating. It can achieve a high conversion rate at a relatively low temperature (280℃). In addition, 1,1,1,3-tetrachloropropane is completely vaporized in the preheater before entering the reactor, which avoids "liquid film encapsulation" when the liquid raw material comes into contact with the self-supported structured metal catalyst, ensuring the uniformity of the reaction. Furthermore, by controlling the space velocity and residence time, the reaction conditions can be optimized, the product yield and purity can be improved, energy consumption can be reduced, and local overheating and catalyst deactivation can be avoided. Attached Figure Description

[0027] Figure 1 This is a schematic diagram of a system for producing 1,1,3-trichloropropylene, where 1-feed pump, 2-vaporization device, 3-tubular fixed bed reactor, 4-condensation recovery device, 5-gas-liquid separation device, 6-tail gas buffer tank, 7-acid washing tower, and 8-blower.

[0028] Figure 2 This is an enlarged structural diagram of a θ-ringed metal catalyst. Detailed Implementation

[0029] To make the objectives, features, and advantages of this invention more apparent and understandable, a detailed description is provided below through specific embodiments. Many specific details are set forth in the following description to provide a thorough understanding of the invention. However, the invention can be practiced in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of the invention. Therefore, the invention is not limited to the specific embodiments disclosed below. Technical features in various embodiments of the invention can be combined appropriately without mutual conflict.

[0030] Unless otherwise specified, the operating methods in the following examples are generally performed under conventional conditions or as recommended by the manufacturer. Contents not described in detail in this specification are prior art known to those skilled in the art. Unless otherwise specified, the experimental materials used in the examples below can be purchased from conventional biochemical reagent companies.

[0031] like Figure 1 As shown, the system structure for producing 1,1,3-trichloropropylene includes: Vaporization device 2: used to preheat and vaporize the 1,1,1,3-tetrachloropropane pumped in by feed pump 1; Tubular fixed bed reactor 3: The feed inlet of the tubular fixed bed reactor 3 is connected to the discharge outlet of the vaporization device 2. It is filled with a self-supporting structured metal catalyst. The self-supporting structured metal catalyst has an open-pore annular structure. The open-pore annular structure is selected from Raschig rings, Pall rings or step rings. Heating and temperature control device: used for heating and temperature control of tubular fixed bed reactor 3; Condensation recovery device 4: The inlet of condensation recovery device 4 is connected to the outlet of tubular fixed bed reactor 3; Gas-liquid separation device 5: The outlet of the condensation recovery device 4 is connected to the inlet of the gas-liquid separation device 5 to achieve the separation of condensate and non-condensable gas. Exhaust gas treatment device: The exhaust gas treatment device is used for the absorption and treatment of non-condensable gases, including an interconnected exhaust gas buffer tank 6, an acid washing tower 7, and a blower 8.

[0032] In the embodiments, the self-supporting structured metal catalyst was customized by Tianjin Pusheng Technology Co., Ltd., and can be identified by the batch number "Wire Mesh θ Ring Packing\Ф3x3 / CS" (Examples 1-3). Its microstructure schematic diagram is shown below. Figure 2 As shown.

[0033] Example 1 250 g of 3 mm × 3 mm × 3 mm θ-ring pure iron catalyst was packed into an Inconel 600 alloy tubular fixed-bed reactor with an inner diameter of 25 mm (bulk density of 0.5 g / cm³). 3 After purging with nitrogen, the system was activated at 450°C for 3 hours by increasing the temperature at 3°C / min. The system temperature was then reduced to 350°C, while the system pressure was maintained at atmospheric pressure. 1,1,1,3-Tetrachloropropane was pumped into the vaporization unit at a rate of 78 g / h using a feed pump. After vaporization at 160°C, the vaporized material entered a tubular fixed-bed reactor, passing through the catalyst bed for dehydrochlorination. No carrier gas was introduced; the feed was continuous, and the space velocity was controlled at 26 min. -1 The reaction was carried out under a pressure of 100 kPa to 120 kPa with a residence time of 2.3 s. Liquid products were continuously collected at the outlet condenser, while non-condensable vapors were absorbed by a tail gas absorption tower to produce hydrochloric acid for other uses. After the reaction had been running stably for 20 min, samples were taken for analysis. Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 78.3%, the selectivity of 1,1,3-trichloropropene was 97.4%, and the yield reached 76.3%.

[0034] Example 2 In this embodiment, the preparation method of 1,1,3-trichloropropene is the same as that in Example 1, except that the reaction temperature is adjusted to 280°C.

[0035] Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 61.4%, the selectivity of 1,1,3-trichloropropene was 98.2%, and the yield reached 60.3%.

[0036] Example 3 In this embodiment, the preparation method of 1,1,3-trichloropropene is the same as that in Example 1, except that the reaction temperature is adjusted to 450°C.

[0037] Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 85.5%, the selectivity of 1,1,3-trichloropropene was 92.2%, and the yield reached 78.8%, with a slight increase in the content of high-boiling substances in the product.

[0038] Example 4 In this embodiment, the preparation method of 1,1,3-trichloropropylene is the same as that in Example 1, except that the self-supporting structured metal catalyst is a Pall ring of iron and zinc mixed metal (the mass ratio of iron to zinc is 1:0.2).

[0039] Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 71.4%, the selectivity of 1,1,3-trichloropropene was 96.1%, and the yield reached 68.56%, with a slight increase in the content of high-boiling substances in the product.

[0040] Example 5 In this embodiment, the preparation method of 1,1,3-trichloropropene is the same as that in Example 1, except that the self-supporting structured metal catalyst is a Raschig ring of iron and copper mixed metal (the mass ratio of iron to copper is 1:0.3).

[0041] Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 64.7%, the selectivity of 1,1,3-trichloropropene was 93.3%, and the yield reached 63.3%, with a slight increase in the content of high-boiling substances in the product.

[0042] Comparative Example 1 In this comparative example, the preparation method of 1,1,3-trichloropropene is the same as in Example 1, except that the catalyst is replaced with an equal volume (approximately 500 cm³). 3 Loose iron filings with a diameter of 3 mm.

[0043] Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 41.6%, the selectivity of 1,1,3-trichloropropene was 84.1%, and the yield was only 35.0%. This indicates that under the same conditions, the efficiency of conventional iron filings catalysts is much lower than that of the structured catalyst described in this invention.

[0044] Comparative Example 2 In this comparative example, the preparation method of 1,1,3-trichloropropene is the same as that in Example 1, except that the reaction temperature is 250°C.

[0045] Gas chromatography analysis showed that the conversion of 1,1,1,3-tetrachloropropane dropped sharply to 40.5%, the selectivity of 1,1,3-trichloropropene was 97.9%, and the yield was 39.6%. The reaction rate at this temperature was too slow and not economical.

[0046] Comparative Example 3 In this comparative example, the preparation method of 1,1,3-trichloropropene is the same as that in Example 1, except that the reaction temperature is 550°C.

[0047] Gas chromatography analysis showed that the conversion rate of 1,1,1,3-tetrachloropropane was 91.7%, but the selectivity of 1,1,3-trichloropropene dropped sharply to 65.4%, the yield was 60.0%, the product was dark black, and the pressure drop of the catalyst bed increased significantly, indicating that severe over-cracking and carbon deposition had occurred.

[0048] The embodiments described above provide a detailed explanation of the technical solutions of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, additions, or similar substitutions made within the scope of the principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis, characterized in that, Includes the following steps: 1,1,1,3-Tetrachloropropane is preheated to vaporization and then passed into a tubular fixed-bed reactor equipped with a catalyst bed to carry out a dehydrochlorination reaction to obtain 1,1,3-trichloropropene. The catalyst bed is formed by stacking self-supporting structured metal catalysts with a packing density of 0.35~2 g / cm³. 3 The self-supporting structured metal catalyst is made of one or a combination of iron, zinc, copper, cobalt, and nickel; the self-supporting structured metal catalyst has an open-pore ring structure, which is selected from Raschig rings, Pall rings, θ rings, or step rings. The tubular fixed-bed reactor is made of Inconel, Hastelloy, or stainless steel.

2. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, The preheating temperature of 1,1,1,3-tetrachloropropane is 80℃~200℃.

3. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, The parameters for the dehydrochlorination reaction include: space velocity 1–60 min. -1 The reaction pressure is 50 kPa to 300 kPa, the reaction temperature is 280℃ to 450℃, and the residence time is 1 to 30 seconds.

4. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, The parameters for the dehydrochlorination reaction include: space velocity 20–30 min. -1 The reaction pressure is 90 kPa to 120 kPa, the reaction temperature is 340℃ to 360℃, and the residence time is 1 to 10 seconds.

5. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, The self-supporting structured metal catalyst is made of a mixture of iron and zinc, or a mixture of iron and copper.

6. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 5, characterized in that, When the self-supporting structured metal catalyst is a mixture of iron and zinc, the mass ratio of iron to zinc is 1:0.05~0.3; when the self-supporting structured metal catalyst is a mixture of iron and copper, the mass ratio of iron to copper is 1:0.05~0.

3.

7. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, Pretreatment of self-supporting structured metal catalysts before use: The self-supporting structured metal catalyst is loaded into a tubular fixed-bed reactor and heated to 300-500℃ at a heating rate of 2-5℃ / min under an inert gas atmosphere, and held at that temperature for 2-4 hours.

8. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, After vaporized 1,1,1,3-tetrachloropropane is introduced into one end of a tubular fixed-bed reactor for dehydrochlorination, the reaction products are collected at the other end of the tubular fixed-bed reactor. The reaction products are condensed and separated into gas and liquid phases. The condensed products are then separated by distillation to obtain 1,1,3-trichloropropene.

9. The method for preparing 1,1,3-trichloropropene by gas-phase pyrolysis according to claim 1, characterized in that, The conversion rate of 1,1,1,3-tetrachloropropane was 60%–90%, and the selectivity of 1,1,3-trichloropropene was 90%–99%.

10. A system for producing 1,1,3-trichloropropene, characterized in that, The structure includes: Vaporization device: used to preheat 1,1,1,3-tetrachloropropane to vaporize it; Tubular fixed-bed reactor: The feed inlet of the tubular fixed-bed reactor is connected to the discharge outlet of the gasification device. It is filled with a self-supporting structured metal catalyst. The self-supporting structured metal catalyst has an open-pore annular structure, which is selected from Raschig rings, Pall rings, θ rings or step rings. Heating and temperature control device: used for heating and temperature control of tubular fixed-bed reactors; Condensation recovery unit: The inlet of the condensation recovery unit is connected to the outlet of the tubular fixed-bed reactor; Gas-liquid separation device: The outlet of the condensation recovery device is connected to the inlet of the gas-liquid separation device to achieve the separation of condensate and non-condensable gas; Exhaust gas treatment device: The exhaust gas treatment device is used for the absorption and treatment of non-condensable gases.

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