Efficient heat transfer reactor for catalytic oxidation of hydrogen chloride

Abstract

The utility model relates to the technical field of high-efficiency heat transfer reactors, in particular to a hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor which comprises a barrel, a first seal head is mounted at the top of the barrel, a gas outlet pipe is mounted on the first seal head and communicated with a liquid inlet pipe through a condensation part, and the liquid inlet pipe is fixed on the side surface of the barrel and communicated with the inside of the barrel; a fixed bed is mounted in the barrel and is used for completing catalytic oxidation reaction of hydrogen chloride; a second sealing head is mounted at the bottom of the barrel, a mixing part is mounted in the barrel, an inlet of the mixing part is communicated with a liquid outlet pipe, the liquid outlet pipe is mounted at the bottom of the barrel and communicated with the interior of the barrel, and an outlet of the mixing part is formed in the barrel. According to the utility model, the gasified heat-transfer medium is liquefied in time through the condensation part and then recycled, and the heat-transfer medium is effectively distributed and circulated through the mixing part, so that efficient heat exchange between reaction heat in the fixed bed and the heat-transfer medium is realized, and stable and efficient reaction in the fixed bed is ensured.

Description

TECHNICAL FIELD

[0001] The utility model relates to high -efficient heat transfer reactor technical field especially relates to a hydrogen chloride catalytic oxidation high -efficient heat transfer reactor. BACKGROUND

[0002] In the industrial process of producing various chlorine products, the utilization rate of chlorine is less than half, and byproduct gas hydrogen chloride is produced. Due to its strong corrosion, high transportation cost, oversupply and other disadvantages, hydrogen chloride is often used as raw material to prepare chlorine, so as to achieve the dual purposes of hydrogen chloride treatment and chlorine element recycling.

[0003] At present, among the chemical process methods for preparing chlorine gas with hydrogen chloride as raw material, the catalytic oxidation method is the most competitive, so it is widely used in industrial production. Catalytic oxidation method is a method for generating chlorine gas by oxidizing hydrogen chloride with oxygen or air as oxidant under the action of catalyst, and its stoichiometric formula can be expressed as:

[0004]

[0005] This reaction is a strong exothermic reaction, and generally adopts the way of strengthening heat transfer to prevent the formation of hot spots inside the reactor and avoid affecting the service life of the catalyst. CN116899558B reports a high-thermal-stability high-thermal-conductivity ruthenium catalyst doped with high-thermal-conductivity ceramics, which improves the removal of heat generated during the reaction process and prolongs the service life of the catalyst. CN115155632B also uses a high-thermal-conductivity composite carrier to improve the heat removal efficiency of the hydrogen chloride oxidation catalyst and significantly improve the stability and service life of the catalyst.

[0006] The above method is to strengthen the heat transfer by strengthening the heat transfer efficiency of the catalyst inside the fixed bed reaction tube. While strengthening the heat transfer inside the reaction tube, the heat transfer efficiency outside the reaction tube also needs to be strengthened to avoid the temperature inside the reaction tube being too high due to the untimely external heat transfer, thereby affecting the service life of the catalyst.

[0007] At present, CN101223104B discloses a multi-tube heat exchange reactor, which is divided into multiple areas by a partition, and each area has a heat transfer medium circulating therein. Although this process realizes constant temperature control, and since the heat transfer medium does not undergo phase change, the heat transfer coefficient of this heat transfer process is relatively low, and the untimely heat transfer can easily cause hot spots, leading to catalyst deactivation. Moreover, a large heat transfer temperature difference will cause the temperature of the laminar flow bottom layer near the heat transfer surface to be low, which is quite different from the target temperature, resulting in a decrease in reaction yield.

[0008] JP2001139499A discloses a heat medium circulation method of a multi-tube reactor, circulating the heat medium taken out from the reactor shell to a specific position of the circulation device, and mixing the heat medium after heat exchange with the heat medium discharged from the reactor shell very effectively; although this process increases the effective mixing of the heat medium and the heat medium after heat exchange, the way of increasing the mixing only increases the circulation, and the heat transfer temperature difference still needs to be controlled at 15 DEG C or more, which reduces the catalytic efficiency of the heat transfer laminar flow catalyst.

[0009] DE1601162C3 reactor realizes effective removal of reaction heat by externally arranging a conveyor and a cooler, and is provided with a ring line with uniform openings, so that the heat transfer medium is uniformly pressed radially into the space around the tube bundle, and is provided with a baffle to ensure uniform heat exchange of the whole device; DE3409159C2 reactor is provided with a plurality of open outer annular tubes on the wall of each end to introduce or remove heat, so as to cause uniform temperature distribution, and the contact tube bundle and the radial supply and discharge of the heat and endothermic catalytic reaction are carried out through the annular channel in the loop through the external heat exchanger. Although the above two devices can improve the heat exchange effect to a certain extent, the ability to improve the heat transfer coefficient is limited, and there is a large temperature difference between the inlet and outlet of the heat transfer medium, thereby reducing the catalytic effect of the catalyst and affecting the reaction efficiency of the whole device. The above patents cannot well solve the problem of low external heat transfer efficiency. Practical new type content

[0010] In order to solve the foregoing technical problems, the utility model provides a hydrogen chloride catalytic oxidation high -efficient heat transfer reactor, this reactor is through setting up several flow guide mouth according to different needs in different regions, increased medium heat transfer effect, solve the problem of low heat transfer efficiency, specifically through the following technical scheme realizes.

[0011] The utility model discloses a hydrogen chloride catalytic oxidation high -efficient heat transfer reactor including cylinder, first end cover is installed at the top of cylinder, the gas pipe is installed on first end cover, the gas pipe with cylinder inside intercommunication, the gas pipe passes through first pipeline and communicates with liquid inlet pipe, and the liquid inlet pipe is fixed on the side of cylinder and communicates with its inside.

[0012] Pressure regulating valve, condensing portion, heat transfer medium buffer tank, feeding pump are installed in proper order on first pipeline, and the condensing portion is used for liquefying gaseous heat transfer medium again.

[0013] A plurality of supports are installed in the cylinder, and a fixed bed is installed on the support, the fixed bed includes a reaction tube, a plurality of reaction tubes are vertically arranged in the cylinder, and the reaction tube is not communicated with the inside of the cylinder.

[0014] The bottom of the cylinder is provided with a second head, and a mixing part is arranged in the cylinder, which comprises a mixing liquid inlet pipe, the first end of which is fixedly connected with a third head, the third head is fixedly connected with a plurality of mixing cylinders, the mixing cylinders are vertically arranged between the reaction tubes, and a plurality of flow guide openings are arranged on the mixing cylinders and connected with the inside of the cylinder.

[0015] The second end of the mixing liquid inlet pipe penetrates through the second head and is connected with a liquid outlet pipe through a second pipeline, the liquid outlet pipe is arranged at the bottom of the cylinder and connected with the inside of the cylinder, and a circulating pump is arranged on the second pipeline.

[0016] Preferably, the top of the mixing cylinder is sealed, and the mixing cylinder is a tubular structure with a diameter of 0.5-2.5 m, and the length of the mixing cylinder is 0.3-0.8 m longer than the reaction tube.

[0017] Preferably, the fixed bed further comprises a fourth head, the top of the reaction tube is fixedly connected with the fourth head, and the fourth head is connected with a reaction gas inlet pipe.

[0018] The bottom of the reaction tube is fixedly connected with a fifth head, and the fifth head is connected with a reaction gas outlet pipe.

[0019] Preferably, the condensing part comprises a feeding pipe, the gas outlet pipe is connected with the feeding pipe, the feeding pipe is connected with the first end of a plurality of heat exchange pipes, the second end of the heat exchange pipe is connected with a discharging pipe, and the discharging pipe is connected with the liquid inlet pipe.

[0020] A plurality of heat exchange pipes are uniformly arranged in a heat exchange area, the first end of the heat exchange area is fixedly connected with a water inlet pipe, and the second end of the heat exchange area is fixedly connected with a steam outlet pipe.

[0021] Preferably, the support device comprises a support column and a spring, the spring is fixedly connected with the support column, the support column is fixedly connected with the fixed bed, and the spring is fixedly connected with the second head.

[0022] Preferably, the flow guide opening is a circular through hole with an opening diameter of 2-10 cm.

[0023] Preferably, the structure composed of the mixing cylinder and the flow guide opening is uniformly and centrally symmetrically distributed about the axis of the cylinder.

[0024] Preferably, the mixing cylinder is divided into four regions along the height, each region has a height of 0.5-2 m, the opening rate of the highest region is 40%-50%, and the opening rate of each region decreases by 3%-5% from top to bottom.

[0025] After adopting the above technical solution, the beneficial effects of the utility model are:

[0026] 1. The reactor is equipped with a mixing component inside to fully remove the reaction heat through the gasification of the heat transfer medium. According to the reaction intensity of different areas, a number of dispersed diversion ports of different sizes are arranged in sequence to increase the heat transfer effect of the medium and greatly improve the heat transfer efficiency.

[0027] 2. The reactor uses reaction heat to prepare steam and adjusts the reaction temperature through the gas phase outlet pressure regulating valve and reaction temperature interlock control, making the reaction temperature control more precise and maintaining the high catalytic efficiency of the catalyst, thereby stably and efficiently preparing chlorine and effectively reducing production costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0029] Figure 1 Schematic diagram of a high-efficiency heat transfer reactor for catalytic oxidation of hydrogen chloride;

[0030] Figure 2 It is a structural diagram of the mixing section;

[0031] Figure 3 It is a transverse cross-sectional schematic diagram of the interior of the cylinder;

[0032] Figure 4 Schematic diagram of the fixed bed structure;

[0033] Figure 5 Schematic diagram of the structure of the condensation unit.

[0034] Description of reference numerals:

[0035] 10-cylinder, 11-first end cap, 12-second end cap, 13-support, 14-air outlet pipe, 15-liquid inlet pipe, 16-liquid outlet pipe;

[0036] 30- condensation section, 31- feed pipe, 32- discharge pipe, 33- water inlet pipe, 34- steam outlet pipe, 35- heat exchange area;

[0037] 40-heat transfer medium buffer tank, 50-feed pump, 60-circulation pump;

[0038] 70-mixing part, 71-mixing liquid inlet pipe, 72-third head, 73-mixing cylinder, 74-diversion port;

[0039] 80 - fixed bed, 81 - reaction tube, 82 - fourth head, 83 - reaction inlet tube, 84 - fifth head, 85 - reaction outlet tube. DETAILED DESCRIPTION

[0040] The features and exemplary embodiments of each aspect of the present application will be described below in detail, in order to make the purpose, technical scheme and advantages of the present application more clear and apparent, the present application will be described further in detail below in combination with the drawings and specific embodiments. It should be understood that the specific embodiments described herein are configured only to explain the present application and are not configured to limit the present application. For those skilled in the art, the present application can be implemented without some of these specific details. The following description of the embodiments is only to provide a better understanding of the present application by showing examples of the present application.

[0041] The orientation words appearing in the following description are the directions shown in the drawings, and are not limited to the specific structure of the present application. In the description of the present application, it should be noted that, unless otherwise explicitly specified and limited, the terms "mounting", "connection" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected or integrally connected; it can be directly connected or indirectly connected. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0042] The embodiment of the present application provides a hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor, referring to Figure 1 The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor comprises a cylinder body 10, a first head 11 is sealingly and fixedly installed at the top of the cylinder body 10, a gas outlet pipe 14 is fixedly installed on the first head 11, the gas outlet pipe 14 is communicated with the inside of the cylinder body 10, the gas outlet pipe 14 is communicated with a liquid inlet pipe 15 through a first pipeline, the liquid inlet pipe 15 is fixedly installed on the side of the cylinder body 10 and communicated with the inside of the cylinder body 10, and a pressure regulating valve, a condensing part 30, a heat transfer medium buffer tank 40 and a feed pump 50 are sequentially installed on the first pipeline, and the condensing part 30 is used for liquefying the vaporized heat transfer medium again.

[0043] A plurality of support devices 13 are fixedly installed in the inside of the cylinder body 10, a fixed bed 80 is fixedly installed on the support device 13, the fixed bed 80 comprises a reaction tube 81, a plurality of reaction tubes 81 are vertically arranged in the inside of the cylinder body 10, the reaction tube 81 is not communicated with the inside of the cylinder body 10, and the catalytic oxidation reaction of hydrogen chloride is completed in the inside of the reaction tube 81.

[0044] The bottom of the cylinder 10 is sealingly and fixedly installed with a second head 12, and the inside of the cylinder 10 is fixedly installed with a mixing part 70, which comprises a mixing liquid inlet pipe 71, the first end of which is fixedly connected with and communicates with the bottom of a third head 72, the top of the third head 72 is fixedly connected with and communicates with the first ends of a plurality of mixing cylinders 73, the plurality of mixing cylinders 73 are evenly and vertically arranged between a plurality of reaction tubes 81, and a flow guide opening 74 is formed in the side wall of the mixing cylinder 73, which communicates the inside of the mixing cylinder 73 with the inside of the cylinder 10.

[0045] The second end of the mixing liquid inlet pipe 71 communicates with a liquid outlet pipe 16 through a second pipeline after passing through the second head 12, the liquid outlet pipe 16 is fixedly installed at the bottom of the cylinder 10 and communicates with the inside of the cylinder 10, and a circulating pump 60 is installed on the second pipeline.

[0046] Among them, the person skilled in the art can adjust the pressure regulating valve on the first pipeline, thereby controlling the pressure in the cylinder 10, so as to effectively adjust the temperature in the cylinder 10, and realize the accurate control of the temperature in the cylinder 10.

[0047] Among them, the high-efficiency heat transfer reactor is preferably filled with a catalyst with high thermal conductivity, such as a catalyst doped with a high-thermal-conductivity metal material, or a catalyst doped with a high-thermal-conductivity ceramic material such as silicon carbide, silicon nitride, boron nitride, etc., or a catalyst based on SiC, BN, and α-Al2O3.

[0048] Among them, the support 13 comprises a support column and a spring, the spring is fixedly connected with the support column, the support column is fixedly connected with the bottom of the fixed bed 80, and the spring is fixedly connected with the second head 12, and through the buffering effect of the spring, the damage to the equipment can be effectively reduced.

[0049] In the process of completing the catalytic oxidation of hydrogen chloride by using the high-efficiency heat transfer reactor with the above structure, the temperature control in the reactor is realized through the circulation of the heat transfer medium in two paths.

[0050] The first path is that the gaseous heat transfer medium in the reactor is discharged outward through the gas outlet pipe 14, and then returns to the inside of the cylinder 10 through the first pipeline in turn through the pressure regulating valve, the condensing part 30, the heat transfer medium buffer tank 40, the feeding pump 50, and the liquid inlet pipe 15, and when passing through the condensing part 30, the gaseous heat transfer medium is liquefied again, and then participates in the circulation again after the temperature control through the standing of the heat transfer medium buffer tank 40.

[0051] The second path is that the heat transfer medium without vaporization in the reactor is discharged from the bottom of the cylinder 10 to the outside through the liquid outlet pipe 16, and is returned to the inside of the cylinder 10 through the second pipeline in turn through the circulating pump 60, the mixed liquid inlet pipe 71, the third head 72, the mixing cylinder 73, and the flow guide port 74. In the circulation process, on the one hand, the original heat transfer medium in the cylinder 10 is mixed with the heat transfer medium re-entering the inside of the cylinder 10 after being liquefied, and on the other hand, the heat transfer medium is uniformly distributed to the inside of the cylinder 10 through the flow guide port 74, so that the heat transfer medium is uniformly attached to the outer wall of the reaction tube 81, thereby performing more efficient heat transfer and being beneficial to controlling the reaction temperature.

[0052] As a further explanation of the utility model, see Figure 2 、 3 The top of the mixing cylinder 73 in the above embodiment is sealed, and the mixing cylinder 73 is a tubular structure, the pipe diameter of which is 0.5-2.5 m, preferably 0.8-1.5 m, and the length of the mixing cylinder 73 is 0.3-0.8 m longer than the reaction tube 81.

[0053] The mixing cylinder 73 is divided into several regions, preferably four regions, along the height direction from top to bottom, the height of each region is 0.5-2 m, preferably 0.8-1.5 m, the density of the flow guide port 74 opened on each region is different, that is, the opening rate of each region is different, and the opening rate decreases from top to bottom, the opening rate of the highest region (the region at the top of the mixing cylinder 73, for example, the first region shown in Figure 2 The opening rate of the highest region (the region at the top of the mixing cylinder 73, for example, the first region shown in

[0054] The structure composed of the mixing cylinder 73 and the flow guide port 74 is uniformly and centrally symmetrically distributed in multiple groups, preferably four groups, about the axis of the cylinder 10.

[0055] The flow guide port 74 is a circular through hole, and the opening diameter is 2-10 cm, preferably 3-6 cm.

[0056] The above structure in the embodiment realizes the balance of the temperature at different positions by opening the flow guide ports 74 with different densities at different horizontal height positions. Since the flow direction of the heat transfer medium in the mixing cylinder 73 is from bottom to top, more flow guide ports 74 are opened at higher horizontal height positions, thereby ensuring the temperature balance of the upper and lower positions of the reaction tube 81 and promoting the efficient and balanced reaction.

[0057] As a further explanation of the utility model, see Figure 4The fixed bed 80 in the above embodiment further comprises a fourth head 82, a reaction gas inlet pipe 83, a fifth head 84 and a reaction gas outlet pipe 85, the top of the plurality of reaction pipes 81 is fixedly connected to the bottom of the fourth head 82 and in communication, the top of the fourth head 82 is fixedly connected to the first end of the reaction gas inlet pipe 83 and in communication, the second end of the reaction gas inlet pipe 83 penetrates the side wall of the cylinder body 10 and is in communication with the outside, and the reaction gas enters the reaction pipe 81 through the reaction gas inlet pipe 83.

[0058] The bottom of the plurality of reaction pipes 81 is fixedly connected to the top of the fifth head 84 and in communication, the bottom of the fifth head 84 is fixedly connected to the first end of the reaction gas outlet pipe 85 and in communication, the second end of the reaction gas outlet pipe 85 penetrates the side wall of the cylinder body 10 and is in communication with the outside, and the product gas in the reaction pipe 81 is outputted to the outside through the reaction gas outlet pipe 85.

[0059] Through the above structure, the reaction gas enters the fourth head 82 from the reaction gas inlet pipe 83, the reaction gas is uniformly distributed in the fourth head 82 and then enters each reaction pipe 81, and after the reaction is completed in the reaction pipe 81, the product gas is gathered in the fifth head 84 and flows out of the reactor through the reaction gas outlet pipe 85.

[0060] As another embodiment of the utility model, the condensing part 30 is a steam generator, which comprises a feeding pipe 31, a discharging pipe 32, a water inlet pipe 33, a steam outlet pipe 34 and a heat exchange area 35; the gas outlet pipe 14 is in communication with the feeding pipe 31, the feeding pipe 31 is connected to the first end of a plurality of heat exchange pipes and in communication, the second end of the plurality of heat exchange pipes is connected to the discharging pipe 32 and in communication, and the discharging pipe 32 is in communication with the liquid inlet pipe 15.

[0061] The plurality of heat exchange pipes are uniformly arranged in the heat exchange area 35, the first end of the heat exchange area 35 is fixedly connected to the water inlet pipe 33 and in communication, and the second end of the heat exchange area 35 is fixedly connected to the steam outlet pipe 34 and in communication.

[0062] In this embodiment, the gaseous heat transfer medium is transmitted to the feeding pipe 31 through the gas outlet pipe 14 and enters the heat exchange pipe, heat exchange is realized in the heat exchange pipe, so that the gaseous heat transfer medium is liquefied again and flows back to the inside of the cylinder body 10 through the discharging pipe 32 and the liquid inlet pipe 15.

[0063] In this process, the heat exchange pipe transfers the excess heat to the cooling water outside the heat exchange pipe, so that the water is vaporized to generate steam, and the process realizes the recycling and effective utilization of energy, energy saving and environmental protection.

[0064] In accordance with the above embodiments of the present application, these embodiments do not describe all the details, nor limit the present application to only specific embodiments. Obviously, according to the above description, many modifications and changes can be made. The present application selects and specifically describes these embodiments in order to better explain the principles and practical applications of the present application, so that those skilled in the art can well utilize the present application and make modifications based on the present application. Any modification, equivalent replacement, improvement, etc. made within the spirit and principles of the present application shall be included in the protection scope of the present application.

Claims

1. A high-efficiency heat transfer reactor for catalytic oxidation of hydrogen chloride comprising a cylinder (10), characterized in that: The top of the cylinder (10) is provided with a first head (11), the first head (11) is provided with a gas outlet pipe (14), the gas outlet pipe (14) is communicated with the inside of the cylinder (10), the gas outlet pipe (14) is communicated with a liquid inlet pipe (15) through a first pipeline, the liquid inlet pipe (15) is fixed on the side of the cylinder (10) and communicated with the inside of the cylinder (10); The first pipeline is sequentially provided with a pressure regulating valve, a condensing part (30), a heat transfer medium buffer tank (40) and a feed pump (50), the condensing part (30) is used for liquefying the gaseous heat transfer medium; The inside of the cylinder (10) is provided with a plurality of support devices (13), the support devices (13) are provided with fixed beds (80), the fixed beds (80) comprise reaction tubes (81), a plurality of reaction tubes (81) are vertically arranged in the cylinder (10), and the reaction tubes (81) are not communicated with the inside of the cylinder (10); The bottom of the cylinder (10) is provided with a second head (12), the inside of the cylinder (10) is provided with a mixing part (70), the mixing part (70) comprises a mixing liquid inlet pipe (71), the first end of the mixing liquid inlet pipe (71) is fixed and communicated with a third head (72), the third head (72) is fixed and communicated with a plurality of mixing cylinders (73), a plurality of mixing cylinders (73) are vertically arranged between a plurality of reaction tubes (81), a plurality of flow guide openings (74) are formed in the mixing cylinders (73), and the flow guide openings (74) are communicated between the mixing cylinders (73) and the inside of the cylinder (10); The second end of the mixing liquid inlet pipe (71) penetrates through the second head (12) and is communicated with a liquid outlet pipe (16) through a second pipeline, the liquid outlet pipe (16) is arranged at the bottom of the cylinder (10) and communicated with the inside of the cylinder (10), and a circulating pump (60) is arranged on the second pipeline.

2. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The top of the mixing cylinder (73) is sealed, and the mixing cylinder (73) is a tubular structure, the pipe diameter of the mixing cylinder (73) is 0.5-2.5 m, and the length of the mixing cylinder (73) is longer than that of the reaction tube (81) by 0.3-0.8 m.

3. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The fixed bed (80) further comprises a fourth head (82), the top of a plurality of reaction tubes (81) is fixed and communicated with the fourth head (82), and the fourth head (82) is communicated with a reaction gas inlet pipe (83); The bottom of a plurality of reaction tubes (81) is fixed and communicated with a fifth head (84), and the fifth head (84) is communicated with a reaction gas outlet pipe (85).

4. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The condensing part (30) comprises a feeding pipe (31), the gas outlet pipe (14) communicates with the feeding pipe (31), the feeding pipe (31) communicates with the first ends of a plurality of heat exchange pipes, the second ends of the plurality of heat exchange pipes communicate with a discharging pipe (32), and the discharging pipe (32) communicates with the liquid inlet pipe (15); The plurality of heat exchange pipes are uniformly arranged in a heat exchange zone (35), the first end of the heat exchange zone (35) is fixed with a water inlet pipe (33), and the second end of the heat exchange zone (35) is fixed with a steam outlet pipe (34).

5. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The support device (13) comprises a support column and a spring, the spring is fixed with the support column, the support column is fixed with the fixed bed (80), and the spring is fixed with the second end cover (12).

6. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The flow guide opening (74) is a circular through hole, and the opening diameter is 2-10 cm.

7. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The structure composed of the mixing cylinder (73) and the flow guide opening (74) is uniformly and centrally symmetrically distributed in four groups about the axis of the cylinder (10).

8. The hydrogen chloride catalytic oxidation high-efficiency heat transfer reactor according to claim 1, characterized in that: The mixing cylinder (73) is divided into four regions along the height, the height of each region is 0.5-2 m, the opening rate of the highest region is 40%-50%, and the opening rate of each region decreases by 3%-5% from top to bottom.

Images