Gas-solid phase catalytic reactor

Abstract

The invention relates to the technical field of gas-solid phase catalytic reaction equipment, and discloses a gas-solid phase catalytic reactor, which comprises a reactor body and a plurality of catalyst bed layers arranged in the inner cavity of the reactor body, the plurality of catalyst bed layers are arranged at intervals along the flowing direction of reaction raw materials, the discharge side of each catalyst bed layer is provided with a quenching filler layer, and the discharge side of each catalyst bed layer is provided with a quenching filler layer. The quenching filler layer is arranged to be capable of quenching flames generated by the reaction raw materials; according to the invention, through a plurality of catalyst bed layers arranged at intervals, the intensity of gas-solid phase catalytic reaction is directly reduced, so that combustion explosion of combustible gas in reaction raw materials caused by release of excessive heat is avoided; the quenching filler layer is used for quenching flames possibly generated by reaction raw materials, so that combustible gas and oxygen can be subjected to a gas-solid phase catalytic reaction within the explosion limit, the reaction rate is increased, the reaction efficiency is improved, the economic benefits are further improved, and the device has the advantages of being safe and reliable.

Description

Technical Field

[0001] The 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, which is widely used in the oil refining, chemical, metallurgical and other industries, such as gas-phase alkylation, ammonia synthesis, benzene oxidation to produce anhydride, low-pressure methanol synthesis, etc. 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 of 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, and the reactants need to be kept at a low concentration. The reaction efficiency and economy are limited, which directly restricts its industrial application. For example, the reaction of directly combining hydrogen and oxygen to prepare hydrogen peroxide has 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, when synthesizing hydrogen peroxide at a concentration below the lower explosion limit of hydrogen, the low yield requires repeated separation and concentration steps, which increases production costs and is economically unfeasible. Another example is the direct epoxidation of propylene in the gas phase, which reduces the two-step synthesis in the liquid phase to one step. Compared with existing technologies such as the HPPO method and the chlorohydrin method, it is more energy-saving and environmentally friendly. However, it is also limited by the risk of combustion and explosion in the reaction system, and a considerable amount of diluent gas must be introduced. Another example is the process of preparing phthalic anhydride by the selective catalytic oxidation reaction of o-xylene. If the oxygen concentration in this process is too low, o-xylene will undergo incomplete oxidation reaction to produce phthalide, benzoic acid, citric anhydride, etc. If the oxygen concentration is increased, the reaction will proceed within the explosion limit, and the reactor will have the risk of combustion and explosion. Therefore, how to reduce or even eliminate the combustion and explosion risk of gas-solid phase combustible systems while maintaining high reaction efficiency has become a difficult problem that urgently needs to be solved in the chemical industry to improve quality and efficiency.

[0003] In recent years, researchers have successively prevented flame generation by adding ignition inhibitors (inert gas, fine water mist, kaolinite) to the system, improving pipeline materials to interrupt free radical chain extension reactions, and controlling the reaction residence time to be less than the autoignition induction time of the system. However, the above methods either introduce new substances into the reaction system or place high demands on the equipment material and capacity, and are not universal.

[0004] Specifically, the Chinese invention patent application with the publication number of "CN 104368100 A" discloses a hydrogen-oxygen mixed gas dry-wet integrated flame arrester, the technical points of which are: a hydrogen-oxygen mixed gas outlet pipe is arranged on the top of the sub-fire arrester shell, an explosion-proof membrane and a pressure sensor connected to the control circuit are arranged at the bottom of the shell, the mother fire arrester shell is isolated by a stainless steel hole-shaped fire arrester plate, and a fire-retardant filler layer, a stainless steel capillary layer and a water seal layer are filled from top to bottom, a safety valve connecting pipe is arranged on the top of the mother fire arrester shell, and a hydrogen-oxygen mixed gas inlet and a liquid level sensor connected to the control circuit are arranged on the side wall of the water seal layer at the bottom of the shell. Its structural design is reasonable, and it is safe and reliable to use. It not only has the function of sealing and stopping fire of a dry flame arrester, but also can use water seals and baffles to reduce the flame temperature and pressure reduction, and can effectively prevent the hazards of hydrogen-oxygen mixed gas during tempering, flash explosion and deflagration. However, the technology involves a flame arrester structure, which cannot be installed in a reactor, and the water seal will cause the catalyst in the reactor to cement 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 test system, an automatic gas distribution system, a temperature test system, an ion probe detection system, a data acquisition instrument, a high-voltage ignition system and a synchronous controller. The device can be used for: (1) studying 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) studying the control and suppression effects of inhibitors, metal fire arrester nets, fine water mist, etc. on flame propagation, and developing 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, the 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 ABC ultrafine dry powder explosion suppression experimental device, which is specifically composed of an explosion pipe, a flange plate, a multi-stage cavity, an electric ignition head, a gas distribution device, an explosion suppression powder injection device and a data acquisition device. The invention device studies the effect of the change of the spatial position of the dry powder explosion suppression device on the explosion suppression effect under different gas concentrations. However, the dry powder explosion suppression device cannot be used in a reactor for gas-solid phase catalytic reaction. Summary of the invention

[0007] The purpose of the present invention is to overcome the defects of existing gas-solid phase catalytic reactors that are limited by the explosion risk of the reaction system, and many reactions containing oxygen 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, effectively improving the selectivity and conversion rate of the oxidation process.

[0008] In order to achieve the above-mentioned purpose, 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, 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.

[0009] Optionally, the quenching packing layer comprises a plurality of corrugated packing plates stacked in a direction parallel to the axial direction of the reactor body, and a plurality of through holes are formed on the plate body of each of the corrugated packing plates 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 toward 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 packing layer is arranged to be spaced apart from the adjacent catalyst bed layer.

[0018] Optionally, a fire-retardant and explosion-proof filler is arranged in the inner cavity of the reactor body, and the fire-retardant and explosion-proof filler is arranged at the feed end of the catalyst bed layer 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, a plurality of reaction tubes for loading catalysts are arranged 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 a liquid inlet pipeline and a liquid outlet pipeline connected to the shell-side space are provided on the reactor body, 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, 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 It is a structural schematic diagram of a gas-solid phase catalytic reactor provided by the present invention;

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

[0030] Figure 3 It 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 packing layer provided by the present invention.

[0032] Description of Reference Numerals

[0033] 10. Reactor body; 11. First feed inlet; 111. First pipeline; 12. Second feed inlet; 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 pipeline; 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 specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.

[0035] In order to avoid the risk of combustion and explosion 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, and 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, 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.

[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 arranged 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 the traditional gas-solid phase catalytic reactor 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 continuous propagation of the flame 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 in the existing green process route, and providing an intrinsically safe solution for the gas-solid phase catalytic reaction process with a higher risk of explosion.

[0039] As a specific implementation method 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 includes a plurality of corrugated packing plates 31 stacked in a direction parallel to the axial direction of the reactor body 10, and a plurality of through holes are provided on the plate body of each of the corrugated packing plates 31 for quenching the flame generated by the reaction raw materials. It can be understood that the quenching packing layer 30 also includes a packing ring 32 for fixing the plurality of stacked corrugated packing plates 31 to form a quenching packing layer 30 with a certain height.

[0040] In this embodiment, the through holes provided on the corrugated packing plate 31 can change the direction of the airflow, so that the flame cannot propagate and quench the flame. The through holes can be holes of various shapes, such as circular holes, triangular holes, square holes or rectangular holes, preferably rectangular holes. The multiple through holes can be holes of the same shape or holes 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 be operated within the explosion limit, thereby increasing its oxidation efficiency.

[0043] In the present application, the inventors discovered the structure-function 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 according to the quenching distance between the combustible gas flames of different components at different concentrations and the height of the catalyst bed 20, thereby designing the matching form between different quenching packing layers 30 and the height of the catalyst bed 20, 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 combustible gas to enter and a second feed port 12 for oxygen to enter, and 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. By providing the quenching filler layer 30 between the first feed port 11 and the second feed port 12, the flame is prevented 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 conveying 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 conveying oxygen into the inner cavity of the reactor body 10 .

[0049] Further, in the present invention, the reactor body 10 is provided with a discharge port 13 for the reaction product to flow out at one end away from the first feed port 11 and the second feed port 12. It is understood that the discharge port 13 is connected to a discharge pipeline 131 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, 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. The reaction raw materials are fully mixed by the gas distributor 40 before entering the catalyst bed 20, ensuring the efficient catalytic oxidation reaction and avoiding the situation where the catalyst bed 20 is locally overheated due to 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 to respectively input the reaction raw materials into the inner cavity of the reactor body 10. 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 relatively low 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 the 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 one commonly used by those skilled 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 sequence along the flow direction of the reaction raw materials in the spiral pipe 41. By designing the apertures of the plurality of gas outlet holes 42 in the flow direction of the reaction raw materials, it is ensured that the reaction raw materials are evenly distributed in the radial direction of the inner cavity of the reactor body 10.

[0054] In some embodiments, the quenching filler layer 30 is disposed to be spaced apart from the adjacent catalyst bed layer 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 layer of 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 disposed in the inner cavity of the reactor body 10 , and the fire-retardant and explosion-proof filler 50 is disposed 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 flame retardancy, but also promote the reaction raw materials entering the first catalyst bed 20 to be more evenly distributed 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, 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 arranged between the two baffles 21, 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 a liquid inlet pipeline 14 and a liquid outlet pipeline 15 connected to the shell-side space 202 are provided on the reactor body 10, the liquid inlet pipeline 14 is used to introduce 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 in the reactor body 10 divided into multiple layers and arranged at intervals along the flow direction of the reaction raw materials, but also a component capable of achieving heat transfer is arranged for each catalyst bed 20. In specific use, a heat exchange medium is introduced into the shell space 202 of the catalyst bed 20 through the liquid inlet pipeline 14, and the heat generated by the gas-solid phase catalytic reaction in the reaction tube 22 is quickly removed to avoid overheating of the catalyst bed 20 and damage to the catalyst, and at the same time, the temperature is assisted to be lowered to below the autoignition point of the system, which significantly reduces the risk of combustion and explosion of the combustible gas / oxygen system, so that the gas-solid phase catalytic reactor can ensure that the catalytic oxidation reaction of the combustible gas and oxygen is operated 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 risk of combustion and explosion of the combustible gas / oxygen system.

[0061] The inventors of the present application have found that by making the distance between the quenching packing layer 30 and the adjacent catalyst bed layer 20 satisfy the following relationship, it is possible to ensure that the reaction raw materials are better mixed before entering the next catalyst bed layer 20, and avoid the problem of increased equipment investment due to excessive distance between the two. The relationship is:

[0062]

[0063] Among them, h is the distance between the quenching filler layer 30 and the adjacent catalyst bed layer 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 pass cooling water into the shell space 202, and the liquid outlet line 15 is used to pass the heated cooling water into the steam generator 60 to generate steam. By setting up the steam generator 60, the heat of the gas-solid phase catalytic reaction is recycled and utilized, thereby reducing the 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 can be understood that the steam generator 60 is also connected to a steam pipeline 62 for sending 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 a DCS control device to form an interlocking control. The DCS control device is configured to control the opening of the pressure regulating valve 621 according to a 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 controlled by feedback adjustment, 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 also 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 arranged at the top of the reactor body 10. Flow out, after the flow rate stabilizes, the molar ratio of methane to oxygen in the discharge pipeline 131 is detected to be 1:2; the catalyst bed 20 is ignited by the spark plug 70, when the height d1 of the catalyst bed 20 is 0.5m, the inner diameter R of the reactor body 10 is 0.5m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, a corrugated packing plate 31 with a thickness δ of 0.3mm is used, and when the height d2 of the quenching packing layer 30 is 0.028m, 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 plate 31 are adjusted respectively, and an orthogonal test is 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 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 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 rate v of the material in the reaction tube 22 filled with the catalyst was 8m / s, the diameter d of the reaction tube 22 filled with the catalyst was 10mm, and the total area D of the reaction tube 22 filled with a single layer of catalyst was 0.15m 2 When the material temperature T in the reactor is 500K and the spacing 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 spacing h between the quenching packing layer 30 and the adjacent catalyst bed layer 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 loaded with catalyst, and the total area D of the reaction tube 22 loaded 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 filler layer 30 and the adjacent catalyst bed layer 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 arranged 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 0.5m, the inner diameter R of the reactor body 10 is 0.5m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, a corrugated packing plate 31 with a thickness δ of 0.3mm is used. When the height d2 of the quenching packing layer 30 is 0.052m, 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 plate 31 are adjusted respectively, and an orthogonal test is 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 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 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 rate v of the material in the reaction tube 22 filled with the catalyst was 8 m / s, the diameter d of the reaction tube 22 filled with the catalyst was 10 mm, and the total area D of the reaction tube 22 filled with a single layer of catalyst was 0.15 m 2 When the material temperature T in the reactor is 500K and the spacing h between the quenching packing layer 30 and the adjacent catalyst bed layer 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 spacing h between the quenching packing layer 30 and the adjacent catalyst bed layer 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 loaded with catalyst, and the total area D of the reaction tube 22 loaded 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 filler layer 30 and the adjacent catalyst bed layer 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 arranged at the top of the reactor body 10. Flow out, after the flow rate stabilizes, the molar ratio of propane to oxygen in the discharge pipeline 131 is detected to be 1:5; the catalyst bed 20 is ignited by the spark plug 70, when the height d1 of the catalyst bed 20 is 0.5m, the inner diameter R of the reactor body 10 is 0.5m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, a corrugated packing plate 31 with a thickness δ of 0.3mm is used, and when the height d2 of the quenching packing layer 30 is 0.076m, 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 plate 31 are adjusted respectively, and an orthogonal test is 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 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 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 rate v of the material in the reaction tube 22 filled with the catalyst was 8m / s, the diameter d of the reaction tube 22 filled with the catalyst was 10mm, and the total area D of the reaction tube 22 filled with a single layer of catalyst was 0.15m 2 When the material temperature T in the reactor is 500K and the spacing h between the quenching packing layer 30 and the adjacent catalyst bed layer 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 layer 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 loaded with catalyst, and the total area D of the reaction tube 22 loaded 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 filler layer 30 and the adjacent catalyst bed layer 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] According to the experimental data of the height of the catalyst bed 20 of methane, ethane and propane in the reactor body 10, the distance between the adjacent corrugated packing plates 31 in the quenching packing layer 30, the thickness of the corrugated packing plate 31, the inner diameter of the reactor body 10 and the height of the quenching packing layer 30, after the relative molecular mass of the combustible gas is introduced, 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 can be operated within its explosion limit, thereby increasing its oxidation efficiency and improving 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] Take the catalytic oxidation of ethylene to produce ethylene oxide as an example for comparison. When the height d1 of the catalyst bed 20 is 0.5m, the inner diameter R of the reactor body 10 is 0.5m, and the spacing d3 between adjacent corrugated packing plates 31 in the quenching packing layer 30 is 0.1mm, a corrugated packing plate 31 with a thickness δ of 0.3mm is used, and when the height d2 of the quenching packing layer 30 is 0.076m. Ethylene at a temperature of 200°C is introduced into the reactor body 10 from the bottom through the first pipeline 111; oxygen at 200°C is introduced into the gas distributor 40 through the second pipeline 121 respectively, and the oxygen distributed by the gas distributor 40 and the ethylene dispersed by the quenching packing layer 30 are further mixed through the flame-retardant and explosion-proof filler 50, and then enter the catalyst bed 20 (the catalyst filled in the catalyst bed 20 is honeycomb-shaped, and the active component is precious metal Ag), and the reaction product flows out through the discharge pipeline 131 arranged at the top of the reactor body 10. According to the above results, it can be concluded that the conversion rate of ethylene reaches 85-90%, and the selectivity of ethylene oxide is 90-95%. Similarly, using a traditional gas-solid phase catalytic reactor, it can be concluded that the conversion rate of ethylene is 60-70%, and the selectivity of ethylene oxide is 80-85%.

[0129] The preferred embodiments of the present invention are described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope 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 arranged to be able to quench the flame generated by the reaction raw materials.

2. The gas-solid phase catalytic reactor according to claim 1, characterized in that: 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.

3. The gas-solid phase catalytic reactor according to claim 2, characterized in that: The gas-solid phase catalytic reactor satisfies the following relationship: Wherein, 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).

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

5. The gas-solid phase catalytic reactor according to claim 4, 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 inlet (11) and the second feed inlet (12).

6. The gas-solid phase catalytic reactor according to claim 4, 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).

7. The gas-solid phase catalytic reactor according to claim 6, 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 successively.

8. The gas-solid phase catalytic reactor according to claim 1, characterized in that: The quenching filler layer (30) is arranged to be spaced apart from the adjacent catalyst bed layer (20).

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

10. The gas-solid phase catalytic reactor according to claim 9, characterized in that: The fire-retardant and explosion-proof filler (50) is a porous spherical non-metallic organic material.

11. The gas-solid phase catalytic reactor according to any one of claims 1 to 10, characterized in that: Each of the catalyst beds (20) comprises two baffles (21) installed in the inner cavity of the reactor body (10), the two baffles (21) being arranged at intervals along the flow direction of the reaction raw materials, a plurality of reaction tubes (22) for loading catalysts being arranged between the two baffles (21), the tube lumens of the plurality of reaction tubes (22) forming 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) connected to 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).

12. The gas-solid phase catalytic reactor according to claim 11, characterized in that: The distance between the quenching packing layer (30) and the adjacent catalyst bed layer (20) satisfies the following relationship: Wherein, h is the distance between the quenching filler layer (30) and the adjacent catalyst bed layer (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) loaded with a single layer of catalyst, and T is the material temperature in the reactor body (10).

13. The gas-solid phase catalytic reactor according to claim 11, 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.

14. The gas-solid phase catalytic reactor according to claim 13, characterized in that: The liquid inlet pipeline (14) comprises a liquid inlet main pipe (141) and a plurality of liquid inlet branch pipes (142) respectively connected to the liquid inlet main pipe (141), wherein the plurality of liquid inlet branch pipes (142) correspond one-to-one to the plurality of catalyst beds (20) so as to be used 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).

Images