Gas-solid phase catalytic reactor

Abstract

The present invention relates to the technical field of gas-solid phase catalytic reaction equipment, and discloses a gas-solid phase catalytic reactor, comprising a reactor body and a plurality of catalyst beds arranged in an inner cavity of the reactor body, wherein the plurality of catalyst beds are arranged at intervals along the flow direction of the reaction raw materials, and a quenching filler layer is provided on the discharge side of each catalyst bed, and the quenching filler layer is arranged to quench the flame generated by the reaction raw materials; the present invention directly reduces the intensity of the gas-solid phase catalytic reaction by using the plurality of catalyst beds arranged at intervals, thereby avoiding the combustion and explosion of the combustible gas in the reaction raw materials caused by the release of excessive heat; the quenching filler layer is used to quench the flame that may be generated by the reaction raw materials, so that the combustible gas and oxygen can undergo a gas-solid phase catalytic reaction within the explosion limit, thereby improving the reaction rate, improving the reaction efficiency, and thus improving the economic benefit, and has the advantages of safety and reliability.

Description

Technical Field

[0001] The present invention relates to the technical field of gas-solid phase catalytic reaction equipment, in particular to a gas-solid phase catalytic reactor. Background Art

[0002] Gas-solid phase catalysis is an important type of chemical reaction process that is widely used in the oil refining, chemical, metallurgical and other industries, such as gas-phase alkylation, ammonia synthesis, benzene oxidation to produce anhydrides, and low-pressure methanol synthesis. Since the reaction raw materials are mostly flammable gases, when the reactants contain a certain concentration of oxygen, a flammable system is formed. In order to avoid the risk of combustion and explosion in the combustible gas / oxygen system, many reactions in the oxygen-containing phase can only be carried out outside the explosion limit of the combustible gas. The reactants need to be kept at a low concentration, which limits the reaction efficiency and economy, directly restricting its industrial application. For example, the reaction of directly combining hydrogen and oxygen to prepare hydrogen peroxide is an economical and green route, which has significant advantages over the existing anthraquinone method. However, due to the wide range of hydrogen's explosion limits, the process is prone to combustion and explosion, and the risk factor is high. For example, synthesizing hydrogen peroxide at concentrations below the lower explosion limit of hydrogen requires repeated separation and concentration steps, increasing production costs and making it economically unfeasible. Another example is the direct vapor-phase epoxidation of propylene, which reduces the two-step liquid-phase synthesis to a single step. This is more energy-efficient and environmentally friendly than existing technologies such as the HPPO method and the chlorohydrin method. However, it is also limited by the explosion risk of the reaction system and requires the introduction of a considerable amount of diluent gas. Another example is the selective catalytic oxidation of o-xylene to produce phthalic anhydride. If the oxygen concentration is too low, o-xylene undergoes incomplete oxidation to produce phthalide, benzoic acid, and citric anhydride. Raising the oxygen concentration will cause the reaction to proceed within the explosion limit, exposing the reactor to explosion risk. Therefore, how to reduce or even eliminate the explosion risk of gas-solid combustible systems while maintaining high reaction efficiency has become a pressing challenge for the chemical industry to improve quality and efficiency.

[0003] In recent years, researchers have attempted to prevent flame formation by adding ignition inhibitors (inert gas, water mist, kaolinite), improving piping materials to interrupt free radical chain propagation reactions, and controlling the reaction residence time to be less than the system's autoignition induction time. However, these methods either introduce new substances into the reaction system or place high demands on equipment materials and capabilities, making them unsuitable for universal application.

[0004] Specifically, the Chinese invention patent application with publication number "CN 104368100 A" discloses a combined wet and dry flame arrester for hydrogen and oxygen mixtures. Its key technical features include: a hydrogen and oxygen mixture outlet pipe is located at the top of the sub-flame arrester shell, an explosion-proof membrane and a pressure sensor connected to a control circuit are located at the bottom of the shell, and the mother shell is isolated by a stainless steel perforated flame arrester plate. From top to bottom, a flame arrester filler layer, a stainless steel capillary layer, and a water seal layer are arranged. A safety valve connection pipe is located at the top of the mother shell, and a hydrogen and oxygen mixture inlet and a liquid level sensor connected to the control circuit are located on the sidewalls of the water seal layer at the bottom of the shell. This device has a rational structural design and is safe and reliable in use. It not only has the sealing and backstopping functions of a dry flame arrester, but also utilizes a water seal and baffle to reduce flame temperature and pressure, effectively preventing the hazards caused by hydrogen and oxygen mixtures during backfire, flash explosion, and deflagration. However, this technology involves a flame arrester structure that cannot be installed in a reactor, and the water seal can cause the catalyst in the reactor to agglomerate or collapse, thereby losing its activity.

[0005] For example, the Chinese invention patent application with publication number "CN 103454308 A" discloses a test device for flame propagation and suppression during the explosion of premixed gas of combustible gas and air. The test device includes a combustion pipe, a fine water mist generating device, a metal mesh fire arrester, a high-speed camera, a schlieren system, a pressure testing system, an automatic gas distribution system, a temperature testing system, an ion probe detection system, a data acquisition instrument, a high-voltage ignition system and a synchronous controller. The device can be used to: (1) study the flame propagation characteristics and laws during the explosion of premixed gas under the influence of factors such as different combustible gas components, different opening states, different ignition positions, and different flame instabilities; (2) study the control and suppression effects of inhibitors, metal fire arrester mesh, fine water mist, etc. on flame propagation, and develop methods and technologies for suppressing premixed flame propagation under physical-chemical coupling. However, the patent only proposes a device for studying flame propagation, and does not elaborate on the filler structure and fire arrester type that suppress the fire arresting effect. In addition, fine water mist also has a great influence on the stability of the catalyst, and is not suitable for reactors for gas-solid phase catalytic reactions.

[0006] For example, the Chinese invention patent application with publication number "CN 107290388 A" discloses an experimental device for explosion suppression using ultrafine ABC dry powder. The device consists of an explosion pipe, a flange plate, a multi-stage chamber, an electric ignition head, a gas distribution device, an explosion suppression powder injection device, and a data acquisition device. This device studies the effect of varying the spatial position of the dry powder explosion suppression device on its suppression effectiveness under varying gas concentrations. However, this dry powder explosion suppression device cannot be applied to reactors for gas-solid catalytic reactions. Summary of the Invention

[0007] The purpose of the present invention is to overcome the defects of existing gas-solid phase catalytic reactors, which are limited by the explosion risk of the reaction system. Many oxygen-containing reactions can only be carried out outside the explosion limit of the combustible gas, resulting in low reactant concentration, limited reaction efficiency and economy. A gas-solid phase catalytic reactor is provided, through which the combustible gas and oxygen can safely undergo gas-solid phase catalytic reaction within the explosion limit range, effectively improving the selectivity and conversion rate of the oxidation process.

[0008] In order to achieve the above-mentioned objectives, the present invention provides a gas-solid phase catalytic reactor, comprising a reactor body and a plurality of catalyst beds arranged in the inner cavity of the reactor body, wherein the plurality of catalyst beds are arranged at intervals along the flow direction of the reaction raw materials, and a quenching filler layer is provided on the discharge side of each catalyst bed, wherein the quenching filler layer is configured to quench the flame generated by the reaction raw materials.

[0009] Optionally, the quenching packing layer includes a plurality of corrugated packing plates stacked in a direction parallel to the axial direction of the reactor body, and each of the corrugated packing plates is provided with a plurality of through holes for quenching the flame generated by the reaction raw materials.

[0010] Optionally, the gas-solid phase catalytic reactor satisfies the following relationship:

[0011]

[0012] Among them, d2 is the height of the quenching packing layer, M is the relative molecular mass of the combustible gas in the reaction raw material, d3 is the distance between adjacent corrugated packing plates, d1 is the height of the catalyst bed, δ is the thickness of the corrugated packing plate, and R is the inner diameter of the reactor body.

[0013] Optionally, the reactor body has a first feed inlet for combustible gas and a second feed inlet for oxygen, and the inner cavity of the reactor body is provided with the quenching filler layer located between the first feed inlet and the second feed inlet.

[0014] Optionally, an outlet for the reaction product to flow out is provided at one end of the reactor body away from the first feed inlet and the second feed inlet.

[0015] Optionally, a gas distributor connected to the first feed port and / or the second feed port is provided in the inner cavity of the reactor body, and the gas distributor is used to distribute the reaction raw materials entering the inner cavity of the reactor body through the first feed port and / or the second feed port.

[0016] Optionally, the gas distributor includes a spiral pipe and a plurality of gas outlet holes arranged on the spiral pipe, the openings of the gas outlet holes are facing one side of the spiral pipe, and the apertures of the gas outlet holes increase successively along the flow direction of the reaction raw materials in the spiral pipe.

[0017] Optionally, the quenching filler layer is arranged to be spaced apart from the adjacent catalyst bed layer.

[0018] Optionally, a fire-retardant and explosion-proof filler is provided in the inner cavity of the reactor body, and the fire-retardant and explosion-proof filler is provided at the feed end of the catalyst bed close to the feed side of the reactor body.

[0019] Optionally, the fire-retardant and explosion-proof filler is a porous spherical non-metallic organic material.

[0020] Optionally, each of the catalyst beds includes two baffles installed in the inner cavity of the reactor body, the two baffles are spaced apart along the flow direction of the reaction raw materials, and a plurality of reaction tubes for loading catalysts are provided between the two baffles. The tube lumens of the plurality of reaction tubes form a tube-side space for the reaction raw materials to flow from one side of the catalyst bed to the other side; a shell-side space is formed between the outer walls of the plurality of reaction tubes and the two baffles, and the reactor body is provided with a liquid inlet pipeline and a liquid outlet pipeline connected to the shell-side space, the liquid inlet pipeline is used to introduce heat exchange medium into the shell-side space, and the heat exchange medium can be discharged through the liquid outlet pipeline.

[0021] Optionally, the distance between the quenching packing layer and the adjacent catalyst bed layer satisfies the following relationship:

[0022]

[0023] Wherein, h is the distance between the quenching packing layer and the adjacent catalyst bed layer, v is the flow rate of the material in the reaction tube, d is the inner diameter of the reaction tube, M is the relative molecular mass of the combustible gas in the reaction raw material, D is the total area of ​​the reaction tube filled with a single layer of catalyst, and T is the material temperature in the reactor body.

[0024] Optionally, the liquid inlet pipeline is used to pass cooling water into the shell-side space, and the liquid outlet pipeline is used to pass the heated cooling water into the steam generator to generate steam.

[0025] Optionally, the liquid inlet pipeline includes a liquid inlet main pipe and a plurality of liquid inlet branches respectively connected to the liquid inlet main pipe, and the plurality of liquid inlet branches correspond one-to-one to the plurality of catalyst beds for introducing cooling water into the shell-side space of the corresponding catalyst beds; the liquid inlet main pipe is provided with a regulating valve and a control device for controlling the opening of the regulating valve, and the steam generator is provided with a liquid level gauge, and the liquid level gauge is electrically connected to the control device so that the control device can control the opening of the regulating valve according to the liquid level height signal of the steam generator monitored by the liquid level gauge.

[0026] Compared with the prior art, the present invention directly reduces the intensity of the gas-solid phase catalytic reaction in the catalyst bed by dividing the catalyst bed in the reactor body into multiple layers and arranging them at intervals along the flow direction of the reaction raw materials, thereby avoiding the release of excessive heat that causes the combustible gas in the reaction raw materials to explode.

[0027] By arranging a quenching filler layer on the discharge side of each catalyst bed, the flame generated by the reaction raw materials is quenched by the quenching filler layer, so that the combustible gas and oxygen can undergo a gas-solid phase catalytic reaction within the explosion limit, thereby improving the reaction rate. Compared with traditional gas-solid phase catalytic reactors that can only react outside the explosion limit, the gas-solid phase catalytic reactor provided by the present invention significantly improves the conversion rate of the reaction raw materials, thereby improving the economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 This is a schematic structural diagram of a gas-solid phase catalytic reactor provided by the present invention;

[0029] Figure 2 This is a schematic structural diagram of a reactor body provided by the present invention;

[0030] Figure 3 This is a structural schematic diagram of a gas distributor provided by the present invention;

[0031] Figure 4 It is a top view schematic diagram of a quenching filler layer provided by the present invention.

[0032] Description of Reference Numerals

[0033] 10. Reactor body; 11. First feed port; 111. First pipeline; 12. Second feed port; 121. Second pipeline; 13. Discharge port; 131. Discharge pipeline; 14. Liquid inlet pipeline; 141. Liquid inlet main pipe; 142. Liquid inlet branch pipe; 143. Regulating valve; 15. Liquid outlet pipeline; 20. Catalyst bed; 201. Tube-side space; 202. Shell-side space; 21. Baffle; 22. Reaction tube; 30. Quenching packing layer; 31. Corrugated packing plate; 32. Packing ring; 40. Gas distributor; 41. Spiral pipe; 42. Air outlet; 50. Fire-proof and explosion-proof packing; 60. Steam generator; 61. Liquid level gauge; 62. Steam pipeline; 621. Pressure regulating valve; 63. Pressure gauge; 64. Thermometer; 70. Spark plug. DETAILED DESCRIPTION

[0034] The following describes the specific embodiments of the present invention in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention and are not intended to limit the present invention.

[0035] In order to avoid the explosion risk of combustible gas / oxygen systems, existing gas-solid catalytic reactions in oxygen-containing phases can only be carried out outside the explosion limit of the combustible gas. The reactants need to be maintained at a low concentration, resulting in limited reaction efficiency and economy, which directly restricts the industrial application of gas-solid catalytic reactions.

[0036] To this end, the present invention provides a gas-solid phase catalytic reactor, which includes a reactor body 10 and a plurality of catalyst beds 20 arranged in the inner cavity of the reactor body 10. The plurality of catalyst beds 20 are arranged at intervals along the flow direction of the reaction raw materials. A quenching filler layer 30 is provided on the discharge side of each catalyst bed 20. The quenching filler layer 30 is configured to quench the flame generated by the reaction raw materials.

[0037] In the present invention, by dividing the catalyst bed 20 in the reactor body 10 into multiple layers and arranging them at intervals along the flow direction of the reaction raw materials, the intensity of the gas-solid phase catalytic reaction in the catalyst bed 20 is directly reduced, thereby avoiding the release of excessive heat that causes the combustible gas in the reaction raw materials to explode; further, a quenching filler layer 30 is set on the discharge side of each catalyst bed 20, and the quenching filler layer 30 is used to quench the flame generated by the reaction raw materials, so that the combustible gas and oxygen can undergo a gas-solid phase catalytic reaction within the explosion limit, thereby improving the reaction rate. Compared with traditional gas-solid phase catalytic reactors that can only react outside the explosion limit, the gas-solid phase catalytic reactor provided by the present invention significantly improves the conversion rate of the reaction raw materials, thereby improving the economic benefits.

[0038] In the present invention, the function of the quenching filler layer 30 is to prevent the flame from continuing to propagate in the catalyst bed 20. Even if the combustible gas and oxygen explode within the explosion limit, the quenching filler layer 30 can still quench the flame, thereby allowing the reaction raw materials to undergo gas-solid phase catalytic reaction under high concentration conditions, breaking through the bottleneck of low reaction efficiency and inability to achieve large-scale production of existing green process routes, and providing an inherently safe solution for gas-solid phase catalytic reaction processes with higher explosion risks.

[0039] As a specific embodiment of quenching the flame and preventing the flame from spreading, the quenching filler layer 30 is combined with Figure 4 As shown, the quenching packing layer 30 comprises a plurality of corrugated packing plates 31 stacked parallel to the axial direction of the reactor body 10. Each corrugated packing plate 31 has a plurality of through-holes formed therein for quenching the flame generated by the reaction materials. It will be appreciated that the quenching packing layer 30 also includes a packing ring 32 for securing the stacked corrugated packing plates 31, thereby forming a quenching packing layer 30 of a certain height.

[0040] In this embodiment, the through-holes provided in the corrugated packing sheet 31 can redirect the airflow, preventing the flame from propagating and quenching the flame. The through-holes can be of various shapes, such as circular, triangular, square, or rectangular, with rectangular holes being preferred. The multiple through-holes can be of the same shape or of different shapes.

[0041] The material of the corrugated packing plate 31 needs to be specifically selected according to the reaction raw materials of the gas-solid phase catalytic reactor. For example, when the reaction raw materials contain acidic gas, it is necessary to select a material resistant to acid corrosion, such as aluminosilicate acid-resistant and chemical-resistant ceramic material.

[0042] In the present invention, by alternately installing multiple catalyst beds 20 and multiple quenching filler layers 30 in the inner cavity of the reactor body 10, the heat generated by the gas-solid phase catalytic reaction can be reduced, and the flame generated by the reaction raw materials can be quenched, so that the catalytic oxidation reaction of oxygen and combustible gas can operate within the explosion limit, thereby increasing its oxidation efficiency.

[0043] In the present application, the inventors discovered the structure-activity relationship between the height of the quenching packing layer 30, the spacing between adjacent corrugated packing plates 31 in the quenching packing layer 30 and the height of the catalyst bed 20, and the inner diameter of the reactor body 10 based on the quenching distance between the combustible gas flames of different components at different concentrations and the catalyst bed 20, thereby designing the matching form between different quenching packing layers 30 and the catalyst bed 20 height, so that the gas-solid phase catalytic reactor can ensure that the catalytic oxidation reaction of the combustible gas and oxygen operates within its explosion limit, thereby improving the selectivity and conversion rate of the oxidation process.

[0044] Specifically, the gas-solid phase catalytic reactor satisfies the following relationship:

[0045]

[0046] Among them, d2 is the height of the quenching packing layer 30, M is the relative molecular mass of the combustible gas in the reaction raw material, d3 is the distance between adjacent corrugated packing plates 31, d1 is the height of the catalyst bed 20, δ is the thickness of the corrugated packing plate 31, and R is the inner diameter of the reactor body 10.

[0047] In the present invention, the reactor body 10 has a first feed port 11 for the inlet of combustible gas and a second feed port 12 for the inlet of oxygen. The inner cavity of the reactor body 10 is provided with the quenching packing layer 30 located between the first feed port 11 and the second feed port 12. The quenching packing layer 30 is provided between the first feed port 11 and the second feed port 12 to prevent the flame from spreading to the feed side, thereby ensuring safety.

[0048] Specifically, combined Figure 1 As shown, the first feed port 11 is connected to a first pipeline 111 for transporting combustible gas into the inner cavity of the reactor body 10 , and the second feed port 12 is connected to a second pipeline 121 for transporting oxygen into the inner cavity of the reactor body 10 .

[0049] Furthermore, in the present invention, a discharge port 13 for the reaction product to flow out is provided at one end of the reactor body 10 away from the first feed port 11 and the second feed port 12. It is understood that a discharge pipeline 131 is connected to the discharge port 13 for outputting the reaction product to the outside.

[0050] In some embodiments, a gas distributor 40 connected to the first feed port 11 and / or the second feed port 12 is provided in the inner cavity of the reactor body 10. The gas distributor 40 is used to distribute the reaction raw materials entering the inner cavity of the reactor body 10 through the first feed port 11 and / or the second feed port 12. The gas distributor 40 allows the reaction raw materials to be fully mixed before entering the catalyst bed 20, ensuring efficient catalytic oxidation reaction and avoiding local overheating of the catalyst bed 20 caused by uneven mixing of the reaction raw materials.

[0051] The specific positions of the first feed port 11 and the second feed port 12 on the reactor body 10 are selected according to specific circumstances. For example, the first feed port 11 and the second feed port 12 are both arranged at the bottom side of the reactor body 10 and at different heights, so as to be used for respectively inputting reaction raw materials into the inner cavity of the reactor body 10. In some embodiments, in combination with Figure 1 As shown, the first feed port 11 is arranged at the bottom center position of the reactor body 10, and the second feed port 12 is arranged at the bottom side of the reactor body 10. Based on the fact that the quenching filler layer 30 arranged between the first feed port 11 and the second feed port 12 has a certain gas dispersion effect, it is only necessary to set a gas distributor 40 connected to the second feed port 12 in the inner cavity of the reactor body 10. In this way, the reaction raw materials can be fully mixed before entering the catalyst bed 20 with a lower equipment investment.

[0052] In the present invention, the function of the gas distributor 40 is to make the reaction raw materials entering the inner cavity of the reactor body 10 through the first feed port 11 or the second feed port 12 evenly distributed in its radial direction, so that they can evenly enter the catalyst bed 20 at different positions to carry out gas-solid phase catalytic reaction.

[0053] The gas distributor 40 can be any commonly used one in the art, as long as it can evenly distribute the reaction materials in the radial direction of the inner cavity of the reactor body 10. Figure 3 As shown, the gas distributor 40 includes a spiral pipe 41 and a plurality of gas outlet holes 42 disposed on the spiral pipe 41. The openings of the gas outlet holes 42 face one side of the spiral pipe 41, and the apertures of the gas outlet holes 42 increase in size along the flow direction of the reaction material within the spiral pipe 41. By designing the apertures of the plurality of gas outlet holes 42 in the direction of the reaction material flow, the reaction material is uniformly distributed in the radial direction of the inner cavity of the reactor body 10.

[0054] In some embodiments, the quenching filler layer 30 is spaced apart from the adjacent catalyst bed 20. Figure 2 As shown, a plurality of catalyst beds 20 arranged at intervals are provided in the inner cavity of the reactor body 10. After the reaction raw materials pass through a layer of catalyst bed 20 and react under the catalytic action of the catalyst, the reaction raw materials are still uneven in the radial direction of the reactor body 10. By setting a spacing between the quenching filler layer 30 and the adjacent catalyst bed 20, the reaction raw materials are further mixed in the spacing, which makes the reaction raw materials tend to be uniform when entering the next catalyst bed 20, thereby improving the uniformity of the gas-solid phase catalytic reaction.

[0055] In some embodiments, a fire-retardant and explosion-proof filler 50 is provided in the inner cavity of the reactor body 10 , and the fire-retardant and explosion-proof filler 50 is provided at the feed end of the catalyst bed 20 close to the feed side of the reactor body 10 .

[0056] It can be understood that the flame-retardant and explosion-proof filler 50 can not only play a role in fire retardancy, but also promote the reaction raw materials entering the first catalyst bed 20 to be distributed more evenly in the radial direction of the reactor body 10, thereby improving the uniformity of the gas-solid phase catalytic reaction, avoiding the generation of local hot spots in the catalyst bed 20, and reducing the risk of combustion and explosion.

[0057] In some embodiments, the fire-retardant and explosion-proof filler 50 is a porous spherical non-metallic organic material.

[0058] In some embodiments, each of the catalyst beds 20 includes two baffles 21 installed in the inner cavity of the reactor body 10, and the two baffles 21 are spaced apart along the flow direction of the reaction raw materials. A plurality of reaction tubes 22 for loading catalysts are provided between the two baffles 21, and the tube lumens of the plurality of reaction tubes 22 form a tube-side space 201 for the reaction raw materials to flow from one side of the catalyst bed 20 to the other side; a shell-side space 202 is formed between the outer walls of the plurality of reaction tubes 22 and the two baffles 21, and the reactor body 10 is provided with a liquid inlet pipeline 14 and a liquid outlet pipeline 15 connected to the shell-side space 202, and the liquid inlet pipeline 14 is used to pass heat exchange medium into the shell-side space 202, and the heat exchange medium can be discharged through the liquid outlet pipeline 15.

[0059] In the technical solution provided by the present invention, not only is the catalyst bed 20 within the reactor body 10 divided into multiple layers and spaced apart along the flow direction of the reaction raw materials, but a component capable of heat removal is also provided for each catalyst bed 20. During specific use, a heat exchange medium is introduced into the shell-side space 202 of the catalyst bed 20 through the liquid inlet pipeline 14 to rapidly remove the heat generated by the gas-solid phase catalytic reaction in the reaction tube 22, thereby preventing the catalyst bed 20 from overheating and damaging the catalyst. At the same time, the temperature is lowered to below the autoignition point of the system, significantly reducing the risk of combustion and explosion of the combustible gas / oxygen system. This allows the gas-solid phase catalytic reactor to ensure that the catalytic oxidation reaction of the combustible gas and oxygen operates within its explosion limit, effectively improving the selectivity and conversion rate of the oxidation process.

[0060] It is understandable that in the present invention, by forming a flowing heat exchange medium in the shell space 202 of each catalyst bed 20, the heat of the gas-solid phase catalytic reaction is continuously removed, which can effectively reduce the explosion risk of the combustible gas / oxygen system.

[0061] The inventors of this application have discovered that by ensuring that the spacing between the quenching packing layer 30 and the adjacent catalyst bed 20 satisfies the following relationship, the reaction materials can be better mixed before entering the next catalyst bed 20 while avoiding the problem of increased equipment investment due to excessive spacing between the two. The relationship is:

[0062]

[0063] Among them, h is the distance between the quenching packing layer 30 and the adjacent catalyst bed 20, v is the flow rate of the material in the reaction tube 22, d is the inner diameter of the reaction tube 22, M is the relative molecular mass of the combustible gas in the reaction raw material, D is the total area of ​​the reaction tube 22 filled with a single layer of catalyst, and T is the material temperature in the reactor body 10.

[0064] In some embodiments, the liquid inlet line 14 is used to introduce cooling water into the shell-side space 202, and the liquid outlet line 15 is used to introduce the heated cooling water into the steam generator 60 to generate steam. By providing the steam generator 60, the heat from the gas-solid phase catalytic reaction is recovered and utilized, thereby reducing overall energy consumption.

[0065] In some embodiments, the liquid inlet pipeline 14 includes a liquid inlet main pipe 141 and a plurality of liquid inlet branches 142 respectively connected to the liquid inlet main pipe 141, and the plurality of liquid inlet branches 142 correspond one-to-one to the plurality of catalyst beds 20 for introducing cooling water into the shell space 202 of the corresponding catalyst bed 20; the liquid inlet main pipe 141 is provided with a regulating valve 143 and a control device for controlling the opening of the regulating valve 143, and the steam generator 60 is provided with a liquid level gauge 61, and the liquid level gauge 61 is electrically connected to the control device so that the control device can control the opening of the regulating valve 143 according to the liquid level height signal of the steam generator 60 monitored by the liquid level gauge 61.

[0066] It is understandable that the steam generator 60 is also connected to a steam pipeline 62 for delivering the generated steam to the steam network.

[0067] Furthermore, a pressure regulating valve 621 is provided on the steam pipeline 62, and a pressure gauge 63 is provided on the steam generator 60. The pressure regulating valve 621 and the pressure gauge 63 are both electrically connected to the DCS control device to form interlock control. The DCS control device is configured to control the opening of the pressure regulating valve 621 based on the pressure signal of the steam generator 60 monitored by the pressure gauge 63. During specific use, the pressure in the steam generator 60 is monitored in real time by the pressure gauge 63, and the opening of the pressure regulating valve 621 is adjusted and controlled by feedback, so that the steam generated in the steam generator 60 is discharged in time, thereby ensuring the safe operation of the steam generator 60.

[0068] The steam generator 60 is further provided with a thermometer 64 for detecting the real-time temperature inside the steam generator 60 .

[0069] Experimental group 1

[0070] based on Figure 1 The provided gas-solid phase catalytic reactor was tested: a certain flow rate of methane was introduced into the reactor body 10 from the bottom through the first pipeline 111, and the feed temperature was 25°C; a certain flow rate of oxygen was introduced into the gas distributor 40 through the second pipeline 121, and the oxygen distributed by the gas distributor 40 and the methane dispersed through the quenching filler layer 30 were further mixed through the flame-retardant and explosion-proof filler 50, and then entered the catalyst bed 20 (the catalyst filled in the catalyst bed 20 was honeycomb Al2O3, and the active component was the precious metal Pd / Au), and finally passed through the discharge pipeline 131 set at the top of the reactor body 10. The catalyst bed 20 is ignited by the spark plug 70. When the height d1 of the catalyst bed 20 is 0.5 m, the inner diameter R of the reactor body 10 is 0.5 m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1 mm, a corrugated packing plate 31 with a thickness δ of 0.3 mm is used. When the height d2 of the quenching packing layer 30 is 0.028 m, the flame can be quenched, and the discharge pipeline 131 contains a small amount of CO2 (about 5%), but most of it is methane and oxygen.

[0071] According to the above steps, the height d1 of the catalyst bed 20 is adjusted to 0.8m, the inner diameter R of the reactor body 10 is 0.6m, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, and the corrugated packing plates 31 with a thickness δ of 0.4mm are used. When the height d2 of the quenching packing layer 30 is 0.034m, the flame can be quenched.

[0072] Similarly, according to the above steps, the height d1 of the catalyst bed 20, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30, and the thickness δ of the corrugated packing plates 31 were adjusted respectively, and an orthogonal test was performed. The test data are shown in Table 1 below.

[0073] Table 1:

[0074]

[0075] Through fitting, the relationship between various parameters is obtained as follows:

[0076]

[0077] Wherein, d2 is the height of the quenching packing layer 30 , d3 is the distance between adjacent corrugated packing plates 31 , d1 is the height of the catalyst bed 20 , δ is the thickness of the corrugated packing plate 31 , and R is the inner diameter of the reactor body 10 .

[0078] Further, based on Figure 1 The provided gas-solid phase catalytic reactor was tested: a certain flow rate of methane was introduced into the reactor body 10 from the bottom through the first pipeline 111, and the feed temperature was 25°C; a certain flow rate of oxygen was introduced into the gas distributor 40 through the second pipeline 121, and the oxygen distributed by the gas distributor 40 and the methane dispersed by the quenching filler layer 30 were further mixed by the flame-retardant and explosion-proof filler 50, and then entered the catalyst bed 20 (the catalyst filled in the catalyst bed 20 was honeycomb Al2O3, and the active component was precious metal Pd / Au), and finally flowed out through the discharge pipeline 131 arranged at the top of the reactor body 10. After the flow rate stabilized, the molar ratio of methane to oxygen in the discharge pipeline 131 was detected to be 1:2; the flow velocity v of the material in the reaction tube 22 loaded with the catalyst was 8 m / s, the diameter d of the reaction tube 22 loaded with the catalyst was 10 mm, and the total area D of the reaction tube 22 loaded with a single layer of catalyst was 0.15 m 2 When the material temperature T in the reactor is 500K and the distance h between the quenching packing layer 30 and the adjacent catalyst bed 20 is 0.046m, the oxygen content and methane content in the reactor discharge pipeline 131 are the lowest, that is, methane and oxygen are fully reacted.

[0079] According to the above steps, the material flow rate v in the reaction tube 22 is adjusted to 9 m / s, the diameter d of the reaction tube 22 filled with catalyst is 10 mm, and the total area D of the reaction tube 22 filled with a single layer of catalyst is 0.15 m 2 When the material temperature T in the reactor is 500K and the distance h between the quenching packing layer 30 and the adjacent catalyst bed 20 is 0.052m, the oxygen content and methane content in the reactor discharge pipeline 131 are the lowest.

[0080] Similarly, according to the above steps, the material flow rate v in the reaction tube 22, the diameter d of the reaction tube 22 filled with catalyst, and the total area D of the reaction tube 22 filled with a single layer of catalyst are adjusted respectively. The experimental data are shown in Table 2 below.

[0081] Table 2:

[0082]

[0083]

[0084] Through fitting, the relationship between various parameters is obtained as follows:

[0085]

[0086] Among them, h is the distance between the quenching packing layer 30 and the adjacent catalyst bed 20, v is the flow rate of the material in the reaction tube 22, d is the inner diameter of the reaction tube 22, M is the relative molecular mass of the combustible gas in the reaction raw material, D is the total area of ​​the reaction tube 22 filled with a single layer of catalyst, and T is the material temperature in the reactor body 10.

[0087] Experimental Group 2

[0088] based on Figure 1 The gas-solid phase catalytic reactor provided was tested: a certain flow rate of ethane was introduced into the reactor body 10 from the bottom through the first pipeline 111, and the feed temperature was 25°C; a certain flow rate of oxygen was introduced into the gas distributor 40 through the second pipeline 121, and the oxygen distributed by the gas distributor 40 and the ethane dispersed through the quenching filler layer 30 were further mixed through the flame-retardant and explosion-proof filler 50, and then entered the catalyst bed 20 (the catalyst filled in the catalyst bed 20 was honeycomb Al2O3, and the active component was the precious metal Pd / Au), and finally flowed through the discharge pipeline 131 set at the top of the reactor body 10. After the flow rate stabilizes, the molar ratio of ethane to oxygen in the discharge pipeline 131 is detected to be 1:3.5; the catalyst bed 20 is ignited by the spark plug 70. When the height d1 of the catalyst bed 20 is 0.5 m, the inner diameter R of the reactor body 10 is 0.5 m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1 mm, a corrugated packing plate 31 with a thickness δ of 0.3 mm is used. When the height d2 of the quenching packing layer 30 is 0.052 m, the flame can be quenched, and the discharge pipeline 131 contains a small amount of CO2 (about 5%), but most of it is ethane and oxygen.

[0089] According to the above steps, the height d1 of the catalyst bed 20 is adjusted to 0.8m, the inner diameter R of the reactor body 10 is 0.6m, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, and the corrugated packing plates 31 with a thickness δ of 0.4mm are used. When the height d2 of the quenching packing layer 30 is 0.064m, the flame can be quenched.

[0090] Similarly, according to the above steps, the height d1 of the catalyst bed 20, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30, and the thickness δ of the corrugated packing plates 31 were adjusted respectively, and an orthogonal test was performed. The test data are shown in Table 3 below.

[0091] Table 3:

[0092]

[0093] Through fitting, the relationship between various parameters is obtained as follows:

[0094]

[0095] Wherein, d2 is the height of the quenching packing layer 30 , d3 is the distance between adjacent corrugated packing plates 31 , d1 is the height of the catalyst bed 20 , δ is the thickness of the corrugated packing plate 31 , and R is the inner diameter of the reactor body 10 .

[0096] Further, based on Figure 1 The provided gas-solid phase catalytic reactor was tested: a certain flow rate of ethane was introduced into the reactor body 10 from the bottom through the first pipeline 111, and the feed temperature was 25°C; a certain flow rate of oxygen was introduced into the gas distributor 40 through the second pipeline 121, and the oxygen distributed by the gas distributor 40 and the ethane dispersed by the quenching filler layer 30 were further mixed through the flame-retardant and explosion-proof filler 50, and then entered the catalyst bed 20 (the catalyst filled in the catalyst bed 20 was honeycomb Al2O3, and the active component was precious metal Pd / Au), and finally flowed out through the discharge pipeline 131 arranged at the top of the reactor body 10. After the flow rate stabilized, the molar ratio of ethane to oxygen in the discharge pipeline 131 was detected to be 1:3.5; the flow velocity v of the material in the reaction tube 22 loaded with the catalyst was 8 m / s, the diameter d of the reaction tube 22 loaded with the catalyst was 10 mm, and the total area D of the reaction tube 22 loaded with a single layer of catalyst was 0.15 m 2 When the material temperature T in the reactor is 500K and the distance h between the quenching packing layer 30 and the adjacent catalyst bed 20 is 0.086m, the oxygen content and ethane content in the reactor discharge pipeline 131 are the lowest.

[0097] According to the above steps, the material flow rate v in the reaction tube 22 is adjusted to 9 m / s, the diameter d of the reaction tube 22 filled with catalyst is 10 mm, and the total area D of the reaction tube 22 filled with a single layer of catalyst is 0.15 m 2 When the material temperature T in the reactor is 500K and the distance h between the quenching packing layer 30 and the adjacent catalyst bed 20 is 0.097m, the oxygen content and ethane content in the reactor discharge pipeline 131 are the lowest.

[0098] Similarly, according to the above steps, the material flow rate v in the reaction tube 22, the diameter d of the reaction tube 22 filled with catalyst, and the total area D of the reaction tube 22 filled with a single layer of catalyst are adjusted respectively. The experimental data are shown in Table 4 below.

[0099] Table 4:

[0100]

[0101]

[0102] The relationship between various parameters is obtained as follows:

[0103]

[0104] Among them, h is the distance between the quenching packing layer 30 and the adjacent catalyst bed 20, v is the flow rate of the material in the reaction tube 22, d is the inner diameter of the reaction tube 22, M is the relative molecular mass of the combustible gas in the reaction raw material, D is the total area of ​​the reaction tube 22 filled with a single layer of catalyst, and T is the material temperature in the reactor body 10.

[0105] Experimental Group 3

[0106] based on Figure 1The provided gas-solid phase catalytic reactor was tested: a certain flow rate of propane was introduced into the reactor body 10 from the bottom through the first pipeline 111, and the feed temperature was 25°C; a certain flow rate of oxygen was introduced into the gas distributor 40 through the second pipeline 121, and the oxygen distributed by the gas distributor 40 and the propane dispersed through the quenching filler layer 30 were further mixed through the flame-retardant and explosion-proof filler 50, and then entered the catalyst bed 20 (the catalyst filled in the catalyst bed 20 was honeycomb Al2O3, and the active component was the precious metal Pd / Au), and finally passed through the discharge pipeline 131 set at the top of the reactor body 10. The catalyst bed 20 is ignited by the spark plug 70. When the height d1 of the catalyst bed 20 is 0.5 m, the inner diameter R of the reactor body 10 is 0.5 m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1 mm, a corrugated packing plate 31 with a thickness δ of 0.3 mm is used. When the height d2 of the quenching packing layer 30 is 0.076 m, the flame can be quenched, and the discharge pipeline 131 contains a small amount of CO2 (about 5%), but most of it is propane and oxygen.

[0107] According to the above steps, the height d1 of the catalyst bed 20 is adjusted to 0.8m, the inner diameter R of the reactor body 10 is 0.6m, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, and the corrugated packing plates 31 with a thickness δ of 0.4mm are used. When the height d2 of the quenching packing layer 30 is 0.094m, the flame can be quenched.

[0108] Similarly, according to the above steps, the height d1 of the catalyst bed 20, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30, and the thickness δ of the corrugated packing plates 31 were adjusted respectively, and an orthogonal test was performed. The test data are shown in Table 5 below.

[0109] Table 5:

[0110]

[0111] Through fitting, the relationship between various parameters is obtained as follows:

[0112]

[0113] Wherein, d2 is the height of the quenching packing layer 30 , d3 is the distance between adjacent corrugated packing plates 31 , d1 is the height of the catalyst bed 20 , δ is the thickness of the corrugated packing plate 31 , and R is the inner diameter of the reactor body 10 .

[0114] Further, based on Figure 1The provided gas-solid phase catalytic reactor was tested: a certain flow rate of propane was introduced into the reactor body 10 from the bottom through the first pipeline 111, and the feed temperature was 25°C; a certain flow rate of oxygen was introduced into the gas distributor 40 through the second pipeline 121, and the oxygen distributed by the gas distributor 40 and the propane dispersed by the quenching filler layer 30 were further mixed by the flame-retardant and explosion-proof filler 50, and then entered the catalyst bed 20 (the catalyst filled in the catalyst bed 20 was honeycomb Al2O3, and the active component was precious metal Pd / Au), and finally flowed out through the discharge pipeline 131 arranged at the top of the reactor body 10. After the flow rate stabilized, the molar ratio of propane to oxygen in the discharge pipeline 131 was detected to be 1:5; the flow velocity v of the material in the reaction tube 22 loaded with the catalyst was 8 m / s, the diameter d of the reaction tube 22 loaded with the catalyst was 10 mm, and the total area D of the reaction tube 22 loaded with a single layer of catalyst was 0.15 m 2 When the material temperature T in the reactor is 500K and the distance h between the quenching packing layer 30 and the adjacent catalyst bed 20 is 0.126m, the oxygen content and propane content in the reactor discharge pipeline 131 are the lowest.

[0115] According to the above steps, the material flow rate v in the reaction tube 22 is adjusted to 9 m / s, the diameter d of the reaction tube 22 filled with catalyst is 10 mm, and the total area D of the reaction tube 22 filled with a single layer of catalyst is 0.15 m 2 When the material temperature T in the reactor is 500K and the distance h between the quenching packing layer 30 and the adjacent catalyst bed 20 is 0.142m, the oxygen content and propane content in the reactor discharge pipeline 131 are the lowest.

[0116] Similarly, according to the above steps, the material flow rate v in the reaction tube 22, the diameter d of the reaction tube 22 filled with catalyst, and the total area D of the reaction tube 22 filled with a single layer of catalyst are adjusted respectively. The experimental data are shown in Table 6 below.

[0117] Table 6:

[0118]

[0119]

[0120] The relationship between various parameters is obtained as follows:

[0121]

[0122] Among them, h is the distance between the quenching packing layer 30 and the adjacent catalyst bed 20, v is the flow rate of the material in the reaction tube 22, d is the inner diameter of the reaction tube 22, M is the relative molecular mass of the combustible gas in the reaction raw material, D is the total area of ​​the reaction tube 22 filled with a single layer of catalyst, and T is the material temperature in the reactor body 10.

[0123] Based on experimental data on the height of the catalyst bed 20 of methane, ethane, and propane in the reactor body 10, the spacing between adjacent corrugated packing plates 31 in the quenching packing layer 30, the thickness of the corrugated packing plates 31, the inner diameter of the reactor body 10, and the height of the quenching packing layer 30, and after introducing the relative molecular mass of the combustible gas, the following relationship is obtained:

[0124]

[0125] Among them, d2 is the height of the quenching packing layer 30, M is the relative molecular mass of the combustible gas in the reaction raw material, d3 is the distance between adjacent corrugated packing plates 31, d1 is the height of the catalyst bed 20, δ is the thickness of the corrugated packing plate 31, and R is the inner diameter of the reactor body 10.

[0126] That is to say, the gas-solid phase catalytic reactor provided by the present invention can ensure that the flame generated by the reaction raw materials is quenched when the above-mentioned relationship is met, so that the catalytic oxidation reaction of the combustible gas and oxygen operates within its explosion limit, increases its oxidation efficiency, and improves the selectivity and conversion rate of the oxidation process.

[0127] The advantages of the gas-solid phase catalytic reactor provided by the present invention are further illustrated below with reference to specific examples.

[0128] Taking the catalytic oxidation of ethylene to produce ethylene oxide as an example for comparison, when the catalyst bed 20 height d1 is 0.5 m, the inner diameter R of the reactor body 10 is 0.5 m, the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1 mm, and the corrugated packing plates 31 have a thickness δ of 0.3 mm, and the height d2 of the quenching packing layer 30 is 0.076 m, ethylene at a temperature of 200°C is introduced into the reactor body 10 from the bottom via a first pipeline 111; oxygen at 200°C is introduced into a gas distributor 40 via a second pipeline 121. The oxygen distributed by the gas distributor 40 and the ethylene dispersed through the quenching packing layer 30 are further mixed by flame-retardant and explosion-proof packing 50 before entering the catalyst bed 20 (the catalyst filled in the catalyst bed 20 is honeycomb-shaped, and the active component is precious metal Ag). The reaction products flow out through a discharge line 131 located at the top of the reactor body 10. Based on the above results, it can be concluded that the ethylene conversion rate reaches 85-90% and the ethylene oxide selectivity is 90-95%. Similarly, using a traditional gas-solid phase catalytic reactor, it can be concluded that the ethylene conversion rate is 60-70% and the ethylene oxide selectivity is 80-85%.

[0129] While the preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, the present invention is not limited thereto. Within the technical scope of the present invention, various simple variations of the technical solution of the present invention may be made. To avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple variations and combinations should also be considered as disclosed herein and fall within the scope of protection of the present invention.

Claims

1. A gas-solid phase catalytic reactor, characterized in that: The invention comprises a reactor body (10) and a plurality of catalyst beds (20) arranged in the inner cavity of the reactor body (10), wherein the plurality of catalyst beds (20) are arranged at intervals along the flow direction of the reaction raw materials, and a quenching filler layer (30) is provided on the discharge side of each catalyst bed (20), and the quenching filler layer (30) is configured to quench the flame generated by the reaction raw materials; The quenching filler layer (30) comprises a plurality of corrugated filler plates (31) stacked in a direction parallel to the axial direction of the reactor body (10), and each of the corrugated filler plates (31) is provided with a plurality of through holes for quenching the flame generated by the reaction raw materials; The gas-solid phase catalytic reactor satisfies the following relationship: in, d 2 is the height of the quenching packing layer (30), meters; M is the relative molecular mass of the combustible gas in the reaction raw materials; d 3 is the distance between adjacent corrugated packing plates (31), in millimeters; d 1 is the height of the catalyst bed (20), m; δ is the thickness of the corrugated packing plate (31), mm; R is the inner diameter of the reactor body (10), in meters; The quenching filler layer (30) is arranged to be spaced apart from the adjacent catalyst bed layer (20).

2. The gas-solid phase catalytic reactor according to claim 1, characterized in that: The reactor body (10) has a first feed port (11) for the entry of combustible gas and a second feed port (12) for the entry of oxygen. The inner cavity of the reactor body (10) is provided with the quenching filler layer (30) located between the first feed port (11) and the second feed port (12).

3. The gas-solid phase catalytic reactor according to claim 2, characterized in that: An outlet (13) for the reaction product to flow out is provided at one end of the reactor body (10) away from the first feed port (11) and the second feed port (12).

4. The gas-solid phase catalytic reactor according to claim 2, characterized in that: A gas distributor (40) connected to the first feed port (11) and / or the second feed port (12) is provided in the inner cavity of the reactor body (10), and the gas distributor (40) is used to distribute the reaction raw materials entering the inner cavity of the reactor body (10) through the first feed port (11) and / or the second feed port (12).

5. The gas-solid phase catalytic reactor according to claim 4, characterized in that: The gas distributor (40) comprises a spiral pipe (41) and a plurality of gas outlet holes (42) arranged on the spiral pipe (41), wherein the openings of the gas outlet holes (42) face one side of the spiral pipe (41), and along the flow direction of the reaction raw materials in the spiral pipe (41), the apertures of the gas outlet holes (42) increase in sequence.

6. The gas-solid phase catalytic reactor according to claim 1, characterized in that: A fire-retardant and explosion-proof filler (50) is provided in the inner cavity of the reactor body (10), and the fire-retardant and explosion-proof filler (50) is provided at the feed end of the catalyst bed (20) close to the feed side of the reactor body (10).

7. The gas-solid phase catalytic reactor according to claim 6, characterized in that: The fire-retardant and explosion-proof filler (50) is a porous spherical non-metallic organic material.

8. The gas-solid phase catalytic reactor according to any one of claims 1 to 7, characterized in that: Each catalyst bed (20) comprises two baffles (21) installed in the inner cavity of the reactor body (10), the two baffles (21) are spaced apart along the flow direction of the reaction raw materials, a plurality of reaction tubes (22) for loading catalysts are provided between the two baffles (21), and the tube lumens of the plurality of reaction tubes (22) form a tube-side space (201) for the reaction raw materials to flow from one side of the catalyst bed (20) to the other side; A shell-side space (202) is formed between the outer walls of the plurality of reaction tubes (22) and the two baffles (21). A liquid inlet pipeline (14) and a liquid outlet pipeline (15) communicating with the shell-side space (202) are provided on the reactor body (10). The liquid inlet pipeline (14) is used to introduce a heat exchange medium into the shell-side space (202), and the heat exchange medium can be discharged through the liquid outlet pipeline (15).

9. The gas-solid phase catalytic reactor according to claim 8, characterized in that: The distance between the quenching filler layer (30) and the adjacent catalyst bed layer (20) satisfies the following relationship: in, h is the distance between the quenching packing layer (30) and the adjacent catalyst bed layer (20), in meters; v is the flow rate of the material in the reaction tube (22), meters per second; d is the inner diameter of the reaction tube (22), m; M is the relative molecular mass of the combustible gas in the reaction raw materials; D is the total area of ​​the reaction tube (22) filled with a single layer of catalyst, in square meters; T is the temperature of the material in the reactor body (10), in degrees Kelvin.

10. The gas-solid phase catalytic reactor according to claim 8, characterized in that: The liquid inlet pipeline (14) is used to pass cooling water into the shell-side space (202), and the liquid outlet pipeline (15) is used to pass the heated cooling water into the steam generator (60) to generate steam.

11. The gas-solid phase catalytic reactor according to claim 10, characterized in that: The liquid inlet pipeline (14) includes a liquid inlet main pipe (141) and a plurality of liquid inlet branch pipes (142) respectively connected to the liquid inlet main pipe (141), and the plurality of liquid inlet branch pipes (142) correspond one-to-one to the plurality of catalyst beds (20) for introducing cooling water into the shell-side space (202) of the corresponding catalyst bed (20); The liquid inlet main pipe (141) is provided with a regulating valve (143) and a control device for controlling the opening of the regulating valve (143); the steam generator (60) is provided with a liquid level meter (61); the liquid level meter (61) is electrically connected to the control device so that the control device can control the opening of the regulating valve (143) according to a liquid level height signal of the steam generator (60) monitored by the liquid level meter (61).

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