Sleeve tubular reactor, system and method for preparing chlorine by oxidizing hydrogen chloride

Abstract

The invention discloses a casing tubular reactor for preparing chlorine by oxidizing hydrogen chloride, which comprises a main body, and a lower seal head and an upper seal head which are respectively arranged at the bottom end and the top end of the main body, a casing reaction tube is arranged in the main body, and the casing reaction tube comprises a central tube and a jacket which is arranged on the outer wall of the central tube in a surrounding manner. A heating medium flows through the central pipe and the jacket, so that the heat exchange area is increased, and the heating medium is timely moved away from the reactor to take away heat generated by heat release of oxidation reaction, so that excessive concentration of bed reaction heat is avoided; and the obvious defect of traditional reaction equipment in the aspect of heat removal is overcome, the problems that the reaction efficiency is limited and the energy consumption is high are solved, and the reaction efficiency can be greatly improved. The invention also provides a system and a method for preparing chlorine by oxidizing hydrogen chloride, which realize recycling of reaction heat, reduction of energy consumption, recycling of tail gas discharged from an absorption tower after treatment, improvement of the utilization rate of raw materials, closed-loop operation of chlorine elements and reduction of the production cost.

Description

Technical Field

[0001] The invention belongs to the technical field of chlorine preparation, and particularly relates to a shell-and-tube reactor, a system and a method for preparing chlorine by hydrogenating chloride and hydrogenating hydrogen. Background Art

[0002] Hydrogen chloride is widely produced in chlorine chemical production processes, such as the synthesis of vinyl chloride and methane chloride. Direct discharge of this hydrogen chloride wastes resources and pollutes the environment. The oxidation of hydrogen chloride to produce chlorine gas, enabling the recycling of chlorine, is of great significance to the green and sustainable development of the chlorine chemical industry.

[0003] Currently, common hydrogen chloride oxidation processes for chlorine production, such as the Deacon process, face difficulties removing the heat of reaction. The reaction releases a significant amount of heat, and if not removed promptly and effectively, it can make it difficult to control the reaction temperature. Localized overheating not only reduces catalyst activity and service life but also increases side reactions, reducing chlorine selectivity and yield.

[0004] Traditional fixed-bed reactors have low heat transfer efficiency and limited heat removal capacity. Shell-and-tube reactors, while offering some improvement, still cannot meet the demand for efficient heat removal when the reaction heat intensity is high. This limits the expansion of reaction scale and the improvement of production efficiency, and increases production costs.

[0005] The development of the chlorine industry is placing higher demands on the efficiency and economic viability of the hydrogen chloride oxidation process for chlorine production. Developing efficient heat transfer reaction equipment and processes, precisely controlling reaction temperatures, improving reaction efficiency and chlorine yield, and reducing energy consumption and costs have become key challenges facing the industry. Summary of the Invention

[0006] In view of the defects in heat removal in traditional reaction equipment during the oxidation of hydrogen chloride to produce chlorine in the prior art, the present invention provides a shell-and-tube reactor, system and method for hydrogen chloride oxidation to produce chlorine, which can effectively remove the heat generated by the reaction in a timely manner and improve the reaction efficiency.

[0007] A shell-and-tube reactor for producing chlorine by oxidation of hydrogen chloride comprises a main body and a lower head and an upper head respectively arranged at the bottom and top ends of the main body. A shell-and-tube reaction tube is arranged in the main body, the shell-and-tube reaction tube comprising a central tube and a jacket arranged around the outer wall of the central tube, and a product drainage tube is arranged at the bottom end of the jacket. A first upper cover plate is provided along the inner wall of the main body between the central tube and the upper cover, a lower cover plate is provided between the central tube and the lower head, and the product drainage pipe passes through the lower cover plate; A second upper cover plate and an upper blind plate are sequentially arranged along the inner wall of the main body and below the first upper cover plate, and the central tube and the jacket pass through the second upper cover plate and the upper blind plate respectively; A catalyst bed is provided in the jacket, and the catalyst bed is located below the upper blind plate; On the side wall of the main body, a raw mixed gas inlet is provided between the second upper cover plate and the upper blind plate, a first heating medium inlet is provided between the jacket and the lower cover plate, a first heating medium outlet is provided between the first upper cover plate and the second upper cover plate, and a second heating medium outlet is provided below the upper blind plate and above the catalyst bed; A product outlet is provided at the bottom of the lower head.

[0008] Preferably, a plurality of the jacketed reaction tubes are provided.

[0009] Preferably, a distributor is provided at the top end of the jacket.

[0010] Preferably, the upper blind plate is connected to the jacket and the inner wall of the main body by welding; the second upper cover plate is connected to the central tube and the inner wall of the main body by threaded sleeves.

[0011] Preferably, the jacketed reaction tube has a height of 3-10 m and an outer diameter of 30-100 mm, a ratio of the thickness of the jacket to the outer diameter of the central tube is 0.3-0.9, and a ratio of the outer diameter of the product drainage tube to the thickness of the jacket is 0.1-0.5.

[0012] Preferably, the porosity of the distributor is 5-30%; the bottom of the product drainage tube is provided with holes, and the porosity of the bottom of the product drainage tube is 5-20%.

[0013] The material of the shell-and-tube reactor only needs to meet the reaction requirements; preferably, the material of the shell-and-tube reactor is pure nickel, nickel alloy, quartz or ceramic.

[0014] A system for preparing chlorine by oxidizing hydrogen chloride comprises the aforementioned tubular shell and tube reactor, wherein the product outlet of the tubular shell and tube reactor is connected to a heat exchanger, the heat exchanger is further connected to a preheater, a raw material mixing pipeline, and a condenser, respectively, and the condenser is sequentially connected to a gas-liquid separator, an absorption tower, a desorption tower, and a distillation tower; the preheater is further connected to an inlet for the raw material mixed gas, and is further provided with a second heating medium inlet and a third heating medium outlet, the second heating medium inlet is connected to the first and second heating medium outlets, the third heating medium outlet is connected to the first heating medium inlet, and the second heating medium inlet is provided with a flow regulating valve; and an absorbent inlet is provided at the top of the absorption tower.

[0015] Preferably, the heat exchanger is a tube bundle heat exchanger or a plate heat exchanger.

[0016] Preferably, the condenser is a shell and tube condenser.

[0017] Preferably, the circulating heating medium is thermal oil or molten salt.

[0018] A method for preparing chlorine by oxidation of hydrogen chloride, using the above system, comprises the following steps: (1) Preheating the catalyst bed: loading the catalyst into the jacket to form a catalyst bed, and circulating heating medium entering from the first heating medium inlet to preheat the catalyst bed; (2) Oxidation reaction: When the temperature of the catalyst bed is preheated to 200-300°C, oxygen and hydrogen chloride gas are mixed and introduced into the raw material mixing pipeline. After being preheated once in the heat exchanger, the gas enters the preheater for secondary preheating. The gas then enters the raw material mixed gas inlet, is dispersed by the homogenizer, and enters the jacket. The temperature of the catalyst bed is adjusted to the reaction temperature for oxidation reaction. The product flows out through the product drainage pipe and is then discharged from the product outlet. The reaction temperature is 50-150°C higher than the preheating temperature of the catalyst bed. (3) Heat recovery and utilization: The product discharged from the product outlet enters the heat exchanger for heat exchange; the circulating heating medium flows out from the first heating medium outlet and the second heating medium outlet, enters the second heating medium inlet, and after completing the heat exchange in the preheater, flows out through the third heating medium outlet to the first heating medium inlet; (IV) Product separation: After the heat exchange is completed in the heat exchanger, the product enters the condenser for condensation and is then separated by the gas-liquid separator. The separated gas is discharged from the top of the gas-liquid separator and enters the bottom of the absorption tower. The absorption tower adopts countercurrent operation. The unabsorbed tail gas is discharged from the top of the absorption tower, and the absorbent that absorbs chlorine is discharged from the bottom of the absorption tower to the desorption tower for desorption. The desorbed chlorine is sent to the distillation tower for distillation and discharged from the top of the distillation tower.

[0019] Preferably, the mass space velocity of hydrogen chloride is 0.2-3h -1 , the molar ratio of oxygen to hydrogen chloride is 1:4-3:1.

[0020] Preferably, the temperature of the absorption tower is 30-50°C and the pressure is 0.5-0.8 MPa; the temperature of the desorption tower is 80-100°C and the pressure is 0.1-0.3 MPa; the temperature of the distillation tower is 120-130°C and the reflux ratio is 3-5.

[0021] Preferably, the absorbent is a mixture of an organic amine and an ionic liquid in a mass ratio of (0.2-1):1. More preferably, the organic amine is one of monoethanolamine, diethanolamine, N-methyldiethanolamine, and diisopropanolamine, and the ionic liquid is one of 1-butyl-4-methyl-imidazolium sodium tetrafluoroborate, 1-ethyl-3-methylimidazolium acetate, 1-butylpyridinium tetrafluoroborate, tetrabutylammonium chloride, and alanine ionic liquid.

[0022] The catalyst of the present invention is a conventional catalyst in the prior art that can generate chlorine and water through oxidation reaction of hydrogen chloride gas and oxygen.

[0023] Preferably, the catalyst is a composite metal oxide, and the main components of the catalyst include metal oxides of copper, chromium, titanium, aluminum or cerium containing RuO2.

[0024] Preferably, the catalyst comprises a copper compound and / or a ruthenium compound, preferably a copper compound and / or a ruthenium compound supported on a carrier such as alumina or titanium dioxide, for example, alumina supported on copper chloride or ruthenium chloride, preferably a ruthenium compound.

[0025] More preferably, the catalyst of the present invention further contains other promoters, such as compounds of metals such as gold, palladium, platinum, rhodium, iridium, nickel or chromium, alkali metals, alkaline earth metals and rare earth metals.

[0026] Preferably, suitable catalysts may have different shapes, such as rings, cylinders or spheres, etc., preferably suitable catalysts have similar external dimensions.

[0027] Advantages of the present invention: (1) In the shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride provided by the present invention, the heating medium flows through the central tube and the jacket, thereby increasing the heat exchange area. The heating medium is removed from the reactor in a timely manner, taking away the heat generated by the oxidation reaction, without causing excessive concentration of the bed reaction heat. The reactor solves the significant defects of traditional reaction equipment in heat removal, overcomes the problems of limited reaction efficiency and high energy consumption, and can greatly improve the reaction efficiency.

[0028] (2) In the described shell-and-tube reactor, by controlling the height, outer diameter, ratio of jacket thickness to outer diameter of the central tube, opening ratio of the distributor and product drainage tube and other parameters of the shell-and-tube reactor, the reaction is facilitated to proceed stably and the reaction process is precisely controlled; (3) The system and method for preparing chlorine by oxidation of hydrogen chloride realizes the recovery and utilization of reaction heat, reduces energy consumption, and the tail gas discharged from the absorption tower is recycled after treatment, thereby improving the utilization rate of raw materials, and the closed-loop operation of the chlorine element reduces production costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 This is a schematic structural diagram of the shell-and-tube reactor for producing chlorine by oxidation of hydrogen chloride according to the present invention; Figure 2 This is a schematic diagram of the system structure for preparing chlorine by oxidation of hydrogen chloride according to the present invention; Among them, 1-main body, 2-raw material mixed gas inlet, 3-product outlet, 4-first heating medium inlet, 5-second heating medium outlet, 6-first heating medium outlet, 7-upper head, 8-lower head, 9-upper blind plate, 10-second upper cover plate, 11-first upper cover plate, 12-lower cover plate, 13-center tube, 14-jacket, 15-drainage pipe, 16-distributor; 21-heat exchanger, 22-preheater, 23-condenser, 24-gas-liquid separator, 25-absorption tower, 26-desorption tower, 27-distillation tower. DETAILED DESCRIPTION

[0030] Example 1 A shell-and-tube reactor for producing chlorine by oxidation of hydrogen chloride comprises a main body 1 and a lower head 8 and an upper head 7 respectively arranged at the bottom and top ends of the main body 1. A shell-and-tube reaction tube is arranged within the main body 1. The shell-and-tube reaction tube comprises a central tube 13 and a jacket 14 arranged around the outer wall of the central tube 13. A product drainage tube 15 is provided at the bottom end of the jacket 14. A first upper cover plate 11 is provided along the inner wall of the main body 1 between the central tube 13 and the upper cover, a lower cover plate 12 is provided between the central tube 13 and the lower head 8, and the product drainage pipe 15 passes through the lower cover plate 12; A second upper cover plate 10 and an upper blind plate 9 are sequentially arranged along the inner wall of the main body 1 and below the first upper cover plate 11, and the central tube 13 and the jacket 14 pass through the second upper cover plate 10 and the upper blind plate 9 respectively; A catalyst bed is provided in the jacket 14 and is located below the upper blind plate 9; On the side wall of the main body 1, a raw mixed gas inlet 2 is provided between the second upper cover plate 10 and the upper blind plate 9, a first heating medium inlet 4 is provided between the jacket 14 and the lower cover plate 12, a first heating medium outlet 6 is provided between the first upper cover plate 11 and the second upper cover plate 10, and a second heating medium outlet 5 is provided below the upper blind plate 9 and above the catalyst bed. A product outlet 3 is provided at the bottom of the lower head 8 .

[0031] The circulating heating medium enters the reactor through the first heating medium inlet 4 to preheat the catalyst bed. When the preheating temperature reaches 200-300°C, the preheated O2 and HCl enter the reactor through the raw mixed gas inlet 2. After being evenly dispersed by the homogenizer 16, they enter the catalyst bed in the jacket 14 for oxidation reaction. The product is discharged from the jacket 14 through the drainage pipe 15 and finally discharged from the product outlet 3. Because this reaction is exothermic, the circulating heating medium is discharged from the first heating medium outlet 6 and the second heating medium outlet 5 to remove heat in a timely manner. The heating medium flows through the central tube 13 and the jacket 14, increasing the heat exchange area and preventing excessive concentration of reaction heat in the bed.

[0032] Example 2 Based on the above embodiment 1, a plurality of the double-tube reaction tubes are provided. More preferably, two double-tube reaction tubes are provided.

[0033] A distributor 16 is provided at the top of the jacket 14 .

[0034] The upper blind plate 9 is connected to the jacket 14 and the inner wall of the main body 1 by welding; the second upper cover plate 10 is connected to the central tube 13 and the inner wall of the main body 1 by threaded sleeves.

[0035] The jacketed reaction tube has a height of 3-10m and an outer diameter of 30-100mm. The ratio of the thickness of the jacket 14 to the outer diameter of the central tube 13 is 0.3-0.9. The ratio of the outer diameter of the product drainage tube 15 to the thickness of the jacket 14 is 0.1-0.5.

[0036] The porosity of the distributor 16 is 5-30%. The bottom of the product drainage pipe 15 is provided with holes, and the porosity of the bottom of the product drainage pipe 15 is 5-20%.

[0037] The material of the shell-and-tube reactor only needs to meet the reaction requirements; preferably, the material of the shell-and-tube reactor is pure nickel, nickel alloy, quartz or ceramic.

[0038] Example 3 A system for preparing chlorine by hydrogen chloride oxidation comprises the aforementioned tubular shell and tube reactor, wherein the product outlet 3 of the tubular shell and tube reactor is connected to a heat exchanger 21, the heat exchanger 21 is further connected to a preheater 22, a raw material mixing pipeline, and a condenser 23, respectively, and the condenser 23 is sequentially connected to a gas-liquid separator 24, an absorption tower 25, a desorption tower 26, and a distillation tower 27; the preheater 22 is further connected to a raw material mixed gas inlet 2, and is further provided with a second heating medium inlet and a third heating medium outlet, the second heating medium inlet is connected to a first heating medium outlet 6 and a second heating medium outlet 5, the third heating medium outlet is connected to the first heating medium inlet 4, and the second heating medium inlet is provided with a flow regulating valve; and an absorbent inlet is provided at the top of the absorption tower 25.

[0039] The heat exchanger is a tube bundle heat exchanger or a plate heat exchanger.

[0040] The condenser 23 is a shell and tube condenser.

[0041] The circulating heating medium is thermal oil or molten salt.

[0042] Example 4 A method for preparing chlorine by oxidation of hydrogen chloride, using the system of Example 3 above, comprises the following steps: (1) Preheating the catalyst bed: The catalyst is loaded into the jacket 14 to form a catalyst bed, and a circulating heating medium enters from the first heating medium inlet 4 to preheat the catalyst bed; (II) Oxidation reaction: When the temperature of the catalyst bed is preheated to 200-300°C, oxygen and hydrogen chloride gas are mixed and introduced into the raw material mixing pipeline. After being preheated once in the heat exchanger 21, the gas enters the preheater 22 for secondary preheating. The gas then enters the raw material mixed gas inlet 2, is dispersed by the uniform distributor 16, and enters the jacket 14. The temperature of the catalyst bed is adjusted to the reaction temperature for oxidation reaction. The product flows out through the product drainage pipe 15 and is discharged from the product outlet 3. The reaction temperature is 50-150°C higher than the preheating temperature of the catalyst bed. (III) Heat recovery: The product discharged from the product outlet 3 enters the heat exchanger 21 for heat exchange, and the heat of the product can be used to preheat the raw materials. Since the reaction is an exothermic reaction, the circulating heating medium absorbs a large amount of reaction heat, flows out from the first heating medium outlet 6 and the second heating medium outlet 5, and enters the preheater 22 through the second heating medium inlet. In the preheater 22, the mixed raw materials are further preheated. After the heat exchange is completed, the temperature of the circulating heating medium decreases, and then flows out through the third heating medium outlet to the first heating medium inlet 4, realizing the recovery of reaction heat. According to the bed temperature, the amount of the circulating heating medium is adjusted in time to ensure the reaction temperature of the bed. (IV) Product separation: After the heat exchange in the heat exchanger 21 is completed, the product enters the condenser 23 for condensation, and the water vapor is condensed into liquid water. The condensed gas-liquid mixture is separated by the gas-liquid separator 24. The water and gas are quickly separated by the centrifugal force and gravity sedimentation principle. The water is discharged from the bottom of the gas-liquid separator 24, and the separated gas is discharged from the top of the gas-liquid separator 24 and enters the bottom of the absorption tower 25. The absorbent is sprayed down from the top of the tower. The absorption tower 25 adopts countercurrent operation. The unabsorbed tail gas (O2 and HCl) is discharged from the top of the absorption tower 25 and can be recycled after treatment; the absorbent that absorbs chlorine is discharged from the bottom of the absorption tower 25 to the desorption tower 26 for desorption. The desorbed chlorine is sent to the distillation tower 27 for distillation and discharged from the top of the distillation tower 27 to obtain chlorine with a purity higher than 99.8wt%.

[0043] The mass space velocity of hydrogen chloride is 0.2-3h -1 , the molar ratio of oxygen to hydrogen chloride is 1:4-3:1.

[0044] The absorption tower 25 has a temperature of 30-50°C and a pressure of 0.5-0.8 MPa; the desorption tower 26 has a temperature of 80-100°C and a pressure of 0.1-0.3 MPa; the distillation tower 27 has a temperature of 120-130°C and a reflux ratio of 3-5.

[0045] The absorbent is a mixture of an organic amine and an ionic liquid. More preferably, the organic amine is one of monoethanolamine, diethanolamine, N-methyldiethanolamine, and diisopropanolamine, and the ionic liquid is one of 1-butyl-4-methyl-imidazolium sodium tetrafluoroborate, 1-ethyl-3-methylimidazolium acetate, 1-butylpyridinium tetrafluoroborate, tetrabutylammonium chloride, and alanine ionic liquid.

[0046] The catalyst of the present invention is a conventional catalyst in the prior art that can generate chlorine and water through oxidation reaction of hydrogen chloride gas and oxygen.

[0047] Example 5 Based on the above Example 4, 30 jacketed reaction tubes were provided, each having a height of 5 m and an outer diameter of 60 mm. The ratio of the thickness of the jacket 14 to the outer diameter of the central tube 13 was 0.5, and the ratio of the outer diameter of the product drainage tube 15 to the thickness of the jacket 14 was 0.2. The porosity of the distributor 16 is 20%; the bottom of the product drainage pipe 15 is provided with holes, and the porosity of the bottom of the product drainage pipe 15 is 20%; The material of the shell-and-tube reactor is pure nickel; The heat exchanger is a tube bundle heat exchanger; The circulating heating medium is thermal oil.

[0048] A method for preparing chlorine by oxidation of hydrogen chloride comprises the following steps: (1) Preheating the catalyst bed: Japan Sumitomo SR155 3% ruthenium aluminum titanium catalyst is loaded into the jacket 14 to form a catalyst bed with a catalyst bed height of 4.5 m. Thermal oil heating medium enters from the first heating medium inlet 4 to preheat the catalyst bed; (II) Oxidation reaction: When the temperature of the catalyst bed is preheated to 250°C, oxygen and hydrogen chloride gas are mixed and enter the raw material mixing pipeline. After being preheated once in the heat exchanger 21, they enter the preheater 22 for secondary preheating. Then, they enter the raw material mixed gas inlet 2, are dispersed by the uniform distributor 16, and enter the catalyst bed in the jacket 14. The temperature of the catalyst bed is adjusted to the reaction temperature of 300°C. The oxidation reaction is carried out, and the product flows out through the product drainage pipe 15 and is then discharged from the product outlet 3. The mass space velocity of hydrogen chloride is 0.8h -1 , the molar ratio of oxygen to hydrogen chloride is 1:2; the conversion rate of hydrogen chloride in the oxidation reaction is greater than 93%; (III) Heat recovery: The product discharged from the product outlet 3 enters the heat exchanger 21 for heat exchange and preheating the raw materials. Since the reaction is exothermic, the circulating heat transfer oil absorbs a large amount of reaction heat and flows out from the first heating medium outlet 6 and the second heating medium outlet 5 through the second heating medium inlet to the preheater 22. The raw materials are further preheated in the preheater 22. After the heat exchange is completed, the temperature of the circulating heat transfer oil medium decreases and then flows out through the third heating medium outlet to the first heating medium inlet 4, realizing the recovery of reaction heat. According to the bed temperature, the amount of the circulating heating medium is adjusted in time to ensure the reaction temperature of the bed. (IV) Product separation: After the heat exchange in the heat exchanger 21 is completed, the product enters the condenser 23 for condensation, and the water vapor is condensed into liquid water. The condensed gas-liquid mixture is separated by the gas-liquid separator 24. The water and gas are quickly separated by the centrifugal force and gravity sedimentation principle. The water is discharged from the bottom of the gas-liquid separator 24, and the separated gas is discharged from the top of the gas-liquid separator 24 and enters the bottom of the absorption tower 25. The absorbent is a mixed solution of diethanolamine and 1-butyl-4-methyl-imidazolium tetrafluoroborate with a mass ratio of 0.5:1. The absorbent is sprayed down from the top of the tower. The absorption tower 25 adopts Using countercurrent operation, the unabsorbed tail gas (O2 and HCl) is discharged from the top of the absorption tower 25 and can be recycled after treatment. The temperature of the absorption tower 25 is 40°C and the pressure is 0.6 MPa. The absorbent that has absorbed chlorine is discharged from the bottom of the absorption tower 25 to the desorption tower 26 for desorption. The temperature of the desorption tower 26 is 90°C and the pressure is 0.3 MPa. The desorbed chlorine is sent to the distillation tower 27 for distillation. The temperature of the distillation tower 27 is 120°C and the reflux ratio is 4. It is then discharged from the top of the distillation tower 27 to obtain chlorine with a purity higher than 99.8wt%.

Claims

1. A shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride, comprising a main body (1) and a lower head (8) and an upper head (7) respectively arranged at the bottom and top ends of the main body (1), characterized in that: A jacketed reaction tube is provided in the main body (1), the jacketed reaction tube comprising a central tube (13) and a jacket (14) surrounding the outer wall of the central tube (13), and a product drainage tube (15) is provided at the bottom end of the jacket (14); A first upper cover plate (11) is provided along the inner wall of the main body (1) and between the central tube (13) and the upper cover, a lower cover plate (12) is provided between the central tube (13) and the lower head (8), and the product drainage pipe (15) passes through the lower cover plate (12); A second upper cover plate (10) and an upper blind plate (9) are sequentially arranged along the inner wall of the main body (1) and below the first upper cover plate (11), and the central tube (13) and the jacket (14) respectively penetrate the second upper cover plate (10) and the upper blind plate (9); A catalyst bed is provided in the jacket (14), and the catalyst bed is located below the upper blind plate (9); On the side wall of the main body (1), a raw material mixed gas inlet (2) is provided between the second upper cover plate (10) and the upper blind plate (9), a first heating medium inlet (4) is provided between the jacket (14) and the lower cover plate (12), a first heating medium outlet (6) is provided between the first upper cover plate (11) and the second upper cover plate (10), and a second heating medium outlet (5) is provided below the upper blind plate (9) and above the catalyst bed. A product outlet (3) is provided at the bottom of the lower head (8).

2. The shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride according to claim 1, characterized in that: There are multiple jacketed reaction tubes.

3. The shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride according to claim 1 or 2, characterized in that: A distributor (16) is provided at the top end of the jacket (14).

4. The shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride according to claim 1 or 2, characterized in that: The upper blind plate (9) is connected to the jacket (14) and the inner wall of the main body (1) by welding; the second upper cover plate (10) is connected to the central tube (13) and the inner wall of the main body (1) by threaded sleeves.

5. The shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride according to claim 1 or 2, characterized in that: The height of the jacketed reaction tube is 3-10m and the outer diameter is 30-100mm. The ratio of the thickness of the jacket (14) to the outer diameter of the central tube (13) is 0.3-0.

9. The ratio of the outer diameter of the product drainage tube (15) to the thickness of the jacket (14) is 0.1-0.

5.

6. The shell-and-tube reactor for preparing chlorine by oxidation of hydrogen chloride according to claim 1 or 2, characterized in that: The porosity of the distributor (16) is 5-30%; the bottom of the product drainage pipe (15) is provided with holes, and the porosity of the bottom of the product drainage pipe (15) is 5-20%.

7. A system for preparing chlorine by oxidation of hydrogen chloride, characterized in that: The invention comprises a shell-and-tube reactor as claimed in claim 1 or 2, wherein the product outlet (3) of the shell-and-tube reactor is connected to a heat exchanger (21), and the heat exchanger (21) is further connected to a preheater (22), a raw material mixing pipeline, and a condenser (23), and the condenser (23) is sequentially connected to a gas-liquid separator (24), an absorption tower (25), a desorption tower (26), and a distillation tower (27); the preheater (22) is further connected to a raw material mixed gas inlet (2), and a second heating medium inlet and a third heating medium outlet are further provided on the preheater (22), the second heating medium inlet is connected to the first heating medium outlet (6) and the second heating medium outlet (5), the third heating medium outlet is connected to the first heating medium inlet (4), and a flow regulating valve is provided on the second heating medium inlet; and an absorbent inlet is provided at the top of the absorption tower (25).

8. A method for preparing chlorine by oxidation of hydrogen chloride, characterized in that: The method of claim 7 comprises the following steps: (1) Preheating the catalyst bed: The catalyst is loaded into the jacket (14) to form a catalyst bed, and a circulating heating medium enters from the first heating medium inlet (4) to preheat the catalyst bed; (ii) Oxidation reaction: When the temperature of the catalyst bed is preheated to 200-300°C, oxygen and hydrogen chloride gas are mixed and introduced into the raw material mixing pipeline, preheated once in the heat exchanger (21), and then preheated twice in the preheater (22), and then introduced into the raw material mixed gas inlet (2), dispersed by the uniform distributor (16), and then introduced into the jacket (14), and the temperature of the catalyst bed is adjusted to the reaction temperature for oxidation reaction, and the product flows out through the product drainage pipe (15) and is then discharged from the product outlet (3); wherein, the reaction temperature is 50-150°C higher than the preheating temperature of the catalyst bed; (3) Heat recovery and utilization: the product discharged from the product outlet (3) enters the heat exchanger (21) for heat exchange; the circulating heating medium flows out from the first heating medium outlet (6) and the second heating medium outlet (5) and enters the preheater (22) through the second heating medium inlet, completes the heat exchange in the preheater (22), and then flows out through the third heating medium outlet to the first heating medium inlet (4); (IV) Product separation: After the heat exchange is completed in the heat exchanger (21), the product enters the condenser (23) for condensation and is then separated by the gas-liquid separator (24). The separated gas is discharged from the top of the gas-liquid separator (24) and enters the bottom of the absorption tower (25). The absorption tower (25) adopts a countercurrent operation. The unabsorbed tail gas is discharged from the top of the absorption tower (25). The absorbent that has absorbed chlorine is discharged from the bottom of the absorption tower (25) to the desorption tower (26) for desorption. The desorbed chlorine is sent to the distillation tower (27) for distillation and is discharged from the top of the distillation tower (27).

9. The method for preparing chlorine by oxidation of hydrogen chloride according to claim 8, characterized in that: The mass space velocity of hydrogen chloride is 0.2-3h -1 , the molar ratio of oxygen to hydrogen chloride is 1:4-3:

1.

10. The method for preparing chlorine by oxidation of hydrogen chloride according to claim 9, characterized in that: The temperature of the absorption tower (25) is 30-50°C and the pressure is 0.5-0.8 MPa; the temperature of the desorption tower (26) is 80-100°C and the pressure is 0.1-0.3 MPa; the temperature of the distillation tower (27) is 120-130°C and the reflux ratio is 3-5.

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